УЛУЧШЕННАЯ КОНСТРУКЦИЯ РЕАКТОРА ОЛИГОМЕРИЗАЦИИ/ТРИМЕРИЗАЦИИ/ТЕТРАМЕРИЗАЦИИ ЭТИЛЕНА

Изобретение касается способа олигомеризации олефинового мономера, включающего периодическое или непрерывное введение олефинового мономера, и периодическое или непрерывное введение каталитической системы или компонентов каталитической системы в реакционную смесь реакционной системы; олигомеризацию олефинового мономера в реакционной смеси с образованием олигомерного продукта; и периодический или непрерывный вывод выходящего потока реакционной системы, содержащего олигомерный продукт, из реакционной системы, причем реакционная система содержит общий объем реакционной смеси реакционной системы; и теплообменный участок реакционной системы, содержащий объем теплообменной реакционной смеси и общую площадь поверхности теплообмена, обеспечивающую непрямой термоконтакт между реакционной смесью и теплоносителем; при этом соотношение общей площади теплообменной поверхности к общему объему реакционной смеси реакционной системы находится в диапазоне от 1,25 дюйм-1до 5 дюйм-1; и при том что скорость вывода ...

ТЕПЛООБМЕННЫЙ РЕАКТОР ДЛЯ ПРОИЗВОДСТВА ВОДОРОДА С ПОМОЩЬЮ ВСТРОЕННОГО ПУЧКА ПАРОГЕНЕРАТОРА

Изобретение предназначено для осуществления реакций парового риформинга и может быть использовано в химической промышленности. Теплообменный реактор содержит множество байонетных труб (4), подвешенных к верхнему своду (2), простирающихся до уровня нижнего дна (3) и заключенных в кожух (1), содержащий впускной (Е) и выпускной (S) патрубки для дымовых газов. Теплообменный реактор содержит пучок труб парогенератора, образованный множеством вертикальных труб (5), подвешенных к верхнему своду (2) и заключенных в периферийное пространство между внутренней перегородкой (Bi) и вертикальной стенкой кожуха (1). Внутренняя перегородка (Bi) содержит отверстие (Oi) для прохода дымовых газов из середины реактора к периферийному пространству. Вертикальные трубы (5) питаются водой из нижнего распределителя (9). Пароводяная смесь, выходящая из вертикальных труб (5), собирается в верхнем коллекторе (7), расположенном над верхним сводом (2). Нижняя линия (14) связывает жидкую фазу сепараторного резервуара ...

УСТАНОВКА ДЛЯ ПОЛУЧЕНИЯ (МЕТ)АКРИЛОВОЙ КИСЛОТЫ И СПОСОБ ПОЛУЧЕНИЯ (МЕТ)АКРИЛОВОЙ КИСЛОТЫ

Изобретение относится к установке для получения (мет)акриловой кислоты, которая включает в себя: реактор для получения (мет)акриловой кислоты посредством реакции газофазного каталитического окисления одного, двух или большего количества исходных соединений, включающих пропан, пропилен, изобутилен и (мет)акролеин, в газовой смеси исходных веществ, содержащей одно, два или большее количество исходных соединений, включающих пропан, пропилен, изобутилен и (мет)акролеин, и кислорода; соединенный с реактором теплообменник, предназначенный для охлаждения реакционной газовой смеси, содержащей полученную (мет)акриловую кислоту; и соединенную с теплообменником абсорбционную башню, предназначенную для контактирования поглощающей жидкости, с целью абсорбции (мет)акриловой кислоты, и реакционной газовой смеси таким образом, что (мет)акриловая кислота из реакционной газовой смеси абсорбируется поглощающей жидкостью, при этом установка дополнительно содержит: обводную трубу, предназначенную для соединения ...

ЦИРКУЛЯЦИОННЫЙ РЕАКТОР С ПЕРЕМЕННЫМ ДИАМЕТРОМ ДЛЯ ПОЛИМЕРИЗАЦИИ ОЛЕФИНОВ

Изобретение относится к способу полимеризации этилена, в частности к способу полимеризации этилена в циркуляционном реакторе. Полимеризацию проводят при температуре от 20 до 150°С, но ниже точки плавления получаемого полимера и давлении от 5 до 100 бар. Полимер присутствует в суспензии в жидкой или суперкритической суспензионной среде. Суспензия циркулирует посредством аксиального насоса. Циркуляционный реактор имеет диаметр, который варьируется на 10%. Также реактор имеет одно расширение и сужение в области, отличной от области аксиального насоса. Способ позволяет получать продукт реакции с высоким выходом в единицу времени. 6 з.п. ф-лы, 3 табл.

КОЖУХОТРУБНЫЕ РЕАКТОРЫ С ЖИДКОСТНЫМ ОХЛАЖДЕНИЕМ ПОД ДАВЛЕНИЕМ

Изобретение относится к комплекту предварительно изготовленных узлов кожухотрубного реактора, выполненных с возможностью сборки на строительной площадке с образованием кожухотрубного реактора для проведения каталитических реакций в газовой и/или жидкой фазе. Реактор содержит пучок вертикальных, заполненных катализатором реакторных труб, концы которых герметично закреплены в верхней и нижней трубных решетках. Трубы окружены корпусом реактора, который герметично соединен с трубными решетками. Корпус реактора вместе с трубными решетками образует емкость под давлением, в которой жидкий теплоноситель омывает под давлением реакторные трубы. Трубные решетки перекрыты крышками реактора, которые соединены с корпусом реактора и с которыми сообщаются реакторные трубы. В реакторе имеются подводящие трубы для подачи теплоносителя, омывающего под давлением реакторные трубы, и отводящие трубы для отвода теплоносителя, омывающего под давлением реакторные трубы. Подводящие и/или отводящие трубы проходят ...

СИСТЕМА И СПОСОБ ДЛЯ ОБРАБОТКИ ТВЕРДЫХ МАТЕРИАЛОВ С ИСПОЛЬЗОВАНИЕМ УДАРНЫХ ВОЛН, СОЗДАВАЕМЫХ В СВЕРХЗВУКОВОМ ГАЗОВОМ ВИХРЕ

Группа изобретений относится к системам и способам обработки твердых материалов посредством ударных волн, создаваемых в сверхзвуковом газовом вихре. Система содержит устройство подачи твердого материала, реактор с камерой, входом для твердого материала, входом для газа от источника газа и выходом и накопитель. Реактор выполнен с возможностью проведения химических реакций и измельчения твердого загружаемого материала посредством ударных волн в камере. При этом выход включает в себя трубку Вентури для повышения давления в камере и осуществления быстрого охлаждения обработанного твердого материала, выходящего из реактора. Накопитель выполнен с возможностью сбора обработанного материала, переданного через выход реактора. Вход для газа содержит впускное сопло, выполненное с возможностью ускорения потока газа до сверхзвуковой скорости и испускания ударных волн из впускного сопла в камеру, при этом впускное сопло дополнительно выполнено с возможностью управления ударными волнами, вводимыми в камеру ...

КОНВЕРТЕРНАЯ СИСТЕМА С МАКСИМАЛЬНОЙ СКОРОСТЬЮ РЕАКЦИИ ДЛЯ ЭКЗОТЕРМИЧЕСКИХ РЕАКЦИЙ

Способ конверсии для синтеза аммиака включает: введение газообразного, обогащенного реагентами потока, содержащего смесь водорода и азота, при температуре подачи в теплообменный канал теплообменной реакционной зоны для подогрева обогащенного реагентами потока до температуры на входе, где теплообменная реакционная зона содержит кожухотрубный теплообменник, теплообменный канал представляет собой межтрубный канал через теплообменник, и реакционный канал содержит множество трубок, содержащих в себе катализатор, введение предварительно подогретого обогащенного реагентами потока при температуре на входе в противоточный, содержащий катализатор реакционный канал для экзотермической конверсии газа-реагента в получаемый газ с образованием обогащенной продуктом смеси из газа-реагента и получаемых газов, где реакционный канал содержит множество последовательных чередующихся, содержащих катализатор зон и зон, ограничивающих реакцию, косвенную передачу тепла от реакционного канала к теплообменному каналу ...

РЕАКЦИОННАЯ ЕМКОСТЬ

Изобретение относится к реакционной емкости для стабилизации температуры жидкой смеси веществ. Реакционная емкость (1), предназначенная для температурной стабилизации жидкой смеси веществ (12), включает верхнюю часть (2) емкости и нижнюю часть (15) емкости. Верхняя часть (2) емкости конструктивно выполнена таким образом, чтобы ее габаритные размеры превышали габаритные размеры нижней части (15) емкости. Нижняя часть (15) емкости снабжена погружным насосом (13) и перемешивающим устройством, а также внутренним устройством прямого охлаждения (9), внешним устройством непрямого охлаждения (10) и внутренним устройством прямого нагревания (9) и внешним устройством непрямого нагревания (10), соединенными с системой терморегулирования. Технический результат: поддержание постоянной температуры жидкой смеси веществ в процессе реакции. 3 н. и 5 з.п. ф-лы, 1 ил.

МНОГОРЕАКТОРНАЯ ХИМИЧЕСКАЯ ПРОИЗВОДСТВЕННАЯ СИСТЕМА

Изобретение относится к многореакторной системе и способу для производства продукта, получаемого по ограничиваемой равновесием реакции. Система содержит реакторную емкость, выполненную с возможностью выдерживания рабочих температур и давлений реакции получения продукта, причем реакторная емкость содержит множество реакционных зон, образованных в реакторной емкости с помощью разделительных стенок, емкость сепарации, выполненную с возможностью выдерживания рабочих температур и давлений реакции получения продукта, причем емкость сепарации содержит множество зон сепарации, образованных в емкости сепарации с помощью разделительных стенок, и реакторные комплекты, содержащие множество теплообменников подаваемый поток/отходящий поток. Причем теплообменник первого реакторного комплекта функционально соединен с реакционной зоной подаваемым потоком, а теплообменники остальных реакторных комплектов функционально соединены с реакционной зоной возвращаемым потоком. Изобретение обеспечивает экономику ...

СПОСОБ ВВЕДЕНИЯ В ЭКСПЛУАТАЦИЮ ПАРЦИАЛЬНОГО ГАЗОФАЗНОГО ОКИСЛЕНИЯ АКРОЛЕИНА В АКРИЛОВУЮ КИСЛОТУ ИЛИ МЕТАРОЛЕИНА В МЕТАКРИЛОВУЮ КИСЛОТУ НА ГЕТЕРОГЕННОМ КАТАЛИЗАТОРЕ

... 1. Способ введения в эксплуатацию газофазного парциального окисления на гетерогенном катализаторе акролеина в акриловую кислоту и метакролеина в метакриловую кислоту на фиксированном слое катализатора, который находится в кожухотрубном реакторе в реакционных трубках вертикально расположенного пучка реакционных трубок, заключенного в кожух реактора, когда оба конца каждой из реакционных трубок открыты и каждая реакционная трубка своим верхним концом плотно входит в сквозное отверстие плотно встроенной в верхнюю часть кожуха реактора верхней трубной решетки, а своим нижним концом плотно входит в сквозное отверстие плотно встроенной в нижнюю часть кожуха реактора нижней трубной решетки, при этом внешняя поверхность реакционных трубок, верхняя и нижняя трубная решетки, а также кожух реактора вместе ограничивают пространство, окружающее реакционные трубки, при этом также каждая из двух трубных решеток закрыта крышкой реактора с не менее чем одним отверстием, когда для введения в эксплуатацию ...

СПОСОБ КАТАЛИТИЧЕСКОГО ОКИСЛЕНИЯ В ПАРОВОЙ ФАЗЕ

... 1. Способ каталитического окисления в паровой фазе для получения газообразного реакционного продукта при использовании многотрубного реактора с неподвижным слоем теплообменного типа, образованного множеством реакционных труб и подачей исходного газообразного материала внутрь реакционных труб, набитых катализатором, при котором осуществляют регулирование потерь давления соответствующих реакционных труб таким образом, что потери давления соответствующих реакционных труб после набивки катализатора находятся в пределах ±20% от средней потери давления реакционных труб при набивке инертного вещества во впускную часть исходного газообразного материала реакционных труб или удалении набитого катализатора и повторной набивке катализатора для реакционной трубы, имеющей потерю давления меньше средней потери давления реакционных труб; и удалении набитого катализатора и повторной набивке катализатора для реакционной трубы, имеющей потерю давления больше средней потери давления реакционных труб. 2. Способ ...

НЕПРЕРЫВНЫЙ СПОСОБ КОНВЕРСИИ ЛИГНИНА В СОЕДИНЕНИЯ, ПОДХОДЯЩИЕ ДЛЯ ПРИМЕНЕНИЯ

... 1. Непрерывный способ конверсии лигнинового сырья, содержащего лигнин, причем указанный способ включает:дезоксигенирование лигнина до совокупности продуктов конверсии лигнина в реакторе для конверсии лигнина, содержащем содержимое реактора, содержащее жидкую композицию, содержащую по меньшей мере одно соединение, являющееся жидкостью при 1 бар и 25°C; и при этом одновременное непрерывное выведение по меньшей мере части совокупности продуктов конверсии лигнина из реактора;где конверсию лигнина проводят путем приведения лигнина в контакт с водородом и первым катализатором; иконверсию лигнина проводят при температуре конверсии лигнина и давлении конверсии лигнина, где температура конверсии лигнина находится в интервале выше температуры кипения указанной жидкой композиции при атмосферном давлении и ниже критической температуры жидкой композиции, а давление конверсии лигнина выше давления в пузырьке указанной жидкой композиции при температуре конверсии лигнина, при этом давление конверсии лигнина ...

СИСТЕМЫ И СПОСОБЫ ДЛЯ ОБРАБОТКИ ТВЕРДЫХ МАТЕРИАЛОВ С ИСПОЛЬЗОВАНИЕМ УДАРНЫХ ВОЛН, СОЗДАВАЕМЫХ В СВЕРХЗВУКОВОМ ГАЗОВОМ ВИХРЕ

РЕАКТОРЫ ДЛЯ НЕПРЕРЫВНОЙ ОБРАБОТКИ И СПОСОБЫ ИХ ПРИМЕНЕНИЯ

... 1. Реактор, содержащий:внешний резервуар, имеющий внутреннюю поверхность, напротив которой может находиться обрабатываемая текучая среда;внутренний резервуар, находящийся внутри внешнего резервуара и имеющий внешнюю поверхность, служащую в качестве поверхности теплообмена для обрабатываемой текучей среды; икольцевое пространство, заданное между внешним резервуаром и внутренним резервуаром, для обеспечения прохода, вдоль которого может подаваться обрабатываемая текучая среда, где данное кольцевое пространство разработано так, чтобы поддерживать разность температур между внешним резервуаром и внутренним резервуаром, придавая обрабатываемой текучей среде относительно высокие скорости переноса.2. Реактор по п.1, где внутренняя поверхность внешнего резервуара разработана так, чтобы позволять обрабатываемой текучей среде опускаться в, по существу, равномерную тонкую пленку.3. Реактор по п.2, где данная, по существу, равномерная тонкая пленка позволяет обрабатываемой текучей среде хорошо подходить ...

