МНОГОСТУПЕНЧАТАЯ СЕПАРАТОРНАЯ ЕМКОСТЬ

Изобретение относится к химической промышленности и может быть использовано, в частности, для удаления мелких фракций катализатора из горячих регенерационных топочных газов блока жидкостного каталитического крекинга. Емкость 50 содержит стенку 86, в которой выполнено впускное отверстие 54 для загрязненного газового потока и выпускное отверстие 80b. Имеется также первичная ступень А циклонов, связанных по потоку с впускным отверстием 54 с первичной первой и второй трубными решетками 56а и 74а, перекрывающими внутреннее пространство, и первичное множество сепараторных циклонов 51, предназначенных для придания загрязненному газовому потоку центростремительного ускорения и для выгрузки частиц между соответствующими первичной первой и второй трубными решетками 56а и 74а. Каждый из циклонов имеет вертикальный корпус 62 с первым концом 58, прикрепленным к первой трубной решетке 56а, и со вторым концом 66. Первый конец 58 определяет впускное отверстие 60 циклона для приема загрязненного частицами ...

СПОСОБ ПРЕВРАЩЕНИЯ ОЛЕФИНА ИЛИ СПИРТА И СПОСОБ ПОЛУЧЕНИЯ ПРОПИЛЕНА ИЛИ АРОМАТИЧЕСКОГО СОЕДИНЕНИЯ

Изобретение относится к способу превращения олефина или спирта и способу получения пропилена или ароматического соединения. Способ превращения олефина или спирта включает этап предварительной обработки, в котором получают проводящий катализатор путем загрузки реактора с псевдоожиженным слоем непроводящим катализатором, содержащим цеолит и/или оксид кремния, и подачи нагретого углеводородного газа в реактор с псевдоожиженным слоем для осаждения углеродистого кокса и нанесения на непроводящий катализатор, и этап превращения олефина или спирта с помощью реакции в псевдоожиженном слое, в котором используют данный проводящий катализатор, где скорость подачи газа составляет 0,40 м/с или менее на стадии предварительной обработки в виде скорости потока газа в реакторе с псевдоожиженным слоем, и скорость подачи газа составляет 0,5 м/с или более на стадии превращения олефина или спирта в виде скорости потока газа в реакторе с псевдоожиженным слоем. Изобретение обеспечивает подавление электростатического ...

УСТАНОВКА ОБЕССЕРИВАНИЯ С УЛУЧШЕННЫМ КОНТАКТОМ ЖИДКОСТЬ/ТВЕРДАЯ ФАЗА

Установка для удаления серы из углеводородсодержащего потока текучей среды, содержащая реактор с псевдоожиженным слоем, который включает ряд разнесенных по вертикали усиливающих контакт элементов, расположенных горизонтально в реакционной зоне, где обессеривание усиливается улучшением контакта между углеводородсодержащим потоком текучей среды и поглощающими серу твердыми частицами. Согласно изобретению на упомянутой установке осуществляют способ обессеривания, включающий четыре стадии: контактирование углеводородсодержащего потока текучей среды с твердыми тонкодисперсными частицами сорбента; контактирование, по меньшей мере, части углеводородсодержащего потока и частиц сорбента с рядом дефлекторов; контактирование наполненных серой частиц сорбента с кислородсодержащим регенерирующим потоком; контактирование регенерированных частиц сорбента с водородсодержащим восстанавливающим потоком; дополнительно включена стадия контактирования указанных восстановленных частиц сорбента с углеводородсодержащим ...

СИСТЕМНЫЕ КОМПОНЕНТЫ СИСТЕМ РЕАКТОРА С ПСЕВДООЖИЖЕННЫМ КАТАЛИЗАТОРОМ

Группа изобретений относится к реакторным установкам для химической обработки, в частности к системе реактора с псевдоожиженным катализатором и системному компоненту системы реактора. Системный компонент содержит секцию отделения катализатора, содержащую стенки отделительной секции, образующие внутреннюю область секции отделения катализатора, выпускное отверстие для газа, отверстие стояка, отделительное устройство и выпускное отверстие для катализатора, стояк, проходящий через отверстие стояка секции отделения катализатора и содержащий основной внутренний сегмент стенки стояка, основной наружный сегмент стенки стояка и переходный сегмент стенки стояка, причем основной внутренний сегмент стенки стояка расположен по меньшей мере частично во внутренней области секции отделения катализатора и соединен по меньшей мере с переходным сегментом стенки стояка, а наружный сегмент стенки стояка расположен по меньшей мере частично за пределами секции отделения катализатора, и бак реактора, содержащий ...

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.

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 ...

СПОСОБ ПОЛУЧЕНИЯ ЛЕГКИХ ОЛЕФИНОВ ИЗ КИСЛОРОДСОДЕРЖАЩИХ СОЕДИНЕНИЙ И УСТАНОВКА ДЛЯ ЕГО ОСУЩЕСТВЛЕНИЯ

Предлагаемое изобретение относится к способу получения легких олефинов, представляющих собой этилен, пропилен или их смеси из кислородсодержащих соединений в реакторе, которые содержат по меньшей мере, один атом кислорода и от 1 до 10 атомов углерода, характеризующемуся тем, что включает следующие стадии: а) подачу сырьевого потока кислородсодержащих соединений через распределитель потока в реактор с флюидизированной зоной превращения кислородсодержащих соединений с катализатором, содержащим молекулярное сито ELAPO, контактирование кислородсодержащих соединений с катализатором с целью получения смеси, содержащей легкие олефины, диолефины, непрореагировавшие кислородсодержащие соединения и другие побочные продукты; b) отделение непрореагировавших кислородсодержащих соединений и диолефинов от легких олефинов и побочных продуктов и с) возврат непрореагировавших кислородсодержащих соединений и диолефинов на вход в реактор, отдельно от сырьевого потока кислородсодержащих соединений. Также изобретение ...

СПОСОБ ПРЕВРАЩЕНИЯ КИСЛОРОДСОДЕРЖАЩИХ СОЕДИНЕНИЙ В ОЛЕФИНЫ И УСТРОЙСТВО ДЛЯ ЕГО ОСУЩЕСТВЛЕНИЯ

Изобретение относится к способу превращения кислородсодержащих соединений, имеющих по меньшей мере от 1 до 10 атомов углерода в олефины, характеризующемуся тем, что включает следующие стадии: а) контактирование в реакторе кислородсодержащих соединений с флюидизированным катализатором, содержащим ELAPO, с превращением указанных соединений в углеводороды, причем в реакторе имеются, по меньшей мере две зоны: первая зона, в которой газ движется с большей скоростью, чем во второй зоне, в которой газ движется с меньшей скоростью, и b) введение продувочного газа, содержащего некоторое количество инертного газа, во вторую зону отдельно от сырьевого потока. Также изобретение относится к устройству для осуществления настоящего способа. Применение настоящего изобретения позволяет предотвратить накопление нежелательных побочных продуктов в застойных зонах внутри реактора и уменьшает количество кокса, осажденного на катализаторе в застойных зонах или на поверхности внутри этих зон. 2 н. и 6 з.п. ф-лы ...

УСТРОЙСТВА ДЛЯ ОСАЖДЕНИЯ ЧАСТИЦ

Группа изобретений относится к устройству и способу осаждения клеток или частиц и может быть использовано для отделения мелких частиц от основной жидкости в различных областях, таких как выращивание культур клеток (микробов, млекопитающих, растений, насекомых или водорослей), отделение частиц твердого катализатора от жидкости или газа и очистка сточных вод. Осадительное устройство содержит верхний (503А) и нижний (503В) конический участки, имеющие по меньшей мере один порт, цилиндрический участок (508), стопку конусов (509), расположенную внутри осадительного устройства, и диффузор (570), расположенный внутри осадительного устройства. Каждый конус в стопке конусов имеет малое отверстие и большое отверстие, при этом малое отверстие ориентировано к одному из верхнего конического участка и нижнего конического участка, причем указанная стопка конусов центрирована вокруг продольной оси осадительного устройства. Диффузор содержит трубчатый стержень, соединенный с портом, выбранным из по меньшей ...

СПОСОБ ДЕГИДРИРОВАНИЯ ЭТИЛБЕНЗОЛА ДО СТИРОЛА

Использование: получение углеводородов. Сущность: проводят дегидрирование этилбензола в системе, содержащей реактор с псевдоожиженным слоем и регенератор, с использованием катализатора на основе оксида железа, нанесенного на модифицированный кремнием оксид алюминия и содержащего промоторы, представляющие собой дополнительные оксиды металлов. Технический результат: упрощение технологии. 17 з.п.ф-лы, 3 табл., 1 ил.

СИСТЕМА И СПОСОБ ПОЛУЧЕНИЯ ВАНАДИЕВОГО ЭЛЕКТРОЛИТА ВЫСОКОЙ ЧИСТОТЫ

Изобретение относится к области электротехники, а именно к системе и способу получения ванадиевого электролита высокой чистоты, который затем используется в проточном редокс-аккумуляторе. Способ включает получение оксида ванадия низкой валентности из окситрихлорида ванадия, выступающего в качестве исходного материала, путем осаждения аммонийной соли, восстановления в псевдоожиженном слое и получения ванадиевого электролита высокой чистоты при низкой температуре путем добавления раствора серной кислоты и чистой воды с растворением и активацией в условиях воздействия ультразвука. Эффективное использование тепла достигается путем теплообмена между аммонийной солью и восстановительным отходящим газом и за счет теплообмена между продуктом восстановления и псевдоожиженным газообразным азотом. Газообразный аммиак в восстановительном отходящем газе восстанавливают для осаждения ванадия с целью обеспечения повторного использования газообразного аммиака. Внутренний элемент введен в псевдоожиженный ...

УСТРОЙСТВО ДЛЯ МОДИФИКАЦИИ КАТАЛИЗАТОРА НА ОСНОВЕ МОЛЕКУЛЯРНОГО СИТА И СПОСОБ

Изобретение относится к устройствам и к их использованию. Описан способ модификации катализатора на основе молекулярного сита в устройстве для модификации катализатора на основе молекулярного сита, включающий введение катализатора на основе молекулярного сита, на основе молекулярного сита HZSM-5 и HZSM-11 и модификатора в модифицирующий блок, соответственно, через питающий блок, причем катализатор модифицируют посредством модификатора в модифицирующем блоке и затем выпускают в охлаждающий блок для охлаждения до температуры, составляющей менее чем 50°C, и затем охлаждаемый модифицированный катализатор перемещают в любое устройство для хранения, причем модификацию осуществляют в атмосфере инертного газа при температуре в диапазоне от 150 до 600°C в течение времени модификации в диапазоне от 0 до 10 ч; модификатор представляет собой по меньшей мере один модификатор, выбранный из фосфорного реагента, силилирующего реагента и толуола. Технический результат - возможность применения способа модификации ...

ЦИРКУЛЯЦИОННЫЙ РЕАКТОР КИСЛОРОДНОГО СЖИГАНИЯ С ПСЕВДООЖИЖЕННЫМ СЛОЕМ И СПОСОБ ЭКСПЛУАТАЦИИ ТАКОГО РЕАКТОРА

Группа изобретений относится к реакторам кислородного сжигания с псевдоожиженным слоем и их эксплуатации и обеспечивает при ее использовании снижение содержания диоксида углерода при сжигании углеродсодержащих топлив. Указанный технический результат достигается при осуществлении способа эксплуатации циркуляционного реактора кислородного сжигания с псевдоожиженным слоем, содержащего камеру (15) реактора и газораспределительное устройство (50), предусмотренное в нижней секции камеры реактора для введения газа в камеру реактора, причем газораспределительное устройство содержит первую систему (70) подачи газа и вторую систему (75) подачи газа для введения газа, обогащенного кислородом, в камеру (15) реактора. Первая система (70) подачи газа содержит первую дутьевую камеру (71), а вторая система (75) подачи газа содержит вторую дутьевую камеру (80), и при этом первая дутьевая камера имеет общую стенку (77) с камерой реактора, а вторая дутьевая камера, расположенная под первой дутьевой камерой ...

СПОСОБ АДСОРБЦИОННОЙ ДЕСУЛЬФУРИЗАЦИИ УГЛЕВОДОРОДОВ И РЕАКТОРНОЕ УСТРОЙСТВО ДЛЯ ЕГО ОСУЩЕСТВЛЕНИЯ

... 1. Воздушный классификатор частиц, включающий:герметично закрытый сверху основной блок классификатора, выпускное отверстие, выпускной трубопровод и, по меньшей мере, одно направляющее входное отверстие;внутреннее пространство основного блока классификатора, включающее, сверху вниз, зону в виде прямой трубы и коническую зону, при этом коническое основание конической зоны соединено с зоной в виде прямой трубы;выпускное отверстие, расположенное в нижней части конической зоны;направляющее входное отверстие, расположенное в верхней части зоны в виде прямой трубы в тангенциальном направлении зоны в виде прямой трубы и соединенное с внутренним пространством основного блока классификатора;выпускной трубопровод, герметично встроенный в верхнюю часть основного блока классификатора и продолжающийся вниз до нижней части зоны в виде прямой трубы, при этом указанный выпускной трубопровод имеет герметично закрытый нижний конец;где нижняя часть выпускного трубопровода выполнена, по меньшей мере, с одним ...

СПОСОБ И УСТРОЙСТВО ДЛЯ ПОЛУЧЕНИЯ ВИНИЛХЛОРИДА

... 1. Способ получения винилхлорида, включающий: ! подачу газообразного хлора и этана к области реакции хлорирования этана, расположенной в нижней части реактора пиролиза, в которой присутствуют твердые частицы; ! проведение реакции хлорирования этана при контакте газообразного хлора и этана с твердыми частицами таким образом, что продукт реакции хлорирования этана и твердые частицы поднимаются в верхнюю часть реактора пиролиза одновременно, при этом образовавшийся кокс оседает на твердых частицах; ! проведение реакции пиролиза в области реакции пиролиза, расположенной в верхней части реактора пиролиза, при контакте продукта реакции хлорирования этана с твердыми частицами таким образом, что продукт реакции хлорирования этана и твердые частицы поднимаются одновременно, при этом образовавшийся кокс оседает на твердых частицах; ! разделение твердых частиц, полученных при реакции пиролиза, и продукта реакции пиролиза в сепараторе; ! перемещение отделенных твердых частиц к реактору регенерации ...

СЕПАРАТОРНАЯ СИСТЕМА ЛИФТ-РЕАКТОРА

Группа изобретений относится к устройствам и способам для сепарации газообразной смеси от потока частиц. Устройство содержит реакционную и сепараторную емкости. Реакционная емкость содержит находящуюся снизу область размещения отпарного слоя и находящуюся сверху область размещения вторичного сепаратора. Сепараторная емкость содержит чередующиеся сепараторную и собирающую камеры, распределенные в осевом направлении вокруг центрального лифт-реактора вблизи выпускного отверстия центрального лифт-реактора. Каждая сепараторная камера содержит две вертикальные боковые стенки, которые также содержат стенку смежной собирающей камеры, впускное отверстие сепараторной камеры, дефлектор сепараторной камеры. По меньшей мере одна из вертикальных боковых стенок каждой камеры содержит боковое выпускное отверстие. Каждая собирающая камера содержит внешнюю стенку собирающей камеры, которая содержит входное окно отпарного газа, пол собирающей камеры, который вместе с внешней стенкой собирающей камеры, указанными ...

КОНТРОЛЬ ТЕМПЕРАТУРЫ РЕАКТОРА АММОКСИДИРОВАНИЯ

СПОСОБ ПОЛУЧЕНИЯ РАСПЛАВЛЕННОГО ЧУГУНА И УСТАНОВКА ДЛЯ ПОЛУЧЕНИЯ РАСПЛАВЛЕННОГО ЧУГУНА

... 1. Установка для получения расплавленного чугуна, содержащая: ! по меньшей мере один реактор восстановления с псевдоожиженным слоем, в котором восстанавливают мелкодисперсную железную руду и превращают эту мелкодисперсную железную руду в восстановленное железо; ! бункер для загрузки мелкодисперсной железной руды, из которого подают мелкодисперсную железную руду в реактор восстановления с псевдоожиженным слоем; ! линию для загрузки мелкодисперсной железной руды, которая непосредственно соединяет бункер для загрузки мелкодисперсной железной руды с каждым из реакторов восстановления с псевдоожиженным слоем, и через которую непосредственно загружают мелкодисперсную железную руду в каждый из реакторов восстановления с псевдоожиженным слоем; ! плавильную печь-газификатор, в которую загружают кусковые углеродсодержащие материалы и восстановленное железо и подают кислород, при этом в плавильной печи-газификаторе получают расплавленный чугун; и ! линию подачи восстановительного газа, по которой ...

