СПОСОБ И УСТРОЙСТВО ДЛЯ УМЕНЬШЕНИЯ СОДЕРЖАНИЯ NOxИ N2O В ГАЗАХ

Изобретение относится к способу уменьшения содержания оксидов азота в газах, в частности в технологических и отходящих газах, а также к применяемому для этого устройству. Способ включает пропускание N2O- и NOx-содержащего газа через ряд двух слоев катализатора, содержащих один тип или несколько типов нагруженных железом цеолитов, добавление восстановителя для NOx между этими слоями катализатора, поддержание температуры менее чем 500°С в первом слое катализатора и во втором слое катализатора, поддержание газового давления, по меньшей мере, 2 бар в обоих слоях катализаторов, выбор такой объемной скорости в первом и втором слоях катализатора, что в первом слое катализатора происходит разложение N2O, до содержания не более чем 90% в расчете на содержание N2O на входе первого слоя катализатора и устанавливается содержание N2O более чем 200 частей на млн. и что во втором слое катализатора происходит дальнейшее разложение содержащегося в газе N2O, по меньшей мере, на 30% в расчете на содержание ...

КОЛЛЕКТОРНЫЙ ТРУБОПРОВОД ДЛЯ ТРУБЧАТЫХ ПЕЧЕЙ РИФОРМИНГА

Изобретение относится к коллекторному трубопроводу для трубчатых печей риформинга и трубчатой печи риформинга, содержащей один или несколько коллекторных трубопроводов. Коллекторный трубопровод для отвода горячих технологических газов в трубчатых печах риформинга содержит изнутри наружу, по меньшей мере, оба слоя: изоляционный слой из огнеупорного бетона или огнеупорной кладки, стенку металлической внешней трубы, и дополнительно содержит несколько патрубков, через которые реакционные трубы трубчатой печи риформинга имеют возможность соединения с коллекторным трубопроводом, который в направлении периметра имеет разные термические сопротивления. Изобретение обеспечивает предотвращение повреждений в трубопроводе и улучшенный коллекторный трубопровод. 2 н. и 7 з.п. ф-лы, 1 ил.

ТВЕРДОЖИДКОСТНАЯ РЕАКЦИЯ

Изобретение относится к химической промышленности и может быть использовано для получения простых или сложных эфиров или смешанных ангидридов кислот. Способ проведения твердожидкостной реакции включает: а) получение реакционной суспензии, в которой первый реагент находится в суспендированной форме, а второй реагент находится в растворенной форме в суспензионной среде, причем один из продуктов реакции является нерастворимым в суспензионной среде, б) прохождение реакционной суспензии через удлиненную реакционную зону, таким образом, что число Рейнольдса потока составляет меньше чем 20000, в) отделение образовавшегося нерастворимого продукта реакции. Технический результат изобретения заключается в том, что нерастворимый продукт реакции получают в форме, которая легко фильтруется. 13 з.п. ф-лы, 1 ил.

СПОСОБ РЕГУЛИРОВАНИЯ ЭКЗОТЕРМИЧЕСКОЙ РЕАКЦИИ И УСТРОЙСТВО, ПРЕДНАЗНАЧЕННОЕ ДЛЯ ЕГО ОСУЩЕСТВЛЕНИЯ

Изобретение относится к способу регулирования экзотермической реакции. Способ включает стадии: i) проведение экзотермической реакции в реакторе (1) с получением продукта, ii) измерение температуры и/или давления в реакторе, и iii) введение инертного продукта, уже полученного ранее в экзотермической реакции, в реактор (1) из контейнера для хранения (8), если температура и/или давление превышает(ют) критическую(ие) величину(ы), где инертный продукт представляет собой жидкий продукт и его теплота парообразования используется для понижения температуры реактора. Также изобретение относится к устройству. Использование предлагаемого изобретения позволяет предотвратить значительное число неконтролируемых реакций, при этом не требует остановки реактора и его чистки. 2 н. и 8 з.п. ф-лы, 1 ил.

РАСПРЕДЕЛИТЕЛЬ ГАЗОВОГО КАРМАНА И СПОСОБ ГИДРООБРАБОТКИ ПОТОКА УГЛЕВОДОРОДНОГО СЫРЬЯ

Узел распределителя для гидрообработки углеводородной смеси водородосодержащего газа и жидкого потока углеводородного сырья имеет кольцеобразную пластину со множеством полых стояков, прикрепленных к ней для распределения водородосодержащего газа и жидкого углеводородного сырья через отверстия в кольцеобразном пластинчатом элементе. Узел распределителя соединен с внутренней стенкой реактора. Способ гидрообработки потока подаваемого углеводородного сырья включает протекание смеси водородосодержащего газа и жидкого потока углеводородного сырья в зону реактора для получения выделяемого водородосодержащего газа и протекание смеси водородосодержащего газа и жидкого углеводородного сырья через множество трубчатых зон при одновременном примешивании к ней выделяемого водородосодержащего газа. Технический результат - создание устойчивого и плавного потока смеси газа и жидкости в камеру. 3 с. и 2 з.п. ф-лы, 7 ил.

РЕАКТОР ДЛЯ ПРОВЕДЕНИЯ ТРЕХФАЗНОЙ РЕАКЦИИ ЖИДКОЙ И ГАЗООБРАЗНОЙ ФАЗ В НЕПОДВИЖНОМ СЛОЕ КАТАЛИЗАТОРА

Изобретение относится к реактору для осуществления трехфазной реакции жидкой и газообразной фаз в неподвижном слое катализатора, способу осуществления трехфазной реакции и их применению для селективной гидрогенизации фракций углеводородов. Реактор содержит слой катализатора, смесительное и распределительное устройство над слоем катализатора, через которое сверху вниз направляется равномерным потоком жидкая фаза и газообразная фаза. Смесительное и распределительное устройство включает лотковый распределитель с имеющими форму лотков каналами и отводными трубочками для жидкой фазы, а также распределительную тарелку, расположенную под лотковым распределителем с вертикальными насадками. Лотковый распределитель имеет отверстия для впуска газообразной фазы и расположенные под ними отверстия для поступления жидкой фазы. Причем количество и размер отверстий для поступления жидкой фазы рассчитаны так, что при заданном притоке жидкости уровень жидкости на распределительной тарелке устанавливается ...

КАТАЛИТИЧЕСКИЙ РЕАКТОР С ПЛАВАЮЩИМ УЛАВЛИВАТЕЛЕМ ЧАСТИЦ

Изобретение относится к каталитическому химическому реактору с разделением частиц. Более конкретно изобретение относится к реактору с сепаратором частиц, который поддерживается слоем катализатора внутри реактора. Каталитический реактор включает слой катализатора, по меньшей мере один блок плавающего улавливателя частиц, который представляет собой комбинированную сборку улавливателя частиц и распределителя текучей среды, приспособленную для улавливания частиц и примесей из технологической текучей среды, поступающей в каталитический реактор, прежде чем они достигнут слоя катализатора, и равномерного распределения технологической текучей среды по верхней части слоя катализатора, причем указанный блок плавающего улавливателя частиц включает: базовую секцию, включающую верхнюю поверхность базовой секции, нижнюю поверхность базовой секции, выполненную с возможностью плавучей поддержки на слое катализатора, экран и выпускное отверстие блока улавливателя частиц; канал, в верхней части которого ...

КАТАЛИТИЧЕСКИЙ РЕАКТОР С ИЗЛУЧАЮЩЕЙ СТЕНКОЙ И СПОСОБ ОСУЩЕСТВЛЕНИЯ ХИМИЧЕСКОЙ РЕАКЦИИ В ТАКОМ РЕАКТОРЕ

Изобретение относится к каталитическому реактору с улучшенной теплопередачей и способу осуществления в этом реакторе эндотермических химических реакций в газовой фазе. Реактор содержит реакторную камеру (1) и излучающую стенку для передачи тепла от внутренней поверхности (8) стенки реакторной камеры (1) за счет излучения для поддержания в целом эндотермической реакции в газовой фазе, протекающей в реакторной камере (1). Реакторная камера (1) имеет входной порт (2) для введения газообразного реагента в непрерывном режиме, выходной порт (3) для выхода газообразного продукта в непрерывном режиме, катализаторные сегменты (5), содержащие катализаторный материал (4), через который протекает газовый поток и вступает с ним в контакт, пустотные сегменты (6), в которых обеспечена возможность излучения тепла от внутренней поверхности (8) стенки к поверхности (9) катализаторного сегмента (5), образующей поверхность раздела между катализаторным сегментом (5) и пустотным сегментом (6), а также нагревательное ...

СПОСОБ МОДИФИКАЦИИ ГЕТЕРОГЕННОГО ЭКЗОТЕРМИЧЕСКОГО РЕАКТОРА СИНТЕЗА, РЕАКТОР СИНТЕЗА И СПОСОБ ОСУЩЕСТВЛЕНИЯ ГЕТЕРОГЕННЫХ ЭКЗОТЕРМИЧЕСКИХ РЕАКЦИЙ СИНТЕЗА

Способ модификации гетерогенного экзотермического реактора синтеза включает стадии обеспечения, по крайней мере, первого и, по крайней мере, второго каталитического слоя в верхней и, соответственно, нижней части реактора, обеспечения дополнительно самого нижнего каталитического слоя в нижней части реактора, имеющего реакционный объем меньший, чем реакционный объем второго каталитического слоя, и загрузки самого нижнего каталитического слоя катализатором, имеющим активность более высокую, чем активность катализатора, загруженного в другие слои. Изобретение позволяет получить реактор с высокой степенью превращения. 3 с. и 8 з.п. ф-лы, 2 ил.

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 ...

РЕАКТОР ПИРОЛИЗА БИОМАССЫ

Изобретение относится к устройству для осуществления пиролиза биомассы. Устройство содержит реактор с корпусом и образованной в нем реакторной камерой; первый подающий трубопровод для материала, включающего биомассу, сообщающийся с верхней зоной указанной реакторной камеры; второй подводящий трубопровод для нагретого материала, служащего теплоносителем, сообщающийся с верхней зоной реакторной камеры; первый отводящий трубопровод для пиролитического газа, сообщающийся с верхней зоной указанной реакторной камеры, расположенный на некотором расстоянии от первого подающего трубопровода; и второй отводящий трубопровод для твердого материала и материала, являющегося теплоносителем, сообщающийся с нижней частью реакторной камеры. Устройство характеризуется тем, что в реакторной камере размещена механическая мешалка с целью смешивания поступающего потока материала, включающего биомассу, с поступающим потоком предварительно нагретого материала, служащего теплоносителем; и максимальная средняя скорость ...

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 ...

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

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

РЕАКТОР ДЛЯ ПРОВЕДЕНИЯ РЕАКЦИИ МЕЖДУ ДВУМЯ ТЕКУЧИМИ ИСХОДНЫМИ ВЕЩЕСТВАМИ В КАТАЛИЗАТОРНОМ СЛОЕ С ПРЕДВАРИТЕЛЬНЫМ СМЕШИВАНИЕМ ТЕКУЧИХ ИСХОДНЫХ ВЕЩЕСТВ В УСТРОЙСТВЕ ДЛЯ СМЕШИВАНИЯ

Изобретение относится к реактору для проведения реакции между двумя текучими исходными веществами в катализаторном слое с предварительным смешиванием текучих исходных веществ и может использоваться в химической промышленности. Перед подводом в катализаторный слой текучие исходные вещества смешивают в устройстве для смешивания, которе образовано из элементов, расположенных поперек направления набегания первого текучего потока исходного вещества. Элементы включают два или три расположенных друг за другом ряда труб с генераторами турбулентности на их наружной стороне, которые сужают поперечное сечение прохода для первого текучего потока. Через внутренние пространства труб направляется второй текучий поток исходного материала и через отверстия в трубах вдувается в первый текучий поток исходного вещества. Перед трубами и за ними установлены перфорированные металлические листы. Технический результат состоит в улучшении смешивания веществ перед катализаторным слоем при малой длине устройства и ...

ГОРИЗОНТАЛЬНЫЙ РЕАКТОР ДЛЯ РЕАКЦИИ ОБМЕНА ТЕКУЧЕГО ПОТОКА ИСХОДНОГО ВЕЩЕСТВА С ТЕКУЧИМ ПОТОКОМ ОКИСЛИТЕЛЯ В ПРИСУТСТВИИ ТВЕРДОГО КАТАЛИЗАТОРА

... 1. Горизонтальный реактор (1) для реакции обмена текучего потока (2) исходного вещества с текучим потоком (3) окислителя в присутствии твердого катализатора (4) в двух или нескольких ступенях на двух или нескольких катализаторных стационарных слоях (5), которые расположены горизонтально, параллельно продольной оси корпуса (6) реактора, имеющего форму круглого цилиндра, в его внутреннем пространстве, с разъемным образом установленными на концах корпуса (6) реактора крышками (7), отличающийся тем, что ! - два или несколько катализаторных стационарных слоя (5) образованы соответственно большим количеством модулей, включая ! - соответственно раму квадратной формы (8), которая простирается по всей высоте катализаторного стационарного слоя и, в которой ! - установлены одна или несколько нижних сеток (9) и одна верхняя сетка (10) и, причем ! - между одной или несколькими нижними сетками (9) и верхней сеткой уложен твердый катализатор (4), что ! - все модули одного катализаторного слоя (5) объединены ...

ПРОВОЛОЧНЫЕ ПРОСТАВКИ ДЛЯ НАРАЩИВАЕМЫХ СТРУКТУРНЫХ РЕАКТОРОВ

... 1. Реактор, содержащий:а) внешнюю трубу;b) один или более компонентов реактора, при этом один или более компонентов реактора имеют внешнюю окружную поверхность, и один или более компонентов реактора установлены во внешней трубе;с) проволочную проставку, участок которой установлен между внешней трубой и одним или более компонентами реактора для предотвращения соприкосновения одного или более компонентов реактора с внешней трубой.2. Реактор по п. 1, в котором проволочная проставка имеет диаметр в диапазоне от 0,25 до 10 мм.3. Реактор по п. 1 или 2, в котором внешняя окружная поверхность одного или более компонентов реактора расположена на расстоянии, по меньшей мере, от 0,25 до 10 мм от внешней трубы.4. Реактор по п. 1 или 2, в котором проволочная проставка прикреплена к, по меньшей мере, одному из одного или более компонентов реактора.5. Реактор по п. 1 или 2, в котором проволочная проставка имеет концевую часть, имеющую прямолинейный участок, при этом концевая часть проходит внутрь в, по ...

РАСПРЕДЕЛИТЕЛЬНАЯ ПЛАСТИНА ДЛЯ РАСПРЕДЕЛЕНИЯ МНОГОФАЗНОЙ СМЕСИ С НАКЛОННЫМИ КАНАЛАМИ ПО ПЕРИМЕТРУ

Изобретение относится к области распределения многофазных текучих сред в каталитических реакторах с неподвижным слоем, а также способу гидрообработки или гидрирования нефтяных фракций в реакторах. Реактор содержит вертикальные стенки, верхний купол и распределительную пластину, расположенную в верхней части реактора над слоем каталитических частиц и содержащую множество каналов, по существу перпендикулярных пластине, снабженных отверстиями для прохождения жидкости, распределенными по всей высоте каналов, и отверстием для прохождения газа, расположенным на их верхнем конце. При этом часть каналов, расположенных на периферии пластины, на расстоянии от стенки реактора от 25 до 450 мм, имеет свою верхнюю часть, наклоненную под углом от 10° до 45° по отношению к вертикали, причем наклон направлен приблизительно к центру реактора. Изобретение позволяет увеличить высоту каталитического слоя и химическую конверсию и обеспечивает эффективное распределение многофазных текучих сред. 2 н. и 11 з.п.

КАТАЛИТИЧЕСКИЙ РЕАКТОР С НИСХОДЯЩИМ ПОТОКОМ

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

ТРУБА ИЗ МУЛЬТИМОДАЛЬНОГО ПОЛИЭТИЛЕНА

Изобретение относится к композиции мультимодального полиэтилена. Композиция мультимодального полиэтилена содержит (А) 51-58 мас.ч. низкомолекулярного полиэтилена или среднемолекулярного полиэтилена, полученного путем полимеризации в первом реакторе, (В) 12-21 мас.ч. первого высокомолекулярного полиэтилена или первого сверхвысокомолекулярного полиэтилена, полученного путем полимеризации во втором реакторе, и (С) 27-33 мас.ч. второго высокомолекулярного полиэтилена или второго сверхвысокомолекулярного полиэтиленового сополимера, полученного путем полимеризации в третьем реакторе. Полиэтилен, полученный в каждом реакторе, обладает отличающейся молекулярной массой. Соотношение Mw/Mn между среднемассовой молекулярной массой Mw композиции мультимодального полиэтилена и среднечисленной молекулярной массой Mn композиции мультимодального полиэтилена находится в диапазоне 10-23. Композиция мультимодального полиэтилена характеризуется высокой стойкостью к ударным нагрузкам по Шарпи, улучшенным балансом ...

УСТРОЙСТВО РАСПРЕДЕЛЕНИЯ ПОТОКА ТЕКУЧЕЙ СРЕДЫ ДЛЯ КАТАЛИТИЧЕСКИХ РЕАКТОРОВ С НИСХОДЯЩИМ ПОТОКОМ

... 1. Устройство для распределения полифазной текучей среды на гранулированном твердом материале, содержащее, по меньшей мере один газовод для введения газовой фазы в смесительную камеру, имеющую диаметр поперечного сечения, превышающий диаметр поперечного сечения газовода, при этом газовод проходит от впускного отверстия для газа и имеет нижнее отверстие, выходящее в смесительную камеру и расположенное не ниже нижнего участка жидкостного трубопровода, предназначенного для введения жидкой фазы в смесительную камеру, и полифазное сопло для ускорения и диспергирования жидких и газовых фаз, выходящих из указанного устройства, имеющее впускное отверстие, которое фиксировано соединено и соосно выровнено со смесительной камерой.2. Устройство по п.1, в котором газовод является цилиндрическим.3. Устройство по п.1, в котором газовод расположен вертикально.4. Устройство по п.1, в котором отверстие газовода расположено в горизонтальной плоскости между нижним участком и верхним участком жидкостного трубопровода ...

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 ...

УСТРОЙСТВО ДЛЯ ЭНДОТЕРМИЧЕСКОЙ РЕАКЦИИ

Эндотермическая реакционная печь 102 содержит одну или более удлиненных труб 110, разделяющих ее внутреннюю часть на проточный канал для реакционной среды и проточный канал для горючей среды для проведения эндотермической реакции. Проточный канал для горючей среды расположен так, что топливо и горючий воздух нагреваются отдельно внутри печи 102 до температуры, значительно превышающей их температуру самовоспламенения, до соединения в зоне 116 сгорания, где они смешиваются, самовоспламеняются и сгорают.

РЕАКТОР ДЛЯ ПРОВЕДЕНИЯ РЕАКЦИИ МЕЖДУ ДВУМЯ ТЕКУЧИМИ ИСХОДНЫМИ ВЕЩЕСТВАМИ В КАТАЛИЗАТОРНОМ СЛОЕ С ПРЕДВАРИТЕЛЬНЫМ СМЕШИВАНИЕМ ТЕКУЧИХ ИСХОДНЫХ ВЕЩЕСТВ В УСТРОЙСТВЕ ДЛЯ СМЕШИВАНИЯ

... 1. Реактор для проведения реакции между двумя текучими исходными веществами (2, 3) в катализаторном слое (4) с предварительным смешиванием текучих исходных веществ (2, 3) перед подводом к катализаторному слою в течение времени задержки менее 150 мс в устройстве (5) для смешивания, отличающийся тем, что устройство (5) для смешивания образовано следующими элементами, которые расположены в основном поперек направления набегания первого текучего потока (2) исходного вещества: ! двумя или тремя расположенными друг за другом рядами труб (6) с генераторами турбулентности на их наружной стороне, которые сужают поперечное сечение прохода для первого текучего потока (2) исходного вещества на от 1/2 до 1/10, причем через внутренние пространства труб (6) направляется второй текучий поток (3) исходного вещества и через отверстия (7) в трубах (6) вдувается в первый текучий поток (2) исходного вещества, а также ! установленным впереди труб (6) перфорированным металлическим листом (10) ! установленным ...

ТВЕРДО-ЖИДКОСТНАЯ РЕАКЦИЯ

... 1. Способ проведения твердо-жидкостной реакции, включающий получение реакционной суспензии, в которой первый реагент находится в суспендированной форме, а второй реагент находится в растворенной форме в суспензионной среде, причем один из продуктов реакции является нерастворимым в суспензионной среде, прохождение реакционной суспензии через удлиненную реакционную зону, таким образом, что число Рейнольдса потока составляет меньше чем 20000, и отделение образовавшегося нерастворимого продукта реакции. 2. Способ по п.1, отличающийся тем, что число Рейнольдса потока составляет меньше чем 10000. 3. Способ по п.1 или 2, отличающийся тем, что продольная ось реакционной зоны является вертикальной. 4. Способ по п.1 или 2, отличающийся тем, что реакционную суспензию, получают путем смешивания суспензии первого реагента в суспензионной среде с жидким или растворенным вторым реагентом. 5. Способ по п.4, отличающийся тем, что время нахождения реакционной суспензии в реакционной зоне, по крайней мере ...