КОНВЕРТЕРНАЯ СИСТЕМА С МАКСИМАЛЬНОЙ СКОРОСТЬЮ РЕАКЦИИ ДЛЯ ЭКЗОТЕРМИЧЕСКИХ РЕАКЦИЙ

... 1. Способ конверсии для синтеза аммиака, включающий введение газообразного, обогащенного реагентами потока при температуре подачи в теплообменный канал теплообменной реакционной зоны для подогрева обогащенного реагентами потока до температуры на входе, введение предварительно подогретого обогащенного реагентами потока при температуре на входе в противоточный, содержащий катализатор реакционный канал для экзотермической конверсии газа-реагента в получаемый газ с образованием обогащенной продуктом смеси из газа-реагента и получаемого газов, косвенную передачу тепла от реакционного канала к теплообменному каналу со скоростью, эффективной для поддержания температуры смеси газов ниже равновесной температуры, и отвод выходящего потока, обогащенного получаемым газом, от выхода из реакционного канала при температуре выпуска. 2. Способ по п.1, при котором обогащенная продуктом смесь имеет равновесную концентрацию продукта, которая увеличивается с уменьшением температуры, и коэффициент скорости реакции ...

КОМПАКТНЫЙ РЕДУКТОР РЕФОРМИНГА

... 1. Реактор реформинга для превращения исходной жидкости в водород, включающий не менее чем один подающий патрубок, несущий поступающую на превращение исходную жидкость, секцию реформинга, находящуюся в закрытом объеме, секцию кипения и секцию горения, в котором названная секция реформинга содержит одну или несколько заполненных катализатором реформинга катализаторных трубок, названная секция кипения имеет один или несколько сквозных каналов для прохождения газообразных продуктов горения из секции горения, и названная секция горения снабжена не менее чем одной горелкой, при этом теплообменная среда, которая нужна для реформинга названной исходной жидкости в одной или в нескольких катализаторных трубках, представляет собой газожидкостную смесь, которая самопроизвольно циркулирует, находясь в названном закрытом объеме, и при этом по крайней мере часть названного закрытого объема находится внутри названной секции кипения. ! 2. Реактор по п.1, в котором часть названного закрытого объема, внутри ...

СПОСОБ И УСТРОЙСТВО ДЛЯ ПЕРЕРАБОТКИ УГЛЕРОДСОДЕРЖАЩЕГО ИСХОДНОГО МАТЕРИАЛА В ГАЗ ПУТЕМ ГАЗИФИКАЦИИ

... 1. Устройство для газификации с нижней тягой, включающее:продолговатый внешний резервуар,продолговатый внутренний резервуар, где указанный внутренний резервуар расположен внутри указанного внешнего резервуара, в результате чего образуется полость между указанным внутренним резервуаром и указанным внешним резервуаром,загрузочный механизм, включающий продолговатый корпус загрузочного механизма и подающее исходный материал устройство для перемещения указанного исходного материала вдоль указанного продолговатого корпуса загрузочного механизма,корпус газогенератора с внутренней поверхностью и внешней поверхностью,камеру сгорания,газоотвод имеханизм для выгрузки шлака.2. Устройство по п. 1, в котором указанный корпус газогенератора отличается наличием оси и дополнительно включает верхний край, нижний край и множество щелей, расположенных вдоль указанного корпуса газогенератора, где каждая из указанного множества щелей отличается наличием верхнего края щели и нижнего края щели.3. Устройство по ...

РЕАКЦИОННАЯ ЕМКОСТЬ

TPУБЧATЫЙ KATAЛИTИЧECKИЙ PEAKTOP

WIRBELBETTREAKTORSYSTEM UND METHODE ZU DESSEN HERSTELLUNG

Reaktor zur Durchführung rascher stark exothermer Reaktionen und dessen Verwendung

The invention relates to a tube bundle reactor (1) for rapid highly exothermic reactions, consisting of a reactor housing (2) with a bundle (3) of tubes (6) as a reaction zone, said tubes being optionally interconnected radially in relation to their longitudinal extension, eduction pipes (4, 11), a product outlet (12) and a heat exchanger (5). The invention is characterised in that said eduction pipes (4) are configured as pipelines (4a, 4b, 4c, 4d) which are arranged in the tubes (6) of the bundle (3) and which are provided with a plurality of openings (7), said openings (7) in the pipelines (4a, 4b, 4c, 4d) being spread over the entire length of or a section of the length of the reaction zone.

Synthesevorrichtung und Verfahren zur Herstellung eines Produkts

Die Erfindung betrifft eine Synthesevorrichtung, insbesondere einen Ammoniaksynthesekonverter, wobei die Synthesevorrichtung (13) die folgenden Komponenten umfasst: a) einen Druckbehälter (14), welcher einen Einlass (15) und einen Auslass (16) für ein Fluid umfasst; b) mindestens ein Katalysatorbett (9), welches innerhalb des Druckbehälters (14) angeordnet ist; c) mindestens einen Wärmetauscher (7, 8), wobei der Wärmetauscher (7, 8) im Strömungsweg des Fluids zwischen dem Einlass (15) des Druckbehälters (14) und dem Katalysatorbett (9) derart angeordnet ist, dass das in das Katalysatorbett (9) einströmende Fluid durch das aus dem Katalysatorbett (9) ausströmende Fluid erwärmt wird; wobei der Wärmetauscher als Plattenwärmetauscher (7) oder als Spiralwärmetauscher (8) ausgebildet ist.

Tube bundle reactor for catalytic gas phase reactions, automatically bypasses recirculated heating medium in cold, viscous state, during start up

During reactor (2) start up, heat exchange medium bypass (22) throughput, corresponds with a comparatively-cold and viscous state. In this case, the reactor vessel (8) is partially bypassed. During steady-state reactor operation, flow is automatically controlled as a function of the instantaneous heating power required in the reactor. In this case, heat exchange medium passes through the reactor at an essentially constant flow rate. Preferred Features: Control functions are carried out in a common unit. Bypassing is controlled on temperature and ranges of bypass ratio are specified for start-up and running conditions. Annular channels and openings form inlets and outlets for the heat exchange medium. A heater (30) is provided for the medium, and is used during start up. It is in e.g. a valved, auxiliary circuit in a location unrelated to the main medium inlet and outlet. An external heating medium is employed in a heater. Further details of the bypass, its valving and circulating pump ( ...

Verfahren zur Herstellung von Monosilan

Anlage zur kontinuierlichen Herstellung von Monosilan und Tetrachlorsilan durch katalytische Dismutierung von Trichlorsilan bei einer Betriebstemperatur und einem Druck von 1 bis 50 bar basierend auf folgenden Einheiten • einem Gegenstromreaktor (1) mit Doppelmantel (2), • mindestens ein im Gegenstromreaktor (1) angeordnetes und mit Katalysator (3) bestücktes Katalysatorbett (4), • einem Kondensator (5) am Kopf des Gegenstromreaktors (1), • einer Verdampfereinheit (6) am Sumpf des Gegenstromreaktors (1), • mindestens einer Trichlorsilanzuführung (A) für die Aufgabe von Trichlorsilan (7.1, 7.2) in den Gegenstromreaktor (1), • einem Wärmetauscher (7), wobei das Trichlorsilan zunächst mittels Leitung (7.1, 7.2) über den Wärmetauscher (7) geführt und dort vorgewärmt wird und dazu Sumpfprodukt mittels Leitung (6.1, 6.2) aus der Verdampfereinheit (6) über den Wärmetauscher (7) dem Doppelmantel (2) auf einer Höhe im unteren Teil des Gegenstromreaktors (1) zugeführt und auf einer Höhe im oberen ...

Waermebehandlungsanlage

Kuehlvorrichtung fuer Reaktorrohre

Double heat exchanger for exothermic reactions - has set of tubes contg. catalyst which act as reactor tubes, with bundle above and below, having heat transfer medium around tubes

Tubular reactor is for carrying out gas phase catalytic reactions. Two tube bundles are used above and below a common inlet branch (or outlet). The gas stream divides and flows out from either end of the vessel. On the cooling side, distributor plates are used to give uniform coolant flow along the walls of the tubes. The apertures on these increase towards the centre. A further baffle is used in the cooling side at the level of max. heat release. Used for strongly exothermic gas phase catalytic reaction. Can also be used on endothermic reactions. The capacity is not limited by the heat transfer factors nor by the construction.

Plattenwärmetauscher, Synthesevorrichtung und Verfahren zur Herstellung eines Produkts

Die Erfindung betrifft einen Plattenwärmetauscher für eine Synthesevorrichtung, insbesondere für einen Ammoniaksynthesekonverter, mit einem Plattenstapel aus mehreren kreisringförmigen oder kreisringsegmentförmige Platten, welche parallel zueinander um eine gemeinsame Längsachse angeordnet sind, wobei zwischen den Platten in radialer Richtung verlaufende erste Strömungskanäle für ein erstes Fluid angeordnet sind, und ein Strömungsrohr für ein zweites Fluid, welches derart entlang der Längsachse verlaufend angeordnet ist, dass die Platten das Strömungsrohr konzentrisch umgeben.

Verfahren zu katalytischen Gasphasenoxidation von Propen zu Acrolein

Verfahren zum Anfahren eines Reaktors und Reaktorsystem

Verfahren zur Herstellung von 1,2-Dichlorethan

Precipitated silica for use, e.g., in tires, battery separators or anti-blocking agents is produced in Taylor reactor fed with aqueous silicate solution and acidifying agent

The inlet(s) of a Taylor reactor comprising an outer reactor with an inner rotor, and used for the production of precipitated silica, is(are) fed with an aqueous silicate solution and an acidifying agent. An Independent claim is included for the precipitated silica.

Verfahren zur katalytischen Dampfphasenoxidation und Röhrenkesselreaktor

Preparation of chlorine involves oxidation of hydrogen chloride and gas stream comprising molecular oxygen in presence of fixed-bed catalyst is carried out in reactor having annular and disk-shaped deflection plates between catalyst tubes

Preparation of chlorine involves passing hydrogen chloride and molecular oxygen in a reactor (1) having parallel catalyst tubes (2) charged with fixed-bed catalyst aligned in longitudinal direction of reactor; and alternatively arranged annular and disk-shaped deflection plates (6 and 7) which leave annular passage (9) free. A liquid heat transfer medium circulates between tubes.

Improved reactor for catalytic reactions

... A catalytic reactor particularly suitable for the oxidation of olefins comprises a plurality of long thin tubes 29 of high chromium steel secured in closely-spaced relation in tube plates 28 and enclosed in a shell 10 which has inlets and outlets 22, 23 respectively for circulating a cooling fluid such as diphenyl around the tubes. The tubes, which are packed with a catalyst, e.g. of silver, preferably contain 8-18 per cent. of chromium and substantially no nickel. The shell 11 may be made of mild steel which has a slightly higher thermal expansion coefficient than the tubes, thus avoiding distortion of the latter. A tubular baffle 32 may be fitted between the tubes and the shell. The tube plates form flanges for the attachment of the inlet and outlet heads 12, 13 for the reactant stream.

Primary steam reforming plant

A plant for the synthesis of a product from a synthesis gas includes a synthesis gas generation stage including a high pressure reforming stage using tubes heated externally by means of pressurised combustion products; a synthesis stage wherein the product is synthesised from the synthesis gas; a combustion stage wherein part of the synthesis gas, or waste gas remaining after synthesis of the product, is combusted with compressed air to form the pressurised combustion products at a pressure similar to the reforming pressure; a trip system responsive to a plant malfunction including means to shut off the supply of feedstock to the reformer tubes, but not to isolate the synthesis stage and combustion stage from the reforming stage, and means to depressurise the combustion stage.

CATALYTIC REACTOR.

PURPOSE:To improve heat exchange efficiency and to suppress the pressure drop of a reaction fluid side and/or combustion gas side as far as possible so as to reduce required driving power for press feeding by providing a heat recovering means which projects from the inside surface on the inside surface of an inner cylindrical pipe. CONSTITUTION:The other end of the outer cylindrical pipe 9 of the concentrical double cylindrical pipe-shaped reaction apparatus 1 having an inlet 5 and outlet 23 for reaction fluid on the same one end is closed and the other end side, except a part of one end side is projected into a heating chamber. The reaction fluid is passed from the inlet 5 through the annular space which is delineated and formed of the outer cylindrical pipe 9 and the inner cylindrical pipe 11 and is packed with a catalyst; thereafter, the fluid is turned over at the other end and is then passed through the inside space of the inner cylindrical pipe 11 so as to be introduced to the outlet ...

APPARATUS AND METHOD FOR CARRYING OUT EXOTHERMIC CATALYTIC REACTIONS

... 1,219,973. Exothermic chemical reactions; temperature-control. REICHHOLD CHEMICALS Inc. 1 May, 1968 [14 June, 1967], No. 20552/68. Heading B1X. [Also in Division F4] Exothermic chemical reactions are carried out within a group of catalyst-containing tubes 17 extending between headers 13, 14 and surrounded by a shell 11 which is supplied through. inlet pipe 20 with a liquid heat-transfer medium which boils as it removes heat from the reaction taking place within the tubes, the reactor being designed so that the group of tubes is closer to inlet pipe 20 than to the outlet pipe 21 for vaporized and residual liquid H.T. medium. The reactants are supplied to tubes 17 through inlet 15; and the reaction products are withdrawn through outlet 16. The vapours of H.T. medium flow through pipe 23 to a condenser, and the condensate flows through pipe 25 to pipe 20 where it mixes with hot liquid H.T. medium from vessel 22. The mixture flows back to the shell of the reactor. The reactor may be used for ...

Improvements in or relating to the polymerisation of formaldehyde

Formaldehyde is polymerized by simultaneously introducing gaseous monomeric formaldehyde and a polymerization catalyst in the vapour or aerosol state into a reaction vessel and effecting the polymerization in contact with pulverulent formaldehyde polymer dispersed therein. Specified catalysts are trimethyl, triethyl, tripropyl, tributyl, trihexyl, dimethyloctadecyl, cyclohexyldibutyl and cyclohexyldiethyl amines. An apparatus for carrying out the process is described. Specification 925,145 is referred to.

Particulate medium for fluidized bed operations

In the operation of a fluidized bed for pre-heating workpiece parts as a step in a metal working process, the bed is comprised of graphite or other solid lubricant instead of the refractory particles e.g., sand conventionally employed. Thus, the parts may be removed from the bed for a succeeding operation without the necessity of coating the part with a lubricant as a separate step. Stearate-type lubricants can be used for treating yarns.

Method of activating a catalyst, reactor, and method of obtaining hydrocarbons in the fischer-tropsch process

The invention relates to Fischer-Tropsch synthesis in its compact form. A compact reactor comprises a housing having rectangular reaction channels accommodated therein and filled with a cobalt catalyst, nozzles for injecting synthesis gas in an amount determined by the ratio of the number of channels to the number of synthesis gas injection nozzles, and a nozzle for injecting and withdrawing a heat-transfer agent, on which nozzle a pressure regulator and an assembly for the withdrawal of synthetic hydrocarbons is arranged. The cobalt catalyst is activated by passing oxygen through the same. Synthetic hydrocarbons are obtained when synthesis gas is passed through the reaction channels of the reactor, which are filled with activated cobalt catalyst. Every 300-500 hours, the flow rate of the synthesis gas is increased, and then there is a return to the initial process conditions. This allows high-molecular hydrocarbon output per unit mass of the reactor to be achieved.

Reactor

Process

CATALYTIC CONVERSION OF GAS/LIQUID

Process for the production of an n-cyclohexyl sulphamate

Cyclohexylammonium N - cyclohexylsulphamate is prepared by reacting cyclohexylamine in finely divided liquid form with SO3 vapour in a molar ratio of from 1.5:1 to 3.0:1. The product may be worked up by extracting an aqueous solution thereof with a water-immiscible aromatic solvent and separating the aqueous solution of the cyclohexylammonium N-cyclohexylsulphamate. If the latter is treated with a solution of a base (e.g. NaOH) the N-cyclohexylsulphamate derived from that base is obtained in solution; this may be extracted with an organic water-immiscible solvent to remove N,N1-dicyclohexylsulphamide.

