СПОСОБ ГАЗОФАЗНОЙ ПОЛИМЕРИЗАЦИИ ОЛЕФИНОВ

Изобретение относится к способу газофазной полимеризации олефинов и полимеризации, проводимой в реакторе, имеющем взаимосвязанные полимеризационные зоны. Способ газофазной полимеризации α-олефинов CH2=CHR, где R представляет собой водород или углеводородный радикал, имеющий 1-12 углеродных атомов, осуществляют в первой и второй взаимосвязанных полимеризационных зонах. Один или более α-олефинов подают в присутствии катализатора. Растущие полимерные частицы проходят через первую из указанных зон (труба, идущая вверх) в условиях быстрого псевдоожижения, выходят из трубы, идущей вверх, и поступают во вторую из указанных полимеризационных зон (труба, идущая вниз), через которую они проходят вниз в уплотненной форме, выходят из трубы, идущей вниз, и повторно вводятся в указанную трубу, идущую вверх. Газовая смесь, присутствующая в трубе, идущей вверх, полностью или частично предотвращается от поступления в трубу, идущую вниз. Газообразная композиция внутри части трубы, идущей вниз, поддерживается ...

ЭЛЕМЕНТ В ВИДЕ ДВУХ ТРАПЕЦИЙ, УСТАНОВКА С ПСЕВДООЖИЖЕННЫМ СЛОЕМ И СПОСОБ ПРОВЕДЕНИЯ РЕАКЦИИ ГИДРИРОВАНИЯ НИТРОСОЕДИНЕНИЯ

Группа изобретений относится к реактору с псевдоожиженным слоем, конструктивному элементу в виде двух трапеций и реактору с псевдоожиженным слоем, содержащему конструктивный элемент в виде двух трапеций. Реактор с псевдоожиженным слоем для гидрирования содержит оболочку, газораспределитель и внутреннюю камеру, ограниченную внутренней стенкой оболочки и верхней поверхностью газораспределителя. Внутренняя камера имеет нижнюю часть, соответствующую верхней поверхности газораспределителя, и верхнюю часть в направлении центральной оси реактора с псевдоожиженным слоем. Вертикальное расстояние между нижней частью и верхней частью равно H, область внутренней камеры от нижней части и вверх до 0,1H, 0,2H, 0,3H, 0,4H, 0,5H, 0,6H, 0,7H или 0,8H представляет собой нижнюю область. Область внутренней камеры от верхней части и вниз до 0,1H, 0,2H, 0,3H, 0,4H, 0,5H, 0,6H, 0,7H или 0,8H представляет собой верхнюю область. Область внутренней камеры между нижней областью и верхней областью представляет собой ...

УСТРОЙСТВА ДЛЯ РАСПРЕДЕЛЕНИЯ ТЕКУЧЕЙ СРЕДЫ

Группа изобретений относится к устройству распределения текучей среды, а также к блоку обработки текучей среды в сосуде с псевдоожиженным слоем. Указанное устройство включает в себя стояк, имеющий первый конец и второй конец. Устройство включает крышку, выполненную с возможностью функционального соединения со вторым концом стояка. Крышка имеет внутреннюю поверхность и внешнюю поверхность с множеством отверстий, образованных между внутренней и внешней поверхностями. Устройство включает в себя по меньшей мере один распределительный выступ, проходящий радиально наружу от крышки. По меньшей мере один распределительный выступ имеет внутреннюю поверхность и внешнюю поверхность. По меньшей мере один распределительный выступ имеет множество отверстий между внутренней поверхностью и внешней поверхностью. Блок обработки включает в себя сосуд, образующий внутреннее пространство, и устройство распределения текучей среды, включающее в себя стояк, установленный во внутреннем пространстве сосуда, имеющий ...

ПРОЦЕССЫ И УСТРОЙСТВО ДЛЯ КРЕКИНГА С ПСЕВДООЖИЖЕННЫМ КАТАЛИЗАТОРОМ

Изобретение относится к системе для обработки углеводородов, содержащей реактор с восходящим потоком в комбинации с реактором псевдоожиженного слоя. Выходы реактора с восходящим потоком и реактора со смешанным потоком обрабатываются в системе разделения, выполненной с возможностью приема выходящего потока углеводородов реактора с восходящим потоком и выходного потока реактора с восходящим потоком в сосуде для отделения катализатора, и катализаторы, используемые в каждом реакторе, могут быть регенерированы в регенераторе для регенерации катализатора. Также система включает охладитель частиц катализатора. Изобретение также касается способа для обработки углеводородов. Технический результат - максимизация производства легких олефинов. 2 н. и 9 з.п. ф-лы, 6 ил.

РАСПРЕДЕЛИТЕЛЬ ОТРАБОТАВШЕГО КАТАЛИЗАТОРА

Изобретение относится к способу и устройству, предназначенным для улучшения распределения как отработавшего катализатора, так и транспортирующих газов переноса в регенераторе установки крекинга с псевдоожиженным катализатором. Распределитель отработавшего катализатора, предназначенный для использования в регенераторе установки с псевдоожиженным катализатором, содержит: трубопровод, отверстие которого заканчивается внутри указанного регенератора, предназначенный для подачи смеси отработавшего катализатора и транспортирующего газа в регенератор; первый диск, окружающий отверстие трубопровода на верхнем торце трубопровода, в регенераторе; второй диск, расположенный на некотором расстоянии вверх от первого диска и жестко соединенный с ним (первым диском), так что благодаря этому между ними формируется, по существу, открытое пространство; конус отражателя, прикрепленный своим основанием ко второму диску, причем конус отражателя направлен вниз и установлен по центру над выходным отверстием трубопровода ...

СИСТЕМА ДЛЯ ОБЕССЕРИВАНИЯ С МЕХАНИЗМОМ ПЕРЕНОСА СОРБЕНТА

Изобретение относится к способу и установке для удаления серы из содержащих углеводороды потоков текучей среды. Способ обессеривания включает стадии: а) контактирование углеводородсодержащего потока текучей среды с твердыми частицами сорбента в реакторе, (b) повышение давления в шлюзовом бункере реактора до давления наполнения, (с) транспортировку наполненных серой частиц сорбента из реактора в находящийся под давлением шлюзовой бункер реактора, (d) сброс давления в наполненном шлюзовом бункере под высоким давлением до давления выпуска, (е) транспортировку наполненных серой частиц сорбента из находящегося при низком давлении наполненного шлюзового бункера реактора в регенератор и (f) контактирование частиц сорбента с содержащим кислород регенерирующим потоком. Установка обессеривания содержит реактор с псевдоожиженным слоем сорбента, приемник реактора для приема наполненных серой частиц сорбента, шлюзовой бункер реактора, регенератор с псевдоожиженным слоем для приема наполненных серой ...

УСТРОЙСТВО, ИСПОЛЬЗУЕМОЕ В ПСЕВДООЖИЖЕННОМ РЕАКЦИОННОМ ПРОЦЕССЕ

Изобретение относится к устройству для направления и поддержки райзера, используемому в псевдоожиженном реакционном процессе. Устройство содержит резервуар, райзер, расположенный в резервуаре, и множество наклонных направляющих опор, каждая из которых содержит трубчатую секцию, имеющую первый конец и второй конец, первый шарнир, первый конец которого соединен с первым концом трубчатой секции, второй шарнир, первый конец которого соединен со вторым концом трубчатой секции, при этом второй конец первого шарнира соединен с внутренней поверхностью резервуара, а второй конец второго шарнира соединен с направляющим устройством райзера, которое включает непрерывную по окружности конструкцию вокруг внешней стороны райзера. Изобретение обеспечивает прямое или косвенное боковое направление райзера в резервуаре, а также горизонтальное или вертикальное направление райзера во время значительного термического расширения, во время псевдоожиженного реакционного процесса. 7 з.п. ф-лы, 8 ил.

УСТРОЙСТВО ДЛЯ КОНТАКТИРОВАНИЯ ГАЗА И ТВЕРДОГО МАТЕРИАЛА

Изобретение относится к устройству для обработки потока материала в виде частиц за счет контакта с потоком газа. Устройство (10) для обработки потока материала в виде частиц за счет контакта с потоком газа, содержащее корпус (12), образующий рабочую камеру (18). Эта камера (18) содержит газораспределительную пластину (30), имеющую отверстия (32). Газораспределительная пластина (930) отделяет нижнюю газовую напорную камеру (18) от зоны (22) контакта газа с твердым веществом. Зона (22) контакта имеет по меньшей мере одну цилиндрическую перегородку, отходящую вертикально вверх от газораспределительной пластины, отделяющую внутреннюю секцию (36) от соседней кольцевой наружной секции (38; 40). Указанная по меньшей мере одна перегородка снабжена перепускным отверстием (50) для материала в виде частиц. Корпус (12) также имеет вход (44) для подачи материала в виде частиц во внутреннюю секцию (36) и выход (42) для выпуска обработанного материала в виде частиц из кольцевой наружной секции (40). Технический ...

СИСТЕМА ОКИСЛЕНИЯ С ВТОРИЧНЫМ РЕАКТОРОМ ДЛЯ БОКОВОЙ ФРАКЦИИ

Изобретение относится к усовершенствованному способу получения композиции ароматической дикарбоновой кислоты, включающему (а) проведение окисления многофазной реакционной среды в реакторе первичного окисления с получением в результате первой суспензии; (b) проведение дополнительного окисления, по меньшей мере, части указанной первой суспензии в реакторе вторичного окисления, где указанный реактор вторичного окисления представляет собой реактор по типу барботажной колонны, причем способ дополнительно включает введение ароматического соединения в указанный реактор первичного окисления, где, по меньшей мере, приблизительно 80% мас. указанного ароматического соединения, введенного в указанный реактор первичного окисления, окисляется в указанном реакторе первичного окисления, причем головные газы перемещают из верха реактора вторичного окисления в реактор первичного окисления. Раскрыты оптимизированный процесс и оборудование для более эффективного и экономичного проведения жидкофазного окисления ...

РЕАКТОР С ПСЕВДООЖИЖЕННЫМ СЛОЕМ, ТРЕХФАЗНЫЙ ШЛАМОВЫЙ РЕАКТОР И СПОСОБЫ ОБЕСПЕЧЕНИЯ ИХ ФУНКЦИОНИРОВАНИЯ (ВАРИАНТЫ)

Изобретение относится к реакторам с псевдоожиженным слоем. Один из вариантов раскрывает способ обеспечения функционирования двухфазного реактора с псевдоожиженным слоем, включающий следующие операции: подачу на низком уровне по меньшей мере одного газообразного реагента в вертикально расположенную псевдоожиженную массу твердых частиц, причем псевдоожиженная масса находится по меньшей мере в двух вертикально идущих стволах, расположенных рядом друг с другом внутри общей оболочки реактора, при этом каждый ствол разделен на множество вертикально идущих каналов, по меньшей мере часть которых имеют связь по потоку псевдоожиженной массы, причем псевдоожиженная масса присутствует по меньшей мере в некоторых из каналов, при этом по меньшей мере некоторые из стволов и/или каналов ограничены поверхностями теплообмена; создание условий для реакции газообразного реагента, когда он проходит вверх через псевдоожиженную массу, присутствующую по меньшей мере в некоторых из каналов стволов, в результате ...

ПНЕВМАТИЧЕСКАЯ СИСТЕМА ПЛОТНОЙ ЗАГРУЗКИ КАТАЛИЗАТОРА В БАЙОНЕТНЫЕ ТРУБЫ ДЛЯ РЕАКТОРА-ТЕПЛООБМЕННИКА КОНВЕРСИИ С ВОДЯНЫМ ПАРОМ

Изобретение относится к устройству и способу загрузки каталитических труб, используемых в трубчатых реакторах-теплообменниках, которые могут быть использованы при конверсии с водяным паром природного газа или различных углеводородных фракций с целью получения синтез-газа. Для плотной и равномерной загрузки катализатора в реактор-теплообменник конверсии с водяным паром, состоящий из множества систем из двух коаксиальных труб с кольцевым пространством между ними, заключенных в каландр, кольцевое пространство разделено на два или три одинаковых горизонтальных сектора. Каждый сектор простирается на всю длину труб посредством «центратора», расположенного в верхней части кольцевого пространства, и каждый сектор снабжен собственной системой съемных дефлекторов. Дефлекторы соединены между собой цепью, которая наматывается вокруг барабана, расположенного вне заполняемой трубы. Частицы катализатора подают в кольцевое пространство посредством воронки. 2 н. и 4 з.п. ф-лы, 2 ил., 1 пр.

МНОГОРЕАКТОРНАЯ И МНОГОЗОНАЛЬНАЯ ПОЛИМЕРИЗАЦИЯ ПОЛИОЛЕФИНА

Настоящее изобретение относится к группе изобретений, а именно к вариантам устройства для производства мультимодального полиэтилена. Устройство для производства мультимодального полиэтилена содержит: первый реактор, выполненный с возможностью производства первого полиэтилена; второй реактор, выполненный с возможностью производства второго полиэтилена и третьего полиэтилена, причем второй реактор содержит: восходящую трубу, выполненную с возможностью производства второго полиэтилена; верхний трубопровод, имеющий конец, соединенный по текучей среде с верхней частью восходящей трубы; сепаратор, соединенный по текучей среде с противоположным концом верхнего трубопровода; спускную трубу, выполненную с возможностью производства третьего полиэтилена, при этом верхняя часть спускной трубы соединена по текучей среде с сепаратором через жидкостный барьер в верхней части спускной трубы; нагревательное устройство, выполненное с возможностью добавления или отведения тепла из спускной трубы; и нижний ...

УСТРОЙСТВО И СПОСОБ РЕГУЛИРОВАНИЯ ПОТОКА ТВЕРДЫХ ЧАСТИЦ И РЕАКТОР С ПСЕВДООЖИЖЕННЫМ СЛОЕМ

Изобретения относят к регулированию потоков твердых частиц. Описано устройство регулирования потока твердых частиц, которое содержит вертикальную впускную трубу для направления потока твердых частиц вниз по ней, и нижняя часть которой находится на уровне L0, первый выпускной желоб и второй выпускной желоб, находящиеся в соединении по потоку частиц с вертикальной впускной трубой, и средства псевдоожижения для направления регулируемых первого и второго субпотоков, образованных из потока твердых частиц, в первый и второй выпускные желоба, устройство содержит ответвление, находящееся в соединении по потоку частиц с отверстием в боковой стенке вертикальной впускной трубы, для направления первого субпотока твердых частиц в первый выпускной желоб, причем отверстие имеет нижний край, находящийся на уровне L1, который выше, чем L0, и ответвление содержит переливной барьер, через который должны пройти твердые частицы, чтобы попасть в первый выпускной желоб, и причем отверстие имеет верхний край, ...

УСТАНОВКА КИПЯЩЕГО СЛОЯ

Полезная модель относится к оборудованию для термической обработки сыпучих материалов в кипящем слое и может быть использована, например, для их сушки в химической, строительной, фармацевтической и других отраслях промышленности. В установке кипящего слоя, содержащей цилиндрический корпус с загрузочным патрубком, газораспределительную решетку, патрубок подвода газа, патрубок отвода газодисперсной смеси и циклон, внутри корпуса с зазором к его внутренней поверхности размещена цилиндрическая обечайка, в верхней части которой установлена цилиндроконическая вставка с аксиальными лопастями, образующими наклонные каналы для закручивания потока газодисперсной смеси. Технический результат предлагаемой полезной модели заключается в повышении производительности установки кипящего слоя при одновременном повышении качества термообработанного сыпучего материала.

СПОСОБ ПОЛУЧЕНИЯ ТРИХЛОРСИЛАНА И КРЕМНИЙ ДЛЯ ИСПОЛЬЗОВАНИЯ В ПОЛУЧЕНИИ ТРИХЛОРСИЛАНА

Изобретение относится к способу получения трихлорсилана. Производят взаимодействия кремния с газообразным HCl при температуре между 250°С и 1100°С и абсолютном давлении 0,5-30 атм. Процесс может быть осуществлён в реакторе с псевдоожиженным слоем, в реакторе с перемешиваемым слоем или в реакторе со сплошным слоем. Кремний, подаваемый на взаимодействие, содержит 40-10000 ч./млн бария по массе и возможно 40-10000 ч./млн меди по массе. Изобретение обеспечивает увеличение селективности процесса получения трихлорсилана. 2 н. и 12 з.п. ф-лы, 4 ил., 2 табл., 4 пр.

СИСТЕМА РЕАКТОРА С ПСЕВДООЖИЖЕННЫМ СЛОЕМ, ИМЕЮЩАЯГАЗОСБОРНИК ДЛЯ ВЫПУСКАЕМОГО ГАЗА

Изобретение относится к устройству, в котором сжигание происходит в псевдоожиженном слое топлива. Система реактора с циркулирующим псевдоожиженным слоем содержит реакционную камеру, имеющую псевдоожиженный слой твердых частиц и образованную потолком, дном и стенками, по меньшей мере частично образованными панелями водяных труб, средство введения газа для псевдоожижения в реакционную камеру, по меньшей мере, два выпускных отверстия, расположенных в стенках реакционной камеры, для удаления суспензии частиц из выпускаемых газов и твердых частиц из реакционной камеры, по меньшей мере, два сепаратора частиц, соединенных с выпускными отверстиями, для сепарации твердых частиц из суспензии частиц, и имеющих каждый выпускное отверстие для газа в его верхней части для выпуска очищенных выпускаемых газов, соединенное с выпускным каналом, секцию для рекуперации теплоты, в которую направляются очищенные выпускаемые газы, и газосборник, образованный кожухом, содержащим потолок, дно и стенки, размещенный ...

СПОСОБ И УСТРОЙСТВО ДЛЯ ДЕПОЛИМЕРИЗАЦИИ

... 1. Способ регенерации мономерных сложных эфиров замещенной или незамещенной акриловой кислоты, мономерного стирола и/или мономерных производных стирола из содержащего соответствующие структурные единицы полимерного материала, причем осуществляют контакт полимерного материала с теплоносителем в обогреваемом реакторе (1; 51), теплоноситель и полимерный материал в реакторе (1; 51) приводят в движение и образующийся в реакторе (1; 51), содержащий мономер газ выводят из реактора (1; 51), причем теплоноситель состоит из множества сферических частиц (67), прежде всего обладающих диаметром от 0,075 до 0,25 мм. 2. Способ по п.1, причем полимерный материал содержит акриловые соединения и средняя температура частиц (67) теплоносителя в реакторе (1; 51) составляет от 250 до 600°С. 3. Способ по п.1, причем реактор (1; 51) имеет электрообогрев. 4. Способ по одному из пп.1-3, причем сферические частицы (67) выполнены из материала, не участвующего в протекающих при регенерации мономера реакциях. 5. Способ ...

РАСПРЕДЕЛИТЕЛЬНОЕ ДНИЩЕ ДЛЯ РАСПРЕДЕЛЕНИЯ ГАЗА, СОДЕРЖАЩЕГО МЕЛКИЕ ЧАСТИЦЫ ТВЕРДОГО ВЕЩЕСТВА

... 1. Распределительное днище (1), в частности, распределительное днище с соплами, для распределения газа, содержащего тонкие частицы твердого вещества, предназначенное преимущественно для применения в агрегате с кипящим слоем, для восстановления частиц твердого вещества, содержащих окись металла, причем на распределительном днище (1) расположено, по меньшей мере, одно очистительное устройство, которое позволяет уменьшить во время работы распределительного днища образование отложений на распределительном днище, в частности, на соплах (2) днища (1) и/или, по меньшей мере, частично удалить уже образовавшиеся отложения, отличающееся тем, что очистительное устройство содержит средство (3) для очистки распределительного днища путем непосредственного механического ударного воздействия на распределительное днище, в частности, на сопла распределительного днища. 2. Распределительное днище по п. 1, отличающееся тем, что средство (3) для очистки распределительного днища выполнено с возможностью восприятия ...

СПОСОБ ОКИСЛЕНИЯ ХЛОРИСТОГО ВОДОРОДА КИСЛОРОДОМ

... 1. Способ проведения процесса окисления хлористого водорода а) кислородом которое может протекать в присутствии катализатора, с б) одностадийным или многостадийным охлаждением газообразных продуктов реакции, с выделением в) из газообразных продуктов реакции непрореагировавшего хлористого водорода и образовавшейся в реакции воды, с сушкой г) газообразных продуктов реакции и с выделением д) хлора из смеси, отличающийся тем, что окисление хлористого водорода а) проводят в реакторе, у которого контактирующие с реакционной смесью элементы конструкции изготовлены из никеля или из содержащего никель сплава, причем содержание никеля составляет не менее 60 мас.%, в частности конструкционный материал выбирают из ряда: С-типы Hastelloy®, В-типы Hastelloy®, Inconel® 600, Inconel® 625. ! 2. Способ по п.1, отличающийся тем, что охлаждение б) реакционных газов проводят в первом теплообменнике, начиная от температуры на выходе из реактора до температуры от 140 до 250°C, в предпочтительном случае от 160 ...

ГАЗОФАЗНЫЙ ПРОЦЕСС И УСТАНОВКА ДЛЯ ПОЛИМЕРИЗАЦИИ ОЛЕФИНОВ

... 1. Газофазный способ полимеризации одного или нескольких α-олефинов в реакторе с псевдоожиженным слоем в присутствии катализатора полимеризации, причем указанный реактор псевдоожиженного слоя оборудован решеткой для псевдоожижения, расположенной в его основании, и внешними устройствами для рециркуляции и охлаждения непрореагировавшего газа с верха указанного реактора к указанной решетке для псевдоожижения, где способ отличается тем, что осуществляют: ! (i) непрерывный пневматический рецикл полимера посредством циркуляционной петли, связывающей указанную решетку для псевдоожижения с верхней областью реактора с псевдоожиженным слоем; ! (ii) непрерывную выгрузку полимера из зоны указанной циркуляционной петли, имеющей концентрацию полимера выше, чем концентрация полимера внутри слоя псевдоожиженного полимера. ! 2. Способ согласно п.1, в котором указанная циркуляционная петля включает практически вертикальный стояк и трубу пневматического конвейера. ! 3. Способ согласно п.1, в котором порошок ...

