Настройки

Укажите год
-

Небесная энциклопедия

Космические корабли и станции, автоматические КА и методы их проектирования, бортовые комплексы управления, системы и средства жизнеобеспечения, особенности технологии производства ракетно-космических систем

Подробнее
-

Мониторинг СМИ

Мониторинг СМИ и социальных сетей. Сканирование интернета, новостных сайтов, специализированных контентных площадок на базе мессенджеров. Гибкие настройки фильтров и первоначальных источников.

Подробнее

Форма поиска

Поддерживает ввод нескольких поисковых фраз (по одной на строку). При поиске обеспечивает поддержку морфологии русского и английского языка
Ведите корректный номера.
Ведите корректный номера.
Ведите корректный номера.
Ведите корректный номера.
Укажите год
Укажите год

Применить Всего найдено 6169. Отображено 200.
10-03-2008 дата публикации

СПОСОБ И УСТРОЙСТВО ДЛЯ УМЕНЬШЕНИЯ СОДЕРЖАНИЯ NOxИ N2O В ГАЗАХ

Номер: RU2318581C2
Принадлежит: УДЕ ГМБХ (DE)

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

Подробнее
04-08-2020 дата публикации

НОВЫЙ СПОСОБ ПРОИЗВОДСТВА МЕТАНОЛА ИЗ НИЗКОКАЧЕСТВЕННОГО СИНТЕТИЧЕСКОГО ГАЗА

Номер: RU2729077C2
Принадлежит: ХАЛЬДОР ТОПСЕЭ А/С (DK)

Настоящее изобретение относится к способу производства метанола из синтетического газа, а также к компоновке реактора для его осуществления. Способ включает следующие стадии: - предоставление свежего сжатого газа для синтеза метанола, содержащего водород, монооксид углерода и диоксид углерода, который предварительно нагревают и пропускают через адиабатический метанольный предварительный конвертер/предохранительный реактор, в котором синтетический газ частично конвертируют в метанол в присутствии гетерогенного метанольного катализатора, а ядовитые примеси из подаваемого газа удаляют, - предоставление рециркуляционного газового потока из схемы синтеза, содержащего частично конвертированный газ для синтеза метанола, и смешивание части рециркуляционного газового потока со свежим синтетическим газом, если это необходимо, как в случае частичной загрузки, с получением потока технологического газа, - охлаждение потока технологического газа из предварительного конвертера/предохранительного реактора ...

Подробнее
17-03-2020 дата публикации

Способ модернизации аммиачного конвертера

Номер: RU2717062C2
Принадлежит: КАСАЛЕ СА (CH)

Изобретение относится к модернизации многослойного аммиачного конвертера с промежуточным охлаждением. Описан способ модернизации многослойного аммиачного конвертера (1), содержащего несколько адиабатических каталитических слоев, включая первый каталитический слой (3) и один или более последующих каталитических слоев (4, 5), расположенных друг за другом, так чтобы исходящий поток слоя далее вступал в реакцию в последующем слое; по меньшей мере первый межслойный теплообменник (6), размещенный между первым каталитическим слоем (3) и вторым каталитическим слоем (4) для охлаждения исходящего потока первого слоя перед его пропуском во второй слой, и, по выбору, следующий межслойный теплообменник(и) (7), размещенный(ые) между последующими слоями, при этом способ отличается тем, что преобразуют первый каталитический слой (3) в изотермический каталитический слой. Также описан многослойный аммиачный конвертер. Технический результат: увеличение конверсионного выхода и/или производительности конвертера ...

Подробнее
15-06-2017 дата публикации

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

Номер: RU2622442C2

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

Подробнее
11-08-2021 дата публикации

СПОСОБ И УСТРОЙСТВО ДЛЯ ПРОВЕДЕНИЯ ЭНДОТЕРМИЧЕСКИХ ГАЗОФАЗНЫХ ИЛИ ГАЗ-ТВЕРДОТЕЛЬНЫХ РЕАКЦИЙ

Номер: RU2752976C2
Принадлежит: БАСФ СЕ (DE)

Группа изобретений относится к реактору и способу проведения эндотермических газофазных или газ-твердотельных реакций. Способ включает проведение эндотермической реакции на стадии образования продукта в первой зоне реактора, зоне образования продукта, заполненной предварительно нагретыми частицами твердого вещества, выведение потока газа, содержащего продукт и его пропускание через вторую зону реактора, зону рекуперации тепла, причем тепло потока газа, содержащего продукт, накапливается в неподвижном слое, введение тепла в зоне нагрева, которая расположена между зоной образования продукта и зоной рекуперации тепла, пропускание продувочного газа в том же направлении на стадии очистки и пропускание газа в фазе регенерации в обратном направлении, при этом способ проводят циклически. Предложенная концепция способа проведения реакций предоставляет возможность режима работы с интегрированным обратным теплообменом, исключает использование арматуры в горячей области технологического пространства ...

Подробнее
19-07-2017 дата публикации

РАСПРЕДЕЛИТЕЛЬНОЕ УСТРОЙСТВО ДЛЯ МНОГОСЛОЙНОГО РЕАКТОРА С НИСХОДЯЩИМ ПОТОКОМ

Номер: RU2625854C2

Изобретение относится к распределительному устройству для распределения жидкости и газа в многослойном реакторе с нисходящим потоком, реактору, содержащему такое распределительное устройство, к использованию таких распределительного устройства и реактора при обработке углеводородов и к способу распределения жидкости и газа в многослойном реакторе. Распределительное устройство содержит по существу горизонтально расположенную сборную тарелку, содержащую центральное проходное отверстие для газа и проходные отверстия для жидкости, расположенные вокруг центрального отверстия, завихритель, размещенный над сборной тарелкой вокруг центрального отверстия и содержащий лопатки, задающие направление завихрения потока и расположенные с возможностью придания вращательного движения газу, проходящему через центральное отверстие так, что газ выходит из центрального отверстия в виде вихря, закрученного в направлении завихрения вокруг вертикальной оси завихрения, одно или большее число эжекционных сопел, ...

Подробнее
27-02-2013 дата публикации

ФИЛЬТРУЮЩАЯ ТАРЕЛКА ПРЕДВАРИТЕЛЬНОГО РАСПРЕДЕЛЕНИЯ С ПЕРЕЛИВНОЙ ТРУБОЙ ДЛЯ РЕАКТОРА С НЕПОДВИЖНЫМ СЛОЕМ И ПАРАЛЛЕЛЬНЫМИ НИСХОДЯЩИМИ ПОТОКАМИ ГАЗА И ЖИДКОСТИ

Номер: RU2476255C2
Принадлежит: ИФП (FR)

Устройство, описанное в настоящем изобретении, позволяет осуществить предварительное распределение исходных потоков газа и жидкости, поступающих в реактор, работающий по принципу параллельных нисходящих потоков газа и жидкости. Это достигается посредством тарелки предварительного распределения, содержащей фильтрующую среду и переливную трубу, позволяющую регулировать расход жидкости, поступающей на распределительную тарелку, расположенную на выходе устройства. Данное устройство более предпочтительно применяется при обработке селективным гидрированием исходных смесей, содержащих соединения ацетиленового и диенового рядов. 2 н. и 1 з.п. ф-лы, 3 ил., 1 табл.

Подробнее
20-07-2012 дата публикации

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

Номер: RU2456067C2
Принадлежит: БАСФ СЕ (DE)

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

Подробнее
10-03-2012 дата публикации

СПОСОБ РЕАЛИЗУЕМОГО В НЕПРЕРЫВНОМ РЕЖИМЕ ДЛИТЕЛЬНОГО ГЕТЕРОГЕННО КАТАЛИЗИРУЕМОГО ЧАСТИЧНОГО ДЕГИДРИРОВАНИЯ УГЛЕВОДОРОДОВ

Номер: RU2444400C2
Принадлежит: БАСФ СЕ (DE)

Изобретение относится к способу гетерогенно катализируемого частичного дегидрирования углеводорода. Способ заключается в том, что поток реакционной газовой смеси, который содержит углеводород в исходном молярном количестве KW, пропускают через совокупный слой катализатора, состоящий из нескольких отдельных слоев, в суммарном количестве М, так чтобы в рабочий момент t0 при прохождении потока через первую треть количества М в дегидрированный углеводород превращалась доля А исходного количества KW, через вторую треть превращалась доля В и через третью треть превращалась доля С, при условии, что А>В>С. Причем в поток между его входом в совокупный слой катализатора и выходом из него при необходимости вводят вспомогательные газы дегидрирования. Деактивированию совокупного слоя катализатора, происходящему по мере его эксплуатации, противодействуют тем, что варьируют ход температуры потока внутри совокупного слоя катализатора и/или расход при необходимости используемых вспомогательных газов дегидрирования ...