PROCESS FOR PREPARING ACRYLONITRILE

CATALYTIC REACTOR APPARATUS AND USE THEREOF

Method of activating a catalyst, reactor, and method of obtaining hydrocarbons in the fischer-tropsch process

REFORMING OF HYDROCARBONS

Flow reactors for chemical conversions with heterogeneous catalysts.

Flow reactors for chemical conversions with heterogeneous catalysts.

A apparatus for use in process systems which include exothermic chemical conversions of organic compounds to value added products is disclosed mote particularly, flow reactors for exothermic chemical conversions using a fixed heterogeneous catalyst with means for control of the exortherm. Flow reactors of the invention comprise a plurality of walled conduits (3) each having an outer surface disposed for contact with a heat-transfer medium, an inlet distribution manifold (2) adapted for flow communication with a downstream manifold (4) through channels formed by heterogeneous catalytic material disposed within each conduit during operation in a sequence of zones for catalyst having the same or different length along the longitudinal coordinate of the conduit and within each zone essentially uniform cross-section of the conduit measured in a plane perpendicular to the longitudinal coordinate thereby defining volume of the zone, and the sequence of zones comprising of at least two zones (5 ...

Flow reactors for chemical conversions with heterogeneous catalysts.

Continuous processing reactors and methods of using same.

Flow reactors for chemical conversions with heterogeneous catalysts.

Continuous processing reactors and methods of using same.

DRIVE DEVICE WITH ENGINE AND TRANSMISSION PART FOR FROM PLAY COMPONENT SYSTEM ELEMENTS ZUSAMMENGE ONES SET TOY MODELS

PROCEDURE FOR ELKTROINDUKTIVEN THE HEATING UP OF FLUID BED LAYERS AND DEVICE FOR THE BY FUEHRUNG THE PROCEDURE

DEVICE FOR THE DRYING PROCESS OF THERMALUNSTABLE, FOR CAKING BENDING PRODUCTS ON

GLEICHGEWICHTSREAKTION AND GAS/CLIQUID REACTION IN THE SCHLAUFENREAKTOR

REACTOR AND RADIATOR SYSTEM FOR EXOTHERMS REACTIONS

VERFAHREN ZUR HERSTELLUNG VON ACROLEIN UND ACRYLSAURE ODER METHACROLEIN UND METHACRYLSAURE

REAKTIONSAPPARAT ZUR DURCHFUEHRUNG KATALYTISCHER RAKTIONEN

PROCEDURE FOR THE PRODUCTION OF A LINEAR OLEFIN OF OLIGOMER USING A HEAT EXCHANGER

PROCEDURE OF THE START-UP OF A HETEROGENEOUSLY CATALYZED PARTIAL ONE GASEOUS PHASE OXIDATION OF ACROLEIN TO ACRYLIC ACID OR OF METHACROLEIN TOO METHACRYLSÄURE

PROCEDURE FOR THE CHANGE OF TEMPERATURE OF A BANK OF TUBES REACTOR

PROCEDURE FOR THE PRODUCTION OF CHLORINE BY GASEOUS PHASE OXIDATION OF HYDROGEN CHLORIDE

METAL PASSIVATION IN A WÄRMEAUSTAUSCHREFORMER

REAKTOR ZUR DURCHFUEHRUNG KATALYTISCHER REAKTIONEN

Katalysatoreinheit für ein Hochtemperatur-Brennstoffzellensystem

The invention relates to a catalytic converter unit (10) for a high-temperature fuel cell system, having a reformer catalytic converter (11) for the treatment of a fuel for the fuel cell and having an oxidation catalytic converter (12) for the aftertreatment of the exhaust gas from the fuel cell, wherein the oxidation catalytic converter (12) is arranged annularly around the cylindrical reformer catalytic converter (11). According to the invention, the gas paths of the oxidation catalytic converter (12) and of the reformer catalytic converter (11) are separated by a metal pipe (13) that accommodates the reformer catalytic converter (11), wherein the metal pipe (13) has a sleeve (14), which forms a housing for the reformer catalytic converter (11), and an inner pipe (15), which forms the inner wall of the annular oxidation catalytic converter (12).

Reformer unit for fuel cell system

Die Erfindung betrifft eine Reformereinheit (1), insbesondere für ein Brennstoffzellensystem (2), mit einem Brenner (3), welcher eine Brennkammer (4) aufweist, und einem Reformer (5), welcher zumindest teilweise in der Brennkammer (4) angeordnet ist und einer ersten Leitung (6), die den Reformer (5) mit Prozessgas, welches insbesondere rezirkuliertes Anodenabgas und Kohlenwasserstoffe aufweist, versorgt. Der Reformer (5) weist einen Prozessgasverteiler (7) auf, in welchen die erste Leitung (6) mündet und ist zumindest teilweise in der Brennkammer (4) angeordnet. Die Reformereinheit weist weiters einen Startbrenner (11) auf, der mit der Brennkammer (4) über ein Flammrohr (12) verbunden ist.

Reformereinheit für Brennstoffzellensystem

The invention relates to a reformer unit (1), in particular for a fuel cell system (2), having a burner (3) which comprises a combustion chamber (4), and a reformer (5) which is arranged at least in part in the combustion chamber (4), and a first conduit (6) which supplies the reformer (5) with process gas, which comprises in particular recirculated anode off-gas and hydrocarbons. According to the invention, the reformer (5) comprises a manifold (7) into which the first conduit (6) opens out.

REACTOR FOR THE PRODUCTION OF C2BIS C8OLEFINEN FROM ONE OXYGENAT, WATER VAPOUR AND ONE OR MORE HYDROCARBONS CONTAINING MATERIAL FLOW

MULTI-LEVEL PROCEDURE FOR THE POLYMERIZATION OF OLEFINEN

PROCEDURE FOR THE PRODUCTION OF A CHEMICAL REACTION PRODUCT OF MEANS FIXED BED REACTOR

VERFAHREN ZUR HERSTELLUNG EINES CHEMISCHEN REAKTIONSPRODUKTS MITTELS FESTBETTREAKTOR

PROCEDURE AND REACTOR FOR THE PRODUCTION OF METHANOL

CATALYTIC GASEOUS PHASE POLYMERIZATION OF OLEFINEN

REACTOR FOR THE EXECUTION OF CATALYTIC REACTIONS

PROCEDURE AND DEVICE FOR THE TRANSPORT OF CELEBRATIONS PARTICLES BETWEEN AREAS

CENTRIFUGAL DISCONNECTING SWITCH

CATALYTIC CONVERSION OF GAS OR LIQUID IN A PLURALROHRREAKTOR.

HYDROGENATION PROCEDURE.

PROCEDURE AND DEVICE FOR THE ENTERPRISE OF A SYSTEM WITH CIRCULATING FLUIDISED BED

ROHRBUNDELREAKTOR FUR THE CATALYTIC GASEOUS PHASE OXIDATION

Reactor for the production of methanol

BANK OF TUBES

METHOD AND DEVICE FOR CIRCULATING SOLID IN A WIRBELSCHICHTREAKTOR

PROCEDURE AND DEVICE FOR THE ENTERPRISE OF A REACTOR SYSTEM WITH CIRCULATING FLUIDISED BED

CONTINUOUS GASEOUS PHASE PROCEDURE FOR THE COATING OF POLYMERIZATION CATALYSTS

LYING TUBULAR REACTOR FOR THE TREATMENT OF PASTY PROPERTY OR BULK MATERIAL

Reaktionsrohr for tube furnaces as well as procedure for its production

CHEMICAL REACTOR WITH HEAT EXCHANGER

PROCEDURE FOR MODIFYING THE TEMPERATURE AT THE PROXIMITY OF THE REACTOR WALL IN A GAS POLYMERIZATION REACTOR

Compact methanol reformer for a submarine

The present invention relates to a methanol reformer (10) having a reaction region (20), a charging region (30) and a discharge region (40). The reaction region (20), the charging region (30) and the discharge region (40) are arranged one above the other with the reaction region (20) at the bottom. At least one first coaxial reaction tube (50) is arranged vertically in the reaction region (20), the at least one first coaxial reaction tube (50) having an outer tube region (52) and an inner tube region (54), the outer tube region (52) being filled with a catalyst. The outer tube region (52) is connected to the charging region (30) and the inner tube region (54) is connected to the discharge region (40). A preheating device (100) for preheating the methanol-water mixture is disposed in the reaction region (20).

METHOD FOR PRODUCING HYDROGEN AND APPARATUS FOR SUPPLYING HYDROGEN

Commercial Fischer-Tropsch reactor

Catalyst withdrawal apparatus and method for regulating catalyst inventory in a fluid catalyst cracking unit

CATALYST WITHDRAWAL APPARATUS AND METHOD FOR REGULATING CATALYST INVENTORY IN A FLUID CATALYST CRACKING UNIT Abstract A catalyst withdrawal apparatus and method for regulating catalyst inventory in a fluid catalytic cracking catalyst (FCC) unit (210) is provided. In one embodiment, a catalyst withdrawal apparatus for removing catalyst from a FCC unit (210) includes a pressure vessel having a metering device (256) coupled to a fill port (314). A heat dissipater (258) is located adjacent the metering device (256) and is adapted to cool catalyst entering the pressure vessel (310). A sensor (264) is coupled to the pressure 10 vessel arranged to provide a metric indicative of catalyst entering the pressure vessel through the metering device (256). In another embodiment, a method for regulating catalyst inventory in a FCC unit (210) includes the steps of determining a change of catalyst present in a FCC unit (210), withdrawing catalyst from the FCC unit (210) into an isolatable storage vessel ...

HEAT TREATMENT OF PARTICULATE SOLID MATERIALS

Method and apparatus for processing of carbon-containing feed stock into gasification gas

The invention relates to chemical technology and equipment, in particular to apparatuses of processing of solid household and industrial waste, as well as other carbon-containing feedstock into combustible gasification gas and methods for pyrolysis and downdraft gasification process.

Hydrogen production by an autothermal heat exchanger packed-bed membrane gas reformer

A process for producing hydrogen from natural gas, said process comprises the steps of: (i) providing an autothermal heat exchanger packed-bed membrane reformer (APBMR) comprising: (a) an elongated external gas oxidation compartment comprising an inlet, an outlet and packed oxidation catalyst particles, said inlet and outlet being located each at one extremity of said external gas oxidation compartment; (b) an elongated internal gas steam-reforming compartment comprising an inlet, an outlet and packed steam-reforming catalyst particles, said inlet and outlet being located each at one extremity of said internal gas steam-reforming compartment; (c) one or more hydrogen-separating membrane(s) positioned in said steam-reforming compartment substantially parallel to the longitudinal axis of said steam-reforming compartment; (d) one insulation layer surrounding said external compartment; and, optionally, (e) one or more elongated internal gas oxidation compartment(s) positioned in said steamreforming compartment substantially parallel to the longitudinal axis of said gas steam-reforming internal compartment, and comprising an inlet, an outlet and packed oxidation catalyst particles, said inlet and outlet being located each at an extremity of said internal gas oxidation compartment(s); (ii) supplying a mixture comprising said natural gas and air to said gas oxidation compartment(s) of said reformer; and (iii) supplying a mixture comprising said natural gas and water to said gas steam-reforming compartment, wherein the water-to-gas molar ratio

Method and Installation for the Manufacture of Carbon Nanotubes

Method for the manufacture of carbon nanotubes by thermal decomposition of at least one gaseous hydrocarbon ( 14 ) in the presence of a solid catalyst in a reactor ( 4 ) into which the catalyst is introduced via an inlet lock chamber ( 17 ) flushed by an inert gas ( 21, 22, 25, 26 ) and from which the carbon nanotubes are withdrawn via an outlet lock chamber ( 37 ) which is flushed with a flow of inert gas ( 39, 40 ).

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.

Tunable catalytic gasifiers and related methods

The present disclosure provides tunable catalytic gasifier systems suitable for gasifying coal, biomass, and other fuel sources. The gasifier reactors of the disclosed systems may be heated by, e.g., a catalytic tube or other jacket that generates heat by catalytically combusting syngas, which syngas may be syngas produced by the gasifier system.

Heat exchanger reformer

A catalytic reformer assembly includes a heated medium flow path for a first medium and a reforming flow path for a second medium. A catalyst substrate is located within the reforming flow path and supports a catalyst. A heat exchanger is disposed within the heated medium flow path for transferring heat from the heated medium flow path to the catalyst substrate.

Compact fischer tropsch system with integrated primary and secondary bed temperature control

A Fischer Tropsch (“FT”) reactor includes at least one FT tube. The FT tube may include a catalyst that is designed to catalyze an FT reaction, thereby creating a hydrocarbon from syngas. The FT reactor also includes a primary cooling fluid flow path that extends in a direction that is substantially parallel to the longitudinal length of the FT tube. A secondary cooling fluid flow path extends in a direction that is different than the direction of the primary cooling fluid flow path.

Methods for Supplying Solid Catalysts to a Solution Polymerization Reactor

Disclosed is a solution polymerization process, or, alternatively, a method of delivering powder catalysts to a solution polymerization reactor, comprising combining a homogeneous single-site catalyst precursor with α-olefin monomers to form a polyolefin, wherein the homogeneous single-site catalyst precursor is in the form of (i) a dry powder, (ii) suspended in a aliphatic hydrocarbon solvent, or (iii) suspended in an oil or wax, wherein the homogeneous single-site catalyst precursor is at a concentration greater than 0.8 mmole/liter when suspended in the aliphatic hydrocarbon solvent prior to entering the solution polymerization reactor.

Fluidized Bed Reactor Adapted For The Production Of Biphased Systems

A fluidized bed reactor designed for in situ gas phase impregnation. The reactor comprises a tube with an upstream zone and a downstream zone, the upstream zone and the downstream zone being separated by a separation filter. A method for a controlled-deposition of a sublimated precursor onto a fluidized solid support. The method is remarkable in that it is carried out in situ within the tube of the fluidized bed reactor in accordance with the fluidized bed reactor. 120-. (canceled)21. A fluidized bed reactor , said fluidized bed reactor comprising:a gas inlet and a gas outlet being located downstream from the gas inlet;a tube inserted between the gas inlet and the gas outlet; anda heating part connected to the tube,wherein the tube comprises an upstream zone and a downstream zone, the upstream zone and the downstream zone being separated by a separation filter.22. The fluidized bed reactor according to claim 21 , wherein the tube is made of material which is resistant to temperature of at least up to 1000° C. and is transparent.23. The fluidized bed reactor according to claim 21 , wherein the tube is made of quartz.24. The fluidized bed reactor according to claim 21 , wherein the upstream zone is delimited by the separation filter and by a first porous filter claim 21 , and the downstream zone is delimited by the separation filter and by a second porous filter.25. The fluidized bed reactor according to claim 24 , wherein the tube is inserted between the gas inlet and the gas outlet with respectively a first seal and a second seal.26. The fluidized bed reactor according to claim 25 , wherein the first porous filter is adjacent to the first seal and the second porous filter is adjacent to the second seal.27. The fluidized bed reactor according to claim 21 , wherein the heating part is at least one of a heating cable claim 21 , a heating jacket and a thermal activation source.28. The fluidized bed reactor according to claim 21 , wherein at least one vibrator is ...

Method for producing devulcanized rubber and an apparatus therefor

A method for producing devulcanized rubber and an apparatus ( 100 ) therefor. The method for producing devulcanized rubber comprises the steps of (1) providing vulcanized rubber particles with a pre-determined particle size and (2) devulcanizing the vulcanized rubber particles. The vulcanized rubber particles are devulcanized mechanically by impact forces and devulcanized chemically by a chemical composition. The impact forces break sulphur-sulphur and sulphur-carbon bonds of the vulcanized rubber particles causing surfaces of the rubber to become receptive in reacting with the chemical composition and the chemical composition renders the sulphur passive to prevent reattachment of the bonds, of which the chemical composition comprises at least one accelerator, at least one inorganic activator and at least one organic activator.