УСТАНОВКА ДЛЯ ПОЛУЧЕНИЯ РАСПЛАВЛЕННОГО ЧУГУНА

... 1. Установка для получения расплавленного чугуна, включающая: ! по меньшей мере один реактор восстановления с псевдоожиженным слоем, в котором восстанавливают железную руду и придают ей пластичность, и превращают эту железную руду в восстановленные материалы; ! плавильную печь-газификатор, в которую загружают восстановленную руду и вводят кислород, и в плавильной печи-газификаторе изготавливают расплавленный чугун и ! линию подачи восстановительного газа, по которой подают восстановительный газ, выходящий из плавильной печи-газификатора, в реактор восстановления с псевдоожиженным слоем, ! где реактор восстановления с псевдоожиженным слоем включает циклон, который установлен в этом реакторе восстановления с псевдоожиженным слоем для того, чтобы собирать мелкодисперсную железную руду, и ! где к циклону присоединен газовый инжектор, с помощью которого предотвращают слипание мелкодисперсной руды путем введения углеродсодержащего газа. ! 2. Установка по п.1, в которой газовый инжектор присоединен ...

СПОСОБ И УСТРОЙСТВО ДЛЯ ХИМИЧЕСКОГО ЦИКЛИЧЕСКОГО СЖИГАНИЯ (CLC)ХЦС С ПОЛУЧЕНИЕМ АЗОТА ВЫСОКОЙ СТЕПЕНИ ЧИСТОТЫ

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 получения полиолефинов

VERFAHREN UND VORRICHTUNG ZUM TRENNEN VON SUSPENSIONEN AUS KATALYSATORTEILCHEN UND GASFOERMIGEN KOHLENWASSERSTOFFEN UND ZUM ABSTREIFEN VON KOHLENWASSERSTOFFEN VON DEN KATALYSATORTEILCHEN

Verfahren zur Einstellung einer zirkulierenden Wirbelschicht und Verwendung des Verfahrens

In this process, at least part of the pure gas stream discharged from the cyclone (2) is used as at least part of the carrier gas at least in one spot of the circulating fluidised bed, the pure gas used as part of the carrier gas is mixed in an injector mixer (8) with 10 to 90 wt % propellant gas, relative to the volume of the pure gas stream discharged from the cyclone (2), before the supply line into the circulating fluidised bed, and the mixture is supplied as carrier gas to the circulating fluidised bed.

VERFAHREN ZUR KATALYTISCHEN UMWANDLUNG VON KOHLENWASSERSTOFFEN

CLOSED REACTOR FCC SYSTEM WITH PROVISIONS FOR SURGE CAPACITY

Verfahren zur Herstellung von Acrylsaeurenitril und Methacrylsaeurenitril durch Umsetzung von Propylen oder Isobutylen mit Sauerstoff und Ammoniak

Support system for high temperature fluid solid cyclones and plenum

Each of a plurality of cyclones is suspended from the roof of a vessel by means of tubular extensions of their barrels. These tubular extensions are slotted lengthwise to minimize thermal stresses in the vessel head. Importantly, this hanging scheme provides a direct extension within the load path for the cyclone weight, thus supporting the cyclone in tension stresses rather than high bending stresses.

FLUIDIZABLE CATALYST REGENERATION PROCESS AND APPARATUS

APPARATUS AND PROCESS FOR THE SEPARATION OF FLUID CRACKING CATALYST PARTICLES FROM GASEOUS HYDROCARBONS

An improved process for the separation of powdered material from gases

In a process for regenerating powdered solid catalysts used in a hydrocarbon cracking process, the catalyst particles are burnt with an oxidizing gas and the regenerated particles are removed from the gases by passing them through a cyclone separator, a Cottrell precipitator and an oil-scrubbing zone, the vaporized oil in the regeneration gases then being condensed and recovered by passing them through a waterscrubbing zone (see Group XII).

OPERATING FLUIDIZED BED REACTOR

Fluidized Catalyst Reactor.

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

Oxycombustion in transport oxycombustor

Oxycombustion in transport oxycombustor

VERFAHREN ZUM AUSBRINGEN VON FEINTEILCHENFÖRMIGEM MATERIAL AUS EINEM WIRBELBETT

PROCEDURE AND DEVICE FOR SEPARATING FINE SOLID PARTICLES FROM FLOWING GASES

DEVICE FOR BURNING THE INFLAMMABLE COMPONENTS OF WASTE, IN PARTICULAR SEWAGE MUD

VERFAHREN UND VORRICHTUNG ZUR BEHANDLUNG EINES FEINTEILCHENFÖRMIGEN, INSBESONDERE METALLHALTIGEN, EINSATZMATERIALES

CONTINUOUS MASS PRODUCTION OF CARBON NANO-TUBES IN A NANO-AGGLOMERATE FLUIDISED BED

IMPROVED DEEP CATALYTIC CRACKING PROCEDURE

VERFAHREN UND EINRICHTUNG ZUM RÜCKFÜHREN EINES AUS EINEM REAKTORGEFÄSS MIT EINEM GAS AUSGETRAGENEN FEINTEILIGEN FESTSTOFFES

PROCEDURE AND DEVICE FOR A THERMAL TREATMENT IN A FLUID BED

PROCEDURE AND MECHANISM FOR RECONDUCTING A FROM A REACTOR CONTAINER WITH A GAS DELIVERING PURIFY-HASTY SOLID

CYCLONE FOR THE CENTRIFUGAL SEPARATION OF A MIXTURE FROM GAS AND SOLID PARTICLE WITH HEAT RECOVERY

VERFAHREN UND VORRICHTUNG ZUR BEHANDLUNG EINES FEINTEILCHENFÖRMIGEN, INSBESONDERE METALLHALTIGEN, EINSATZMATERIALES

VERBESSERTES WIRBELSCHICHTREAKTORSYSTEM

The invention relates to a fluidized bed reactor system consisting of at least two fluidized bed reactors, comprising a first and a second reactor (1, 2), which are each designed as a circulating fluidized bed, a particle line (7) comprising a particle separator (3) for transporting fluidized bed particles from the first into the second reactor, and a particle line (17) leading out in the lower half of the second reactor (2) for transporting fluidized bed particles back into the first reactor (1), characterized in that, at least in the second reactor (2), reaction zones (9, 10, 22) that are separated from one another by one or more flow regulators (18, 21) are provided, and the particle line (7) opens into the second reactor (2) above at least one flow regulator (18).

Wirbelschichtreaktorsystem

The invention relates to a fluidised bed reactor system comprising one or more fluidised bed reactors (1, 2, 20) for carrying out chemical or physical reactions, at least one reactor thereof being in the form of a rapidly fluidised reactor to be operated as a circulating fluidised bed and comprising, at the upper end, a fluid outlet (5, 6), a particle separator (3, 4), and a particle line (7, 8) connected thereto for the purpose of feeding back separated fluidised bed particles into the same or a further reactor. In at least one rapidly fluidised reactor, one or more flow control devices (18, 21) are provided so as to produce reaction zones (9, 10, 22) that are separate from one another, said invention being characterised in that in order to control the flow conditions into said reaction zones (9, 10, 22), one or more of these flow control devices (18, 21) is/are specifically adjustable from outside of the system.

VERBESSERTES WIRBELSCHICHTREAKTORSYSTEM

BELUFTETES TUBING.

DEVICE FOR THE SEPARATION OF CELEBRATIONS PARTICLES FROM A GASEOUS EFFUSION.

PROCEDURE FOR THE PYROLYSIS OF CARBON-CONTAINING FEEDS

PROCEDURE AND DEVICE FOR STRIPPING

PROCEDURE AND DEVICE FOR THE POLYMERIZATION OF ETHYLS

DEVICE WITH A CIRCULATING FLUIDISED BED FOR CHEMICAL AND PHYSICAL PROCESSES

PROCEDURE AND DEVICE FOR CONTACTING GASES AND SOLID PARTICLES IN FLUIDISED BEDS

Procedure for the production of things from high-molecular, thermoplastic polycarbonates with roughened up, matte surfaces

CONTINUOUS GASEOUS PHASE PROCEDURE FOR THE COATING OF POLYMERIZATION CATALYSTS

VЕRFАНRЕN ZUМ АUSВRINGЕN VОN FЕINТЕILСНЕNFÖRМIGЕМ МАТЕRIАL АUS ЕINЕМ WIRВЕLВЕТТ

VЕRFАНRЕN ZUМ АUSВRINGЕN VОN FЕINТЕILСНЕNFÖRМIGЕМ МАТЕRIАL АUS ЕINЕМ WIRВЕLВЕТТ

VЕRFАНRЕN ZUМ АUSВRINGЕN VОN FЕINТЕILСНЕNFÖRМIGЕМ МАТЕRIАL АUS ЕINЕМ WIRВЕLВЕТТ

VЕRFАНRЕN ZUМ АUSВRINGЕN VОN FЕINТЕILСНЕNFÖRМIGЕМ МАТЕRIАL АUS ЕINЕМ WIRВЕLВЕТТ

VЕRFАНRЕN ZUМ АUSВRINGЕN VОN FЕINТЕILСНЕNFÖRМIGЕМ МАТЕRIАL АUS ЕINЕМ WIRВЕLВЕТТ

VЕRFАНRЕN ZUМ АUSВRINGЕN VОN FЕINТЕILСНЕNFÖRМIGЕМ МАТЕRIАL АUS ЕINЕМ WIRВЕLВЕТТ

VЕRFАНRЕN ZUМ АUSВRINGЕN VОN FЕINТЕILСНЕNFÖRМIGЕМ МАТЕRIАL АUS ЕINЕМ WIRВЕLВЕТТ

VЕRFАНRЕN ZUМ АUSВRINGЕN VОN FЕINТЕILСНЕNFÖRМIGЕМ МАТЕRIАL АUS ЕINЕМ WIRВЕLВЕТТ

VЕRFАНRЕN ZUМ АUSВRINGЕN VОN FЕINТЕILСНЕNFÖRМIGЕМ МАТЕRIАL АUS ЕINЕМ WIRВЕLВЕТТ

VЕRFАНRЕN ZUМ АUSВRINGЕN VОN FЕINТЕILСНЕNFÖRМIGЕМ МАТЕRIАL АUS ЕINЕМ WIRВЕLВЕТТ

VЕRFАНRЕN ZUМ АUSВRINGЕN VОN FЕINТЕILСНЕNFÖRМIGЕМ МАТЕRIАL АUS ЕINЕМ WIRВЕLВЕТТ

TURBULENT FLUID BED PARAFFIN CONVERSION PROCESS

FCC CATALYST STRIPPING METHOD AND APPARATUS

Fluidized bed reactor system

The invention relates to a fluidized bed reactor system consisting of at least two fluidized bed reactors, comprising a first and a second reactor (1, 2), which are each designed as a circulating fluidized bed, a particle line (7) comprising a particle separator (3) for transporting fluidized bed particles from the first into the second reactor, and a particle line (17) leading out in the lower half of the second reactor (2) for transporting fluidized bed particles back into the first reactor (1), characterized in that, at least in the second reactor (2), reaction zones (9, 10, 22) that are separated from one another by one or more flow regulators (18, 21) are provided, and the particle line (7) opens into the second reactor (2) above at least one flow regulator (18).

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).

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

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

Process for preparing ethylene and/or propylene

The present invention provides a process for preparing ethylene and/or propylene, wherein oxygenates and olefins are converted to ethylene and/or propylene over a zeolite-comprising catalyst, comprising the steps of: a) reacting in a first reactor an oxygenate feed over the zeolite-comprising catalyst at a temperature in the range of from 350 to 1000 °C and retrieving from the first reactor a first reactor effluent stream comprising gaseous products, including ethylene and/or propylene, and zeolite-comprising catalyst; b) reacting in a second reactor an olefin feed over the zeolite-comprising catalyst at a temperature in the range of from 500 to 700 °C and retrieving from the second reactor a second reactor effluent stream comprising gaseous products, including ethylene and/or propylene, and zeolite-comprising catalyst; c) providing the first and second reactor effluent stream to one or more gas/solid separators to retrieve zeolite-comprising catalyst from the first and second reactor effluent ...

Process for converting a solid biomass material

A process for converting a solid biomass material, comprising contacting the solid biomass material with a catalytic cracking catalyst at a temperature of more than 400°C in a riser reactor to produce one or more cracked products, wherein the riser reactor comprises: - a riser reactor pipe, which riser reactor pipe has a diameter that increases in a downstream direction; and - a bottom section, which bottom section has a larger diameter than the riser reactor pipe; and wherein the solid biomass material is supplied to the riser reactor in the bottom section.

System and method for producing 3.5-valent highly pure vanadium electrolyte

A system and method for producing a 3.5-valent highly pure vanadium electrolyte: use a fluidized bed (2) to hydrolyze highly pure vanadium oxytrichloride to vanadium pentoxide by means of gas-phase hydrolysis, accurately control the reduction of vanadium pentoxide in a reducing fluidized bed (5) to a low-valent vanadium oxide with an average vanadium valence state at 3.5, and under an externally applied microwave field, add water and a sulfuric acid solution to dissolve at a low temperature to obtain a 3.5-valent highly pure vanadium electrolyte, which can be directly used in new piles of vanadium redox flow batteries. The preparation of vanadium pentoxide by means of gas-phase hydrolysis by using the fluidized bed (2) has a short flow and high efficiency. By providing an internal member within the reducing fluidized bed (5), the accurate regulation of the valence state of reduction products may be achieved. The special chemical effect of the microwave field promotes dissolution of vanadium ...

CLC method and facility with production of high-purity nitrogen

The invention relates to a CLC method, and the facility for same, producing high-purity dinitrogen, comprising: (a) combustion of a hydrocarbon feedstock by reduction of an oxidation-reduction active mass placed in contact with the feedstock, (b) a first oxidation step of the reduced active mass (25) from step (a) in contact with a fraction of a depleted stream of air (21b) in order to produce a high-purity stream of dinitrogen (28) and a stream of partially re-oxidised active mass (26); (c) a second oxidation step of the active mass stream (26) in contact with air (20) to produce the depleted air stream and the re-oxidised active mass stream (24) intended to be used in step (a); (d) dividing the depleted air stream from step (c) in order to form the depleted air fraction used in step (b) and a complementary depleted air fraction extracted from the CLC.

Turbulent fluidized-bed reactor, device, and method using oxygen-containing compound for manufacturing propene and C4 hydrocarbon

Provided are a turbulent fluidized-bed reactor, device, and method using an oxygen-containing compound for manufacturing propene or a C4 hydrocarbon. The device comprises a turbulent fluidized-bed reactor and a fluidized-bed regenerator for regenerating a catalyst. The method comprises: a) directing raw material of an oxygen-containing compound from n reactor feed distributors into a reaction area of a turbulent fluidized-bed reactor to contact with a catalyst, then generating a material flow comprising a target product and a carbon-containing catalyst to be regenerated; b) sending the material flow comprising the target product discharged from the turbulent fluidized-bed reactor into a product separation system, and separating to obtain various fractions such as propene, a C4 hydrocarbon, a light fraction, and the like, then returning, by using the reactor feed distributor at the bottom-most portion of the turbulent fluidized-bed reactor, at least 70 weight percent of the light fraction ...

CYCLONE FOR SEPARATING CATALYST PARTICLES FROM GASEOUS HYDROCARBONS

Method and apparatus for processing magnetite

C:\Interwovn\NRPortbl\DCC\TXB132475_l.docx-l/08/2019 35526281 An apparatus for processing magnetite iron ore, including a screen arranged to send oversize material to a regrind mill and undersize material to a high grade concentrate thickener and includes a CCD thickener type system for product grade improvements.

Method and apparatus for processing magnetite

An apparatus for processing magnetite iron ore, including an upstream cyclone and a mill for grinding particles, wherein the upstream cyclone is arranged to operate as a splitter by diverting material in an overflow of the upstream cyclone to bypass the mill and by feeding material in an underflow of the upstream cyclone to the mill.

Process for treating a material containing metal and organic matter, including metal separation

Continuous slurry polymerization volatile removal

Underflow cyclone with perforated barrel

Method and assembly for separating solids from a gaseous phase

REACTION CHAMBER

METHOD FOR IMPROVING THE OPERATION OF A FLUIDIZED BED

SEPARATION OF FLUE GAS FROM REGENERATED CATALYST

CONTINUOUS VOLATILE REMOVAL IN SLURRY POLYMERIZATION

A process/apparatus is disclosed for continuously separating a liquid medium comprising diluent and unreacted monomers from a polymerization effluent comprising diluent, unreacted monomers and polymer solids, comprising a continuous discharge of the polymerization effluent from a slurry loop reactor (1) through a discharge valve (8b) and transfer conduit (9) into a first intermediate pressure flash tank (11) with a conical bottom defined by substantially straight sides inclined at an angle to that of horizontal equal to or greater than the angle of slide of the slurry/polymer solids and an exit seal chamber (17) of such diameter (d) and length (1) as to maintain a desired volume of concentrated polymer solids/slurry in the exit seal chamber (17) such as to form a pressure seal while continuously discharging a plug flow of concentrated polymer solids/slurry bottom product of said first flash tank (11) from the exit seal chamber (17) through a seal chamber exit reducer with inclined sides ...