СПОСОБ ЭФФЕКТИВНОЙ ПРОДУВКИ ПОЛИМЕРНЫХ ЧАСТИЦ

ОЧИСТКА ЗАГРЯЗНЕННЫХ ЖИДКОСТЕЙ

... 1. Способ удаления загрязнителей из некоторого количества загрязненной жидкости, содержащий этапы, на которых:подают жидкость в очистной резервуар, содержащий материал адсорбента на основе углерода, обладающий способностью к электрохимической регенерации и расположенный в форме слоя частиц на дне резервуара;перемешивают слой для распределения материала адсорбента в жидкости и адсорбции из жидкости загрязнителей;прекращают перемешивание и дают слою материала осесть;регенерируют адсорбент, пропуская электрический ток через слой для высвобождения из адсорбента газообразных продуктов, полученных из загрязнителя, в форме пузырьков, поднимающихся сквозь жидкость в резервуаре, иудаляют очищенную жидкость из бака.2. Способ по п.1, в котором этапы перемешивания слоя и осаждения слоя и регенерирования адсорбента повторяют для удаления дополнительного количества загрязнителя из жидкости перед ее извлечением.3. Способ по п.1 или 2, в котором слой материала адсорбента перемешивают путем подачи текучей ...

УСТРОЙСТВА ДЛЯ НАГНЕТАНИЯ ПОТОКОВ ГАЗА В ПСЕВДООЖИЖЕННЫЙ СЛОЙ ТВЕРДЫХ ЧАСТИЦ

... 1. Нагнетательная форсунка для использования в газораспределительном устройстве, содержащая:трубку, имеющую впуск для текучей среды, выпуск для текучей среды, внутренний диаметр и осевую длину;причем впуск для текучей среды содержит множество отверстий, ограничивающих поток, распределенных по осевому концу трубки.2. Нагнетательная форсунка для использования в газораспределительном устройстве, содержащая:трубку, имеющую впуск для текучей среды и выпуск для текучей среды,причем впуск для текучей среды содержит множество ограничивающих поток отверстий, распределенных по окружности и проходящих сквозь трубку.3. Форсунка по п.1 или 2, в которой отношение внутреннего диаметра выпуска для текучей среды трубки к диаметру по меньшей мере одного ограничивающего поток отверстия превышает 2:1.4. Форсунка по п.1 или 2, в котором осевая длина трубки по меньшей мере в 5 раз превышает внутренний диаметр выпуска для текучей среды трубки.5. Форсунка по п.1, в которой ограничивающие поток отверстия аксиально ...

СПОСОБ И УСТРОЙСТВО ДЛЯ ПОЛИМЕРИЗАЦИИ ПРОПИЛЕНА

... 1. Способ получения гетерофазных пропиленовых сополимеров путем полимеризации пропилена в присутствии катализатора полимеризации и водорода в качестве регулятора молекулярного веса, включающий следующие стадии: а) полимеризация пропилена в газовой или жидкой фазе, необязательно совместно с одним или более α-олефиновыми сомономерами, с получением фракции кристаллического полимера; b) сополимеризация этилена с пропиленом и/или 1-бутеном и необязательно одним или более альфа-олефиновыми сомономерами С5-С12 в газофазном реакторе с соединенными друг с другом зонами полимеризации, где растущие полимерные частицы перетекают снизу вверх через первую зону полимеризации (устройство с восходящим потоком) в условиях быстрого псевдоожижения или транспортирования, покидают упомянутое устройство с восходящим потоком и поступают во вторую зону полимеризации (устройство с нисходящим потоком), через которую они перетекают сверху вниз под действием силы тяжести, покидают упомянутое устройство с нисходящим ...

ТЕХНОЛОГИЧЕСКАЯ СХЕМА НОВОГО РЕАКТОРА ДЕГИДРИРОВАНИЯ ПРОПАНА ДО ПРОПИЛЕНА

... 1. Способ дегидрирования пропана, включающий:пропускание предварительно нагретого исходного потока пропана в реактор дегидрирования;смешивание и взаимодействие исходного потока пропана с псевдоожиженным неметаллическим катализатором в реакторе дегидрирования, который представляет собой реактор быстрого псевдоожижения с образованием потока продукта, содержащего пропилен, причем катализатор находится в реакторе при среднем времени пребывания от 15 до 45 минут;пропускание отработанного катализатора в блок регенерации катализатора с образованием потока регенерированного катализатора; ипропускание потока регенерированного катализатора в реактор дегидрирования.2. Способ по п.1, в котором реактором быстрого псевдоожижения управляют при условиях обратного смешивания катализатора и реагентов.3. Способ по п.1, в котором условия реакции включают температуру от 600°C до 700°C.4. Способ по п.1, в котором условия реакции включают давление на выходе реактора в диапазоне от 108 кПа до 170 кПа.5. Способ ...

СПОСОБЫ ПОЛУЧЕНИЯ ТРИФТОРИДА АЛЮМИНИЯ

... 1. Способ получения трифторида алюминия, включающий:приведение в контакт фторалюминатного сырья, содержащего, по меньшей мере, около 30% вес. фторидов щелочного металла или щелочноземельного металла и алюминия, и кислоты с получением трифторида алюминия и, по меньшей мере, одного побочного продукта.2. Способ по п.1, в котором сырье содержит по меньшей мере, около 50%, по меньшей мере, около 70%, по меньшей мере, около 80%, по меньшей мере, около 90%, от примерно 30% до примерно 95% или от примерно 70% до примерно 95% вес. фторидов щелочного металла или щелочноземельного металла и алюминия.3. Способ по п.1, в котором кислота выбрана из соляной кислоты, серной кислоты и их смесей.4. Способ по п.1, в котором кислота представляет собой соляную кислоту.5. Способ по п.1, в котором сырье приводят в контакт с кислотой в отсутствие источника кремния.6. Способ по п.1, в котором щелочной или щелочноземельный металл выбран из лития, натрия, калия, магния, бария, кальция и их смесей.7. Способ по п.1 ...

СИСТЕМА КАМЕРЫ СГОРАНИЯ ТОПЛИВНОГО ГАЗА С КИПЯЩИМ СЛОЕМ ДЛЯ ПРОЦЕССА КАТАЛИТИЧЕСКОЙ ДЕГИДРОГЕНИЗАЦИИ

ТЕПЛООБМЕННИК ДЛЯ ПРОВЕДЕНИЯ ЭКЗОТЕРМИЧЕСКОЙ РЕАКЦИИ

... 1. Съемный модуль (1) охлаждения, имеющий первый и второй концы, предназначенный для использования в реакторе (20) для проведения экзотермической реакции, содержащий трубу (2) для подачи хладагента, распределительную камеру (4), большое количество циркуляционных труб (5) и коллекторную камеру (6), при этом на первом конце указанной трубы (2) для подачи хладагента имеется входной патрубок (3), служащий для подачи в модуль (1) охлаждения хладагента, а вторым концом труба (2) сообщается с указанной распределительной камерой (4), каждая из указанных циркуляционных труб (5) сообщается с распределительной камерой (4) посредством первого конца и сообщается посредством второго конца с указанной коллекторной камерой (6), причем коллекторная камера (6) имеет выходной патрубок (7) для отвода хладагента, входной патрубок (3) и выходной патрубок (7) расположены на одном и том же конце модуля (1) охлаждения, входной патрубок (3) приспособлен для присоединения к подводящему трубопроводу (8) с помощью ...

СМЕШИВАЮЩАЯ РАСХОДНАЯ РЕЗЕРВУАРНАЯ СИСТЕМА

... 1. Расходная резервуарная система для хранения суспензии, содержащая:резервуар для хранения, имеющий первый конец, второй конец и, по меньшей мере, одну стенку, окружающую внутренний объем между первым и вторым концами;впуск для суспензии в сообщении по текучей среде с внутренним объемом;выпуск в сообщении по текучей среде с внутренним объемом;впуск для рециркуляции в сообщении по текучей среде с внутренним объемом у первого конца резервуара для хранения;насос, имеющий всасывающую линию в сообщении по текучей среде с выпуском;клапан рециркуляции в сообщении по текучей среде с выпускной линией насоса и впуском для рециркуляции; ивыпускной клапан в сообщении по текучей среде с выпускной линией насоса.2. Система по п. 1, дополнительно содержащая дефлектор, расположенный в данном внутреннем объеме, и выполненный с возможностью перенаправления потока между впуском для суспензии и впуском для рециркуляции.3. Система по п. 1, в которой указанный первый конец наклонен в направлении впуска для рециркуляции ...

СПОСОБ ОКИСЛЕНИЯ В РЕАКТОРЕ С ПСЕВДООЖИЖЕННЫМ СЛОЕМ

... 1. Способ проведения реакции в реакторе с псевдоожиженным слоем по меньшей мере одного способного окисляться реагента с молекулярным кислородом в присутствии каталитически активного псевдоожиженного слоя твердых частиц, причем в этом способе содержащий молекулярный кислород газ, концентрация кислорода в котором превышает его концентрацию в воздухе, вводят в псевдоожиженный слой при одновременном поддержании в псевдоожиженном слое турбулентного режима. 2. Способ по п.1, в котором турбулентный режим характеризуется соотношением скорость перехода (Uk): конечная скорость (Ut) в интервале от 0,1:1 до 25:1. 3. Способ по п.1 или 2, в котором твердые частицы обладают диаметром в интервале от 20 до 300 мкм. 4. Способ по п.3, в котором распределение по диаметрам частиц составляет по меньшей мере 20 мкм. 5. Способ по п.1 или 2, в котором псевдоожиженный слой включает твердые частицы, размеры которых находятся в соответствии с одним или несколькими из следующих независимых критериев: (I) по меньшей ...

VERFAHREN ZUR HERSTELLUNG VON CHLOR.

VERFAHREN UND VORRICHTUNG ZUR BEHANDLUNG VON PULVER.

Verfahren zur Durchfuehrung exothermer chemischer Reaktionen zwischen gasfoermigen Reaktionsteilnehmern unter Gewinnung mechanischer Energie

Verfahren und Vorrichtung zur Umsetzung eines festen, in Teilchenform vorliegenden, in der Hitze verdampfbaren Reaktionsteilnehmers mit einem gasfoermigen Reaktionsteilnemer

Vorrichtung zum Waerme- oder Stoffaustausch zwischen einem feinkoernigen oder staubfoermigen Gut und einem gasfoermigen Medium

Vorrichtung zum Behandeln von in Pulverform oder als Granulat vorliegenden Stoffen

Thermoplastische Polyurethane

Verfahren zur Herstellung von thermoplastischem Polyurethan, dadurch gekennzeichnet, dass man die Ausgangsstoffe zur Herstellung der thermoplastischen Polyurethane mischt und, die Mischung enthaltend, die Ausgangsstoffe versprüht.

Verfahren und Anlage zur Wärmebehandlung von eisenoxidhaltigen Feststoffen

Verfahren zur Wärmebehandlung von eisenoxidhaltigen Feststoffen, bei dem feinkörnige Feststoffe in einem Reaktor (8) mit Wirbelbett auf eine Temperatur von 700 bis 1.150°C erhitzt werden, dadurch gekennzeichnet, dass ein erstes Gas oder Gasgemisch von unten durch wenigstens ein Gaszufuhrrohr (9) in einen Wirbelmischkammerbereich (15) des Reaktors (8) eingeführt wird, wobei das Gaszufuhrrohr (9) wenigstens teilweise von einer durch Zufuhr von Fluidisierungsgas fluidisierten, stationären Ringwirbelschicht (12) umgeben wird, und dass die Gasgeschwindigkeiten des ersten Gases oder Gasgemisches sowie des Fluidisierungsgases für die Ringwirbelschicht (12) derart eingestellt werden, dass die Partikel-Froude-Zahlen in dem Gaszufuhrrohr (9) zwischen 1 und 100, in der Ringwirbelschicht (12) zwischen 0,02 und 2 sowie in der Wirbelmischkammer (15) zwischen 0,3 und 30 betragen.

Fluidized bed reactor

... 1,108,313. Fluidized bed reactors. DORROLIVER Inc. 13 July, 1965 [16 July, 1964], No. 29618/65. Heading B1F. Apparatus for the calcination of finely divided minerals comprises a preheat system 10, a reactor 12 and cyclones 54 and 60. Solids to be treated e.g. limestone or phosphate rock, pass to chamber 14 by conduit 34, and thence by conduits 38 and 40 successively into chambers 16 and 18, before passing into calcination system 12 by conduits 42 and 45 and valve 44. Fluidizing and preheating gas from calcination system 12 passes by cyclone 54 and windbox 20 before passing up through chambers 18, 16, and 14 and perforated plates 19, 17 and 15. Exhaust gas passes by conduit 59 to cyclone 60, whence fines are delivered back to calcination system 12. Calcination system 12 comprises constriction plates 25 and 24 separating windbox 26, cooling chamber 24 and calcination chamber 22. Fuel is introduced by inlet 72 into calcination chamber 22 to maintain its temperature at about 1800‹F. Solids ...

FLUIDIZED CATALYTIC CRACKING PROCESS

... 1413978 Cracking UNIVERSAL OIL PRODUCTS CO 20 Dec 1972 [27 Dec 1971] 58723/72 Heading C5E In a catalytic cracking process in which a stream of cracked oil and catalyst is discharged from a riser (2) into a reception zone (1) in which there are a dilute phase in the upper portion (3) and a fluidized dense bed in the lower portion (4), and catalyst is discharged from the dense bed, the stream of cracked oil and catalyst is discharged into the dilute phase downwards at a point (12) near the inlet (13) of a cyclone separator but far enough above the dense bed to maintain a low average density (less than 10 -lb./ft.3) in the dilute phase.

An apparatus for the suspension gasification of finely divided fuel

... 725,896. Gasifying finely divided fuels. KOPPERS GES., H. July 24, 1953 [July 25, 1952], No. 20625/53. Class 55(1). In gasifying finely divided fuels in suspension in oxygen or oxygen enriched air and possibly endothermic reacting media a metal gas withdrawal pipe 6 from the upper part of a reaction chamber of refractory material projects downwardly into the chamber and has a water &c. cooling jacket 7. Both are supported outside and independently of the chamber on carriers 8.

Process and plant for the thermal treatment of fine-grained solids

Improvements in or relating to the conveying of solid particles through a pipeline by means of carrier gas

... 1,066,152. Pneumatic conveying. ALLIED CHEMICAL CORPORATION. July 13, 1965 [July 14, 1964], No. 29720/65. Heading B8A. A system for conveying comminuted solid particles of coal admixed with a pressurized carrier gas, e.g. steam, from a coal crusher chamber 23 to a main 28 feeding a plurality of coking chambers, comprises a pipeline 27 having gas injectors 37 spaced therealong and bleed-off devices for centrifugally separating the particles from the gas whereby a portion of the particle free gas is withdrawn from the system in order that the steam pressure, conveying velocity, and steam/coal weight ratio may be controlled. A pressurized coal line 21 is fed with steam via pipe 24, the mixture being admitted to the chamber 23 through gate valve 25. The steam injectors 37 are supplied from a steam line 35 and inject at sonic or supersonic adjustable velocity into the pipeline 27 in the direction of flow to boost the velocity thereof. A first separating and bleed-off device comprises a curvilinear ...

Slurry bubble column reactor

Subjecting solid objects to conditioning gas with whriling motion

... 1,142,762. Drying and cooling apparatus. R. E. FUTER. 2 Aug., 1966 [13 Sept., 1965], No. 34547/66. Headings F4G and F4U. [Also in Division A2] In apparatus for conditioning, e.g. chilling, freezing, drying or humidifying, solid products in the form of particles, e.g. grain, berries, nuts, sawdust, cement or plastic nibs or powder, the particles are fed into a chamber and whirled in a stream of a conditioning gas, such as air, nitrogen, carbon dioxide or methane, which is fed into the chamber so as to whirl in close proximity to its inner wall. In the apparatus shown in Figs. 1 and 3, a plurality of cylindrical trough-like chambers 14 having end-walls 15 and 16, open mouths 17 preferably with lips 34, and bias weights 36, are pivotally supported between two endless chains 18 travelling around driven sprockets 32 and idler sprockets 31. During the upper run of the chambers 14, the weights 36 keep the mouths 17 uppermost. At the end of said upper run, a curved guide 37 swings the chambers ...

Heat exchange system for a slurry bubble column reactor

A METHOD OF SHUTTING DOWN AN OPERATING THREE-PHASE SLURRY BUBBLE COLUMN REACTOR

Slurry phase apparatus

Slurry phase apparatus

Slurry phase apparatus

Method and apparatus for separating low density particles from feed slurries

Pneumatic device of transport of a product in powder form.

Slurry phase apparatus

VERTEILERBODEN ZUR VERTEILUNG EINES MIT FEINEN FESTSTOFFPARTIKELN BELADENEN GASES

VERFAHREN ZUR HERSTELLUNG EINES TETRACHLORIERTEN PHTHALONITRIL

RADIAL MIXING APPARATUSES FOR BENT ROTATION REACTORS

PROCEDURE FOR THE GASEOUS PHASE POLYMERIZATION OF OLEFINEN

PROCEDURES FOR HEATING THE PET PELLET SUPPLY UP FOR A NACHPOLYMERISATIONSVERFAHREN BY HEAT EXCHANGE WITH HOISTING NACHPOLYMERISIERTEN PELLETS

PROCEDURE FOR THE PRODUCTION OF A OLEFINI PRODUCT

CATALYTIC REACTOR FOR THE DEHYDROGENATION FROM ETHYLBENZOL TO STYRENE

PROCEDURE AND DEVICE FOR THE POLYMERIZATION OF PROPYLENE

PROCEDURE FOR THE PRODUCTION OF A TETRACHLORIERTEN PHTHALONITRIL

MECHANISM FOR THE FLUIDIZATION OF GRANULAR PROPERTY

Device for the continuous pneumatic promotion of a powdered product

PROCEDURE AND DEVICE FOR THE POLYMERIZATION OF ETHYLS

PROCEDURE FOR THE PRODUCTION OF HYDROCARBONS

Device for sequential treating from flour-like to granular property with gas

Method and apparatus for treating high pressure particulate material

Method for controlling NOx emissions in the FCCU

Sealpot and method for controlling a solids flow rate therethrough

A sealpot (100) for a combustion power plant includes a downcomer standpipe (15) which receives solids of the combustion power plant, a bed (20) including a first end and a second opposite end, the first end connected to the downcomer standpipe, a discharge standpipe (30) disposed at the second opposite end of the bed, and an orifice plate (110) disposed between the bed and the discharge standpipe separating the discharge standpipe from the bed. The orifice plate includes apertures (210,220) disposed at a height above the bed which allow transport of fluidized solids and gas through the orifice plate.

Apparatus for the treatment of solids and/or gases

An apparatus for the treatment of solids and/or gases includes a fluidized-bed reactor (1) in which the solids are fluidized by means of fluidizing gas and are thermally and/or chemically treated, and a centrifugal separator (2) in which gas and solids are separated from each other, wherein the fluidized-bed reactor (1) is connected with the centrifugal separator (2) via a transfer duct (3). To avoid the formation of a streak extremely loaded with solids in the upper region of the centrifugal separator, the transfer duct (3) branches off from the fluidized-bed reactor (1) with a cross-section whose horizontal dimension is greater than the vertical dimension, wherein the cross-section of the transfer duct (3) expands downwards in vertical direction from the fluidized-bed reactor (1) to the centrifugal separator (2).

Silicon production with a fluidized bed reactor utilizing tetrachlorosilane to reduce wall deposition

A method of shutting down an operating three-phase slurry bubble column reactor

A method is provided of shutting down an operating three-phase slurry bubble column reactor (10) having downwardly directed gas distribution nozzles (30) submerged in a slurry body (19) of solid particulate material suspended in a suspension liquid contained inside a reactor vessel (12), with the gas distribution nozzles (30) being in flow communication with a gas feed line (26) through which gas is being fed to the gas distribution nozzles (30) by means of which the gas is injected downwardly into the slurry body (19). The method includes abruptly stopping flow of gas from the gas feed line (26) to the gas distribution nozzles (30) to trap gas in the gas distribution nozzles (30) thereby to inhibit slurry ingress upwardly into the gas distribution nozzles (30).

FLUIDIZED CATALYTIC CRACKING PROCESS

METHOD AND APPARATUS FOR TREATING HIGH PRESSURE PARTICULATE MATERIAL

A method and an apparatus for conveying particulate material of a reactor pneumatically from a high pressure delivery vessel (10) to a receiving vessel (40) at a lower pressure using gas discharging from the reactor as a carrier gas, by using an apparatus comprising a conveyor line (20) and a collecting vessel (30), which collecting vessel comprises means (50) to discharge carrier gas and means (54) to control the flow rate of the carrier gas, in which the pressure in the collecting vessel is controlled in such a way that the material has almost the same pressure as the delivery vessel when conveyed to the collecting vessel, from which it is transferred to the receiving vessel essentially at the same pressure as the receiving vessel.

APPARATUS FOR THE TREATMENT OF SOLIDS AND/OR GASES

An apparatus for the treatment of solids and/or gases includes a fluidized-bed reactor (1) in which the solids are fluidized by means of fluidizing gas and are thermally and/or chemically treated, and a centrifugal separator (2) in which gas and solids are separated from each other, wherein the fluidized-bed reactor (1) is connected with the centrifugal separator (2) via a transfer duct (3). To avoid the formation of a streak extremely loaded with solids in the upper region of the centrifugal separator, the transfer duct (3) branches off from the fluidized-bed reactor (1) with a cross-section whose horizontal dimension is greater than the vertical dimension, wherein the cross-section of the transfer duct (3) expands downwards in vertical direction from the fluidized-bed reactor (1) to the centrifugal separator (2).