Подробнее
14-04-2020 дата публикации

Номер: RU2018125893A3
Автор:
Принадлежит:

Подробнее
14-05-2020 дата публикации

Номер: RU2018125955A3
Автор:
Принадлежит:

Подробнее
31-01-2020 дата публикации

Номер: RU2018121310A3
Автор:
Принадлежит:

Подробнее
20-12-2019 дата публикации

Номер: RU2018108151A3
Автор:
Принадлежит:

Подробнее
26-03-2020 дата публикации

Номер: RU2018133588A3
Автор:
Принадлежит:

Подробнее
18-12-2020 дата публикации

Номер: RU2019118428A3
Автор:
Принадлежит:

Подробнее
17-05-2017 дата публикации

КОНТАКТНЫЙ АППАРАТ ДЛЯ ОКИСЛЕНИЯ ДИОКСИДА СЕРЫ В ТРЕХОКИСЬ СЕРЫ ПРИ ПЕРЕРАБОТКЕ НИЗКОКОНЦЕНТРИРОВАННЫХ СЕРНИСТЫХ ГАЗОВ

Номер: RU171032U1

Контактный аппарат для окисления SOв SОпри переработке низкоконцентрированных сернистых газов в нестационарных условиях с неизменным направлением движения нескольких тепловых фронтов - зон реакции в секциях с катализатором. Использование данного типа контактного аппарата на 2-ой стадии окисления SOв SOв контактном узле, работающем по схеме ДК/ДА, позволит обеспечить существенное сокращение капитальных и эксплуатационных затрат.

Подробнее
27-02-2011 дата публикации

НЕПРЕРЫВНЫЙ ПРОЦЕСС И АППАРАТ ДЛЯ ФЕРМЕНТАТИВНОЙ ОБРАБОТКИ ЛИПИДОВ

Номер: RU2412984C1
Принадлежит: БАНДЖ ОЙЛЗ, ИНК. (US)

Изобретение относится к масложировой промышленности. Способ и система для ферментативной обработки содержащего липиды исходного материала, включающий осуществление контакта исходного материала с технологической добавкой, затем обеспечение прохождения исходного материала с, по существу, постоянной скоростью потока через систему обработки, включающую несколько содержащих фермент реакторов с неподвижным слоем, соединенных один с другим последовательно. Реакторы с неподвижным слоем могут обслуживаться индивидуально, скорость потока исходного материала через систему остается, по существу, постоянной при отключении одного реактора для обслуживания. Технологическая добавка представляет собой, по существу, свободный от влаги кремнезем, имеющий размер пор более чем 150 ангстрем. Технологическая добавка может быть помещена в один или более реакторов с неподвижным слоем, располагаясь поверх слоя фермента в реакторе, или может находиться в системе предварительной обработки, включающей один или более ...

Подробнее
20-12-2016 дата публикации

РЕАКТОР СИНТЕЗА АММИАКА С РАЗДЕЛЕННЫМ ПОТОКОМ И ТРУБЧАТОЙ НАСАДКОЙ

Номер: RU2015120312A
Принадлежит:

... 1. Реактор синтеза аммиака, в котором синтез-газ, содержащий азот и водород, разделен на два или более основных потока, каждый из которых подается в механически изолированную реакционную зону, причем охлаждение реакционных зон осуществляется с помощью теплообменных трубок, находящихся в слое катализатора, а движение газа через слои катализатора и охлаждающего вещества через теплообменные трубки, расположенные в катализаторе, осуществляется преимущественно вертикально.2. Реактор по п. 1, в котором в каждой реакционной зоне могут присутствовать два или боле слоев катализатора.3. Реактор по п. 2, в котором по крайней мере один слой катализатора снабжен теплоотводящими трубками.4. Реактор по п. 1, в котором катализатор располагается внутри трубок, а охлаждающее вещество подается в межтрубное пространство.5. Способ реконструкции существующего аппарата с получением реактора, описанного в пп. 1-4.

Подробнее
09-04-2020 дата публикации

Микродиспергатор для генерирования капель

Номер: RU2718617C1

Изобретение относится к микродиспергаторам, в которых генерируются микрокапли преимущественно сферической формы нанолитрового и субнанолитрового объема, и далее сгенерированные капли могут быть использованы в химических, фармацевтических и других технологиях, в том числе для проведения массообменных процессов и химических реакций между реагентами, растворенными в каплях, либо растворенными в каплях и в сплошной среде, а также для последующего нанесения биологически активных веществ на поверхности сформированных капель. Сущность изобретения заключается в том, что в микродиспергаторе для генерирования капель одной жидкости в другой с узким дисперсным составом, включающем корпус в виде канала протяженной формы, присоединенный к корпусу соосно ему патрубок для ввода дисперсной фазы, и присоединенные к боковой поверхности корпуса один или более патрубков для ввода сплошной фазы, поперечное сечение канала от среза патрубка для ввода дисперсной фазы выполнено периодически изменяющимся, при этом ...

Подробнее
10-12-2007 дата публикации

КАТАЛИТИЧЕСКИЙ РЕАКТОР С НИСХОДЯЩИМ ПОТОКОМ

Номер: RU2006116389A
Принадлежит:

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

Подробнее
29-07-2020 дата публикации

РЕАКТОР И СПОСОБ МАКСИМИЗАЦИИ ВЫХОДА МЕТАНОЛА С ПРИМЕНЕНИЕМ СЛОЕВ КАТАЛИЗАТОРА

Номер: RU2728351C1

Изобретение относится к способу каталитического производства метанола из синтез-газа. Способ включает обеспечение реактора, содержащего два слоя катализатора, где первый слой катализатора расположен выше по ходу и второй слой катализатора расположен ниже по потоку и где активность первого слоя катализатора выше, чем активность второго слоя катализатора, применение синтез-газа в реакторе, содержащего водород и оксиды углерода, превращение синтез-газа в метанол и канализирование полученного метанола и не превращенного синтез-газа из реактора. Изобретение обеспечивает усовершенствование способа каталитического производства метанола и увеличение объемной производительности. 3 з.п. ф-лы, 5 ил., 3 табл., 3 пр.

Подробнее
20-08-2015 дата публикации

СИСТЕМЫ И СПОСОБЫ ИСПОЛЬЗОВАНИЯ ОСТАТОЧНОГО ГАЗА СИНТЕЗА ФИШЕРА-ТРОПША В ТЕХНОЛОГИЧЕСКОМ ПРОЦЕССЕ ПОЛУЧЕНИЯ СИНТЕТИЧЕСКОГО ЖИДКОГО ТОПЛИВА ИЗ ПРИРОДНОГО ГАЗА

Номер: RU2560874C1

Изобретение относится к вариантам системы переработки остаточного газа синтеза Фишера-Тропша. Один из вариантов включает: реактор синтеза Фишера-Тропша, обеспечивающий наличие источника остаточного газа; первый подогреватель для предварительного нагрева остаточного газа; аппарат гидрирования для гидрирования предварительно нагретого остаточного газа; дросселирующее устройство для понижения давления предварительно нагретого и прогидрированного остаточного газа; второй подогреватель для предварительного нагрева предварительно нагретого, прогидрированного и дросселированного остаточного газа с получением исходного газа, состоящего из остаточного газа и пара; и реактор каталитического риформинга для осуществления риформинга исходного газа в присутствии катализатора. Причем первый подогреватель предварительно нагревает остаточный газ до температуры в интервале приблизительно от 200 до 300°C, дросселирующее устройство понижает давление предварительно нагретого и прогидрированного остаточного ...

Подробнее
18-04-2018 дата публикации

КОНТАКТНЫЙ АППАРАТ ДЛЯ ПРОЦЕССА КАТАЛИТИЧЕСКОГО ОКИСЛЕНИЯ ДИОКСИДА СЕРЫ В ТРИОКСИД СЕРЫ

Номер: RU2651256C1

Изобретение относится к конструкции контактных аппаратов, предназначенных для каталитического окисления SOв SO. Целью изобретения является повышение надежности конструкции контактного аппарата. Контактный аппарат состоит из обечайки, центральной опорной колонны, нескольких полок для загрузки на них катализатора и нескольких герметичных перегородок между ними. Каждая полка контактного аппарата состоит из нескольких вантовых плит изогнутого типа. Плиты приварены противоположными краями обечайке и центральной колонне, соединены между собой подвижными скобами или сплошным сварным швом. Снаружи по периметрам обечайки и центральной опорной колонны напротив зон приварки вантовых плит изогнутого типа сплошным швом привариваются бандажные пояса жесткости, предотвращающие деформацию. Все напряжения растяжения вантовых плит изогнутого типа будут восприниматься обечайкой и центральной опорной колонной, усиленных накладкой бандажных поясов жесткости. В результате предотвращается деформация обечайки ...