System for generating h2s in an alkaline medium and method of using the same

Method of producing hydrogen sulfide in an alkaline environment. A mixture having a sodium salt, elemental sulfur (S) and water is added to a reactor for the purpose of generating hydrogen sulfide (H 2 S) gas as the main product and sodium sulfate (Na 2 SO 4 ) as a byproduct.

APPARATUS AND PROCESS FOR THE PRODUCTION OF FORMALDEHYDE

An apparatus for the production of formaldehyde is disclosed. The apparatus comprises a cooled tubular reactor section () having a first inlet, a first outlet and a plurality of tubes each having a first end in fluid communication with the first inlet and a second end in fluid communication with the first outlet. The plurality of tubes contain a first catalyst for the production of formaldehyde by oxidative dehydrogenation. The apparatus is characterised in that the apparatus further comprises a pre-reactor section (). The pre-reactor section () has an inlet. The pre-reactor section () has an outlet in fluid communication with the first inlet of the cooled tubular reactor section (). The pre-reactor section () is configured to contain, in use, an adiabatic catalyst bed. The adiabatic catalyst bed comprises a second catalyst for the production of formaldehyde by catalytic oxidative dehydrogenation. 1. An apparatus for the production of formaldehyde , the apparatus comprisinga cooled tubular reactor section having a first inlet, a first outlet, and a plurality of tubes each having a first end in fluid communication with the first inlet and a second end in fluid communication with the first outlet, the plurality of tubes configured to contain, in use, a first catalyst for the production of formaldehyde by catalytic oxidative dehydrogenation,a pre-reactor section having an inlet, and having an outlet in fluid communication with the first inlet of the cooled tubular reactor section, the pre-reactor section being configured to contain, in use, an adiabatic catalyst bed comprising a second catalyst for the production of formaldehyde by catalytic oxidative dehydrogenation.2. The apparatus according to claim 1 , wherein the cooled tubular reactor section further comprises a shell surrounding the plurality of tubes and having at least one second inlet and at least one second outlet for passing heat transfer fluid through the shell in use.3. The apparatus according to claim 1 ...

Method and system for the production of hydrogen

Disclosed is a process for the production of hydrogen in a reactor system comprising a steam reforming reaction zone comprising a reforming catalyst and a membrane separation zone comprising a hydrogen-selective membrane. The process involves a reaction system of so-called open architecture, wherein the reforming zone and the membrane separation zone operate independently of each other. The invention provides the heat for the reforming reaction through heat exchange from liquid molten salts, preferably heated by solar energy.

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.

Process for Preparing Polyolefins

The present invention relates to a process of preparing a polyolefin in a loop reactor by introducing anti-fouling agent in by-pass pipes. Also, the invention relates to the use of anti-fouling agent to prevent blockage by feeding the anti-fouling agent into the by-pass pipes of the loop reactor.

Design of an Ethylene Oligomerization/Trimerization/Tetramerization Reactor

A process includes periodically or continuously introducing an olefin monomer and periodically or continuously introducing a catalyst system or catalyst system components into a reaction mixture within a reaction system, oligomerizing the olefin monomer within the reaction mixture to form an oligomer product, and periodically or continuously discharging a reaction system effluent comprising the oligomer product from the reaction system. The reaction system includes a total reaction mixture volume and a heat exchanged portion of the reaction system comprising a heat exchanged reaction mixture volume and a total heat exchanged surface area providing indirect contact between the reaction mixture and a heat exchange medium. A ratio of the total heat exchanged surface area to the total reaction mixture volume within the reaction system is in a range from 0.75 into 5 in, and an oligomer product discharge rate from the reaction system is between 1.0 (lb)(hr)(gal) to 6.0 (lb)(hr)(gal). 1. A process comprising:periodically or continuously introducing an olefin monomer and periodically or continuously introducing a catalyst system or catalyst system components into a reaction mixture within a reaction system;oligomerizing the olefin monomer within the reaction mixture to form an oligomer product; andperiodically or continuously discharging a reaction system effluent comprising the oligomer product from the reaction system;wherein the reaction system comprises: a total reaction mixture volume within the reaction system; and a heat exchanged portion of the reaction system comprising a heat exchanged reaction mixture volume and a total heat exchanged surface area providing indirect thermal contact between the reaction mixture and a heat exchange medium;{'sup': −1', '−1', '−1', '−1, 'wherein an oligomer product discharge rate from the reaction system is between 1.5 (lb)(hr)(gal) to 6.0 (lb)(hr)(gal); and'}{'sup': −1', '−1, 'wherein a ratio of the total heat exchanged surface area ...

MULTI-BED CATALYTIC CONVERTER WITH INTER-BED COOLING

A multi-bed catalytic converter comprising at least a first catalytic bed, a second catalytic bed and a heat exchanger arranged between said first bed and said second bed, wherein said heat exchanger is arranged to transfer heat from the hot effluent of the first bed to a cooling medium; said heat exchanger comprises a plurality of stacked round plates, wherein adjacent plates define gaps therebetween, and the effluent of the first catalytic bed and the cooling medium are respectively fed into alternate gaps. 124-. (canceled)25. A multi-bed cylindrical catalytic converter , comprising:a first catalytic bed;a second catalytic bed;a heat exchanger arranged between said first catalytic bed and said second catalytic bed, said heat exchanger being arranged to transfer heat from a first medium to a second medium;an input and an output for the first medium; andan input and an output for the second medium;wherein the first medium is the hot effluent of the first catalytic bed before admission into the second catalytic bed, and the second medium is a cooling medium;wherein said heat exchanger comprises a plurality of stacked round plates, said plurality of stacked round plates being full circular plates or annular plates, and adjacent plates of the plurality of stacked round rates define gaps therebetween;wherein the hot effluent of the first catalytic bed and the cooling medium pass respectively through alternating ones of the gaps between the plurality of stacked round plates;wherein said first catalytic bed is a hollow cylinder comprising a cavity and said heat exchanger is arranged coaxially to the first catalytic bed inside said cavity.26. The multi-bed cylindrical catalytic converter according to claim 25 , wherein said plurality of stacked round plates are stamped plates obtained mechanically by metal sheet pressing.27. The multi-bed cylindrical catalytic converter according to claim 25 , wherein at least one of the input or the output of at least one of the first ...

REACTION CONTAINER

The invention relates to a reaction container for stabilizing the temperature of a liquid mixture substances, the reaction container comprising an upper container part and a lower container part, in which the lower container part has an inner direct means of refrigeration and an outer indirect means of refrigeration in addition to an inner, direct means of heating and an outer, indirect means of heating. 111-. (canceled)12. A reaction container comprising ,a container upper part and a container bottom part, wherein the container bottom part has an internal, direct cooling and an external, indirect cooling and an inner, direct heating and an outer, indirect heating to stabilize the temperature of a liquid substance mixture.13. The reaction container according to claim 12 , wherein the inner cooling and the inner heating and the outer cooling and the outer heating are coupled to a thermal management system.14. The reaction container according to claim 13 , wherein the thermal management system comprises a thermal oil heater.15. The reaction container according to claim 12 , wherein the container upper part is configured larger than the container bottom part.16. The reaction container according to claim 14 , further comprising one or more distillation columns arranged on the container upper part.17. The reaction container according to claim 16 , wherein a pressure relief valve is arranged on the container upper part.18. The reaction container according to claim 16 , wherein a heavy particle collector is arranged on the container lower part.19. The reaction container according to claim 12 , further comprising a submersible pump and/or an agitator arranged in the container interior.20. A method of using the reaction vessel according to comprising claim 12 , carrying out a catalytic pressureless depolymerization of carbonaceous input material.21. A method to temperature-stabilize a liquid substance mixture hi the reaction container of comprising claim 13 ,keeping the ...

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.

ENERGY EFFICIENT POLYOLEFIN PROCESS

A manufacturing system for producing polyolefin includes a polymerization reactor, a flash chamber, and a purge column. In certain embodiments, the purge column may receive a solids stream directly from the flash chamber. Further, the purge column may function as a feed tank for an extruder within an extrusion/loadout system. According to certain embodiments, the manufacturing system may be configured to consume less than 445 kilowatt-hours of energy per metric ton of polyolefin produced based on consumption of electricity, steam, and fuel gas. 121.-. (canceled)22. A system , comprising:a polymerization reactor configured to produce a slurry comprising polyolefin particles and a diluent;a coolant system configured to provide a coolant to a reactor jacket disposed along a portion of the polymerization reactor, wherein an outlet temperature of the coolant exiting the reactor jacket is about 15° F. or more greater than an inlet temperature of the coolant entering the reactor jacket; and receive an input indicative of the outlet temperature of the coolant exiting the reactor jacket; and', 'activate an output to actuate the coolant system to provide the coolant to the reactor jacket based at least in part on the input to maintain the outlet temperature about 15° F. or more greater than the inlet temperature of the coolant entering the reactor jacket., 'one or more automation controllers configured to23. The system of claim 22 , wherein the coolant system is configured to provide the coolant to the reactor jacket such that the outlet temperature of the coolant exiting the reactor jacket is between about 15° F. and about 30° F. greater than the inlet temperature of the coolant entering the reactor jacket.24. The system of claim 22 , wherein the coolant system is configured to provide the coolant to the reactor jacket such that the outlet temperature of the coolant exiting the reactor jacket is between about 15° F. and about 50° F. greater than the inlet temperature of the ...

APPARATUS FOR PRODUCING WATER-ABSORBING RESIN PARTICLES

An apparatus for producing water-absorbing resin particles for which surface cross-linking treatment is conducted by spraying a surface cross-linking agent to a water-absorbing resin particle precursor and heating the agent and the precursor, the apparatus includes a treatment container in which the surface cross-linking treatment is conducted, a stirring device including a stirring member disposed in the treatment container, a heating device that heats an inside of the treatment container; and a spray nozzle disposed in the treatment container, the spray nozzle spraying into the treatment container the surface cross-linking agent supplied from a surface cross-linking agent supply source in an exterior of the treatment container through a supply pipe. In a flow path in the spray nozzle spanning from an entrance of the spray nozzle to a spray exit, a point whose opening cross-section is smallest in a flow path through which a fluid passes is the spray exit. 1. An apparatus for producing water-absorbing resin particles for which surface cross-linking treatment is conducted , the surface cross-linking treatment being conducted by spraying a surface cross-linking agent to a water-absorbing resin particle precursor and heating the agent and the precursor , the apparatus comprising:a treatment container in which the surface cross-linking treatment is conducted;a stirring device including a stirring member disposed in the treatment container;a heating device that heats an inside of the treatment container; anda spray nozzle disposed in the treatment container, the spray nozzle spraying into the treatment container the surface cross-linking agent supplied from a surface cross-linking agent supply source in an exterior of the treatment container through a supply pipe, whereinin a flow path in the spray nozzle spanning from an entrance of the spray nozzle to a spray exit, a point whose opening cross-section is smallest in a flow path through which a fluid passes is the spray ...

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 ...

METHOD FOR THE OXIDATIVE DEHYDRATION OF N-BUTENES INTO 1,3-BUTADIEN

The invention relates to a method for producing 1,3 butadien by means of the oxidative dehydration of n-butenes on a heterogenous particulate multimetal oxide catalyst which contains molybdenum as the active compound and at least one other metal and which is filled into the contact tubes (KR) of two or more tube bundle reactors (R-I, R-II), wherein a heat transfer medium flows around the intermediate space between the contact tubes (KR) of the two or more tube bundle reactors (R-I, R-II). The method includes a production mode and a regeneration mode which are carried out in an alternating manner. In the production mode, an n-butene-containing feed flow is mixed with an oxygen-containing gas flow and conducted as a supply flow () over the heterogenous particulate multimetal oxide catalyst filled into the contact tubes (KR) of the two or more tube bundle reactors (R-I, R-II), and the heat transfer medium absorbs the released reaction heat, minus the heat quantity used to heat the supply flow () to the reaction temperature in the production mode, by means of an indirect heat exchange and completely or partly dispenses the reaction heat onto a secondary heat transfer medium (H2Oliq) in an external cooler (SBK). In the regeneration mode, the heterogenous particulate multimetal oxide catalyst is regenerated by conducting an oxygen-containing gas mixture () over the catalyst and burning off the deposits accumulated on the heterogenous particulate multimetal oxide catalyst. The invention is characterized in that the two or more tube bundle reactors (R-I, R-II) have a single heat transfer medium circuit and as many of the two or more tube bundle reactors (R-I, R-II) as necessary are operated constantly in the production mode so that the released reaction heat, minus the heat quantity used to heat the supply flow () to the reaction temperature in the production mode, suffices to keep the temperature of the heat transfer medium in the intermediate spaces between the content ...

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.

Reactor for performing equilibrium-reduced reactions

A reactor for performing equilibrium-reduced reactions, includes a tubular reactor housing in which a first zone is arranged, through which a liquid absorbent flows, and which extends in the longitudinal direction of the tube. Aa second zone is arranged for receiving a catalyst material and also extends in the longitudinal direction of the tube. The first zone and the second zone are separated by a gas-permeable separation zone. The separation zone has a mechanically self-supporting structure and the aspect ratio of the tubular reactor housing along a reaction zone is greater than 6.

Design of an Ethylene Oligomerization/Trimerization/Tetramerization Reactor

A process includes periodically or continuously introducing an olefin monomer and periodically or continuously introducing a catalyst system or catalyst system components into a reaction mixture within a reaction system, oligomerizing the olefin monomer within the reaction mixture to form an oligomer product, and periodically or continuously discharging a reaction system effluent comprising the oligomer product from the reaction system. The reaction system includes a total reaction mixture volume and a heat exchanged portion of the reaction system comprising a heat exchanged reaction mixture volume and a total heat exchanged surface area providing indirect contact between the reaction mixture and a heat exchange medium. A ratio of the total heat exchanged surface area to the total reaction mixture volume within the reaction system is in a range from 0.75 into 5 in, and an oligomer product discharge rate from the reaction system is between 1.0 (lb)(hr)(gal) to 6.0 (lb)(hr)(gal). 1. A reaction system for oligomerizing an olefin monomer , the reaction system comprising:one or more reaction system inlets configured to periodically or continuously introduce an olefin monomer, a catalyst system or catalyst system components, or any combination thereof to a reaction mixture within the reaction system;one or more reaction system reaction mixture outlets configured to periodically or continuously discharge a reaction system effluent comprising an oligomer product from the reaction system;a total reaction mixture volume within the reaction system; anda heat exchanged portion of the reaction system comprising a heat exchanged reaction mixture volume and a total heat exchanged surface area providing indirect thermal contact between the reaction mixture and a heat exchange medium;wherein an oligomer product discharge rate from the reaction system is between 1.5 lb/hr/gal to 6.0 lb/hr/gal; and{'sup': −1', '−1, 'wherein a ratio of the total heat exchanged surface area to the total ...

Heat Exchanger

This heat exchanger ( 100 ) includes a core portion ( 1 ), a header portion ( 2 ), and an intermediate member ( 3 ), and the curvature radius of a corner ( 31 a to 31 d ) of the intermediate member is configured to be smaller than the curvature radius at a header portion side.