CLOSED CYCLONE FCC SYSTEM WITH PROVISIONS FOR SURGE CAPACITY

DEVICE AND PROCEDURE FOR SEPARATING LIQUID PRODUCTS FROM A SUSPENSION PRODUCED BY A FISCHER-TROPSCH REACTOR AND IN THE PRESENCE OF A DILUENT

L'invention concerne un procédé de séparation de produits liquides à partir d'une suspension issue d'un réacteur Fischer-Tropsch et contenant au moins un catalyseur Fischer-Tropsch, et un dispositif de séparation desdits produits liquides comprenant au moins un moyen permettant d'extraire d'un réacteur Fischer-Tropsch, une partie d'une suspension contenant au moins un catalyseur Fischer-Tropsch, au moins un moyen permettant d'ajouter un diluant à tout ou partie de la suspension extraite via le moyen, au moins un moyen de séparation primaire muni d'au moins un moyen permettant d'amener la suspension diluée vers ledit ou lesdits moyens de séparation, d'au moins un moyen permettant de recueillir le liquide séparé, et d'au moins un moyen permettant de recueillir une suspension plus concentrée, et au moins un moyen de séparation secondaire permettant de séparer puis recueillir via au moins un moyen un liquide essentiellement épuré.

DEVICE AND PROCEDURE FOR SEPARATING LIQUID PRODUCTS FROM A SUSPENSION CONTAINING A SOLID AND IN THE PRESENCE OF A DILUENT

L'invention concerne un procédé de séparation de produits liquides à partir d'une suspension issue d'un réacteur multiphasique contenant au moins un solide, et un dispositif de séparation desdits produits liquides comprenant au moins un moyen permettant d'extraire d'un réacteur, une partie d'une suspension contenant un solide; au moins un moyen permettant d'ajouter un diluant à tout ou partie de la suspension extraite via le ou les moyen(s); au moins un moyen de séparation primaire muni d'au moins un moyen permettant d'amener tout ou partie de la suspension diluée vers ledit ou lesdits moyens de séparation, d'au moins un moyen permettant de recueillir le liquide séparé, et d'au moins un moyen permettant de recueillir une suspension plus concentrée; au moins un moyen de séparation secondaire permettant de séparer puis recueillir via au moins un moyen un liquide essentiellement épuré.

PROCESS FOR THE DEHYDROGENATION OF ETHYLBENZENE TO STYRENE

A process is described for the dehydrogenation of ethylbenzene to styrene in a fluid-bed reactor-regenerator system, which uses a catalyst based on iron oxide supported on a modified alumina and promoted with further metal oxides.

APPARATUS AND PROCESS FOR MINIMIZING CATALYST RESIDENCE TIME IN A REACTOR VESSEL

We have discovered a way to minimize the time that catalyst and gaseous products are in contact after exiting the discharge opening (22) of a reactor conduit (10). The reactor conduit discharges into a disengaging chamber (24) that is directly connected to a separator (32). A dipleg (34) of the separator is directly connected to the disengaging chamber or to an intermediate chamber (64) which is in direct communication with the disengaging chamber. Accordingly, catalyst never gets a chance to become entrained in the large open volume of the reactor vessel. Consequently, catalyst which makes it out of the disengaging chamber is quickly returned back to the disengaging chamber, thereby minimizing the time that catalyst and product gases are in contact after being discharged from the reactor conduit.

THE SEPARATOR OF SOLID PARTICLES FROM STEAM-GAS MIXTURE

The present invention is related to the separator (dust chamber) for separating solid particles from vapour-gas mixture, particularly to the structure of the dust chamber belonging amongst installation of the plant processing the fossil fuels or materials containing organic matter. The dust chamber (1) for separating solid particles from vapour-gas mixture comprises main body (2) with inner refractory lining (7) arranged to the inner surface of said main body, first and second stage cyclones (3, 4), lamella compensators (18, 19), dust removal conduits (5, 15) and inlet conduit (13) of the vapour-gas mixture into the first cyclone (3). The main body (2) of the dust chamber (1) is manufactured in all height from the cylinder of equal diameter and first and second stage cyclones (3, 4) are placed outside of the main body (2) of the dust chamber (1). For the refractory lining of the main body (2) of the dust chamber (1) and first and second stage cyclones (3, 4) the non-porous and wear proof ...

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.

Fluid Separation Systems And Methods

Systems and methods for separating particles from fluids are provided. The system comprises a vessel with a fluid inlet and a fluid outlet and a baffle assembly located within the vessel. The baffle assembly has a plurality of baffles that can provide a change in direction to fluid entering the vessel thereby separating particles. During shut-down of a polymerization reactor, reaction mixture is discharged to a separation system where polymer particles are removed from the mixture prior to being released into the atmosphere.

Process for the gas phase polymerisation of olefins

The present invention relates to a process for the gas phase polymerisation of olefins, and, in particular, to a process for the gas phase polymerisation of olefins with recycle of fines to the reaction zone.

Dual riser catalytic cracking process for making middle distillate and lower olefins

A dual riser catalytic cracking process for preferentially making middle distillate and lower olefins. The system and process provide for the processing of multiple hydrocarbon feedstocks so as to selectively produce middle distillate boiling range product and lower olefins. The system and process uses two riser reactors, a single vessel for separating the cracked product and cracking catalyst received from both riser reactors, and a regenerator for regenerating coked or spent cracking catalyst.

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.

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.

Recirculated-suspension pre-calciner system

A recirculated-suspension pre-calciner system is disclosed, comprising: a vortex cyclone dust collecting equipment including a plurality of devices, wherein a top device of the vortex cyclone dust collecting equipment is used as a feed system; a vertical combustion kiln; a blower; and a powder purge system, wherein powders in the feed system fall into the vortex cyclone dust collecting equipment and pass through a plurality of the devices to mix and exchange heat with flue gas comprising CO 2 , generating calcination reaction and releasing CO2 into the flue gas. and the steam is separated and transported to the feed system by the blower and acts as a carrier gas of powders.

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.

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.

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 ...

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 ...

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 ...

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.

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 ...

FLUID CATALYTIC CRACKING PROCESS AND APPARATUS FOR MAXIMIZING LIGHT OLEFIN YIELD AND OTHER APPLICATIONS

Apparatus and processes herein provide for converting hydrocarbon feeds to light olefins and other hydrocarbons. The processes and apparatus include, in some embodiments, feeding a hydrocarbon, a first catalyst and a second catalyst to a reactor, wherein the first catalyst has a smaller average particle size and is less dense than the second catalyst. A first portion of the second catalyst may be recovered as a bottoms product from the reactor, and a cracked hydrocarbon effluent, a second portion of the second catalyst, and the first catalyst may be recovered as an overhead product from the reactor. The second portion of the second catalyst may be separated from the overhead product, providing a first stream comprising the first catalyst and the hydrocarbon effluent and a second stream comprising the separated second catalyst, allowing return of the separated second catalyst in the second stream to the reactor. 1. A process for the conversion of hydrocarbons , comprising:feeding a mixture of first particles and second particles from a regenerator to a transport vessel or riser reactor, wherein the first particles have a smaller average particle size and/or are less dense than the second particles, and wherein the first particles and second particles may independently be catalytic or non-catalytic particles;feeding a reactive and/or non-reactive carrier fluid to the transport vessel or riser reactor;recovering an overhead product from the transport vessel/riser reactor comprising the carrier fluid and/or a reaction product of the carrier fluid, the second particles, and the first particles; a housing;', 'a solids separation device disposed within the housing for separating the second particles from the overhead product to provide a first stream, comprising the first particles and the carrier fluid and/or a reaction product of the carrier fluid, and a second stream, comprising the separated second particles;', 'one or more cyclones disposed within the housing for ...

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 ...

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 ...

DEVICE FOR GAS SOLIDS FLUIDIZED SYSTEM TO ENHANCE STRIPPING

A device for the intimate mixing of solid particles and a gaseous medium within a gas-solid fluidized bed, comprising a plurality corrugated and/or ribbed planar stanchions arranged in alternating intersecting planes that provide a plurality of open spaces between or adjacent the alternating intersecting planar stanchions. The element has a three-dimensional lattice configuration and the corrugated and/or ribbed planar stanchions are formed from metal having peaks and valleys or ribs, such that the peaks and valleys or ribs are angled at less than 90 degrees from the fall-line of the planar stanchion when assembled into the element. The angled peaks and valleys or ribs form channels that enhance lateral movement of catalyst particles into the spaces between the stanchions to provide improved vapor/solids mixing and contact. 1. A gas-solid fluidized bed comprising: a vessel having a shell and an open internal region within the shell; at least one ripple packing element positioned within the open internal region and comprising a plurality corrugated and/or ribbed planar stanchions arranged in alternating intersecting planes that provide a plurality of open spaces between or adjacent the alternating intersecting planar stanchions , the ripple packing element having a three-dimensional lattice configuration; solid particles within the ripple packing element; and at least one gas stream flowing counter-currently to the solid particles through the ripple packing element and causing fluidization of the solid particles within the ripple packing element to form the gas-solid fluidized bed.2. The gas-solid fluidized bed of claim 1 , wherein the corrugated planar stanchions comprise peaks and valleys arranged longitudinally or laterally or a combination of both.3. The gas-solid fluidized bed of claim 2 , wherein the peaks and valleys are angled at less than 90 degrees from the fall-line of said planar stanchion when assembled into the ripple packing element.4. The gas-solid ...

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 ...

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 ...

PARTICLE DISENGAGEMENT DEVICE

A particle disengagements device comprising a baffle plate, wherein the baffle plate comprises one or more guide baffles and one or more separation baffles, wherein the one or more guide baffles and the one or more separation baffles define one or more air flow paths and one or more solid flow paths and associated systems and methods. 1. A particle disengagement device comprising a circular baffle plate , wherein the baffle plate comprises one or more guide baffles and one or more separation baffles , wherein the one or more guide baffles and the one or more separation baffles define one or more air flow paths and one or more solid flow paths.2. The particle disengagement device of claim 1 , wherein the baffle plate has a diameter in the range of from 1 meter to 15 meters.3. The particle disengagement device of claim 1 , wherein the baffle plate has a height in the range of from 1 to 20 inches.4. The particle disengagement device of claim 1 , wherein the one or more guide baffles comprise 10 to 50 guide baffles and the one or more separation vessel comprise 10 to 50 separation baffles.5. The particle disengagement device of claim 1 , wherein the baffle plate has a baffle arrangement comprising one or more parallel rows of guide baffles and separation baffles.6. The particle disengagement device of claim 1 , wherein the guide baffles comprise a protrusion.7. The particle disengagement device of claim 1 , wherein the separation baffle comprises a protrusion.8. The particle disengagement device of claim 6 , wherein the protrusion has a length in the range of from 0.1 inches to 8 inches.9. The particle disengagement device of claim 6 , wherein the protrusion has a rectangular cross sectional shape.10. The particle disengagement device of claim 1 , wherein the one or more guide baffles are spaced apart a distance in the range of from 4 inches to 25 inches.11. The particle disengagement device of claim 1 , wherein the one or more separation baffles are spaced apart a ...

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 ...

FLUID CATALYTIC CRACKING PROCESS AND APPARATUS FOR MAXIMIZING LIGHT OLEFIN YIELD AND OTHER APPLICATIONS

Apparatus and processes herein provide for converting hydrocarbon feeds to light olefins and other hydrocarbons. The processes and apparatus include, in some embodiments, feeding a hydrocarbon, a first catalyst and a second catalyst to a reactor, wherein the first catalyst has a smaller average particle size and is less dense than the second catalyst. A first portion of the second catalyst may be recovered as a bottoms product from the reactor, and a cracked hydrocarbon effluent, a second portion of the second catalyst, and the first catalyst may be recovered as an overhead product from the reactor. The second portion of the second catalyst may be separated from the overhead product, providing a first stream comprising the first catalyst and the hydrocarbon effluent and a second stream comprising the separated second catalyst, allowing return of the separated second catalyst in the second stream to the reactor. 1. (canceled)2. (canceled)3. (canceled)4. (canceled)5. (canceled)6. An integrated disengagement vessel comprising:a housing;a solids separation device disposed within the housing for separating a hydrocarbon stream comprising a hydrocarbon fraction, a second particles, and a first particles into a first stream, comprising the first particles and the hydrocarbon fraction, and a second stream, comprising the separated second particles;one or more cyclones disposed within the housing for separating the first stream to recover a solids fraction, comprising the first particles, and a vapor fraction, comprising the hydrocarbon fraction;an internal vessel disposed within the housing for receiving the second stream comprising the separated second particles;an annular region between the housing and the internal vessel for receiving the solids fraction comprising the first particles;a vapor outlet for recovering the vapor fraction.7. The system of claim 6 , further comprising a flow line for feeding the solids fraction from the annular region to a regenerator.8. The ...

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 ...

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 ...

MICROWAVE REACTOR SYSTEM ENCLOSING A SELF-IGNITING PLASMA

This disclosure provides a reactor system that includes a microwave energy source that generates a microwave energy, a field-enhancing waveguide (FEWG) coupled to the microwave source. The FEWG includes a field-enhancing zone having a cross-sectional area that decreases along a length of the FEWG. The field-enhancing zone includes a supply gas inlet that receives a supply gas, a reaction zone that generates a plasma in response to excitation of the supply gas by the microwave energy, a process inlet that injects a raw material into the reaction zone, and a constricted region that retains a portion of the plasma and combines the plasma and the raw material in response to the microwave energy within the reaction zone. An expansion chamber is in fluid communication with the constricted region facilitates expansion of the plasma. An outlet outputs a plurality of carbon-inclusive particles derived from the expanded plasma and the raw material. 1. A reactor system comprising:a microwave energy source configured to generate a microwave energy; a supply gas inlet configured to receive a supply gas;', 'a reaction zone configured to generate a plasma in response to excitation of the supply gas by the microwave energy;', 'a process inlet configured to inject a raw material into the reaction zone; and', 'a constricted region configured to retain at least some of the generated plasma within the reaction zone, the constricted region further configured to combine the plasma and the raw material in response to microwave energy within the constricted region;, 'a field-enhancing waveguide (FEWG) coupled to the microwave energy source, the FEWG including a field-enhancing zone having a cross-sectional area that decreases along a length of the FEWG, the field-enhancing zone comprisingan expansion chamber in fluid communication with the constricted region and configured to expand the plasma; andan outlet configured to output a plurality of carbon-inclusive particles derived from the ...

DEVICE AND METHOD FOR PREPARING PARA-XYLENE AND CO-PRODUCING LIGHT OLEFINS FROM METHANOL AND/OR DIMETHYL ETHER AND BENZENE

A fast fluidized bed reactor, device and method for preparing para-xylene and co-producing light olefins from methanol and/or dimethyl ether and benzene, resolving or improving the competition problem between an MTO reaction and an alkylation reaction during the process of producing para-xylene and co-producing light olefins from methanol and/or dimethyl ether and benzene, and achieving a synergistic effect between the MTO reaction and the alkylation reaction. By controlling the mass transfer and reaction, competition between the MTO reaction and the alkylation reaction is coordinated and optimized to facilitate a synergistic effect of the two reactions, so that the conversion rate of benzene, the yield of para-xylene, and the selectivity of light olefins are increased. 124-. (canceled)25. A fast fluidized bed reactor for preparing para-xylene and co-producing light olefins from methanol and/or dimethyl ether and benzene , wherein the fast fluidized bed reactor comprises a first reactor feed distributor and a plurality of second reactor feed distributors , the first reactor feed distributor and the plurality of second reactor feed distributors are sequentially arranged along the gas flow direction in the fast fluidized bed reactor.26. The fast fluidized bed reactor of claim 25 , wherein the number of the second reactor feed distributors is in a range from 2 to 10.27. The fast fluidized bed reactor of claim 25 , wherein the fast fluidized bed reactor comprises a first reactor gas-solid separator and a second reactor gas-solid separator claim 25 , the first reactor gas-solid separator is placed in a dilute phase zone or outside a reactor shell claim 25 , and the second reactor gas-solid separator is placed in the dilute phase zone or outside the reactor shell;the first reactor gas-solid separator is provided with a regenerated catalyst inlet, a catalyst outlet of the first reactor gas-solid separator is placed at the bottom of a reaction zone, and a gas outlet of the ...

Solids circulation system and method for capture and conversion of reactive solids with fluidized bed temperature control

A solids circulation system receives a gas stream containing char or other reacting solids from a first reactor. The solids circulation system includes a cyclone configured to receive the gas stream from the first reactor, a dipleg from the cyclone to a second reactor, and a riser from the second reactor which merges with the gas stream received by the cyclone. The second reactor has a dense fluid bed and converts the received materials to gaseous products. A conveying fluid transports a portion of the bed media from the second reactor through the riser to mix with the gas stream prior to cyclone entry. The bed media helps manipulate the solids that is received by the cyclone to facilitate flow of solids down the dipleg into the second reactor. The second reactor provides additional residence time, mixing and gas-solid contact for efficient conversion of char or reacting solids.