Подробнее
27-01-2012 дата публикации

ФИЛЬТРУЮЩАЯ ТАРЕЛКА ПРЕДВАРИТЕЛЬНОГО РАСПРЕДЕЛЕНИЯ С ПЕРЕЛИВНОЙ ТРУБОЙ ДЛЯ РЕАКТОРА С НЕПОДВИЖНЫМ СЛОЕМ И ПАРАЛЕЛЛЬНЫМИ НИСХОДЯЩИМИ ПОТОКАМИ ГАЗА И ЖИДКОСТИ

Номер: RU2010129496A
Принадлежит:

... 1. Устройство фильтрования и предварительного распределения газовой и жидкой фаз, составляющих поток, поступающий в каталитический реактор, работающий по принципу параллельных нисходящих потоков газа и жидкости, причем жидкая фаза содержит кольматирующие частицы, а упомянутое устройство расположено на выходе распределительной тарелки, называемой "выходной" распределительной тарелкой (10), и содержит: !- перфорированную тарелку с отверстиями (7) диаметром (do), которая расположена практически горизонтально, жестко соединена со стенками реактора и на которой закреплены каналы (3), которые расположены практически вертикально, и открыты со стороны верхних концов для впуска газа и со стороны нижних концов для выпуска данного газа, причем данная тарелка поддерживает фильтрующий слой (2), окружающий каналы (3); ! - по меньшей мере одну трубу (4), служащую для перелива жидкости (и называемую переливной трубой (4)), проходящая практически вертикально от верхнего уровня, расположенного ниже уровня ...

Подробнее
20-12-2012 дата публикации

НОВЫЙ СПОСОБ КАТАЛИТИЧЕСКОГО РИФОРМИНГА С РЕЦИРКУЛЯЦИЕЙ ГАЗОВЫХ ОТХОДОВ ПРОЦЕССА ВОССТАНОВЛЕНИЯ НА ВХОД ПЕРВОГО РЕАКТОРА И С ПОДАЧЕЙ РЕЦИРКУЛИРУЕМОГО ГАЗА В ЦЕЛЯХ ЕГО РЕЦИРКУЛЯЦИИ НА ЕДИНИЧНЫЙ ПОСЛЕДНИЙ РЕАКТОР БЛОКА ИЛИ НА ПОСЛЕДНИЕ РЕАКТОРЫ БЛОКА

Номер: RU2011123173A
Принадлежит:

... 1. Способ каталитического риформинга бензина в интервале дистилляции от 60 до 250°C в блоке каталитического риформинга в подвижном слое, включающем реакционноспособную зону, состоящую из четырех последовательно соединенных реакторов (R1, R2, R3 и R4), и зону регенерации указанного катализатора, регенерация включает в себя этап восстановления катализатора в атмосфере водорода, в ходе которой газовые отходы (4) вышеупомянутого этапа восстановления катализатора подают частично на вход рекуперативного теплообменника (El), расположенного перед первым реактором (R1) серии, а частично - непосредственно в головную часть реактора R1, и в котором газовые отходы (7) подают частично или полностью из компрессора рециркуляции (RCY), расположенного между разделительным резервуаром (BS) и блоком реакторов (R1, R2, R3 и R4), в головную часть предпоследнего реактора (R3).2. Способ каталитического риформинга бензина согласно п.1, в котором газовые отходы восстановления (4) полностью направляют в головную ...

Подробнее
27-08-2014 дата публикации

УСТРОЙСТВО ДЛЯ МНОГОФАЗНОГО КОНТАКТА И РАСПРЕДЕЛЕНИЯ ДЛЯ ГИДРОПРОЦЕССИНГА

Номер: RU2013107029A
Принадлежит:

... 1. Реакторная система, включающая:(а) корпус реактора;(b) подающее первичное распределительное устройство, расположенное в корпусе реактора; и(с) по меньшей мере, одно подающее вторичное распределительное устройство, расположенное под подающим первичным распределительным устройством в корпусе реактора, при этом,(d) подающее первичное распределительное устройство включает в себя первичную отклоняющую пластину и первую сопловую тарелку, расположенную под отклоняющей пластиной; и(е) упомянутое, по меньшей мере, одно подающее вторичное распределительное устройство содержит сборную тарелку и вторую сопловую тарелку, расположенную под сборной тарелкой, при этом первая сопловая тарелка и вторая сопловая тарелка, каждая, содержит множество сопел, каждое сопло содержит корпус сопла, включающий в себя дальнюю часть, имеющую, по меньшей мере, один впуск для жидкости, выполненный с возможностью прохождения через него жидкости, указанная дальняя часть корпуса ограничивает, по существу, цилиндрическую ...

Подробнее
08-08-2019 дата публикации

Способ модернизации аммиачного конвертера

Номер: RU2018104559A
Принадлежит:

Подробнее
27-01-2011 дата публикации

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

Номер: RU2009127502A
Принадлежит:

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

Подробнее
10-02-2016 дата публикации

РАСПРЕДЕЛИТЕЛЬНОЕ УСТРОЙСТВО ДЛЯ МНОГОСЛОЙНОГО РЕАКТОРА С НИСХОДЯЩИМ ПОТОКОМ

Номер: RU2014130099A
Принадлежит:

... 1. Распределительное устройство для распределения жидкости и газа в многослойном реакторе с опускным течением, содержащеепо существу горизонтально расположенную сборную тарелку (20), содержащую центральное проходное отверстие (30) для газа и проходные отверстия (40) для жидкости, расположенные вокруг указанного центрального проходного отверстия для газа;завихритель (100), который размещен над сборной тарелкой (20) вокруг центрального проходного отверстии (30) для газа и содержит лопатки (95), устанавливающие направление (107) завихрения потока и расположенные с возможностью придания вращательного движения газу, проходящему через центральное проходное отверстие (30) так, что газ выходит из центрального проходного отверстия (30) в виде вихря (108), закрученного в указанном направлении (107) завихрения вокруг вертикальной оси (106) завихрения;одно или большее число эжекционных сопел (130), расположенных выше сборной тарелки и предназначенных для эжекции, в направлении эжекции, охлаждающей ...

Подробнее
14-10-1999 дата публикации

Verfahren zur Herstellung von 1,2-Dichlorethan

Номер: DE0069602880T2
Принадлежит: TOSOH CORP, TOSOH CORP.

Подробнее
05-04-2007 дата публикации

WASSERDAMPFREFORMIERUNG MIT INTERNER WASSERSTOFFREINIGUNG

Номер: DE0069835503T2
Принадлежит: IDATECH LLC, IDATECH, LLC.

Подробнее
23-01-1975 дата публикации

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

Номер: DE0002166659A1
Принадлежит:

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

Подробнее
26-06-1913 дата публикации

Apparatus for the Chemical Transformation of Gases by Multiple Contact Action at Regulatable Temperatures.

Номер: GB0191301994A
Автор:
Принадлежит:

... 1994. Farbenfabriken vorm. F. Bayer & Co. Feb. 13, 1912, [Convention date]. Catalytic or contact apparatus. - Apparatus for the catalytic treatment of mixtures of gases, such as hydrochloric acid or sulphurous acid and air, is provided with alternately superposed contact .and heat exchanging - chambers I. R2, respectively, which communicate directly with each other the gas supply pipe to the first contact chamber having branch pipes at intervals to the several heat exchanging-chambers for the regulation of the temperatures in the several parts of the apparatus. The regulation is effected by controlling the amount of gas passing through these chambers by means of regulating-valves V1, V2.

Подробнее
30-03-1988 дата публикации

APPARATUS FOR REFINING CRUDE LIQUID SULFUR

Номер: GB0008805128D0
Автор:
Принадлежит:

Подробнее
26-10-1988 дата публикации

Refining liquid sulphur

Номер: GB0002203732A
Принадлежит:

Apparatus for refining crude liquid sulfur containing hydrogen sulfide and hydrogen polysulfides comprises a vessel provided with a liquid sulfur supply conduit, a sweep gas supply conduit, a refined sulfur discharge conduit and a sweep gas discharge conduit, in which a catalyst means capable of decomposing hydrogen polysulfides is submerged at least partly in the liquid sulfur to be filled in the vessel.

Подробнее
03-04-1991 дата публикации

AN APPARATUS FOR REFINING CRUDE LIQUID SULFUR.

Номер: GB0002203732B
Принадлежит: JGC CORP, * JGC CORPORATION

Подробнее
17-01-2007 дата публикации

Integrated Fuel Processor For Distributed Hydrogen Production

Номер: GB0002428039A
Принадлежит:

A fuel processing system is provided wherein heat is transferred from a reformate flow (32) downstream from a water-gas shift (38) to both a) a combustor feed flow (40) that is supplied to a combustor (25); and b) a water flow (26) that is supplied to a reformer feed mix (34) for a steam reformer (28).

Подробнее
11-10-1948 дата публикации

Improvements in or relating to contact apparatus for gas reactions

Номер: GB0000610007A
Автор:
Принадлежит:

To control the temperature of gas phase catalytic reactions loose pieces or grains of a heat-conducting chemically resistant material are interspersed or arranged in layers in the contact material. Pieces of wire, sheet, or turnings of metal, particularly aluminium are suitable material. The distribution of conducting material may be graded along the course of the gases according to the intensity of the reaction, and towards the exit end the material may be insulated from the exterior of the reaction chamber. Processes mentioned are the manufacture of sulphuric acid, the oxidation of ammonia, the oxidation of naphthalene to phthalic anhydride, and the conversion of ethyl alcohol to ethylene.