APPARATUS FOR THE TREATMENT OF SOLIDS AND/OR GASES

An apparatus for the treatment of solids and/or gases includes a fluidized-bed reactor (1) in which the solids are fluidized by means of fluidizing gas and are thermally and/or chemically treated, and a centrifugal separator (2) in which gas and solids are separated from each other, wherein the fluidized-bed reactor (1) is connected with the centrifugal separator (2) via a transfer duct (3). To avoid the formation of a streak extremely loaded with solids in the upper region of the centrifugal separator, the transfer duct (3) branches off from the fluidized-bed reactor (1) with a cross-section whose horizontal dimension is greater than the vertical dimension, wherein the cross-section of the transfer duct (3) expands downwards in vertical direction from the fluidized-bed reactor (1) to the centrifugal separator (2).

CONTINUOUS PROCESS FOR CONVERTING NATURAL GAS TO LIQUID HYDROCARBONS

A method comprising: providing a first halogen stream; providing a first alkane stream; reacting at least a portion of the first halogen stream with at least a portion of the first alkane stream in a first reaction vessel to form a first halogenated stream; providing a second alkane stream comprising C2 and higher hydrocarbons; providing a second halogen stream; and reacting at least a portion of the second halogen stream with at least a portion of the second alkane stream in a second reaction vessel to form a second halogenated stream.

MACHINE FOR PROCESSING A WEB MATERIAL

A machine is disclosed which includes a feeding group, a first rotative cutting and/or creasing group, a second rotative cutting and/or creasing group and a rotative stripping group. The drive of the rotative tools and of a feeding cylinder is obtained from a DC motor acting on a driving pinion of the first group. The driving pinion engages with a toothed wheel of a lower rotative tool of the first group, transmitting its movement to the feeding cylinder with a wide pinion, a gear-train and a differential. The rotation is communicated to the second group and to the rotative stripping group by an intermediary wheel mounted on an angular phasing device engaging with a driving pinion coupled with the wheel of the lower rotative tool of the second group. A wide pinion connected with a braking member engages with a toothed wheel driving a train of chains and controlling the rotative stripping group. An angular phasing device allows the setting of the angular positioning of the stripping tools ...

DRAIN AND SAMPLING VALVE ASSEMBLY FOR A FLUIDIZED BED REACTOR

A PROCESS FOR REACTING OXYGEN CARRYING REGENERATED CATALYST PRIOR TO USE IN A FLUIDIZED BED REACTOR

A process to react an oxygen containing regenerated catalyst stream prior to use in a fluidized bed reactor comprising providing a regenerated catalyst stream which comprises at least 0.001 wt% oxygen; reacting the regenerated catalyst stream with a fuel source thereby forming oxides and reducing the amount of oxygen in the regenerated catalyst stream to produce a usable regenerated catalyst stream; and injecting the usable regenerated catalyst stream into a hydrocarbon fluidized bed reactor is provided.

VACUUM POWERED ADDITION SYSTEM

An addition apparatus, a fluid catalytic cracking (FCC) system having an addition apparatus, and a method for adding material to an FCC unit are provided. In one embodiment, an addition system for an FCC unit includes a container, a first eductor and a sensor. The eductor is coupled to an outlet of the container. The sensor is configured to detect a metric of material dispensed from the container through the eductor. A valve is provided for controlling the flow through the eductor. A controller provides a control signal for regulating an operational state of the valve. In another embodiment, an FCC system having an addition system is provided. In yet another embodiment, a method for adding material to an FCC unit is provided.

VACUUM POWERED ADDITION SYSTEM

An addition apparatus, a fluid catalytic cracking (FCC) system having an addition apparatus, and a method for adding material to an FCC unit are prov ided. In one embodiment, an addition system for an FCC unit includes a conta iner, a first eductor and a sensor. The eductor is coupled to an outlet of t he container. The sensor is configured to detect a metric of material dispen sed from the container through the eductor. A valve is provided for controll ing the flow through the eductor. A controller provides a control signal for regulating an operational state of the valve. In another embodiment, an FCC system having an addition system is provided. In yet another embodiment, a method for adding material to an FCC unit is provided.

INTERGRATION OF RESIDUE HYDROCRACKING AND SOLVENT DEASPHALTING

A process for upgrading residuum hydrocarbons is disclosed. The process may include: contacting a residuum hydrocarbon fraction and hydrogen with a first hydroconversion catalyst in a first ebullated bed hydroconversion reactor system; recovering a first effluent from the first ebullated bed hydroconversion reactor system; solvent deasphalting a vacuum residuum fraction to produce a deasphalted oil fraction and an asphalt fraction; contacting the deasphalted oil fraction and hydrogen with a second hydroconversion catalyst in a second hydroconversion reactor system; recovering a second effluent from the second hydroconversion reactor system; and fractionating the first effluent from the first ebullated bed hydroconversion reactor system and the second effluent from the second hydroconversion reactor system to recover one or more hydrocarbon fractions and the vacuum residuum fraction in a common fractionation system.

RADIAL MIXING DEVICES FOR ROTATING INCLINED REACTORS

Disclosed in this specification is the design for an internal mixing devi ce which increases the plug flow like behaviour of the rotating inclined rea ctor.

UTILIZATION OF BAFFLES IN CHLORINATION ZONE FOR CONTINUOUS CATALYST REGENERATION

Catalyst regeneration vessels including a chlorination zone that includes an outer mixing chamber, an inner mixing chamber, and a catalyst bed. The outer mixing chamber can include a lower portion and an upper portion, the lower portion of the outer mixing chamber including at least one air nozzle that injects a drying air stream into the outer mixing chamber, at least one chlorine input nozzle that injects a chlorine input stream into the outer mixing chamber, and at least a first baffle. The chlorination zone can also contain a second baffle that directs the mixed drying air stream and chlorine input stream from the outer mixing chamber to the inner mixing chamber.

CARBOCATALYSTS FOR CHEMICAL TRANSFORMATIONS

The disclosure relates to catalytically active carbocatalysts, e.g., a graphene oxide or graphite oxide catalyst suitable for use in a variety of chemical transformations. In one embodiment, it relates to a method of catalyzing a chemical reaction of an organic molecule by reacting the organic molecule in the presence of a sufficient amount of graphene oxide or graphite oxide for a time and at a temperature sufficient to allow catalysis of a chemical reaction. According to other embodiments, the reaction may be an oxidation reaction, a hydration reaction, a dehydrogenation reaction, a condensation reaction, or a polymerization reaction. Some reactions may include auto-tandem reactions. The disclosure further provides reaction mixtures containing an organic molecule and graphene oxide or graphite oxide in an amount sufficient to catalyze a reaction of the organic molecule.

GASIFIER FLUIDIZATION

A method of producing synthesis gas by introducing a feed material to be gasified into a gasification apparatus comprising at least one fluidized component operable as a fluidized bed, wherein the gasification apparatus is configured to convert at least a portion of the feed material into a gasifier product gas comprising synthesis gas; and maintaining fluidization of the at least one fluidized component by introducing a fluidization gas thereto, wherein the fluidization gas comprises at least one component other than steam. A system for producing synthesis gas is also provided.

Perverbindungen enthaltende, als Wasch-, Reinigungs-, Bleich- und Spülmittel verwendbare Mischung.

Verfahren zur Durchführung von Reaktionen zwischen Gasen und Feststoffpartikeln und Vorrichtung zur Durchführung dieses Verfahrens.

Vorrichtung, um zwei oder mehr Phasen in innige Berührung miteinander zu bringen, und Verfahren zu ihrem Betrieb

Verfahren zur Behandlung von schüttfähigen festen Stoffen mit Gasen

Durchlaufvorrichtung zur kontinuierlichen Bearbeitung von Substanzen

Verfahren zur Herstellung von Pyromellithsäure.

Vorrichtung zum Stabilisieren von freischwebenden Wirbelschichten

Verfahren zum Überziehen fester Stoffe, insbesondere von Produkten zum Waschen, Reinigen usw., mit einer homogenen Deckschicht

Vorrichtung zum kontinuierlichen Durchführen von Reaktionen mit Feststoffen in einer Wirbelschicht

Process for preparing aromatics from methane

The present invention relates to a process for carrying out endothermic, heterogeneously catalyzed reactions in which the reaction of the starting materials is carried out in the presence of a mixture of inert heat transfer particles and catalyst particles, where the catalyst particles are regenerated in a nonoxidative atmosphere at regular intervals and the heat of reaction required is introduced by separating off the inert heat transfer particles, heating the heat transfer particles in a heating zone and recirculating the heated heat transfer particles to the reaction zone. The process of the invention is particularly suitable for the nonoxidative dehydroaromatization of C 1 -C 4 -aliphatics in the presence of zeolite-comprising catalysts.

Methods and Apparatus for Enhanced Gas Distribution

Methods and apparatus for introducing a gas into the reaction zone of a reactor. Such methods and apparatus can more evenly distribute the gas throughout the reaction zone. Spargers for introducing a gas into the reaction zone of a reactor can be employed in systems and methods for carrying out the liquid-phase oxidation of an oxidizable compound, such as para-xylene.

Titanium bearing material flow control in the manufacture of titanium tetrachloride with silica content monitoring of the titanium product

This disclosure relates to a process for controlling chlorination reactions in manufacturing titanium tetrachloride in a fluidized bed reactor, followed by processing to form a titanium product comprising an amount of silica, the process comprising: (a) feeding carbonaceous material, titanium bearing material comprising an amount of silica, and chlorine to the fluidized bed reactor to form a gaseous stream, and condensing the gaseous stream to form titanium tetrachloride, a non-condensed gas stream and a condensable product stream; (b) processing the titanium tetrachloride to form a titanium product comprising an amount of silica; (c) analyzing the titanium product comprising an amount of silica to determine the analyzed concentration of silica; (d) identifying a set point concentration of silica; (e) calculating the difference between the analyzed concentration of silica and the set point concentration of silica; and (f) generating a signal which corresponds to the difference calculated in step (e) which provides a feedback response that controls the flow of the titanium bearing material into the fluidized bed reactor.

Apparatus for producing trichlorosilane and method for producing trichlorosilane

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

Mixing calciner

An object of this invention is to provide a mixing calciner that can separate and recover CO 2 gas in a high concentration, which is generated when a to-be-calcined cement material is mixed with a superheated calcined portion and calcined, by employing a fluidized-bed type or a spouted-bed type. The invention provides a mixing calciner ( 12 ) which mixes the calcined cement material with the superheated calcined portion to cause a calcination reaction, wherein the mixing calciner is the fluidized-bed type or the spouted-bed type, and is provided with a plurality of feed lines ( 25 ) for feeding the to-be-calcined cement material. In addition, this invention provides a mixing calciner which easily fluidizes or spouts a cement material even when a heat medium has a particle diameter larger than that of the cement material, and can separate and recover CO 2 gas generated in a cement-manufacturing facility in a high concentration.

Biomass and waste plastics depolymerization machine and methods via supercritical water

A method for transforming a selected polymeric material into a plurality of reaction products via supercritical water is disclosed. The method comprises: conveying the selected polymeric material through an extruder, wherein the extruder is configured to continuously convey the selected polymeric material to a supercritical fluid reaction zone; injecting hot compressed water into the supercritical fluid reaction zone, while the extruder is conveying the selected polymeric material into the supercritical fluid reaction zone so as to yield a mixture; retaining the mixture within the reaction zone for a period of time sufficient to yield the plurality of reaction products. The reaction zone may be characterized by a tubular reactor having an adjustably positionable inner tubular spear, wherein the tubular reactor and the inner tubular spear further define an annular space within the reaction zone, and wherein the mixture flows through the annular space and into a reaction products chamber.

Production of polycrystalline silicon in substantially closed-loop processes that involve disproportionation operations

Production of polycrystalline silicon in substantially closed-loop processes and systems is disclosed. The processes and systems generally involve disproportionation of trichlorosilane to produce silane or dichlorosilane and thermal decomposition of silane or dichlorosilane to produce polycrystalline silicon.

Dispersed Bubble Reactor For Enhanced Gas-Liquid-Solids Contact And Mass Transfer

An apparatus to promote gas-liquid contact and facilitate enhanced mass transfer. The dispersed bubble reactor (DBR) operates in the dispersed bubble flow regime to selectively absorb gas phase constituents into the liquid phase. The dispersion is achieved by shearing the large inlet gas bubbles into fine bubbles with circulating liquid and additional pumped liquid solvent when necessary. The DBR is capable of handling precipitates that may form during absorption or fine catalysts that may be necessary to promote liquid phase reactions. The DBR can be configured with multistage counter current flow sections by inserting concentric cylindrical sections into the riser to facilitate annular flow. While the DBR can absorb CO 2 in liquid solvents that may lead to precipitates at high loadings, it is equally capable of handling many different types of chemical processes involving solids (precipitates/catalysts) along with gas and liquid phases.

Apparatus for venting a catalyst cooler

The apparatus herein provide a catalyst cooler with a vent that communicates fluidizing gas to a lower chamber of a regenerator. Air that is used as fluidizing gas can then be consumed in the regenerator without promoting after burn in the upper chamber.

Apparatus and method for hydroconversion

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

Solids processing valve

A dome valve selectively dispenses a silicon product from a chamber of a vessel. The dome valve comprises a valve body defining a pass-through channel in communication with the chamber of the vessel to allow the silicon product to exit the vessel. The dome valve also comprising a valve seat defining an opening through which the silicon product enters the pass-through channel. The dome valve further comprising a domed body having a semi-hemispherical configuration. The domed body has a sealing surface. The domed body is rotatable between a closed position and an open position for allowing the selective dispensing of the silicon product from the vessel.

Process for increasing the efficiency of heat removal from a fischer-tropsch slurry reactor

The present invention is directed to a cooling system for removing heat from a Fischer-Tropsch (F-T) slurry reactor. The cooling system including a downcomer disposed within the F-T reactor to deliver a coolant downward through the F-T reactor at a predetermined velocity. The downcomer and the pressure of the introduced coolant cooperate to increase the coolant velocity, thereby maintaining the coolant in the substantially liquid phase in the downcomer. The cooling system further includes a plenum connected to the downcomer, wherein the coolant remains in the substantially liquid phase. Additionally, the cooling system includes at least one riser extending upward from the plenum, wherein a portion of the coolant vaporizes to provide a boiling heat transfer surface on the at least one riser.

Method Of Operating A Fluid Bed Reactor

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

CONTINUOUS PROCESS FOR CONVERTING NATURAL GAS TO LIQUID HYDROCARBONS

A method comprising: providing an alkyl halide stream; contacting at least some of the alkyl halides with a coupling catalyst to form a product stream comprising higher hydrocarbons and hydrogen halide; contacting the product stream with a solid reactant to remove at least a portion of the hydrogen halide from the product stream; and reacting the solid reactant with a source of oxygen to generate a corresponding halogen. 1. A system comprising:a coupling reactor comprising a coupling catalyst for receiving an alkyl halide stream and contacting at least a portion of the alkyl halide stream with the coupling catalyst to form a product stream comprising higher hydrocarbons and hydrogen halide;a separator unit for separating at least some of the product stream from the hydrogen halide; andan oxidation reactor comprising an aqueous solution comprising a metal capable of forming multiple stable oxidation states for receiving a source of oxygen and at least a portion of the hydrogen halide from the separator unit and generating a corresponding halogen and water.2. The system of wherein the metal capable of forming multiple oxidation states in the oxidation reactor comprises at least one metal selected from the group consisting of: Cu claim 1 , Fe claim 1 , Sb claim 1 , Mn claim 1 , V claim 1 , As claim 1 , Ru claim 1 , and a combination thereof.3. The system of wherein the aqueous solution in the oxidation reactor has a pH less than about 7.0.4. The system of wherein the oxidation reactor is at a temperature from about 65° C. to about 300° C.5. The system of wherein the oxidation reactor is at a pressure from about 0.1 atm to about 40 atm.6. The system of wherein the oxidation reactor comprises at least one reactor type selected from the group consisting of: a continuous stirred tank reactor claim 1 , a plug flow reactor claim 1 , a packed column reactor claim 1 , a fixed bed reactor claim 1 , and a fluidized bed reactor.7. The system of further comprising a product ...

Systems for producing silane

Methods and systems for producing silane that use electrolysis to regenerate reactive components therein are disclosed. The methods and systems may be substantially closed-loop with respect to halogen, an alkali or alkaline earth metal and/or hydrogen.

POLYCRYSTAL SILICON MANUFACTURING APPARATUS

There is disclosed a polycrystal silicon manufacturing apparatus including a reaction pipe configured to provide a reaction space where seed silicon grows into polycrystal silicon, a flowing-gas supply unit configured to supply flowing gas to the seed silicon and the polycrystal silicon provided in the reaction pipe, a sensing unit configured to output level information based on the height of a fluidized bed which is changeable according to the growth of the polycrystal silicon, and a particle outlet configured to exhaust the polycrystal silicon formed in the reaction pipe outside, when the height of the fluidized bed corresponding to the level information is larger than an exhaustion start height of the fluidized bed corresponding to a start level. 1. A polycrystal silicon manufacturing apparatus comprising:a reaction pipe configured to provide a reaction space where seed silicon grows into polycrystal silicon;a flowing-gas supply unit configured to supply flowing gas to the seed silicon and the polycrystal silicon provided in the reaction pipe;a sensing unit configured to output level information based on the height of a fluidized bed which is changeable according to the growth of the polycrystal silicon; anda particle outlet configured to exhaust the polycrystal silicon formed in the reaction pipe outside, when the height of the fluidized bed corresponding to the level information is larger than an exhaustion start height of the fluidized bed corresponding to an exhaustion start level.2. The polycrystal silicon manufacturing apparatus according to claim 1 , wherein the sensing unit comprises a distance sensor configured to sense a distance to the fluidized bed claim 1 , which is changeable according to the growth of the polycrystal silicon claim 1 , as the level information claim 1 , andthe particle outlet is configured to exhaust the polycrystal silicon formed in the reaction pipe, when the distance between the distance sensor and the fluidized bed is an ...

FLUIDIZED BED REACTOR SYSTEM

A fluidized-bed reactor system with at least two fluidized-bed reactors, each being a circulating fluidized bed, a particle line with a particle separator for transferring fluidized-bed particles from the first to the second reactor, and a particle line exiting at the lower half of the second reactor for transferring fluidized-bed particles back to the first reactor, wherein, at least in the second reactor, two or more reaction zones separated by one or more flow controllers and that the particle line opens into the second reactor above at least one flow controller. 1. A fluidized-bed reactor system , comprising:a first fluidized-bed reactor;a second fluidized-bed reactor;a particle line comprising a particle separator configured to transfer fluidized-bed particles from the first to the second reactor; anda particle line exiting at a lower half of the second reactor, configured to transfer fluidized-bed particles back to the first reactor,wherein the first and the second fluidized-bed reactors each comprise a circulating fluidized bed,wherein at least the second fluidized-bed reactor comprises two or more reaction zones separated by one or more flow controllers, andwherein the particle line opens into the second fluidized-bed reactor above at least one flow controller.2. The system of claim 1 , wherein the one or more flow controllers provided are (i) constrictions of a reactor cross-section claim 1 , (ii) diversions of a particle flow or (iii) constrictions of the reactor cross-section claim 1 , and diversions of particle flow claim 1 ,3. The system of claim 1 , wherein the particle line opens into the second fluidized-bed reaction above an uppermost flow controller in the second reactor.4. The system of claim 1 , wherein the second fluidized-bed reactor comprises a particle feedback line with a particle separator claim 1 , which opens into the second fluidized-bed reactor below at least one flow controller in the second fluidized-bed reactor.5. The system of claim ...

Process and apparatus for mixing two streams of catalyst

A process and apparatus for mixing streams of regenerated and carbonized catalyst involves passing a catalyst stream into and out of a chamber in a lower section of a riser. The chamber fosters mixing of the catalyst streams to reduce their temperature differential before contacting hydrocarbon feed.

Method, system and apparatus for controlling particle size in a fluidized bed reactor

A method, system, and apparatus for controlling the average particle size and the particle size distribution during a fluidized bed process in a fluidized bed reactor. More particularly, this disclosure relates to a method, system, and apparatus for controlling the average silicon particle size and the silicon particle size distribution during the production of high purity silicon.

Fluid Bed Reactor with Staged Baffles

The invention relates to a process of alkylating aromatic hydrocarbons, and more particularly a process of making paraxylene by alkylation of benzene and/or toluene with methanol and/or dimethyl ether, and to an apparatus for carrying out said process, the improvement comprising staged injection of one of the reactants, with the stages separated by structured packing so as to minimize at least one of gas phase back-mixing, by-pass phenomena, and gas bubble size.

TOROIDAL BED REACTOR

The present invention provides an apparatus for the processing of a particulate material, the apparatus comprising: 1. An apparatus for the processing of a particulate material , the apparatus comprising:a processing chamber having one or more inlets for admitting particulate material to be processed and one or more outlets for processed particulate material;the processing chamber comprising an annular treatment zone and a plurality of processing fluid inlets arranged in a base of said annular treatment zone and configured so that, in use, jets of processing fluid pass into the annular treatment zone through the plurality of processing fluid inlets to establish a spiral flow of particulate material in the annular processing zone;wherein said one or more outlets for processed particulate material are located in the base of said annular treatment zone and surrounded by said plurality of processing fluid inlets so that the spiral flow of particulate material circulates around said one or more outlets;the processing chamber further comprising a deflector for deflecting a portion of the spiral flow of particulate material in the annular processing zone radially inwards from said spiral flow so that said particulate material leaves the processing chamber through said one or more outlets for processed particulate material.2. An apparatus according to claim 1 , wherein the apparatus further comprises a cap arranged over said one or more outlets for processed particulate material to prevent particulate material leaving the chamber via said outlet without having been deflected by said deflector for deflecting a portion of the spiral flow of particulate material.3. An apparatus according to claim 1 , wherein said deflector for deflecting is adjustable between a first condition whereby claim 1 , in use claim 1 , it deflects a portion of the spiral flow of particulate material in the annular processing zone radially inwards from said spiral flow claim 1 , and a second condition ...