FAST FLUIDIZED-BED REACTOR, DEVICE, AND METHOD USING OXYGEN-CONTAINING COMPOUND FOR MANUFACTURING PROPENE OR C4 HYDROCARBON

A fast fluidized-bed reactor, device and method for preparing propylene and C4 hydrocarbons from oxygen-containing compounds. The device includes the fast fluidized-bed reactor and a fluidized-bed regenerator for regenerating a catalyst. The method includes: a) feeding a raw material containing the oxygen-containing compounds from reactor feed distributors to a dense phase zone of the fast fluidized-bed reactor, and contacting the raw material with a catalyst, to generate a stream containing target product and a spent catalyst containing carbon; b) sending the stream into a product separation system, obtaining propylene, C4 hydrocarbons, light fractions and the like after separation, returning 70 wt. % or more of the light fractions to the dense phase zone of the fast fluidized-bed reactor from the reactor feed distributor. 115-. (canceled)16. A fast fluidized-bed reactor for preparing propylene and C4 hydrocarbons from oxygen-containing compounds , comprising:a reactor shell, one or more reactor feed distributors, a first reactor gas-solid separator, a second reactor gas-solid separator, a reactor heat extractor, a product gas outlet and a reactor stripper, wherein the lower part of the fast fluidized-bed reactor is a dense phase zone, the upper part of the fast fluidized-bed reactor is a dilute phase zone, one and more reactor feed distributors are disposed in the dense phase zone, the reactor heat extractor is disposed inside or outside the reactor shell, the first reactor gas-solid separator and the second reactor gas-solid separator are placed outside the reactor shell, the first reactor gas-solid separator is equipped with a regenerated catalyst inlet, the catalyst outlet of the first reactor gas-solid separator is located at the bottom of the dense phase zone, the gas outlet of the first reactor gas-solid separator is located in the dilute phase zone, the inlet of the second reactor gas-solid separator is located in the dilute phase zone, the catalyst outlet ...

External steam reduction method in a fluidized catalytic cracker

The present disclosure generally relates to methods to reduce the external steam supplied to a fluidized catalytic cracker by injecting a stream comprising a water-containing renewable fuel oil into a riser of a fluidized catalytic cracker.

Fluidized catalytic cracker riser quench system

The present application generally relates to a riser quench system comprising a quench line and one or more quench injecting ports for injecting a renewable fuel oil into the riser of a fluidized catalytic cracker co-processing a renewable fuel oil and a petroleum fraction as reactants.

Fluidized Bed Dehydrogenation Process For Light Olefin Production

The present invention discloses process and apparatus for the production of light olefins from their respective alkanes by catalytic dehydrogenation, where in the dehydrogenation reaction is carried out in multiple semi-continuously operated fluidized bed isothermal reactors, connected to a common regenerator and wherein the process is carried out in a sequence of steps in each cycle i.e., entry of hot regenerated catalyst, pre-treatment with reducing gas, dehydrogenation reaction, stripping, transfer of catalyst to regenerator and catalyst regeneration. Process cycle in each reactor starts at different times such that the catalyst inventory in the regenerator is invariable with time. 2. The process as claimed in claim 1 , wherein the fluidized bed reactors are maintained under isothermal conditions by an additional heating element (F).3. The process as claimed in claim 1 , wherein the temperature of hot regenerated catalyst entering the reactor is 600-800° C. claim 1 , and wherein diluent stream comprises of nitrogen or steam or helium or any other gas claim 1 , and wherein pre-heated alkane feed is sent to reactor with or without diluents.4. The process as claimed in claim 1 , wherein the reducing gas is selected from the group consisting of hydrogen or methane or hydrogen containing gas or dry gas from FCCU or Pressure Swing Adsorption (PSA) off-gas from Hydrogen Generation Unit (HGU) or any combination thereof.5. The process as claimed in claim 1 , wherein the dehydrogenation reaction is carried out at a temperature in the range of 500-850° C. claim 1 , preferably 550-700° C.; pressure in the range of 0.1-3.0 bar; gas hourly space velocity (GHSV) of the feed stream in the range of 500-10000 h claim 1 , and molar ratio of diluent to hydrocarbon in the feed stream is in the range of 0.1 to 5.6. The process as claimed in claim 1 , wherein the alkane feed stream comprises of ethane or propane or iso-butane or n-butane or any combination.7. The process as claimed in ...

METHOD FOR PRODUCING POLYOLEFIN AND POLYOLEFIN PRODUCTION SYSTEM

A polyolefin production system is provided. The polyolefin production system includes a plurality of gas-phase polymerization tanks configured to polymerize an olefin gas to form a polyolefin, a compressor comprising an inlet and an outlet and being configured to compress a an olefin-containing gas, an individual gas feed line disposed at each of the gas-phase polymerization tanks and configured to guide the gas fed from the outlet of the compressor to each of the gas-phase polymerization tanks, an individual gas discharge line disposed at each of the gas-phase polymerization tanks and discharging the gas from each of the gas-phase polymerization tanks, and a first valve installed in each of the individual gas feed lines. 1. A polyolefin production system comprising:a plurality of gas-phase polymerization tanks configured to polymerize an olefin gas to form a polyolefin;a compressor comprising an inlet and an outlet and being configured to compress an olefin-containing gas;an individual gas feed line disposed at each of the gas-phase polymerization tanks, configured to guide the gas fed from the outlet of the compressor to each of the gas-phase polymerization tanks;an individual gas discharge line disposed at each of the gas-phase polymerization tanks, configured to discharge the gas from each of the gas-phase polymerization tanks; anda first valve installed in each of the individual gas feed lines.2. The polyolefin production system according to claim 1 , further comprising a particle transfer series line connecting the plurality of the gas-phase polymerization tanks in series.3. The polyolefin production system according to claim 1 , wherein the first valve is a butterfly valve or an eccentric rotary plug valve.4. The polyolefin production system according to claim 1 , further comprising a second valve installed in each of the individual gas discharge lines.5. The polyolefin production system according to claim 4 , wherein the second valve is a butterfly valve or ...

DEVICE FOR TREATING PARTICLES IN A ROTATING FLUIDIZED BED

Device for treating particles having a vortex chamber defined by end walls at both ends and a circular wall, a rotation imparting device with a fluid feeder arranged in a mainly tangential direction, a particle outlet and a central fluid outlet, an auxiliary chamber coaxially arranged with the vortex chamber defining a treating zone, which auxiliary chamber has a circular outer wall and an end wall and opens into the vortex chamber through an opening in the end wall of the vortex chamber opposite the central fluid outlet, a device for injecting particles coaxially into the treating zone, and a device for feeding a treating fluid into the treating zone in mainly axial direction, wherein the ratio of the area of the opening to the cross-sectional area of the vortex chamber is less than 0.50. 1. Device for treating particles , comprising a vortex chamber defined by end walls at both ends and a circular wall , a rotation imparting device comprising a fluid feeder arranged in a mainly tangential direction , a particle outlet and a central fluid outlet , an auxiliary chamber coaxially arranged with the vortex chamber defining a treating zone , which auxiliary chamber has a circular outer wall and an end wall and opens into the vortex chamber through an opening in the end wall of the vortex chamber opposite the central fluid outlet , a device for injecting particles coaxially into the treating zone , and a device for feeding a treating fluid into the treating zone in mainly axial direction , wherein the ratio of the area of the opening to the cross-sectional area of the vortex chamber is less than 0.50.2. Device according to claim 1 , wherein the ratio of the area of the opening to the cross-sectional area of the vortex chamber is less than 0.40 claim 1 , suitably in the range of from 0.04 to 0.25 and more suitably in the range of from 0.02 to 0.25.3. Device according to claim 1 , wherein the device for feeding treating fluid into the treating zone is arranged near the end ...

MINIMIZING COKE FORMATION IN A REACTOR STRIPPER

The presently disclosed subject matter relates to systems and methods for catalyst regeneration. In particular, the presently disclosed subject matter provides for an integrated fluidized bed reactor and catalyst regeneration system to minimize hydrocarbon accumulation. In one embodiment, the presently disclosed subject matter provides for a fluidized bed reactor unit including a catalyst riser having a partially perforated surface in close proximity to a reactor stripper. 1. A catalyst reaction and regenerator system , comprising:a fluidized bed reactor comprising: 'a reactor stripper in close proximity to the partially perforated surface of the catalyst riser; and', 'a catalyst riser having a partially perforated surface; and'}a catalyst regenerator having at least two transfer lines to the fluidized bed reactor.2. The system of claim 1 , wherein one of the transfer lines connects the catalyst riser to the catalyst regenerator.3. The system of claim 1 , wherein one of the two transfer lines connects the reactor stripper and the catalyst regenerator.4. The system of claim 1 , wherein the perforated surface of the catalyst riser does not allow more than about 5% to about 10% of a catalyst to flow inside the catalyst riser from the reactor stripper.5. The system of claim 1 , wherein the partially perforated surface of the catalyst riser minimizes coke formation.6. The system of claim 1 , wherein the system further comprises a second reactor.7. The system of claim 6 , wherein the second reactor is connected to the fluidized bed reactor by a transfer line.8. A method of regenerating catalyst claim 6 , comprising: generating a chemical product in the presence of a catalyst in the catalyst riser;', 'separating the chemical product from the catalyst in the catalyst riser;', 'feeding the catalyst from the catalyst riser to the reactor stripper;', 'transferring the catalyst from the reactor stripper to a catalyst regenerator through a transfer line; and, 'feeding a ...

Method and Device for Using Oxygen in the Steam Reforming of Biomass

A device is presented and described for the use of oxygen for the thermochemical gasification of biomass in at least one fluidised bed reactor, a heater being arranged in the fluidised bed of the fluidised bed reactor and the fluidised bed reactor being heatable by at least partial oxidation of a combustible gas with oxygen.

METHOD AND APPARATUS FOR PREPARING COMPOSITE

A method and apparatus for preparing a composite, in which the angle between the apparatus base and the apparatus body is adjusted by the elevator device, the solid raw material is loaded into the reactor by the solid feeding device, the main reaction gas, the auxiliary gas and the carrier gas are introduced from the front gas intake unit into the main reaction zone at a preset ratio, followed by the active material deposited on solid particles, the post-processing reaction gas is introduced from the middle gas intake unit to the post-processing reaction zone to form a functional layer on the active material, the prepared composite powder is separated and collected from the gas-solid mixture in the collection device. The exhaust gas is released from the exhaust manifold into an exhaust gas treatment system after minority powder filtered by the filter.

METHOD AND DEVICE FOR PRODUCING LITHIUM TRANSITION METAL OXIDE

Provided is a method for producing a lithium transition metal oxide, comprising, A) mixing a lithium salt and a precursor, adding the mixture into a reactor for precalcination; the lithium salt has a particle size D50 of 10-20 μm and the precursor has a particle size D50 of 1-20 μm, and the precursor is one or more selected from transition metal oxyhydroxide, transition metal hydroxide and transition metal carbonate; and B) adding the product obtained from the precalcination into a fluidized bed reactor, subjecting to a first calcination and a second calcination to obtain the lithium transition metal oxide. Raw materials for the lithium transition metal oxide further includes a main-group metal compound containing oxygen, which is added in the precalcination, the first calcination or the second calcination; and the main-group metal compound containing oxygen has an average particle size of 10-100 nm. A fluidized bed reactor is also provided.

PROCESS AND APPARATUS FOR REMOVING POLYMER MATERIAL FROM A GAS-SOLIDS OLEFIN POLYMERIZATION REACTOR

The present invention relates to a process for removing polymer material from a gas-solids olefm polymerization reactor wherein the gas-solids olefm polymerization reactor is connected to the top part of an outlet vessel via a feed pipe wherein the powder surface of discharged polymer material and the barrier gas injection point are situated in the outlet vessel as such to fulfill the following criteria: R′=X/Y≤2.0; and R″=X/D≥1.0; wherein X=Distance between the powder surface and the barrier gas injection point; Y=Distance between the barrier gas injection point and the vessel outlet; and D=Equivalent outlet vessel diameter, an apparatus for continuously removing polymer material comprising a gas-solids olefm polymerization reactor, an outlet vessel and a feed pipe connecting the gas-solids olefm polymerization reactor with the top part of the outlet vessel and the use of said apparatus for polymerizing alpha-olefm homo- or copolymers having alpha-olefin monomer units of from 2 to 12 carbon atoms and for increasing the barrier gas efficiency of the gas-solids olefin reactor to at least 75%. 1. A process for removing polymer material from a gas-solid olefin polymerization reactor wherein the gas-solid olefin polymerization reactor is connected to the top part of an outlet vessel via a feed pipe , the process comprising the steps of:(i) discharging polymer material from the gas-solid olefin polymerization reactor via the feed pipe into the outlet vessel;(ii) establishing a powder surface of discharged polymer material within the outlet vessel in a section of the middle part of the outlet vessel;(iii) injecting barrier gas through a barrier gas injection point in a section of the bottom part of the outlet vessel below the powder surface;(iv) recovering polymer material from the outlet vessel through a vessel outlet in a section below the barrier gas injection point;characterized in that [{'br': None, 'i': 'R′=X/Y≤', '2.0;'}, {'br': None, 'and'}, {'br': None, 'i': 'R″= ...

SYSTEMS AND METHODS FOR REDUCING HEAT EXCHANGER FOULING RATE

Systems and methods of reducing heat exchanger fouling rate and of producing polyolefins are provide herein. In some aspects, the methods include providing a first gas stream comprising a gas and entrained fine polyolefin particles to a gas outlet line; preferentially removing a portion of the entrained fine polyolefin particles from the gas outlet line to form a bypass stream comprising a higher concentration of the entrained fine polyolefin particles than is present in the first gas stream; providing the bypass stream to a bypass line comprising a bypass line inlet and a bypass line outlet, wherein the bypass line inlet is located upstream of a first heat exchanger, and wherein the bypass line outlet is located downstream of the first heat exchanger; providing at least a portion of the first gas stream to the first heat exchanger, which produces a first cooled gas stream; and combining the bypass stream and a second gas stream at the bypass line outlet to form a combined gas stream comprising one or more olefins or paraffins, wherein a temperature of the combined gas stream is below the dew point of the combined gas stream. 1. A system for reducing heat exchanger fouling rate comprising:a gas outlet line configured to pass a first gas stream comprising a gas and entrained fine polyolefin particles;a first heat exchanger configured to receive at least a portion of the first gas stream and produce a first cooled gas stream; anda bypass line configured to remove a portion of the entrained fine polyolefin particles from the gas outlet line to form a bypass stream comprising a higher concentration of the entrained fine polyolefin particles than is present in the first gas stream, the bypass line comprising a bypass line inlet and a bypass line outlet,wherein the bypass line inlet is located upstream of the first heat exchanger,wherein the bypass line outlet is located downstream of the first heat exchanger, andwherein the bypass line is configured so that the bypass ...

ESTIMATION OF CYCLONE LIFE BASED ON REMAINING ABRASION RESISTANT LINING THICKNESS

A Fluid Catalytic Cracking process converts heavy crude oil fractions into lighter hydrocarbon products at high temperature and moderate pressure in the presence of a catalyst. During this process, catalyst particles stay entrained in the descending gas stream. An inlet scroll on the cyclone may be used to keep the inlet gas stream and the entrained particles away from the entrance to the gas outlet tube. Refractory material may applied to the interior of the wall of the cyclone to form an abrasion resistant lining to insulate the walls of the cyclone from the gas flow contents. The inlet feed velocity may be used as a predictive factor to determine a wear rate of the cyclones. Thus, lining erosion can be predicted so that the lining can be repaired or replaced during a planned turnaround. 1. A system comprising:a reactor configured to perform a fluid catalytic cracking process, the reactor including a cyclone with an abrasion resistant lining on an interior wall of the cyclone;a gas flow rate sensor configured to measure a feed velocity of a feed to the cyclone; a processor of the data analysis platform;', receive feed velocity data from the gas flow rate sensor, the feed velocity data indicating the feed velocity of the feed to the cyclone;', 'determine an erosion rate of the abrasion resistant lining on the interior wall of the cyclone based on the feed velocity of the feed to the cyclone;', 'based on the erosion rate, determine a recommended adjustment to an operating parameter of the reactor;', 'send the recommended adjustment to the operating parameter of the reactor; and, 'memory of the data analysis platform, the memory storing executable instructions that, when executed, cause the data analysis platform to], 'a data analysis platform comprising a processor of the control platform; and', receive the recommended adjustment to the operating parameter of the reactor; and', 'adjust the operating parameter of the reactor., 'memory of the control platform, the ...

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.

FLUIDIZED BED DEVICE AND METHOD FOR PREPARING PARA-XYLENE AND CO-PRODUCING LIGHT OLEFINS FROM METHANOL AND/OR DIMETHYL ETHER AND BENZENE

A turbulent fluidized bed reactor, device and method for preparing para-xylene and co-producing light olefins from methanol and/or dimethyl ether and benzene, resolving or improving the competition problem between an MTO reaction and an alkylation reaction during the process of producing para-xylene and co-producing light olefins from methanol and/or dimethyl ether and benzene, and achieving a synergistic effect between the MTO reaction and the alkylation reaction. By controlling the mass transfer and reaction, competition between the MTO reaction and the alkylation reaction is coordinated and optimized to facilitate a synergistic effect of the two reactions, so that the conversion rate of benzene, the yield of para-xylene, and the selectivity of light olefins are increased. The turbulent fluidized bed reactor includes a first reactor feed distributor and a number of second reactor feed distributors; the first reactor feed distributor and the plurality of second reactor feed distributions are sequentially arranged. 126-. (canceled)27. A turbulent fluidized bed reactor for preparing para-xylene and co-producing light olefins from methanol and/or dimethyl ether and benzene , the turbulent fluidized bed reactor comprising a first reactor feed distributor and a plurality of second reactor feed distributors , the first reactor feed distributor and the plurality of second reactor feed distributors are sequentially arranged along the gas flow direction in the turbulent fluidized bed reactor; andthe number of the second reactor feed distributors is in a range from 2 to 10.28. The turbulent fluidized bed reactor of claim 27 , the turbulent fluidized bed reactor further comprises a first reactor gas-solid separator and a second reactor gas-solid separator claim 27 , the first reactor gas-solid separator is placed in a dilute phase zone or outside a reactor shell claim 27 , and the second reactor gas-solid separator is placed in the dilute phase zone or outside the reactor ...