Подробнее
21-06-1967 дата публикации

Method for the reprocessing of uranium-containing nuclear fuels

Номер: GB0001073000A
Автор:
Принадлежит:

A uranium-containing fuel is reprocessed by fluorination at 800-900 DEG C. with sulphur hexafluoride, with the formation of uranium hexafluoride. An oxidizing agent, for example oxygen, air, or pyrolusite, may also be present. The reaction may be carried out by a fluidized bed process or in a rotating tube furnace; the spent fuel may be mixed with corundum or fluorspar. Preliminary heating to 700-800 DEG C. volatilizes fission product fluorides and forms uranyl fluoride which is converted to uranium hexafluoride at the higher temperature. The fuel may be in metal, oxide or carbide form. If fuel particles coated with carbon or silicon carbide are treated, they should first be comminuted or treated at 900-1100 DEG C. with oxygen-containing gas in the presence of a combustion catalyst. The UF6 formed may be further decontaminated by passage through columns of sodium fluoride.

Подробнее
21-02-2007 дата публикации

Integrated fuel processor for distributed hydrogen production

Номер: GB0002429274A
Принадлежит:

An integrated steam reformer/combustor assembly (42) is provided for use in a fuel processor (20) that supplies a steam/fuel feed mix (34) to be reformed in the assembly and a combustor feed (40) to be combusted in the assembly (42). The assembly (42) includes a housing (44,58) defining first and second axially extending, concentric annular passages in heat transfer relation to each other; a first convoluted fin (46) located in the first passage to direct the feed mix therethrough, the first convoluted fin coated with a catalyst that induces a desired reaction in the feed mix; and a second convoluted fin (50) located in the second passage to direct the combustor feed therethrough, the second convoluted fin coated with a catalyst that induces a desired reaction in the combustor feed.

Подробнее
21-10-2015 дата публикации

Inert gas recovery system

Номер: GB0002477322B

Подробнее
04-01-2023 дата публикации

Multi-disc catalytic reactor

Номер: GB0002608426A
Принадлежит:

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

Подробнее
31-10-2015 дата публикации

PROCESS FOR THE SYNTHESIS OF METHANOL

Номер: AP0000003450A
Принадлежит:

Подробнее
28-02-2007 дата публикации

Catalytic plant and process for performing fischer-tropsch synthesis

Номер: AP2007003876A0
Автор: BOWE MICHAEL JOSEPH
Принадлежит:

Подробнее
31-08-2012 дата публикации

Process for the synthesis of methanol

Номер: AP2012006428A0
Принадлежит:

Подробнее
31-08-1979 дата публикации

Process and apparatus to establish a contact intimate between fluids.

Номер: OA0000003973A
Автор:
Принадлежит:

Подробнее
15-12-1970 дата публикации

Process and device for the realization under adiabatic conditions of endothermic catalytic reactions.

Номер: OA0000002830A
Автор:
Принадлежит:

Подробнее
15-10-1975 дата публикации

REAKTIONSAPPARAT ZUR DURCHFUHRUNG MEHRSTUFIGER KATALYTISCHER REAKTIONEN

Номер: ATA268773A
Автор:
Принадлежит:

Подробнее
15-07-2021 дата публикации

Reinigungsvorrichtung, Brennstoffzellensystem, Biomasseanlage und Verfahren zum Betreiben einer Reinigungsvorrichtung

Номер: AT523124B1
Принадлежит:

Die vorliegende Erfindung betrifft eine Reinigungsvorrichtung (10) zum Reinigen von Produktgas aus einem Biomassevergaser (50) für die Verwendung in einem Brennstoffzellenstapel (31) eines Brennstoffzellensystems (30), aufweisend einen Reaktor (13), der ein Reaktorgehäuse (14) mit einem Produktgaseinlass (15) zum Einbringen von Produktgas in das Reaktorgehäuse (14) und einem Produktgasauslass (16) zum Auslassen von gereinigtem Produktgas aus dem Reaktorgehäuse (14) umfasst, wobei im Reaktorgehäuse (14) mehrere unterschiedliche Reaktionsschichten (17, 18, 19) zum Entfernen von unterschiedlichen Verunreinigungsbestandteilen aus dem Produktgas angeordnet sind. Ferner betrifft die Erfindung ein Brennstoffzellensystem (30) mit einer erfindungsgemäßen Reinigungsvorrichtung (10), eine Biomasseanlage (50) mit einem erfindungsgemäßen Brennstoffzellensystem (30) sowie ein Verfahren zum Betreiben einer erfindungsgemäßen Reinigungsvorrichtung (10).

Подробнее
15-10-1975 дата публикации

REACTION APPARATUS TO DURCHFUHRUNG MULTI-LEVEL CATALYTIC REACTIONS

Номер: AT0000268773A
Автор:
Принадлежит:

Подробнее
15-08-2011 дата публикации

PRODUCTION OF ALKYL AROMATICS

Номер: AT0000518820T
Принадлежит:

Подробнее
15-11-1988 дата публикации

DEVICE FOR THE CATALYTIC SHIFTING OF GASES.

Номер: AT0000038476T
Принадлежит:

Подробнее
28-11-2019 дата публикации

Use of treating elements to facilitate flow in vessels

Номер: AU2017217834B2
Принадлежит: Davies Collison Cave Pty Ltd

A method for facilitating the distribution of the flow of one or more streams within a bed vessel is provided. Disposed within the bed vessel are internal materials and structures including multiple operating zones. One type of operating zone can be a processing zone composed of one or more beds of solid processing material. Another type of operating zone can be a treating zone. Treating zones can facilitate the distribution of the one or more streams fed to processing zones. The distribution can facilitate contact between the feed streams and the processing materials contained in the processing zones.

Подробнее
22-04-2021 дата публикации

A methanol synthesis process layout for large production capacity

Номер: AU2017242105B2
Принадлежит:

A process layout for large scale methanol synthesis comprises one or more boiling water reactors and one or more radial flow reactors in series, the boiling water reactor (s) being fed with approximately fresh make-up syngas. The methanol synthesis loop comprises a make-up gas compressor K1, a recycle gas compressor K2, two or more boiling water converters for methanol synthesis (A1, A2,..), a radial flow converter (B) for methanol synthesis, a steam drum (V1), a high pressure separator (V2), a low pressure separator (V3), feed effluent heat exchangers (E1 and E2), a wash column (C), an air cooler (E3) and a water cooler (E4).

Подробнее
30-06-1983 дата публикации

METHANATION CATALYST

Номер: AU0007874281A
Принадлежит:

Подробнее
10-05-2018 дата публикации

Natural gas processing and systems

Номер: AU2013288708B2
Принадлежит: Davies Collison Cave Pty Ltd

The present disclosure provides natural gas and petrochemical processing systems including oxidative coupling of methane reactor systems that integrate process inputs and outputs to cooperatively utilize different inputs and outputs of the various systems in the production of higher hydrocarbons from natural gas and other hydrocarbon feedstocks.

Подробнее
17-04-2014 дата публикации

Simultaneous warm gas desulfurization and complete co-shift for improved syngas cleanup

Номер: AU2009322850B2
Принадлежит:

The present invention involves both separated beds (or physical mixture) and a process for treating a fuel gas comprising sending the fuel gas to a separated bed (or physical mixture), in which the separated beds comprise a first bed of a sulfur sorbent and a second bed of a water gas shift catalyst (a physical mixture of a sulfur sorbent and a water gas shift catalyst). The process comprises first sending the fuel gas to the first bed to remove sulfur compounds from said fuel gas and then the fuel gas goes to the second bed to undergo a water gas shift reaction in which carbon monoxide is converted to carbon dioxide and water is converted to hydrogen. (or sending the fuel gas simultaneously to the physical mixture to remove simultaneously the sulfur compounds and to react CO with water to CO2 and hydrogen).

Подробнее
18-01-2018 дата публикации

A method for revamping an ammonia converter

Номер: AU2016289324A1
Принадлежит: K&L GATES

Method for revamping a multi-bed ammonia converter, wherein said converter comprises a plurality of adiabatic catalytic beds including a first catalytic bed and one or more further catalytic bed(s), said catalytic beds being arranged in series so that the effluent of a bed is further reacted in the subsequent bed; at least a first inter-bed heat exchanger arranged between said first catalytic bed and a second catalytic bed to cool the effluent of said first bed before admission into said second bed, and optionally further inter-bed heat exchanger(s) arranged between consecutive beds; said method involves the conversion of said first catalytic bed into an isothermal catalytic bed.