MULTI-BED CATALYTIC CONVERTER

A multi-bed catalytic converter comprising: a plurality of catalytic beds which are traversed in series by a process gas, sequentially from a first catalytic bed to a last catalytic bed of said plurality, and at least one inter-bed heat exchanger () positioned between a first catalytic bed and a second catalytic bed of said plurality, wherein at least the last catalytic bed of said plurality is adiabatic and is made of fine catalyst with a particle size not greater than 2 mm. 115-. (canceled)16. A multi-bed catalytic converter , comprising:a plurality of catalytic beds which are traversed in series by a process gas, sequentially from a first catalytic bed to a last catalytic bed of said plurality of catalytic beds; andat least one inter-bed heat exchanger positioned between the first catalytic bed and a second catalytic bed of said plurality of catalytic beds, and arranged to remove heat from the process gas leaving the first catalytic bed before entering the second catalytic bed;wherein at least the last catalytic bed of said plurality of catalytic beds is adiabatic and is made of a fine catalyst with a particle size not greater than 2 mm;wherein each of the plurality of catalytic beds includes at least one gas distributor and at least one gas collector arrange to provide that the catalytic bed is traversed by the process gas with a radial flow or axial-radial flow.17. The multi-bed catalytic converter of claim 16 , wherein the particle size of said fine catalyst is 0.8 mm to 1.4 mm.18. The multi-bed catalytic converter of claim 17 , wherein the particle size is 0.8 mm to 1.4 mm.19. The multi-bed catalytic converter of claim 16 , wherein said fine catalyst has a particle size of 1.3 mm or about 1.3 mm.20. The multi-bed catalytic converter of claim 16 , wherein only the last catalytic bed of said plurality of catalytic beds is made of fine catalyst claim 16 , the other catalytic bed(s) of the plurality of catalytic beds being made of catalyst with greater particle ...

NESTED-FLOW HEAT EXCHANGERS AND CHEMICAL REACTORS

Disclosed is a technology based upon the nesting of tubes to provide chemical reactors or chemical reactors with built in heat exchanger. As a chemical reactor, the technology provides the ability to manage the temperature within a process flow for improved performance, control the location of reactions for corrosion control, or implement multiple process steps within the same piece of equipment. As a chemical reactor with built in heat exchanger, the technology can provide large surface areas per unit volume and large heat transfer coefficients. The technology can recover the thermal energy from the product flow to heat the reactant flow to the reactant temperature, significantly reducing the energy needs for accomplishment of a process. 1. (canceled)2. A chemical reactor comprising:a first tube;a second tube positioned in the first tube and defining an annular space between the first tube and the second tube; anda manifold assembly coupled to a first end of the first tube and a first end of the second tube, wherein the manifold assembly defines a first opening in direct fluid communication with the annular space between the first tube and the second tube and a second opening in direct fluid communication with a channel along the length of the second tube,wherein a second end of the second tube is open proximate a second end of the first tube.3. The chemical reactor of claim 2 , wherein the first tube and the second tube are coaxial.4. The chemical reactor of claim 2 , wherein a bayonet flow path is defined by the annular space claim 2 , the first and second openings claim 2 , and the channel claim 2 , and comprising a catalyst disposed along the bayonet flow path.5. The chemical reactor of claim 2 , comprising a heating assembly disposed around the manifold assembly.6. The chemical reactor of claim 2 , comprising a water shift reaction (WSR) unit configured to receive a product gas generated in the chemical reactor.7. The chemical reactor of claim 2 , wherein a ...

REACTOR FOR PREPARING HYDROGEN CYANIDE BY THE ANDRUSSOW PROCESS, EQUIPMENT COMPRISING SAID REACTOR AND PROCESS USING SUCH AN EQUIPMENT

The present invention relates to a reactor () for preparing hydrogen cyanide by the Andrussow process, to an equipment () comprising said reactor and to a process for preparing hydrogen cyanide by the Andrussow process. The reactor () comprising at least one gas inlet (I) for reactant gases mixture, a catalyst (), a porous support for the catalyst (), a porous sub support () and at least one outlet (P) for the reaction products. According to the invention, said reactor has a cone frustum shaped metallic casing () and comprises inside the metallic casing, a gas distributor () located between the gas inlet and the catalyst, said distributor comprising at least one cone frustum element (D, . . . Dn) having an upper base directed towards the gas inlet (I). 1201210202203. Reactor for preparing hydrogen cyanide by the Andrussow process , with at least one gas inlet for reactant gases mixture , a catalyst , at least one support for the catalyst and at least one outlet for the reaction products , wherein said reactor () comprises a cone frustum shaped casing () and comprises inside said casing , a gas distributor () located between a gas inlet (I) and a catalyst () , said distributor comprising at least onecone frustum element (Dn) having an upper base directed towards the gas inlet.2201. Reactor for preparing hydrogen cyanide by the Andrussow process according to claim 1 , wherein said reactor () is a cone frustum shaped with cylindrical bases.311212. Reactor for preparing hydrogen cyanide claim 1 , according to claim 1 , wherein the gas distributor comprises a plurality of coaxial cone frustum elements (D claim 1 , . . . Dn) being arranged around each other with a central cone frustum element having a height h claim 1 , an outer cone frustum element having an height hn claim 1 , and intermediate elements having respectively height h claim 1 , . . . claim 1 , h(n−1) claim 1 , where h is smaller than h claim 1 , and respectively h(n−1) is smaller than hn.42150. Reactor for ...

SYSTEMS AND METHODS FOR PREDICTING AND CONTROLLING THE PROPERTIES OF A CHEMICAL SPECIES DURING A TIME-DEPENDENT PROCESS

Devices and methods for controlling the properties of chemical species during time-dependent processes. A device includes a reactor for containing one or more chemical species of a time-dependent process, an extraction pump for automatically and continuously extracting an amount of the one or more chemical species from the reactor, one or more detectors for measuring property changes of the one or more extracted chemical species and generating a continuous stream of data related to the one or more property changes to the one or more chemical species during a time interval, and a process controller configured to fit the continuous stream of data to a mathematical function to predict one or more properties of the one or more chemical species at a future time point and make one or more process decisions based on the prediction of one or more properties at the future time point. 131-. (canceled)32. A method comprising:introducing, in a reactor, one or more chemical species to be monitored during a time-dependent process;detecting, using one or more detectors, one or more property changes to the one or more chemical species over a time interval;receiving, from the one or more detectors, a continuous stream of data related to the one or more property changes to the one or more chemical species during the time interval;fitting, using a process controller, the continuous stream of data to a mathematical function to predict one or more properties of the one or more chemical species at a future time point; andmaking, by the process controller, one or more process decisions based on the prediction of one or more properties at the future time point;wherein the continuous stream of data comprises one or more of UV absorption, visible absorption, infra-red absorption, Raman scattering, fluorescence, reduced viscosity, intrinsic viscosity, dynamic light scattering, static light scattering, Mie scattering, and evaporative light scattering.33. The method of claim 32 , wherein the ...

Energy efficient polyolefin process

A manufacturing system for producing polyolefin includes a polymerization reactor, a flash chamber, and a purge column. In certain embodiments, the purge column may receive a solids stream directly from the flash chamber. Further, the purge column may function as a feed tank for an extruder within an extrusion/loadout system. According to certain embodiments, the manufacturing system may be configured to consume less than 445 kilowatt-hours of energy per metric ton of polyolefin produced based on consumption of electricity, steam, and fuel gas.

METHOD AND APPARATUS FOR PRODUCING HIGH PURITY PHOSGENE

A reactor for producing phosgene, the reactor comprising: tube located in a shell and a space located between the tube and the shell; a cooling medium located in the space and a catalyst located in the tube or cooling medium located in the tube and a catalyst located in the space; a feed inlet; and a product mixture outlet; wherein the tube comprises one or more of: a mini-tube and a second tube section; a first concentric tube concentrically located in the shell; a twisted tube; an internal scaffold; and an external scaffold.

CONTINUOUS REACTION DEVICE FOR SYNTHESIZING POLYOXYMETHYLENE DIMETHYL ETHERS

The present invention pertains to the technical field of energy resource chemical industry, and in particular relates to a continuous reaction device and process for synthesizing polyoxymethylene dimethyl ethers by using paraformaldehyde and methylal as feedstock or using trioxane and methylal as feedstock in the presence of an acidic catalyst. The continuous reaction device comprises multiple slurry bed stirred tank reactors connected in series or in combination of series connection and parallel connection, and also comprises an on-line solid-liquid separation device to perform separation of the reaction mixture from the catalyst. Each of the tank reactors is provided with an axial-flow stirring paddle having 2-6 blades per layer, to ensure sufficient mixing of the reactants with the catalyst. By using a distributed control pattern of reaction temperature and feedstock supplying to enhance the process and to optimize the operation, the reaction device of the present invention can effectively achieve large-scale continuous production of polyoxymethylene dimethyl ethers, and both the yield rates and the distribution of the reaction product are better than those of prior art. 1. A continuous reaction device for synthesizing polyoxymethylene dimethyl ethers , the reaction using paraformaldehyde and methylal as feedstock or using trioxane and methylal as feedstock and being carried out in the presence of an acidic catalyst , wherein ,the continuous reaction device comprises multiple reactors connected in series or in combination of series connection and parallel connection, and also comprises an on-line solid-liquid separation device to perform solid-liquid separation of the reaction mixture from the catalyst;each of the tank reactors is independently controlled at a pressure of 1.0-4.0 MPa and a temperature of 50-120° C.; a molar ratio of paraformaldehyde or trioxane, metered in mole number of formaldehyde contained therein, to methylal in the feedstock is 0.5-5.0; ...

DEVICE FOR PRODUCING HYDROGEN BY REFORMING REACTION AND WASTE HEAT

A hydrogen producing device is mounted at an exhaust gas port of a vehicle to receive exhaust gas and waste heat as a heat source necessary for a reforming reaction with a catalyst member in a reaction chamber. The hydrogen producing device includes a heating chamber in which the reaction chamber is received, a fuel introducing tube disposed to introduce fuel to the reaction chamber, an air introducing tube disposed in the heating chamber to exchange heat with a reaction air thereinto and introducing the reaction air into the reaction chamber for the reforming reaction, and a product discharging tube disposed to discharge a hydrogen-rich synthesis gas generated in the reaction chamber. 1. A hydrogen producing device adapted to be mounted at an exhaust gas port of a vehicle , comprising:an outer housing having a surrounding wall which defines therein a heating chamber that has a primary intake port and a primary outlet port, said primary intake port being in communication with the exhaust gas port to permit exhaust gas and waste heat from the exhaust gas port to flow into said heating chamber and to be discharged through said primary outlet port;a reaction unit including an inner housing which is disposed in said heating chamber and which defines therein a reaction chamber that is not in communication with said heating chamber, and a catalyst member disposed in said reaction chamber; and a fuel introducing tube which has a first fuel end disposed in said heating chamber and in spatial communication with said reaction chamber, and which extends from said first fuel end and through said surrounding wall to terminate at a second fuel end for connection with a fuel supplying unit so as to introduce fuel from the fuel supplying unit to said reaction chamber,', 'an air introducing tube which has an air introducing segment extending through said surrounding wall and into said heating chamber for introduction of reaction air thereinto, a winding segment extending from said ...

BI-PHASIC CONTINUOUS-FLOW TUBULAR REACTOR AND HETEROGENEOUS CATALYSTS PREPARATION METHOD FOR PRODUCTION OF 5-HYDROXYMETHYL FURFURAL

Disclosed is a cost-effective process for catalytic conversion of simple C-based sugars (such as glucose and fructose) and industrial-grade sugar syrups derived from starch (such as different grades of High Fructose Corn Syrup) and cellulosic biomass to 5-HydroxyMethylFurfural (5-HMF) in a continuous-flow tubular reactor in bi-phasic media using inexpensive heterogeneous solid catalysts. Commercial and synthesized heterogeneous solid catalysts were used and their activities in terms of sugar conversion and HMF selectivity and yield were compared. Continuous dehydration of fructose, glucose and industrial-grade sugar syrups derived from corn and wood to HMF was achieved and the stability of selected catalysts and feasibility of catalyst recycling and regeneration were demonstrated. The performance of the catalysts and reactor system were examined under different operating conditions including reaction temperature, feeding flow rate, initial feedstock concentration, catalyst loading, presence of extracting organic solvent and phase transfer catalyst and aqueous to organic phase ratio. At the best operating conditions, HMF yield attained 60%, 45% and 53%, from dehydration of fructose, glucose and HFCS-, respectively. 1. A method for production of 5-hydroxymethyl furfural (5-HMF) from feedstock containing any one or combination of simple C-based sugars , industrial-grade sugar syrups and sugars derived from starch and/or cellulosic biomass , comprising:continuously flowing a bi-phasic reaction medium including water, an organic solvent and the feedstock through an elongate tubular reactor having located therein a packed-bed column of heterogeneous solid catalyst containing any one or combination of Brønsted acid sites and Lewis acid sites, the packed-bed column extending along a preselected length of the said elongate tubular reactor, the packed-bed column of heterogeneous solid catalyst having first and second opposed ends located within the tubular reactor;heating the ...

METHOD AND APPARATUS FOR PRODUCING HIGH PURITY PHOSGENE

In an embodiment, a method of producing phosgene in a tube reactor comprises introducing a feed comprising carbon monoxide and chlorine to a tube of the reactor, the tube having a particulate catalyst disposed therein, wherein a thermally conductive material separate from the tube contacts at least a portion of the particulate catalyst; to produce a product composition comprising phosgene, and carbon tetrachloride in an amount of 0 to 10 ppm by volume based on the volume of the phosgene. 1. A method of producing phosgene in a tube reactor , the method comprising:introducing a feed comprising carbon monoxide and chlorine to a tube of the reactor, the tube having a particulate catalyst disposed therein, wherein a thermally conductive material separate from the tube contacts at least a portion of the particulate catalyst;to produce a product composition comprising phosgene, and carbon tetrachloride in an amount of 0 to 10 ppm by volume based on the volume of the phosgene.2. The method of claim 1 , wherein the thermally conductive material comprises a coating disposed on at least a portion of an exterior surface of the particulate catalyst claim 1 , or a portion of an exterior surface of an agglomerate of the particulate catalyst claim 1 , or both.3. The method of claim 2 , wherein the coating has a coating thickness of 0.001 to 1 micrometer.4. The method of claim 1 , wherein the thermally conductive particulate material comprises a thermally conductive claim 1 , 3-dimensional mesh claim 1 , and wherein the mesh has openings and wherein the openings of the mesh have an average diameter larger than the average diameter of the particulate catalyst.5. The method of claim 1 , wherein the thermally conductive material comprises a particulate material distributed within and in contact with the particulate catalyst.6. The method of claim 1 , wherein the thermally conductive material comprises a doping material that is doped in the catalyst in an amount of greater than or equal ...

Packed-bed tubular reactor for heterogeneous exothermic or endothermic catalytic reactions

A reactor for Fischer-Tropsch reaction effected in a three-phase system essentially consisting of a gaseous reagent phase, a liquid reacted phase and a solid catalytic phase, wherein the solid catalytic phase is composed of packed bodies encaged in at least one open-cell foam structure with a high thermal conductivity.