Hochtemperatur-Wärmetauscher

Behälter mit Leitplattenanordnung

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.

VERFAHREN ZUR DURCHFÜHRUNG VON STARK EXOTHERMEN OXIDATIONSREAKTIONEN UNTER PSEUDO-ISOTHERMISCHEN BEDINGUNGEN

VORRICHTUNG ZUR ABDICHTUNG UND ZUR AUFNAHME VON AUSDEHNUNGSUNTERSCHIEDEN ZWISCHEN EINEM KUEHLRAUM FUER TEILCHEN IN DER SCHWEBE UND EINER RUECKFUEHRLEITUNG.

Kontaktkorb fuer bei hohen Temperaturen in einer Katalysatorschicht durchzufuehrende Reaktionen

REAKTOR FUER EXOTHERME KATALYTISCHE VERFAHREN

Katalysatoranlage mit Durchlaufstrahlenabschirmung und Verfahren zur Herstellung von Blausäure mit derselben

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.

Catalytic synthesis of ammonia or methanol - from synthesis gas contg inert gas in compact reactor

A catalyst reactor for high pressure, high temp. exothermic reactions, e.g., synthesis of ammonia and methanol, esp. where synthesis gases contg. >20% inert gas content are used, comprises a vertical pressure vessel with catalyst-collector regions and heat exchangers. The adiabatically operating catalyst zone is situated immediately above the catalyst collector regions and has an axial gas feed. The catalyst collector regions comprises a number of concentric heat exchange double tubes, in which the inner tube tapers towards the top and has synthesis gas insulation and pressure-balancing openings; a heat exchanger in the lower part of the reactor is filled, both inside and outside its tubes, with metal balls.

Control of gas composition

Catalyst or sorbent beds

REACTOR FOR THE CATALYTIC SYNTHESIS OF AMMONIA AT HIGH TEMPERATURES AND PRESSURES

... 1356151 Ammonia synthesis COMBINATUL CHIMIC FAGARAS 14 May 1971 15054/71 Heading C1A [Also in Division B1] In a catalytic ammonia synthesis pressure reactor, Fig. 1, nitrogen/hydrogen mixture is led in through the top of the reactor, passes down the outer annular space a, then passes up through the intertubular space of heat exchanger 5 which contains a metal ball packing 6 to chamber c, then up tubes 9 which have walls of upwardly tapering thickness, and down heat conducting tubes 8, up tube 13 to pass radially through catalyst 12 where heat is dissipated, through mixing chamber 16 where a whirling motion is created by blades 17, Fig. 2, thence down through catalyst bed 11 where further heat is dissipated, through ball filter layer 22, down through the tubes in heat exchanger 5 which contain a metal ball; and hence out at the bottom of the reactor. Tubes 9 are insulated at their lower ends by gas cushions formed in hollows e, Fig. 9. Packing 6 may be fluidized for cleaning and its upper ...

Catalytic reactor and catalyst structure

Chemical reactions in which hydrogen is a reaction product

Aliphatic or alicyclic C1 to C20 hydrocarbons are dehydrogenated in a process wherein the hydrogen produced is separated from the gaseous reaction mixture by contacting the reaction mixture with one side of a membrane selectively permeable to hydrogen, the unconverted reactants being further reacted to produce more hydrogen. There is reference to the dehydrogenation of propane and butane to olefins, isopentane to isoprene and cyclohexane to benzene.ALSO: Hydrogen is produced by a gas phase chemical reaction in a process which includes the step of contacting the reaction mixture with one side of a membrane selectively permeable to hydrogen to separate a diffused gaseous hydrogen stream from the undiffused gaseous reaction mixture containing unconverted reactant(s), and further reacting the unconverted reactant(s) to produce more hydrogen. Examples relate to (1) the dissociation of ammonia at 800-1200 DEG F. using as catalyst, for example, platinum, palladium, rhodium or ...

Port closure

PROCESS FOR THE MANUFACTURE OF DICHLOROETHANE

... 1,272,037. Dichloroethane. SOC. ITALIANA RESINE S.p.A. 20 Oct., 1970 [14 Nov., 1969], No. 49789/70. Heading C2C. Dichloroethane is manufactured by oxychlorination of ethylene with O 2 and HCl gas in the presence of a supported catalyst containing a salt of a variable valency metal, the process being characterized in that: (i) in a reactor of height : diameter ratio of at least 3 : 1 there are established a bottom zone of a fixed bed of solid inert particles and a top zone consisting of a bed of the supported catalyst in the form of solid particles of size 30-100 mesh; (ii) there is established a first gaseous stream containing C 2 H 4 and 50-90% by volume of the HCl gas to be reacted; (iii) there is established a second gaseous stream containing O 2 and the balance of HCl gas; (iv) one of these streams, after being preheated, is fed to the bottom of the fixed bed; (v) the other stream, after being preheated is fed to the bottom of the bed of catalytic particles; (vi) the gas streams being ...

Fluidized granulator

In conventional fluidized granulators whose housing is made of a steel plate, a powder tends to cause blocking if it is highly hygroscopic, and the bag filter used therein causes clogging. These problems have been solved in the present invention by forming the housing of a fluidized granulator with a porous membrane in place of the conventional steel plate. This fluidized granulator produces granules or a coated powder by spraying powder with water, a binder fluid or a coating fluid while maintaining the powder in a fluidized state.

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.

Catalyst or sorbent beds

Reactor

Fluidized Catalyst Reactor.

... 1,194,366. Fluidised bed catalytic reactor. STANDARD OIL CO. 6 July, 1967 [21 July, 1966], No. 31260/67. Heading B1F. Deposition, stagnation, reduction and fusion of catalyst in the upper part of a fluidised bed catalytic reactor is prevented by a horizontal plate with an aperture across the top part of the reactor and inert gas which is passed into the top of the reactor. The plate is fitted around the cyclones and associated pipe work to allow for thermal expansion. The apparatus may be used for oxidation of olefin/ammonia mixtures to form unsaturated nitriles, oxidation of olefines to aldehydes and acids, and oxidative dehydrogenation of butene-1 to butadiene.

Gas flow reactor

A continuous type process method to increase the rate of reaction between solids, liquids, and gasses per area of the land occupied by two rasctors.

Multi-disc catalytic reactor

A multi-disc catalytic reactor comprising: a housing defining a cavity; at least one inlet in communication with the cavity and configured to communicate with one or more reagent feed streams; at least one outlet in communication with the cavity and configured to provide one or more product feed streams; a rotatable shaft located within and rotatable relative to the cavity of the housing; a drive means in communication with and operable to rotate the shaft; and a plurality of immobilized catalyst discs comprising a mesh support and a catalyst immobilized thereon are located within the reactor, wherein the discs are configured to be mounted on and rotatable with the shaft. The at least one inlet may comprise one or more nozzle rings mounted above the catalyst discs on the shaft or non-rotationally mounted. The nozzle ring may provide a plurality of spaced circumferential inlets which can be angled to point in the shaft rotation direction. The plurality of catalyst discs can be spaced e.g ...

Furnace and steam reforming process

A steam reforming furnace (F) has a plurality of substantially vertical reformer tubes (T). Each reformer tube (T) has a feed inlet (P) at its lower end, and outlet at its upper end, and a catalyst containment zone disposed intermediate its upper and lower ends and contains a charge of a particulate steam reforming catalyst (C) which is insufficient to fill completely the catalyst containment zone. An upper retainer means (3) is mounted at the upper end of the catalyst containment zone and is permeable to gas or vapour but retains particles of the catalyst (C) in the catalyst containment zone. A follower means (4; 24) is movably mounted in the catalyst containment zone beneath the charge catalyst (C) for movement upwardly from a lower end of the containment zone upon upward flow of gas through the catalyst containment zone at a rate beyond a threshold rate. A reactant mixture comprising the hydrocarbon feedstock and steam flows upwardly through each reformer tube (T) at a flow rate which ...

Process and apparatus for loading a particulate solid into a vertical tube

A process is described in which an elastic fluid is contacted with a paniculate solid. This comprises providing a substantially vertical elongate tubular containment zone (1) containing a charge of the particulate solid (5), the volume of the containment zone (1) being greater than the settled volume of the particulate solid (5). An upper retainer means (3) is mounted at the upper end of the containment zone (1), the upper retainer means (3) being permeable to the fluid but adapted to retain particulate solid (5) in the containment zone (1). A follower means (4) is movably mounted in the containment zone (1) beneath the charge of particulate solid (5) for movement upwardly from the lower end of the containment zone (1) upon upward flow of elastic fluid through the containment zone (1) at a rate beyond a threshold rate. In the process the elastic fluid is caused to flow upwardly through the containment zone (1) at a rate which is sufficient to cause particulate solid (5) to rise up towards ...

Furnace and steam reforming process.

Process and apparatus for loading a particulate solid into a vertical tube.

Process and apparatus for loading a particulate solid into a vertical tube.

Furnage and steam reforming process.

Process and apparatus for loading a particulate solid into a vertical tube.

Furnace and steam reforming process.

Process and apparatus for loading a particulate solid into a vertical tube.

Furnace and steam reforming process.

REACTOR

REACTOR WITH EVEN DISTRIBUTION OF OPERATIONAL FUNDS

DEVICE TO MIXING WITH LOW PRESSURE LOSS AND PROCEDURE FOR MIXING TWO GAS/CSTEAMS

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

REACTOR AND PROCEDURE FOR THE PRODUCTION OF HYDROGEN SULFIDE

PLATE-TYPE HEAT EXCHANGER UNIT FOR REACTORS WITH CATALYST POURING

REACTOR TO THE EXECUTION OF HIGH PRESSURE REACTIONS, PROCEDURE FOR START-UP AS WELL AS PROCEDURE FOR THE EXECUTION OF A REACTION

DEVICE FOR THE TREATMENT OF A LIQUID AND AN APPLICATION FOR THE SEPARATION OF AT LEAST ONE COMPONENT FROM A GAS MIXTURE

FLOW REACTOR

ADSORBENT FOR THE CHROMATOGRAPHY, METHOD FOR THE PRODUCTION OF THE SAME AND YOUR USE AS A FIXED PHASE MATRIX IN A FLUIDIZED-BED REACTOR

CATALYTIC REACTOR FOR THE REDUCTION OF SLIP BREAKING THE CATALYST

ARRANGEMENT CONCERNING A VERSCHLEISSFESTEN COATING IN A PARTICLE FEEDING DEVICE AND METHOD TO THEIR PRODUCTION

DEVICE FOR THE LOADING AND UNLOADING A REACTOR TO DENITRIERUNG FLUE GASES WITH MOBILE MODULES.

ROHRBUNDELREAKTOR FUR THE CATALYTIC GASEOUS PHASE OXIDATION

BANK OF TUBES

HEAT EXCHANGE MORE REFORMER WITH LOW PRESSURE LOSS

PROCEDURE FOR THE PRODUCTION OF SYNTHESIS GAS OF MEANS OF CATALYTIC PARTIAL OXIDATION

PROCEDURE AND DEVICE FOR STRIPPING

PROCEDURE FOR SUPERVISING AND/OR TAXES AND RULES OF A GRANULATIONS, AN AGGLOMERATION, INSTANTISIERUNGS, COATING AND DRYING PROCESS IN A FLUIDISED BED OR A MOVED POURING BY DETERMINATION OF THE PRODUCT DAMPNESS AS WELL AS AERIAL ENGINEERING APPARATUS FOR THE EXECUTION OF THE PROCEDURE

CATALYTIC REACTOR

STEIGHRORHREAKTOR A FCC PLANT

SUPPORT SYSTEM FOR BED FROM GRANULAR MATERIAL

Reaktionsrohr for tube furnaces as well as procedure for its production

POLYPHASE GRADATIONS PASSIVE REACTOR

Multimodal polyethylene thin film

The present invention relates to a reactor system for a multimodal polyethylene polymerization process, comprising; (a) a first reactor; (b) a hydrogen removal unit arranged between the first reactor and a second reactor comprising at least one vessel connected with a depressurization equipment, preferably selected from vacuum pump, compressor, blower, ejector or a combination, thereof, the depressurization equipment allowing to adjust an operating pressure to a pressure in a range of 100 - 200 kPa (abs); (c) the second reactor; and. (d) a third reactor and the use of a film thereof.

Fluidized bed reactor comprising a nozzle grate

Steam reforming apparatus

Device and method for blowing down and measuring the back pressure of chemical reactor tubes

METHOD AND DEVICE FOR SUPPORTING CATALYST GAUZES IN AN AMMONIA OXIDATION BURNER

Method for realizing internal walls of catalytic reactors

Reactor (1 ) for catalytic chemical reactions, comprising: a partially open outer vessel (2) comprising a manhole (6) for accessing to the interior, and at least one internal wall (5) comprising a plurality of panels (5.1, 5.2,...5.n) assembled inside the vessel (2) so as to form said wall (5); the panels are flexible and deformable so that they may be inserted through said manhole (6), and the resulting wall (5) is not self-supporting and rests against a load-bearing wall (7) of the reactor.

Converter for converting so3

The aim of the invention is to reduce the mechanical load of the casing and/or the central pipe of a tray of a contact kettle. To this end, a segment is provided for forming a membrane bottom for a contact kettle, particularly for the oxidation of SO ...

Inhibiting of erosion of vessels

Reactor filled with catalyst material, and catalyst therefor

Inhibition of carbon deposition on fuel gas steam reformer walls

Endothermic reaction apparatus

Process and reaction particles for carrying out reactions

Method of removing reactive metal from a metal-coated reactor system

Split Flow Contactor

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

HOT ISOSTATIC PRESSING

A process is provided for producing a component. The process comprising the steps of: producing a former corresponding to the internal dimensions of the component to be formed; providing a layer of a second material on at least one surface of the former; locating the former in a containment and filling the containment with a first material; subjecting the containment to hot isostatic pressing such that the second material diffuses into the first material. 1. A process for producing a component , the process comprising the steps of: producing a former corresponding to the internal dimensions of the component to be formed; providing a layer of a second material on at least one surface of the former; locating the former in a containment and filling the containment with a first material; subjecting the containment to hot isostatic pressing such that the second material diffuses into the first material.2. The process according to claim 1 , wherein the former is removed from the component after the HIP process.3. The process according to claim 1 , wherein the first and/or second materials are metal powders.4. The process according to claim 1 , wherein the second material is a ceramic.5. The process according to claim 1 , wherein the second material includes Boron Nitride and Chromium.6. The process according to claim 1 , wherein the second material may be thermally sprayed claim 1 , plasma sprayed claim 1 , aqueous sprayed or deposited by vapour phase deposition onto the former.7. The process according to claim 1 , wherein the first material is a Nickel alloy such as Sagitite®.8. The process according to claim 1 , wherein the second material includes Nickel and the first material includes aluminium.9. The process according to claim 1 , wherein the second powder diffuses through the top 1000 μm to 2000 μm (i.e. 1-2 mm) of the component.10. The process according to claim 1 , wherein the second powder has a plurality of constituent parts that are applied homogeneously.11. ...

REACTOR, AND METHOD FOR THE GASIFICATION OF BIOMASS

A reactor for the gasification of biomass having a reactor vessel that defines a gasification chamber with an oxidation zone, to which oxidation zone an oxygen containing gasification agent, in particular air, may be supplied from outside of the reactor vessel, wherein biomass may be continuously transported to the oxidation zone in the gasification chamber, wherein air supply elements having exit openings in the area of the oxidation zone are arranged in the reactor vessel, which extend in the transport direction of the biomass. The air supply elements are each configured in lance form and provided along at least one insulation section with an external insulation layer. 1. A reactor for the gasification of biomass having a reactor vessel that defines a gasification chamber with an oxidation zone , to which oxidation zone an oxygen containing gasification agent , in particular air , may be supplied from outside of the reactor vessel , wherein biomass may be continuously transported to the oxidation zone in the gasification chamber as well as air supply elements having exit openings in the area of the oxidation zone are arranged in the reactor vessel , which extend in the transport direction of the biomass , wherein the air supply elements are each configured in lance form and provided along at least one insulation section with an external insulation layer.211. A reactor according to claim 1 , wherein the air supply elements are provided in groups with a common insulation layer along at least one insulation section ().3. A reactor according to claim 1 , wherein the air supply elements are provided along at least one heat exchange section with an external heat exchanger.4. A reactor according to claim 1 , wherein the air supply elements are arranged over the cross-section of the gasification chamber.5. A reactor according to claim 1 , wherein the air supply elements are arranged ring-like in the gasification chamber.6. A reactor according to claim 1 , wherein the air ...

GASIFICATION OF CARBONACEOUS MATERIALS AND GAS TO LIQUID PROCESSES

Herein disclosed is a system for producing an organic, the system including at least one high shear mixing device having at least one rotor and at least one stator separated by a shear gap, wherein the shear gap is the minimum distance between the at least one rotor and the at least one stator; a pump configured for delivering a fluid stream comprising liquid medium and light gas to the at least one high shear mixing device, wherein the at least one high shear mixing device is configured to form a dispersion of the light gas in the liquid medium; and a reactor comprising at least one inlet and at least one outlet, wherein the at least one inlet of the reactor is fluidly connected to the at least one high shear mixing device, and wherein the at least one outlet is configured for extracting the organic therefrom. 1. A system for producing an organic , the system comprisingat least one high shear mixing device comprising at least one rotor and at least one stator separated by a shear gap, wherein the shear gap is the minimum distance between the at least one rotor and the at least one stator;a pump configured for delivering a fluid stream comprising liquid medium and light gas to the at least one high shear mixing device, wherein the at least one high shear mixing device is configured to form a dispersion of the light gas in the liquid medium; anda reactor comprising at least one inlet and at least one outlet, wherein the at least one inlet of the reactor is fluidly connected to the at least one high shear mixing device, and wherein the at least one outlet of the reactor is configured for extracting the organic therefrom.2. The system of claim 1 , wherein the reactor is a Fischer-Tropsch reactor claim 1 , a fixed-bed reactor claim 1 , or a slurry reactor claim 1 , and wherein the reactor comprises a multifunctional catalyst.3. The system of claim 2 , wherein the multifunctional catalyst promotes at least two of the following reactions: dehydrogenation claim 2 , water ...

Reaction device for producing hydrocarbons from synthesis gas

Disclosed is a reaction device for producing hydrocarbons from synthesis gas, in which hydrocarbons, olefins, oxygenates, etc., are produced over a Fischer-Tropsch catalyst by using synthesis gas, so that catalyst particles can easily be from a slurry which is discharged to the outside. That is, the present invention provides a reaction device for producing hydrocarbons from synthesis gas, in which an internal filter system for separating particles enlarged due to a agglomeration phenomenon of a catalyst is installed inside the reactor, and an separating device is separately disposed outside, such that it is possible to recirculate only particles having a size appropriate for performing F-T synthesis in the slurry phase, and additionally, it is possible to effectively discharge and process a catalyst aggregated due to a combination of fine catalyst particles, the catalyst chipped off during the operation, etc., liquid hydrocarbon, resulting water, etc., in the slurry phase reactor.

START-UP METHOD FOR REACTION-REGENERATION UNIT USED TO PREPARE LIGHT OLEFINS FROM METHANOL

The invention provides a start-up method for a reaction-regeneration unit for preparing light olefins from methanol, which comprises: (a) heating a regenerator with an auxiliary combustion chamber and a reactor with a start-up furnace; (b) charging a catalyst into the regenerator and reactor; (c) closing a spent catalyst slide valve and a regenerated catalyst slide valve after the reactor reaches about 350° C. or more; (d) feeding methanol to the reactor after the dense phase stage of the regenerator reaches about 350° C. or more; (e) opening the spent catalyst slide valve and introducing a carbon deposited catalyst from the reactor to the regenerator after the dense phase stage reaches about 400° C. or more and the average amount of carbon deposits on the catalyst in the reactor reaches about 2.5% or more; (f) raising the regenerator to above about 580° C.; and (g) stopping the start-up furnace and auxiliary combustion chamber. 1. A start-up method for a reaction-regeneration unit used to prepare light olefins from methanol , comprising the following steps:(a) heating air with an auxiliary combustion chamber and then introducing the air into a regenerator to heat the dense phase stage of the regenerator to a temperature in the range from about 350 to about 550° C., and meanwhile heating a water vapor with a start-up furnace to a temperature in the range from about 400 to about 550° C. and then introducing the water vapor into a reactor;(b) charging a catalyst into the regenerator through a regenerator large-scale catalyst feeding line, charging a catalyst into the reactor through a reactor large-scale catalyst feeding line, further heating the reactor with the water vapor heated by the start-up furnace and further heating the regenerator with the air heated by the auxiliary combustion chamber;{'sup': '3', '(c) closing a spent catalyst slide valve and a regenerated catalyst slide valve after the temperature of the reactor reaches about 350° C. or more, introducing a ...