Подробнее
25-07-2019 дата публикации

Converter for converting so3

Номер: AU2018217864A1
Принадлежит: Spruson & Ferguson

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

Подробнее
05-06-2000 дата публикации

Inhibition of carbon deposition on fuel gas steam reformer walls

Номер: AU0002843000A
Принадлежит:

Подробнее
17-02-1994 дата публикации

Catalyst-downcomer-tray for chemical process tower

Номер: AU0004209393A
Принадлежит:

Подробнее
13-11-2006 дата публикации

IMPROVED DISTRIBUTOR SYSTEM FOR DOWNFLOW REACTORS

Номер: CA0002546359A1
Принадлежит:

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

Подробнее
10-06-1980 дата публикации

OXYCHLORINATION OF ETHYLENE

Номер: CA1079258A

Oxychlorination of ethylene is carried out using a three-reactor system containing beds of a catalyst comprising a spherical, high-surface area activated alumina impregnated with cupric chloride and potassium chloride. In the first two reactors, the catalyst bed is divided into two sections, with a more active catalyst in the lower section than in the upper. The catalyst is substantially undiluted with inert particles.

Подробнее
24-07-1973 дата публикации

METHOD OF PRODUCING ISOPRENE AND APPARATUS THEREFOR

Номер: CA930750A
Автор:
Принадлежит:

Подробнее
20-04-1976 дата публикации

FABRICATION DU STYRENE

Номер: CA0000987688A1
Принадлежит:

Подробнее
21-08-1984 дата публикации

CONVERTER

Номер: CA0001172829A2
Автор: MCFARLAND JOHN
Принадлежит:

Подробнее
12-01-2017 дата публикации

A METHOD FOR REVAMPING AN AMMONIA CONVERTER

Номер: CA0002989048A1
Принадлежит:

Method for revamping a multi-bed ammonia converter, wherein said converter comprises a plurality of adiabatic catalytic beds including a first catalytic bed and one or more further catalytic bed(s), said catalytic beds being arranged in series so that the effluent of a bed is further reacted in the subsequent bed; at least a first inter-bed heat exchanger arranged between said first catalytic bed and a second catalytic bed to cool the effluent of said first bed before admission into said second bed, and optionally further inter-bed heat exchanger(s) arranged between consecutive beds; said method involves the conversion of said first catalytic bed into an isothermal catalytic bed.

Подробнее
08-08-2017 дата публикации

METHOD FOR HYDROTREATING HEAVY HYDROCARBON FEEDSTOCKS USING PERMUTABLE REACTORS, INCLUDING AT LEAST ONE STEP OF GRADUAL PERMUTATION

Номер: CA0002821019C
Принадлежит: IFP ENERGIES NOUVELLES, IFP ENERGIES NOW

Procédé d'hydrotraitement d'une fraction lourde d'hydrocarbures utilisant un système de zones de garde permutables en lits fixes contenant chacune au moins un lit catalytique incluant au moins une étape au cours de laquelle le flux de la charge alimentant la première zone de garde mise en contact avec la charge est en partie basculé vers la prochaine zone de garde en aval, de préférence de façon progressive.

Подробнее
02-03-2021 дата публикации

MIXING DEVICE WITH TANGENTIAL INLETS FOR TWO-PHASE CONCURRENT VESSELS

Номер: CA2843264C

Vapor and liquid flow concurrently through a vertical vessel. A horizontal flow obstructing mixing device is located within the vessel and forces the vapor and liquid to pass in a vertical direction through one or more inlet openings to the mixing device. The mixing device consists of circular top and bottom walls and a cylindrical side wall. Inside the mixing device curved flow baffles are provided. These flow baffles form one or more tangential inlet orifices, which are located as far from the vessel centerline as possible. The entire process stream flows through the one or more tangential inlet orifices at high flow velocity and in a tangential direction into a swirl box. The high momentum of the process stream in the tangential inlet orifices, the pure tangential direction of the stream, and the large distance between the tangential inlet orifice(s) and the vessel centerline result in a violet swirling flow and in a large number of fluid rotations in the swirl box. The large number ...

Подробнее
29-04-2014 дата публикации

PROCESS FOR THE PRODUCTION OF OLEFINS

Номер: CA0002748570C

Disclosed is a process for the production of C2 to C3 olefins via the catalytic cracking of feedstocks including C4 and heavier olefins in an integrated reaction / regeneration system.

Подробнее
18-10-2012 дата публикации

APPARATUS FOR THE SYNTHESIS OF ANHYDROUS HYDROGEN HALIDE AND ANHYDROUS CARBON DIOXIDE

Номер: CA0002831449A1
Принадлежит:

An apparatus for the synthesis of anhydrous hydrogen halide fluids from organic halide fluids, such as perfluorocarbon fluids and refrigerant fluids, and anhydrous carbon dioxide for the environmentally safe disposition thereof.

Подробнее
06-10-2011 дата публикации

HYDROGEN/SYNGAS GENERATOR

Номер: CA0002795015A1
Принадлежит:

The present invention relates to a compact, concentric auto thermal hydrogen/ syngas generator for production of hydrogen/ syngas without any external heating. Further, the auto thermal hydrogen/ syngas generator of the present invention involves combination of reactions such as partial oxidation, steam reforming, dry reforming, auto thermal reforming, dry autothermal reforming, water gas shift, preferential oxidation or methanation that takes place without external heating, for converting air, steam and fuel into a reformate mainly containing CO, CO2, N2, CH4 and H2O which is subsequently converted to hydro gen/syn gas as a feed for fuel cell or syngas applications.

Подробнее
11-04-1991 дата публикации

LIQUID PHASE REACTION PROCESS

Номер: CA0002027266A1
Принадлежит:

B 35456 "LIQUID PHASE REACTION PROCESS" A process and apparatus for the decomposition of reactants, e.g. hypochlorite ions, contained in a liquid stream into a gaseous product, e.g. oxygen, by contact with a particulate catalyst disposed in a plurality of reaction volumes connected in series. The flowrate of the gaseous product is required to be at least 0.5 that of the liquid stream, and the vertical velocity of the gaseous product is limited to less than 5 cm.s-1.

Подробнее
11-10-1996 дата публикации

PROCESS FOR OPERATING EQUILIBRIUM CONTROLLED REACTIONS

Номер: CA0002173423A1
Принадлежит: OSLER, HOSKIN & HARCOURT LLP

The present invention is a process for operating equilibrium controlled reactions in continuous mode wherein a feedstock is reacted in a plurality of reactors containing an admixture of a desired process catalyst and an adsorbent to form a product which is selectively adsorbed by the adsorbent and an admixture containing a product which is withdrawn from the reactor. A series of separation steps is used to desorb the product which is selectively adsorbed by the adsorbent and to prepare the reactor for a subsequent process cycle. The process utilizes a novel series of adsorption and desorption steps to collect the less selectively adsorbed product in substantially pure form under relatively constant flow rate at feedstock pressure.

Подробнее
26-10-1999 дата публикации

PROCESS FOR OPERATING EQUILIBRIUM-CONTROLLED REACTIONS

Номер: CA0002173809C
Принадлежит: OSLER, HOSKIN & HARCOURT LLP

A cyclic process for operating an equilibrium controlled reaction in a plurality of reactors containing an admixture of an adsorbent and a reaction catalyst suitable for performing the desired reaction which is operated in a predetermined timed sequence wherein the heating and cooling requirements in a moving reaction mass transfer zone within each reactor are provided by indirect heat exchange with a fluid capable of phase change at temperatures maintained in each reactor during sorpreaction, depressurization, purging and pressurization steps during each process cycle.

Подробнее
14-08-1997 дата публикации

ETHERIFICATION-HYDROGENATION PROCESS

Номер: CA0002245581A1
Принадлежит:

A process for removing dienes from etherification uses a hydrogenation zone (24) in the reactor distillation column (20) above the etherification zone (22). MTBE is produced and the unreacted C4 stream is also subjected to selected hydrogenation of the butadiene contained in the C4 feed stream. The C4 stream is introduced via line (101) and methanol is introduced via line (102) which is combined in flow line (104) and subsequently enters the distillation column (20) via line (103) wherein the C4 stream is contacted with methanol in the etherification zone (22) where the MTBE is distilled downward. The unreacted C4's then are subjected to selective hydrogenation in the hydrogenation zone (24) wherein butadiene in the overhead raffinate (108) is reduced by over 90 %. The hydrotreated C4's are thus suitable for cold acid alkylation or other use wherein butadiene is harmful.

Подробнее
16-08-1923 дата публикации

Procédé pour régler la température de réactions exothermiques entre des gaz.

Номер: CH0000100937A
Принадлежит: COURTNEY CONOVER

Подробнее
15-03-1985 дата публикации

DEVICE FOR THE CATALYTIC OXIDATION FROM DEUTERIUM TO HEAVY WATER.