ALKOXYLATION PROCESS USING TUBULAR REACTOR

Alkylene oxides are polymerized in a tubular reactor. The alkylene oxide is continuously introduced into the tubular reactor through multiple introduction points located along the length of the tubular reactor. Monomer flow rates are increased along the length of the reactor to maintain a nearly constant concentration of unreacted alkylene oxide. 1. A process for manufacturing a polyether by polymerizing at least one alkylene oxide in a tubular reactor having an inlet end and an outlet end , wherein an initiator composition containing at least one initiator compound and an alkylene oxide polymerization catalyst is continuously introduced into said inlet end and the polyether is continuously removed from the outlet end , wherein the tubular reactor includes at least one monomer feed section wherein at least one alkylene oxide is continuously introduced under polymerization conditions through multiple alkylene oxide ports arranged along the length of said monomer feed section to form a reaction mixture , the process being further characterized in that the concentration of unreacted alkylene oxide is maintained in the range 0.1 to 12 weight percent at each point along the length of the monomer feed section.2. The process of claim 1 , wherein the rate of addition of the alkylene oxide per unit length of the monomer feed section increases along the length of the monomer feed section in a downstream direction.3. The process of claim 2 , wherein the number of alkylene oxide injection ports in the monomer feed section is at least 50.4. The process of claim 2 , wherein the tubular reactor is separated from a reservoir of the alkylene oxide by a semi-permeable membrane claim 2 , and the alkylene oxide is introduced into the tubular reactor by passing through the semi-permeable membrane.5. The process of claim 2 , wherein the tubular reactor is disposed in a shell claim 2 , and heat of reaction is removed from the tubular reactor by passing a thermal fluid through the shell ...

Two-stage reactor for exothermal and reversible reactions and methods thereof

The present invention relates a two-stage reactor for exothermal, reversible reactions. In particular, the reactor contains a first semi-isothermal stage followed by a second cooling stage. The reactor allows for high conversion of products in an exothermal, reversible reaction.

Heat treatment device

A heat treatment device causing a first fluid and a second fluid to flow therethrough includes heat transfer bodies including first flow channels through which the first fluid flows and second flow channels through which the second fluid flows adjacent to the first flow channels without contact, and pipe-like members detachably placed in the first flow channels and each including a pipe wall having an outer wall surface conforming to a wall surface defining each first flow channel and an inner wall surface with which the first fluid comes into contact.

NOVEL METHODS AND RELATED TOOLS FOR CBD CONVERSION TO THC

The present invention is directed to methods of producing THC from CBD utilizing non-harsh methodology and resulting in substantially increased yields, as well as devices built upon these novel methods. The methods and devices are material efficient, and in certain embodiments, solvent-free. In particular, in certain embodiments, these methods and related devices are suitable for commercial production of THC from CBD. Furthermore, in certain embodiments, the present invention provides methods of producing THC from CBD in manner that affords tunability to select the ratio of THC-8 to THC-9.

METHOD FOR PRODUCING DEVULCANIZED RUBBER AND AN APPARATUS THEREFOR

A method for producing devulcanized rubber and an apparatus () therefor. The method for producing devulcanized rubber comprises the steps of (1) providing vulcanized rubber particles with a pre-determined particle size and (2) devulcanizing the vulcanized rubber particles. The vulcanized rubber particles are devulcanized mechanically by impact forces and devulcanized chemically by a chemical composition. The impact forces break sulphur- sulphur and sulphur-carbon bonds of the vulcanized rubber particles causing surfaces of the rubber to become receptive in reacting with the chemical composition and the chemical composition renders the sulphur passive to prevent reattachment of the bonds, of which the chemical composition comprises at least one accelerator, at least one inorganic activator and at least one organic activator. 132.-. (canceled)33. A method for producing devulcanized rubber comprising the steps of:a) providing vulcanized rubber particles with a pre-determined particle size; andb) devulcanizing the vulcanized rubber particles,wherein the vulcanized rubber particles are devulcanized mechanically by impact forces and devulcanized chemically by a chemical composition, whereby the impact forces break sulphur-sulphur and sulphur-carbon bonds of the vulcanized rubber particles causing surfaces of the rubber to become receptive in reacting with the chemical composition and the chemical composition renders the sulphur passive to prevent reattachment of the bonds, of which the chemical composition comprises at least one accelerator, at least one inorganic activator and at least one organic activator, andwherein the method for producing devulcanized rubber further comprises a step of introducing clay.34. The method for producing devulcanized rubber as claimed in claim 33 , wherein the method further comprising a step of introducing a plasticizer to the devulcanized rubber.35. The method for producing devulcanized rubber as claimed in claim 34 , wherein the ...

DEVICE AND METHOD FOR CLEANING PRODUCER GAS USING A MICROWAVE INDUCED PLASMA CLEANING DEVICE

A device and method for cleaning producer gas includes a filter bed housing and a microwave chamber. The filter bed housing comprises an inlet for carbon-based material and a spent carbon outlet. The microwave chamber comprises a permeable top and wave guides around the perimeter through which microwaves can be introduced into the device using magnetrons. The method comprises using the device by filling the filter bed housing with carbon-based material, introducing microwaves into the microwave chamber using the magnetrons and wave guides, passing the gas through carbon-based material in the filter bed chamber, the microwave chamber, the gas permeable top and the gas outlet. 2. The device of claim 1 , wherein the conduit is in the shape of a sideways “T′.3. The device of claim 1 , wherein the conduit is a wave guide.4. The device of claim 1 , further comprising a wave guide connected to the conduit.5. The device of claim 1 , further comprising an unobstructed path for microwaves to enter the microwave chamber from the magnetron claim 1 , wherein the conduit is a sideways T-shaped conduit so that when the device is operated claim 1 , the first catalytic chamber is outside the path of microwaves being directed through the conduit.6. The device of claim 1 , further comprising at least one elbow shaped wave guide attached to the conduit that allows for the magnetron to be positioned horizontally with respect to a vertical orientation of the microwave chamber.7. The device of claim 1 , further comprising multiple wave guides connected to the conduit.8. The catalytic chamber of claim 1 , further comprising microwave absorbing material in the catalytic chamber.9. The device of claim 8 , wherein the microwave absorbing material of the catalytic chamber comprises ceramic tiles impregnated with a material that catalyzes conversion of microwave energy into heat energy.10. The catalytic chamber of claim 1 , further comprising ceramic tiles vertically aligned claim 1 , parallel ...

SYSTEM FOR GENERATING H2S IN AN ALKALINE MEDIUM AND METHOD OF USING THE SAME

Method of producing hydrogen sulfide in an alkaline environment. A mixture having a sodium salt, elemental sulfur (S) and water is added to a reactor for the purpose of generating hydrogen sulfide (HS) gas as the main product and sodium sulfate (NaSO) as a byproduct. 1. A method for producing hydrogen sulfide (HS) gas , the method comprising:placing elemental sulfur and a sodium salt solution comprising a sodium salt in water in a reaction vessel;{'sub': 2', '2', '4, 'reacting the elemental sulfur with the sodium salt solution to form hydrogen sulfide (HS) and sodium sulfate (NaSO);'}{'sub': 2', '4, 'removing the formed NaSOfrom the reaction vessel;'}{'sub': 2', '4, 'crystallizing the NaSOusing a crystallizer;'}{'sub': 2', '4', '2, 'reducing the crystallized NaSOto produce NaS;'}{'sub': 2', '2, 'forming a NaS solution with the produced NaS;'}{'sub': '2', 'placing elemental sulfur and the NaS solution in the reaction vessel; and'}{'sub': '2', 'reacting the elemental sulfur with the NaS solution to form hydrogen sulfide and sodium sulfate.'}2. The method of claim 1 , wherein the reaction vessel is pressurized to a pressure ranging from about 500 psi to about 1500 psi and heated to a temperature ranging from about room temperature to about 400° C.3. The method of claim 1 , wherein the reaction vessel is pressurized to a pressure ranging from about 500 psi to about 700 psi and heated to a temperature ranging from about 200° C. to about 300° C.4. The method of claim 1 , further comprising:pressuring the reaction vessel to a pressure of about 600 psi; orheating the reaction vessel to a temperature ranging from about 230° C. to about 240° C.5. The method of claim 1 , further comprising agitating the elemental sulfur and the sodium salt solution in the reaction vessel.6. The method of claim 1 , wherein the crystallized NaSOis reduced to produce NaS by a carbothermal reduction system.7. The method of claim 1 , further comprising reacting the formed hydrogen sulfide with an ...

METHOD OF STEAM METHANE REFORMING

A convectively heated steam/methane reformer having a shell and tube reforming reactor for hydrogen production. A reactor core containing the reactants is convectively heated by hot air flowing through the shell or annulus of the reactor. Heated air is supplied to the reactor through several fluid inlets on the shell side of the reformer. 1. (canceled)2. The method of claim 13 , wherein the plurality of hot fluid inlets further comprise an adjustable valve that opens or closes to maintain temperature stability inside the shell side annulus.3. The method of claim 13 , wherein the adjustable valve may be opened or closed at an angle ranging from 0°-90°.4. The method of claim 13 , wherein the plurality of not fluid inlets are positioned at an angle ranging from 45°-90° to the shell side of the reformer.5. The method of claim 13 , wherein the hot air outlet is positioned on the perimeter of the shell.6. The method of claim 13 , wherein the hot air outlet is positioned on the surface of the shell.7. The method of claim 13 , wherein the shell side annulus is a single zone with no baffles.8. The method of claim 13 , wherein the healing medium is selected front the group consisting of air claim 13 , nitrogen claim 13 , helium claim 13 , and combinations thereof.9. The method of claim 13 , wherein the solid catalyst is nickel and/or magnesium aluminate.10. The method of claim 13 , wherein the plurality of hot fluid inlets are disposed in two groups each spirally positioned to wrap around the circumference of the shell side of the tube and shell reactor.11. The method of claim 10 , wherein the two groups of the plurality of hot fluid inlets are disposed on opposite sides of the shell side of the tube and shell reactor.12. The method of claim 13 , wherein the plurality of hot fluid inlets are tubular extensions from the surface of the shell side of the tube and shell reactor.13. A method for converting methane to hydrogen gas claim 13 , comprising:heating a shell side annulus ...

Tungsten Hexafluoride Production Method

According to the present invention, there is provided a method of producing tungsten hexafluoride by reacting tungsten with a fluorine-containing gas at a temperature of 800° C. or higher. The method according to the present invention is advantageous in that the amount of production of the tungsten hexafluoride per unit capacity of the reaction vessel is increased as compared to conventional techniques of producing tungsten hexafluoride from a fluorine-containing gas and metal tungsten while controlling the reaction temperature to 400° C. or lower. It is preferable that the reaction vessel is equipped with a coolant jacket for maintaining an inner wall temperature of the reaction vessel at 400° C. or lower. 110.-. (canceled)11. A production method of tungsten hexafluoride , comprising: forming tungsten hexafluoride by reaction of tungsten with a fluorine-containing gas in a reaction vessel ,wherein the reaction vessel is equipped with a coolant jacket, andwherein the reaction is performed in the reaction vessel at a reaction temperature of 800° C. or higher while an inner wall temperature of the reaction vessel is maintained at a temperature of 400° C. or lower by the coolant jacket.12. The production method of tungsten hexafluoride according to claim 11 , wherein the fluorine-containing gas is either one or both of fluorine gas and nitrogen trifluoride gas.13. The production method of tungsten hexafluoride according to claim 11 , wherein the fluorine-containing gas is undiluted fluorine gas.14. The production method of tungsten hexafluoride according to claim 11 , wherein the tungsten is filled in the form of a fixed bed in the reaction vessel.15. The production method of tungsten hexafluoride according to claim 11 , wherein the reaction temperature is in a range of 1200° C. to 2000° C.16. The production method of tungsten hexafluoride according to claim 11 ,wherein a coolant flowing through the coolant jacket is water, and{'sup': '2', 'wherein a film coefficient ...

APPARATUS FOR ENDOTHERMIC REACTIONS

A carbonaceous feed pyrolysis apparatus is provided including two or more hot particle fluidised beds, one of which contains a combustion zone, and one or more positive displacement apparatus for the transfer of hot particles beds. Also provided is a bio-oil production process including two or more fluidised beds, a first combustion zone carried out in one or more combustion fluidised beds in which a particulate material is fluidised and heated, and a second pyrolysis zone carried out in one or more pyrolysis fluidised beds in which hot particles heated in the combustion zone are used for pyrolysis of bio-mass, the combustion zone being operated at or about atmospheric pressure at a temperature of from 400° C. to 1100° C., and the pyrolysis zone being operated at a pressure of from atmospheric to 100 Barg at a temperature of from 400° C. to 900° C. 120-. (canceled)30. An endothermic reaction process , comprising: two or more fluidized bed zones comprising a first fluidized bed zone and a second fluidized bed zone;', 'a second fluidized bed zone gas feed comprising a closed gas loop configured such that, in use, a portion of a gas produced in the second fluidized bed zone is recycled in the closed gas loop to the first fluidized bed zone, such that the recycled gas is used as a gaseous fuel for the first fluidized bed zone, either fully or in part;', 'an apertured divider having one or more apertures therethrough connecting at least two of the fluidized bed zones;', 'a mass transfer device for transferring particulate matter from at least one fluidized bed zone to an other fluidized bed zone;', 'a gas loop purge configured such that, in use, a part of the recycled gas stream from the second fluidized bed zone is purged from the closed gas loop; and', 'a flow rate regulator configured to, in use, regulate a flow rate to a predeterminable rate;, 'providing an endothermic reaction apparatus, comprisingcombusting a carbonaceous material in a presence of oxygen in a hot ...

CHEMICAL REACTOR WITH ADIABATIC CATALYTIC BEDS AND AXIAL FLOW

Axial reactor for exothermic or endothermic chemical reactions, comprising at least a first catalytic bed () and a second catalytic bed () operating in series and at least one heat exchanger () between the two catalytic beds, wherein the first catalytic bed has a collector bottom () having a box-like structure with flat and parallel walls, which are gas-permeable, and a plurality of parallel channels () defined between the walls, wherein a first series of said channels collects the gaseous flow exiting the catalytic bed and passing through the first wall, said gaseous flow is directed towards the heat exchanger, and the flow exiting the exchanger is directed towards the second catalytic bed via a second series of said channels of the collector bottom. 115-. (canceled)16. A reactor for carrying out exothermic or endothermic chemical reactions , the reactor comprising:an axial stack of catalytic beds including at least a first catalytic bed and a second catalytic bed operating in series with axial flow, the first and second catalytic beds being stacked one next to the other in an axial direction of the reactor, wherein a gaseous flow exiting the first catalytic bed is subjected to a further reaction stage in the second catalytic bed; andat least one heat exchanger located sideways relative to the axial stack of catalytic beds, said at least one heat exchanger being arranged to cool or heat, via indirect heat exchange with a heating or cooling medium, said gaseous flow exiting the first catalytic bed before entry into the second catalytic bed;wherein the first catalytic bed has a collector bottom having a box-like structure, including a first wall and a second wall spaced and parallel with respect to each other, and a plurality of parallel channels that are defined between said first and second walls;wherein said first wall is exposed to the gaseous flow exiting the first catalytic bed, and the second wall communicates with a gas inlet of the second catalytic bed, and ...

METHODS AND RELATED TOOLS FOR CBD CONVERSION TO THC

The present invention is directed to methods of producing THC from CBD utilizing non-harsh methodology and resulting in substantially increased yields, as well as devices built upon these novel methods. The methods and devices are material efficient, and in certain embodiments, solvent-free. In particular, in certain embodiments, these methods and related devices are suitable for commercial production of THC from CBD. Furthermore, in certain embodiments, the present invention provides methods of producing THC from CBD in manner that affords tunability to select the ratio of THC-8 to THC-9. 2. The material-efficient method of claim 1 , wherein the THC produced in the accelerated conversion environment is produced with enhanced conversion efficiency of the CBD with greater than 75% efficiency.3. The material-efficient method of claim 1 , wherein the THC produced in the accelerated conversion environment is greater than 80% pure.4. The material-efficient method of claim 1 , wherein the THC produced in the accelerated conversion environment is 500 g or greater.6. A tetrahydrocannabinol (THC) production device comprising:a vessel for containing acidicly enriched solid support particles; anda plurality of CBD-activated acidicly enriched solid support particles positioned inside the vessel, wherein THC is produced from the CBD-activated acidicly enriched solid support particleswherein the THC is produced at an enhanced rate.7. The THC production device of claim 6 , wherein the heating source is a heating jacket.8. The THC production device of claim 6 , further comprising a means for extraction of the THC from the acidicly enriched solid support particles in the vessel.9. The THC production device of claim 6 , wherein 500 g or greater of THC may be produced in a single use of the device.10. The THC production device of claim 6 , wherein the THC is produced with enhanced conversion efficiency of the CBD with greater than 75% efficiency.11. The THC production device of claim ...