Catalytic Reactor and Catalyst Structure

A reactor defines first and second flow channels within the reactor, the first flow channels and the second flow channels extending in parallel directions along at least the major part of their lengths. A removable non-structural catalyst insert is provided in those channels in which a reaction is to occur, the catalyst insert comprising a plurality of foils bonded together and which subdivide the flow channel into a multiplicity of flow sub-channels. At least one end portion of the catalyst insert is devoid of active catalytic material. The end portion that is devoid of active catalytic material suppresses the reaction in that part of the flow channel, and so reduces the requirement for any thermal transfer at that part of the flow channel. 1. A reactor defining first and second flow channels within the reactor , the first flow channels and the second flow channels extending in parallel directions along at least the major part of their lengths , with a removable catalyst insert provided in those channels in which a reaction is to occur , each catalyst insert comprising a plurality of foils bonded together and which subdivide the flow channel into a multiplicity of flow sub-channels , wherein at least one end portion of each catalyst insert is devoid of active catalytic material and wherein catalyst inserts in at least one set of flow channels are slightly longer than the length of those flow channels , so as to protrude from an end of the flow channel.2. A reactor as claimed in wherein the first or second flow channels include inlet or outlet portions that connect to an inlet or outlet port or to a header claim 1 , and extend in a direction that is not parallel to the direction of the major part of the length of the flow channel.3. A reactor as claimed in wherein active catalytic material is provided only on those portions of the catalyst insert that locate in a region of the reactor in which the first and second flow channels extend in parallel directions.4. ( ...

Wire standoffs for stackable structural reactors

A wire standoff suitable for use in a tubular reactor, such as a reformer, is described. The wire standoff includes a portion or segment positioned between an outer reactor tube and one or more reactor components located within the tube. The reactor components and the outer tube are prevented from coming into directed contact with one another by the positioning of the wire standoff. The wire standoff can be secured to a reactor component at one of its ends or to a washer located between stacked reactor components. Prevention of the reactor components from contact with the outer tube promotes fluid flow through the reactor and can enhance heat transfer and reactor efficiency for carrying out catalytic reactions.

Apparatuses Including Support Member Modifications and Processes Related Thereto

Embodiments of an invention disclosed herein relate to apparatuses and processes related thereto including modifications of support members that significantly reduce the magnitude of stress at junctions between the support members and the shell walls of the apparatuses. 1. An apparatus comprising:(a) a shell having an inner wall and an outer wall;(b) at least two support members, wherein the at least two support members extend through the inner wall and the outer wall of the shell;(c) a plurality of side supports proximal to the outer wall and coupled to the at least two support members; and(d) at least one stiffener coupling the inner wall and one or more of the at least two support members.2. The apparatus of claim 1 , wherein the apparatus further comprises at least one of (e) a base and (f) a plurality of tubular bundles.3. The apparatus of claim 1 , wherein the apparatus further comprises lower support members claim 1 , middle support members claim 1 , and upper support members.4. The apparatus of claim 1 , wherein the apparatus further comprises outer support members and inner support members.5. The apparatus of claim 1 , wherein the support members are placed equidistant with relation to each other along the vertical axis of the apparatus.6. The apparatus of claim 1 , wherein the support members are placed equidistant with relation to each other along the horizontal axis of the apparatus.7. The apparatus of claim 1 , wherein the at least one stiffener comprises an internal rib and a doubler plate.8. The apparatus of claim 7 , wherein the stiffener further comprises an internal rib support member coupled to the internal rib and the support member.9. The apparatus of claim 1 , wherein the at least one stiffener comprises at least one insert plate.10. The apparatus of claim 1 , wherein any of the junctions of the support members claim 1 , the at least one stiffener claim 1 , the inner wall claim 1 , and the outer wall are made permanent claim 1 , optionally or ...

REACTOR AND METHOD FOR THE AT LEAST PARTIAL DECOMPOSITION, IN PARTICULAR DEPOLYMERIZATION, AND/OR PURIFICATION OF PLASTIC MATERIAL

The invention relates to a reactor for gasifying and/or purifying, in particular depolymerizing, plastic material (), comprising a reactor vessel () for holding the plastic material () and a heater () for heating the plastic material () in the reactor vessel (), the reactor vessel being at least partially filled with a metal bath (). According to the invention, a deceleration device () is provided in an interior () of the reactor vessel () to decelerate a flow of liquefied plastic material () in the reactor vessel (), said deceleration device () having a plurality of elements () that are movably arranged in the interior (). 2. The reactor according to claim 1 , wherein the elements are made from ferromagnetic material.3. The reactor according to claim 1 , wherein the deceleration device is designed in such a way that it forces the liquefied plastic material onto a meandering path.4. The reactor according to claim 1 , wherein the heater is an inductive heater.5. The reactor according to claim 1 , characterized by at least one restraint device for the prevention of the flotation of the elements claim 1 , in particular the balls.6. The reactor according to claim 1 , wherein at least one restraint device is connected to at least one movement device for moving the restraint device up and down.7. The reactor claim 1 , wherein the restraint device is connected to a motor claim 1 , so that the restraint device can be moved in an oscillating movement claim 1 , in particular along a longitudinal axis (L) of the reactor vessel.8. The reactor according to claim 1 , characterized by a plurality of restraint devices which can be automatically moved independently from each other in an oscillating movement claim 1 , in particular along a longitudinal axis (L) of the reactor vessel.9. A process for at least partially decomposing claim 1 , in particular depolymerizing claim 1 , and/or purifying plastic material characterized by the steps:(a) introduction of the plastic material into ...

REACTOR FOR PRODUCING HIGH-PURITY GRANULAR SILICON

The present invention provides a reactor and a method for the production of high purity silicon granules. The reactor includes a reactor chamber; and the reaction chamber is equipped with a solid feeding port, auxiliary gas inlet, raw material gas inlet, and exhaust gas export. The reaction chamber is also equipped with an internal gas distributor; a heating unit; an external exhaust gas processing unit connected between a preheating unit and a gas inlet. The reaction chamber is further equipped with a surface finishing unit, a heating unit and a dynamics generating unit. The reaction is through decomposition of silicon containing gas in densely stacked high purity granular silicon layer reaction bed in relative motion, and to use remaining heat of exhaust gas for reheating. The present invention is to achieve a large scale, efficient, energy saving, continuous, low cost production of high purity silicon granules. 1. A reactor for the production of high purity granular silicon , comprising:At least one reaction chamber system comprising a reaction chamber equipped with at least a solid feeding port; a solid output port, an auxiliary gas inlet; a raw material gas inlet; and an outlet for exhaust gas; the reaction chamber being configured to receive silicon granules and to allow the silicon granules to form a silicon bed layer;the reaction chamber being internally equipped with at least a gas distributor for the dispersion of auxiliary gas and raw material gas to deposit silicon on the surface of silicon granules inside the reaction chamber without the limitation for minimum flow and velocity required as in fluidized bed reactor; a preheating unit to recover the heat from the exhaust gas, and', 'an exhaust gas processing unit to separate components of the exhaust gas and recycle at least a portion of the exhaust gas into the reaction chamber., 'the reaction chamber system further comprising2. The reactor of claim 1 , further comprising a gas-solid separating unit ...

Apparatus for Retaining Solid Material in a Radial Flow Reactor and Method of Making

An apparatus for use in radial flow reactors is presented. The apparatus includes a first partition and a second partition with support members coupled therebetween. The first partition include a first opening and a second opening to allow the passage of fluid therethrough. A baffle extends into a flow channel formed by adjacent support members to obstruct an upper or lower portion of the first opening to interrupt a portion of the fluid flow therethrough.

DIGESTION UNITS CONFIGURED FOR HIGH YIELD BIOMASS PROCESSING

Digestion units for processing cellulosic biomass can comprise a chamber having a height that is greater than its width, the chamber having an opening suitable for solids introduction located within the upper 20% of its height; one or more first fluid conduits connected to the chamber within the lower 20% of its height, at least one of the first fluid conduits extending into the chamber and being elevated above the bottom of the chamber; one or more second fluid conduits connected to the chamber within the upper 20% of its height, at least one of the first fluid conduits being fluidly coupled to at least one of the second fluid conduits; a porous medium located in the chamber within the lower 20% of its height; and a movable pressure isolation device covering the opening; wherein the digestion unit is operable to maintain a pressure of at least about 30 bar. 1. A digestion unit comprising:a chamber having a height that is greater than its width, the chamber having an opening suitable for solids introduction located within the upper 20% of its height;one or more first fluid conduits connected to the chamber within the lower 20% of its height, at least one of the first fluid conduits extending into the chamber and being elevated above the bottom of the chamber;one or more second fluid conduits connected to the chamber within the upper 20% of its height, at least one of the first fluid conduits being fluidly coupled to at least one of the second fluid conduits so as to establish a fluid circulation loop;a porous medium located in the chamber within the lower 20% of its height; anda movable pressure isolation device covering the opening;wherein the digestion unit is operable to maintain a pressure of at least about 30 bar.2. The digestion unit of claim 1 , further comprising:a pressurizable solids introduction vessel that is operably connected to the chamber via the movable pressure isolation device.3. The digestion unit of claim 1 , wherein the chamber lacks a ...

Regenerative Gas Generator

Systems, methods, and computer program products are disclosed that overcome the deficiencies of traditional steam engines and internal combustion engines. In an embodiment, a system is disclosed for generating reaction products having elevated temperature and pressure. The system comprises a first chamber including a reactor to decompose hydrogen peroxide to generate oxygen and water vapor. The system further comprises a second chamber including a reactor to catalytically combust a mixture of the generated oxygen and a fuel to generate reaction products having elevated temperature and pressure. The system further comprises a passageway to receive reaction products exiting the second chamber and to channel the reaction products to come into contact with external surfaces of the first and second chambers to thereby transfer heat to the first and second chambers, and an outlet to allow the reaction products to exit the system.

CONTINUOUS CATALYST REGENERATION REACTOR WITH DEFLECTOR MEANS FOR DEFLECTING THE FLOW OF CATALYST IN THE OXYCHLORINATION ZONE

The reactor for continuously regenerating grains of catalyst is composed of a vessel containing an oxychlorination zone positioned above a calcining zone provided with a line for introducing calcining gas , the reactor containing an oxychlorination gas injection line opening into the bottom of the oxychlorination zone and a gas evacuation line at the head of the oxychlorination zone, characterized in that the oxychlorination zone contains at least one deflector means for deflecting the flow of grains of catalyst. 1127275767372747282b. A reactor () for the continuous regeneration of grains of catalyst , containing a vessel () comprising a first zone () positioned above a second zone () provided with a line () for introducing a first gas , the reactor comprising a line () for injecting a second gas opening into the bottom of the first zone () and a gas evacuation line () at the head of the first zone , characterized in that the first zone () comprises at least one deflector () for deflecting the flow of grains of catalyst.2. A reactor according to claim 1 , characterized in that the first zone is composed of an oxychlorination zone claim 1 , the second zone is composed of a calcining zone claim 1 , the first gas is composed of a calcining gas claim 1 , and the second gas is composed of an oxychlorination gas.382. A reactor according to claim 2 , characterized in that the deflector () is composed of a plate which is impervious to grains of catalyst and impervious to gas.482. A reactor according to claim 2 , characterized in that the deflector () is composed of a plate which is impervious to grains of catalyst and permeable to gas.58273. A reactor according to claim 2 , characterized in that the deflector () is separated by a height of at least 10 cm with respect to the position at which the oxychlorination gas injection line () opens into the oxychlorination zone.682. A reactor according to claim 2 , characterized in that the surface of the deflector () projected onto ...

Filtration tray for catalytic chemical reactor

A particle separation system for a catalytic chemical reactor.

Fluid Solids Contacting Device

A fluid solids contacting device comprising a vessel; one or more grid structures comprising two or more levels, wherein each level comprises a plurality of grid assembly sections; a base formed from structural members used to support the multi-tiered structure; and three or more chairs attached to an inside surface of the vessel and spaced apart to support the base; and wherein the base is supported by the chairs is provided. 1. A fluid solids contacting device comprising:a vessel;a grid structure comprising one or more grid levels, wherein each grid level comprises a plurality of grid assembly sections;a base formed from structural members and on which the grid structure is supported; andthree or more chairs attached to an inside surface of the vessel and spaced apart to support the base; andwherein the base is supported by the chairs.2. The fluid solids contacting device according to claim 1 , wherein the base is formed from I-beams and has a central portion which is a closed geometric shape and three or more arms attached at one end to the central portion claim 1 , wherein the arms are spaced substantially at substantially equal distances around a perimeter of the central portion.3. The fluid solids contacting device according to claim 1 , wherein each grid assembly section comprises a bottom platform claim 1 , a frame structure extending upward from two opposing sides of the bottom platform claim 1 , wherein each frame structure comprises an optional diagonal support and an optional top guide section configured to accept a bottom platform of a grid assembly section.4. The fluid solids contacting device according to claim 3 , wherein the central portion of the base is circular.5. The fluid solids contacting device according to claim 3 , wherein the bottom platform comprises one or more of the group consisting of subway grating claim 3 , chevrons a packing structures or other structure that obstructs an open area.6. The fluid solids contacting device according to ...

PRODUCTION OF LOW CLOUD POINT DISTILLATE FUELS

Systems and methods are provided for catalytically dewaxing a diesel boiling range feed. In some aspects, catalytic dewaxing can be performed at low hydrogen treat gas rates and/or low hydrogen purity conditions. In other aspects, the systems and methods can allow for distillate dewaxing while reducing or minimizing the amount of equipment required. 1. A method for producing distillate fuel boiling range material , comprising:{'sup': 3', '3', '3', '3, 'sub': '2', 'exposing a distillate fuel boiling range feedstock having a sulfur content of about 15 wppm or less to a dewaxing catalyst comprising a molecular sieve and a metal hydrogenation component under dewaxing conditions to produce a dewaxed effluent comprising a distillate fuel boiling range product and/or blendstock having a cloud point that is reduced relative to a cloud point of the feedstock by at least about 5° C., the dewaxing conditions comprising a total pressure of about 200 psig (about 1.4 MPag) or less, a hydrogen partial pressure of about 100 psig (about 700 kPag) or less, and a treat gas rate of about 100 SCF/bbl (about 17 Nm/m) to about 5000 SCF/bbl (about 850 Nm/m) of a treat gas comprising about 5 vol % to about 50 vol % H.'}2. The method of claim 1 , wherein the vol % of Hin the treat gas is lower than a vol % of Hin a gaseous portion of the dewaxed effluent.3. The method of claim 1 , wherein the treat gas has a sulfur content of about 0.001 vol % or less.4. The method of claim 1 , wherein the dewaxing conditions further comprise a temperature of from about 500° F. (˜260° C.) to about 750° F. (˜399° C.) and a space velocity from about 0.3 hrto about 5.0 hr.5. The method of claim 1 , further comprising exposing a second feedstock to a hydrotreating catalyst to form a hydrotreated effluent claim 1 , and separating the hydrotreated effluent to form the distillate fuel boiling range feedstock.6. The method of claim 5 , wherein the effective hydrotreating conditions comprise a pressure from about 200 ...

FCC YIELD SELECTIVITY IMPROVEMENTS IN HIGH CONTAINMENT RISER TERMINATION SYSTEMS

The invention provides an improved system for separation technology intended to reduce unwanted catalyst/thermal reactions by minimizing contact of the hydrocarbons and the catalyst within the reactor. 1. The process for increasing hydrocarbon yield and decreasing coke production in an FCC reactor having a separation unit and at least one chamber window , wherein the bottom of the separation unit is spaced apart from a bed of fluidized catalyst , comprising the step of locating the bed of fluidized catalyst level in the FCC reactor such that the bed of fluidized catalyst is directly above the at least one chamber windows of the separation unit.2. The process of wherein the catalyst bed level falls within the range of 125 IWC to 170 IWC.3. The process of wherein the catalyst bed density is 32.8 lbs/ftat an operating level of 125 IWC at an elevation of 164 ft.4. The process of wherein the catalyst bed density is 36.9 lbs/ftat an operating level of 140 IWC at an elevation of 164 ft.5. The process of wherein the catalyst bed density is 41 lbs/ftat an operating level of 150 IWC at an elevation of 164 ft.6. The process of wherein the catalyst bed density is 45.1 lbs/ftat an operating level of 170 IWC at an elevation of 164 ft.7. The process of wherein the distance between the bottom of the separation unit and the top of the catalyst bed is maximized to prevent fluidized catalyst from entering the bottom of the separator unit.8. The process of wherein fluidized catalyst is prevented from entering the separation unit by means of a baffle member positioned between the bottom of the separation unit and the top of the fluidized bed.9. The process of wherein hydrocarbon gases evacuate from the fluidized bed after residence in the catalyst through at least one vent tube which carry the clean hydrocarbon gases directly to the top region of the separator unit.10. A process for increasing hydrocarbon yield and decreasing coke production in an FCC reactor having a separation unit ...

Multi-Stage Process and Device for Distributive Production of a Low Sulfur Heavy Marine Fuel Oil

A multi-stage process for the distributive production of an ISO8217 compliant Product Heavy Marine Fuel Oil from ISO 8217 compliant Feedstock Heavy Marine Fuel Oil involving a core desulfurizing process that is distributed in a Reaction System composed of multiple reaction vessels. The Product Heavy Marine Fuel Oil has a sulfur level has a maximum sulfur content (ISO 14596 or ISO 8754) between the range of 0.05 mass % to 1.0 mass. A process plant for conducting the process for conducting the distributive process is disclosed that can utilize a modular reactor vessel contained within a frame work based on ISO 40 foot or ISO 20 foot container dimensions. 1. A process for the distributive production of a Heavy Marine Fuel Oil , the process comprising: mixing a quantity of Feedstock Heavy Marine Fuel Oil with a quantity of Activating Gas mixture to give a Feedstock Mixture; contacting the Feedstock Mixture with one or more catalysts under reactive conditions in a Reaction System to form a Process Mixture from said Feedstock Mixture; receiving said Process Mixture and separating the liquid components of the Process Mixture from the bulk gaseous components of the Process Mixture; subsequently separating any residual gaseous components and by-product hydrocarbon components from the Product Heavy Marine Fuel Oil; and , discharging the Product Heavy Marine Fuel Oil; wherein the Reaction System comprises two or more reactor vessels wherein said reactor vessels are configured in a matrix of at least 2 reactors by 2 reactors.2. The process of wherein the Feedstock Heavy Marine Fuel Oil complies with ISO 8217 (2017) and has a sulfur content (ISO 14596 or ISO 8754) between the range of 5.0 mass % to 1.0 mass % and wherein the Product Heavy Marine Fuel Oil complies with ISO 8217 (2017) and has a sulfur content (ISO 14596 or ISO 8754) between the range of 0.50 mass % to 0.05 mass %.3. The process of claim 2 , wherein said Feedstock Heavy Marine Fuel Oil has: a maximum of kinematic ...

RECIRCULATING INERT GAS PURIFICATION APPARATUS USED WITH GLOVEBOXES, GLOVEBOXES INCORPORATING THE SAME AND METHODS OF USING THE SAME

An apparatus that may entirely be contained in a glovebox for the removal of at least one contaminant from an inert atmosphere. The apparatus includes a body, a media in the body for the removal of at least one of the contaminants from the inert atmosphere flowing through the media, a fan for causing the inert atmosphere to flow through the media and body, and a motor for driving the fan. The apparatus may be provided in combination with a glovebox. A method of purification of the inert atmosphere using such an apparatus is also provided. 1. An apparatus for the removal of at least one contaminant from an inert atmosphere , the apparatus comprising:a body;a media in the body for the removal of at least one of said contaminant from said inert atmosphere flowing through said media;a fan for causing said inert atmosphere to flow through said body and media; anda motor for driving said fan.2. The apparatus as recited in claim 1 , wherein said at least one contaminant is selected from the group consisting essentially of moisture claim 1 , oxygen claim 1 , solvent claim 1 , nitrogen and combinations thereof.3. The apparatus as recited in claim 1 , wherein the media is selected from the group of media consisting essentially of molecular sieve claim 1 , activated carbon claim 1 , silica gel desiccants claim 1 , copper catalysts and combinations thereof.4. The apparatus as recited in claim 1 , wherein the inert atmosphere is an atmosphere selected from the group consisting essentially of nitrogen claim 1 , argon claim 1 , neon claim 1 , helium claim 1 , combinations thereof claim 1 , and air combined with either of the aforementioned atmospheres.5. A glovebox with a purification apparatus combination comprising:a glovebox having an interior space; a body,', 'a media in the body for the removal of at least one contaminant from said inert atmosphere flowing through said media and body,', 'a fan for causing the inert atmosphere to flow through said media, and', 'a motor for ...