Номер: CH0000648270A5

Подробнее
15-07-1988 дата публикации

Modifying axial gas flow reactors synthesis

Номер: CH0000666197A5

A pressurised catalyst synthesis reactor of the Kellogg type with the catalyst granules contained in annular perforated baskets of graduated size to form the catalyst beds. These beds have an inner perforated tube (Fi) and a solid metal base to induce a mainly radial gas flow through the catalyst instead of the axial or vertical flow in the conventional design. Quench gases are injected into each bed by the normal circular sparger pipe rings and the prod. gases exit through the heat exchanger and the top nozzle in the normal manner.

Подробнее
25-06-2011 дата публикации

СПОСОБ ПОЛУЧЕНИЯ ПРОДУКТА В КОНДЕНСИРОВАННОЙ ФАЗЕ ИЗ ОДНОГО ИЛИ НЕСКОЛЬКИХ ГАЗОФАЗОВЫХ РЕАГЕНТОВ

Номер: UA0000094927C2

Способ получения как минимум одного продукта в конденсированной фазе из одного или нескольких газофазовых реагентов в присутствии твердого катализатора, который включает один или несколько каталитических компонентов, в котором твердый катализатор имеет две или большее число зон, в которых продолжительность контакта одного или нескольких газофазовых реагентов с одним или несколькими каталитическими компонентами разная.

Подробнее
29-10-2010 дата публикации

УСТАНОВКА ПО ПОЛУЧЕНИЮ СИНТЕТИЧЕСКОГО ЖИДКОГО ТОПЛИВА, ИСПОЛЬЗУЮЩАЯ ПАРАЛЛЕЛЬНЫЕ ЗВЕНЬЯ

Номер: EA0201070426A1
Принадлежит:

Изобретение относится к установке по переработке природного газа. Установка включает два и более модуля, соединенных параллельно. Установку конфигурируют для преобразования попутного газа в материал, имеющий более высокую плотность. Кроме того, изобретение относится к способу переработки газа, попутного для одной или нескольких нефтяных скважин. Способ включает этапы обеспечения наличия модульной установки, содержащей два и более модуля, соединенных параллельно, где по меньшей мере один из модулей является модулем, устойчивым к сбоям, и по меньшей мере один из модулей является экономичным модулем; снижения производительности одного или нескольких модулей в случае уменьшения продуктивности; выключения одного или нескольких модулей, по меньшей мере, в случае уменьшения продуктивности за границы предела снижения производительности. Природный газ перерабатывают в звене Фишера-Тропша.

Подробнее
30-10-2008 дата публикации

СПОСОБ ПОЛУЧЕНИЯ ПРОДУКТА В КОНДЕНСИРОВАННОЙ ФАЗЕ ИЗ ОДНОГО ИЛИ НЕСКОЛЬКИХ ГАЗОФАЗНЫХ РЕАГЕНТОВ

Номер: EA200801451A1
Принадлежит:

В заявке описан способ получения по меньшей мере одного продукта в конденсированной фазе из одного или нескольких газофазных реагентов в присутствии твердого катализатора, включающего один или несколько каталитических компонентов, в котором твердый катализатор обладает двумя или большим числом зон, в которых продолжительность контактирования одного или нескольких газофазных реагентов с одним или несколькими каталитическими компонентами различна.

Подробнее
29-06-2021 дата публикации

Устройство усовершенствованной микроповерхностной реакции гидрирования с нисходящим потоком и фиксированным слоем для производства нефтепродуктов

Номер: RU0000205181U1

Полезная модель относится к устройству усовершенствованной микроповерхностной реакции гидрирования с нисходящим потоком и фиксированным слоем для производства нефтепродуктов. Устройство включает в себя реактор с фиксированным слоем и генератор микроповерхностей, при этом генератор микроповерхностей расположен над реактором с фиксированным слоем для преобразования энергии давления водорода и/или кинетической энергии нефтепродукта во время реакции в поверхностную энергию пузырька и передачи поверхностной энергии пузырьку водорода, так что пузырек водорода дробится на микропузырьки и микропузырьки смешиваются с нефтепродуктом в процессе реакции для образования газожидкостной эмульсии; реактор с фиксированным слоем используется в качестве места протекания реакции гидрирования для образования стабильной усовершенствованной газожидкостной системы для реакции с фиксированным слоем, когда газожидкостная эмульсия поступает в реактор с фиксированным слоем; резервуар для разделения газа и жидкости соединен с реактором с фиксированным слоем для отделения газа от жидкости в смеси, являющейся результатом реакции в реакторе с фиксированным слоем. Устройство микроповерхностной реакции гидрирования с фиксированным слоем имеет преимущества низкого потребления энергии, низкого рабочего давления, большой площади межфазной границы массопереноса газ-жидкость, высокой видимой скорости реакции и высокой эффективности использования газа. РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 205 181 U1 (51) МПК B01J 8/02 (2006.01) C10G 45/08 (2006.01) C10G 45/22 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ПОЛЕЗНОЙ МОДЕЛИ К ПАТЕНТУ (52) СПК B01J 8/02 (2021.02); C10G 45/08 (2021.02); C10G 45/22 (2021.02) (21)(22) Заявка: 2020129865, 06.06.2019 (24) Дата начала отсчета срока действия патента: Дата регистрации: 29.06.2021 15.03.2019 CN 201910196596.X (45) Опубликовано: 29.06.2021 Бюл. № 19 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 10.09.2020 (73) ...

Подробнее
19-01-2012 дата публикации

Multiphase contact and distribution apparatus for hydroprocessing

Номер: US20120014847A1
Принадлежит: Chevron USA Inc

Systems and apparatus for mixing, cooling, and distributing multiphase fluid mixtures within a reactor, wherein reactor internal apparatus of the present invention provides not only improved fluid mixing and distribution to each underlying catalyst bed surface, but also offers other advantages including: decreased mixing tray height; easier maintenance, assembly and disassembly; and decreased amounts of fabrication material. In an embodiment, fluid may be evenly distributed to a catalyst bed from a fluid distribution unit comprising a nozzle tray including a plurality of nozzles, wherein the nozzles include at least one liquid inlet disposed tangentially to an inner surface of the nozzle.

Подробнее
29-03-2012 дата публикации

Removal of Hydrogen From Dehydrogenation Processes

Номер: US20120078024A1
Принадлежит: Fina Technology Inc

A process and system for dehydrogenating certain hydrocarbons is disclosed. The process includes contacting a dehydrogenatable hydrocarbon with steam in the presence of a dehydrogenation catalyst to form hydrogen and a dehydrogenated hydrocarbon. Some of the hydrogen is then removed and some of the remaining dehydrogenatable hydrocarbon is dehydrogenated.

Подробнее
21-06-2012 дата публикации

Method of making a catalyst

Номер: US20120157299A1
Принадлежит: ENERGIA TECHNOLOGIES Inc

Presented are one or more aspects and/or one or more embodiments of catalysts, methods of preparation of catalyst, methods of deoxygenation, and methods of fuel production.

Подробнее
21-06-2012 дата публикации

Methods of deoxygenation and systems for fuel production

Номер: US20120157727A1
Принадлежит: ENERGIA TECHNOLOGIES Inc

Presented are one or more aspects and/or one or more embodiments of catalysts, methods of preparation of catalyst, methods of deoxygenation, and methods of fuel production.

Подробнее
19-07-2012 дата публикации

Method and arrangement for feeding heat-sensitive materials to fixed-bed reactors

Номер: US20120184792A1
Принадлежит: Neste Oyj

The invention relates to an arrangement for feeding heat-sensitive feedstock to a fixed-bed reactor system comprising means for product recycle and a fixed-bed reactor system comprising a fixed-bed reactor comprising at least one reaction zone having at least one catalyst bed and said reaction zone comprising a cold feed distributor arranged on top of each catalyst bed and a conventional distributor arranged above each cold feed distributor. Also a method is provided for feeding heat-sensitive feedstock to a fixed-bed reactor system wherein said fixed-bed reactor system comprises means for product recycle and a fixed-bed reactor comprising at least one reaction zone having at least one catalyst bed and said reaction zone comprising a cold feed distributor arranged on top of each catalyst bed and a conventional distributor arranged above each cold feed distributor.

Подробнее
20-09-2012 дата публикации

Split Flow Contactor

Номер: US20120237434A1
Принадлежит: Kellogg Brown and Root LLC

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

Подробнее
25-10-2012 дата публикации

Method and apparatus for catalytic and thermochemical reactions

Номер: US20120269709A1
Автор: Hristo Sapoundjiev
Принадлежит: Canada Minister of Natural Resources

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

Подробнее
01-11-2012 дата публикации

Vessel For Containing Catalyst In A Tubular Reactor

Номер: US20120277331A1
Принадлежит: Davy Process Technology Ltd

A catalyst carrier for insertion in a radial tube reactor, said catalyst carrier comprising: an annular container for holding catalyst in use, said container having a perforated inner wall defining a tube, a perforated outer wall, a top surface closing the annular container and a bottom surface closing the annular container; a surface closing the bottom of said tube formed by the inner wall of the annular container; a skirt extending upwardly from the perforated outer wall of the annular container from a position at or near the bottom surface of said container to a position below the location of a seal; and a seal located at or near the top surface and extending from the container by a distance which extends beyond an outer surface of the skirt.