Heat Transfer Baffle System and Uses Thereof

This disclosure describes an improved heat transfer system for use in reaction vessels used in chemical and biological processes. In one embodiment, a heat transfer baffle comprising two sub-assemblies adjoined to one another is provided. 1. A heat transfer baffle comprising at least one distribution channel and at least one relief channel.222-. (canceled) This application claims priority to U.S. Ser. No. 61/240,029 filed Sep. 4, 2009.This disclosure relates to equipment utilized to manufacture chemical agents, particularly biopharmaceuticals.This disclosure relates to equipment having reaction vessels used to manufacture chemical and/or biological products such as biopharmaceuticals. For instance, fermentors commonly provide a reaction vessel for cultivation of microbial organisms or mammalian, insect, or plant cells to produce such products. It is important to control the temperature of the reaction to ensure optimal production of the product. For example, fermentations typically produce excess heat that must be dissipated or removed from the system to ensure proper reaction conditions. Those of skill in the art have suggested various systems for controlling the temperature within reaction vessels, as briefly reviewed below. However, there remains a need in the art for improved heat control systems that also incorporates the use of sanitary material surfaces, such as that provided herein.Previously available systems are described in several U.S. and foreign patents. For instance, U.S. Pat. No. 2,973,944 (Etter, et al.) describes a system of “individual coil units” that each contain a group of tubes that serve as heat transfer elements in a reaction vessel. The units are indirectly affixed to the inner part of the vessel using bracing members located at the top, bottom, and/or throughout the length of each unit. The '944 patent points out that an advantage of such indirect attachment is that the expansion and contraction units during will not damage the reactor ...

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.

Process and system for production of dichlorine

The present disclosure provides a process and a system for producing dichlorine (Cl 2 ).

Reactors for separating wax products from lightweight gaseous products of a reaction

A reactor for hydrocarbon production that separates wax reaction products from lightweight gaseous reaction products. The reactor has a housing, a catalyst bed, a product recovery zone, and a stripping zone. The catalyst bed can be provided in multi-tubular and other fixed bed configurations. The stripping zone receives light-weight gas reaction products from the product recovery zone, while a gas outlet of the housing receives non-lightweight gaseous hydrocarbon reaction products from the product recovery zone. A wax outlet of the housing receives wax products from the product recovery zone.

MULTI-TUBULAR REACTOR AND MULTI-TUBULAR REACTOR DESIGN AND FABRICATION METHOD

A multi-tubular reactor () comprising a cylindrical shell (), a plurality of reaction tubes () located in the shell, and a disk-and-doughnut type baffle (), wherein

APPARATUS FOR PRODUCING WATER-ABSORBING RESIN PARTICLES

An apparatus for producing water-absorbing resin particles for which surface cross-linking treatment is conducted, the surface cross-linking treatment being conducted by spraying a surface cross-linking agent to a water-absorbing resin particle precursor and heating the agent and the precursor, the apparatus includes a treatment container in which the surface cross-linking treatment is conducted, a stirring device including a stirring member disposed in the treatment container, a heating device that heats an inside of the treatment container; and a spray nozzle disposed in the treatment container, the spray nozzle spraying into the treatment container the surface cross-linking agent supplied from a surface cross-linking agent supply source in an exterior of the treatment container through a supply pipe. In a flow path in the spray nozzle spanning from an entrance of the spray nozzle to a spray exit, a point whose opening cross-section is smallest in a flow path through which a fluid passes is the spray exit. A product with further stable physical properties can thereby be acquired. 1. A method for producing water-absorbing resin particles , the method comprising a surface cross-linking treatment being conducted by spraying a surface cross-linking agent to a water-absorbing resin particle precursor and heating the agent and the precursor , the water-absorbing resin particle precursor including unreacted monomers , whereinthe surface cross-linking treatment is conducted by an apparatus for producing water-absorbing resin particles, andthe apparatus includes:a treatment container in which the surface cross-linking treatment is conducted;a stirring device including a stirring member disposed in the treatment container;a heating device that heats an inside of the treatment container;a decompressing device that reduces a pressure in the treatment container; anda spray nozzle disposed in the treatment container, the spray nozzle spraying into the treatment container the ...

METHOD OF PREPARING CORE-SHELL PARTICLES

A method of manufacturing core-shell particles comprises: filling a buffer into a rotor, which is extended in a longitudinal direction, and is accommodated so as to be spaced apart from an inner wall side of a non-rotational hollow cylinder extended in a longitudinal direction and then discharging air to outside; rotating the rotor after terminating the filling; forming a core-shell precursor by supplying raw materials from a first storage and a second storage, which comprise a material forming a core, into an interior of the cylinder in which the rotor rotates; supplying a shell material for coating the core to the interior of the cylinder in which a core-type precursor is formed; separating a liquid comprising core-shell particles formed through the supplying into a solid and a liquid; and drying the core-shell particles obtained through the separating. 1. A method of manufacturing core-shell particles , the method comprising:filling a buffer into a rotor, which is extended in a longitudinal direction, and is accommodated so as to be spaced apart from an inner wall side of an non-rotational hollow cylinder extended in a longitudinal direction and then discharging air to outside;rotating the rotor after terminating the filling;forming a core-shell precursor by supplying raw materials from a first storage and a second storage, which comprise a material forming a core, into an interior of the cylinder in which the rotor rotates;supplying a shell material for coating the core to the interior of the cylinder in which a core-type precursor is formed;separating a liquid comprising core-shell particles formed through the supplying into a solid and a liquid; anddrying the core-shell particles obtained through the separating.2. The method according to claim 1 , wherein as the liquid comprising the core-shell particles separated at the separating claim 1 , a reactant in a normal state within the reactor is used.3. The method according to claim 1 , wherein lithium chloride ...

Apparatus And Process For The Production Of Formaldehyde

An apparatus for the production of formaldehyde is disclosed. The apparatus comprises a cooled tubular reactor section () having a first inlet, a first outlet and a plurality of tubes each having a first end in fluid communication with the first inlet and a second end in fluid communication with the first outlet. The plurality of tubes contain a first catalyst for the production of formaldehyde by oxidative dehydrogenation. The apparatus is characterised in that the apparatus further comprises a pre-reactor section (). The pre-reactor section () has an inlet. The pre-reactor section () has an outlet in fluid communication with the first inlet of the cooled tubular reactor section (). The pre-reactor section () is configured to contain, in use, an adiabatic catalyst bed. The adiabatic catalyst bed comprises a second catalyst for the production of formaldehyde by catalytic oxidative dehydrogenation. 1. An apparatus for the production of formaldehyde , the apparatus comprisinga cooled tubular reactor section having a first inlet, a first outlet, and a plurality of tubes each having a first end in fluid communication with the first inlet and a second end in fluid communication with the first outlet, the plurality of tubes configured to contain, in use, a first catalyst for the production of formaldehyde by catalytic oxidative dehydrogenation, a pre-reactor section having an inlet, and having an outlet in fluid communication with the first inlet of the cooled tubular reactor section, the pre-reactor section being configured to contain, in use, an adiabatic catalyst bed comprising a second catalyst for the production of formaldehyde by catalytic oxidative dehydrogenation.2. The apparatus according to claim 1 , wherein the cooled tubular reactor section further comprises a shell surrounding the plurality of tubes and having at least one second inlet and at least one second outlet for passing heat transfer fluid through the shell in use.3. The apparatus according to claim 1 ...

METHOD AND SYSTEM FOR CARRYING OUT AN EXOTHERMIC GAS PHASE REACTION ON A HETEROGENEOUS PARTICULATE CATALYST

The invention relates to a method for producing 1,3 butadien by means of the oxidative dehydration of n-butenes on a heterogenous particulate multimetal oxide catalyst which contains molybdenum as the active compound and at least one other metal and which is filled into the contact tubes (KR) of two or more tube bundle reactors (R-I, R-II), wherein a heat transfer medium flows around the intermediate space between the contact tubes (KR) of the two or more tube bundle reactors (R-I, R-II). The method includes a production mode and a regeneration mode which are carried out in an alternating manner. In the production mode, an n-butene-containing feed flow is mixed with an oxygen-containing gas flow and conducted as a supply flow () over the heterogenous particulate multimetal oxide catalyst filled into the contact tubes (KR) of the two or more tube bundle reactors (R-I, R-II), and the heat transfer medium absorbs the released reaction heat, minus the heat quantity used to heat the supply flow () to the reaction temperature in the production mode, by means of an indirect heat exchange and completely or partly dispenses the reaction heat onto a secondary heat transfer medium (H2Oliq) in an external cooler (SBK). In the regeneration mode, the heterogenous particulate multimetal oxide catalyst is regenerated by conducting an oxygen-containing gas mixture () over the catalyst and burning off the deposits accumulated on the heterogenous particulate multimetal oxide catalyst. The invention is characterized in that the two or more tube bundle reactors (R-I, R-II) have a single heat transfer medium circuit and as many of the two or more tube bundle reactors (R-I, R-II) as necessary are operated constantly in the production mode so that the released reaction heat, minus the heat quantity used to heat the supply flow () to the reaction temperature in the production mode, suffices to keep the temperature of the heat transfer medium in the intermediate spaces between the content ...

REACTOR JACKET DESIGN

Reactor systems, reactor coolant systems, and associated processes for polymerizing polyolefins are described. The reactor systems generally include a reactor pipe and a coolant system, in which the coolant system includes a jacket pipe surrounding at least a portion of the reactor pipe to form an annulus therebetween, at least one spacer coupling the jacket to the reactor pipe, and a coolant which flows through the annulus to remove heat from the reactor pipe. At least one of the external surface of the reactor pipe, the internal surface of the jacket, and at least one spacer, are independently modified, for example by polishing, coating, or reshaping, to reduce the fluid resistance of the coolant flow through the annulus. 1. A reactor system comprising:a reactor pipe having an external surface characterized by an unmodified surface roughness; and a jacket having an internal surface characterized by an unmodified surface roughness, the jacket spaced apart from and surrounding at least a portion of the reactor pipe to form an annulus between the internal surface of the jacket and the external surface of the reactor pipe,', 'a coolant which flows through the annulus to remove heat from the reactor pipe, and', 'at least one spacer having a leading edge and a trailing edge with respect to the coolant flow and characterized by an unmodified surface roughness, the spacer coupling the jacket to the reactor pipe;, 'a coolant system, the coolant system comprising'}wherein the external surface of the reactor pipe, the internal surface of the jacket, the at least one spacer, or any combination thereof are independently modified to reduce the fluid resistance of the coolant flow through the annulus.2. The reactor system of claim 1 , wherein the external surface of the reactor pipe claim 1 , the internal surface of the jacket claim 1 , the at least one spacer claim 1 , or any combination thereof are independently modified by polishing or by coating with a friction-reducing ...

DEVICE FOR POWDER METERING FOR CHEMICAL PRODUCTION PROCESSES UNDER CLEAN-ROOM CONDITIONS, USE THEREOF AND METERED ADDITION METHOD

Device for metering powder, in particular in clean-rooms, which includes a vessel containing powder and a sealing head with a septum for the vessel, wherein the sealing head is connectable powder-tight with the vessel and the septum powder-tight with the sealing head and the device further includes a vessel holder, which serves to hold the sealing head of the vessel, and the vessel with its opening points downwards, so that the powder can flow out of the vessel, wherein a gap is provided between the sealing head and a holding bowl of the vessel holder, in which a gas flow between the holding bowl and the sealing head can be created. The invention also relates to a use of the device and a metered addition method. 1. Device for metering powder , which comprises a vessel containing powder and a sealing head with a septum for the vessel , and the vessel points downwards with its opening , so that the powder can flow out of the vessel , and the device further has a vessel holder , which serves to hold the sealing head of the vessel , wherein the vessel holder has a cannula for piercing the septum and a gas for fluidizing the downward-flowing powder is fed to the cannula , and further a metering system is provided , which is based on the filling of a volume in a connecting hose separable by valves , wherein the bulk density of the powder in the connecting hose is kept essentially constant by a gas flow varying with time during the fluidization.2. Device according to claim 1 , wherein the gas volume of the fluidization amounts to between 0.3 and 3.0 times claim 1 , preferably between 0.5 and 2.0 times the separable volume in the connecting hose and/or the gas flow is greatest at the end of the fluidization.3. Device according to claim 1 , wherein the sealing head is connectable powder-tight with the vessel and the septum with the sealing head claim 1 , and wherein a gap is present between the sealing head and a holding bowl of the vessel holder claim 1 , in which a gas ...

VORTEX MIXING APPARATUS AND METHOD OF USE THEREOF

An apparatus comprising: a vessel component comprising a flow-through interior chamber having an interior sidewall and an exterior sidewall; at least two inlets for introducing chemical components into the flow-through interior chamber; at least one outlet for removing product from the flow-through interior chamber; and an off center rotation component which is operatively connected to the vessel component. During operation of the apparatus, the off center rotation component generates vortical movement of at least two chemical components through the flow-through interior chamber of the vessel, and converts at least a portion of the at least two chemical components to at least one reaction product or product mixture. A method of using the apparatus to produce reaction products or product mixtures. The apparatus and method are useful for producing specialty chemicals such as fragrance and flavor compounds, insect pheromones, petrochemicals, pharmaceutical compounds, agrichemical compounds, and the like. 1. A method comprising: a vessel component comprising a flow-through interior chamber having an interior sidewall and an exterior sidewall;', 'at least two inlets for introducing chemical components into the flow-through interior chamber; wherein the at least two inlets are operatively connected to a bottom portion of the flow-through interior chamber; and', 'at least one outlet for removing product from the flow-through interior chamber;, 'providing an apparatus comprisingintroducing through the at least two inlets, at least two chemical components into the flow-through interior chamber of the vessel component;generating vortical movement of the at least two chemical components through the flow-through interior chamber of the vessel component by an external oscillatory surface; andconverting at least a portion of the at least two chemical components to at least one reaction product or product mixture.2. The method of wherein the external oscillatory surface is ...

Production method for trichlorosilane, and pipe

To prevent solidified aluminum chloride from adhering to and accumulating on a pipe and also prevent stress-corrosion cracking in the pipe, a method for producing trichlorosilane includes a cooling step of cooling a discharge gas that is discharged from a fluidized-bed reactor and that contains the trichlorosilane, the cooling step involving causing a fluid to flow through a space ( 4 ) inside a side wall ( 3 ) of a pipe ( 10 ), the pipe being a pipe for discharging the discharge gas from the fluidized-bed reactor, in such a manner that the side wall ( 3 ) has a surface ( 1 a ) having a temperature of not lower than 110° C.

Reactor systems and processes for using the same

circulating fluidized bed reactor

Method of modifying near-wall temperature in a gas phase polymerization reactor

A falling film of water is applied around the periphery of a fluid bed olefin polymerization reactor to cool the wall and reduce the temperature in the fluid bed near the inside surface of the wall. Cooling has the effect of reducing static in the reactor, which in turn ameliorates a sheeting problem and can enhance production by facilitating control of the relation of the reactor temperature and the dew point of recycled gas. The process may be used concurrently with a gas cooling and condensing recycle system wherein at least some of the condensed recycle gas is injected in the vicinity of the internal wall surface.