FLUID DISTRIBUTION DEVICE FOR MULTIBED REACTORS

A fluid distribution device is presented for the collection and distribution of fluid between reactor beds. According to various aspects, the device includes a collection tray, a mixing chamber in fluid communication with the collection tray, a rough distribution tray in fluid communication with the mixing chamber, and a fine distribution tray in fluid communication with the rough distribution tray. The rough distribution tray includes an overflow weir with an upper liquid retention baffle. 1. A device for the distribution of fluid over the top of a reactor bed , comprising:a collection tray having a top and a bottom, and having outlet ports therethrough;a mixing chamber in fluid communication with the collection tray outlet ports, and having a mixing chamber outlet;a rough distribution tray in fluid communication with the mixing chamber outlet and having rough distribution tray liquid outlet ports therethrough;an upstanding overflow weir at an outer edge portion of the rough distribution tray; andan upper liquid retention baffle of the overflow weir with at least a portion thereof extending radially inwardly from the overflow weir to retain fluid within the rough distribution tray.2. The device of wherein the liquid retention baffle includes a baffle having one edge portion joined to an upper end portion of the overflow weir and an opposite edge portion extending inwardly in a radial direction.3. The device of claim 2 , wherein the liquid retention baffle extends axially upward at an incline from the overflow weir upper end portion.4. The device of claim 2 , wherein the liquid retention baffle extends axially downwardly at a decline from the overflow weir upper end portion.5. The device of claim 2 , wherein the liquid retention baffle extends generally orthogonally from the overflow weir upper end portion.6. The device of claim 1 , wherein the upstanding overflow weir includes an axial height above the rough distribution tray of between about 80% and about 195% of ...

TUBE ISOTHERMAL CATALYTIC REACTOR

Vertical reactor () for chemical reactions, comprising a tube heat exchanger () immersed in a catalytic bed (), wherein said tube exchanger () comprises a plurality of straight tube bundles () with respective tube plates for feeding () and collecting () the heat exchange fluid, and wherein the tube bundles and the respective tube plates are vertically staggered so as to allow access to the shell side. 1. A vertical chemical reactor comprising at least a catalytic bed and a tube heat exchanger immersed in said catalytic bed and fed with a heat exchange fluid , wherein:said tube exchanger comprises a plurality of straight tube bundles, each tube bundle having a respective feed tube plate and a respective collection tube plate for the fluid,wherein said plurality of tube bundles comprises at least a first set of tube bundles arranged at a first height inside the reactor and a second set of tube bundles arranged at a second height inside the reactor, the bundles of the first set and the second set being alternated so that each tube bundle is staggered vertically with respect to the adjacent bundles,wherein said tube plates are shaped as circular sectors or ring sectors and each one of said sectors extend substantially along the full radial extension of said catalytic bed.2. The reactor according to claim 1 , wherein said tube plates have a surface of interface with the tubes claim 1 , which is flat.3. The reactor according to claim 1 , wherein the free spaces between adjacent tube plates claim 1 , due to the vertically staggered arrangement claim 1 , define access points to the reactor zone containing the catalytic bed claim 1 , which can be used for loading and unloading catalyst.4. The reactor according to claim 1 , wherein the tube plates claim 1 , viewed in cross-section claim 1 , cover the entire cross-section of the catalytic bed.5. The reactor according to claim 1 , wherein the tube bundles comprise straight tubes having the same length.6. The reactor according ...

FLAMELESS THERMAL OXIDIZER AND RELATED METHOD OF SHAPING REACTION ZONE

A flameless thermal oxidizer (FTO) includes at least one baffle constructed and arranged in a reaction chamber of the FTO to coact with a diptube of the FTO to radially expand a resulting “bubble” or reaction envelope from the diptube outward into a porous matrix of the FTO. A related method is also provided. 1. A flameless thermal oxidizer (FTO) , comprising:at least one baffle constructed and arranged in a reactive chamber of the FTO to coact with a diptube of the FTO to radiate and expand a resulting reaction envelope from the diptube outward into a porous matrix of the FTO.2. The FTO of claim 1 , wherein the at least one baffle is constructed from a material selected from the group consisting of an impermeable material claim 1 , and a semi-permeable material.3. The FTO of claim 1 , wherein the at least one baffle is positioned in the reactive chamber at a surface of the porous matrix.4. The FTO of claim 1 , wherein the reaction envelope comprises a bubble shape beneath the at least one baffle.5. The FTO of claim 1 , wherein the at least one baffle extends across a substantial portion of a surface area of the porous matrix.6. The FTO of claim 1 , wherein the at least one baffle is positioned in the reactive chamber below a surface of the porous matrix.7. The FTO of claim 6 , wherein the at least one baffle is positioned closer to an outlet of the diptube than the surface of the porous mixture.8. The FTO of claim 6 , wherein the at least one baffle is constructed from a material selected from the group consisting of an impermeable material claim 6 , and a semi-permeable material.9. The FTO of claim 1 , wherein the at least one baffle is an upper baffle positioned in the reactive chamber at a surface of the porous matrix claim 1 , and further comprising a lower baffle positioned in the reactive chamber below the surface of the porous mixture and spaced apart from the upper baffle.10. The FTO of claim 9 , wherein the upper and lower baffles each comprise similar ...

PROCESS AND APPARATUS FOR REACTING FEED WITH A FLUIDIZED CATALYST OVER A TEMPERATURE PROFILE

A fluidized catalytic reactor utilizes an ascending temperature profile. The apparatus and process deliver cooler spent catalyst to a first catalyst distributor and a hotter regenerated catalyst to a second catalyst distributor that are spaced apart from each other. The reactant stream first encounters the first stream of catalyst and then encounters the second stream of catalyst. The process and apparatus stage the addition of hot catalyst to the reactant stream. The process and apparatus may be particularly advantageous in an endothermic reaction because the hotter catalyst will encounter reactants that have cooled due to the progression of endothermic reactions. 1. A reactor for contacting a reactant stream with a catalyst comprising:a reactant distributor for distributing the reactant stream to the reactor;a first catalyst inlet for feeding a first stream of catalyst to the reactor;a second catalyst inlet for feeding a second stream of catalyst to the reactor, the first catalyst inlet being closer to the reactant distributor than the second catalyst inlet;a product outlet for discharging product from the reactor, the second catalyst distributor being closer to the reactant distributor than the product outlet.2. The reactor of further comprising a regenerated catalyst pipe connected to said second catalyst inlet claim 1 , the regenerated catalyst pipe having an inlet connected to a catalyst regenerator.3. The reactor of further comprising a reaction chamber containing said first catalyst inlet and said second catalyst inlet and a separation chamber comprising a primary catalyst separator for separating catalyst from product gases claim 1 , said primary catalyst separator being located closer to the second catalyst inlet than the product outlet.4. The reactor of further comprising a recycle catalyst pipe connected to said first catalyst inlet claim 3 , the recycle catalyst pipe having an inlet in the separation chamber.5. The reactor of further comprising a ...

SYSTEMS AND METHODS FOR IMPROVING FLOW IN RADIAL FLOW REACTOR

A scallop, center pipe, and outer basket for use in a radial flow reactor are provided. Each of the scallop, the center pipe, and the outer basket is formed of an elongated conduit having a top end and an opposing bottom end, and a plurality of openings formed in the elongated conduit through a thickness thereof. A diameter of the plurality of openings progressively increases or decreases from the top end to the opposing bottom end of the elongated conduit so as to allow a feedstock to flow radially out through the plurality of openings on the scallop or outer basket, or to allow a feedstock to flow uniformly into the center pipe through the plurality of openings. A system utilizing the center pipe together with either the scallop or the outer basket is also provided. 1. A scallop for use in a radial flow reactor , comprising:an elongated conduit having a top end and an opposing bottom end and a rounded distribution side;a plurality of openings formed in the elongated conduit through a thickness thereof,wherein a diameter of the plurality of openings progressively increases or decreases from the top end to the opposing bottom end of the elongated conduit so as to allow a feedstock to flow uniformly out of the scallop through the plurality of openings; anda profile wire scallop overlay positioned on the rounded distribution side of the elongated conduit to prevent catalyst particles from flowing into the scallop.2. The scallop of claim 1 , wherein the plurality of openings are generally circular claim 1 , square claim 1 , rectangular claim 1 , triangular claim 1 , oval claim 1 , or oblong in shape.3. The scallop of claim 1 , wherein the elongated conduit is formed of stainless steel.4. The scallop of claim 1 , wherein the elongated conduit has a back side and with the rounded distribution side forms a “D”-shaped cross section.5. (canceled)6. The scallop of claim 4 , wherein the radial flow reactor includes a reactor vessel claim 4 , and the back side of the elongated ...

Catalyst Reactor Basket

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

METASTABLE STATE MIXING

Metastable state spore incubation mixing systems are described. An example system includes a spore container to store spores, a nutrient container, an arrangement of valves and tubes, a reciprocating pump, a mixing tube, and a holding tank. In a drawing phase of the system, a controller can control the reciprocating pump to draw a ratioed volume of the spores, the nutrients, and water through the valves and tubes. During an expelling phase of the system, the controller can control flow control valves to direct the spores, nutrients, and water through the mixing tube and into the holding tank. The controller can also direct a heater to heat the mixture in the holding tank to a predetermined temperature. Once the mixture reaches the temperature, the controller can also direct the system through a number of other phases of operation, including cooling and purging phases. 1. A method , comprising:drawing, via a reciprocating pump operated by a controller, a volume of a solution of spores from a spore container, a volume of a solution of nutrients from a nutrient container, and a volume of water through an arrangement of valves and tubes;expelling, via the reciprocating pump, the volume of the solution of spores, the volume of the solution of nutrients, and the volume of water from the reciprocating pump to a mixing tube;mixing, via the mixing tube, the volume of the solution of spores, the volume of the solution of nutrients, and the volume of water together into a mixture of the spores, the nutrients, and the water;providing the mixture of the spores, the nutrients, and the water to a holding tank from the mixing tube; andheating, via a heater operated by the controller, the mixture of the spores, the nutrients, and the water in the holding tank, wherein a thermocouple is used to measure a temperature of the mixture in the holding tank.2. The method of claim 1 , wherein the arrangement of valves and tubes comprises a number of flow control valves claim 1 , a number of ...

Method and apparatus for discharging a polymer from a gas-phase reactor

Process for discharging polyolefin particles from a gas-phase polymerization reactor of a pressure from 1.0 MPa to 10 MPa to a discharge vessel of a pressure from 0.1 MPa to 1.0 MPa wherein the discharging is carried out discontinuously through at least two discharge lines in which the polyolefin particles are transported horizontally or upwards, process for polymerizing olefins at temperatures of from 30° C. to 160° C. and pressures of from 1.0 MPa to 10 MPa in the presence of a polymerization catalyst in a gas-phase polymerization reactor comprising discharging the obtained polyolefin particles from the gas-phase polymerization reactor by the process for discharging polyolefin particles and apparatus for polymerizing olefins in the gas-phase comprising a polymerization reactor, a discharge vessel and at least two pipes connecting the polymerization reactor and the discharge vessel for discharging polyolefin particles, wherein the discharge lines are constructed in a way that the polyolefin particles conveyed from the polymerization reactor to the discharge vessel are transported horizontally or upwards.

MULTILAYER CATALYTIC BED FOR THE PARTIAL OXIDATION OF N-BUTANE TO MALEIC ANHYDRIDE

A catalytic bed for the partial oxidation of n-butane to maleic anhydride which comprises at least one first catalytic layer and at least one second catalytic layer, wherein each catalytic layer consists of a vanadium and phosphorus mixed oxide (VPO) catalyst and only the catalyst of the second catalytic layer further comprises tungsten, and wherein the second catalytic layer constitutes 25% to 45% of the total length of the catalytic bed and is arranged consecutively after the first catalytic layer along the direction in which the mixture of gases comprising the oxidation reagents flows. The present invention also relates to a process for producing maleic anhydride by partial oxidation of n-butane which uses the catalytic bed. 1. A catalytic bed for the partial oxidation of n-butane to maleic anhydride comprising a first catalytic layer and a second catalytic layer , wherein{'sub': 2', '2', '7, 'the first catalytic layer and the second catalytic layer consist of a vanadium and phosphorus mixed oxide (VPO) catalyst comprising vanadyl pyrophosphate (VO)POas main component and only the VPO catalyst of the second catalytic layer further comprises tungsten,'}the second catalytic layer constitutes 25% to 45% of the total length of the catalytic bed and is arranged consecutively after the first catalytic layer, so that a mixture of gases comprising n-butane and oxygen flows first through the first catalytic layer and then through the second catalytic layer, andthe VPO catalyst of the second catalytic layer comprises tungsten in an amount corresponding to an atomic ratio of vanadium to tungsten between 250:1 and 60:1.2. The catalytic bed according to claim 1 , wherein the second catalytic layer constitutes 36% of the total length of the catalytic bed.3. The catalytic bed according to claim 1 , wherein the VPO catalyst of the second catalytic layer comprises tungsten in an amount corresponding to an atomic ratio of vanadium to tungsten of 100:1.4. The catalytic bed ...

GRAPHENE MANUFACTURING DEVICE AND GRAPHENE MANUFACTURING METHOD USING SAME

A graphene manufacturing device using Joule heating includes: a chamber having a space provided therein so as to synthesize graphene; and a first roller portion and a second roller portion disposed inside the chamber to be spaced from each other such that same support a catalyst metal penetrating the interior of the chamber and are supplied with an electric current for graphene synthesis, thereby Joule-heating the catalyst metal. In order to compensate for a temperature deviation of the catalyst metal passing between the first roller portion and the second roller portion, a first area of the catalyst metal, which is close to the first roller portion, and a second area of the catalyst metal, which is close to the second roller portion, are disposed to have movement paths facing each other. 1. A graphene manufacturing device comprising:a chamber having an inner space for graphene synthesis; anda first roller unit and a second roller unit disposed in the chamber with a distance therebetween, supporting a catalytic metal passing through an inside of the chamber, and heating the catalytic metal by Joule heating using electric current supplied thereto for graphene synthesis,wherein a first region of the catalytic metal close to the first roller unit and a second region of the catalytic metal close to the second roller unit are positioned to have respective movement paths facing each other to compensate for temperature variation in the catalytic metal passing through a section between the first roller unit and the second roller unit.2. The graphene manufacturing device according to claim 1 , wherein the first region and the second region have the respective movement paths facing each other as the catalytic metal sags between the first roller unit and the second roller unit.3. The graphene manufacturing device according to claim 2 , further comprising:a displacement sensor disposed below the first roller unit and the second roller unit and detecting whether a sagging length ...

FILTER FOR CHEMICAL REACTORS

A chemical reactor is implemented on a substrate and has an inlet for receiving a fluid and/or a gas; a filter element for reducing or preventing that materials cause a blockage in the fluid supplied and/or the gas supplied in a part of the chemical reactor located further away; and a part located further away for transporting and/or processing the fluid and/or the gas. The part located further away has a depth dlow smaller than the depth dhigh of the inlet. The filter element has a first duct part and a second duct part; the first duct part is positioned closer up against the inlet than the second duct part, the first duct part is deeper than the second duct part, the first duct part has a diverging width and is free from pillar structures, and the second duct part is filled with filter pillars. 116.-. (canceled)17. A chemical reactor implemented on a substrate , the chemical reactor comprising:an inlet for receiving a fluid and/or a gas, wherein the inlet has a first depth dhigh and has been adjusted to accommodate a capillary,a filter element for reducing or preventing that materials cause a blockage in the fluid and/or gas supplied in a part of the chemical reactor located further away, anda part located further away for transporting and/or processing the fluid and/or the gas, wherein the part located further away has a depth dlow smaller than depth dhigh of the inlet,whereinthe filter element comprises a first duct part and a second duct part, whereinthe first duct part is positioned closer up against the inlet than the second duct part,the first duct part has a greater depth than a depth of the second duct part,the first duct part has a diverging width so that the first duct part has a widening of the width in a downstream direction from the duct inlet towards the part located further away and the first duct part is free from pillar structures, andthe second duct part is filled with filter pillars.18. The chemical reactor according to claim 17 , in which the ...

TOWER BOTTOMS COKE CATCHING DEVICE

A coke catching apparatus for use in hydrocarbon cracking to assist in the removal of coke and the prevention of coke build up in high coking hydrocarbon processing units. The apparatus includes a grid device for preventing large pieces of coke from entering the outlet of the process refining equipment while allowing small pieces of coke to pass through and be disposed of The coke catching apparatus can be easily disassembled to be removed from the refining process equipment and cleaned. 1. A coke catching apparatus to remove of coke in a liquid petroleum product when being processed in a petroleum product processing unit , prior to output of a refined liquid petroleum product , the coke catching apparatus comprising:a grid device having a bottom section, a grid portion having a first section positioned proximate the bottom section and a second section positioned proximate the first section of the grid portion, and a top section positioned proximate the second section of the grid portion, the grid portion including a plurality of openings, the grid device also being configured to be positioned within the petroleum product processing unit to catch coke in the liquid petroleum product when passing through the grid device and being positioned to have the bottom section proximate to an outlet of the petroleum product processing unit, the bottom section including a bottom plate of a substantially solid material and a plurality of drain holes to allow for refined liquid petroleum product to exit the outlet of the petroleum product processing unit, the plurality of openings of the grid portion of the grid device being sized to allow small pieces of coke contained in the liquid petroleum product when within the petroleum product processing unit to pass through the bottom section of the grid device to the outlet while preventing large pieces of coke contained in the liquid petroleum product from passing through when the liquid petroleum product flows into the grid device and ...

Gas Collection Apparatus

The disclosure provides a gas collection apparatus. The present apparatus may be used, for example, in a system for producing biocoal or biochar or bio-oil from biomass. The present gas collection apparatus may be part of a thermochemical biomass reactor. The present gas collection apparatus may be part of a syngas management system. Embodiments of the present disclosure relate to a gas collection apparatus for fluidly communicating with a retort of a biomass reactor, said collection apparatus comprising two or more gas collection pipes in fluid communication with spaced apart sections of said retort; and a gas collection manifold in fluid communication with said pipes. The gas collection apparatus is designed such that the gases collected by one pipe do not mix with those collected by another within the piping network.

METHOD TO PRODUCE LIGHT HYDROCARBONS BY COx HYDROGENATION IN A DIELECTRIC BARRIER DISCHARGE PLASMA REACTOR SYSTEM

The present invention relates to a dielectric barrier discharge (DBD) plasma reactor comprising a catalyst bed for COX hydrogenation in a discharge region; and a method to produce light hydrocarbons from a COX-containing gas mixture in the DBD plasma reactor. In the DBD plasma reactor for a COX hydrogenation reaction, the catalyst for COX hydrogenation comprises a catalytically active component on a mesoporous support that is a dielectric. When the DBD plasma reactor for a COX hydrogenation reaction according to the present invention is used, it is possible to convert by-product gases or waste gases into higher-value-added chemical products without additional heat supply from the outside.

CORE-SHELL CATALYST FOR NATURAL GAS REFORMING

A natural gas reforming catalyst includes a metal core and rhodium deposited on the metal core. A natural gas reformer includes a hydrocarbon inlet, a reforming catalyst for generating hydrogen from a hydrocarbon and water and a hydrogen outlet. The reforming catalyst includes a metal core and a rhodium layer deposited on the metal core. A method for preparing a natural gas reforming catalyst includes adding a rhodium compound and a metal core to a reaction vessel and depositing the rhodium compound on the metal core. 1. A natural gas reforming catalyst comprising:a metal core; andrhodium deposited on the metal core.2. The natural gas reforming catalyst of claim 1 , wherein the metal core comprises nickel.3. The natural gas reforming catalyst of claim 1 , wherein the metal core comprises palladium.4. The natural gas reforming catalyst of claim 1 , wherein the rhodium is alloyed with a metal selected from the group consisting of platinum claim 1 , palladium claim 1 , iridium and combinations thereof.5. The natural gas reforming catalyst of claim 1 , wherein the rhodium is deposited on the metal core as a monolayer.6. The natural gas reforming catalyst of claim 5 , wherein the rhodium monolayer has a thickness of about 0.25 nanometers.7. The natural gas reforming catalyst of claim 1 , wherein the rhodium is deposited on the metal core as a submonolayer.8. The natural gas reforming catalyst of claim 7 , wherein the metal core has a surface claim 7 , and wherein rhodium covers between about 10% and about 80% of the surface of the metal core.9. The natural gas reforming catalyst of claim 8 , wherein rhodium covers between about 10% and about 100% of the surface of the metal core.10. The natural gas reforming catalyst of claim 1 , wherein multiple layers of rhodium are deposited on the metal core.11. The natural gas reforming catalyst of claim 10 , wherein the multiple layers of rhodium have a combined thickness between about 0.5 nanometers and about 3 nanometers.12. A ...

METHODS AND APPARATUSES FOR REGENERATING CATALYST PARTICLES

Apparatuses and methods are provided for regenerating catalyst particles. In one embodiment, a method for regenerating catalyst particles includes passing the catalyst particles through a halogenation zone and a drying zone. The method feeds drying gas to the drying zone and passes a first portion of the drying gas from the drying zone to the halogenation zone. The method includes removing a second portion of the drying gas from the drying zone and injecting a halogen gas into the second portion of the drying gas. Further, the method includes delivering the halogen gas and the second portion of the drying gas to the halogenation zone. In the method, substantially all of the drying gas fed to the drying zone enters the halogenation zone. 1. A method for regenerating catalyst particles , the method comprising the steps of:passing the catalyst particles through a halogenation zone and a drying zone;feeding drying gas to the drying zone;passing a first portion of the drying gas from the drying zone to the halogenation zone;removing a second portion of the drying gas from the drying zone;injecting a halogen gas into the second portion of the drying gas; anddelivering the halogen gas and the second portion of the drying gas to the halogenation zone, wherein substantially all of the drying gas fed to the drying zone enters the halogenation zone.2. The method of wherein the halogenation zone and the drying zone are located in a vessel claim 1 , and wherein removing the second portion of the drying gas from the drying zone comprises removing the second portion of the drying gas from the vessel.3. The method of wherein delivering the halogen gas and the second portion of the drying gas to the halogenation zone comprises delivering the halogen gas and the second portion of the drying gas to the vessel.4. The method of further comprising passing the second portion of the drying gas through an external tunnel from the drying zone to the halogenation zone claim 3 , wherein ...