Подробнее
08-11-2012 дата публикации

Method for carrying out sequential reactions using a heating medium heated by means of induction

Номер: US20120283449A1
Принадлежит: Individual

A method for performing at least two successive chemical reactions to produce a target compound from at least one first, and at least one second and/or a further reactant, comprising a first reaction and a further reaction in a reaction medium, the reaction medium in contact with a solid heating medium heated by electromagnetic induction and which is located inside the reactor and surrounded by the reaction medium, and the heating medium being heated by electromagnetic induction with the aid of an inductor, an intermediate compound being formed in a first reaction, from which the target compound forms in a further reaction, and at least one reactant, not present in the reactor before the first reaction, being added between the first and the further reaction, and the target compound being separated from the heating medium.

Подробнее
22-11-2012 дата публикации

Process for alkylation of toluene to form styrene and ethylbenzene

Номер: US20120296136A1
Автор: Sivadinarayana Chinta
Принадлежит: Fina Technology Inc

A process is disclosed for making styrene and/or ethylbenzene by reacting toluene with a C 1 source over a catalyst in at least one radial reactor to form a product stream comprising styrene and/or ethylbenzene.

Подробнее
14-03-2013 дата публикации

VORTEX-TYPE MIXING DEVICE FOR A DOWN-FLOW HYDROPROCESSING REACTOR

Номер: US20130064740A1
Принадлежит:

The present invention is directed to a vortex-type mixing device for a down-flow hydroprocessing reactor. In particular, the device improves the effectiveness of an existing mixing volume in mixing the gas phase and liquid phase of two-phase systems. According to the present invention, the mixing device helps create a highly arcuate flow to incoming effluents and a high degree of mixing within a constrained interbed space of a hydroprocessing reactor. 1. A mixing device for a multi-bed down-flow catalytic reactor , the mixing device comprising:a. a horizontal top plate having an inner surface;b. a base plate extending parallel to the top plate, the base plate having an inner surface and a base plate aperture;c. a plurality of inwardly-curved vanes extending vertically between the inner surfaces of the top and base plates;d. a vertical weir ring extending vertically from the base plate inner surface proximal to the base plate aperture, the weir ring having a weir ring top edge and a weir ring diameter;e. a mixing region; andf. a bubble cap extending downwardly from the inner surface of the cover plate into the mixing region, the bubble cap having a bubble cap diameter and a bottom edge, the bubble cap diameter being smaller than the weir ring diameter, the bubble cap bottom edge extending below the weir ring top edge.2. The mixing device of claim 1 , therein the vertical weir ring further comprises a horizontal plate extending outwardly from the weir ring top edge.3. The mixing device of claim 2 , wherein the weir ring horizontal plate is perforated.4. The mixing device of claim 2 , wherein the weir ring has a vertical height that his one-half of a height of the vanes.5. The mixing device of claim 1 , the top plate further comprising an outer periphery claim 1 , wherein each vane comprises an external end proximal to the outer periphery of the top plate and an internal end proximal to the mixing region claim 1 , the mixing device further comprising a plurality of ...

Подробнее
11-04-2013 дата публикации

Process for Selective Removal of a Product from a Gaseous System

Номер: US20130087444A1
Автор: Sergio Panza
Принадлежит: AMMONIA CASALE SA

A process for selective removal of a gaseous product (P) from a gaseous system comprising said product and other components (R 1 , R 2 ), wherein the gaseous system is admitted to a first environment, which is separated from a second environment by a boundary wall, and a permeation membrane ( 3, 300 ) forms at least part of said boundary wall; a spatially non-uniform electric field ( 4 ) is generated between a first electrode or first plurality of electrodes ( 1, 301 ) located in the first environment and a second electrode or second plurality of electrodes ( 2, 302 ) located in the second environment, so that field lines of said non-uniform electric field cross said membrane, and a dielectrophoretic force generated on particles of said gaseous component (P) is at least part of a driving force of the permeation through said membrane, an amount of said product (P) being selectively removed from the first environment and collected in the second environment.

Подробнее
23-05-2013 дата публикации

Hydrogen/syngas generator

Номер: US20130129610A1
Автор: Ganesh Ravindra Kale

The present invention relates to a compact, concentric auto thermal hydrogen/syngas generator for production of hydrogen/syngas without any external heating. Further, the auto thermal hydrogen/syngas generator of the present invention involves combination of reactions such as partial oxidation, steam reforming, dry reforming, auto thermal reforming, dry autothermal reforming, water gas shift, preferential oxidation or methanation that takes place without external heating, for converting air, steam and fuel into a reformate mainly containing CO, CO 2 , N 2 , CH 4 and H 2 O which is subsequently converted to hydrogen/syngas as a feed for fuel cell or syngas applications.

Подробнее
01-08-2013 дата публикации

Heat exchanger reformer

Номер: US20130195736A1
Автор: Bernard A. Fischer
Принадлежит: Delphi Technologies Inc

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

Подробнее
03-10-2013 дата публикации

Transalkylation Of Heavy Aromatic Hydrocarbon Feedstocks

Номер: US20130259775A1
Принадлежит:

In a process for producing xylene by transalkylation of a C+ aromatic hydrocarbon feedstock with a Cand/or Caromatic hydrocarbon, the C+ aromatic hydrocarbon feedstock, at least one Cand/or Caromatic hydrocarbon and hydrogen are contacted with a first catalyst comprising (i) a first molecular sieve having a Constraint Index in the range of about 3 to about 12 and (ii) at least first and second different metals or compounds thereof of Groups 6 to 12 of the Periodic Table of the Elements. Contacting with the first catalyst is conducted under conditions effective to dealkylate aromatic hydrocarbons in the feedstock containing C+ alkyl groups and to saturate C+ olefins formed so as to produce a first effluent. At least a portion of the first effluent is then contacted with a second catalyst comprising a second molecular sieve having a Constraint Index less than 3 under conditions effective to transalkylate C+ aromatic hydrocarbons with said at least one C-Caromatic hydrocarbon to form a second effluent comprising xylene. 120-. (canceled)21. A catalyst system comprising:(a) a first catalyst bed comprising (i) a first molecular sieve having a Constraint Index in the range of about 3 to about 12 and (ii) at least one metal selected from platinum, palladium, iridium, and rhenium, and at least one metal selected from copper, silver, gold, ruthenium, iron, tungsten, molybdenum, cobalt, nickel and zinc; and(b) a second catalyst bed comprising (i) a second molecular sieve having a Constraint Index less than 3 and (ii) at least one metal selected from platinum, palladium, iridium, and rhenium, and at least one metal selected from copper, silver, gold, ruthenium, iron, tungsten, molybdenum, cobalt, nickel and zinc.22. The catalyst system of claim 21 , wherein said first catalyst bed comprises platinum and copper.23. The catalyst system of claim 21 , wherein said second catalyst bed comprises platinum and copper.24. The catalyst system of claim 21 , wherein said first catalyst bed ...

Подробнее
17-10-2013 дата публикации

SHELL AND TUBE OXIDATION REACTOR WITH IMPROVED RESISTANCE TO FOULING

Номер: US20130274508A1
Принадлежит: Arkema Inc.

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

Подробнее
21-11-2013 дата публикации

Hydrocarbon Conversion Process

Номер: US20130310601A1
Принадлежит: ExxonMobil Chemical Patents Inc

The invention relates to processes for converting hydrocarbons to phthalic acids such as terephthalic acid. The invention also relates to polymerizing phthalic acid derivatives to produce, e.g., synthetic fibers.

Подробнее
16-01-2014 дата публикации

Sulfur recovery unit and sulfur recovery method

Номер: US20140017162A1
Принадлежит: JGC Corp

A sulfur recovery unit comprising: a reaction furnace configured to carry out a high-temperature Claus reaction between hydrogen-sulfide-containing gas and oxygen-containing gas introduced to the reaction furnace; a sulfur condenser configured to cool reaction gas discharged from the reaction furnace and condense sulfur contained in the reaction gas; and a pipe that connects the reaction furnace to the sulfur condenser, wherein the reaction furnace is fixed to the ground; and the sulfur condenser and the pipe are arranged so as to be able to move relative to the reaction furnace.