Method for calcination of a carbon dioxide rich sorbent

A method for calcination includes providing a heated coarse solid particle stream with a carbon dioxide rich sorbent to a reactor having a rotatable container.

Light alkanes to liquid fuels

The present disclosure relates generally processes and systems for converting a C2-C7 light alkanes feed to liquid transportation fuels or value-added chemicals. The feed is contacted with an aromatization catalyst at a temperature and pressure that selectively converts C4 and larger alkanes to an intermediate product comprising monocyclic aromatics and olefins. Following separation of the aromatics and C5+ hydrocarbons from the intermediate product, unconverted C2-C3 alkanes are thermally-cracked to produce olefins that are subsequently oligomerized to produce a liquid transportation fuel blend stock or value-added chemicals.

Methods for alkane dehydrogenation

Disclosed herein are methods for dehydrogenation of alkanes to olefins by co-injecting the alkane feed with hydrogen. The present methods provide the improved feed conversion, desired product selectivity, total olefins in product stream, and lower catalyst deactivation rate.

THERMOLYTIC FRAGMENTATION OF SUGARS

A process for large scale and energy efficient product on of oxygenates from sugar is disclosed in which a sugar feedstock is introduced into a thermolytic fragmentation reactor comprising a fluidized stream of heat carrying particles. The heat carrying particles may be separated from the fluidized stream prior to cooling the fragmentation product and may be directed to a reheater to reheat the particles and recirculate the heated particles to the fragmentation reactor. 1. A process for thermolytic fragmentation of a sugar into C-Coxygenates , said process comprising the steps of:a. providing particles carrying heat and suitable for fluidization;b. providing a fluidized bed fragmentation reactor comprising a riser and suitable for conducting thermolytic fragmentation and suitable for fluidizing a stream of particles;c. providing a feedstock solution comprising a sugar;d. introducing the particles into the reactor at a rate sufficient to maintain a temperature of at least 250° C., such as at least 300 350, 400 or 450° C., after the thermolytic fragmentation has taken place, and sufficient to obtain a fluidized stream of particles;e. introducing the feedstock into the fluidized stream of particles to obtain thermolytic fragmentation of the sugar to produce a particle dense fragmentation product; thenf. separating a fraction of the particles from the particle dense fragmentation product to produce a particle lean fragmentation product;g. quenching the particle lean fragmentation product at least 50° C. such that from introducing the feedstock into the particle containing fluidization stream to the quench is performed, the mean residence time of the gas is maximum 5, such as maximum 3 seconds, such as maximum 2, 1, 0.8 or 0.6 seconds;h. recovering the crude fragmentation product,i. transferring the particles separated in step f) to a reheater for heating; andj. recirculating the heated particles to the fragmentation reactor.2. The process according to claim 1 , wherein ...

APPARATUSES FOR DEHYDROGENATION OF ALKANES

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

A METHOD, AN ARRANGEMENT AND USE OF AN ARRANGEMENT OF PREPARING POLYMER

A method and arrangement of producing polymer comprising polymerizing in reactor having a top zone having a generally conical shape, a middle zone in direct contact with and below said top zone having a generally cylindrical shape, a bottom zone having a generally conical shape thereby polymerizing at least one olefin, in the presence of a polymerization catalyst and fluidization gas to obtain (i) a first stream comprising fluidization gas and particles of olefin polymer, (ii) a second stream comprising fluidization gas and agglomerates of olefin polymer, (iii) a third olefin polymer product stream—directing the first stream comprising fluidization gas and olefin polymer particles to a series of at least three cyclones connected to the fluidized bed reactor—separating agglomerates of olefin polymer from the second stream, withdrawing from the fluidized bed polymerization reactor the third olefin polymer product stream. 1. A method of producing polymer particles wherein the method comprises (i) a first stream comprising fluidization gas and olefin polymer particles,', '(ii) a second stream comprising fluidization gas and agglomerates of olefin polymer,', '(iii) a third olefin polymer product stream,, 'polymerizing in a fluidized bed polymerization reactor comprising a fluidized bed in the reactor and the reactor having a top zone having a generally conical shape, a middle zone in direct contact with and below said top zone having a generally cylindrical shape, a bottom zone in direct contact with and below the middle zone and having a generally conical shape thereby polymerizing at least one olefin, optionally at least one comonomer and optionally hydrogen, in the presence of a polymerization catalyst and fluidization gas to obtain'}directing the first stream comprising fluidization gas and olefin polymer particles to a series of at least three cyclones connected to the fluidized bed polymerization reactor thereby obtaining from a last cyclone in the series a final ...

REACTION-REGENERATION DEVICE AND PROCESS FOR ALKANE DEHYDROGENATION TO ALKENE

A reaction-regeneration device for catalytic dehydrogenation or/and catalytic cracking of alkanes comprises a reaction device and a regeneration device. The reaction device comprises a reactor and a disengager, and the disengager is located at an upper part of the reactor. The reactor comprises a tapering section, and diameters of cross sections of the tapering section gradually decrease from bottom to top. Secondary conversion of alkenes caused by back-mixing is reduced, and thus the yield and selectivity to alkenes are increased. 1. A catalyst regeneration device , comprisinga regenerator for accommodating a catalyst and a regeneration disengager,wherein diameters of cross sections of the regenerator are decreased from top to bottom, anda circular pipe sleeve is arranged at a lower position inside the regenerator.2. The catalyst regeneration device according to claim 1 , wherein the circular pipe sleeve is parallel to an axis of the regenerator.3. The catalyst regeneration device according to claim 1 , wherein the circular pipe sleeve is coaxial with the regenerator.4. The catalyst regeneration device according to claim 1 , wherein a height of the circular pipe sleeve in the regenerator is less than two thirds of a height of a catalyst dense-phase bed layer.5. The catalyst regeneration device according to claim 1 , wherein a height of the circular pipe sleeve in the regenerator is less than one third of a height of a catalyst dense-phase bed layer.6. The catalyst regeneration device according to claim 1 , wherein claim 1 , fuel and air are directly fed into the circular pipe sleeve.7. A regeneration method for alkane dehydrogenation catalyst claim 1 , comprising the following step:spent catalyst entering a regeneration disengager, and fuel and air entering a regenerator from a lower part or bottom of the regenerator;gas moving upwards in the regenerator, a linear speed of the gas gradually decreasing from bottom to top, and, the spent catalyst moving upwards at a ...

Nozzle for wet gas scrubber

A nozzle and methods of gas stripping utilizing the nozzle are provided. A nozzle is provided comprising a ceramic nozzle assembly comprising an inlet at one end of a cylindrical portion, an outlet at one end of a conical portion; the cylindrical portion transitioning to the conical portion at an end of the cylindrical portion distal from the inlet; the conical portion transitioning to the cylindrical portion at an end of the conical portion distal from the outlet; and a ceramic vane assembly within the cylindrical portion; the vane assembly comprising a central vane support located substantially concentrically within the cylindrical portion, and a plurality of angled vanes extending from the central vane support to an inner wall of the cylindrical portion; wherein the ceramic nozzle assembly and the ceramic vane assembly are manufactured such that the two assemblies comprise a single piece of ceramic.

Concentrated solar heat receiver, reactor, and heater

A heat receiver, a reactor, and a heater utilize the heat of concentrated solar light for thermal decomposition and/or chemical reaction of coals, etc. The heat receiver includes: a side portion forming a substantially cylindrical side surface; a substantially circular bottom portion connected to the lower edge of the side portion; and a ceiling connected to the upper edge of the side portion. A substantially circular aperture is formed in the center of the ceiling. The heat receiver has a substantially cylindrical cavity and the opening portion is open. When the cavity has a diameter of D and a length of L, and the aperture has a diameter of d, d=D/2 or less and L=2D or more. Concentrated solar light entering the heat receiver is to be contained in the heat receiver to effectively utilize the solar light.

FLUIDIZED BED DEVICE AND METHOD FOR PREPARING PARA-XYLENE AND CO-PRODUCING LIGHT OLEFINS FROM METHANOL AND/OR DIMETHYL ETHER AND TOLUENE

A turbulent fluidized bed reactor, device and method for preparing para-xylene and co-producing light olefins from methanol and/or dimethyl ether and toluene, resolving or improving the competition problem between an MTO reaction and an alkylation reaction during the process of producing para-xylene and co-producing light olefins from methanol and/or dimethyl ether and toluene, and achieving a synergistic effect between the MTO reaction and the alkylation reaction. By controlling the mass transfer and reaction, competition between the MTO reaction and the alkylation reaction is coordinated and optimized to facilitate a synergistic effect of the two reactions, so that the conversion rate of toluene, the yield of para-xylene, and the selectivity of light olefins are increased. The turbulent fluidized bed reactor includes a first reactor feed distributor and a number of second reactor feed distributors and are arranged sequentially along the gas flow direction. 126-. (canceled)27. A turbulent fluidized bed reactor for preparing para-xylene and co-producing light olefins from methanol and/or dimethyl ether and toluene , the turbulent fluidized bed reactor comprising: a first reactor feed distributor and a plurality of second reactor feed distributors , the first reactor feed distributor and the plurality of second reactor feed distributors are sequentially arranged along the gas flow direction in the turbulent fluidized bed reactor;the feed to the first reactor feed distributor comprises toluene and a portion of methanol and/or dimethyl ether;the feed to the second reactor feed distributor comprises methanol and/or dimethyl ether; andthe number of the second reactor feed distributors is in a range from 2 to 10.28. The turbulent fluidized bed reactor of claim 27 , the turbulent fluidized bed reactor further comprising a first reactor gas-solid separator and a second reactor gas-solid separator claim 27 , the first reactor gas-solid separator is placed in a dilute phase ...

Device for producing nanocarbon

Using a device for producing nanocarbon, a fluidized bed is formed by supplying a low hydrocarbon and oxygen to a fluid catalyst, and nanocarbon and hydrogen are produced by a decomposition reaction of the low hydrocarbon accompanied by a self-combustion of the low hydrocarbon and the oxygen. The device includes: a fluidized bed reactor for containing the fluid catalyst and for causing the self-combustion thereof while being supplied with the low hydrocarbon and the oxygen; a gas supplying unit connected to the fluidized bed reactor for supplying the low hydrocarbon and the oxygen to the fluidized bed reactor; an exhaust gas path connected to the fluidized bed reactor for exhausting an exhaust gas in the fluidized bed reactor to outside; and a supplying unit connected to the fluidized bed reactor for supplying the fluid catalyst to the fluidized bed reactor.

SYSTEMS AND METHODS FOR PRODUCING SYNGAS FROM A SOLID CARBON-CONTAINING SUBSTANCE USING A REACTOR HAVING HOLLOW ENGINEERED PARTICLES

A solids circulation system receives a gas stream containing char or other reacting solids from a first reactor. The solids circulation system includes a cyclone configured to receive the gas stream from the first reactor, a dipleg from the cyclone to a second reactor, and a riser from the second reactor which merges with the gas stream received by the cyclone. The second reactor has a dense fluid bed and converts the received materials to gaseous products. A conveying fluid transports a portion of the bed media from the second reactor through the riser to mix with the gas stream prior to cyclone entry. The bed media helps manipulate the solids that is received by the cyclone to facilitate flow of solids down the dipleg into the second reactor. The second reactor provides additional residence time, mixing and gas-solid contact for efficient conversion of char or reacting solids. 1100. A reactor () for producing carbon monoxide , carbon dioxide , and hydrogen from a solid carbon-containing substance , comprising:(a) a fluidized bed comprising bed material in the form of hollow engineered particles selected from the group consisting of alumina, zirconia, sand, olivine sand, limestone, dolomite and metal catalyst;{'b': '160', '(b) a freeboard () located above a bed level of the fluidized bed;'}{'b': 700', '160', '100', '700, '(c) a cyclone () positioned within the freeboard () of the reactor (), the cyclone () configured to capture and recycle entrained bed material and char particles to the fluidized bed;'}{'b': 160', '160, 'sub': 2', '2, '(d) a plurality of fluid addition stages located in the freeboard (), the plurality of fluid addition stages configured to introduce a mixture of oxygen and superheated steam to the freeboard () to promote conversion of char into CO, CO, and H;'}{'b': 140', '130, '(e) a distributor () configured to accept and distribute a fluidization media () comprising oxygen and superheated steam into the bed material of the fluidized bed;'}{'b': ...

PROCESS AND APPARATUS FOR CRACKING HYDROCARBONS TO LIGHTER HYDROCARBONS

A process and apparatus for catalytically cracking fresh heavy hydrocarbon feed to produce cracked products is disclosed. A fraction of the cracked products can be obtained to re-crack it in a downer reactor. The downer reactor may produce high selectivity to light olefins. Spent catalyst from both reactors can be regenerated in the same regenerator. 1. A process for catalytically cracking hydrocarbons comprising:contacting a fresh hydrocarbon feed stream with an upwardly rising catalyst stream to produce a cracked hydrocarbon stream and a first spent catalyst stream;separating said first spent catalyst stream from said cracked hydrocarbon stream; andcontacting a second hydrocarbon feed stream with a downwardly falling catalyst stream to produce a light hydrocarbon stream and a second spent catalyst stream.2. The process of further comprising fractionating said cracked hydrocarbon stream to produce said second hydrocarbon feed stream.3. The process of wherein said second hydrocarbon stream has a lower boiling point range than the fresh hydrocarbon feed stream.4. The process of wherein said first spent catalyst stream and said second spent catalyst stream are mixed.5. The process of further comprising regenerating said first spent catalyst stream and said second spent catalyst stream to produce regenerated catalyst.6. The process of wherein said upwardly rising catalyst stream comprises said regenerated catalyst.7. The process of wherein said downwardly falling catalyst stream comprises said regenerated catalyst.8. The process of wherein said fresh hydrocarbon feed stream is contacted with said upwardly rising catalyst stream in a riser reactor.9. The process of wherein said second hydrocarbon feed stream is contacted with said downwardly falling catalyst stream in a reactor chamber.10. The process of further comprising collecting said cracked hydrocarbon stream and said light hydrocarbon stream in a plenum above a disengager for separating said first spent catalyst ...

Solids Circulation System and Method For Capture and Conversion of Reactive Solids

A solids circulation system receives a gas stream containing char or other reacting solids from a first reactor. The solids circulation system includes a cyclone configured to receive the gas stream from the first reactor, a dipleg from the cyclone to a second reactor, and a riser from the second reactor which merges with the gas stream received by the cyclone. The second reactor has a dense fluid bed and converts the received materials to gaseous products. A conveying fluid transports a portion of the bed media from the second reactor through the riser to mix with the gas stream prior to cyclone entry. The bed media helps manipulate the solids that is received by the cyclone to facilitate flow of solids down the dipleg into the second reactor. The second reactor provides additional residence time, mixing and gas-solid contact for efficient conversion of char or reacting solids.

VCC SLURRY MID REACTOR SEPARATION

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

FCC COUNTER-CURRENT REGENERATOR WITH A REGENERATOR RISER

A counter-current catalyst regenerator with at least two stages of counter-current contact along with a regenerator riser is proposed. Each stage may comprise a permeable barrier that allows upward passage of oxygen-containing gas and downward passage of coked catalyst into each stage, but inhibits upward movement of catalyst to mitigate back mixing and approximate true counter-current contact and efficient combustion of coke from catalyst. The regenerator riser may provide a passage to transport the catalyst and may serve as a secondary stage for coke combustion to provide the regenerated catalyst. 1. A process for combusting coke from coked catalyst in a regenerator vessel , the process comprising:(a) providing a coked catalyst to an inlet in a bottom of a regenerator riser;(b) propelling the coked catalyst upwardly from the bottom of the regenerator riser to a top of the regenerator riser via a secondary stream of gas;(c) discharging catalyst from an outlet in the top of the regenerator riser;(d) passing the catalyst downwardly through a one or more stages, each of the one or more stages comprising a permeable barrier;(e) passing a primary stream of oxygen-containing gas upwardly through the one or more stages in counter-current contact with the catalyst to combust coke from the coked catalyst to provide a regenerated catalyst and a flue gas; and(f) passing the regenerated catalyst from a regenerated catalyst outlet to a riser reactor through a regenerated catalyst standpipe.2. The process of claim 1 , wherein the step of propelling the coked catalyst upwardly from the bottom of the regenerator riser provides a partially regenerated catalyst via combustion of the coked catalyst.3. The process of claim 2 , wherein the step of passing the primary stream of oxygen-containing gas in counter-current contact with the coked catalyst provides a completely regenerated catalyst via combustion of coke from the partially regenerated catalyst.4. The process of further ...