MICROCHEMICAL SYSTEM APPARATUS AND RELATED METHODS OF FABRICATION

The disclosure relates to microchemical (or microfluidic) apparatus as well as related methods for making the same. The methods generally include partial sintering of sintering powder (e.g., binderless or otherwise free-flowing sintering powder) that encloses a fugitive phase material having a shape corresponding to a desired cavity structure in the formed apparatus. Partial sintering removes the fugitive phase and produces a porous compact, which can then be machined if desired and then further fully sintered to form the final apparatus. The process can produce apparatus with small, controllable cavities shaped as desired for various microchemical or microfluidic unit operations, with a generally smooth interior cavity finish, and with materials (e.g., ceramics) able to withstand harsh environments for such unit operations. 1. A method for forming a microchemical apparatus , the method comprising:(a) providing a first metal oxide powder;(b) placing a first fugitive phase material in the first metal oxide powder, the first fugitive phase material having a geometry corresponding to a negative cavity geometry in the formed microchemical apparatus;(c) placing a second metal oxide powder over the first metal oxide powder and over the first fugitive phase material;(d) partially sintering the first metal oxide powder and the second metal oxide powder at a temperature and pressure sufficient (i) to convert the first fugitive phase material to a gaseous material and (ii) to convert the first metal oxide powder and the second metal oxide powder to a porous, partially sintered compact, thereby allowing the gaseous material to escape from the partially sintered compact interior volume and forming an interior cavity within the partially sintered compact interior volume having a geometry corresponding to the original first fugitive phase material geometry;(e) optionally machining the partially sintered compact; and(f) fully sintering the partially sintered compact at a ...

REFORMER FLUE GAS TUNNEL AND REFRACTORY COMPONENTS THEREFOR

A refractory block for a steam reformer furnace tunnel includes a hollow main body, at least one first mechanical mating member defining a protruded portion extending from an upper surface of the main body, at least one second corresponding mechanical mating member defining an opening corresponding to the protruded portion formed in a portion of a lower surface of the main body, at least one third mechanical mating member defining a tab provided in a portion one of a first end and an opposed second end or a first side and an opposed second side of the main body, at least one fourth mechanical mating member comprising a groove formed in the other of the first end and the second end or the first side and the opposed second side of the main body, and at least one cavity formed in the lower surface of the main body. 1. A refractory tunnel assembly for a steam reformer furnace , said tunnel assembly comprising:a plurality of hollow base components, each said base component comprising a plurality of corresponding mechanical mating members;a plurality of hollow wall blocks, each said wall block comprising a plurality of corresponding mechanical mating members that further correspond to said mechanical mating members of said base components; anda plurality of hollow lid components, each said lid component comprising a plurality of mechanical mating members that further correspond to said mechanical mating members of said base components and said wall blocks;wherein said base components are arranged to extend in a horizontal arrangement direction defining a width of said tunnel assembly and a longitudinal arrangement direction defining a length of the tunnel assembly;wherein said wall blocks are stacked upon and mechanically interconnected to said base components via said corresponding mechanical mating members, without the use of mortar, in a vertical arrangement direction and along said longitudinal arrangement direction, and are stacked upon one and mechanically ...

REFORMED GAS CONSUMING PLANT AND SOURCE GAS REFORMING METHOD

A plant that consumes a reformed gas obtained by reforming a source gas including at least methane and carbon dioxide includes: a reforming device that includes a reforming catalyst for reforming the source gas and an electric power supply member for supplying electric power to the reforming catalyst and that supplies electric power to the reforming catalyst to reform the source gas; and a reformed gas consuming apparatus that consumes the reformed gas A reaction temperature of a reforming reaction of the source gas in the reforming device can be adjusted by adjusting a supply amount of a heating medium including exhaust heat generated due to consumption of the reformed gas in the reformed gas consuming apparatus to the reforming device when heat exchange between the source gas and the heat medium is performed in the reforming gas. 1. A plant that consumes a reformed gas obtained by reforming a source gas including at least methane and carbon dioxide , the plant comprising:a reforming device including a reforming catalyst for reforming the source gas and an electric power supply member for supplying electric power to the reforming catalyst, the reforming device being configured to supply electric power to the reforming catalyst to reform the source gas; anda reformed gas consuming apparatus configured to consume the reformed gas, whereina reaction temperature of a reforming reaction of the source gas in the reforming device is adjustable by adjusting a supply amount of a heating medium to the reforming device when heat exchange between the source gas and the heat medium is performed in the reforming gas, the heat medium including exhaust heat generated due to consumption of the reformed gas in the reformed gas consuming apparatus.2. The plant according to claim 1 , whereinthe reformed gas consuming apparatus is a methanol synthesis apparatus in which the reformed gas is consumed as a raw material of synthesis of a methanol, andthe reforming reaction of the source ...

Multimodal polyethylene pipe

The present invention relates to a reactor system for a multimodal polyethylene polymerization process, comprising; (a) first reactor; (b) a hydrogen removal unit arranged between the first reactor and a second reactor comprising at least one vessel connected with a depressurization equipment, preferably selected, from vacuum pump, compressor, blower, ejector or a combination thereof, the depressurization equipment allowing to adjust an operating pressure to a pressure in a range of 100-200 kPa (abs); (c) the second reactor; and (d) a third reactor and use thereof as a pipe.

METHOD FOR PRODUCING OLIGOSILANE

A method for producing an oligosilane including a reaction step of introducing a fluid containing a hydrosilane into a continuous reactor provided with a catalyst layer inside to produce an oligosilane from the hydrosilane and discharging a fluid containing the oligosilane from the reactor. The reaction step satisfies all of the following conditions (i) to (iii): (i) a temperature of the hydrosilane-containing fluid at an inlet of the catalyst layer is higher than a temperature of the oligosilane-containing fluid at an outlet of the catalyst layer; (ii) the temperature of the hydrosilane-containing fluid at the inlet of the catalyst layer is from 200 to 400° C.; and (iii) the temperature of the oligosilane-containing fluid at the outlet of the catalyst layer is from 50 to 300° C. 1. A method for producing an oligosilane , comprising a reaction step of introducing a fluid containing a hydrosilane into a continuous reactor provided with a catalyst layer inside to produce an oligosilane from the hydrosilane and discharging a fluid containing the oligosilane from the reactor , whereinthe reaction step satisfies all of the following conditions (i) to (iii):(i) a temperature of the hydrosilane-containing fluid at an inlet of the catalyst layer is higher than a temperature of the oligosilane-containing fluid at an outlet of the catalyst layer;(ii) the temperature of the hydrosilane-containing fluid at the inlet of the catalyst layer is from 200 to 400° C.; and(iii) the temperature of the oligosilane-containing fluid at the outlet of the catalyst layer is from 50 to 300° C.2. The method for producing an oligosilane according to claim 1 , whereinthe temperature of the hydrosilane-containing fluid at the inlet of the catalyst layer is from 10 to 200° C. higher than the temperature of the oligosilane-containing fluid at the outlet of the catalyst layer.3. The method for producing an oligosilane according to claim 1 , whereinthe hydrosilane-containing fluid is a gas containing ...

Methods and apparatus for fluid contacting in a downflow vessel

A contacting device and method are presented for the collection, contacting, and distribution of fluids between particulate beds of a downflow vessel, which may operate in co-current flow. By one approach, the contacting device includes a liquid collection tray, a mixing channel in fluid communication with the liquid collection tray, and a liquid distribution zone.

REFORMER FLUE GAS TUNNEL AND REFRACTORY COMPONENTS THEREFOR

A refractory block for a steam reformer furnace tunnel includes a hollow main body, at least one first mechanical mating member defining a protruded portion extending from an upper surface of the main body, at least one second corresponding mechanical mating member defining an opening corresponding to the protruded portion formed in a portion of a lower surface of the main body, at least one third mechanical mating member defining a tab provided in a portion one of a first end and an opposed second end or a first side and an opposed second side of the main body, at least one fourth mechanical mating member comprising a groove formed in the other of the first end and the second end or the first side and the opposed second side of the main body, and at least one cavity formed in the lower surface of the main body. 1. A refractory tunnel assembly for a steam reformer furnace , said tunnel assembly comprising:a plurality of hollow base components, each said base component comprising a plurality of corresponding mechanical mating members;a plurality of hollow wall blocks, each said wall block comprising a plurality of corresponding mechanical mating members that further correspond to said mechanical mating members of said base components; anda plurality of hollow lid components, each said lid component comprising a plurality of mechanical mating members that further correspond to said mechanical mating members of said base components and said wall blocks;wherein said base components are arranged to extend in a horizontal arrangement direction defining a width of said tunnel assembly and a longitudinal arrangement direction defining a length of the tunnel assembly;wherein said wall blocks are stacked upon and mechanically interconnected to said base components via said corresponding mechanical mating members, without the use of mortar, in a vertical arrangement direction and along said longitudinal arrangement direction, and are stacked upon one and mechanically ...

Radial Flow Adsorption Vessel Comprising Flexible Screen

The present invention pertains to a radial flow adsorption vessel comprising a cylindrical outer shell and at least one cylindrical porous wall disposed co-axially inside the shell, wherein inside the shell one or more fluid permeable screens are rigidly connected to the at least one cylindrical porous wall, by a multitude of separate standoff elements so that the screen has a cylindrical shape co-axial to the shell, and to an adsorption process using the radial flow adsorption vessel. 1. A radial flow adsorption vessel comprising a cylindrical outer shell and at least one cylindrical porous wall disposed co-axially inside the shell , wherein inside the shell one or more fluid permeable screens are rigidly connected to the at least one porous wall by a multitude of separate standoff elements so that the screen has a cylindrical shape co-axial to the shell.2. Radial flow adsorption vessel according to wherein the screen comprises a mesh wire claim 1 , woven wire cloth or an expanded metal.3. Radial flow adsorption vessel according to or wherein the screen comprises a material having a stiffness of less than 35 Nm.4. Radial flow adsorption vessel according to any of the preceding claims comprising at least an inner and an outer cylindrical porous wall disposed co-axially inside the shell and wherein the fluid permeable screen is rigidly connected to one of the porous walls by the multitude of separate standoff elements so that the screen has a cylindrical shape co-axial to the shell.5. Radial flow adsorption vessel according to any of the preceding claims wherein the standoff elements are mounted so that they have their smallest extension in the plane perpendicular to the filling direction of the adsorbent particles.6. Radial flow adsorption vessel according to any of the preceding claims wherein the edges of the standoff elements pointing in the filling direction of the adsorbent particles are tapered.7. Radial flow adsorption vessel according to any of the preceding ...

MACHINE AND METHODS FOR TRANSFORMING BIOMASS AND/OR WASTE PLASTICS VIA SUPERCRITICAL WATER REACTION

The machinery and methods disclosed herein are based on the use of a specialized extruder configured to continuously convey and plasticize/moltenize selected lignocellulosic biomass and/or waste plastic materials into a novel variable volume tubular reactor, wherein the plasticized/moltenized material undergoes reaction with circumferentially injected supercritical water—thereby yielding valuable simple sugar solutions and/or liquid hydrocarbon mixtures (e.g., “neodiesel”), both of which are key chemical commodity products. The reaction time may be adjusted by changing the reactor volume. The machinery includes four zones: (1) a feedstock conveyance and plasticization/moltenization zone; (2) a steam generation and manifold distribution zone; (3) a central supercritical water reaction zone; and (4) a pressure let-down and reaction product separation zone. The machinery and methods minimize water usage—thereby enabling the economic utilization of abundant biomass and waste plastics as viable renewable feedstocks for subsequent conversion into alternative liquid transportation fuels and valuable green-chemical products. 1. (canceled)2. (canceled)3. (canceled)4. (canceled)5. (canceled)6. (canceled)7. (canceled)8. (canceled)9. (canceled)10. (canceled)11. (canceled)12. (canceled)13. A machine for transforming a selected polymeric material into a plurality of reaction products via supercritical water reaction , comprising:an extruder having an inlet and a downstream outlet, wherein the downstream outlet is coincident with the longitudinal axis of the extruder;a steam generator fluidically connected to a downstream inlet manifold;a tubular reactor having an interior space fluidically connected to an inlet end and an outlet end, wherein the inlet end of the tubular reactor is fluidically connected to both (i) the outlet of the extruder, and the inlet manifold, and wherein the outlet end of the tubular reactor is fluidically connected to;a first downstream chamber; and ...

Multimodal polyethylene screw cap

The present invention relates to a multimodal polyethylene composition comprising: (A)35 to 65 parts by weight, preferably 45 to 65 parts by weight, most preferred 50 to 60 parts by weight, of the low molecular weight polyethylene having a weight average molecular weight (Mw) of 20,000 to 90,000 g/mol; (B) 5 to 40 parts by weight, preferably 5 to 30 parts by weight, most preferred 5 to 20 parts by weight, of the first high molecular weight polyethylene having a weight average molecular weight (Mw) of more than 150,000 to 1,000,000g/mol or the first ultra high molecular weight polyethylene having a weight average molecular weight (Mw) of more than 1,000,000 to 5,000,000g/mol; and (C) 20 to 60 parts by weight, preferably 25 to 60 parts by weight, most preferred 35 to 55 parts by weight, of the second high molecular weight polyethylene having a weight average molecular weight (Mw) of more than 150,000 to 1,000,000g/mol or the second ultra high molecular weight polyethylene having a weight average molecular weight (Mw) of more than 1,000,000 to 5,000,000g/mol, wherein the molecular weight distribution of the multimodal polyethylene composition is from 10 to 25, preferably 10 to 20, determined by Gel Permeation Chromatography; the isothermal crystallization half-time of the multimodal polyethylene composition at a temperature of 123° C. is 7 min or less, preferably 6 min or less, preferably 2- 6 min, according to Differential Scanning Calorimetry; and a spiral flow length at a temperature of 220° C. is at least 200 mm, preferably 250-400 mm and a screw cap comprising the same.

METHOD OF MAKING A PACKAGED FUEL UNIT FOR A HYDROGEN GENERATOR

A method of making a package for a fuel unit, a fuel unit including the package, and a hydrogen generator including one or more of the fuel units are disclosed. The package includes a package strip made by forming apertures in a nonconductive substrate strip, forming conductor sections in a conductor strip, aligning the substrate and conductor strips, bonding the conductor sections to the substrate strip to cover the apertures, and removing non-bonded portions of the conductor strip. A package enclosing a hydrogen generating reactant is formed by securing a segment of the package strip to itself, to one or more other segments and/or to one or more other package components. One or more conductor sections in the package strip are in thermal contact with one or more quantities of reactant composition so heat can be transferred thermally decompose the reactant composition and generate hydrogen gas. 1. A method of making a package for a hydrogen generator fuel unit , the method comprising the steps:(a) providing a substrate strip made of an electrically nonconductive material with a thermal conductivity less than 10 watts/meter·Kelvin;(b) forming an array of apertures in the substrate strip;(c) providing a conductor strip made of an electrically conductive material with a thermal conductivity greater than 10 watts/meter·Kelvin;(d) forming an array of conductor sections in the conductor strip;(e) aligning individual conductor sections in the conductor strip with apertures in the substrate strip;(f) bonding a peripheral portion of each of the individual conductor sections to a portion of the substrate strip surrounding one or more of the apertures to form a bonded strip; and,(g) removing nonbonded portions of the conductor strip from around the bonded conductor sections of the bonded strip to form a package strip.2. The method according to claim 1 , wherein the substrate strip is made from at least one high temperature polymer claim 1 , the high temperature polymer having ...

FUEL REFORMER WITH THERMAL MANAGEMENT

A fuel reformer includes a feedstream delivery unit and a catalytic reactor. The feedstream delivery unit is configured to receive reactants and to provide the reactants to the catalytic reactor. The reformer further includes a flame arrestor disposed between the feedstream delivery unit and the catalytic reactor, and at least one spacer disposed between the feedstream delivery unit and the catalytic reactor, wherein the spacer is configured to allow the reactants to flow therethrough while inhibiting thermal radiation therethrough. In a further aspect, the surfaces of the feedstream delivery unit that come into contact with the reactants in use include coatings that eliminate catalytic reactions of the feedstream within the feedstream delivery unit. 1. A fuel reformer comprising a feedstream delivery unit and a catalytic reactor , the feedstream delivery unit configured to receive reactants through an inlet port and to provide the reactants to the catalytic reactor , said reformer further comprising:a flame arrestor disposed between the inlet port of the feedstream delivery unit and the catalytic reactor;at least one spacer disposed between the inlet port of the feedstream delivery unit and the catalytic reactor, said spacer configured to allow the reactants to flow therethrough while inhibiting thermal radiation therethrough.2. The fuel reformer of claim 1 , wherein the flame arrestor defines a plurality of channels therethrough claim 1 , wherein the channels are configured such that the velocity of reactants flowing therethrough from the inlet port of the feedstream delivery unit to the catalytic reactor is sufficient to inhibit propagation of combustion from the catalytic reactor to the feedstream delivery unit.3. The fuel reformer of claim 1 , wherein the spacer comprises a ceramic material.4. The fuel reformer of claim 3 , wherein the spacer comprises ceramic paper or ceramic cloth.5. The fuel reformer of further comprising a substrate disposed between the ...

PREPARATION METHOD FOR CERAMIC COMPOSITE MATERIAL, CERAMIC COMPOSITE MATERIAL, AND WAVELENGTH CONVERTER

Provided is a ceramic composite material and a wavelength converter. The ceramic composite material includes: an alumina matrix, a fluorescent powder uniformly distributed in the alumina matrix, and scattering centers uniformly distributed in the alumina matrix, wherein the alumina matrix is an alumina ceramics, the scattering centers are alumina particles, the alumina particles each have a particle diameter of 1 μm to 10 μm, and the fluorescent powder has a particle diameter of 13 μm to 20 μm.

EXHAUST SYSTEM FOR A STEAM REFORMER AND BEARING THEREFOR

An exhaust system for a steam reformer comprises at least one longitudinal collecting tube, wherein along the longitudinal axis of the longitudinal collecting tube ports for connection to catalyst tubes are provided, which in the connected condition are aligned parallel to each other and vertically to the longitudinal collecting tube, a transverse collector which is connected to the at least one longitudinal collecting tube and has a longitudinal axis which extends vertically to the at least one longitudinal collecting tube and vertically to the catalyst tubes, wherein the longitudinal collecting tube is formed as hot exhaust system and the transverse collector is formed as cold exhaust system. The transverse collector is arranged on a side of the longitudinal collecting tube facing away from the ports centrally to the longitudinal collecting tube. 1. An exhaust system for a steam reformer , comprising:a hot exhaust system comprising at least one longitudinal collecting tube;catalyst tubes aligned parallel to each other and orthogonally to the longitudinal collecting tube;a plurality of ports disposed along the longitudinal axis of a first side of the longitudinal collecting tube, wherein each port is configured to connect to a respective catalyst tube, wherein the ports are arranged such that in the connected condition, the catalyst tubes are aligned parallel to each other and orthogonally to the longitudinal collecting tube;a cold exhaust system comprising a transverse collector which is fluidly connected to a second side of the at least one longitudinal collecting tube and has a longitudinal axis which extends orthogonally to the at least one longitudinal collecting tube and orthogonally to the catalyst tubes,wherein the second side of the longitudinal collecting tube is opposite of the first side the longitudinal collecting tube, wherein the transverse collector is disposed centrally to the longitudinal collecting tube.2. A bearing system for supporting an ...

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

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

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

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

CARBON MONOXIDE OXIDATION DEVICE

A carbon monoxide oxidation device for oxidizing carbon monoxide contained in a hydrogen rich reformat gas includes a housing, wherein the housing incorporates an oxidation catalyst, which is adapted to oxidize the carbon monoxide of the reformat gas by an oxidizing agent to carbon dioxide, includes upstream of the catalyst at least one gas inlet for providing a gas stream of at least the reformat gas into the housing, includes downstream of the catalyst a gas outlet for exiting treated gas from the housing, and incorporates a gas stream perturbation device which is arranged upstream of the catalyst and which is adapted to provide a perturbation in the gas stream, wherein the gas stream perturbation device is designed as at least one propeller-shaped plate with a plate portion having a surface facing the gas stream and at least one blade which is connected to the plate portion and has a leading edge and an effluent edge, wherein a surface defined between leading edge and effluent edge is inclined in relation to the surface of the plate portion with a predetermined blade inclination angle, thereby defining at least one opening in the plate. 1. Water gas shift reactor or preferential oxidation reactor , which purifies a carbon monoxide containing hydrogen rich reformat gas from carbon monoxide contained in the carbon monoxide containing hydrogen rich reformate gas , wherein the water gas shift reactor or the preferential oxidation reactor comprises a housing , wherein the housinga. incorporates an oxidation catalyst, which oxidizes the carbon monoxide of the carbon monoxide containing hydrogen rich reformat gas by means of an oxidizing agent to carbon dioxide,b. comprises upstream of the catalyst at least one gas inlet for providing a gas stream (B; C) of at least the carbon monoxide containing hydrogen rich reformat gas into the housing,c. comprises downstream of the catalyst a gas outlet for exiting purified hydrogen rich gas from the housing, andd. incorporates a ...