Methods for reacting compounds

Shell and tube heat exchangers that include a baffle arrangement that improves the temperature profile and flow pattern throughout the exchanger and/or that are integral with a reaction vessel are disclosed. Methods for using the exchangers including methods that involve use of the exchanger and a reaction vessel to produce a reaction product gas containing trichlorosilane are also disclosed.

APPARATUS FOR THE REDUCTION OF GASOLINE BENZENE CONTENT BY ALKYLATION WITH DILUTE ETHYLENE

The apparatus converts ethylene in a dilute ethylene stream and dilute benzene in an aromatic containing stream via alkylation to heavier hydrocarbons. The catalyst may be a zeolite such as UZM-8. The catalyst is resistant to feed impurities such as hydrogen sulfide, carbon oxides, and hydrogen and selectively converts benzene. At least 40 wt-% of the ethylene in the dilute ethylene stream and at least 20 wt-% of the benzene in the dilute benzene stream can be converted to heavier hydrocarbons. 1. An apparatus for alkylating benzene with ethylene comprising:a fluid catalytic cracking reactor for contacting cracking catalyst with a hydrocarbon feed stream to crack the hydrocarbon feed to cracked products having lower molecular weight and deposit coke on the cracking catalyst to provide coked cracking catalyst;a regenerator for combusting coke from said coked cracking catalyst by contact with oxygen;{'sub': 3', '2, 'a separator in communication with said fluid catalytic cracking reactor for separating Chydrocarbons from Chydrocarbons to provide a dilute ethylene stream;'}a reforming reactor for contacting a naphtha stream with reforming catalyst to produce a reformate stream; andan alkylation reactor in communication with said separator and said reforming reactor for alkylating benzene in said reformate stream with ethylene in said dilute ethylene stream over a fixed bed of alkylation catalyst to heavier alkyl benzene hydrocarbons, wherein no fractionation column is in communication between said separator and said alkylation reactor.2. The apparatus of wherein said separator is a secondary absorber and further comprising a primary absorber in communication with said secondary absorber for providing a secondary off-gas stream comprising said dilute ethylene stream and said alkylation reactor is in communication with said secondary absorber.3. The apparatus of wherein no fractionation column is in communication between said reforming reactor and said alkylation reactor. ...

Thermochemical Reactors and Processes for Hydrolysis of Cupric Chloride

A thermochemical reactor () and associated processes are disclosed. The reactor () and processes are used to conduct reactions relating to the hydrolysis of cupric chloride (CuCl2) within any one of the five-, four- and three-step Cu—Cl cycles. The reactor () comprises a reaction chamber () including a first zone () configured to conduct a spray operation and a second zone () configured to conduct a fluidized, fixed and/or moving bed operation. The first zone () includes a first inlet () configured to introduce a first reactant and an additional inlet () configured to introduce an additional reactant. A distributor () is configured to introduce the additional reactant to the second zone (). One or more product outlets () for communication with the reaction chamber () are provided. 1. A reactor for use in a thermochemical process , the reactor comprising: a first zone comprising at least one first inlet to introduce a first reactant and at least one additional inlet to introduce an additional reactant, the inlets being configured to conduct a spray operation in the first zone; and', 'a second zone in communication with the first zone;, 'a reaction chamber havinga distributor to introduce the additional reactant to the second zone; andat least one product outlet for communication with the reaction chamber.2. The reactor as defined in claim 1 , wherein the at least one first inlet has a first axis and the at least one additional inlet has an additional axis claim 1 , the first axis intersecting the additional axis within the first zone.3. The reactor as defined in claim 1 , wherein the at least one first inlet and the at least one additional inlet are substantially coaxial.4. The reactor as defined in claim 1 , comprising a third inlet configured to introduce the first reactant to the second zone of the reaction chamber.5. The reactor as defined in claim 1 , wherein the at least one product outlet includes a gas product outlet for communication with the first zone and ...

HYDROGEN CHROLIDE GAS EJECTING NOZZLE, REACTION APPARATUS FOR PRODUCING TRICHLOROSILANE AND METHOD FOR PRODUCING TRICHLOROSILANE

There is provided a hydrogen chrolide gas ejecting nozzle 1 used in a reaction apparatus for producing trichlorosilane in which metal silicon powder is reacted with hydrogen chloride gas to generate trichlorosilane. The member is provided with a shaft portion extending in the longitudinal direction and a head portion that is provided on an end of the shaft portion and extends in a direction intersecting the longitudinal direction of the shaft portion. A supply hole extending in the longitudinal direction is formed in the shaft portion, a plurality of ejection holes are formed in the head portion, and each of the ejection holes is communicatively connected to the supply hole and opened on the outer surface of the head portion toward a direction intersecting the direction to which the supply hole extends. 14-. (canceled)5. A method for producing trichlorosilane by reacting hydrogen chloride gas with metal silicon powder comprising the steps of:exhausting a produced trichlorosilane gas including an unreacted metal silicon powder from a trichlorosilane producing reactor;collecting the unreacted metal silicon powder by introducing the produced trichlorosilane gas including the unreacted silicon powder into a cyclone separator; andre-introducing the unreacted metal silicon powder collected by the cyclone separator into the trichlorosilane producing reactor.6. The method for producing trichlorosilane according to further comprising the step of feeding the unreacted metal silicon powder collected by the cyclone separator into a feed hopper that receives a fresh metal silicon powder supplied from a silicon powder supply system to obtain a mixed metal silicon powder claim 5 , which contains the unreacted metal silicon powder collected by the cyclone separator and the fresh metal silicon powder.7. The method for producing trichlorosilane according to further comprising the steps of:mixing the mixed metal silicon powder with a carrier gas to produce a mixture; andsupplying the ...

Installation and method for conversion of paper residue into a mineral product

A method and apparatus for conversion of paper residue into a mineral product uses a fluidized bed device with a distribution plate for securing an even distribution and supply of at least combustion air to the bed material and to the paper residue. An air box below the distribution plate supplies combustion air to the bed material and paper residue above the distribution plate. A heat exchanging section receives in separate parts ambient air and flue gases from the fluidized bed device for exchanging heat between flue gases and ambient air. The heat exchanging section is connected to the air box for supplying the heated ambient air to the air box for use as combustion air. A control system is employed for controlling the amount of bed material and the dimension of its particles and is arranged to monitor and maintain a process parameter within a predefined range.

PROTECTED FISCHER-TROPSCH CATALYST AND METHOD OF PROVIDING SAME TO A FISCHER-TROPSCH PROCESS

A method of preparing a spray dried catalyst by combining spray dried catalyst particles with wax so the spray dried catalyst particles are coated with wax, yielding wax coated catalyst particles, and shaping the wax coated catalyst to provide shaped wax coated catalyst. A method of activating Fischer-Tropsch catalyst particles containing oxides by contacting the catalyst particles with a reducing gas in an activation vessel to produce an activated catalyst, wherein contacting is performed in the absence of a liquid medium under activation conditions. A system for activating a Fischer-Tropsch catalyst containing an activation reactor configured to introduce an activation gas to a fixed or fluidized bed of the Fischer-Tropsch catalyst in the absence of a liquid medium and at least one separation device configured to separate a gas stream comprising entrained catalyst fines having an average particle size below a desired cutoff size from the activation reactor. 1. A method of preparing a spray dried catalyst , the method comprising:combining spray dried catalyst particles with wax such that the spray dried catalyst particles are coated with wax, yielding wax coated catalyst particles; andshaping the wax coated catalyst to provide shaped wax coated catalyst.2. The method of wherein the spray dried catalyst is a Fischer-Tropsch catalyst.3. The method of wherein the spray dried catalyst is a precipitated iron-based catalyst.4. The method of further comprising fluidizing the spray dried catalyst particles claim 1 , to provide a fluidized bed.5. The method of wherein fluidizing comprises introducing an inert gas into a vessel containing the spray dried catalyst particles.6. The method of wherein the vessel is a fixed bed or fluidized bed reactor.7. The method of further comprising activating the catalyst.8. The method of wherein activating comprises contacting the catalyst particles with an activation gas at an activation temperature.9. The method of wherein the activation ...

SYSTEM AND PROCESS FOR MELAMINE PRODUCTION BY GAS-PHASE QUENCHING METHOD OF ENERGY EFFICIENT AND COST SAVING TYPE

A system and process for melamine production by gas-phase quenching method and its process are provided. The said system includes a urea scrubber, after which a fluidized bed reactor, a hot-air cooler, a hot-air filter, a crystallizer and a melamine collector are installed in series successively, where the said melamine collector is connected to the said urea scrubber and the said fluidized bed reactor is connected to a carrier gas pre-heater which is connected to a carrier gas compressor; the said system further includes a gas-liquid separator which is connected to the said urea scrubber which is connected to a crystallizer; wherein a cool air blower is provided between the said gas-liquid separator and the crystallizer. The production system of the invention has the advantages of high productivity, stable operation, low energy consumption, low investment and high economic value of tail gas. 1. A system for melamine production by gas-phase quenching method , including:A urea scrubber, after which a fluidized bed reactor, a hot gas cooler, a hot gas filter, a crystallizer and a melamine collector are installed in series successively, where the said melamine collector is connected to the said urea scrubber;The said fluidized bed reactor is connected to a carrier gas pre-heater which is connected to a carrier gas compressor;The said system for melamine production further comprises a gas-liquid separator connected to the said urea scrubber that is connected to the said crystallizer, The said carrier gas compressor is connected to the said gas-liquid separator;wherein a cold gas blower is provided between the said gas-liquid separator and the said crystallizer.2. A system for melamine production according to claim 1 , wherein a cold gas cooler is provided between the said cold gas blower and the said crystallizer.3. A system for melamine production according to claim 1 , wherein the said carrier gas compressor is connected with the said gas-liquid separator via the said ...

Process and apparatus for distributing hydrocarbon feed and catalyst

A process and apparatus for fluid catalytic cracking feeds catalyst to a chamber of a riser. The catalyst exits the chamber and passes through a plenum and into a reaction zone through a plurality of tubes which distribute the catalyst uniformly over a cross section of the reaction zone of the riser. A hydrocarbon feed is fed to the plenum. The hydrocarbon feed passes from the plenum into the reaction zone through a plate comprising a multiplicity of openings which distribute the hydrocarbon feed uniformly over a cross section of the reaction zone of the riser. The feed is contacted with the catalyst in a reaction zone of the riser.

Process and apparatus for distributing hydrocarbon feed to a catalyst stream

A process and apparatus described is for distributing hydrocarbon feed to catalyst in a riser. Hydrocarbon feed is delivered to a plenum in the riser. Nozzles from the plenum inject feed into the riser to contact the catalyst. Streams of regenerated catalyst and carbonized catalyst may be passed to the riser and mixed around an insert in a lower section of a riser. The plenum may be located in the riser.

HIGH THROUGHPUT REACTOR ASSEMBLY FOR POLYMERIZATION OF OLEFINS

Reactor assembly for the production of polymers including a fluidized bed reactor () comprising a bottom zone (), a middle zone () and an upper zone (), an inlet () for the fluidization gas located in the bottom zone (), an outlet () for the fluidization gas located in the upper zone (); the outlet () for the fluidization gas being coupled with the fluidized bed reactor () via inlet () via a gas circulation line; means for separation of solids from gas () being connected to said gas circulation line; the equivalent cross-sectional diameter of the upper zone () being monotonically decreasing with respect to the flow direction of the fluidization gas through the fluidized bed reactor; the middle zone () having an essentially constant equivalent cross-sectional diameter with respect to the flow direction of the fluidization gas through the fluidized bed reactor; the equivalent cross-sectional diameter of the bottom zone () being monotonically increasing with respect to the flow direction of the fluidization gas through the fluidized bed reactor; characterized in that the ratio of the height of the fluidized bed reactor to the equivalent cross-sectional diameter of the middle zone of the fluidized bed reactor is from 2 to 10; and whereby said upper zone () is directly connected to said middle zone (). 119-. (canceled)2015678597. Reactor assembly for the production of polymers including a fluidized bed reactor () comprising a bottom zone () , a middle zone () and an upper zone () , an inlet () for the fluidization gas located in the bottom zone () , an outlet () for the fluidization gas located in the upper zone ();{'b': 9', '1', '8, 'the outlet () for the fluidization gas being coupled with the fluidized bed reactor () via inlet () via a gas circulation line;'}{'b': '2', 'means for separation of solids from gas () being connected to said gas circulation line;'}{'b': '7', 'the equivalent cross-sectional diameter of the upper zone () being monotonically decreasing with ...

Internal cyclone for fluidized bed reactor

A fluidized bed reactor comprising a reaction column having a fluid portion; a gas inflow means for flowing a gas upwardly from the fluid portion of the reaction column; a particle feed means for feeding particles to the fluid portion of the reaction column; a cyclone capable of separating particles from the gas flowing upwardly from the fluid portion of the reaction column, the cyclone being located within the reaction column and being in communication with the gas flowing upwardly, wherein the cyclone comprises a cyclone body having an inlet, a gas outlet, and a particle drop port; and a particle discharge pipe having an upper part connected to the particle drop port of the cyclone body, and a lower part, wherein the particle discharge pipe is located substantially outside of the reaction column.

DECARBONATION PROCESS

A process for decarbonation of particles of raw meal, to be burnt in a clinkering kiln at a cement plant, the process includes: a) decarbonation of particles of raw meal, in a fluidised bed heat exchanger, the particles being suspended in a rising carrier gas including carbon dioxide, the fluidised bed heat exchanger having a solid heat carrier circulating counter-current relative to the carrier gas, to provide an effluent gas including carbon dioxide and decarbonated raw meal; b) separating the effluent gas and the decarbonated raw meal c) separating the effluent gas into a first and second part; cooling the first part of the effluent gas and recycling to provide carrier gas, d) isolating the second part of effluent gas e) recovering and re-heating the heat carrier and recirculating to step (a). 1. A process for decarbonation of particles of raw meal , to be burnt in a clinkering kiln at a cement plant , which particles having a particle size distribution such that the retention of the particles on a 200 μm sieve is less than 2% by mass and the retention of the particles on a 90 μm sieve is less than 20% by mass , said process comprising:a) decarbonation of particles of raw meal, in a fluidised bed heat exchanger, said particles being suspended in a rising carrier gas comprising carbon dioxide, said fluidised bed heat exchanger having a solid heat carrier circulating counter-current relative to the carrier gas, to provide an effluent gas comprising carbon dioxide and decarbonated raw meal;b) separating said effluent gas and the decarbonated raw mealc) separating the effluent gas into a first and second part; cooling said first part of the effluent gas and recycling to provide carrier gas,d) isolating said second part of effluent gase) recovering and re heating said heat carrier and recirculating to (a).2. The process according to claim 1 , wherein the solid heat carrier comprises particles having an average diameter of 300 to 600 μm.3. The process according to ...

Flexible reactor assembly for polymerization of olefins

The invention relates to a reactor assembly for the production of polymers including a fluidized bed reactor ( 1 ) comprising a bottom zone ( 5 ), a middle zone ( 6 ) and an upper zone ( 7 ), an inlet ( 8 ) for the fluidization gas located in the bottom zone ( 5 ), an outlet ( 9 ) for the fluidization gas located in the upper zone ( 7 ); the outlet ( 9 ) for the fluidization gas being coupled with the fluidized bed reactor ( 1 ) via inlet ( 8 ); the equivalent cross-sectional diameter of the bottom zone ( 5 ) being monotonically increasing with respect to the flow direction of the fluidization gas through the fluidized bed reactor; the middle zone ( 6 ) having an essentially constant equivalent cross-sectional diameter with respect to the flow direction of the fluidization gas through the fluidized bed reactor; the equivalent cross-sectional diameter of the upper zone ( 7 ) being monotonically decreasing with respect to the flow direction of the fluidization gas through the fluidized bed reactor; wherein that the ratio of the height of the fluidized bed reactor to the equivalent cross-sectional diameter of the middle zone of the fluidized bed reactor is from 2 to 10; and wherein there is an unobstructed passageway in the direction of flow of the fluidization gas through the fluidized bed reactor from the bottom zone ( 5 ) to the upper zone ( 7 ).

HEAT TREATING APPARATUS FOR POWDER PARTICLES AND METHOD OF PRODUCING TONER

A heat treating apparatus for powder particles including a cylindrical treating chamber; a powder particle-supplying unit; a hot air-supplying unit that supplies hot air for heat-treating powder particles; a cold air-supplying unit that supplies cold air for cooling the heat-treated powder particles; a regulating unit for regulating a flow of the supplied powder particles; and a recovering unit that recovers the heat-treated powder particles. The regulating unit is a substantially circular columnar member, the hot air-supplying unit has an outlet opposite to the upper end portion of the columnar member, and the regulating unit is equipped with a substantially conic distributing member for distributing the supplied hot air in a circumferential direction and a rotating member for rotating the distributed hot air in a spiral manner, on the center of the upper end portion. 1. A heat treating apparatus for powder particles each of which contains a binder resin and a colorant , the heat treating apparatus comprising:(1) a cylindrical treating chamber in which a heat treatment of the powder particles is performed,(2) a powder particle-supplying unit provided on an outer peripheral portion of the treating chamber, for supplying the powder particles to the treating chamber,(3) a hot air-supplying unit that supplies hot air for heat-treating the supplied powder particles to the treating chamber,(4) a cold air-supplying unit that supplies cold air for cooling the heat-treated powder particles to the treating chamber,(5) a regulating unit provided on the treating chamber, for regulating a flow of the supplied powder particles, and(6) a recovering unit provided at a lower end portion side of the treating chamber, that recovers the heat-treated powder particles, whereinthe regulating unit is a columnar member with a substantially circular cross-section and is arranged on a central axis of the treating chamber so as to be protruded from the lower end portion of the treating ...

Reduced sorbent utilization for circulating dry scrubbers

Circulating dry scrubbing (CDS) systems and methods utilizes a particle classification unit operation to separate unreacted sorbent (such as lime, limestone, or sodium-based sorbent) such that a reactive fraction of the cut stream may be selectively recovered to a flue gas scrubbing system. This reduces the amount of fresh sorbent that must be supplied for pollutant removal. 1. A circulating dry scrubber system comprising: a recycle stream connected to the reactor for reuse in the reactor, and', 'a purge stream; and, 'a recycle diverter configured and adapted to be connected to a circulating dry scrubber reactor to receive sorbent particles therefrom for separating particles into a coarse solids recovery stream connected to recover coarse solids from the classifier and divert them into the reactor, and', 'a waste stream for disposal of fine particles from the classifier., 'a classifier operatively connected to receive particles from the purge stream, wherein the classifier is configured to separate particles from the purge stream into2. A system as recited in claim 1 , further comprising a comminutor selectively connected to receive coarse reagent solids from the coarse solids recovery stream for comminution claim 1 , and to supply comminuted solids to the reactor.3. A system as recited in claim 1 , wherein the classifier is operatively connected to continuously receive particles from the purge stream and to continuously recycle coarse solids to the reactor.4. A system as recited in claim 1 , wherein the classifier is configured and adapted to divide up to about the coarsest 30 wt % of reagent particles from the purge stream into the coarse solids recovery stream.5. A system as recited in claim 1 , wherein the classifier is configured and adapted to divide particles greater than about 50 μm in diameter into the coarse solids recovery stream.6. A system as recited in claim 1 , wherein the classifier is configured and adapted to divide particles greater than about 70 ...

Generating cellulosic-renewable identification numbers in a refinery

The present application generally relates to methods of generating cellulosic-renewable identification numbers by thermally processing a cellulosic biomass to form a renewable fuel oil, and then co-processing the renewable fuel oil with a petroleum fraction in a refinery to form a cellulosic-renewable identification number-compliant fuel.

REACTION DEVICE FOR PREPARING LIGHT OLEFINS FROM METHANOL AND/OR DIMETHYL ETHER

A reaction device for preparing light olefins from methanol and/or dimethyl ether, and more specifically relates to a reaction device for preparing light olefins from methanol and/or dimethyl ether, which mainly comprises a dense phase fluidized bed reactor (), a cyclone separator (), a stripper (), a lift pipe (), a dense phase fluidized bed regenerator (), a cyclone separator (), a stripper (), and a lift pipe (), wherein the dense phase fluidized bed reactor () is separated into n (n≧2) secondary reaction zones by a material flow controller (), and the dense phase fluidized bed regenerator () is separated into m (m≧2) secondary regeneration zones by the material flow controller (). 1. A reaction device for preparing light olefins from methanol and/or dimethyl ether comprising a dense phase fluidized bed reactor , a cyclone separator , a stripper , a lift pipe , a dense phase fluidized bed regenerator , a cyclone separator , a stripper , and a lift pipe; wherein a feeding line for reactor is connected to the bottom of the dense phase fluidized bed reactor; a part of the stripper is in the dense phase fluidized bed reactor , and the remaining part thereof is below the dense phase fluidized bed reactor; the bottom of the lift pipe is connected to the bottom of the stripper , and the top of the lift pipe is connected to the dense phase fluidized bed regenerator; a feeding line for regenerator is connected to the bottom of the dense phase fluidized bed regenerator; a part of the stripper is in the dense phase fluidized bed regenerator , and the remaining part thereof is below the dense phase fluidized bed regenerator; the bottom of the lift pipe is connected to the bottom of the stripper , and the top of the lift pipe is connected to the dense phase fluidized bed reactor , wherein a material flow controller is provided in the dense phase fluidized bed reactor and/or the dense phase fluidized bed regenerator , and the dense phase fluidized bed reactor is separated into ...