Loop reactor with varying diameter for olefin polymerization

Process for polymerizing at least one olefinic monomer in a loop reactor at from 20 to 150°C, but below the melting point of the polymer to be formed, and a pressure of from 5 to 100 bar, where the polymer formed is present in a suspension in a liquid or supercritical suspension medium and this suspension is circulated by means of an axial pump, wherein the loop reactor comprises a cyclic reactor tube whose diameter varies by at least 10%, based on the predominant reactor tube diameter, and in which there is at least one widening and narrowing in a region other than that of the axial pump.

Method and apparatus for preparing and supplying catalyst slurry to a polymerisation reactor.

The present invention relates to an apparatus for preparing and supplying catalyst to an ethylene slurry loop polymerisation reactor and to an apparatus for controlling the injection of catalyst slurry in a polymerization reactor wherein polyethylene is prepared. The present invention a Iso relates to a method for optimising catalyst supply to a polymerisation reactor. The diluted catalyst is transferred to the reactor (1) using a membrane pump (5) controllable in function of the concentration of a reactant in said reactor (1).

Vapor phase reactor off-gas recycle system for use in the vapor state polymerization of monomers

An essentially total reactor off-gas recycle process essentially isobaric in nature is herein disclosed for use in polymerizations wherein a polymerizable monomer or a mixture thereof is polymerized in a vapor state polymerization process using a stirred-bed, quench-cooled, horizontal reactor.

Método e aparelho para preparar e fornecer suspensão catalítica a um reactor de polimerização.

Process for producing polyolefins

Loop reactor

Method for monitoring a polymerization reaction

In some embodiments, a method of monitoring a resin-producing polymerization reaction in a fluid bed reactor system to generate reaction parameter data in on-line fashion, wavelet transforming the reaction parameter data to generate frequency-domain data or determining kurtosis of each of at least two subsets of the reaction parameter data, and optionally also determining from the frequency-domain data or kurtosis values an indication of at least one of degree of resin stickiness, an approach to or imminence of resin stickiness, and an approach to or imminence of an unsafe or undesired reactor operating condition that can result in sheeting or chunking. Optionally also, the reaction is controlled in response to the kurtosis values or frequency-domain data, for example, in an effort to prevent the occurrence of sheeting or another discontinuity event or to maintain the reactor in a stable, non-sticking condition.

オレフィンの気相重合法

Systems and processes for storing resin

Improved systems and processes for storing resins are disclosed herein. These systems and processes are especially useful for reducing the tendency of resins to sinter. In polymerization processes, the improvements disclosed herein can reduce the tendency of resins to sinter while also allowing downstream operations to continue.

気相重合反応装置内の近壁温度を変える方法

(57)【要約】 【課題】 反応装置の外側に水を適用することによって 気相重合反応装置の内壁近くの温度を低下させる方法を 提供する。 【解決手段】 落下水のフィルムを流動床オレフィン重 合反応装置の周囲の回りに適用して壁を冷却しかつ流動 床内の壁の内面近くの温度を低下させる。冷却は、反応 装置内の静電気を低減させる効果を有する、これは、立 ち代わって、反応装置温度と循環ガスの露点との関係の 調節を容易にすることによってシーチング問題を改善し かつ生産を高めることができる。プロセスは、凝縮され た循環ガスの少なくともいくらかを内壁表面の付近に注 入するガス冷却及び凝縮系と協働して用いることができ る。

METHOD AND DEVICE FOR CONTROLLING THE SUPPLY OF CATALYST SLUDGE INTO A POLYMERIZATION REACTOR

Methods for supplying solid catalysts to a solution polymerization reactor

Disclosed is a solution polymerization process, or, alternatively, a method of delivering powder catalysts to a solution polymerization reactor, comprising combining a homogeneous single-site catalyst precursor with α-olefin monomers to form a polyolefin, wherein the homogeneous single-site catalyst precursor is in the form of (i) a dry powder, (ii) suspended in a aliphatic hydrocarbon solvent, or (iii) suspended in an oil or wax, wherein the homogeneous single-site catalyst precursor is at a concentration greater than 0.8 mmole/liter when suspended in the aliphatic hydrocarbon solvent prior to entering the solution polymerization reactor.

Energy efficient polyolefin process

Catalyst injection for Ziegler polymerization

The fouling of the solid cocatalyst inlet nozzle in alpha-olefin Ziegler type polymerizations in stirred liquid phase, mass reaction is eliminated by positioning the inlet nozzle below the liquid surface on substantially the same horizontal plane as the bottom impeller and aligned with the impeller. The inlet nozzle extends from 30 to 80% of the distance between the wall of the reactor and the tip of the impeller. The ratio of the inlet velocity of the solid cocatalyst slurry to the reactor mass cross flow velocity is 2-3:1.

Method and apparatus for adjusting and supplying catalyst slurry to polymerization reactor

Reactor systems and processes for using the same

A process for the polymerization of olefin's, including: introducing an olefin and a polymerization catalyst into a polymerization reactor to form a polyolefin, the polymerization reactor including: a fluidized bed region having a top and a bottom; and a motive bed region; wherein a first end of the motive bed region is fluidly connected to the top of the fluidized bed region; and wherein a second end of the motive bed region is fluidly connected to the bottom of the fluidized bed region; and wherein a diameter of the fluidized bed region is greater than a diameter of the motive bed region; circulating at least a portion of the olefin, the catalyst, and the polyolefin through the fluidized bed region and the motive bed region; maintaining a dense-phase fluidized bed within the fluidized bed region; recovering polyolefin from the fluidized bed region, is provided. A reactor system directed to the process is also provided.

Circulating fluidized bed reactor

A continuous gas phase circulating bed reactor, including: a riser for contacting a catalyst and a first gas composition comprising an olefin to form a polyolefin under fast-fluidization regime or a dilute-phase pneumatic conveying regime conditions; a downer for contacting the catalyst and a second gas composition comprising an olefin to form additional polyolefin under fast fluidization regime or a dilute-phase pneumatic conveying regime conditions; and a transport section for conveying at least a portion of the catalyst, polyolefin, and additional polyolefin from the downer to the riser. Also disclosed is a polymerization process using such a circulating bed reactor.

Ethylene separation with temperature swing adsorption

A process for component separation in a polymer production system, comprising (a) separating a polymerization product stream into a gas stream and a polymer stream, (b) contacting the polymer stream with a purge gas to yield a purged polymer and a spent purge gas comprising purge gas, ethylene, and ethane, (c) contacting the spent purge gas with a temperature swing adsorber contactor (TSAC) to yield a loaded TSAC, wherein at least a portion of the ethylene is adsorbed by the TSAC at a first temperature to yield TSAC-adsorbed ethylene, wherein a portion of the ethane is adsorbed by the TSAC at the first temperature to yield TSAC-adsorbed ethane, (d) heating the loaded TSAC to a second temperature to yield a regenerated TSAC, and (e) contacting the regenerated TSAC with a sweeping gas stream to yield a recovered adsorbed gas stream comprising sweeping gas, recovered ethylene and recovered ethane.

Ethylene separation with temperature swing adsorption

A process for component separation in a polymer production system, comprising (a) separating a polymerization product stream into a gas stream and a polymer stream, (b) contacting the polymer stream with a purge gas to yield a purged polymer and a spent purge gas comprising purge gas, ethylene, and ethane, (c) contacting the spent purge gas with a temperature swing adsorber contactor (TSAC) to yield a loaded TSAC, wherein at least a portion of the ethylene is adsorbed by the TSAC at a first temperature to yield TSAC-adsorbed ethylene, wherein a portion of the ethane is adsorbed by the TSAC at the first temperature to yield TSAC-adsorbed ethane, (d) heating the loaded TSAC to a second temperature to yield a regenerated TSAC, and (e) contacting the regenerated TSAC with a sweeping gas stream to yield a recovered adsorbed gas stream comprising sweeping gas, recovered ethylene and recovered ethane.

Method of modifying near-wall temperature in a gas phase polymerization reactor

A falling film of water is applied around the periphery of a fluid bed olefin polymerization reactor to cool the wall and reduce the temperature in the fluid bed near the inside surface of the wall. Cooling has the effect of reducing static in the reactor, which in turn ameliorates a sheeting problem and can enhance production by facilitating control of the relation of the reactor temperature and the dew point of recycled gas. The process may be used concurrently with a gas cooling and condensing recycle system wherein at least some of the condensed recycle gas is injected in the vicinity of the internal wall surface.

Energy efficient polyolefin process

A manufacturing process for producing polyolefin, having a feed system, a reactor system including at least one polymerization reactor, a diluent/monomer recovery system, a fractionation system, and an extrusion/loadout system having an extruder. The manufacturing process is configured to consume less than 325 kilowatt-hours of electricity per metric ton of polyolefin produced.

Reactor Systems and Processes for Using the Same

A process for the polymerization of olefin's, including: introducing an olefin and a polymerization catalyst into a polymerization reactor to form a polyolefin, the polymerization reactor including: a fluidized bed region having a top and a bottom; and a motive bed region; wherein a first end of the motive bed region is fluidly connected to the top of the fluidized bed region; and wherein a second end of the motive bed region is fluidly connected to the bottom of the fluidized bed region; and wherein a diameter of the fluidized bed region is greater than a diameter of the motive bed region; circulating at least a portion of the olefin, the catalyst, and the polyolefin through the fluidized bed region and the motive bed region; maintaining a dense-phase fluidized bed within the fluidized bed region; recovering polyolefin from the fluidized bed region, is provided. A reactor system directed to the process is also provided.

Circulating Fluidized Bed Reactor

A continuous gas phase circulating bed reactor, including: a riser for contacting a catalyst and a first gas composition comprising an olefin to form a polyolefin under fast-fluidization regime or a dilute-phase pneumatic conveying regime conditions; a downer for contacting the catalyst and a second gas composition comprising an olefin to form additional polyolefin under fast fluidization regime or a dilute-phase pneumatic conveying regime conditions; and a transport section for conveying at least a portion of the catalyst, polyolefin, and additional polyolefin from the downer to the riser. Also disclosed is a polymerization process using such a circulating bed reactor.

Fluidized bed reactor system allowing particle sampling during an ongoing reaction

A fluidized gas reactor includes a system for preventing a fluidizing gas comprising a reactant from premature reaction. The fluidized gas reactor includes a reaction chamber including a particle bed; a gas distribution plate having a plurality of openings therethrough, wherein each opening opens into the reaction chamber; and a plurality of vertical fluidizing gas inlet tubes, each of the fluidizing gas inlet tubes being in fluid communication with one of the openings in the gas distribution plate. Each fluidizing gas inlet tube is configured to receive a fluidizing gas and transport the fluidizing gas to the reaction chamber. A fluidizing gas source provides a stream of the fluidizing gas to the fluidizing gas inlet tubes. A coolant system prevents the fluidizing gas from undergoing reaction before entering the reaction chamber. The coolant system has a fluid inlet; a coolant flow path in fluid communication with the fluid inlet, the coolant flow path being configured to cool each fluidizing gas inlet tube; and a fluid outlet in fluid communication with the coolant flow path. Each fluidizing gas inlet tube may include a particle outlet and a valve system, where the valve system allows the fluidizing gas flow to the fluidizing gas inlet tubes to be stopped; and allows recovery of particles from the particle bed while the fluidizing gas flow is stopped.

Gas phase polymerization of olefins and equipment for carrying out the same

Gaseous-phase polymerization of olefins

Gaseous-phase polymerization of an α-olefin with a catalyst and without a liquid dispersant is carried out under the following conditions: 1. A solid phase comprising said catalyst and particulate olefin polymer is caused principally by mechanical agitation to undergo circulation in the up-and-down directions within a reaction chamber of substantially vertical-cylinder type, a reaction bed being formed by said circulating solid phase; 2. The ratio of the diameter to height of said reaction bed is of the order of from 1 : 0.5 to 1 : 3; 3. The starting-material α-olefin is supplied in liquid state into the reaction chamber from a point above the reaction bed and vaporized within the reaction chamber; and 4. Heat of polymerization reaction is removed principally by the latent heat of vaporization absorbed by said vaporization of the liquid α-olefin.

Apparatus for modifying near-wall temperature in a gas phase polymerization

A falling film of water is applied around the periphery of a fluid bed olefin polymerization reactor to cool the wall and reduce the temperature in the fluid bed near the inside surface of the wall. Cooling has the effect of reducing static in the reactor, which in turn ameliorates a sheeting problem and can enhance production by facilitating control of the relation of the reactor temperature and the dew point of recycled gas. The process may be used concurrently with a gas cooling and condensing recycle system wherein at least some of the condensed recycle gas is injected in the vicinity of the internal wall surface.

Energy efficient polyolefin process

A manufacturing system for producing polyolefin includes a polymerization reactor, a flash chamber, and a purge column. In certain embodiments, the purge column may receive a solids stream directly from the flash chamber. Further, the purge column may function as a feed tank for an extruder within an extrusion/loadout system. According to certain embodiments, the manufacturing system may be configured to consume less than 445 kilowatt-hours of energy per metric ton of polyolefin produced based on consumption of electricity, steam, and fuel gas.

Energy efficient polyolefin process

A manufacturing system for producing polyolefin includes a polymerization reactor, a flash chamber, and a purge column. In certain embodiments, the purge column may receive a solids stream directly from the flash chamber. Further, the purge column may function as a feed tank for an extruder within an extrusion/loadout system. According to certain embodiments, the manufacturing system may be configured to consume less than 445 kilowatt-hours of energy per metric ton of polyolefin produced based on consumption of electricity, steam, and fuel gas.

Energy efficient polyolefin process

A manufacturing system for producing polyolefin includes a polymerization reactor, a flash chamber, and a purge column. In certain embodiments, the purge column may receive a solids stream directly from the flash chamber. Further, the purge column may function as a feed tank for an extruder within an extrusion/loadout system. According to certain embodiments, the manufacturing system may be configured to consume less than 445 kilowatt-hours of energy per metric ton of polyolefin produced based on consumption of electricity, steam, and fuel gas.

Energy efficient polyolefin process

A manufacturing system for producing polyolefin includes a polymerization reactor, a flash chamber, and a purge column. In certain embodiments, the purge column may receive a solids stream directly from the flash chamber. Further, the purge column may function as a feed tank for an extruder within an extrusion/loadout system. According to certain embodiments, the manufacturing system may be configured to consume less than 445 kilowatt-hours of energy per metric ton of polyolefin produced based on consumption of electricity, steam, and fuel gas.

Energy efficient polyolefin process

A manufacturing process for producing polyolefin, having a feed system, a reactor system including at least one polymerization reactor, a diluent/monomer recovery system, a fractionation system, and an extrusion/loadout system having an extruder. The manufacturing process is configured to consume less than 325 kilowatt-hours of electricity per metric ton of polyolefin produced.

Energy efficient polyolefin process

A manufacturing system for producing polyolefin includes a polymerization reactor, a flash chamber, and a purge column. In certain embodiments, the purge column may receive a solids stream directly from the flash chamber. Further, the purge column may function as a feed tank for an extruder within an extrusion/loadout system. According to certain embodiments, the manufacturing system may be configured to consume less than 445 kilowatt-hours of energy per metric ton of polyolefin produced based on consumption of electricity, steam, and fuel gas.

Energy efficient polyolefin process

A manufacturing process for producing polyolefin, having a feed system, a reactor system including at least one polymerization reactor, a diluent/monomer recovery system, a fractionation system, and an extrusion/loadout system having an extruder. The manufacturing process is configured to consume less than 325 kilowatt-hours of electricity per metric ton of polyolefin produced.