FINE PARTICLE MANUFACTURING DEVICE

The present disclosure provides an apparatus for producing fine particles, the apparatus comprising: a particle formation mechanism and a particle-outlet micro-channel. The particle formation mechanism may include a unit-structure, wherein the unit-structure includes: first and second portions adjacent to each other; a first inlet defined in the first portion at a first height, wherein a continuous phase solution is injected into the first inlet; a second inlet defined in the first portion at a second height different from the second height, wherein a dispersed phase solution is injected into the second inlet; a merging volume defined in the second portion adjacent to the first portion, wherein the merging volume is defined at third height, wherein the third height is equal to either the first height and the second height, or has a value between the first height and the second height, wherein the continuous phase solution and the dispersed phase solution are merged in the merging volume, wherein fine particles are formed via the merging between the continuous phase solution and the dispersed phase solution in the merging volume; and a first micro-channel and a second micro-channel branching from the merging volume so as to be in communication with the first inlet and the second inlet, respectively. 1. An apparatus for producing fine particles , the apparatus comprising: first and second portions adjacent to each other;', 'a first inlet defined in the first portion at a first height, wherein a continuous phase solution is injected into the first inlet;', 'a second inlet defined in the first portion at a second height different from the second height, wherein a dispersed phase solution is injected into the second inlet;', 'a merging volume defined in the second portion adjacent to the first portion, wherein the merging volume is defined at third height, wherein the third height is equal to either the first height and the second height, or has a value between the first ...

Apparatus and method for selectively preparing reactive polybutene and nonreactive polybutene

There are disclosed an apparatus and a method for selectively preparing a high reactivity polybutene, a midrange reactivity polybutene and a non-reactive polybutene in a single plant. The apparatus for selectively preparing a reactive polybutene and a non-reactive polybutene, comprises: a reactive polybutene polymerization catalyst feeder for polymerization of the reactive polybutene; a non-reactive polybutene polymerization catalyst feeder for polymerization of the non-reactive polybutene; and a reactor for polymerizing a reactant including isobutene into polybutene, wherein the reactive polybutene polymerization catalyst feeder provides a catalyst to yield the reactive polybutene; and the non-reactive polybutene polymerization catalyst feeder provides a catalyst to yield the non-reactive polybutene.

APPARATUS AND PROCESS FOR PRODUCING DIMETHYL CARBONATE

The present application relates to an apparatus and process for producing dimethyl carbonate, in particular a system (apparatus or process) for DMC synthesis without the need of using a dehydrating agent. More particularly, the feed mixture for the process can be selected from the following options: a) carbon monoxide, methanol and flue gas from the process, b) synthesis gas without COand flue gas from the process, c) synthesis gas with COand added synthesis gas from purified flue gas from the process. The process uses a catalyst cluster comprising a specific combination of different groups of heterogeneous catalysts wherein each group has a different function. Also the invention relates to an apparatus comprising a specific combination of heterogeneous catalysts for applying different routes to produce dimethyl carbonate from each feed mixture option, on continuous basis. 1. Apparatus for producing dimethyl carbonate (DMC) , comprising a DMC reactor for synthesizing DMC from a feed mixture at least comprising MeOH , CO , and CO , wherein the DMC reactor comprises a mixture of at least two heterogeneous catalyst groups comprising catalysts C2 and C3 , wherein catalyst C2 promotes the reaction of MeOH with COto produce DMC and HO as byproduct , and catalyst C3 promotes the transformation of CO and HO to Hand CO.2. Apparatus according to claim 1 , further comprising a MeOH reactor for synthesizing MeOH from a feed mixture at least consisting of CO claim 1 , CO claim 1 , and H claim 1 , wherein the MeOH reactor is either integrally combined within the DMC reactor or is sequentially placed upstream of the DMC reactor claim 1 , wherein the MeOH reactor comprises a third group of heterogeneous catalysts claim 1 , namely catalyst C1 claim 1 , which promotes the reaction of CO claim 1 , Hand COto MeOH.3. Apparatus according to claim 1 , wherein catalysts C1 claim 1 , C2 and C3 are placed in the DMC reactor integrally including the MeOH reactor claim 1 , or catalyst C1 is ...

SYSTEMS AND METHODS FOR CLOSED-LOOP RECYCLING OF A LIQUID COMPONENT OF A LEACHING MIXTURE WHEN RECYCLING LEAD FROM SPENT LEAD-ACID BATTERIES

The present disclosure relates generally to systems and methods for recycling lead-acid batteries, and more specifically, relates to purifying and recycling the lead content from lead-acid batteries. A system includes a reactor that receives and mixes a lead-bearing material waste, a carboxylate source, and a recycled liquid component to form a leaching mixture yielding a lead carboxylate precipitate. The system also includes a phase separation device coupled to the reactor, wherein the phase separation device isolates the lead carboxylate precipitate from a liquid component of the leaching mixture. The system further includes a closed-loop liquid recycling system coupled to the phase separation device and to the reactor, wherein the closed-loop liquid recycling system receives the liquid component isolated by the phase separation device and recycles a substantial portion of the received liquid component back to the reactor as the recycled liquid component. 1. A system , comprising:a reactor that receives and mixes lead-bearing material, a carboxylate source, and a recycled liquid component to form a leaching mixture yielding a lead carboxylate precipitate;a phase separation device coupled to the reactor, wherein the phase separation device isolates the lead carboxylate precipitate from a liquid component of the leaching mixture; anda closed-loop liquid recycling system coupled to the phase separation device and to the reactor, wherein the closed-loop liquid recycling system receives the liquid component isolated by the phase separation device and recycles a substantial portion of the received liquid component back to the reactor as the recycled liquid component.2. The system of claim 1 , wherein the closed-loop liquid recycling system comprises a purification device that removes at least one impurity from the received liquid component before recycling.3. The system of claim 2 , wherein the at least one impurity comprises dissolved sulfates.4. The system of claim 2 ...

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.

APPARATUSES FOR DEHYDROGENATION OF ALKANES

The present disclosure relates to circulating fluidized bed apparatuses for dehydrogenation of alkanes to alkenes with higher yield and selectivity. The apparatus includes a riser-type reactor, a separator section, a regenerator and a withdrawal well disposed downstream to the regenerator. The apparatus includes a transfer line to receive hot regenerated catalyst free of oxygen from the withdrawal well, and to pre-treat the catalyst with a reducing gas to regulate-oxidation state of metals on the catalyst before reintroducing the catalyst to the riser-type reactor. The transfer line is formed in an elongated U-shaped pipe such that the oxidation state of the metals on the catalyst is regulated by the time the pre-treated catalyst reaches the bottom of the riser-type reactor. 1. A circulating fluidized bed apparatus for dehydrogenation of alkanes comprising a riser-type reactor , a separator coupled to the riser-type reactor , a regenerator coupled to the separator and a withdrawal well disposed downstream to the regenerator , and a transfer line connecting the withdrawal well with the riser-type reactor , the transfer line adapted to:receive hot regenerated catalyst free of oxygen from the withdrawal well; andpre-treat the catalyst with a reducing gas to regulate the oxidation state of metals on the catalyst before reintroducing the catalyst to the bottom of the riser-type reactor, wherein the transfer line is formed in an elongated U-shaped pipe such that the oxidation state of the metals on the catalyst is regulated by the time the catalyst reaches the bottom of the riser-type reactor.2. The circulating fluidized bed apparatus as claimed in claim 1 , wherein the riser-type reactor is adapted to accommodate a pre-heated alkane feed stream and a catalyst for dehydrogenation reaction.3. The circulating fluidized bed apparatus as claimed in claim 1 , wherein the separator comprising:a riser termination device for disengaging the catalyst and hydrocarbons;a set of ...

Method of catalyst testing in fluidized bed reactors using catalyst capsules

A method for testing catalysts in a fluidized bed reactor comprises enclosing catalyst material in capsules having pores or holes smaller than the catalyst material, inserting the capsules filled with catalyst material to into a port of the fluidized bed reactor and recovering at least a portion of the catalyst capsules from the fluidized bed reactor after use through an additional port of the fluidized bed reactor, wherein the capsules move with a flow of uplifted fluid and gas in the fluidized bed reactor.

METHOD FOR PRODUCING A HORIZONTAL FLOW ADSORBER AND DIVIDING WALL MODULE FOR USE IN SAID METHOD

The method serves for producing a horizontal through flow adsorber with two adsorbents which contains two immediately adjacent packings in a horizontal or vertical container. Between the two packings there is a vertical interface. In a step (a) a vertical dividing wall is positioned on the bottom of the adsorption bed and then on each side of the dividing wall one of the two adsorbents is charged up to a first height that does not exceed the upper edge of the separating ring. In the following step (b) the vertical dividing wall is displaced upwardly until the lower edge thereof is still placed in the existing packing. Then, on each side of the dividing wall one of the two adsorbents is charged up to a second height that does not exceed the upper edge of the displaced dividing wall. Finally, step (b) is repeated until a predetermined filling height is achieved. According to the invention, the vertical dividing wall is composed of at least three dividing wall modules () that extend only over a part of the length or of the periphery of the vertical dividing wall and are movable in a vertical direction independently of one another. 1. The method for producing a horizontal through flow adsorber with two adsorbents which contains two immediately adjacent packings in a horizontal or vertical container , wherein there is a vertical interface between the two packings , and wherein a first packing contains a first adsorbent and a second packing contains a second adsorbent that differs from the first adsorbent in the chemical composition and/or particle size thereof , wherein , in the method(a) a vertical dividing wall is positioned on the bottom of the adsorption bed and then on each side of the dividing wall one of the two adsorbents is charged up to a first height that does not exceed the upper edge of the dividing wall,(b) the vertical dividing wall is displaced upwardly until the lower edge thereof is still placed in the existing packing, and on each side of the dividing ...

Easy clean catalyst filter basket

A catalyst filter basket for containing catalyst material within a catalytic chemical reactor. The catalyst filter basket includes a central frame having a base ring and a generally cylindrical inner screen portion which extends upwardly from the base ring. A generally cylindrical outer screen assembly is releasably secured to the central frame by a quick release mechanism.

Process for stripping and a fluid catalytic cracking apparatus relating thereto

One exemplary embodiment can be a process for stripping. The process can include passing catalyst to a stripping vessel containing a riser, providing a plurality of baffles having a first baffle and a second baffle, and providing one or more packing layers. The stripping vessel and riser may define an annular zone including annular area for stripping of the catalyst, and the first and second baffles collectively overlap in no more than about 50% of the annular area. Often, the first baffle is coupled to an outer circumference of the riser and extends outward, and the second baffle is coupled to an inner circumference of the stripping vessel and extends inward. Typically, the one or more packing layers are within the annular zone.

PREPARATION METHOD AND DEVICE FOR EFFICIENTLY PREPARING MAGNESIUM HYDROXIDE

The present invention relates to a device for efficiently preparing magnesium hydroxide, comprising a material mixing tank, a pressure control linkage unit I, a reactor, a pressure control linkage unit II, a condenser, a three-way valve, a material storage tank, a pressure control linkage unit III and a vapor generator. The beneficial effect of the present invention is that magnesium hydroxide slurry can be prepared quickly and efficiently. 112345678911223132445561621263733889. A device for efficiently preparing magnesium hydroxide , comprising a mixing tank () , a pressure control linkage unit I () , a reactor () , a pressure control linkage unit II () , a condenser () , a three-way valve () , a storage tank () , a pressure control linkage unit III () , and a vapor generator () , wherein a discharging hole () of the mixing tank is connected with one end of the pressure control linkage unit I () through a pump , the other end of the pressure control linkage unit I () is connected with a feeding hole () of the reactor , a discharging hole () of the reactor is connected with one end of the pressure control linkage unit II () , the other end of the pressure control linkage unit II () is connected with one end of the condenser () , the other end of the condenser () is connected with a first port () of the three-way valve , a second port () of the three-way valve is connected with a returning hole () of the mixing tank , a third port () of the three-way valve is connected with the storage tank () , a vapor inlet () of the reactor is connected with one end of the pressure control linkage unit III () , and the other end of the pressure control linkage unit III () is connected with the vapor generator ().2. The device according to claim 1 , wherein the pressure control linkage unit is composed of a pressure sensor and an electromagnetic valve.3. A preparation method for efficiently preparing magnesium hydroxide claim 1 , wherein the method comprises the following steps:{'b ...

Multi-Stage Process and Device for Treatment Heavy Marine Fuel Oil and Resultant Composition Including Ultrasound Promoted Desulfurization

A multi-stage process for reducing the environmental contaminants in an ISO8217 compliant Feedstock Heavy Marine Fuel Oil involving a core desulfurizing process and a ultrasound treatment process as either a pre-treating step or post-treating step to the core process. The Product Heavy Marine Fuel Oil complies with ISO 8217 for residual marine fuel oils and has a sulfur level has a maximum sulfur content (ISO 14596 or ISO 8754) between the range of 0.05 mass % to 1.0 mass. A process plant for conducting the process is also disclosed. 1. A process for reducing the environmental contaminants in a Feedstock Heavy Marine Fuel Oil , the process comprising: contacting a Feedstock Heavy Marine Fuel Oil , wherein the Feedstock Heavy Marine Fuel Oil complies with ISO 8217 except for the environmental contaminates including a sulfur content (ISO 14596 or ISO 8754) greater than 0.50 wt % , with ultrasound having a frequency in the range of about 10 kHz and about 100 megahertz and a sonic energy in the range of about 30 watts/cmto about 300 watts/cm , and a temperature ranging between 30° C. and 260° C. to give an ultrasonic pre-treated Feedstock Heavy Marine Fuel Oil; mixing a quantity of the ultrasonic pre-treated Feedstock Heavy Marine Fuel Oil with a quantity of Activating Gas mixture to give a Feedstock Mixture; contacting the Feedstock Mixture with one or more supported transition metal catalysts under reactive conditions to form a Process Mixture from said Feedstock Mixture; receiving said Process Mixture and separating the Product Heavy Marine Fuel Oil liquid components of the Process Mixture from the gaseous components and by-product hydrocarbon components of the Process Mixture and , discharging the Product Heavy Marine Fuel Oil.2. The process of claim 1 , wherein the step of contacting a Feedstock Heavy Marine Fuel Oil with ultrasound takes place in the presence of water or supercritical water in which the volume ratio of the Feedstock Heavy Marine Fuel Oil to the ...

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 ...

METHOD AND SYSTEM FOR IMPROVED REACTANT MIXING AND DISTRIBUTION

One aspect of the present invention relates to a mixing system for use in a chemical-process column. The mixing system includes a heavy-reactant mixing surface arranged perpendicular to a flow of reactant through the chemical-process column. The mixing system also includes an aperture formed in the heavy-reactant mixing surface. A pre-distributor is coupled to an underside of the mixing system and fluidly coupled to the aperture. 1. A method of mixing reactants in a chemical-process column , the method comprising:introducing a heavy reactant to a mixing region of the chemical process column;contacting the heavy reactant with a heavy-reactant mixing surface;homogenizing the heavy reactant within a mixing pot; anddistributing the heavy reactant via a pre-distributor.2. The method of claim 1 , comprising directing the heavy reactant toward the mixing pot via a baffle.3. The method of claim 1 , comprising mixing the heavy reactant with a vane disposed at an entrance to the mixing pot.4. The method of claim 1 , comprising mixing the heavy reactant via at least one of a vane claim 1 , a deflector claim 1 , a baffle claim 1 , or a static mixer disposed within the mixing pot.5. The method of claim 1 , comprising:introducing a light reactant to the mixing region of the chemical process column;directing the light reactant through the heavy-reactant mixing surface via a light-reactant duct; andmixing the light reactant via a vectoring member fluidly coupled to the light-reactant duct.6. The method of claim 5 , wherein the vectoring member is arranged proximate to the pre-distributor.7. The method of claim 1 , wherein the distributing comprises directing the heavy reactant through a plurality of channels fluidly coupled to the mixing pot claim 1 , the plurality of channels having a plurality of perforations formed therein.8. The method of claim 1 , wherein the homogenizing comprises inducing turbulent mixing of the heavy reactant within the mixing pot.9. The method of claim 1 , ...

MICROCHEMICAL SYSTEM APPARATUS AND RELATED METHODS OF FABRICATION

The disclosure relates to microchemical (or microfluidic) apparatus as well as related methods for making the same. The methods generally include partial sintering of sintering powder (e.g., binderless or otherwise free-flowing sintering powder) that encloses a fugitive phase material having a shape corresponding to a desired cavity structure in the formed apparatus. Partial sintering removes the fugitive phase and produces a porous compact, which can then be machined if desired and then further fully sintered to form the final apparatus. The process can produce apparatus with small, controllable cavities shaped as desired for various microchemical or microfluidic unit operations, with a generally smooth interior cavity finish, and with materials (e.g., ceramics) able to withstand harsh environments for such unit operations. 120-. (canceled)21. A microchemical apparatus comprising:a fully sintered metal oxide body comprising an interior cavity within the body; the interior cavity has a minimum dimension in a range from 1 μm to 1000 μm; and', 'the interior cavity has a surface roughness of 20 μm or less., 'wherein22. The microchemical apparatus of claim 21 , wherein the fully sintered metal oxide body has a density of at least 80% relative to the theoretical density of the metal oxide.23. The microchemical apparatus of claim 21 , wherein the interior cavity is fully enclosed by the fully sintered metal oxide body.24. The microchemical apparatus of claim 21 , wherein the interior cavity is partially enclosed by the fully sintered metal oxide body. Priority is claimed to U.S. Provisional Application No. 62/378,932 filed Aug. 24, 2016, which is incorporated herein by reference in its entirety.None.The disclosure relates to relates to microchemical (or microfluidic) apparatus as well as related methods for making the same. The methods generally include partial sintering of sintering powder, removal of a fugitive phase material within the powder to create internal ...

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

A multi-stage process for the production of an ISO8217 compliant Product Heavy Marine Fuel Oil from ISO 8217 compliant Feedstock Heavy Marine Fuel Oil involving a core process under reactive conditions in a Reaction System composed of one or more reaction vessels, wherein one or more of the reaction vessels contains one or more catalysts in the form of a structured catalyst bed and is operated under reactive distillation conditions. The Product Heavy Marine Fuel Oil has a sulfur level has a maximum sulfur content (ISO 14596 or ISO 8754) between the range of 0.05 mass % to 1.0 mass. A process plant for conducting the process for conducting the process is disclosed. 1. A process for the production of a Product Heavy Marine Fuel Oil , the process comprising: mixing a quantity of Feedstock Heavy Marine Fuel Oil , wherein Feedstock Heavy Marine Fuel Oil complies with ISO 8217 (2017) but has a sulfur content (ISO 14596 or ISO 8754) greater than 0.5% wt. with a quantity of Activating Gas mixture to give a Feedstock Mixture; contacting the Feedstock Mixture with one or more catalysts under reactive distillation conditions to promote the formation of a Process Mixture from said Feedstock Mixture , wherein said one or more catalysts are in the form of a structured catalyst bed; receiving said Process Mixture and separating the liquid components of the Process Mixture from the bulk gaseous components of the Process Mixture; and separating any residual gaseous components and by-product hydrocarbon components from the Product Heavy Marine Fuel Oil.2. The process of claim 1 , wherein the structured catalyst bed comprises a plurality of catalyst retention structures claim 1 , each catalyst retention structure composed of a pair of fluid permeable corrugated metal sheets claim 1 , wherein the pair of the fluid permeable corrugated metal sheets are aligned such that the corrugations are out of phase and thereby defining a catalyst rich space and a catalyst lean space within the ...

Reactor bed vessel and support assembly

Vessel and support beam assembly includes a vessel having a cylindrical wall defining an interior chamber having a generally circular shape of diameter D in plan view, and a support assembly disposed within the interior chamber. The support assembly includes an inner hub defining an open central region, and a plurality of spokes extending radially from the inner hub. Each spoke is aligned radially with the cylindrical wall of the vessel and joined thereto. At least one open outer region is defined between circumferentially adjacent spokes.

Powder stirring device

A powder stirring device includes a reaction container and a rotation driving device. The reaction container has a cylindrical outer peripheral wall and a pair of end surface walls. The end surface walls are respectively provided at one end and the other end of the outer peripheral wall. The reaction container is arranged in a heat-insulating cover such that an axis of the outer peripheral wall is in parallel with a horizontal direction. The outer peripheral wall has an inner peripheral surface rotationally symmetric with respect to the axis. During the powder process, the powder is stored in the reaction container, and the reaction container is rotated around a rotation axis that passes through the central axis of the outer peripheral wall by the rotation driving device. In this state, a processing gas is supplied into the reaction container. Also, the processing gas in the reaction container is discharged.