Enclosure of an FCC Unit Comprising an Inner Support Device Rigidly Connected to Cyclones

The invention relates to an enclosure () of a fluid catalytic cracking unit in which an inner space is defined by a side wall () having a longitudinal axis extending substantially in the direction of gravity, said enclosure being provided with a plurality of mechanical separation cyclones () located inside the inner space. The enclosure () comprises a supporting device () attached only to the cyclones () by: an annular peripheral support element () extending along the side wall () in a plane perpendicular to the longitudinal axis (X), separated from the side wall by a predetermined clearance; and a plurality of beams () extending in the same plane as the peripheral support element (), the beams being rigidly connected to the peripheral support element and to at least one mechanical separation cyclone by one end or by an attachment part distant from the ends thereof. 116.-. (canceled)17. A chamber of a fluid catalytic cracking unit comprising a lateral wall which delimits an internal volume having a longitudinal axis extending substantially in the direction of gravity , said chamber being provided with a plurality of mechanical separation cyclones situated inside said internal volume , characterized in that said chamber comprises , inside said internal volume , a support device secured only to the mechanical separation cyclones and comprising:a peripheral support element extending along the lateral wall in a plane perpendicular to the longitudinal axis (X), distant from the lateral wall by a predetermined clearance in the plane of the support element,a plurality of beams extending in the same plane as the peripheral support element, the beams being secured to the peripheral support element and to at least one mechanical separation cyclone by an end or by a fixing part distant from its ends.18. The chamber as claimed in claim 17 , characterized in that the support device comprises other beams extending in the same plane as the peripheral support element and chosen ...

PROCESS FOR THE OLIGOMERIZATION OF ETHYLENE WITH STIRRED GAS/LIQUID REACTOR AND PLUG-FLOW REACTOR SEQUENCE

Reaction device which makes possible the oligomerization of olefins to give linear olefins and preferably linear α-olefins, comprising a gas/liquid reactor and a reactor of plug-flow type. The reaction device is also employed in an oligomerization process. 1. Device comprising:{'b': '1', 'a gas/liquid reactor (), of elongated shape along the vertical axis, comprising a liquid phase and a gas phase located above the said liquid phase,'}{'b': '3', 'a means for introduction of the olefin () into the gas/liquid reactor employing a means for injection of the olefin within the said liquid phase of the gas/liquid reactor,'}{'b': '14', 'a means for introduction of the catalytic system () into the gas/liquid reactor,'}{'b': 13', '1, 'a recirculation loop () comprising withdrawal means in the gas/liquid reactor for the withdrawal and the dispatch of a fraction of withdrawn liquid to a heat exchanger capable of cooling the said liquid fraction, and means for introduction of the said cooled liquid, exiting from the heat exchanger, into the upper part of the gas/liquid reactor (),'}{'b': '11', 'a reactor of plug-flow type () comprising withdrawal means in the gas/liquid reactor for the withdrawal and the dispatch of a fraction of withdrawn liquid to the reactor of plug-flow type and means for recovery of a reaction effluent, at the outlet of the reactor of plug-flow type.'}2. Device according to claim 1 , in which the reactor of plug-flow type is located outside the gas/liquid reactor.3. Device according to claim 1 , in which the reactor of plug-flow type comprises a heat exchanger.4. Olefin oligomerization process employing the device according to claim 1 , at a pressure between 1.0 and 10.0 MPa and at a temperature between 0° C. and 200° C. claim 1 , comprising the following stages:{'b': '1', 'a) a catalytic oligomerization system comprising at least one metal precursor and at least one activating agent is introduced into a gas/liquid reactor () comprising a liquid phase and a ...

Method and device for the heat treatment of granular solids

A method for the heat treatment of granular solids includes initially introducing solids into a first reactor configured as a flash reactor or fluidized bed reactor where they are brought into contact with hot gases at temperatures in the range 500° C. to 1500° C. Next, the solids are passed through a residence time reactor in which they are fluidized. The residence time reactor is configured in a manner such that it has various regions which are separated from one another, from which the solid can be withdrawn in a manner such that it is provided with a variety of residence times in the residence time reactor. 1. A method for the heat treatment of granular solids , wherein the solids are initially introduced into a first reactor configured as a flash reactor or fluidized bed reactor where they are brought into contact with hot gases at temperatures in the range 500° C. to 1500° C. , and wherein the solids are then guided through a residence time reactor in which they are fluidized , wherein the residence time reactor is configured in a manner such that it is provided with various mutually separated regions from which the solid is separately removed in a manner such that it has a residence time in the residence time reactor which is of a variable duration , wherein removal from the various regions of the residence time reactor is carried out in a manner such that not all of the regions are fluidized , wherein the fluidized regions are fluidically connected in succession , whereby specific downstream regions are no longer fluidized and therefore actively removed.2. The method as claimed in claim 1 , wherein solid is actively removed from at least one region.3. The method as claimed in claim 1 , wherein the fluidized bed reactor is provided with a circulating fluidized bed.4. The method as claimed claim 1 , wherein the air is used as the fluidizing gas in the residence time reactor.5. The method as claimed in claim 1 , wherein the residence time in the first reactor ...

CARBON NANOSTRUCTURE PREPARATION METHOD, CARBON NANOSTRUCTURE PREPARED BY MEANS OF SAME, AND COMPOSITE MATERIAL COMPRISING SAME

The present invention relates to a method for producing carbon nanostructures using a fluidized bed reactor. According to the method, some of the as-produced carbon nanostructures remain uncollected and are used as fluidic materials to improve the fluidity in the reactor. The method enables the production of carbon nanostructures in a continuous process. In addition, the fluidity of the catalyst and the fluidic materials in the reactor is optimized, making the production of carbon nanostructures efficient. 1. A method for producing carbon nanostructures , comprising allowing a catalyst and reactant gases comprising a carbon source to flow in a fluidized bed reactor to synthesize carbon nanostructures wherein some of the carbon nanostructures remain uncollected and are used as fluidic materials in the fluidized bed reactor and wherein the residual rate of the fluidic materials is from 0.4 to 0.7 , as calculated by Equation 1:{'br': None, 'Residual rate of carbon nanostructures=Volume of remaining carbon nanostructures/(Volume of initially remaining carbon nanostructures+Volume of as-produced carbon nanostructures)\u2003\u2003[Equation 1]'}2. The method according to claim 1 , wherein the residual rate of carbon nanostructures is determined from the difference in pressure between the bottom and top of the reactor.3. The method according to claim 1 , wherein the residual rate y and the conversion x of the carbon source satisfy the relation given by Equation 2:{'br': None, 'i': 'y=px+q', '[Equation 2]'}where p is a constant from 0.4 to 0.7 and q is a constant from 15 to 30.4. The method according to claim 1 , wherein the amount of the catalyst supplied to the reactor satisfies the relation given by Equation 3:{'br': None, 'i': b', 'a+b, 'Catalyst supply rate=/()≦0.1\u2003\u2003[Equation 3]'}where a is the weight (g) of the carbon nanostructures remaining in the fluidized bed reactor and b is the weight (g) of the catalyst supplied.5. The method according to claim 1 , ...

FLUIDIZED BED MEMBRANE REACTOR

Herein disclosed is a dry reforming reactor comprising a gas inlet near the bottom of the reactor; a gas outlet near the top of the reactor; a fluidized bed comprising a catalyst; and one or more hydrogen membranes comprising palladium (Pd). In some cases, the one or more hydrogen membranes comprises Pd alloy membranes, or Pd supported on ceramics or metals. In some cases, the one or more hydrogen membranes are placed vertically in the reactor as hydrogen membrane tubes hanging from the top of the reactor. In some cases, the hydrogen membranes are configured to selectively collect hydrogen from the tubes via one or more internal manifolds and sent to an external hydrogen collection system. 1. A dry reforming reactor comprisinga gas inlet near the bottom of the reactor;a gas outlet near the top of the reactor;a fluidized bed comprising a catalyst; andone or more hydrogen membranes comprising palladium (Pd).2. The reactor of wherein said one or more hydrogen membranes comprises Pd alloy membranes claim 1 , or Pd alloys supported on ceramic or metal substrates.3. The reactor of wherein said one or more hydrogen membranes are placed vertically in the reactor as hydrogen membrane tubes hanging from the top of the reactor.4. The reactor of wherein the hydrogen membranes are configured to selectively collect hydrogen from the tubes via one or more internal manifolds and sent to an external hydrogen collection system.5. The reactor of wherein the gas inlet is configured to allow one or more feed streams to enter the reactor via a manifold or distributor.6. The reactor of wherein the catalyst comprises nickel and alumina.7. The reactor of wherein the reactor is configured to allow reformed gas to exit the top of the reactor and separate from spent catalyst.8. The reactor of wherein no steam or oxygen injection is needed.9. The reactor of is operated at a temperature range of 600-700° C. and a pressure range of 700-800 kPa.10. A method of producing dimethyl ether (DME) ...

FLUIDIZED BED MEMBRANE REACTOR

Herein disclosed is a dry reforming reactor comprising a gas inlet near the bottom of the reactor; a gas outlet near the top of the reactor; a fluidized bed comprising a catalyst; and one or more hydrogen membranes comprising palladium (Pd). In some cases, the one or more hydrogen membranes comprises Pd alloy membranes, or Pd supported on ceramics or metals. In some cases, the one or more hydrogen membranes are placed vertically in the reactor as hydrogen membrane tubes hanging from the top of the reactor. In some cases, the hydrogen membranes are configured to selectively collect hydrogen from the tubes via one or more internal manifolds and sent to an external hydrogen collection system. 1. A dry reforming reactor comprisinga gas inlet near the bottom of the reactor;a gas outlet near the top of the reactor;a fluidized bed comprising a catalyst; andone or more hydrogen membranes comprising palladium (Pd).2. The reactor of wherein said one or more hydrogen membranes comprises Pd alloy membranes claim 1 , or Pd alloys supported on ceramic or metal substrates.3. The reactor of wherein said one or more hydrogen membranes are placed vertically in the reactor as hydrogen membrane tubes hanging from the top of the reactor.4. The reactor of wherein the hydrogen membranes are configured to selectively collect hydrogen from the tubes via one or more internal manifolds and sent to an external hydrogen collection system.5. The reactor of wherein the gas inlet is configured to allow one or more feed streams to enter the reactor via a manifold or distributor.6. The reactor of wherein the catalyst comprises nickel and alumina.7. The reactor of wherein the reactor is configured to allow reformed gas to exit the top of the reactor and separate from spent catalyst.8. The reactor of configured to use no process water and no oxygen.9. The reactor of is operated at a temperature range of 600-700° C. and a pressure range of 700-800 kPa.10. The reactor of comprising one or more internal ...

PROCESSES AND SYSTEMS FOR USING SILICA PARTICLES IN FLUID BED REACTOR

The present disclosure relates to fluid bed processes that utilize silica particles as a fluidization aid. The process comprises reacting one or more reactants in a reactor comprising a fluid bed to form a product. The fluid bed comprises a catalyst composition comprising a catalyst and an inert additive composition comprising silica particles from 0.5 wt % to 30 wt %, based on the total weight of the catalyst composition. The silica particles are discrete, inert particles that are mixed with the catalyst in the fluid bed. 1. A process comprising:reacting one or more reactants in a reactor comprising a fluid bed to form a product;wherein the fluid bed comprises a catalyst composition comprising a catalyst and an inert additive composition comprising from 0.5 wt % to 30 wt % of silica particles, based on the total weight of the catalyst composition,wherein the silica particles have an equivalent median particle diameter ranging from 10 microns to 500 microns.2. The process of claim 1 , wherein the catalyst comprises one or more of antimony claim 1 , uranium claim 1 , iron claim 1 , bismuth claim 1 , vanadium claim 1 , molybdenum claim 1 , nickel claim 1 , potassium claim 1 , cobalt claim 1 , oxides thereof claim 1 , or salts thereof.3. The process of claim 1 , wherein the catalyst has an equivalent median diameter ranging from 1 microns to 125 microns.4. The process of claim 1 , wherein the silica particles have a real density ranging from 1.8 g/cmto 2.8 g/cm claim 1 , and wherein the difference between the density of the silica particles and the catalyst is less than 75%.5. The process of claim 1 , wherein the silica particles have a surface area less than 50 m/g claim 1 , and wherein the silica particles have a hardness ranging from 500 to 720 as measured by ASTM E384 (2018).6. The process of claim 1 , wherein the silica particles have a sphericity ranging from 60% to 99.9%7. The process of claim 1 , wherein the catalyst composition further comprises alumina ...

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 ...

FLUID CATALYTIC CRACKING PROCESSES AND APPARATUS

Apparatus and processes herein provide for converting hydrocarbon feeds to light olefins and other hydrocarbons. The processes and apparatus include a conventional riser reactor in combination with a mixed flow (e.g., including both counter-current and co-current catalyst flows) fluidized bed reactor designed for maximizing light olefins production. The effluents from the riser reactor and mixed flow reactor are processed in a catalyst disengagement vessel, and the catalysts used in each reactor may be regenerated in a common catalyst regeneration vessel. Further, integration of the two-reactor scheme with a catalyst cooler provides a refinery the flexibility of switching the operation between the two-reactor flow scheme, a catalyst cooler only flow scheme, or using both simultaneously. 1. A system for processing hydrocarbons , comprising:a riser reactor configured to contact a mixture of first particles and second particles with a hydrocarbon feedstock to convert at least a portion of the hydrocarbon feedstock and to recover a riser reactor effluent comprising mixed hydrocarbons and the mixture of the first and second particles, wherein the first particle has a smaller average particle size and/or is less dense than the second particle, and wherein the first particle and second particle may independently be catalytic or non-catalytic particles; an overhead product line for recovering from the reactor a reactor effluent comprising first particles, a first portion of the second particles, and hydrocarbons;', 'a bottoms product line for recovering from the reactor a second stream comprising a second portion of the second particles;, 'a reactor configured to contact a mixture comprising the first particles and the second particles with a second hydrocarbon feedstock to convert at least a portion of the second hydrocarbon feedstock, wherein the reactor is fluidly connected toa particle separator configured to separate second particles from the reactor effluent, and to ...

Fluidized catalytic cracking apparatus

The present application generally relates to a fluidized catalytic cracking apparatus having one or more ports for injecting a renewable fuel oil for co-processing the renewable fuel oil and a petroleum fraction.

Fluidized Bed Reactor Adapted For The Production Of Biphased Systems

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

METHOD AND SYSTEM FOR THE TREATMENT OF MATERIALS

A system for the treatment of materials, to be selected from between materials in a fluid state () and particles suspended in a fluid material (), comprising at least one upper kinematic pair equipped with two mechanical elements (), said kinematic pair being in contact with a material in a fluid state () or with particles suspended in a fluid material (); motor means () to generate a pre-set relative velocity (v) between the elements () of said kinematic pair, and tensioning means () to subject said kinematic pair to a pre-set pressure (P). 1. A system for the treatment of materials , selected from between materials in a fluid state and particles suspended in a fluid material , comprising:at least one upper kinematic pair equipped with two mechanical elements, said kinematic pair being in contact with a material in a fluid state or in contact with particles suspended in a fluid material;motor means to generate a pre-set relative velocity (v) between the mechanical elements of said kinematic pair; andtensioning means to subject said kinematic pair to a pre-set contact pressure (p); characterised in that the upper kinematic pair is formed by at least one bearing equipped with rolling elements arranged between a moving ring and a fixed ring.2. The treatment system according to claim 1 , characterised in that the bearing comprises a cage for separating the rolling elements.3. The treatment system according to claim 1 , characterised in that it comprises at least one upper kinematic pair formed by a gear claim 1 , a cam-follower mechanism claim 1 , a chain-sprocket mechanism claim 1 , a chain transmission claim 1 , a belt transmission claim 1 , a cable transmission claim 1 , a pin-on-disk tribometer claim 1 , or a ball-on-disk tribometer.4. The treatment system according to claim 1 , characterised in that the upper kinematic pairs are housed in a chamber hermetically closed by a cover.5. The treatment system according to claim 4 , characterised in that the closed ...

FLUID CATALYTIC CRACKING PROCESS AND APPARATUS FOR MAXIMIZING LIGHT OLEFINS OR MIDDLE DISTILLATES AND LIGHT OLEFINS

A fluid catalytic cracking apparatus and process is disclosed, providing for efficient conversion of heavy hydrocarbon feeds to light olefins, aromatics, and gasoline. A countercurrent flow reactor operating in bubbling or turbulent fluidization regimes is integrated with a fluid catalytic cracking riser reactor. A heavy hydrocarbon feed is catalytically cracked to naphtha and light olefins in the riser reactor, a co-current flow reactor. To enhance the yields and selectivity to light olefins, cracked hydrocarbon products from the riser reactor, such as Cand naphtha range hydrocarbons, may be recycled and processed in the countercurrent flow reactor. The integration of the countercurrent flow reactor with a conventional FCC riser reactor and catalyst regeneration system may overcome heat balance issues commonly associated with two-stage cracking processes, may substantially increase the overall conversion and light olefins yield, and/or may increases the capability to process heavier feedstocks. 117-. (canceled)18. An apparatus for the catalytic cracking of hydrocarbons , comprising:a catalyst regeneration vessel for regenerating a spent catalyst comprising a first cracking catalyst having a first average particle size and density and a second cracking catalyst having a second average particle size and density to form a regenerated catalyst comprising the first cracking catalyst and the second cracking catalyst, wherein the average particle size of the first cracking catalyst is less than the average particle size of the second cracking catalyst;a riser reactor for contacting in co-current flow a first hydrocarbon feed with a first portion of the regenerated catalyst to produce a first effluent comprising a first cracked hydrocarbon product and a spent mixed catalyst fraction;a flow conduit for feeding a second portion of the regenerated catalyst to a second cracking reactor; separate the first cracking catalyst from the second cracking catalyst based on at least ...

COMBUSTOR AIR BAG GRID FOR USE WITHIN A FLUIDIZED BED REACTOR, AND A FLUIDIZED BED REACTOR

A combustor air bar grid for use within a fluidized bed reactor includes at least two main air collector bars in fluid communication with a source of fluidizing gas, a plurality of primary air bars that are transversal to the main air collector bars and arranged on the at least two main air collector bars such that the main air collector bars support them, and in fluid communication to at least two of the main air collector bars. The main air collector bars and the primary air bars define ash removal openings in the air bar grid and a plurality of fluidized nozzles are arranged to each of the primary air bars for fluidizing the bed reactor. A fluidized bed reactor includes such a combustor air bar grid. 112.-. (canceled)13. A combustor air bar grid for use within a fluidized bed reactor , the combustor air bar grid comprising:at least two main air collector bars in fluid communication with a source of fluidizing gas;a plurality of primary air bars that are transverse to the main air collector bars and arranged on the at least two main air collector bars such that the main air collector bars support the plurality of primary air bars, the plurality of primary air bars being in fluid communication with at least two of the main air collector bars, and the main air collector bars and the primary air bars defining ash removal openings in the air bar grid;a plurality of fluidizing nozzles arranged to each of the primary air bars for fluidizing the bed reactor; anda number of ash hoppers arranged beneath the ash removal openings,wherein the main air collector bars are configured to form external air-cooled walls for the ash hoppers that are cooled with the pressurized fluidizing gas.14. The combustor air bar grid according to claim 13 , wherein the main air collector bars are in fluid communication with the primary air bars via fluidizing gas transmitting openings formed in the upper side of each collector bar and in the bottom side of each primary air bar that overlap with ...

CATALYTIC CRACKING SYSTEM WITH BIO-OIL PROCESSING

A catalytic cracking system in which liquid hydrocarbon and bio-oil are directed into a reactor riser of a fluid catalytic cracking unit by separate feed spray nozzle assemblies. To protect liquid bio-oil directed through the liquid bio-oil feed nozzle assembly from high temperature degradation, an insulating layer is provided between a central bio-oil feed tube in a concentrically surrounding atomizing gas passageway. Cooling channels also may be provided in the spray tip of the bio-oil feed nozzle assembly. 1. A catalytic cracking system comprising:a catalytic cracking reactor;a riser communicating upwardly to said catalytic cracking reactor;a supply of a liquid hydrocarbon;a first feed spray nozzle assembly mounted in and extending through a wall of said riser and having a spray tip at a downstream end, said first feed spray nozzle assembly having an upstream end coupled to a supply of liquid hydrocarbon and a supply of atomizing gas such that liquid hydrocarbon directed through said first feed spray nozzle assembly is atomized by the atomizing gas and discharged from said spray tip into riser as a finely atomized liquid hydrocarbon spray;a second feed spray nozzle assembly comprising an elongated nozzle body mounted in and extending through the wall of said catalytic cracking riser and having a spray tip at a downstream end;a bio-oil feed tube supported within the elongated nozzle body having an upstream end connected to a supply of a liquid bio-oil for directing liquid bio-oil through bio-oil feed tube to said spray tip;said elongated nozzle body defining an annular atomizing gas passage in surrounding relation to said bio-oil feed tube; said annular atomizing gas passage being connected to a supply of atomizing gas for direction through said annular atomizing gas passage for atomizing liquid bio-oil discharging from the liquid feed tube and spray tip into a fine particle liquid bio-oil spray; andan annular insulating layer between said bio-oil feed tube and ...