PROCESS FOR PREPARING ETHYLENE AND/OR PROPYLENE

A process for preparing ethylene and/or propylene, wherein oxygenates and olefins are converted to ethylene and/or propylene over a zeolite-comprising catalyst, in two reaction steps. The catalyst is circulated in the reaction system. 1. A process for preparing ethylene and/or propylene , wherein oxygenates and olefins are converted to ethylene and/or propylene over a zeolite-comprising catalyst , comprising the steps of:a) reacting in a first reactor an oxygenate feed over the zeolite-comprising catalyst at a temperature in the range of from 350 to 1000° C. and retrieving from the first reactor a first reactor effluent stream comprising gaseous products, including ethylene and/or propylene, and zeolite-comprising catalyst;b) reacting in a second reactor an olefin feed over the zeolite-comprising catalyst at a temperature in the range of from 500 to 700° C. and retrieving from the second reactor a second reactor effluent stream comprising gaseous products, including ethylene and/or propylene, and zeolite-comprising catalyst;c) providing the first and second reactor effluent stream to one or more gas/solid separators to retrieve zeolite-comprising catalyst from the first and second reactor effluent;d) providing part of the zeolite-comprising catalyst retrieved in step (c) to the first reactor;e) regenerating another part of the zeolite-comprising catalyst retrieved in step (c) by contacting the zeolite-comprising catalyst with oxygen at elevated temperatures to provide a hot regenerated zeolite-comprising catalyst; andf) providing part of the hot regenerated zeolite-comprising catalyst to the first reactor and another part of the hot regenerated zeolite-comprising catalyst to the second reactor.2. A process according to claim 1 , wherein at least part of the first and second effluent are provided to the same gas/solid separator.3. A process according to claim 1 , wherein the first reactor and/or the second reactor is a riser reactor.4. A process according to claim 1 ...

SLURRY PHASE REACTOR WITH INTERNAL CYCLONES

A system for processing a hydrocarbon feed has a final stage reactor and internal separator with cyclone that forms a substantially gas stream and a substantially non-gas stream. The substantially gas stream is sent directly from the final stage reactor and separator to further downstream processing. 1. A system for processing a hydrocarbon feed , comprising:a plurality of serially aligned reactors, the plurality of reactors including a final stage reactor, the final stage reactor including:a vessel,an inlet formed in the vessel for receiving the hydrocarbon feed,a reactor section formed in the vessel, the reactor section receiving the hydrocarbon feed via the inlet; and a nozzle separating the reactor section from the separator section, the nozzle having an opening directing the hydrocarbon feed, hydrogen, and reaction products from the reactor section to the separator section,', 'a first outlet formed in the vessel from which the substantially non-gas stream exits the vessel;', 'at least one cyclone separator positioned inside the separator section and configured to produce the substantially gas stream; and', 'a second outlet from which the substantially gas stream exits the vessel., 'a separator section formed in the vessel, the separator section configured to form a substantially gas stream and a substantially non-gas stream, the separator section including2. The system of claim 1 , wherein the plurality of serially aligned reactors further includes a first stage reactor claim 1 , wherein the first stage reactor is the first reactor through which the hydrocarbon feed is reacted and the final stage reactor is the last reactor through which the hydrocarbon feed is reacted claim 1 , wherein the hydrocarbon feed is reacted with at least a first additive in the first stage reactor and reacted with at least a second additive in the final stage reactor.3. The system of claim 2 , wherein the first additive is selected from one of: activated carbon claim 2 , iron claim 2 ...

SLURRY PHASE REACTOR WITH INTERNAL VAPOR-LIQUID SEPARATOR

A system for processing a hydrocarbon feed has a final stage reactor and internal separator that forms a substantially gas stream and a substantially non-gas stream. The substantially gas stream is sent directly from the final stage reactor to a separator or for other processing. 1. A system for processing a hydrocarbon feed , comprising: a vessel body,', 'an inlet formed in the vessel body for receiving the hydrocarbon feed,', 'a reactor section formed in the vessel body, the reactor section receiving the hydrocarbon feed via the inlet;', 'a separator section formed in the vessel body, the separator section configured to form a substantially gas stream and a substantially non-gas stream;', 'a nozzle separating the reactor section from the separator section, the nozzle having an opening directing the hydrocarbon feed, hydrogen, and reaction products from the reactor section to the separator section;', 'a first outlet formed in the vessel body receiving the substantially non-gas stream;', 'a second outlet formed in the vessel body, the second outlet receiving the substantially gas stream; and, 'a plurality of serially aligned reactors, the plurality of reactors including a final stage reactor, the final stage reactor includinga separator receiving the substantially gas stream from the second outlet.2. The system of claim 1 , further comprising a deflector positioned in the separator section claim 1 , the deflector obstructing axial flow of the hydrocarbon feed in the separator section.3. The system of claim 2 , wherein the deflector is a plate.4. The system of claim 2 , wherein the deflector is a curved tubular member connected to the second outlet.5. The system of claim 1 , further comprising a quench inlet formed in the vessel body claim 1 , the quench inlet receiving at least one of: a cooled hydrogen claim 1 , a vacuum gas oil claim 1 , a cool hydrocarbon stream.6. The system of claim 1 , wherein the plurality of serially aligned reactors further includes a first ...

Microwave Reactor System with Gas-Solids Separation

Microwave chemical processing system having a microwave plasma reactor, and a multi-stage gas-solid separation system are disclosed. The microwave energy source has a waveguide, a reaction zone, and an inlet configured to receive the input material, and the input material is converted into separated components. The separated components include hydrogen gas and carbon particles. The multi-stage gas-solid separation system has a first cyclone separator to filter the carbon particles from the separated components, and a back-pulse filter system coupled to the output of the first cycle separator to filter the carbon particles from the output from the first cyclone separator. 1. A system , comprising: a first waveguide comprising a first reaction zone extending along a reaction length of the first waveguide;', 'a microwave energy source coupled to the first waveguide, wherein the microwave energy source provides microwave energy into the first waveguide and generates a plasma within the first reaction zone; and', 'an input material inlet configured to receive input material comprising a hydrocarbon gas, wherein the input material flows through the input material inlet into the first reaction zone, and the plasma within the first reaction zone is used to separate the input material into first separated components, wherein the first separated components comprise hydrogen gas and first carbon particles; and, 'a microwave plasma reactor comprising a first cyclone separator having an output, wherein the first cyclone separator filters the first carbon particles from the first separated components; and', 'a fines filter coupled to the output of the first cyclone separator, wherein the fines filter filters the first carbon particles from the output from the first cyclone separator., 'a gas-solid separator system coupled to the microwave plasma reactor, wherein the first separated components enter the gas-solid separator system, and the gas-solid separator system comprises2. The ...

DEVICE AND METHOD FOR PREPARING PARA-XYLENE AND CO-PRODUCING LIGHT OLEFINS FROM METHANOL AND/OR DIMETHYL ETHER AND TOLUENE

Disclosed are a fast fluidized bed reactor, device and method for preparing para-xylene and co-producing light olefins from methanol and/or dimethyl ether and toluene, with the reactor, device and method being capable of solving or improving the problem of competition between an alkylation reaction and an MTO reaction during the process of producing the para-xylene and co-producing light olefins from toluene and methanol, thus achieving a synergistic effect between the MTO reaction and the alkylation reaction. By controlling the mass transfer and reaction, the competition between the alkylation reaction and the MTO reaction is coordinated and optimized to achieve a synergistic effect, thereby increasing the conversion rate of toluene, the yield of para-xylene and the selectivity of the light olefins. The fast fluidized bed reactor comprises a first reactor feed distributor and a plurality of second reactor feed distributors, the first reactor feed distributor and the plurality of second reactor feed distributors are sequentially arranged along the gas flow direction in a reaction zone of the fast fluidized bed reactor. 1. A fast fluidized bed reactor for preparing para-xylene and co-producing light olefins from methanol and/or dimethyl ether and toluene , wherein the fast fluidized bed reactor comprises a first reactor feed distributor and a plurality of second reactor feed distributors , the first reactor feed distributor and the plurality of second reactor feed distributors are sequentially arranged along the gas flow direction in the fast fluidized bed reactor.2. The fast fluidized bed reactor of claim 1 , wherein the fast fluidized bed reactor comprises a first reactor gas-solid separator and a second reactor gas-solid separator claim 1 , the first reactor gas-solid separator is placed in a dilute phase zone or outside a reactor shell claim 1 , and the second reactor gas-solid separator is placed in the dilute phase zone or outside the reactor shell;the first ...

CONTINUOUS MANUFACTURING APPARATUS AND METHOD FOR CARBON NANOTUBES HAVING GAS SEPARATION UNITS

The present invention relates to a continuous manufacturing apparatus for a carbon nanotube having gas separation units and a continuous manufacturing method for a carbon nanotube using the same. According to the present invention, the present invention has an effect to provide the continuous manufacturing apparatus of the carbon nanotube and continuous manufacturing method using the same, in which it makes possible to perform a rapid processing; has excellent productivity and excellent conversion rate of carbon source; can significantly reduce the cost of production; can reduce energy consumption because a reactor size can be decreased as compared with capacity; and a gas separation unit that not generate a waste gas. 119-. (canceled)20. A continuous manufacturing apparatus of a carbon nanotube , comprisingi) a reactor for synthesizing the carbon nanotube;ii) a separator for separating a mixed gas and the carbon nanotube transferred from the reactor;iii) a gas separation unit for removing in part or in whole of more than one component gas from the mixed gas separated; andiv) a re-circulation pipe for recirculating the mixed gas without in part or in whole of the component gas to the carbon nanotube reactor,wherein a heat exchanger is installed between the reactor i) and the separator ii).21. The continuous manufacturing apparatus of the carbon nanotube according to claim 20 , wherein the polymer membrane is produced with more than one polymer selected from the group consisting of polysulfone claim 20 , polycarbonate claim 20 , polyimide claim 20 , and polystyrene claim 20 , and is for low temperature to operate at below 50° C.22. The continuous manufacturing apparatus of the carbon nanotube according to claim 20 , wherein the component gas claim 20 , of iii) claim 20 , is hydrogen.23. The continuous manufacturing apparatus of the carbon nanotube according to claim 20 , wherein the component gas of iii) is a byproduct gas produced in the reactor of i).24. The ...

Termination Device of a Reactor of a Fluid Catalytic Cracking Unit

The invention relates to a termination device () of a tubular reactor () comprising at least one separation element () adapted for the separation of solid particles and gaseous effluents and at least one coupling element () that is part of an end of said tubular reactor, said separation element being connected to said coupling element, characterized in that each element of the termination device is made of ceramic material. 114.-. (canceled)15. A termination device of a tubular reactor comprising:{'sub': 4', '3', '4', '2', '3, 'at least one separation element adapted for the separation of solid particles and gaseous effluents and at least one coupling element that is part of an end of the tubular reactor, the separation element being connected to the coupling element, characterized in that each element of the termination device is made of ceramic material and the ceramic material comprises a ceramic matrix selected from silicon carbide SiC, boron carbide BC, silicon nitride SiN, aluminium nitride AlN, boron nitride BN, alumina AlO, or mixtures thereof, incorporated in which ceramic matrix are carbon fibres or ceramic fibres.'}16. The termination device according to claim 15 , characterized in that the ceramic fibres are selected from the group consisting of crystalline alumina fibres claim 15 , mullite fibres claim 15 , crystalline or amorphous silicon carbide fibres claim 15 , zirconia fibres claim 15 , silica-alumina fibres claim 15 , and mixtures thereof17. The termination device according to claim 15 , characterized in that the ceramic material is a sintered ceramic material.18. The termination device according to claim 15 , characterized in that the ceramic material is a Ceramic Matrix Composite (CMC).19. The termination device according to claim 15 , characterized in that the elements form one and the same part made of ceramic material.20. The termination device according to claim 15 , characterized in that the elements are separate elements made of ceramic ...

Dual riser fluid bed process and reactor

Processes and systems for cracking feeds to produce olefins are provided. The process for cracking feeds can include converting a first feed containing at least about 50 wt % methanol in a first riser under a first set of process conditions to produce a first effluent enriched in ethylene, propylene, or a mixture thereof, wherein the first effluent contains at least about 25 wt % dry basis propylene and converting a second feed containing C 4 -C 10 light hydrocarbons in a second riser under a second set of process conditions to produce a second effluent enriched in ethylene, propylene, or a mixture thereof. The process can also include combining the first effluent with the second effluent to produce a mixed effluent, separating the mixed effluent to produce a coked-catalyst and a gaseous product, regenerating the coked-catalyst, and recycling the regenerated catalyst to the first and second risers.

FLUIDIZED BED REACTOR

The invention relates to a fluidized bed reactor, comprising a reaction chamber and a centrifugal separator having a common wall with the reaction chamber. 1. A fluidized bed reactor , comprising the following features:a) a reactor chamber (R) with at least one outlet port upper part,{'b': 12', '20, 'b) the outlet port () is designed as a tunnel (), allowing a mixture of gas and solid particles, exhausted from the reaction chamber (R), enter an associated centrifugal separator (S),'}{'b': 1', '2, 'c) the centrifugal separator (S) is of cylindrical shape and features an outer paneling (P), a first exit (E) for the purified gas at its top end and a second exit (E) for the a solid particles at its bottom end,'}{'b': 20', '22', '24', '26', '28, 'd) the tunnel () comprises a vertically extending outer side wall (), a vertically extending inner side wall (), a horizontally extending bottom wall () and a horizontally extending ceiling wall (),'}{'b': 22', '20', '30, 'e) the outer side wall () of the tunnel () extends continuously into an entrance section () of the outer paneling (P) of the separator (S),'}{'b': 30', '32', '20, 'f) said entrance section () extends continuously into a first curved section () of the outer paneling (P), which first curved section being arranged at least in an axial projection (arrow AP) of the tunnel (),'}{'b': 32', '34', '36', '38', '40', '24', '20, 'g) said first curved section () is followed by one or more further sections (, , , ) of the paneling (P), which end up at the inner side wall () of the tunnel (), wherein'}{'b': '40', 'h) at least one further section () forms a common wall with reactor chamber (R).'}234363840. The fluidized bed reactor according to claim 1 , wherein one or more of the further sections ( claim 1 , claim 1 , claim 1 , ) of the outer paneling (P) are planar.340. The fluidized bed reactor according to claim 1 , wherein the common wall () is a planar wall.432. The fluidized bed reactor according to claim 1 , wherein ...

PROCESS AND SYSTEM FOR THERMAL TREATMENT OF GRANULAR SOLIDS

The invention relates to a process and the respective installation for thermal treatment of granular solids, in particular for producing aluminum oxide from aluminum hydroxide, wherein the solids are heated in at least one preheating stage and then reacted in a reactor at 700 to 1400° C. In at least one preheating stage, the average temperature gradient of the solids amounts to <15K/s and the dwell time of the solids amounts to ≥15 s. 1. A process for thermal treatment of granular solids , in particular for production of aluminum oxide from aluminum hydroxide , in which the solids are heated in at least one preheating stage and then are reacted in a reactor at 700 to 1400° C. , characterized in that , the average temperature gradient of the solids amounts to <15 K/s and the dwell time of the solids amounts to ≥15 s in at least one preheating stage.2. The process according to claim 1 , characterized in that the solids are heated to 140 to 180° C. in a first preheating stage and/or heated to 200 to 400° C. in a preheating stage downstream from the first preheating stage and/or in the downstream preheating stage claim 1 , the average temperature gradient of the solids amounts to <15 K/s and the dwell time of the solids amounts to >15 s.3. The process according to or claim 1 , characterized in that the average temperature gradient of the solids in the first 10% of the dwell time is above the average temperature gradient over the entire dwell time.4. The process according to claim 3 , characterized in that claim 3 , the average temperature gradient of the solids in the first 10% of the dwell time is more than twice as great as the average temperature gradient over the total dwell time.5. The process according to any one of the preceding claims claim 3 , characterized in that the solids are heated in countercurrent with the heating medium in at least two preheating stages connected after one another.6. The process according to any one of the preceding claims claim 3 , ...

CLC PROCESS AND INSTALLATION WITH THE PRODUCTION OF HIGH PURITY NITROGEN

The invention concerns a CLC process, and its installation, producing high purity dinitrogen, comprising: 1. A process for the combustion of a hydrocarbon feed by chemical looping combustion , in which a redox active mass in the form of particles circulates between at least one reduction zone and two oxidation zones operating in fluidized bed mode , in which:(a) combustion of the hydrocarbon feed is carried out by reduction of the redox active mass brought into contact with the feed in at least one reduction zone;(b) in a first oxidation zone, a first step for oxidation of the reduced redox active mass obtained at the end of step (a) is carried out by being brought into contact with a first fraction of a stream of air depleted in oxygen, in order to produce a stream of dinitrogen comprising a quantity of 100 ppmv or less of dioxygen and a stream of partially re-oxidized redox active mass;(c) in a second oxidation zone, a second step for oxidation of the stream of partially re-oxidized redox active mass obtained at the end of step (b) is carried out, by being brought into contact with air in order to produce a stream of air depleted in oxygen and a stream of re-oxidized redox active mass for use in step (a);(d) the stream of air depleted in oxygen obtained at the end of step (c) is divided in order to form the first fraction of a stream of air depleted in oxygen used in step (b) and a second fraction which is complementary to the stream of air depleted in oxygen extracted from the chemical loop.2. The process as claimed in claim 1 , in which the first fraction of the stream of air depleted in oxygen in step (d) is adjusted to the quantity of reduced redox active mass obtained from step (a) and sent to the first oxidation zone in a manner such as to obtain a stream of dinitrogen comprising a given fraction of dioxygen.3. The process as claimed in claim 1 , in which the stream of dinitrogen contains a quantity of 10 ppmv or less of dioxygen.4. The process as claimed in ...