APPARATUS AND METHOD FOR REDUCING CARBON DIOXIDE USING SOLAR LIGHT

The present disclosure relates to an apparatus for a reduction reaction of carbon dioxide using solar energy and a reducing method of carbon dioxide for reacting carbon dioxide gas and hydrogen gas with each other by using solar energy. 1. An apparatus for a reduction reaction of carbon dioxide , comprising:a solar collecting member that absorbs solar heat energy;a reduction reaction member of carbon dioxide, heated by solar heat energy; anda reactant supplying member and a product outlet member, which are connected to the reduction reaction member of carbon dioxide,wherein hydrogen gas and carbon dioxide gas are injected into the reduction reaction member of carbon dioxide via the reactant supplying member to be reacted with each other in the presence of a metal catalyst supported on a metal oxide support loaded into the reduction reaction member of carbon dioxide.2. An apparatus for a reduction reaction of carbon dioxide , comprising:a reduction reaction member of carbon dioxide, in which a photocatalyst is loaded; anda reactant supplying member and a product outlet member, which are connected to the reduction reaction member of carbon dioxide,wherein carbon dioxide gas and hydrogen gas are injected into the reduction reaction member of carbon dioxide via the reactant supplying member to be reacted with each other within the reduction reaction member of carbon dioxide under irradiation of solar light.3. The apparatus for a reduction reaction of carbon dioxide of claim 1 , further comprising a water-splitting reaction member.4. The apparatus for a reduction reaction of carbon dioxide of claim 2 , further comprising a water-splitting reaction member.5. The apparatus for a reduction reaction of carbon dioxide of claim 3 ,wherein the water-splitting reaction member generates oxygen and hydrogen through splitting of water by a solar cell, the generated oxygen is removed, and the generated hydrogen is supplied into the reduction reaction member of carbon dioxide.6. The ...

DEVICE FOR FACILITATING A CHEMICAL REACTION

A device for facilitating a chemical reaction while submerged in a liquid catalyst includes an upper member, a lower member, and a dissolvable member disposed between and ultimately enclosed by said upper and lower members such that upper and lower chambers are formed having substantially equal volumes. The upper chamber may receive a dry sodium chlorite and the lower chamber may receive a dry acid mixture. In order to keep the device submerged in the liquid catalyst, an inert ballast may also be added to the upper and/or lower chamber, such as glass shards. 1. A device for facilitating a chemical reaction comprising:an upper member at least partially defining an upper chamber of a packet containing sodium chlorite;a lower member at least partially defining a lower chamber of a packet containing a dry acid;an inert ballast disposed within said packet to maintain the device within a submerged state within a liquid catalyst; andwherein said upper member and said lower member are joined to one another so as to enclose said sodium chlorite, said dry acid, and said inert ballast within a closed packet.2. The device of claim 1 , wherein said inert ballast is comprised of glass.3. The device of wherein a dissolvable member is disposed between and ultimately enclosed by said upper and lower members such that said upper and lower chambers have substantially equal interior volumes.4. The device of wherein said dissolvable member is fabricated from polyvinyl alcohol and capable of engaging dry acid and sodium chlorite without a reaction.5. The device of wherein said upper and lower members is fabricated from a compressed cellulose cloth.6. The device of claim 5 , wherein said upper and lower members have multiple pores of substantially the same dimension.7. The device of claim 5 , wherein said upper and lower members have multiple pores claim 5 , wherein said lower member is fabricated from a compressed cellulose cloth material having pore sizes relatively smaller and with ...

Method of cleaning spent catalyst material

A method of cleaning spent catalyst material from a catalyst filter basket. The catalyst filter basket includes a central frame having a base ring and a generally cylindrical inner screen portion which extends upwardly from the base ring. A generally cylindrical outer screen assembly is releasably secured to the central frame by a quick release mechanism

Optimized Reactor Configuration for Optimal Performance of the Aromax Catalyst for Aromatics Synthesis

A naphtha reforming reactor system comprising a first reactor comprising a first inlet and a first outlet, wherein the first reactor is configured to operate as an adiabatic reactor, and wherein the first reactor comprises a first naphtha reforming catalyst; and a second reactor comprising a second inlet and a second outlet, wherein the second inlet is in fluid communication with the first outlet of the first reactor, wherein the second reactor is configured to operate as an isothermal reactor, and wherein the second reactor comprises a plurality of tubes disposed within a reactor furnace, a heat source configured to heat the interior of the reactor furnace; and a second naphtha reforming catalyst disposed within the plurality of tubes, wherein the first naphtha reforming catalyst and the second naphtha reforming catalyst are the same or different. 1. A naphtha reforming reactor system comprising: a plurality of tubes disposed within a reactor furnace,', 'a heat source configured to heat an interior of the reactor furnace; and', 'a naphtha reforming catalyst disposed within the plurality of tubes,', 'wherein at least one tube of the plurality of tubes comprises a graded catalyst bed., 'an isothermal reactor comprising23.-. (canceled)4. The naphtha reforming reactor system of claim 1 , wherein the graded catalyst bed contains a plurality of catalyst zones.5. The naphtha reforming reactor system of claim 4 , wherein the plurality of catalyst zones comprises a first catalyst zone and a second catalyst zone claim 4 , wherein the first catalyst zone is upstream of the second catalyst zone.6. The naphtha reforming reactor system of claim 5 , wherein the first catalyst zone contains a first particle size of the naphtha reforming catalyst claim 5 , wherein the second catalyst zone contains a second particle size of the naphtha reforming catalyst claim 5 , and wherein the first particle size is larger than the second particle size.7. The naphtha reforming reactor system of ...

Production Of Cyclopentadiene From Furfural

The application relates to processes and systems that use a furfural compound for producing five-membered carbocyclic rings that are unsaturated, such as cyclopentene and cyclopentadiene. Examples methods for conversion of furfural compounds may include converting a furfural compound to at least a five-membered, saturated carbocyclic ring, and converting the five-membered, saturated carbocyclic ring in a presence of a catalyst to at least a five-membered, unsaturated carbocyclic ring. 1. A method for conversion of furfural compounds , comprising:converting a furfural compound to at least a five-membered, saturated carbocyclic ring; andconverting the five-membered, saturated carbocyclic ring in a presence of a catalyst to at least a five-membered, unsaturated carbocyclic ring, wherein the five-membered, unsaturated carbocyclic ring is selected from the group consisting of a cyclopentene product, a cyclopentadiene product, and combinations thereof.2. The method of claim 1 , where the catalyst comprises a bifunctional catalyst comprising a hydrogenation/dehydrogenation metal functionality and a heterogenous acid component.3. The method of claim 1 , wherein the converting the furfural compound and the converting the five-membered claim 1 , saturated carbocyclic ring occur in a single step over a bi-functional catalyst using at least one reactor selected from the group consisting of a fixed bed reactor claim 1 , a batch reactor claim 1 , a slurry reactor claim 1 , a semi-batch reactor claim 1 , and a fluidized-bed reactor.5. The method of claim 1 , wherein the converting the furfural compound is at a temperature of about 20° C. to about 400° C. and about 15 psig to about 1000 psig claim 1 , and wherein the five-membered claim 1 , saturated carbocyclic ring is selected from the group consisting of cyclopentanol claim 1 , cyclopentanone claim 1 , cyclopentanediol claim 1 , and combinations thereof.6. The method of claim 1 , wherein the converting the five-membered claim 1 ...

REACTOR SYSTEM

A reactor tank is provided having an enzyme inlet, a heating jacket positioned around the exterior center of the tank, a gas outlet communicating with a vacuum apparatus and a condensing unit, a first gas inlet for receiving gas from a feed tank and a first liquid outlet for recirculating the liquid back to the feed tank. The tank further includes a sparged unit connected to the first gas inlet for receiving gas from the feed tank and a screen positioned between the sparged unit and the first liquid outlet. The reactor tank is utilized in a reactor system further including a condensing unit, vacuum pump or venturi valve, a first feed tank, a coalescer having at least one circulation pipe and a first circulation pump. 1. A reactor comprising:a tank having a catalyst inlet;a heating jacket positioned around the exterior center of the tank;a gas outlet for communicating with a contact condenser unit for the continuous removed of water from the tank during use;a first gas inlet for receiving gas from a feed tank;a first liquid outlet for recirculating the liquid from the first liquid outlet back to the feed tank;a sparged unit positioned within the tank and in communication with the first gas inlet to sparge the gas received through the first gas inlet; anda screen positioned within the tank between the sparged unit and the first liquid outlet.2. The reactor of further includes a second gas outlet on the second end of the vessel to vent air from the reactor.3. The reactor of further including an agitator mount.4. The reactor of further including a raw material inlet.5. The reactor of where the sparged unit further includes sparger arms mounted radial about a central pipe hub.6. A reactor system claim 1 , the reactor system including: a catalyst inlet;', 'a heating jacket positioned around the center of the vessel;', 'a first gas outlet at the first end of the vessel;', 'a first gas inlet at the second end of the vessel;', 'a first liquid outlet at the second end of the ...

REACTOR SYSTEM

A reactor tank is provided having an enzyme inlet, a heating jacket positioned around the exterior center of the tank, a gas outlet for communicating with a vacuum apparatus to create a vacuum within the reactor tank and for communicating with a condensing unit, a first gas inlet for receiving gas from a feed tank and a first liquid outlet for recirculating the liquid from the first liquid outlet back to the feed tank. The reactor tank further includes a sparged unit and a screen positioned within the tank between the sparged unit and the first liquid outlet, where the sparged unit is connected to the first gas inlet for receiving gas from the feed tank. The reactor tank is utilized in a reactor system further including a condensing unit, vacuum pump or venturi valve, a first feed tank connected to the first gas inlet, a coalescer having at least one circulation pipe and a first circulation pump connected to the first liquid outlet for circulating a portion of the liquid dispelled from the liquid outlet to the coalescer, which after being filtered through coalescer is recirculated through circulation pipe back to the first feed tank. 1. A reactor comprising:a tank having a catalyst inlet;a heating jacket positioned around the exterior center of the tank;a gas outlet for communicating with a contact condenser unit for the continuous removed of water from the tank during use;a first gas inlet for receiving gas from a feed tank;a first liquid outlet for recirculating the liquid from the first liquid outlet back to the feed tank;a sparged unit positioned within the tank and in communication with the first gas inlet to sparge the gas received through the first gas inlet; anda screen positioned within the tank between the sparged unit and the first liquid outlet.2. The reactor of further includes a second gas outlet on the second end of the vessel to vent air from the reactor.3. The reactor of further including an agitator mount.4. The reactor of further including a raw ...

VCC SLURRY MID REACTOR SEPARATION

A system for separating first reactor effluent product by means of an intermediate separator, and sending the unconverted slurry material from the separator to further reactors. Such intermediate separation decreases the required size of downstream reactors. 1. A system for processing a hydrocarbon feed , comprising:a plurality of serially aligned reactors;a hot separator receiving an effluent from the plurality of serially aligned reactors, the hot separator producing a first converted vapor product and a first unconverted slurry product; andan intermediate separator receiving an intermediate effluent from a first reactor of the plurality of reactors, the intermediate separator producing a second converted vapor product and an second unconverted slurry product, the second unconverted slurry product being directed into a second reactor of the plurality of reactors.2. The system of claim 1 , further comprising a line conveying the second converted vapor product to one of: (i) a cyclone separator claim 1 , (ii) a cooling unit claim 1 , and (iii) a fixed bed Gas Phase reactor.3. The system of claim 1 , wherein at least one of the plurality of serially aligned reactors is configured to receive one of: (i) a carbonaceous additive claim 1 , and (ii) hydrogen.4. The system of claim 1 , wherein the intermediate separator is configured to reduce hydrocarbon vapor in the effluent received from the first reactor.5. The system of claim 1 , wherein at least one of the plurality of serially aligned reactors includes a bubble column allowing entry from a bottom of the bubble column one of: (i) a hydrocarbon claim 1 , (ii) hydrogen claim 1 , and (iii) an additive.6. The system of claim 1 , further comprising a line supplying a hydrogen feed to the second unconverted residue and solids product slurry.7. A method for processing a hydrocarbon feed claim 1 , comprising:feeding the hydrocarbon feed into a plurality of serially aligned reactors;receiving an effluent from the plurality of ...

Systems and methods for catalyst screens in selective catalytic reduction reactors

A system for use in selective catalytic reduction reactor is disclosed. The system may include a catalyst bed and a screen located close to the catalyst bed in a manner so that flow of flue gas to the catalyst bed contacts the screen before it contacts the catalyst bed. The screen may be adapted to support a weight of at least 400 pounds above the catalyst bed so that the weight is not imposed on the catalyst. The screen may have a plurality of holes across its surface in a manner so that the screen is adapted to change the velocity distribution of the flue gas as it flows through the screen.

SYSTEM FOR DISTRIBUTING A LIQUID AND/OR GAS PHASE INTO A REACTION VESSEL

System for distributing a liquid and/or gas phase into a reaction vessel (), reaction vessel () comprising at least one inlet () for injection of the liquid and/or gas phase, the system according to the invention comprising a distributor for distributing this phase by means of at least one tube () provided with a plurality of perforations (), as well as removable fastening means () for the distributor when it is arranged within the reaction vessel. According to the invention, the section of the distributor is smaller than the section of inlet () of reaction vessel (), so as to be able to insert and/or to remove the distributor through inlet () of vessel (). 1. A system for distributing a liquid and/or gas phase into a reaction vessel , the vessel comprising at least one inlet for an injection of the phase , wherein the system comprises:a distributor for distributing the phase, comprising at least one tube, the tube including a plurality of perforations,means for removable fastening of the distributor when it is arranged in inlet of the vessel,and in that the section of at least the distributor is smaller than the section of inlet.2. A system as claimed in claim 1 , wherein the removable fastening means consist of an assembly for reversibly securing at least one of the ends of the distributor to the inlet of the vessel.3. A system as clamed in claim 2 , wherein the assembly comprises at least one flange claim 2 , a seal and at least one screwed joint.4. A system as claimed in claim 1 , wherein the system further comprises means for supporting the distributor at least at one point of the vessel opposite the inlet of the vessel.5. A system as claimed in claim 4 , wherein the support means comprise a rail intended to be fastened along the tube of the distributor claim 4 , two plates intended to be fastened vertically onto a wall of the vessel so as to receive and hold the rail claim 4 , the section of the assembly made up of at least the distributor and the rail being ...

METHOD OF SHUTTING DOWN A REACTOR

A procedure for shutting down a dehydrogenation reactor having a catalyst bed with a chromium-containing catalyst operating at a first elevated temperature comprises cooling the catalyst bed with a first cooling gas to a second elevated temperature lower than the first elevated temperature, removing the first cooling gas, introducing a reducing gas to the catalyst bed, cooling the catalyst bed with a second cooling gas from the second elevated temperature to a third elevated temperature, removing the reducing gas, cooling the catalyst bed to a fourth elevated temperature, and introducing air to cool the catalyst to ambient temperature, whereby the dehydrogenation reactor is shut down. The second cooling gas may be the same as, or different from, the reducing gas. Moreover, the reducing gas may be purged from the reactor by a third cooling gas. 1. A method of shutting down a dehydrogenation reactor , the dehydrogenation reactor housing a catalyst bed containing a chromium-containing catalyst , the catalyst bed operating at a first elevated temperature under standard dehydrogenation conditions , the method comprising:(a) cooling the catalyst bed with a first cooling gas from the first elevated temperature to a second elevated temperature lower than the first elevated temperature;(b) removing the first cooling gas from the catalyst bed while maintaining the catalyst bed at about said second elevated temperature;(c) treating the catalyst bed with a reducing gas for a period of time sufficient to cause chemical reduction of at least some of the chromium in the catalyst to a reduced oxidation state;(d) cooling the catalyst bed with a second cooling gas from the second elevated temperature to a third elevated temperature lower than the second elevated temperature;(e) removing the reducing gas from the catalyst bed;(f) cooling the catalyst bed with a third cooling gas from the third elevated temperature to a fourth elevated temperature lower than the third elevated ...

Catalyst Testing Process and Apparatus

A method for analyzing a catalyst in a catalytic reactor that operates under non-isothermal conditions includes the steps of: positioning a catalyst basket within a catalyst bed within the catalytic reactor, the catalyst basket containing catalyst material the forms the catalyst bed; operating the catalytic reactor, the catalyst basket having dimensions such that a temperature difference (ΔT) along an axial direction (height) of the catalyst basket is non-isothermal; and analyzing the catalyst material contained within the catalyst basket. The temperature difference (ΔT) is, in one embodiment, within a range of 1° C. to 40° C. and preferably, within a range of 5° C. to 25° C. 1. A method for analyzing a catalyst in a catalytic reactor that operates under non-isothermal conditions comprising the steps of:positioning a catalyst basket within a catalyst bed within the catalytic reactor, the catalyst basket containing catalyst material the forms the catalyst bed,operating the catalytic reactor, the catalyst basket having dimensions such that a temperature difference (ΔT) along an axial direction of the catalyst basket is non-isothermal; andanalyzing the catalyst material contained within the catalyst basket.2. The method of claim 2 , wherein the temperature difference (ΔT) is within a range of 1° C. to 40° C.3. The method of claim 3 , wherein the temperature difference (ΔT) is within a range of 5° C. to 25° C.4. The method of claim 1 , wherein the catalyst bed has a height (h1) and an internal diameter (ID1) and the catalyst basket has a height (h2) and an internal diameter (ID2) claim 1 , wherein h2/ID2 is between 1 and 300 claim 1 , and wherein h2/h1 is between 0.05 and 1.5. The method of claim 1 , wherein the catalyst basket has an internal diameter of between about 1 cm to 25 cm claim 1 , a height between 25 cm to 300 cm claim 1 , and a wall thickness between 0.1 cm and 1 cm.6. The method of claim 1 , wherein the step of analyzing the catalyst material contained ...

ADJUSTABLE LIFT ENGAGER

A lift engager for providing a stream of fluidized catalyst particles with an adjustable conduit and process using the lift engager. The lift engager includes a vessel with an inlet configured to receive catalyst from a reaction zone. A first conduit, within the vessel, is configured to supply lift gas into the lift engager. The first conduit includes a fixed member and a movable member secured to the fixed member and is configured to adjust a length of the first conduit within the vessel. A second conduit inside the first conduit and configured to provide fluidized catalyst to a regeneration zone. 1. A lift engager for providing a stream of fluidized catalyst particles , the lift engager comprising:a vessel with an inlet configured to receive catalyst from a reaction zone;a first conduit within the vessel configured to supply lift gas into the lift engager, the first conduit comprising a fixed member and a movable member secured to the fixed member and configured to adjust a length of the first conduit within the vessel; and,a second conduit inside the first conduit and configured to provide fluidized catalyst to a regeneration zone.2. The lift engager of wherein the fixed member includes a first end claim 1 , and wherein the movable member comprises a first end claim 1 , and wherein the first end of the fixed member and the first end of the moveable member are configured complementarily to engage each other and prevent rotation of the movable member relative to the fixed member.3. The lift engager of claim 2 , wherein both first ends comprise a plurality of alternating teeth and gaps claim 2 , the teeth of one first end configured to be received in the gaps of the other first end.4. The lift engager of claim 1 , further comprising:a sleeve disposed about both of the fixed member and the movable member.5. The lift engager of claim 4 , wherein the sleeve includes an inner surface comprising threads claim 4 , and wherein the moveable member includes an outer surface ...

BASKET-LIKE DEVICE HAVING WALL INSULATION

A device D accommodated in a reactor R and containing a gas- and/or liquid-permeable bottom B, in the peripheral region of which is arranged a lateral boundary W which completely surrounds the bottom B and forms a volume V which is partially or completely filled with catalytic and/or non-catalytic moldings, there optionally being located on the side facing the bottom B in the upstream direction at least one noble metal and/or non-noble metal fabric, wherein a thermal insulation layer S is located on at least part of the surface of the inner side of the lateral boundary W of the device D, the material for the thermal insulation layer S being selected from the group consisting of ceramic material, microporous material and silicate fibers. 115.-. (canceled)16. A device that can be accommodated in a reactor , the device comprising:a gas- and/or liquid-permeable bottom;a peripheral region arranged as a lateral boundary that completely surrounds the bottom and forms a volume, the volume which is partially or completely filled with catalytic and/or non-catalytic moldings;a thermal insulation layer positioned on at least part an inner side surface of the lateral boundary of the device, the thermal insulation layer being a microporous, silicatic material that includes highly dispersed silica and opacifiers, and which exhibits no decomposition in a temperature range from 700 to 1100° C., and has a thermal conductivity in a range from 0.04 to 0.09 W/m/K; andoptionally at least one noble metal and/or non-noble metal fabric located on a side facing the bottom in the upstream direction.17. The device of claim 16 , wherein the thermal insulation layer covers 30% to nearly 100% of the inner side surface of the lateral boundary.18. The device of claim 16 , wherein the thermal insulation layer covers at least the lower 30% of the inner side surface of the lateral boundary.19. The device of claim 16 , wherein the cross-section of the bottom is essentially round.20. The device of claim ...