SYSTEM AND METHOD FOR PRODUCING HIGH-PURITY VANADIUM TETRAOXIDE POWDER

The present invention provides a system and method for producing high-purity vanadium tetraoxide powder. Industrial grade vanadium pentoxide is converted to vanadium oxytrichloride by low temperature fluidizing chlorination, wherein chlorinating gas is preheated via heat exchange between fluidizing gas and chlorination flue gas, and an appropriate amount of air is added to enable a part of carbon powder to combust so as to achieve a balanced heat supply during the chlorination, thereby increasing the efficiency of chlorination and ensuring good selectivity in low temperature chlorination. The vanadium oxytrichloride is purified by rectification, and then subjected to fluidized gas phase hydrolyzation, thereby producing a high-purity vanadium pentoxide product and a by-product solution of hydrochloric acid, and further obtaining a high-purity vanadium tetraoxide powder product through fluidized hydrogen reduction. The system and method have advantages of favorable adaptability to raw material, no discharge of contaminated wastewater, low energy consumption, etc. 1. A system for producing high-purity vanadium tetraoxide powder ,comprising a feeding device, a low temperature chlorination fluidized bed, a rectification and purification device, a gas phase hydrolyzation fluidized bed, a high-purity vanadium pentoxide feeding device, a reduction fluidized bed, a tail gas washing absorber, an induced draft fan and a chimney;wherein the feeding device comprises an industrial grade vanadium pentoxide hopper, an industrial grade vanadium pentoxide screw feeder, a carbon powder hopper and a carbon powder screw feeder;the low temperature chlorination fluidized bed comprises a chlorination bed feeder, a chlorination fluidized bed body, a chlorination bed cyclone separator, a flue gas heat exchanger, a flue gas condenser, a chlorination bed acid-seal tank and a chlorination bed spiral slag-discharging device;the rectification and purification device comprises a distilling still, ...

SYSTEMS AND METHODS FOR CONTROLLING BED AGGLOMERATION IN FLUIDIZED-BED BOILERS

The present disclosure relates to fluidized-bed boilers and methods for controlling bed agglomeration that can occur when biomass containing high amounts of phosphorus is used as fuel. Iron-containing compounds, such as iron oxide, are added to the fluidized bed to tie up the phosphorus in a form that will not react under typical operating conditions for fluidized-bed boilers. 1. A method for reducing bed agglomeration in a fluidized-bed boiler when a biomass fuel is combusted , comprising:adding at least one iron-containing compound to a fluidized bed of the fluidized-bed boiler.2. The method of claim 1 , wherein the at least one iron-containing compound is an iron (II) oxide; an iron (III) oxide; an iron (II) halide; an iron (III) halide; an iron (III) iodate; or an iron (II) carbonate.3. The method of claim 1 , wherein the at least one iron-containing compound is water soluble claim 1 , and is added in the form of a solution.4. The method of claim 1 , wherein the at least one iron-containing compound is water insoluble claim 1 , and is added in the form of a suspension or emulsion.5. The method of claim 1 , wherein the biomass fuel is corn stover claim 1 , switch grass claim 1 , miscanthus claim 1 , or hybrid poplar.6. The method of claim 1 , wherein the fluidized-bed boiler operates at a temperature of about 1200° F. to about 2000° F. (about 648° C. to about 1093° C.).7. The method of claim 1 , wherein an air/fuel stoichiometry of the fluidized-bed boiler is about 0.4 to about 0.5.8. The method of claim 1 , wherein the at least one iron-containing compound is added to the fluidized bed in an amount of up to 12 wt % of the biomass fuel.9. The method of claim 1 , wherein the at least one iron-containing compound is added to the fluidized bed in an amount of up to 3 moles per mole of (sodium oxides+potassium oxides+phosphorus oxides).10. The method of claim 1 , wherein the at least one iron-containing compound is added to the fluidized bed in an amount of up to 3 ...

Fluid Bed Steam Cracking Using Direct Heating

Systems and methods are provided for performing steam cracking on a feed while using direct heating of the reaction environment. The heating of the reaction environment can be achieved in part by transporting heat transfer particles from a heating zone to cracking zone. This can be performed in a fluidized bed reactor, a moving bed reactor, a riser reactor, or another type of reactor that can allow for catalyst movement and regeneration during operation. 1. A method for performing steam cracking using direct heat transfer , comprising:fluidizing a bed of heat transfer particles with a fluidizing gas comprising one or more of steam, oxygen, and a first portion of a hydrocarbon feedstock, the fluidized bed of heat transfer particles comprising a heating zone and a cracking zone above the heating zone;exposing the fluidized bed of heat transfer particles to oxygen in the heating zone under oxidizing conditions to generate a temperature in the heating zone of about 760° C. to about 1900° C., at least a portion of the heat transfer particles in the heating zone comprising coke;exposing the hydrocarbon feedstock to the fluidized bed of heat transfer particles in the presence of steam in the cracking zone at a temperature of about 590° C. to about 1060° C. to generate cracked products and coke on heat transfer particles, the temperature in the heating zone being greater than the temperature in the cracking zone;contacting at least a portion of the cracked products with at least one of heat exchange surfaces and quench fluid in a quench zone above the cracking zone to form quenched cracked products; andwithdrawing a portion of the heat transfer particles from the heating zone and returning the heat transfer particles into at least one of the cracking zone and the quench zone.2. The method of claim 1 , further comprising oligomerizing olefins in the quenched cracked product to form an oligomerized product.3. A method for performing steam cracking using direct heat transfer ...

PELLETS USED IN CELL CULTURE AND METHODS OF MAKING THEREOF

The present invention is directed generally to dry cell culture media or feeds in pellet formats which can be reconstituted into liquid media for culturing cells in vitro. Each pellet composition may comprise the same or a different composition; for example, different vitamins, amino acids, buffers, trace salts, pH, iron chelators, etc. The invention also relates to methods of making dry cell culture media by altering ratios of different pellet compositions, or, methods of making modular dry cell culture media, or customizing media formulations for growing a cell type using pellets. The media pellets may be easier to handle either before reconstitution, during shipping and handling; and/or during reconstitution. Media pellets may be used in any container like bags including sterile, single use bags for preparing media formulations. The invention also relates to kits and culture systems using media pellets. 126.-. (canceled)27. A pelletized cell culture medium , feed , supplement or additive comprising one or more amino acids , one or more binders , one or more vitamins , one or more salts , and one or more trace components , wherein the amino acids are 25 to 40 percent , the binders are 20 to 65 percent , the vitamins are 1 to 5 percent , the salts are 2 to 10 percent , and the trace components are 0.01 to 0.05 percent.28. (canceled)29. The pelletized cell culture medium claim 27 , feed claim 27 , supplement or additive of claim 27 , wherein the vitamins are selected from one or more of vitamin B12 claim 27 , biotin claim 27 , choline claim 27 , folic acid claim 27 , niacinamide claim 27 , pyridoxine claim 27 , riboflavin claim 27 , thiamine claim 27 , ascorbic acid claim 27 , and para-aminobenzoic acid (PABA).30. (canceled)31. The pelletized cell culture medium claim 27 , feed claim 27 , supplement or additive of claim 27 , wherein the salts are selected from one or more of buffer salts claim 27 , iron claim 27 , zinc claim 27 , calcium claim 27 , copper claim 27 , ...

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 ...

PROCESS AND APPARATUS FOR REACTING FEED WITH FLUIDIZED CATALYST AND CONFINED QUENCH

A dehydrogenation process and apparatus contact a paraffinic stream with dehydrogenation catalyst to product olefinic product gases. The olefinic product gases are separated from spent dehydrogenation catalyst and contained in a confined space that has a smaller volume than the reactor particularly at the same elevation. The containment of the olefinic product gases facilitates quenching the olefinic product gases to terminate reaction and improve selectivity to propylene. 1. A process for contacting a paraffin stream with dehydrogenation catalyst comprising:distributing a paraffin stream to a reactor;contacting said reactant stream with a dehydrogenation catalyst stream to produce olefinic product gases and spent dehydrogenation catalyst;separating a spent dehydrogenation catalyst stream from an olefinic product gas stream in a primary separator;containing said olefinic product gas in a contained space having a volume smaller than the volume of the reactor at the same elevation;quenching said olefinic product gases in said contained space; anddischarging said olefinic product gases from said reactor.2. The process of wherein said contained space has a wall that is spaced apart from a shell of the reactor.3. The process of further comprising a plurality of cyclone separators in said separation chamber and ducting said olefinic product gases from said contained space into said cyclone separators.4. The process of further comprising separating a spent dehydrogenation catalyst from said olefinic product gases in said cyclone separators and dispensing said dehydrogenation catalyst by dip legs of said cyclone separators through a baffle into a dense dehydrogenation catalyst bed.5. The process of wherein said spent dehydrogenation catalyst stream separated from said olefinic product gases in said primary separator falls into said dense dehydrogenation catalyst bed.6. The process of wherein said spent dehydrogenation catalyst stream separated from said olefinic product ...

On-Line Adjustment of Mixed Catalyst Ratio By Trim and Olefin Polymerization with the Same

In an embodiment, a method for producing a polyolefin is provided. The method includes: contacting a first composition and a second composition in a line to form a third composition, wherein: the first composition comprises a contact product of a first catalyst, a second catalyst, a support, and a diluent, wherein the mol ratio of second catalyst to first catalyst is from 60:40 to 40:60, the second composition comprises a contact product of the second catalyst and a second diluent; introducing the third composition from the line into a gas-phase fluidized bed reactor; exposing the third composition to polymerization conditions; and obtaining a polyolefin.

NAPHTHA CATALYTIC CRACKING CATALYST, CATALYTIC CRACKING METHOD AND REACTION DEVICE

A method for catalytic cracking of naphtha is provided. Naphtha is catalytically cracked under the action of a catalyst. The catalyst includes aluminosilicate, alkali metal oxide, alkaline earth metal oxide, TiO, iron oxide, vanadium oxide and nickel oxide. On the other hand, a rapid separation component is arranged in a disengager of a catalytic cracking reaction device, so that a transport disengaging height is greatly reduced without changing a gas flow and a diameter of the disengager. In addition, the separation efficiency of oil gas and the catalyst is improved. 1. A method for catalytic cracking of naphtha , comprising:{'b': '1', 'S: delivering a catalyst in a pre-lift pipe through a regenerator sloped pipe and to flow upward under the action of a pre-lift medium to enter a dense phase section of a reactor,'}feeding a feedstock containing naphtha into the reactor tangentially upward through a nozzle located at a bottom of the dense phase section of the reactor;feeding the feedstock, by the nozzle of the reactor, along a tangential direction of a circular cross-sectional of the dense phase section of the reactor at an angle of 10-90° to a vertical direction;{'b': '2', 'S: enabling oil gas and the catalyst from a riser pipe to enter a settler of a reaction device,'}enabling the oil gas from the disengager to enter a separation system, and enabling the catalyst to flow out through a conveying part of a cyclone to fall into a settler stripping section;{'b': '3', 'S: stripping the catalyst, enabling the catalyst stripped to enter a regenerator through a spent sloped pipe, and heating the catalyst in the regenerator; and'}{'b': '4', 'S: enabling the catalyst to enter a disengager section of the regenerator to fall into a stripping section of the disengager section of the regenerator and enter a degassing tank, and'}stripping the catalyst in the degassing tank and enabling the catalyst stripped to return to the reactor through the regenerator sloped pipe.2. The ...

FLUIDIZED BED REACTOR AND A PROCESS USING SAME TO PRODUCE HIGH PURITY GRANULAR POLYSILICON

The present invention relates to a fluidized bed reactor, comprising a reaction tube, a distributor and a heating device, the reaction tube and the distributor at the bottom of the reaction tube composing a closed space, the distributor comprising a gas inlet and a product outlet, and the reaction tube comprising a tail gas outlet and a seed inlet at the top or upper part respectively, characterized in that the reaction tube comprises a reaction inner tube and a reaction outer tube, and the heating device is an induction heating device placed within a hollow cavity formed between the external wall of the reaction inner tube and the internal wall of the reaction outer tube, wherein the hollow cavity is filled with hydrogen, nitrogen or inert gas for protection, and is able to maintain a pressure of about 0.01 to about 5 MPa; and also to a process of producing high purity granular polysilicon using the reactor. The fluidized bed reactor according to the present invention uses induction heating to heat directly the silicon particles inside the reaction chamber, such that the temperature of the reaction tube is lower than that inside the reaction chamber, which accordingly avoids deposition on the tube wall and results in more uniform heating, and thus is useful for large diameter fluidized bed reactors with much increased output for a single reactor. 1. A fluidized bed reactor , comprising a reaction tube , a distributor and a heating device , the reaction tube and the distributor at the bottom of the reaction tube composing a closed space , the distributor comprising a gas inlet and a product outlet , and the reaction tube comprising a tail gas outlet and a seed inlet respectively at the top or upper part , wherein the reaction tube comprises a reaction inner tube and a reaction outer tube , and the heating device is an induction heating device placed within a hollow cavity formed between the external wall of the reaction inner tube and the internal wall of the ...

SYSTEMS AND METHODS FOR CONVERTING CARBONACEOUS FUELS

A system for converting carbonaceous fuels is provided. The system includes a gaseous fuel conversion reactor, a solid fuel conversion reactor, and a fuel pretreatment fluidized bed reactor disposed between the gaseous fuel conversion reactor and the solid fuel conversion reactor. The fuel pretreatment fluidized bed reactor devolatilizes a solid fuel using heat to produce an off-gas and a devolatilized solid fuel. The gaseous fuel conversion reactor converts the off-gas from the fuel pretreatment fluidized bed reactor to a product gas stream comprising carbon dioxide and water. The solid fuel conversion reactor receives a mixture of oxygen carrier solids and devolatilized solid fuel from the pretreatment reactor discharge and reduces the devolatilized solid fuel with the oxygen carrier solids to convert the devolatilized solid fuel to an intermediate gas.

Methods and Systems for Forming a Hydrocarbon Product

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

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 ...

A CO TO CO2 COMBUSTION PROMOTER

The invention is directed to a CO to COcombustion promoter comprising microsphere sized porous silica and/or alumina comprising particles further comprising on or more Group VIII noble metals wherein the noble metal is distributed in the particle as an eggshell such that a higher content of noble metal is present in the outer region of the particle as compared to the content of noble metal in the center of the particle. 1. A CO to COcombustion promoter comprising microsphere sized porous particles comprising at least one of silica and alumina and further comprising one or more Group VIII noble metals wherein the noble metal is distributed in the particle as an eggshell such that a higher content of noble metal is present in the outer region of the particle as compared to the content of noble metal in the centre of the particle.2. The combustion promoter according to claim 1 , wherein the microsphere sized particles have an average (D50) size of between 60 and 90 microns as measured by laser diffraction.3. The combustion promoter according to claim 1 , wherein microsphere sized particle is a gamma and/or theta alumina particle.4. The combustion promoter according to claim 1 , wherein the microsphere sized particle is a spray dried silica particle.5. The combustion promoter according to claim 1 , wherein the microsphere sized particle is an equilibrium or spent catalyst as obtained from a fluidized catalytic cracking (FCC) process.6. The combustion promoter according to claim 1 , wherein the attrition index as measured according to ASTM D-5757 of the CO to COcombustion promoter for a sieve fraction of combustion promoter particles of between 40 and 105 microns is between 5 and 25.7. The combustion promoter according to claim 6 , wherein the attrition index of the CO to COcombustion promoter for a sieve fraction of combustion promoter particles of between 40 and 105 microns is between 10 and 20.8. The combustion promoter according to claim 1 , wherein the Group VIII ...

PRODUCING FERTILIZER GRANULES WITH A DEFINED SIZE DISTRIBUTION

A fluid-bed granulator system for producing fertilizer granules with a defined size including a fluid-bed granulator, a first cooler externally connected with the fluid-bed granulator or forming an internal part of the fluid-bed granulator, and a product screen connected with the first cooler. The product screen includes an exit for on-size particles; an exit for oversized particles and an exit for undersized particles. The exit for undersized particles is connected to the fluid-bed granulator and the exit for oversized particles is connected to the fluid-bed granulator via one or more crushers. The exit for on-size particles is connected to a first splitter. The first splitter is connected to the fluid-bed granulator and a post processing unit. A particle size analyzer is located between the fluid-bed granulator and the product screen. 1. A fluid-bed granulator system for producing fertilizer granules with a defined size , comprising:a fluid-bed granulator,a first cooler externally connected to the fluid-bed granulator or forming an internal part of the fluid-bed granulator, an exit for on-size particles,', 'an exit for oversized particles, and', 'an exit for undersized particles;', 'wherein the exit for undersized particles is connected to the fluid-bed granulator and wherein the exit for oversized particles is connected to the fluid-bed granulator via one or more crushers;', 'wherein the exit for on-size particles is connected to a first splitter and wherein the first splitter is connected to the fluid-bed granulator and a post processing unit; and, 'a product screen connected to the first cooler wherein the product screen comprisesa particle size analyzer located between the fluid-bed granulator and the product screen.2. The fluid-bed granulator system of claim 1 , wherein the product screen comprises an exit for large on-size particles and an exit for small on-size particles.3. The fluid-bed granulator system of claim 2 , wherein the product screen comprises ...

Use of Light Gas By-Products in the Production of Paraxylene by the Methylation of Toluene and or Benzene

A process for producing paraxylene by the catalytic alkylation of benzene and/or toluene with methanol, which produces a para-rich mixture of xylene isomers, together with water and some light organic by-products, particularly dimethyl ether and C− olefins. The off-gas stream, containing the C olefins, may be recycled back to the reaction to be co-injected with methanol to reduce the methanol self-decomposition and the reaction of methanol to olefins or to fluidize catalyst particles recovered by a reactor cyclone. By using recycled off-gas rather than water or steam, the deleterious effects of water and/or steam on the catalyst aging and activity rates and the size of downstream equipment necessary to recover olefin by-products may be reduced. 1. A process for the alkylation of toluene and/or benzene to produce paraxylene (PX) comprising contact of said toluene and/or benzene with an alkylating agent selected from methanol , dimethyl ether , and mixtures thereof , in the presence of an alkylation catalyst in a fluidized bed alkylation reactor under conditions effective to produce an alkylation effluent comprising PX and olefins , wherein the alkylation effluent is separated into a stream comprising PX and a light gas stream comprising olefins , the improvement comprising recycling at least a portion of the light gas stream , including olefins , to the alkylation reactor for injection with alkylating agent , fluidizing particles of the alkylation catalyst recovered from the alkylation effluent , or both.2. The process of claim 1 , wherein the light gas stream further comprises oxygenates claim 1 , unreacted alkylating agent claim 1 , and contaminants claim 1 , and is treated to remove at least one of the oxygenates claim 1 , alkylating agent claim 1 , and contaminants prior to recycling the light gas stream to the alkylation reactor.3. The process of claim 1 , wherein the alkylating agent is methanol.4. The process of claim 3 , wherein the methanol and recycled ...

METHODS FOR MAKING LIGHT OLEFINS FROM DIFFERENT FEED STREAMS

According to one or more embodiments of the present disclosure, chemical streams may be processed by a method which may comprise operating a first chemical process, stopping the first chemical process and removing the first catalyst from the reactor, and operating a second chemical process. The reaction of the first chemical process may be a dehydrogenation reaction, a cracking reaction, a dehydration reaction, or a methanol-to-olefin reaction. The reaction of the second chemical process may be a dehydrogenation reaction, a cracking reaction, a dehydration reaction, or a methanol-to-olefin reaction. The first reaction and the second reaction may be different types of reactions. 2. The method of claim 1 , wherein the first product stream and the second product stream comprise one or more of ethylene claim 1 , propylene claim 1 , or butene.3. The method of claim 1 , wherein the first reaction or the second reaction is a dehydrogenation reaction claim 1 , and the first catalyst or the second catalyst comprises gallium claim 1 , platinum claim 1 , or both.4. The method of claim 1 , wherein:the first reaction or the second reaction is a dehydrogenation reaction; andthe first feed stream or the second feed stream comprises one or more of ethane, propane, n-butane, and i-butane.5. The method of claim 1 , wherein the first reaction or the second reaction is a cracking reaction claim 1 , and the first catalyst or the second catalyst comprises one or more zeolites.6. The method of claim 1 , wherein:the first reaction or the second reaction is a cracking reaction; andthe first feed stream or the second feed stream comprises one or more of naphtha, n-butane, or i-butane.7. The method of claim 1 , wherein the first reaction or the second reaction is a dehydration reaction claim 1 , and the first catalyst or second catalyst comprises one or more acid catalysts.8. The method of claim 1 , wherein:the first reaction or the second reaction is a dehydration reaction;the first feed ...

PROTECTED FISCHER-TROPSCH CATALYST AND METHOD OF PROVIDING SAME TO A FISCHER-TROPSCH PROCESS

A method of preparing a spray dried catalyst by combining spray dried catalyst particles with wax so the spray dried catalyst particles are coated with wax, yielding wax coated catalyst particles, and shaping the wax coated catalyst to provide shaped wax coated catalyst. A method of activating Fischer-Tropsch catalyst particles containing oxides by contacting the catalyst particles with a reducing gas in an activation vessel to produce an activated catalyst, wherein contacting is performed in the absence of a liquid medium under activation conditions. A system for activating a Fischer-Tropsch catalyst containing an activation reactor configured to introduce an activation gas to a fixed or fluidized bed of the Fischer-Tropsch catalyst in the absence of a liquid medium and at least one separation device configured to separate a gas stream comprising entrained catalyst fines having an average particle size below a desired cutoff size from the activation reactor. 1. A system for activating a Fischer-Tropsch catalyst , the system comprising:an activation reactor configured to introduce an activation gas to a fixed or fluidized bed of the Fischer-Tropsch catalyst in the absence of a liquid medium; andat least one separation device configured to separate a gas stream comprising entrained catalyst fines having an average particle size below a desired cutoff size from the activation reactor.2. The system of wherein the activation reactor is a fluidized bed reactor.3. The system of wherein the cutoff size is about 10 μm.4. The system of wherein at least one of the at least one separation devices is located at least partially within the activation reactor.5. The system of wherein the at least one separation device located at least partially within the activation reactor is selected from cyclones and filters.6. The system of comprising a cyclone at least partially within the activation reactor.7. The system of further comprising a filtration unit external to the activation ...