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.

Method for Producing Hydrocyanic Acid and Device for Producing Hydrocyanic Acid

Provided are a method for producing hydrocyanic acid and a device for producing hydrocyanic acid, which can improve a yield of the hydrocyanic acid in a vapor phase contact ammoxidation reaction of methanol. The method for producing hydrocyanic acid includes a step of obtaining hydrocyanic acid by a vapor phase contact ammoxidation reaction by supplying a raw material gas including methanol in a fluidized bed reactor () through a raw material gas disperser () disposed in the fluidized bed reactor () and bringing the methanol into contact with ammonia and oxygen in the presence of a metal oxide catalyst, in which the raw material gas disperser () has one or more pores for releasing the raw material gas into the fluidized bed reactor (), and the number of pores per unit cross-sectional area of the fluidized bed reactor () is 10 to 45 pieces/m. 1. A method for producing hydrocyanic acid , comprising:{'sup': '2', 'a step of obtaining hydrocyanic acid by a vapor phase contact ammoxidation reaction by supplying a raw material gas containing methanol in a fluidized bed reactor through a raw material gas disperser disposed in the fluidized bed reactor, and bringing the methanol into contact with ammonia and oxygen in the presence of a metal oxide catalyst, wherein the raw material gas disperser has one or more pores for releasing the raw material gas into the fluidized bed reactor, and the number of pores per unit cross-sectional area of the fluidized bed reactor is 10 to 45 pieces/m.'}2. The method for producing hydrocyanic acid according to claim 1 , wherein the number of pores per unit cross-sectional area of the fluidized bed reactor is 20 to 35 pieces/m.3. The method for producing hydrocyanic acid according to claim 1 , wherein a diameter of the pore is 1 to 12 mm.4. The method for producing hydrocyanic acid according to claim 1 , wherein the raw material gas disperser is a pipe type disperser claim 1 , a rectifier pipe is attached to the raw material gas disperser at ...

Process, reactor and system for catalytic cracking of hydrocarbon oils

A process for the catalytic cracking of hydrocarbon oils includes the step of contacting a hydrocarbon oil feedstock with a catalytic cracking catalyst in a reactor having one or more fast fluidized reaction zones for reaction. At least one of the fast fluidized reaction zones of the reactor is a full dense-phase reaction zone, and the axial solid fraction ε of the catalyst is controlled within a range of about 0.1 to about 0.2 throughout the full dense-phase reaction zone. When used for catalytic cracking of hydrocarbon oils, particularly heavy feedstock oils, the process, reactor and system show a high contact efficiency between oil and catalyst, a selectivity of the catalytic reaction, an effectively reduced yield of dry gas and coke, and an improved yield of high value-added products such as ethylene and propylene. 1. A process for the catalytic cracking of hydrocarbon oils , comprising the step of contacting a hydrocarbon oil feedstock , particularly a heavy feedstock oil , with a catalytic cracking catalyst for reaction in a reactor comprising one or more fast fluidized reaction zones , wherein at least one of the fast fluidized reaction zones of the reactor is a full dense-phase reaction zone , and the axial solid fraction ε of the catalyst is controlled within a range of about 0.1 to about 0.2 throughout the full dense-phase reaction zone.2. The process according to claim 1 , which is used for the production of light olefins from heavy feedstock oils claim 1 , and further comprises the steps of:i) contacting the heavy feedstock oil, such as an inferior heavy oil, with the catalytic cracking catalyst in the full dense-phase reaction zone of the reactor for reaction under conditions effective to produce light olefins, wherein the axial solid fraction ε of the catalyst is controlled within a range of about 0.1 to about 0.2 throughout the full dense-phase reaction zone of the reactor;ii) separating the reaction effluent from the reactor to obtain a reaction ...

Ceramic Cyclone for Fluid Catalytic Cracking Unit

The invention relates to a cyclone () for mechanical separation of particles in suspension in a gas, in particular intended for a fluid catalytic cracking unit, said cyclone comprising the following elements: 113.-. (canceled)14. A cyclone for mechanical separation of particles in suspension in a gas , in particular intended for a fluid catalytic cracking unit , said cyclone comprising the following elements:a separation chamber,an inlet duct that opens into the chamber,a gas outlet duct located in the upper portion of the chamber and{'sub': 4', '3', '4', '2', '3, 'a particle outlet duct located in the lower portion of the chamber, characterized in that each element of the cyclone is made of a ceramic material and the ceramic material comprises a ceramic matrix selected from the group consisting of silicon carbide SiC, boron carbide BC, silicon nitride SiN, aluminum nitride AlN, boron nitride BN, alumina AlO, and mixtures thereof, wherein the ceramic matrix comprises carbon fibres or ceramic fibres.'}15. The cyclone according to claim 14 , characterized in that the ceramic fibres are selected from the group consisting of crystalline alumina fibres claim 14 , mullite fibres claim 14 , crystalline or amorphous silicon carbide fibres claim 14 , zirconia fibres claim 14 , silica-alumina fibres claim 14 , and mixtures thereof16. The cyclone according to claim 14 , characterized in that the ceramic material is a sintered ceramic material.17. The cyclone according to claim 14 , characterized in that the ceramic material is a Ceramic Matrix Composite (CMC).18. The cyclone according to claim 14 , characterized in that the elements of the cyclone form one and the same part made of ceramic material.19. The cyclone according to claim 14 , characterized in that the elements of the cyclone are separate elements made of ceramic material that are assembled together claim 14 , each separate element being made of one part or being made of several portions assembled together.20. The ...

INTERNAL LOOP AIRLIFT REACTOR FOR PROCESS INTENSIFICATION INTEGRATING REACTION AND SEPARATION

An internal loop airlift reactor (ILAR) for process intensification integrating reaction and separation includes a riser, a downcomer, a hydrocyclone, internals preventing occurrence of dead zone, a gas guide cone, vent holes, and a gas-liquid integrated distributor. The hydrocyclone is arranged at the bottom of the ILAR downcomer; the gas guide cone and the vent holes in the downcomer prevent the gas from entering the hydrocyclone; after the slurry enters the hydrocyclone, the solid-containing slurry enters the riser again from the hydrocyclone underflow, and the solid-free clean product flows out through the hydrocyclone overflow. The ILAR in the present invention has a simple structure and low cost and requires no special liquid-solid separation device. It can achieve gas-liquid-solid three-phase reaction, interphase mass transfer, and solid-liquid separation simultaneously, and is suitable for a gas-liquid-solid three-phase reaction in which the catalyst is solid particles. 1. An internal loop airlift reactor for process intensification integrating reaction and separation , comprising a riser , a downcomer , a solid feed inlet , a hydrocyclone inlet , internals preventing the occurrence of dead zone , a liquid inlet , a gas inlet , a gas outlet , a draft tube , a gas guide cone , vent holes , an overflow pipe , a hydrocyclone , an underflow pipe , a gas-liquid integrated distributor and a liquid outlet , wherein the riser and the downcomer are separated by the draft tube; the solid feed inlet is disposed on a side wall of the reactor; the liquid inlet and the gas inlet are disposed at the bottom of the reactor; the gas outlet is disposed at the top of the reactor; a liquid outlet connects the hydrocyclone and the overflow pipe and introduces the clear liquid to the outside of the reactor; the hydrocyclone is arranged at the lower part of the downcomer; the space between a upper surface of a cylindrical segment of the hydrocyclone and a wall of the downcomer is ...

PARTICLE SETTING DEVICES

The present disclosure relates to settling devices for separating particles from a bulk fluid with applications in numerous fields. The particle settling devices of the present disclosure may include a stack of truncoconical cones that may be arranged in opposite orientation, apex to base. Other embodiments include several concentric vertical tubes attached to conical surfaces at the bottom, with inclined settling strips attached to the vertical tubes in annular regions between the tubes. These devices are useful for separating small (millimeter or micron sized) particles from a bulk fluid with applications in numerous fields, such as biological (microbial, mammalian, plant, insect or algal) cell cultures, solid catalyst particle separation from a liquid or gas and waste water treatment. 1. A particle settling device comprising: a first conical portion;', 'a second conical portion;', 'a cylindrical portion located between the first and second conical portions;', 'at least one inlet for introducing liquids into the cyclone housing;', 'a first outlet port in the first conical portion for harvesting a clarified liquid;', 'a second outlet port in the second conical portion for harvesting a concentrated liquid; and', 'a first stack of cones located within the cyclone housing and occupying the first conical portion and at least part of the cylindrical portion, each cone of the first stack of cones including a truncated apex oriented towards the first outlet port and an open base oriented towards the second outlet port, the first stack of cones generally centered around a substantially central opening formed by the truncated apex in each cone of the first stack of cones., 'a cyclone housing including2. The device of claim 1 , wherein at least one cone in the first stack of cones is composed of a metal or a plastic.3. The device of claim 1 , wherein at least one cone in the first stack of cones is composed at least partially of stainless steel.4. The device of claim 1 , ...

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. 120.-. (canceled)21. An apparatus for producing a multimodal polyolefin , comprising:a first reactor configured to produce a first polyolefin; a riser configured to produce the second polyolefin;', 'an upper conduit having an end fluidly connected to a top portion of the riser;', 'a separator fluidly connected to an opposite end of the upper conduit;', 'a downcomer configured to produce the third polyolefin, wherein a top portion of the downcomer is fluidly connected to the separator, optionally via a liquid barrier in the top portion of the downcomer; and', 'a lower conduit having an end fluidly connected to a bottom portion of the downcomer and an opposite end fluidly connected to a bottom portion of the riser,, 'a second reactor configured to produce a second polyolefin and a third polyolefin, where the second reactor comprises the second reactor is configured to receive the first polyolefin from the first reactor, or,', 'the first reactor is configured to receive the second polyolefin and the third polyolefin from the second reactor., 'wherein22. The apparatus of claim 21 , further comprising:a heat apparatus configured to add or remove heat from the downcomer.23. The apparatus of claim 21 , wherein the second reactor further comprises:a first elbow connector connected to the bottom portion of the riser and to the opposite end of the lower conduit;a second elbow connector connected to the top portion of the riser and to the end of the upper conduit; anda third elbow connector connected to the bottom ...

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.

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. 15-. (canceled)6. A trimodal polyethlene 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 e molecular weight of the IMW component; and wherein the trimodal polyethylene resin has a strain hardening modulus of from about 50 MPa to about 90 MPa , when tested in accordance with ISO 18488-2015(E) ,wherein (A1) the HMW component is present in an amount of from about 10 wt. % to about 60 wt. %; (A2) the HMW component has weight average molecular weight of great than about 350 kg/mol; or (A3) both the HMW component is present in an amount of from about 10 wt. % to about 60 wt. %, and the HMW component has weight average molecular weight of greater than about 350 kg/mol;wherein the trimodal polyethylene resin is characterized by (B1) a short chain branching content in the LMW component of ...

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. 18-. (canceled)9. 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 LMW 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/mmol 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; and wherein the trimodal polyethylene resin has a tensile strength in the machine direction (MD) of greater than about 13 ,000 psi (89.6 MPa) , when tested in accordance with ASTM D638 at 90 MPa;wherein (A1) the HMW component is present in an amount of from about 10 wt. % to about 60 wt. %; (A2) the HMW component has weight average molecular weight of greater than about 350 kg/mol; or (A3) both the HMW component is present in an amount of from about 10 wt. % to about 60 wt. %, and the HMW component has weight average molecular weight of greater than about 350 kg/mol;wherein the trimodal polyethylene resin is characterized by (B1) a short chain branching ...

FLUID CATALYTIC CRACKING PROCESS AND APPARATUS FOR MAXIMIZING LIGHT OLEFIN YIELD AND OTHER APPLICATIONS

Apparatus and processes herein provide for converting hydrocarbon feeds to light olefins and other hydrocarbons. The processes and apparatus include, in some embodiments, feeding a hydrocarbon, a first catalyst and a second catalyst to a reactor, wherein the first catalyst has a smaller average particle size and is less dense than the second catalyst. A first portion of the second catalyst may be recovered as a bottoms product from the reactor, and a cracked hydrocarbon effluent, a second portion of the second catalyst, and the first catalyst may be recovered as an overhead product from the reactor. The second portion of the second catalyst may be separated from the overhead product, providing a first stream comprising the first catalyst and the hydrocarbon effluent and a second stream comprising the separated second catalyst, allowing return of the separated second catalyst in the second stream to the reactor. 143.-. (canceled)44. (canceled)45. (canceled)46. (canceled)47. (canceled)48. (canceled)49. (canceled)50. (canceled)51. (canceled)52. (canceled)53. A process for the conversion of hydrocarbons , comprising:regenerating a catalyst mixture comprising a first catalyst and a second particle in a regenerator, wherein the first catalyst has a smaller average particle size and/or is less dense than the second particle, and wherein the second particle may be catalytic or non-catalytic;feeding the catalyst mixture and hydrocarbons to a riser reactor to convert at least a portion of the hydrocarbons and recover a first effluent comprising the catalyst mixture and converted hydrocarbons;feeding the catalyst mixture to a second reactor;feeding a hydrocarbon feedstock to the second reactor and fluidizing the catalyst mixture;recovering an overhead product from the second reactor comprising the second particle, the first catalyst, and a reacted hydrocarbon product;separating the second particle from the overhead product to provide a first stream comprising the first ...

DEVICE FOR INJECTING FLUIDS INTO THE FREE AREA OF A ROTATING FLUIDISED BED

Device for injecting fluids into the free area of a rotating fluidized bed revolving in a fixed cyclone chamber, and method using this device, comprising a device for tangentially injecting secondary fluids, enabling rotating rings of fluids to be formed in said free area along the side walls of said cyclone chamber, in order to separate from said side walls fluid flows exiting along said side walls and accelerate their rotation velocity, and thus to improve the retention of the solid particles entrained by said exiting fluid flows 14355772737. A device for injecting secondary fluids into the free area of a rotating fluidized bed in a fixed cyclone chamber , comprising a peripheral wall () surrounded by two side walls () and (); a device for supplying fluid () through openings () distributed along said peripheral wall , in a mainly tangential direction (); a device for supplying and discharging solid particles; and at least one central tube () for discharging the fluids revolving in said cyclone chamber , characterized in that it comprises:{'b': 17', '17', '1', '15', '15', '1', '3', '5', '18', '18', '1', '19', '19', '1', '3', '5, 'a device for supplying secondary fluids () and (.) through central supply chambers () and (.) located along each of said side walls () and (), having injection openings () and (.) distributed around the axis of cylindrical symmetry, enabling said secondary fluids to be injected in a mainly tangential direction () and (.), in order to form two rotating rings of secondary fluids revolving around said axis of cylindrical symmetry, along said side walls () and (), within said free area, and in that said devices for supplying said secondary fluids enable said secondary fluids to be supplied at a sufficient pressure to make said rotating rings of secondary fluids revolve at a velocity which is greater than the highest rotation velocity of said fluids revolving in cyclone chamber when the latter is in operation without the device for injecting ...

INTEGRATED C3-C4 HYDROCARBON DEHYDROGENATION PROCESS

An integrated process for producing C3-C4 olefins or di-olefins including: contacting a hydrocarbon feed and a catalyst feed in a fluidized dehydrogenation reactor under conditions such that a product mixture is formed and the catalyst is at least partially deactivated; transferring the product mixture and the catalyst from the reactor to a cyclonic separation system under conditions such that the product mixture is converted to form a new product mixture and is separated from the catalyst; transferring at least a portion of the catalyst to a regenerator vessel and heating it in order to combust the coke deposited thereon; subjecting the catalyst to a conditioning step to form an oxygen-containing, at least partially reactivated catalyst; and transferring the partially reactivated catalyst back to the fluidized dehydrogenation reactor. 1. An integrated process for producing C3-C4 olefins or C3-C4 di-olefins comprising the steps of:{'b': '1', 'claim-text': (i) a C3-C4 hydrocarbon feed and', '(ii) a catalyst feed comprising a catalyst;', 'under conditions such that a step (1)(a) product mixture, comprising a C3-C4 target olefin or di-olefin, hydrogen and unreacted C3-C4 hydrocarbon feed, is formed;, '() (a) contacting, in a fluidized dehydrogenation reactor,'} 'the catalyst has coke deposited thereon and is at least partially deactivated such that it forms an at least partially deactivated catalyst; and', 'and'}(b) transferring the step (1)(a) product mixture and the at least partially deactivated catalyst from the fluidized dehydrogenation reactor to a cyclonic separation system, andunder conditions such that the step (1)(a) product mixture is converted to form a step (1)(b) product mixture; andthereafter substantially separating the step (1)(b) product mixture and the at least partially deactivated catalyst from each other;(c) transferring at least a portion of the at least partially deactivated catalyst to a regenerator vessel and heating the at least partially ...