EXHAUST SYSTEM FOR A STEAM REFORMER AND BEARING THEREFOR

An exhaust system for a steam reformer comprises at least one longitudinal collecting tube, wherein along the longitudinal axis of the longitudinal collecting tube ports for connection to catalyst tubes are provided, which in the connected condition are aligned parallel to each other and vertically to the longitudinal collecting tube, a transverse collector which is connected to the at least one longitudinal collecting tube and has a longitudinal axis which extends vertically to the at least one longitudinal collecting tube and vertically to the catalyst tubes, wherein the longitudinal collecting tube is formed as hot exhaust system and the transverse collector is formed as cold exhaust system. The transverse collector is arranged on a side of the longitudinal collecting tube facing away from the ports centrally to the longitudinal collecting tube. 1. An exhaust system for a steam reformer , comprising at least one longitudinal collecting tube , wherein along the longitudinal axis of the longitudinal collecting tube ports for connection to catalyst tubes are provided , which in the connected condition are aligned parallel to each other and vertically to the longitudinal collecting tube , a transverse collector which is connected to the at least one longitudinal collecting tube and has a longitudinal axis which extends vertically to the at least one longitudinal collecting tube and vertically to the catalyst tubes , wherein the longitudinal collecting tube is formed as hot exhaust system and the transverse collector is formed as cold exhaust system , wherein the transverse collector is arranged on a side of the longitudinal collecting tube facing away from the ports centrally to the longitudinal collecting tube.2. The exhaust system according to claim 1 , wherein at least two longitudinal collecting tubes arranged parallel to each other.3. The exhaust system according to claim 1 , wherein the longitudinal collecting tube is connected to the transverse collector by ...

SCALE COLLECTION DEVICE FOR DOWNFLOW REACTORS

The invention involves a scale collection device that is located within downflow reactor head for removing solids from feed streams to increase reactor operating cycle time without impact on effective reactor space for catalyst loading and reactor pressure drop. More particularly, a scale collection device is located in an upper portion of a reactor vessel above a rough liquid distribution tray and a vapor-liquid distribution tray. 1. A reactor comprising an upper portion and a lower portion wherein the upper portion contains a scale collection device above a rough liquid distribution tray , wherein a vapor-liquid distribution tray is located below the rough liquid distribution tray and wherein the scale collection device comprises bottom plate having a plurality of perforations and a side wall with chimneys along the wall.2. The reactor of claim 1 , wherein the scale collection device has a filtering zone spaced a short distance above bottom plate and the filtering zone comprises a single layer of filtering material having the same physical and chemical properties.3. The reactor of claim 1 , wherein the scale collection device has a filtering zone with two or more layers of filtering materials with different physical or chemical properties.4. The reactor of claim 1 , wherein the filtering zone comprises porous ceramic pellets.5. The reactor of claim 1 , wherein the filtering zone comprises filtering materials containing active materials for promoting certain chemical reactions.6. The reactor of claim 1 , wherein the scale collection device is spaced above the rough liquid distribution tray by a plurality of spacers or beams.7. The reactor of claim 1 , wherein the scale collection device comprises profile wire.8. The reactor of claim 1 , wherein the scale collection device comprises grating.9. The reactor of claim 1 , wherein the scale collection device comprises wire mesh.10. The reactor of claim 1 , wherein the perforations on the bottom plate of the scale ...

SCALE COLLECTION DEVICE FOR DOWNFLOW REACTORS

The invention involves a scale collection device that is located within downflow reactor head for removing solids from feed streams to increase reactor operating cycle time without impact on effective reactor space for catalyst loading. More particularly, a filtering zone is located in an upper portion of a reactor vessel above a rough liquid distribution tray and a distribution tray. 1. A reactor comprising an upper portion and a lower portion wherein the upper portion contains an inlet nozzle and a scale collection device wherein a filtering zone is located above a rough liquid distribution tray and wherein a vapor-liquid distribution tray is located below the rough liquid distribution tray.2. The reactor of claim 1 , wherein the lower portion contains a catalyst bed.3. The reactor of claim 1 , wherein the lower portion contains a medium.4. The reactor of claim 1 , wherein the lower portion contains a packing.5. The reactor of claim 1 , wherein the filtering zone comprises one layer of filtering material having the same physical and chemical properties.6. The reactor of claim 1 , wherein the filtering zone comprises multiple layers of filtering material having different physical and chemical properties.7. The reactor of claim 1 , wherein the filtering zone comprises porous ceramic pellets.8. The reactor of claim 1 , wherein a packed bed support plat is space above the rough liquid distribution tray.9. The reactor of claim 8 , wherein the packed bed support plate includes annular perforations for liquid flow.10. The reactor of claim 1 , wherein the vapor-liquid distribution tray comprises a plurality of distributors.11. The reactor of claim 1 , wherein the rough liquid distribution tray contains holes sized to generate the desired liquid level on the rough liquid distribution tray.12. An apparatus comprising an upper portion and a lower portion wherein the upper portion contains an inlet nozzle and a scale collection device wherein a filtering zone is located above ...

METHOD FOR INDUSTRIAL PRODUCTION OF TRANS-BUTADIENE-ISOPRENE COPOLYMER RUBBER AND APPARATUS THEREFOR

A method for industrial production of a butadiene-isoprene copolymer rubber having a trans-1,4-structure (TBIR) and an apparatus for implementing the method. The production method includes: pumping a predetermined amount of a butadiene and an isoprene into a polymerization reactor, and performing bulk polymerization in the presence of a catalyst to obtain TBIR; performing extrusion, devolatilization, granulation and drying on the produced TBIR, and then packaging the produced TBIR; and separating unreacted monomers by a recovery and separation device followed by separately refining the unreacted monomers, and then returning the unreacted monomers to a batching device or a storage tank. The production apparatus has a recovery and refining unit, a polymerization unit, a post-treatment unit and a utility unit. By the production apparatus and the production method industrial production of TBIR by bulk polymerization is realized. 1. A method for industrial production of a butadiene-isoprene copolymer rubber having a trans-1 ,4-structure , the method is as below:{'sup': '−5', '(1) after the polymerization apparatus is vacuumed and the water and oxygen within is replaced fully by the nitrogen, the refined isoprene monomer, butadiene monomer, cocatalyst, electron donor, primary catalyst and hydrogen are sent to the polymerization reactor in order successively according to the predetermined dosage respectively through the batching device, the mole ratio of titanium and/or vanadium element within the primary catalyst to monomer is (0.01˜100)×10:1, the mole ratio of Al element in the co-catalysts to the titanium and/or vanadium element within the main catalyst is 1˜200:1, the mole ratio of hydrogen to the titanium and/or vanadium element within the main catalyst is 1˜2000:1, the copolymerization temperature is 20˜100° C., the feed mole ratio of butadiene to isoprene is 0.01˜50:100, the mole ratio of electron donor to the titanium and/or vanadium element within the main ...

INCLINED BASEPLATE IN DEHYDROGENATION REACTOR

An inclined baseplate for a radial bed reactor improves solids flow from the bottom of the reactor. Gas flow can be improved by utilizing an aerated baseplate or by providing a non-porous section of outer perforated cylinder in the area below the level of the bottom of the inner perforated cylinder. 1. A radial bed reactor with an inclined baseplate comprising:a reactor body;inner and outer perforated cylinders defining a catalyst bed, the catalyst bed having an inlet at an upper end of the catalyst bed and an outlet at a lower end of the catalyst bed, a first portion of the outer perforated cylinder extending below a bottom of the inner perforated cylinder, the first portion having a non-porous section;a baseplate extending from the bottom of the inner perforated cylinder toward a bottom of the outer perforated cylinder, the baseplate being inclined with respect to the inner perforated cylinder;a distribution space defined by at least the inner perforated cylinder;a collection space defined by the outer perforated cylinder and the reactor body;a feed inlet to the distribution space; anda product outlet from the collection space.2. The reactor of wherein the first portion of the outer perforated cylinder further comprises a porous section claim 1 , the porous section positioned below the non-porous section.3. The reactor of wherein the inner perforated cylinder further comprises louvers on the catalyst bed side.4. The reactor of wherein the non-porous section extends below a bottom of a lowest louver.5. The reactor of wherein a hole size claim 2 , a fraction of open area claim 2 , or both of the porous section are different from a hole size claim 2 , a fraction of open area claim 2 , or both of the outer perforated cylinder.6. The reactor of wherein a second portion of the outer perforated cylinder has a first section and a second section claim 1 , wherein the first section of the second portion is above the non-porous section of the first portion claim 1 , and ...

METHOD FOR PRODUCING A PARTICLE CONTAINING POROUS SILICA, POROUS SILICA, AND A PARTICLE CONTAINING POROUS SILICA

Provided is a process for producing satisfactory particles held in porous silica. The process comprises (a) the step of preparing porous silica, (b) the step of bringing the porous silica into contact with a liquid which contains either a metal or a compound that has the metal as a component element and infiltrating the liquid into the pores of the porous silica, and (c) the step of subjecting, after the step (b), the impregnated porous silica to a heat treatment to thereby form fine particles comprising the metal or the metal compound in the pores of the porous silica. When porous silica is synthesized by hydrolyzing an alkoxysilane in a solvent-free system, it is possible to synthesize porous silica having a fine pore diameter. Use of this porous silica as a template facilitates formation of particles (e.g., W, Cu, Cr, Mn, Fe, Co, or Ni or an oxide of any of these metals) that show peculiar properties not observed in the bulk material. 157-. (canceled)58. A method for producing a particle containing porous silica comprising the following steps:(a) preparing porous silica;(b) contacting the porous silica with solution containing a metal or a compound comprising the metal as a component element and thereby, impregnating pores of the porous silica with the solution; and(c) forming a minute particle containing the metal or the metal compound in the pores of the porous silica by heat treatment after the step (b),wherein an average pore diameter of the porous silica is 0.5 nm or more to 1.5 nm or less, andwherein an average diameter of the minute particle is 0.5 nm or more to 1.0 nm or less.59. The method according to claim 58 , wherein the metal compound is a metal oxide claim 58 , a metal sulfide or a metal nitride.60. The method according to claim 58 , wherein the minute particle comprises gold and the solution comprises a gold compound.61. The method according to claim 58 , wherein the solution comprises chloroauric acid aqueous solution.62. The method according to ...

Optimized Reactor Configuration for Optimal Performance of the Aromax Catalyst for Aromatics Synthesis

A naphtha reforming reactor system comprising a first reactor comprising a first inlet and a first outlet, wherein the first reactor is configured to operate as an adiabatic reactor, and wherein the first reactor comprises a first naphtha reforming catalyst; and a second reactor comprising a second inlet and a second outlet, wherein the second inlet is in fluid communication with the first outlet of the first reactor, wherein the second reactor is configured to operate as an isothermal reactor, and wherein the second reactor comprises a plurality of tubes disposed within a reactor furnace, a heat source configured to heat the interior of the reactor furnace; and a second naphtha reforming catalyst disposed within the plurality of tubes, wherein the first naphtha reforming catalyst and the second naphtha reforming catalyst are the same or different. 1. A method comprising:introducing a hydrocarbon feed stream to a first reactor operating under adiabatic naphtha reforming conditions, wherein the first reactor comprises a first naphtha reforming catalyst, and wherein the hydrocarbon feed stream comprises a convertible hydrocarbon;converting at least a portion of the convertible hydrocarbon in the hydrocarbon feed stream to an aromatic hydrocarbon in the first reactor to form a first reactor effluent;passing the first reactor effluent from the first reactor to a second reactor operating under isothermal naphtha reforming conditions, wherein the second reactor comprises a second naphtha reforming catalyst, and wherein the first naphtha reforming catalyst and the second naphtha reforming catalyst are the same or different;converting at least an additional portion of the convertible hydrocarbon in the first reactor effluent to an additional amount of the aromatic hydrocarbon in the second reactor to form a second reactor effluent; andrecovering the second reactor effluent from the second reactor, wherein an amount of the first naphtha reforming catalyst in the first ...

SLOTTED PLATE SCALLOPS

An apparatus in a radial reactor is described. The apparatus comprises a vertically elongated conduit extending around a circumference of an outer wall of the radial reactor, a vertically oriented cylindrical center pipe in the radial reactor, and a catalyst bed. The conduit comprises an inner face and an outer face and a pair of opposing sides. The inner face has a plurality of slots. The pair of opposing sides have a plurality of slots. There is a riser at a top of the vertically elongated conduit. The catalyst bed is defined by the center pipe and the inner face. 1. An apparatus in a radial reactor comprising:a vertically elongated conduit extending around a circumference of an outer wall of the radial reactor, the conduit comprising an inner face and an outer face and a pair of opposing sides, the inner face having a plurality of slots therein, the pair of opposing sides having a plurality of openings therein, and a riser at one end of the vertically elongated conduit;a vertically oriented cylindrical center pipe in the radial reactor; anda catalyst bed defined by the center pipe and the inner face.2. The apparatus of further comprising:at least one stiffener extending from the inner face to the outer face.3. The apparatus of wherein the at least one stiffener extends vertically less than a height of the vertically elongated conduit.4. The apparatus of wherein the at least one stiffener extends vertically from a bottom of the vertically elongated conduit to a location below a top of the vertically elongated conduit claim 2 , the location being a distance in a range of one half to twice a distance between the inner face and the center pipe.5. The apparatus of wherein the plurality of slots extend substantially across the inner face without interruption.6. The apparatus of wherein the plurality of slots are divided into at least two columns of slots separated by a solid portion of the inner face.7. The apparatus of wherein the inner face has more slots than the ...

Fcc yield selectivity improvements in high containment riser termination systems

The invention provides an improved system for separation technology intended to reduce unwanted catalyst/thermal reactions by minimizing contact of the hydrocarbons and the catalyst within the reactor.

Heavy Marine Fuel Compositions

A process for reducing the environmental contaminants in a ISO8217 compliant Feedstock Heavy Marine Fuel Oil, the process involving: mixing a quantity of the Feedstock Heavy Marine Fuel Oil with a quantity of Activating Gas mixture to give a feedstock mixture; contacting the feedstock mixture with one or more catalysts to form a Process Mixture from the feedstock mixture; separating the Product Heavy Marine Fuel Oil liquid components of the Process Mixture from the gaseous components and by-product hydrocarbon components of the Process Mixture and, discharging the Product Heavy Marine Fuel Oil. The Product Heavy Marine Fuel Oil is compliant with ISO 8217 for residual marine fuel oils and the Environmental Contaminants, which are selected from the group consisting of: a sulfur; vanadium, nickel, iron, aluminum and silicon and combinations thereof, have concentration less than 0.5 wt %. The Product Heavy Marine Fuel Oil can be used as or as a blending stock for an ISO 8217 compliant, IMO MARPOL Annex VI (revised) compliant low sulfur or ultralow sulfur heavy marine fuel oil. 1. A low sulfur heavy marine fuel oil , consisting essentially of a 100% hydroprocessed high sulfur heavy marine fuel oil , wherein prior to hydroprocessing the high sulfur heavy marine fuel oil is compliant with ISO 8217: 2017 and is of merchantable quality as a residual marine fuel oil , but Environmental Contaminants have a concentration greater than 0.5% wt. , wherein Environmental Contaminates are selected from the group consisting of: a sulfur; vanadium , nickel , iron , aluminum and silicon and combinations thereof and wherein the low sulfur heavy marine fuel oil is compliant with ISO 8217: 2017 and is of merchantable quality as a residual marine fuel oil and the Environmental Contaminants have concentration less than 0.5 wt %.2. The low sulfur heavy marine fuel oil of claim 1 , wherein sulfur is determined by ISO 14596 or ISO 8754; vanadium is determined by IP 501 or IP 470 or ISO 14597 ...

Heavy Marine Fuel Oil Composition

A process for reducing the environmental contaminants in a ISO 8217 compliant Feedstock Heavy Marine Fuel Oil, the process involving: mixing a quantity of the Feedstock Heavy Marine Fuel Oil with a quantity of Activating Gas mixture to give a feedstock mixture; contacting the feedstock mixture with one or more catalysts to form a Process Mixture from the feedstock mixture; separating the Product Heavy Marine Fuel Oil liquid components of the Process Mixture from the gaseous components and by-product hydrocarbon components of the Process Mixture and, discharging the Product Heavy Marine Fuel Oil. The Product Heavy Marine Fuel Oil is compliant with ISO 8217 for residual marine fuel oils and the sulfur and Specific Contaminants have concentration less than 0.5 wt %., wherein the Specific Contaminates are selected from the group consisting of: vanadium, sodium, aluminum, silicon, calcium, zinc, phosphorus, nickel, iron and combinations thereof. The Product Heavy Marine Fuel Oil can be used as or as a blending stock for an ISO 8217 compliant, IMO MARPOL Annex VI (revised) compliant low sulfur or ultralow sulfur heavy marine fuel oil.

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

A multi-stage process for the production of an ISO 8217 compliant Product Heavy Marine Fuel Oil from ISO 8217 compliant Feedstock Heavy Marine Fuel Oil involving a Reaction System composed of one or more reactor vessels selected from a group reactor wherein said one or more reactor vessels contains one or more reaction sections configured to promote the transformation of the Feedstock Heavy Marine Fuel Oil to the Product Heavy Marine Fuel Oil. The Product Heavy Marine Fuel Oil has a Environmental Contaminate level has a maximum sulfur content (ISO 14596 or ISO 8754) between the range of 0.05 mass % to 1.0 mass. A process plant for conducting the process for conducting the process is disclosed that can utilize a modular reactor vessel. 1. A process for the production of a Product Heavy Marine Fuel Oil , the process comprising: mixing a quantity of a Heavy Marine Fuel Oil feed with a quantity of an Activating Gas to give a Feedstock Mixture , wherein said Heavy Marine Fuel Oil feed complies with ISO 8217 (2017) as a residual marine fuel , except said Heavy Marine Fuel Oil feed has one or more Environmental Contaminants selected from the group consisting of: sulfur; vanadium , nickel , iron , aluminum and silicon and combinations thereof , and wherein said one or more Environmental Contaminants have a combined concentration greater than 0.5% wt.; distributing said Feedstock Mixture to a Reaction System , wherein the Reaction System is comprised of five or more reactor vessels , and wherein each of the five or more reactor vessels is independently selected from the group of operational configurations consisting of: dense packed fixed bed trickle reactor; dense packed fixed bed up-flow reactor; ebulliated bed three phase up-flow reactor; fixed bed divided wall reactor; fixed bed three phase bubble reactor; fixed bed liquid full reactor , fixed bed high flux reactor; fixed bed structured catalyst bed reactor; fixed bed reactive distillation reactor and combinations ...

Reactor for liquid phase fluorination reactions

The present invention relates to a hydrofluorinating process which comprises reacting a fluoroolefin with hydrogen fluoride in the liquid phase in the presence of a hydrofluorination catalyst in the reaction zone of a reactor, said reactor comprised of a reactor body having a length to diameter ratio of about 2:1 or greater; a stirred reaction zone containing said hydrofluorination catalyst, which may be prepared in situ, at least one inlet for supplying said hydrogen fluoride and fluoroolefin to the reaction zone and at least one outlet for recovering said fluoroalkane, said stirrer disposed in the reaction zone and comprising a plurality of blades fixedly attached to shaft drivable by a motor, said blades extending from about the bottom of the reaction zone to about the top of the reaction zone and said shaft extending on a longitudinal axis from the bottom of the reactor to the top of the reactor, said stirrer being rotated at a speed sufficient to promote a swirling of the liquid to effect the occurrence of hydrofluorination reaction and minimize overfluorination. The present invention also relates to said hydrofluorination reactor.

WALL FOR CATALYTIC BEDS OF REACTORS AND METHOD FOR REALIZING THE SAME

Catalytic chemical reactor comprising a perforated wall () adjacent to a supporting wall of the reactor or of a catalytic cartridge contained in the reactor, wherein said perforated wall comprises a plurality of panels () and comprises first sectors () resting on the supporting wall and second sectors () spaced from said supporting wall defining a cavity (), and wherein means are provided for local securing said gas-permeable wall to said supporting wall, said securing means comprising: a plurality of support elements () fixed to the supporting wall () and passing through respective openings () of the first sectors () of the gas-permeable wall and a respective plurality of locking elements () which can be associated with the said support elements, the panels of the gas-permeable wall being gripped between said supporting wall and said locking elements. 1. A catalytic chemical reactor comprising a catalytic bed and a gas-permeable wall facing the catalytic bed , wherein:said gas-permeable wall is an assembly of a plurality of panels and each of said panels extends over an angular sector of said permeable wall;the gas-permeable wall comprises first wall sectors which bear against a supporting wall adjacent to the gas permeable wall, and second wall sectors which are spaced from said supporting wall, the first sectors and the second sectors alternating with each other along the circumferential extension of the permeable wall;wherein said supporting wall is cylindrical or substantially cylindrical,wherein said second wall sectors comprise passages for a gas;the reactor further comprising local securing means of said gas-permeable wall to said supporting wall, said securing means comprising:a plurality of supports firmly fixed to the supporting wall and passing through respective openings of the first sectors of the gas-permeable wall;a respective plurality of locking elements which can be associated with said supports, the panels of the gas-permeable wall being clamped ...