METHOD FOR FLUIDIZING COPPER SILICIDE AND PROCESS FOR PREPARING A HALOSILANE USING THE METHOD

A method is useful for maintaining a uniformly fluidized bed in a fluidized bed apparatus. The method includes the steps of charging a mixture of particles including copper silicide particles and fluidization additive particles into the fluidized bed apparatus, and uniformly fluidizing the particles at a temperature of at least 400° C. in the fluidized bed apparatus. 1. A method maintaining a uniformly fluidized bed in a fluidized bed apparatus comprises:(A) heating, at a temperature of at least 400° C., a mixture of particles comprising greater than 80 weight % to less than 100% copper silicide particles and greater than 0 to 20 weight % fluidization additive particles in the fluidized bed apparatus, and(B) feeding a fluid into the fluidized bed apparatus at a velocity sufficient to maintain uniform fluidization.2. The method of claim 1 , where the copper silicide particles have a particle size of 10 μm to 150 μm.3. The method of claim 1 , where the additive particles are present in an amount of greater than 0 weight % to 10 weight % claim 1 , based on total weight of the mixture.4. The method of claim 1 , where the copper silicide particles are present in an amount of 95 weight % to 98 weight % of the mixture claim 1 , and the fluidization additive particles are present in an amount of 2 weight % to 5 weight % of the mixture.5. The method of claim 1 , where the copper silicide is selected from the group consisting of (i) CuSi claim 1 , (ii) CuSi claim 1 , (iii) CuSi claim 1 , and (iv) CuSi claim 1 , and a mixture of two or more of (i) claim 1 , (ii) claim 1 , (iii) claim 1 , (iv).6. The method of claim 1 , where the copper silicide comprises CuSi.7. The method of claim 1 , where the copper silicide has empirical formula CuSiCrCoFeIrNiPdPtReRu claim 1 , where subscripts b claim 1 , c claim 1 , d claim 1 , e claim 1 , f claim 1 , g claim 1 , h claim 1 , i claim 1 , j claim 1 , k claim 1 , and m represent the molar amounts of each element present claim 1 , and b>0 ...

COLD REGENERATED CATALYST CIRCULATION METHOD AND DEVICE THEREFOR

The present invention provides a method of cooling and cycling a regenerated catalyst. The regenerated catalyst that is from the regenerator is cooled by the catalyst cooler to 200-720° C., and without being mixed with the hot regenerated catalyst directly enters a riser reactor, or mixes with another part of hot regenerated catalyst that has not been cooled to obtain a mixed regenerated catalyst with a temperature below the regenerator temperature, and enters the riser reactor. The hydrocarbon raw material performs the contact reaction with the catalyst in the riser reactor, a reactant stream enters a settler to perform a separation of the catalyst and an oil gas, the separated spent catalyst is steam stripped by a steam stripping section and enters a regenerator to be charring regenerated, and the regenerated catalyst after being cooled returns to the riser reactor to be circularly used. The bottom of each of the catalyst coolers is provided with at least one fluidized medium distributor, the range of the superficial gas velocity is 0-0.7 m/s (preferably 0.005-0.3 m/s, and most preferably 0.01-0.15 m/s), and the temperature of the cold regenerated catalyst is controlled mainly by adjusting a flow rate of the fluidized medium. The method of cooling and cycling a regenerated catalyst of the present invention has extensive application, and can be used for various fluidized catalytic cracking processes, including heavy oil catalytic cracking, wax oil catalytic cracking, gasoline catalytic conversion reforming and the like, and can also be used for other gas-solid reaction processes, including residual oil pretreating, methanol to olefin, methanol to aromatics, methanol to propylene, fluid coking, flexicoking and the like. 1. A cycling method of cold regenerated catalyst , comprising a fluidized catalytic cracking process , wherein: a hydrocarbon raw material performs a contact reaction with a catalyst in a riser reactor having or not having a fluidized bed reactor , a ...

System and Method for Preparing High-Purity Vanadium Pentoxide Powder

The present invention provides a system and method for preparing high-purity vanadium pentoxide powder. Industrial grade vanadium pentoxide is converted to vanadium oxytrichloride by low temperature fluidizing chlorination, wherein chlorinating gas is preheated via heat exchange between fluidizing gas and chlorination flue gas, and an appropriate amount of air is added to enable a part of carbon powder to combust so as to achieve a balanced heat supply during the chlorination, thereby increasing the efficiency of chlorination and ensuring good selectivity in low temperature chlorination. The vanadium oxytrichloride is subjected to purification by rectification, ammonium salt precipitation and fluidized calcination, thereby obtaining high-purity vanadium pentoxide, wherein the ammonia gas produced during calcination is condensed and then recycled for ammonium salt precipitation. The system and method have advantages of favorable adaptability to raw material, less pollution, low energy consumption in production, low operation cost, stable product quality, etc. 1. A system for preparing high-purity vanadium pentoxide powder , comprising a feeding device , a low temperature chlorination fluidized bed , a rectification and purification device , an ammonium salt precipitation device , an ammonium salt feeding device , a calcination fluidized bed , a tail gas washing absorber , an induced draft fan and a chimney;wherein the feeding device comprises an industrial grade vanadium pentoxide hopper, an industrial grade vanadium pentoxide screw feeder, a carbon powder hopper and a carbon powder screw feeder;the low temperature chlorination fluidized bed comprises a chlorination bed feeder, a chlorination fluidized bed body, a chlorination bed cyclone separator, a flue gas heat exchanger, a flue gas condenser, a chlorination bed acid-seal tank and a chlorination bed spiral slag-discharging device;the rectification and purification device comprises a distilling still, a rectifying ...

Process for the Positioning of a Corrosion-Resistant Coating on a Wall of an Item of Equipment of a FCC Unit

The invention relates to a process for the positioning of a corrosion-resistant coating on an internal or external metal wall ( 20 ) of a fluid catalytic cracking unit chamber, comprising: (i) the shaping of a metal anchoring structure ( 10 ) formed from a plurality of strips ( 12 ) assembled in pairs by joining assembly portions ( 121, 122 ) so as to form a plurality of cells ( 14 ), the anchoring structure comprising a plurality of fastening tabs ( 16 ) integral with strip portions other than assembly portions, (ii) the fastening of said anchoring structure ( 10 ) by welding the free edge ( 18 ) of a part at least of the fastening tabs to the metal wall ( 20 ), defining a space between a longitudinal edge ( 12 b ) of an anchoring structure and the metal wall, (iii) the insertion of a composite material into the cells ( 14 ) from the metal wall ( 20 ) and at least up to the upper longitudinal edge ( 12 a ) of each strip.

Using Wavelet Decomposition To Determine the Fluidization Quality In a Fluidized Bed Reactor

A method and apparatus for determining the fluidization quality of a fluidized bed reactor is disclosed. The method includes measuring pressure within the fluidized bed reactor to obtain a pressure signal. The pressure signal is then transformed using wavelet decomposition into higher-frequency details and lower-frequency approximations. The dominance of the various features is then calculated based on the energy of each feature in relation to the normalized wavelet energies. The fluidization quality of the fluidized bed reactor is then determined from a comparison over time of the calculated energies.

Chemical Synthesis And Synthesis Reactors

The present disclosure relates to chemical synthesis. The teachings thereof may be embodied in methods for chemical synthesis and/or reactors for synthesis. The teaching may increase the conversion of equilibrium-limited reactions in a single pass through a synthesis reactor. For example, a method may include: introducing a synthesis reactant into a reaction chamber with a prevailing pressure p; forming a synthesis product; discharging the product and any unreacted reactant; separating the product from the unreacted reactant; and introducing the unreacted reactant into a second reaction chamber with a prevailing pressure p lower than the pressure p 1. A method of conducting a chemical synthesis , the method comprising:{'b': '1', 'introducing a synthesis reactant into a reaction chamber with a prevailing pressure p;'}forming a synthesis product in the reaction chamber consuming at least part of the synthesis reactant;discharging the synthesis product and any unreacted synthesis reactant from the reaction chamber;separating the synthesis product from the unreacted synthesis reactant; and{'b': 2', '1, 'introducing the unreacted synthesis reactant into a second reaction chamber with a prevailing pressure p lower than the pressure p.'}2. The method as claimed in claim 1 , wherein the first and second reaction chambers are connected by a heat pipe; anda heat of reaction resulting from formation of the synthesis product is exchanged between the reaction chambers.3. The method as claimed in claim 1 , wherein the heat pipe passes out of at least one of the first or second reaction chambers claim 1 , and heat energy is removed therefrom.4. The method as claimed in claim 1 , wherein the reaction chambers are charged with carrier liquid into which the synthesis reactant is introduced; andthe synthesis reactant is converted at least in part to the synthesis product with in the carrier liquid.5. The method as claimed in claim 4 , further comprising supplying a particulate ...

DEVICE FOR PRODUCING POLY(METH)ACRYLATE IN POWDER FORM

An apparatus for producing pulverulent poly(meth)acrylate in a reactor for droplet polymerization having an apparatus for dropletization of a monomer solution for the production of the poly(meth)acrylate having holes through which the monomer solution is introduced, an addition point for a gas above the apparatus for dropletization, at least one gas withdrawal point on the circumference of the reactor and a fluidized bed, and above the gas withdrawal point the reactor has a region having a constant hydraulic internal diameter and below the gas withdrawal point the reactor has a hydraulic internal diameter that steadily decreases. 11513519111191193513535. An apparatus for producing pulverulent poly(meth)acrylate , comprising a reactor () for droplet polymerization comprising an apparatus () for dropletization of a monomer solution for the production of the poly(meth)acrylate comprising holes through which the monomer solution is introduced , an addition point () for a gas above the apparatus () for dropletization , at least one gas withdrawal point () on the circumference of the reactor () and a fluidized bed () , wherein above the gas withdrawal point () the reactor () comprises a region having a constant hydraulic internal diameter and below the gas withdrawal point () the reactor has a hydraulic internal diameter that steadily decreases , wherein in the region having a steadily decreasing hydraulic internal diameter there are tappers () affixed to the exterior of the reactor () , wherein the tappers () each generate an impact energy of from 25 J to 165 J and the number of tappers () is chosen such that an area-specific impact energy of from 1 to 7 J/mis applied.235. The apparatus according to claim 1 , wherein the tappers () are impulse tappers.335. The apparatus according to claim 1 , wherein the tappers () have a configuration such that they can generate at least one impact per minute.43535. The apparatus according to claim 1 , wherein the tappers () have a ...

TAPERED FLUIDIZED BED REACTOR AND PROCESS FOR ITS USE

A fluidized bed reactor includes a gas distributor, a tapered section above the gas distributor, and an expanded head above the tapered section. The gas distributor defines a plurality of inlets surrounding a product withdrawal tube, which extends away from the fluidized bed reactor. The fluidized bed reactor is useful in a process for fluidizing relatively large particles, such as Geldart Group B particles and/or Geldart Group D particles, where said particles are in a bubbling fluidized bed residing, in whole or in part, in the tapered section. The fluidized bed reactor and process may be used for manufacturing polycrystalline silicon. 1. A process for preparing polycrystalline silicon in a fluidized bed reactor , where the process comprises:feeding gases comprising hydrogen and a silicon bearing source gas comprising a silicon monomer into a bubbling fluidized bed containing silicon particles, where at least a portion of the bubbling fluidized bed resides in a tapered section of the fluidized bed reactor, where the tapered section expands upward and outward at a cone angle from vertical;feeding silicon particles into the fluidized bed reactor above the tapered section;heating the fluidized bed reactor, thereby causing thermal decomposition of the silicon monomer to produce polycrystalline silicon on surfaces of the silicon particles, thereby producing larger diameter particles; andremoving the larger diameter particles from the fluidized bed reactor.2. The process of claim 1 , where the cone angle ranges from 2.5° to 10.0°.3. The process of claim 1 , where the silicon bearing source gas comprises HSiCland optionally SiCl.4. The process of claim 1 , where the silicon bearing source gas comprises HSiBrand optionally SiBr.5. The process of claim 1 , where the silicon bearing source gas comprises SiH.6. The process of claim 1 , wherein i. a product withdrawal tube is mounted to the gas distributor,', 'ii. the gas distributor defines a plurality of feed inlets, and', ...

MICROCHANNEL REACTORS AND FABRICATION PROCESSES

A method of loading material within a microchannel device, the method comprising: (a) loading particulates into a plurality of microchannels; and, (b) ultrasonically packing the particulates into the plurality of microchannels using a portable, compact ultrasonic densification unit. 135-. (canceled)36. A method of increasing packing density of particulates loaded into a plurality of microchannels in microchannel apparatus , comprising: providing a microchannel apparatus comprising a plurality of microchannels having particulates contained therein; mounting a portable , compact ultrasonic device to a microchannel apparatus , the portable , compact ultrasonic device configured to be repositionable between a first position where the portable , compact ultrasonic device is in acoustic communication with the plurality of microchannels and a second position where the portable , compact ultrasonic device is not in acoustic communication with the plurality of microchannels; and , applying ultrasonic sound to the plurality of microchannels from the portable , compact ultrasonic device to densify the particulates to form a packed bed of particulates within the plurality of microchannels.37. The method of claim 36 , wherein a sonically conductive material is disposed between the portable claim 36 , compact ultrasonic device and the plurality of microchannels.3841-. (canceled)42. The method of claim 36 , wherein the ultrasonic sound is applied in bursts of one to ten seconds.43. The method of claim 36 , wherein each microchannel in the plurality of microchannels has a length of at least 10 cm and at least one dimension of 10 mm or less.44. The method of claim 36 , wherein the microchannel apparatus comprises at least 1000 microchannels and wherein the portable claim 36 , compact ultrasonic device extends over no more than 500 of the at least 1000 microchannels at one time.45. The method of claim 36 , wherein: the microchannel apparatus comprises an insert that extends down the ...

GAS DISTRIBUTION PLATE FOR THERMAL DEPOSITION

Apparatus and methods for providing high velocity gas flow showerheads for deposition chambers are described. The showerhead has a faceplate in contact with a backing plate that has a concave portion to provide a plenum between the backing plate and the faceplate. A plurality of thermal elements is within the concave portion of the backing plate and extends to contact the faceplate. 1. A gas distribution plate comprising:a faceplate having a front surface and a back surface defining a thickness and a plurality of apertures extending through the thickness; anda backing plate having a front surface and a back surface defining a thickness, the front surface in contact with the back surface of the faceplate, the front surface of the backing plate including a concave portion to form a plenum bounded by the concave portion and the back surface of the faceplate, and a plurality of thermal elements extending from a concave surface the concave portion and contacting the back surface of the faceplate.2. The gas distribution plate of claim 1 , wherein each of the thermal elements independently extends a length from the concave surface of the concave portion to a front surface of the thermal element.3. The gas distribution plate of claim 2 , wherein the front surfaces of the thermal elements are substantially coplanar.4. The gas distribution plate of claim 2 , wherein each of the thermal elements has a tapered profile with a flared base at the concave surface of the concave portion and a narrower end at the front surface.5. The gas distribution plate of claim 2 , wherein the backing plate has an outer peripheral edge and the concave portion has an outer peripheral edge.6. The gas distribution plate of claim 5 , wherein an outer front face ring defined as the front surface of the backing plate between the outer peripheral edge of the concave portion and the outer peripheral edge of the backing plate is substantially flat.7. The gas distribution plate of claim 6 , wherein the ...

Feedstock Injection Device of an FCC Unit

The invention relates to an injection device () for atomizing a liquid into droplets using a gas, comprising a hollow tubular body () having a longitudinal direction (X). An inner wall () defines a first region, referred to as contact region (Z), and a second region (Z). The body includes: —at least two inlet ports () for injecting liquid and an inlet port for injecting gas, all of said ports extending to the first region (Z); —at least one outlet port (), located downstream of the first and second regions, for discharging the atomized liquid. The body () has an inner cross-section that varies continuously or constantly over the entire length thereof. Between regions (Z) and (Z), the inner wall () includes at least one baffle () which is shaped such that in each plane running perpendicularly to the longitudinal direction of the body containing said baffle, the baffle reduces an inner cross-section of the body over the entire periphery of the inner wall (). 112.-. (canceled)1312. An injection device configured to atomize a liquid into droplets using a gas , comprising a hollow tubular body extending in a longitudinal direction (X) and of which an internal wall defines a first zone referred to as a first contact zone (Z) and a second zone (Z) situated downstream of the first zone with respect to a direction in which the liquid and the gas circulate inside the body , the latter having:{'b': '1', 'at least two inlet openings opening into the first contact zone (Z), to inject a liquid into the first zone, the said openings each having an axis oriented in such a way that the streams of liquid emanating from the said openings converge on a longitudinal line (X) extending inside the body,'}{'b': '1', 'an inlet opening opening into the first contact zone (Z), so as to inject an atomizing gas into the first contact zone,'}at least one outlet orifice situated downstream of the first and second zones, for removing the atomized liquid from the body,characterized in that the body ...

Reactors and systems for oxidative coupling of methane

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

METHOD FOR DEPOSITING AN IN SITU COATING ONTO THERMALLY AND CHEMICALLY LOADED COMPONENTS OF A FLUIDIZED BED REACTOR FOR PRODUCING HIGH-PURITY POLYSILICON

In situ coating of the reactor tube of a CVD fluidized bed reactor for producing granular polysilicon allows a wider selection of reactor tube materials to be used and provides granular polysilicon product of higher purity. 18.-. (canceled)9. A process for coating thermally and chemically stressed components of a fluidized-bed reactor containing a reactor tube for producing granular polysilicon , comprising flushing the fluidized-bed reactor which is free of bed material or which contains a reduced amount of bed material as compared to the amount of bed material present during steady state production of granular polysilicon , with a reactive gas mixture at an average reactor tube wall temperature of from 600 to 1400° C. for a period of from 1 hour to 8 days and at a pressure of from 1 to 15 bar abs , and thereby providing surfaces of the reactor which have a temperature of more than 600° C. with an in-situ coating of Si and/or SiNby means of a CVD process.10. The process of claim 9 , wherein the reactive gas mixture is a mixture of compounds of the formula SiHCl(I) where 0≤x≤4 and a nitrogen source and/or a carrier gas selected from the group consisting of Ar or Hand/or an organic compound having from 1 to 10 carbon atoms; or is a mixture of one or more compounds of the formula RSiHyCl claim 9 , (II) where 1≤x≤4 claim 9 , 1≤y≤3 and x+y≤4 and R═CH(n=1-5) and a carrier gas selected from the group consisting of Ar claim 9 , H claim 9 , and mixtures thereof.11. The process of claim 9 , wherein the compound of the formula (I) or (II) is used in an amount of from 0.01 to 50% by volume.12. The process of claim 9 , wherein the compound of the formula (I) or (II) is used in an amount of from 0.01 to 10% by volume.13. The process of claim 9 , wherein coating takes place at a surface temperature which differs by not more than ±250° C. claim 9 , from the surface temperature in the steady-state fluidized-bed deposition process.14. The process of claim 9 , wherein coating takes ...

Multiple Reactor and Multiple Zone Polyolefin Polymerization

Apparatuses and processes that produce multimodal polyolefins, and in particular, polyethylene resins, are disclosed herein. This is accomplished by using two reactors in series, where one of the reactors is a multi-zone circulating reactor that can circulate polyolefin particles through two polymerization zones optionally having two different flow regimes so that the final multimodal polyolefin has improved product properties and improved product homogeneity. 1. A trimodal polyethylene resin having a low molecular weight (LMW) component , an intermediate molecular weight (IMW) component , and a high molecular weight (HMW) component; wherein the LMW component is present in an amount of from about 20 wt. % to about 75 wt. %; wherein the IMW component is present in an amount of from about 5 wt. % to about 40 wt. %; wherein the LMW component has a weight average molecular weight of from about 20 kg/mol to about 150 kg/mol; wherein the IMW component has a weight average molecular weight of from about 85 kg/mol to about 350 kg/mol; wherein the weight average molecular weight of the IMW component is greater than the weight average molecular weight of the LMW component; wherein the weight average molecular weight of the HMW component is greater than the weight average molecular weight of the IMW component; wherein the trimodal polyethylene resin has a Young's modulus (E) of equal to or greater than about 900 MPa , when tested in accordance with ASTM D638; and wherein the trimodal polyethylene resin has a density of equal to or greater than about 0.952 g/cc , when tested in accordance with ASTM D1505.2. The trimodal polyethylene resin of claim 1 , wherein the trimodal polyethylene resin has a melt index of less than about 1 g/10 min claim 1 , when tested in accordance with ASTM D1238 under a force of 2.16 kg.3. The trimodal polyethylene resin of claim 1 , wherein the trimodal polyethylene resin has a density of equal to or greater than about 0.955 g/cc claim 1 , when tested ...

EXTENDED CONTACT TIME RISER

A riser includes a housing in communication with a entry conduit and an exit conduit. The housing is defined by a holdup chamber having a volume of between about 1133 liters and about 45307 liters. The riser is designed to receive a hydrocarbon feed and a catalyst. An apparatus for fluid catalytic cracking includes a riser in fluid communication with a reactor vessel. A hydrocarbon feed stream and a catalyst travel through a first section of the riser at a first velocity of between about 1.5 msec to about 10 msec and through a second section of the riser at a second velocity of more than about 15 msec. A process for fluid catalytic cracking uses a riser with a holdup chamber. A hydrocarbon feed and a catalyst decrease in velocity in the holdup chamber to between 1.5 msec and 10 msec. 1. A riser , comprising:a housing in communication with an entry conduit and an exit conduit,wherein the housing is defined by a holdup chamber having a volume of between about 1133 liters to about 45307 liters, and wherein the housing is designed to receive a hydrocarbon feed and a catalyst.2. The riser of claim 1 , wherein the width dimension of the holdup chamber is greater than the width dimension of at least one of the entry conduit or exit conduits.3. The riser of claim 1 , wherein the width dimension of the holdup chamber is greater than the width dimension of both of the entry conduit and exit conduits.4. The riser of claim 1 , wherein the holdup chamber includes an angled lower surface and an angled upper surface.5. The riser of claim 4 , wherein the angled lower surface and the angled upper surface are each characterized by an angle of between about 20 degrees to about 60 degrees.6. The riser of claim 1 , wherein the holdup chamber disrupts the flow of the catalyst along an interior surface thereof. This application is a Division of copending application Ser. No. 13/907,232 filed May 31, 2013, the contents of which are hereby incorporated by reference in its entirety.This ...