PARTICLE DISENGAGEMENT DEVICE

A particle disengagements device comprising a baffle plate, wherein the baffle plate comprises one or more guide baffles and one or more separation baffles, wherein the one or more guide baffles and the one or more separation baffles define one or more air flow paths and one or more solid flow paths and associated systems and methods. 1. A vessel comprising:a fluidized bed;one or more cyclones; and a circular baffle plate,', 'wherein the baffle plate comprises one or more guide baffles and one or more separation baffles,', 'wherein the one or more guide baffles and the one or more separation baffles define one or more air flow paths and one or more solid flow paths;', 'wherein the one or more guide baffles and the one or more separation baffles each comprise a protrusion having a length in the range of from 0.1 to 8 inches;', 'wherein the one or more guide baffles are spaced apart a distance in the range of from 4 inches to 25 inches; and', 'wherein the one or more separation baffles are spaced apart a distance in the range of from 4 inches to 25 inches., 'a particle disengagement device comprising'}2. The vessel of claim 1 , wherein the one or more cyclones comprise one or more primary cyclones and one or more secondary cyclones.3. The vessel of claim 2 , wherein the one or more cyclones comprise one or more diplegs.4. The vessel of claim 3 , wherein the one or more diplegs extend through the particle disengagement device.5. A method comprising:providing a vessel, wherein the vessel comprises fluidized bed, one or more cyclones, and a particle disengagement device, wherein the particle disengagement device is disposed within the vessel at an elevation above the fluidized bed and below a portion of the one or more cyclones; andintroducing a gas/solid feed into the vessel.6. The method of claim 5 , further comprising removing solids from the gas/solid feed. This application is a divisional of U.S. PCT application Ser. No. 15/776657, filed Nov. 22, 2016, which claims ...

DEVICE AND METHOD FOR COOLING OR HEATING A FINE-GRAINED SOLID

A device for cooling a fine-grained solid includes a fluidized bed cooler/heater in which the solid is fluidized with a fluidizing gas and thereby releases energy in the form of heat within the cooler/heater at least two cyclones which are connected in parallel. The cyclones are arranged such that after the fluidization of the solid the fluidizing gas passes through the cyclones so contained particles are removed. 110.-. (canceled)11. A device for cooling a fine-grained solid , comprising a fluidized bed cooler/heater in which the solid is fluidized with a fluidizing gas and thereby releases energy in the form of heat , wherein at least two cyclones connected in parallel are provided within the cooler/heater , whereby the cyclones are arranged such that after the fluidization of the solid the fluidizing gas passes through the cyclones so contained particles are removed wherein all cyclones connected in parallel have a common outlet leg for withdrawing the particles from the fluidized bed cooler/heater.12. The device according to claim 11 , wherein the fluidized bed cooler/heater is divided into at least two different segments which are in fluidic contact with one another.13. The device according to claim 11 , wherein at least one cyclone has a tangential inlet.14. The device according to claim 11 , wherein the common outlet leg features additional nozzles for fluidizing the separated particles.15. The device according to claim 11 , wherein the outlet leg opens into a collecting container.16. The device according to claim 11 , wherein the outlet leg opens into a fluidized bed.17. The device according to claim 11 , wherein the outlet leg opens into the fluidized bed of the fluidized bed cooler/heater established therein during operation.18. The device according to claim 11 , wherein the out-let leg opens into a seal pot.19. The device according to claim 11 , wherein the outlet leg has a flap. The invention belongs to a device and its relating method for cooling or ...

SYSTEMS AND METHODS FOR REDUCING HEAT EXCHANGER FOULING RATE

Methods of reducing heat exchanger fouling rate or of producing polyolefins may include providing a first gas stream comprising a gas and entrained fine polyolefin particles to a gas outlet line; removing a portion of the entrained fine polyolefin particles from the gas outlet line to form a bypass stream; and providing the bypass stream to a bypass line comprising a bypass line inlet and a bypass line outlet. The bypass line inlet and outlet are located upstream and downstream of a first heat exchanger. The methods may further include providing at least a portion of the first gas stream to the first heat exchanger; and combining the bypass stream and a second gas stream at the bypass line outlet to form a combined gas stream comprising one or more olefins or paraffins. A temperature of the combined gas stream is below the dew point of the combined gas stream. 1. A method of reducing heat exchanger fouling rate , the method comprising:providing a first gas stream comprising a gas and entrained fine polyolefin particles to a gas outlet line;removing a portion of the entrained fine polyolefin particles from the gas outlet line to form a bypass stream comprising a higher concentration of the entrained fine polyolefin particles than is present in the first gas stream;providing the bypass stream to a bypass line comprising a bypass line inlet and a bypass line outlet, wherein the bypass line inlet is located upstream of a first heat exchanger, and wherein the bypass line outlet is located downstream of the first heat exchanger;providing at least a portion of the first gas stream to the first heat exchanger, which produces a first cooled gas stream; andcombining the bypass stream and a second gas stream at the bypass line outlet to form a combined gas stream comprising one or more olefins or paraffins, wherein a temperature of the combined gas stream is below the dew point of the combined gas stream.2. The method of claim 1 , wherein the first gas stream comprises one or ...

Oil separator

A centrifugal-separation type oil separator includes a cylindrical separator body, and an inflow pipe arranged to introduce a fluid including an oil into the separator body. The inflow pipe includes a curved portion. A peripheral wall of the separator body and the inflow pipe include a common portion common to each other.

Methods of Polyolefin Solids Recovery

Methods for separating gaseous components, such as unreacted hydrocarbon monomer and/or solvent, from polyolefin solids are provided. The methods include contacting a first stream including polyolefin solids and gaseous unreacted hydrocarbon monomer and/or solvent with a first purge gas in a gas-solid separation vessel to separate the gaseous unreacted hydrocarbon monomer and/or solvent from the polyolefin solids to produce a second stream including polyolefin solids substantially free of gaseous unreacted hydrocarbon monomer and/or solvent and a third stream including the gaseous unreacted hydrocarbon monomer and/or solvent. The first purge gas includes hydrocarbon monomer and/or solvent and has a temperature of at least about 70° C. when entering the gas-solid separation vessel. Systems for carrying out such methods are also provided.

Process for continuous polymerization of olefin monomers in a reactor

The invention relates to a process and system for the continuous polymerization of one or more α-olefin monomers comprising the steps of: (a) withdrawing fluids from a reactor (b) cooling fluids comprising the withdrawn fluids with a cooling unit (c) introducing the cooled fluids to a separator to separate at least part of the liquid from these fluids to form a liquid phase and a gas/liquid phase (d) introducing the gas/liquid phase below to the reactor below a distribution plate (e) introducing the liquid phase to a settling tank to separate liquid from fines that settle down in the settling tank (f) introducing liquid from the settling tank up stream of the cooling unit.

Activation of Waste Metal Oxide as an Oxygen Carrier for Chemical Looping Combustion Applications

A process for producing black powder oxygen carriers for use in a chemical looping combustion unit includes the steps of: (a) removing and collecting the black powder waste material that was formed in a gas pipeline; (b) pre-treating the collected black powder to adjust its spherical shape to avoid attrition and fines production; and (c) activating the black powder to increase its reactivity rate and produce the black powder oxygen carrier that is suitable for use in the chemical looping combustion process as an oxygen carrier. 1. A process for producing an oxygen carrier that is suitable for use in a chemical looping combustion unit , comprising the steps of;removing and collecting black powder that is formed within a gas pipeline;pre-treating the collected black powder; andactivating the collected black powder to increase the reactivity of the black powder to form a black powder oxygen carrier for use in the chemical looping combustion unit.2. The process of claim 1 , wherein the black powder comprises iron hydroxides claim 1 , iron oxides claim 1 , and iron carbonates.3. The process of claim 1 , wherein the black powder is removed from a natural gas pipeline and collected using at least one of a separator and cyclone device such that gas laden with black powder passes through the separator or cyclone claim 1 , and black powder particles are knocked out of the gas stream to walls of the separator or cyclone claim 1 , where they fall and are collected internally within the separator or cyclone in a collection media.4. The process of claim 1 , wherein the collected black powder is pre-treated via a synthesis method.5. The process of claim 4 , wherein the synthesis method consists one of a spray drying process and a freeze granulation process.6. The process of claim 4 , wherein the synthesis method comprises the steps of:forming a powder mixture that comprises about 60.1% black powder and about 39.9% manganese ore; homogenizing the aqueous suspension;', 'spray drying ...

Process and apparatus for distributing fluidizing gas to an fcc riser

A process and apparatus described is for distributing fluidizing gas to a riser. Fluidizing gas is delivered to a plenum below the riser. A first stream of fluidizing gas is distributed from the plenum into a chamber in a riser and a second stream of fluidizing gas is distributed from the plenum into the riser outside of the chamber. First nozzles in the plenum have a first outlet in the chamber and second nozzles in the plenum have a second outlet outside of the chamber. Streams of regenerated catalyst and carbonized catalyst may be passed to the riser and mixed around the chamber in a lower section of a riser.

FLUID CATALYTIC REACTORS WHICH INCLUDE FLOW DIRECTORS

According to one or more embodiments, a fluid catalytic reactor may include a riser, a lower reactor portion, a transition portion, and a flow director. The riser may include a cross-sectional area, and the lower reactor portion may include a cross-sectional area. The transition portion may attach the riser to the lower reactor portion. The cross-sectional area of the riser may be less than the cross-sectional area of the lower reactor portion such that the transition portion is tapered inward from the lower reactor portion to the riser. The flow director may be positioned at least within an interior region of the transition portion. The flow director may include a body which affects the velocity profile of fluids moving from the lower reactor portion to the riser. 1. A fluid catalytic reactor comprising:a riser comprising cross-sectional area;a lower reactor portion comprising a cross-sectional area;a transition portion attaching the riser to the lower reactor portion, wherein the cross-sectional area of the riser is less than the cross-sectional area of the lower reactor portion such that the transition portion is tapered inward from the lower reactor portion to the riser; anda flow director positioned at least within an interior region of the transition portion, wherein the flow director affects the velocity profile of fluids moving from the lower reactor portion to the riser.2. The fluid catalytic reactor of claim 1 , wherein the flow director fills at least 10% of a volume of the transition portion.3. The fluid catalytic reactor of claim 1 , wherein the flow director fills at least 20% of a volume of the transition portion.4. The fluid catalytic reactor of claim 1 , wherein the flow director fills from 20% to 45% of a volume of the transition portion.5. The fluid catalytic reactor of claim 1 , wherein the flow director comprises a conical structure.6. The fluid catalytic reactor of claim 1 , wherein the flow director comprises a frustum structure.7. The fluid ...

TURBULENT FLUIDIZED-BED REACTOR, DEVICE, AND METHOD USING OXYGEN-CONTAINING COMPOUND FOR MANUFACTURING PROPENE AND C4 HYDROCARBON

A turbulent fluidized-bed reactor, device and method for preparing propylene and C4 hydrocarbons from oxygen-containing compounds. The device includes the turbulent fluidized-bed reactor and a fluidized-bed regenerator for regenerating a catalyst. The method includes: a) feeding a raw material containing the oxygen-containing compounds from n reactor feed distributors to a reaction zone of the turbulent fluidized-bed reactor, and contacting the raw material with a catalyst, to generate a stream containing target product and a spent catalyst containing carbon; b) sending the stream discharged into a product separation system, obtaining propylene, C4 hydrocarbons, light fractions and the like after separation, returning 70 wt. % or more of the light fractions to the reaction zone of the turbulent fluidized-bed reactor from the reactor feed distributor, and reacting ethylene and the oxygen-containing compounds to perform an alkylation reaction in presence of the catalyst, to produce products of propylene and the like. 115-. (canceled)16. A turbulent fluidized-bed reactor for preparing propylene and C4 hydrocarbons from oxygen-containing compounds , comprising:a reactor shell, one or more reactor feed distributors, a first reactor gas-solid separator, a second reactor gas-solid separator, a reactor heat extractor, a product gas outlet and a reactor stripper, wherein the lower part of the turbulent fluidized-bed reactor is a reaction zone, the upper part of the turbulent fluidized-bed reactor is a settling zone, the one or more reactor feed distributors are disposed in the reaction zone, the reactor heat extractor is disposed in the reaction zone, the first reactor gas-solid separator and the second reactor gas-solid separator are placed in the settling zone or outside the reactor shell, the first reactor gas-solid separator is equipped with a regenerated catalyst inlet, the catalyst outlet of the first reactor gas-solid separator is located at the bottom of the reaction ...

GAS-PHASE PROCESS FOR PREPARING ETHYLENE POLYMERS

A process for preparation of an ethylene polymer in a gas-phase polymerization unit comprising a gas-phase polymerization reactor by homopolymerizing ethylene or copolymerizing ethylene and one or more C-C-1-alkenes in a reaction gas made from or containing propane as polymerization diluent in the presence of a pre-activated polymerization catalyst, wherein a purified propane feed stream made from or containing at least 99 mol % propane and from 0.1 to 100 ppm mol propylene is fed to the gas-phase polymerization unit. 1. A process for the preparation of an ethylene polymer , comprising the step of{'sub': 4', '12, 'forming an ethylene polymer in particle form in a gas-phase polymerization unit comprising a gas-phase polymerization reactor by homopolymerizing ethylene or copolymerizing ethylene and one or more C-C-1-alkenes at temperatures from 20 to 200° C. and pressures of from 0.5 to 10 MPa in a reaction gas comprising propane as polymerization diluent in the presence of a pre-activated polymerization catalyst,'}wherein a purified propane feed stream comprising at least 99% mol propane and not more than 100 ppm-mol propylene is fed to the gas-phase polymerization unit and the purification has been carried out by passing a hydrocarbon stream through hydrocarbon purification units which reduce at least the concentration of propylene, acetylene, carbon monoxide, carbon dioxide, oxygen and water contained in the hydrocarbon stream.2. The process of claim 1 , wherein the purified propane feed stream fed to the gas-phase polymerization unit comprises not more than 0.03 ppm-mol carbon monoxide claim 1 , not more than 0.4 ppm-mol carbon dioxide claim 1 , not more than 2.0 ppm-mol oxygen claim 1 , not more than 3.0 ppm-mol acetylene claim 1 , and not more than 2.0 ppm-mol water.3. The process of claim 1 , wherein the pre-activation of the polymerization catalyst is carried out by contacting claim 1 , in liquid propane as diluent claim 1 , a solid catalyst component with an ...

Systems and Methods for Renewable Fuel

The present application generally relates to the introduction of a renewable fuel oil as a feedstock into refinery systems or field upgrading equipment. For example, the present application is directed to methods of introducing a liquid thermally produced from biomass into a petroleum conversion unit; for example, a refinery fluid catalytic cracker (FCC), a coker, a field upgrader system, a hydrocracker, and/or hydrotreating unit; for co-processing with petroleum fractions, petroleum fraction reactants, and/or petroleum fraction feedstocks and the products, e.g., fuels, and uses and value of the products resulting therefrom. 1. A fuel , comprising:a product of a fluidized catalytic cracker having a petroleum fraction and a renewable fuel oil as reactants.2. The fuel of claim 1 , wherein the fuel comprises a product of a fluidized catalytic cracker co-processing a petroleum fraction and a renewable fuel oil.3. The fuel according to claim 1 , wherein the fuel comprises a fuel composition derived from:i) 80-99.95 wt. % of the petroleum fraction feedstock; andii) 0.05-20 wt. % of the renewable fuel oil feedstock.4. The fuel according to claim 1 , wherein the prepared fuel is a transportation fuel.5. The fuel according to claim 1 , wherein the renewable fuel oil is derived from a cellulosic biomass.6. The fuel according to claim 1 , wherein the renewable fuel oil is an unenriched renewable fuel oil.71. The fuel according to claim wherein the renewable fuel oil has a pH in the range of 0.5 to 7.8. The fuel according to claim 1 , wherein the renewable fuel oil has a water content in the range of between 10-40 wt. %.9. The fuel according to claim 1 , wherein the renewable fuel oil has in the range of between 35-80 wt. % carbon content and in the range of between 20-50 wt. % oxygen content claim 1 , on a dry basis or moisture-free basis.10. A method of preparing a fuel claim 1 , comprising:processing a petroleum fraction feedstock with a renewable fuel oil feedstock in the ...

Apparatuses and Methods for Controlling Heat for Rapid Thermal Processing of Carbonaceous Material

Embodiments of apparatuses and methods for controlling heat for rapid thermal processing of carbonaceous material are provided herein. The apparatus comprises a reheater for containing a fluidized bubbling bed comprising an oxygen-containing gas, inorganic heat carrier particles, and char and for burning the char into ash to form heated inorganic particles. An inorganic particle cooler is in fluid communication with the reheater to receive a first portion of the heated inorganic particles. The inorganic particle cooler is configured to receive a cooling medium for indirect heat exchange with the first portion of the heated inorganic particles to form first partially-cooled heated inorganic particles that are fluidly communicated to the reheater and combined with a second portion of the heated inorganic particles to form second partially-cooled heated inorganic particles. A reactor is in fluid communication with the reheater to receive the second partially-cooled heated inorganic particles.