BIOMASS DIGESTER WITH TWO LIQUID PHASES AND DRAFT TUBE CIRCULATION

A method comprises introducing biomass solids to a digester comprising a reactor, a circulation system including a first injector; providing a catalyst-containing digestion medium and an organic solvent layer floating thereon; circulating the medium through the circulation system; flowing gas through the medium; keeping the medium hot enough to digest the solids; and operating the digester such a headspace exists above the solvent. The digester includes a first eductor having an inlet in the headspace, a second eductor having an inlet in the organic layer, and a downdraft tube having an inlet in the digestion medium. A motive fluid flowing from the first injector draws gas from the headspace into the first eductor, a motive fluid flowing from the first eductor draws fluid from the organic layer into the second eductor, and a motive fluid flowing from the second eductor draws fluid from the digestion medium into the downdraft tube. 1. A method comprising: i) a reactor;', 'ii) a gas feed line for providing gas to the reactor;', 'iii) a biomass feed system for feeding biomass into the reactor;', 'iv) a fluid circulation system including a fluid inlet, a pump, and at least one fluid injector, wherein at least said fluid inlet and said fluid injector are in fluid communication with said pump and are within said reactor; and', 'v) a screen positioned within the reactor and defining a lower zone therebelow;, 'a) introducing cellulosic biomass solids to a hydrothermal digestion unit comprisingb) providing a liquid phase digestion medium containing a slurry catalyst in the hydrothermal digestion unit, the slurry catalyst being capable of activating molecular hydrogen;c) providing a layer of organic solvent in the hydrothermal digestion unit, said organic solvent being less dense than and substantially immiscible with said digestion medium, whereby said organic solvent forms an organic layer floating on said digestion medium;d) circulating said liquid phase digestion medium ...

FLUIDIZED BED COOLER WITH REGIONAL COORDINATION ENHANCEMENT

The present disclosure discloses a fluidized bed cooler with regional coordination enhancement, comprising a shell, a catalyst inlet, an interior of the shell is divided into a catalyst inlet influence region, a dilute phase region, a dense phase region and a gas distributor influence region; a catalyst inlet inclined tube is provided obliquely upward at the catalyst inlet, and a regional particle distributor is provided at the catalyst inlet; the dense phase region is provided with a plurality of dense phase baffle plates, and the dilute phase region is provided with a plurality of dilute phase baffle plates; and the gas distributor influence region is provided with double gas distributors. The fluidized bed cooler simultaneously well solves the low internal stability and the low heat exchange efficiency of the fluidized bed cooler, thereby realizing the stable and efficient operation of the fluidized bed cooler. 1. A fluidized bed cooler with regional coordination enhancement , comprising a shell which is cylindrical and vertically provided , wherein a plurality of heat exchange tubes are vertically distributed in the shell , a catalyst inlet is provided at an upper portion of the shell , a catalyst outlet is provided at a bottom portion of the shell , and an interior of the shell is divided into a catalyst inlet influence region , a dilute phase region at the upper portion , a dense phase region at the lower portion and a gas distributor influence region at the bottom portion , and wherein the dilute phase region and the dense phase region are located above and below the catalyst inlet influence region , respectively , wherein a catalyst inlet inclined tube is provided obliquely upward at the catalyst inlet , and a regional particle distributor is provided at the catalyst inlet positioned in the catalyst inlet inclined tube;wherein the regional particle distributor comprises a local gas distribution plate, a local gas pre-distributor, a left splitter partition ...

SYSTEM TO MAXIMIZE CO FROM FLUID CATALYTIC CRACKING (FCC) PROCESS BY COKE OXIDATION WITH METAL OXIDES

Provided is a process capable of converting the cokes on spent catalysts in a fluid catalytic cracking (FCC) process into synthesis gas. The produced synthesis gas contains high concentrations of CO and Hand may be utilized in many downstream applications such as syngas fermentation for alcohol production, hydrogen production and synthesis of chemical intermediates. A reducer/regenerator reactor for a fluid catalytic process comprising a chemical looping system to produce synthesis gas is also described. 1. A method for producing synthesis gas from catalyst coke generated from a fluid catalytic cracking process bya) providing a chemical looping system comprising a reducer/regenerator reactor, an oxidizer reactor and a combustor reactor;b) feeding catalyst coke particles and metal oxide particles into the reducer/regenerator reactor of the chemical looping system to produce a plurality of streams comprising a regenerated catalyst stream, a synthesis gas stream and a reduced metal oxide particle stream;c) feeding the stream of reduced metal oxide particles and a stream of water vapor into the oxidizer reactor of the chemical looping system to produce a plurality of streams comprising a hydrogen stream and a stream of oxidized metal oxide particles; andd) feeding the stream of oxidized metal oxide particles and a stream of air into the combustor reactor of the chemical looping system to produce heat and a stream of metal oxide particles.2. The method of claim 1 , wherein the reducer/regenerator reactor is a moving bed reactor.3. The method of claim 2 , wherein the reduced metal oxide particle stream and the regenerated catalyst stream of the moving bed reactor flow in the same direction.4. The method of claim 1 , wherein the reducer/regenerator reactor is a fluidized bed reactor.5. The method of claim 4 , wherein the reduced metal oxide particle stream and the regenerated catalyst stream of the fluidized bed reactor flow in the same direction.6. The method of claim 2 , ...

Catalyst and Process for the Production of Para-Xylene

A fluidized bed process for producing para-xylene via toluene and/or benzene methylation with methanol using a dual function catalyst system. A first catalyst accomplishes the toluene and/or benzene methylation and a second catalyst converts the by-products of the methylation reaction or unconverted methylating agent, improves the yields of the desired products, or a combination thereof. The inclusion of the second catalyst can suppress the C1-C5 non-aromatic fraction by over 50% and significantly enhance the formation of aromatics.

JOINT DESIGN FOR SEGMENTED SILICON CARBIDE LINER IN A FLUIDIZED BED REACTOR

Segmented silicon carbide liners for use in a fluidized bed reactor for production of polysilicon-coated granulate material are disclosed, as well as methods of making and using the segmented silicon carbide liners. Non-contaminating bonding materials for joining silicon carbide segments also are disclosed. One or more of the silicon carbide segments may be constructed of reaction-bonded silicon carbide. 1. A segmented silicon carbide liner for a fluidized bed reactor for production of polysilicon-coated granulate material , comprising:a first silicon carbide segment having a first segment upper edge surface defining one of an upwardly opening first segment depression or an upwardly extending first segment protrusion;a second silicon carbide segment located above and abutted to the first silicon carbide segment, the second silicon carbide segment having a second segment lower edge surface defining a downwardly opening second segment depression if the first segment upper edge surface defines an upwardly extending first segment protrusion or a downwardly extending second segment protrusion if the first segment upper edge surface defines an upwardly opening first segment depression, the protrusion being received within the depression and having smaller dimensions than the depression such that the surface of the depression is spaced apart from the surface of the protrusion and a space is located between the protrusion and the depression; anda volume of bonding material comprising a lithium salt, the bonding material disposed within the space between the protrusion and the depression.2. The segmented silicon carbide liner of claim 1 , wherein:the first silicon carbide segment comprises a first tubular wall having an annular upper surface, the first segment upper edge surface being at least a portion of the annular upper surface, and the first segment depression is a groove that is defined by and extends along at least a portion of the first segment upper edge surface or ...

SYSTEM AND METHOD FOR PERFORMING SEPARATION AND DEHYDROXYLATION OF FUMED SILICA SOOT PARTICLES

The present disclosure provides a separator system for performing separation and dehydroxylation of fumed silica particles. The separator system includes a first inlet, a second inlet, a main body, a first outlet and a second outlet. The first inlet collects a primary feed of fumed silica particles from a gaseous stream into a double entry cyclone. The second inlet collects a secondary feed of chlorine gas into the double entry cyclone. The main body of the double entry cyclone is utilized in treating the primary feed and the secondary feed along with heat inside the double entry cyclone. Furthermore, the first outlet is utilized for releasing the dehydrated fumed silica particles and the second outlet is utilized for releasing the water molecules and other gases. 1. A method for performing separation of fumed silica particles , the method comprising:collecting a primary feed of fumed silica particles from a gaseous stream, wherein the primary feed of fumed silica particles is collected in a fluidized state;collecting a secondary feed of chlorine gas, wherein the secondary feed of chlorine gas is collected for performing separation of the fluidized fumed silica particles;treating the primary feed of the fumed silica particles and the secondary feed of chlorine gas along with heat; andreleasing the dehydrated fumed silica particles from a first outlet, whereby separating the fumed silica particles.2. The method as recited in claim 1 , wherein the primary feed of fumed silica particles from a gaseous stream is collected into a double entry cyclone from a first inlet.3. The method as recited in claim 1 , wherein collecting the secondary feed of chlorine gas into the double entry cyclone from a second inlet.4. The method as recited in further comprising claim 1 , after performing separation of the fumed silica particles claim 1 , releasing water molecules and gases from a second outlet.5. A separator system for performing separation and dehydroxylation of fumed silica ...

SYSTEM AND METHOD FOR PREVENTING CATALYST FROM OVERHEATING

A system for preventing a catalyst from overheating is provided. The system includes: a first reactor filled with a catalyst at least in part and configured to receive reaction gas and produce product gas; and a second reactor configured to cool a catalyst discharged from the first reactor. The catalyst is circulated between the first reactor and the second reactor by injecting the catalyst cooled in the second reactor into the first rector. 1. A system for preventing a catalyst from overheating , the system comprising:a first reactor filled with a catalyst at least in part and configured to receive reaction gas and produce product gas; anda second reactor configured to cool a catalyst discharged from the first reactor,wherein the catalyst is circulated between the first reactor and the second reactor by injecting the catalyst cooled in the second reactor into the first rector.2. The system of claim 1 , wherein the catalyst is a catalyst of a particle shape having a diameter ranging from 1 to 9 claim 1 ,000 micrometers.3. The system of claim 1 , further comprising a path of a first cooling fluid passing through the first reactor claim 1 , andwherein the catalyst in the first reactor is cooled by the first cooling fluid.4. The system of claim 1 , wherein the first reactor is a fluidized bed reactor and the product gas is produced in a state in which the catalyst in the first reactor is fluidized.5. The system of claim 1 , wherein the second reactor is filled with the catalyst discharged from the first reactor at least in part claim 1 , andwherein the system further comprises a path of a second cooling fluid passing through the second reactor.6. The system of claim 1 , further comprising a path to allow the reaction gas to pass through the second reactor claim 1 , andwherein the reaction gas passing through the path of the reaction gas is pre-heated and supplied to the first reactor.7. A method for preventing a catalyst from overheating claim 1 , the method comprising ...

High severity fluidized catalytic cracking systems and processes for producing olefins from petroleum feeds

Systems and processes are disclosed for producing petrochemical products, such as ethylene, propene and other olefins from crude oil in high severity fluid catalytic cracking (HSFCC) units. Processes include separating a crude oil into a light fraction and a heavy fraction, cracking the light fraction and heavy fraction in separation cracking reaction zones, and regenerating the cracking catalysts in a two-zone regenerator having a first regeneration zone for the first catalyst (heavy fraction) and a second regeneration zone for the second catalyst (light fraction) separate from the first regeneration zone. Flue gas from the first catalyst regeneration zone is passed to the second regeneration zone to provide additional heat to raise the temperature of the second catalyst of the light fraction side. The disclosed systems and processes enable different catalysts and operating conditions to be utilized for the light fraction and the heavy fraction of a crude oil feed.

CARBON NANOTUBE-COATED CATALYST PARTICLE

The present invention applies carbon nanotubes to catalyst particles, thereby providing catalyst particles which are usable in fluidized bed reactions, have high catalytic activity, and are easy to handle. The catalyst particles are carbon nanotube-coated catalyst particles which each comprise a carrier particle and a coating layer disposed on the surface of the carrier particle, wherein the carrier particles are flowable in fluidized beds and the coating layer comprises carbon nanotubes which have metal nanoparticles supported thereon and/or which have been doped with nitrogen or boron. The carbon nanotube-coated catalyst particles are flowable in fluidized bed reactions. 1. A carbon nanotube-coated catalyst particle comprising a carrier particle and a coating layer disposed on a surface of the carrier particle , wherein:the carrier particle is flowable in a fluidized bed;the coating layer comprises a carbon nanotube which has a metal nanoparticle supported thereon and/or which has been doped with nitrogen or boron; andthe catalyst particle is flowable in a fluidized bed reaction.2. The carbon nanotube-coated catalyst particle of claim 1 , wherein the coverage of the coating layer comprising the carbon nanotube is 10% or more and 50% or less.3. The carbon nanotube-coated catalyst particle of claim 1 , wherein the carrier particle is a porous ceramic particle.4. The carbon nanotube-coated catalyst particle of claim 3 , wherein the porous ceramic particle includes at least one selected from the group consisting of alumina claim 3 , silica claim 3 , zeolite claim 3 , titanium oxide claim 3 , zirconia claim 3 , lanthanum oxide and ceria.5. The carbon nanotube-coated catalyst particle of claim 1 , wherein the metal nanoparticle includes at least one selected from the group consisting of ruthenium claim 1 , iron and nickel.6. A method of ammonia decomposition claim 1 , comprising decomposing ammonia using the carbon nanotube-coated catalyst particle of as an ammonia ...

Fluidized bed reactor and process for producing olefins from oxygenates

The present invention provides a fluidized bed reactor and its use for producing olefins from oxygenates, the fluidized bed reactor comprises: a reaction zone located in the lower portion of the fluidized bed reactor and comprising a lower dense phase zone and an upper riser, wherein the dense phase zone and the riser are connected with each other transitionally; a separation zone located in the upper portion of the fluidized bed reactor and comprising a settling chamber, a fast gas-solid separation means, a cyclone and a gas collecting chamber, wherein the riser extends upwardly into the separation zone and is connected at its outlet with the inlet of the fast gas-solid separation means, the fast gas-solid separation means is connected at its outlet with the inlet of the cyclone via a fast gas passage, the cyclone is connected at its outlet with the gas collecting chamber, and the gas collecting chamber is located below the reactor outlet and connected therewith; and a catalyst recycle line for recycling the catalyst from the settling chamber back to the dense phase zone, a catalyst withdrawl line for withdrawing the deactivated catalyst from the settling chamber and/or the dense phase zone to the catalyst regeneration means, and a catalyst return line for returning the regenerated catalyst from the catalyst regeneration means to the dense phase zone.

SYSTEM AND METHOD FOR PREPARING VANADIUM BATTERY HIGH-PURITY ELECTROLYTE

A system and method for preparing a vanadium battery high-purity electrolyte, comprising preparing a low-valence vanadium oxide with a valence of 3.5 with liquid phase hydrolysis and fluidization reduction with vanadium oxytrichioride, adding clean water and sulfuric acid for dissolution, and further performing ultraviolet activation to obtain the vanadium electrolyte, for use in an all-vanadium redox flow battery stack. The high-temperature tail gas in the reduction fluidized bed is combusted for preheating the vanadium powder material, to recover the sensible heat and latent heat of the high-temperature tail gas, and the sensible heat of the reduction product is recovered through heat transfer between the reduction product and the fluidized nitrogen gas. An internal member is arranged in the reduction fluidized bed to realize the precise regulation of the valence state of the reduction product, and ultraviolet is used to activate the vanadium ions, improving the activity of the electrolyte. 14. A system for preparing a vanadium battery high-purity electrolyte , comprising a vanadium oxytrichloride storage tank , a liquid phase hydrolysis device , a vanadium pentoxide feeding device , a preheating system () , a reduction fluidized bed , a combustion chamber , a cooling system , a secondary cooling system , a low-valence vanadium oxide feeding device , a dissolution reactor and an activation device;wherein the liquid phase hydrolysis device comprises a liquid phase hydrolysis reaction tank and a washing filter;the vanadium pentoxide feeding device comprises a vanadium pentoxide hopper and a vanadium pentoxide screw feeder;the preheating system comprises a venturi preheater, a primary cyclone preheater, a secondary cyclone preheater and a bag-type dust collector;the reduction fluidized bed comprises a feeder, a bed body, a discharger, a gas heater, a gas purifier and a first cyclone separator;the cooling system comprises a venturi cooler, a cyclone cooler and a ...

A SYSTEM AND METHOD FOR PRODUCING HIGH-PURITY AND HIGH-ACTIVITY VANADIUM ELECTROLYTE

A system and method for producing a high-purity and high-activity vanadium electrolyte, comprising converting high-purity vanadium oxytrichloride into an ammonium salt in a fluidized bed by gas phase ammoniation, then in another fluidized bed, reducing the ammonium salt into a low-valence vanadium oxide having an average vanadium valence of 3.5, adding clean water and sulfuric acid for dissolution, and further performing activation by ultrasound to obtain a 3.5-valence vanadium electrolyte which can be directly used in a new all-vanadium redox flow battery stack. The method of producing an ammonium salt containing vanadium in the fluidized bed by gas phase ammoniation is of short process and high efficiency. Precise regulation of the valence state of the reduction product is implemented by arranging an internal member in the reduction fluidized bed, and ultrasonication is used to activate the vanadium ion, thereby greatly improving the activity of the electrolyte. 1. A system for producing a high-purity and high-activity vanadium electrolyte , comprising a vanadium oxytrichloride storage tank , a gas phase ammoniation fluidized bed , a reduction fluidized bed , a pre-cooling device , a secondary cooling device , a low-valence vanadium oxide feeding device , a dissolution reactor , and an activation device;wherein the gas phase ammoniation fluidized bed comprises a vanadium oxytrichloride vaporizer, a purified ammonia liquor vaporizer, a chloride spray gun, a gas phase ammoniation fluidized bed body, a first cyclone separator, and an ammonium chloride settling tower;the reduction fluidized bed comprises a material valve, a bed body, a discharger, a gas heater, a gas purifier, and a second cyclone separator;the pre-cooling device comprises a cyclone cooler and a third cyclone separator;the low-valence vanadium oxide feeding device comprises a low-valence vanadium oxide hopper and a low-valence vanadium oxide screw feeder;wherein a feed outlet at the bottom of the ...

SYSTEM AND METHOD FOR PRODUCING 3.5-VALENCE HIGH-PURITY VANADIUM ELECTROLYTE

A system and method for producing a 3.5-valence high-purity vanadium electrolyte, comprising hydrolyzing high-purity vanadium oxytrichloride into vanadium pentoxide in a fluidized bed, and reducing vanadium pentoxide into a low-valence vanadium oxide having an average vanadium valence of 3.5 adding water and a sulfuric acid solution under a microwave field applied externally for dissolution at a low temperature, to obtain a 3.5-valence high-purity vanadium electrolyte. The preparation of vanadium pentoxide by means of gas-phase hydrolysis in the fluidized bed is of short process and high efficiency. By providing an internal member within the reduction fluidized bed, the precise regulation of the valence state of the reduction product is achieved, and the special chemical effect of the microwave field is used to promote dissolution of the vanadium oxide and activate the vanadium ions, thereby greatly improving the activity of the electrolyte. 1. A system for producing a 3.5-valence high-purity vanadium electrolyte , comprising a vanadium oxytrichloride storage tank , a gas phase hydrolysis fluidized bed , a vanadium pentoxide feeding device , a preheat dedusting device , a reduction fluidized bed , a primary cooling device , a secondary cooling device , a low-valence vanadium oxide feeding device , a dissolution and activation device a tail gas washing absorber , an induced draft fan and a chimney;wherein the gas phase hydrolysis fluidized bed comprises a vanadium oxytrichloride vaporizer, a clean water vaporize, a chloride spray gun a gas phase hydrolysis fluidized bed body, a hydrolysis fluidized bed discharger, and a hydrochloric acid tail gas absorber;the vanadium pentoxide feeding device comprises a vanadium pentoxide hopper and a vanadium pentoxide screw feeder;the preheat dedusting device comprises a venturi preheater, a first cyclone separator, a cyclone preheater, and a bag-type dust collector;the reduction fluidized bed comprises a feeder, a bed body, a ...

SYSTEM AND METHOD FOR PREPARING HIGH PURITY VANADIUM ELECTROLYTE

A system and method for preparing a high-purity vanadium electrolyte, comprising preparing a low-valence vanadium oxide with vanadium oxytrichloride by ammonium salt precipitation and fluidization reduction, and preparing the high-purity vanadium electrolyte at a low temperature by adding a sulfuric acid solution and clean water under the conditions of ultrasound-assisted dissolution and activation. Efficient utilization of heat is achieved through heat exchange between the ammonium salt and the reduction tail gas and heat exchange between the reduction product and fluidized nitrogen gas. Ammonia gas in the reduction tail gas is recovered for precipitation of vanadium to achieve the recycling of ammonia gas. An internal member is arranged in the reduction fluidized bed to realize the precise regulation of the valence state of the reduction product. Furthermore, ultrasound-assisted dissolution and activation are employed to prepare the vanadium electrolyte at a low temperature, thereby improving the activity of the electrolyte. 1. A system for preparing a high-purity vanadium electrolyte , comprising: a vanadium oxytrichloride storage tank , an ammonium salt precipitating device , an ammonium salt feeding device , a preheating system , a reduction fluidized bed , a cooling system , a secondary cooling device , a low-valence vanadium oxide feeding device , and a dissolution and activation reactor;wherein the ammonium salt precipitating device comprises an ammonium salt precipitating reaction tank and a washing filter;the ammonium salt feeding device comprises an ammonium salt hopper and an ammonium salt screw feeder;the preheating system comprises a primary cyclone preheater, a venturi preheater, a secondary cyclone preheater, and a first cyclone separator;the reduction fluidized bed comprises a feeder, a bed body, a discharger, a gas heater, a gas purifier, and an ammonium chloride settling tower;the cooling system comprises a venturi cooler, a cyclone cooler, and a ...