Подробнее
30-01-2014 дата публикации

BIOMASS CONVERSION SYSTEMS CONTAINING A MOVING BED CATALYST FOR STABILIZATION OF A HYDROLSATE AND METHODS FOR USE THEREOF

Номер: US20140031599A1
Принадлежит: SHELL OIL COMPANY

Digestion of cellulosic biomass solids to form a hydrolysate may be conducted with in situ catalytic reduction to transform soluble carbohydrates in the hydrolysate into a more stable reaction product. Biomass conversion systems for performing such a transformation can comprise: a hydrothermal digestion unit that also contains a first catalyst capable of activating molecular hydrogen, the first catalyst being fluidly mobile within the hydrothermal digestion unit; an optional hydrogen feed line that is operatively connected to the hydrothermal digestion unit; a fluid circulation loop comprising the hydrothermal digestion unit and a catalytic reduction reactor unit that contains a second catalyst capable of activating molecular hydrogen; and a catalyst transport mechanism external to the hydrothermal digestion unit, the catalyst transport mechanism being capable of conveying at least a portion of the first catalyst to another location from a catalyst collection zone located within the hydrothermal digestion unit. 1. A biomass conversion system comprising:a hydrothermal digestion unit that also contains a first catalyst capable of activating molecular hydrogen, the first catalyst being fluidly mobile within the hydrothermal digestion unit;an optional hydrogen feed line that is operatively connected to the hydrothermal digestion unit;a fluid circulation loop comprising the hydrothermal digestion unit and a catalytic reduction reactor unit that contains a second catalyst capable of activating molecular hydrogen; anda catalyst transport mechanism external to the hydrothermal digestion unit, the catalyst transport mechanism being capable of conveying at least a portion of the first catalyst to another location from a catalyst collection zone located within the hydrothermal digestion unit.2. The biomass conversion system of claim 1 , wherein at least a portion of the first catalyst is non-buoyant in a fluid phase.3. The biomass conversion system of claim 1 , wherein the ...

Подробнее
13-02-2014 дата публикации

Regenerative Gas Generator

Номер: US20140041392A1
Автор: Charles Robin Nail
Принадлежит: NW Licensing Co LLC

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

Подробнее
07-01-2021 дата публикации

Bi-Modal Radial Flow Reactor

Номер: US20210001296A1
Принадлежит: Chevron Phillips Chemical Co LP

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

Подробнее
07-01-2021 дата публикации

BAYONET CATALYTIC REACTOR

Номер: US20210001297A1
Принадлежит:

A bayonet reactor including a catalytic reactor in the form of an annular structured packing is provided with increased surface area for the transfer of heat between annulus gas and return gas, an increased coefficient of heat transfer between the annulus and return gases, and a reduced overall pressure drop relative to conventional reactors. The reactors of the present technology can enable intensified catalytic processing. 1. A bayonet catalytic reactor comprising:an outer tube having an open first end and a closed second end;an inner tube disposed at least partially within the outer tube, the inner tube having an open first end and an open second end; anda catalytic reactor comprising a structured packing disposed within an annulus defined by an inner diameter of the outer tube and an outer diameter of the inner tube,wherein the outer diameter of the inner tube is at least 0.45 times the inner diameter of the outer tube.2. The bayonet catalytic reactor of claim 1 , wherein the outer diameter of the inner tube is at least 0.63 times the inner diameter of the outer tube.3. The bayonet catalytic reactor of claim 1 , wherein the outer diameter of the inner tube is at least 0.77 times the inner diameter of the outer tube.4. The bayonet catalytic reactor of claim 1 , further comprising a second catalytic reactor disposed within the inner tube proximate the second end of the inner tube.5. The bayonet catalytic reactor of claim 4 , wherein the second catalytic reactor is a structured reactor comprising a honeycomb catalytic reactor.6. The bayonet catalytic reactor of claim 4 , wherein the second catalytic reactor extends from the second end of the inner tube toward the first end of the inner tube to a distance less than 50% of the distance from the second end of the inner tube to the first end of the inner tube.7. The bayonet catalytic reactor of claim 1 , wherein the bayonet catalytic reactor is a steam reforming reactor.8. The bayonet catalytic reactor of claim 1 , ...

Подробнее
07-01-2021 дата публикации

GUARD BED SYSTEM AND PROCESS

Номер: US20210001298A1
Принадлежит:

The invention provides a reaction system for the production of ethylene carbonate and/or ethylene glycol. The system having a guard bed system upstream of a catalytic EO reactor. The guard bed system having a feed line supplying a gaseous feed to be treated and an effluent line configured to remove the treated gaseous feed. The guard bed system has two or more guard bed vessels arranged in series in sequential order, each having an inlet, a bed of guard bed material and an outlet. The inlet of each guard bed vessel is attached by means of valves to both the feed line and the outlet of the guard bed vessel preceding it in sequential order. The outlet of each guard bed vessel is attached by means of valves to both the effluent line and to the inlet of the guard bed vessel following it in sequential order. 2. A process as claimed in claim 1 , wherein the guard bed material is a silver on alumina-based material or a palladium/gold based material claim 1 , preferably supported on silica.3. A process as claimed in claim 2 , whereinthe guard bed material is a silver on alumina-based material and the guard bed vessels are operated at a temperature of at least 100° C. and at most 145° C.; orthe guard bed material is a palladium/gold based material, preferably supported on silica, and the guard bed vessels are operated at a temperature of at least 65° C. and at most 95° C.4. A process as claimed in claim 1 , wherein the iodide-containing impurities formed in the EO absorber include vinyl iodide and alkyl iodides such as ethyl and methyl iodide.5. A process as claimed in claim 1 , wherein each bed of guard bed material is a radial fixed bed.6. A process as claimed in claim 1 , wherein the reaction system further comprises a carbon dioxide absorber and the guard bed system is also upstream of the carbon dioxide absorber claim 1 , which is upstream of the catalytic EO reactor.7. A process as claimed in claim 1 , wherein two or more guard bed systems operated by this process are ...

Подробнее
04-01-2018 дата публикации

Filtration tray for catalytic chemical reactor

Номер: US20180001288A1
Принадлежит: Haldor Topsoe AS

A particle separation system for a catalytic chemical reactor.

Подробнее
02-01-2020 дата публикации

REACTOR AND METHOD FOR MAXIMIZING METHANOL YIELD BY USING CATALYST LAYERS

Номер: US20200001261A1
Принадлежит:

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

Подробнее
02-01-2020 дата публикации

Catalytic oxidation method and method for producing conjugated diene

Номер: US20200001262A1
Принадлежит: Mitsubishi Chemical Corp

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

Подробнее
03-01-2019 дата публикации

APPARATUS FOR VAPOR-LIQUID DISTRIBUTION

Номер: US20190001292A1
Принадлежит:

The present invention relates to an apparatus for gas-liquid distribution. More specifically, the present invention relates to a gas-liquid distribution device that may be used in an ionic liquid co-current gas and liquid up-flow reactor designed to distribute gas uniformly across the reactor cross section through restriction orifices on distributors located across the distribution tray. 1. An apparatus for gas-liquid distribution , comprising:a tubular housing;a cylindrical riser having an inlet and an outlet which is affixed to the bottom opening of the tubular housing;a distribution plate affixed to the inside of the tubular housing; anda plurality of chimneys affixed to the bottom of the distribution plate wherein each chimney includes a first horizontal opening and a second horizontal opening.2. The apparatus of claim 1 , wherein there are about 4 to about 500 chimneys affixed to the bottom of the distribution plate.3. The apparatus of claim 1 , wherein there are 36 chimneys affixed to the bottom of the distribution plate.4. The apparatus of claim 1 , wherein the tubular housing includes a gas space and a liquid space wherein the gas space is located above the liquid space.5. The apparatus of claim 1 , wherein the cylindrical riser outlet is located in the gas space.6. The apparatus of claim 5 , wherein the first horizontal opening of the chimney is located in the gas space and the second horizontal opening is located in the liquid space.7. The apparatus of claim 5 , wherein both of the first and the second horizontal openings of the chimney are located in the gas space.8. The apparatus of claim 5 , wherein top 30% of the chimneys is located in the gas space and the rest of the chimneys is located in the liquid space.9. The apparatus of claim 5 , wherein top 70% of the chimneys is located in the gas space and the rest in the liquid space.10. The apparatus of claim 1 , wherein the first horizontal openings in the chimneys are circular and the second horizontal ...

Подробнее
05-01-2017 дата публикации

Method for producing carbonates

Номер: US20170001943A1
Принадлежит: SABIC Global Technologies BV

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

Подробнее
03-01-2019 дата публикации

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

Номер: US20190002772A1
Принадлежит: Magēmā Technology, LLC

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

Подробнее
11-01-2018 дата публикации

USE OF TREATING ELEMENTS TO FACILITATE FLOW IN VESSELS

Номер: US20180008952A1
Принадлежит: CRYSTAPHASE PRODUCTS, INC.

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

Подробнее
12-01-2017 дата публикации

Reactor with stripping zone

Номер: US20170009152A1
Принадлежит: UOP LLC

A hydrotreating reactor including a vessel comprising an upper zone, and intermediate zone and a lower zone. The upper zone comprises at least one upper catalyst bed. The intermediate zone comprises a vapor/liquid separation zone, wherein gas separated within the vapor/liquid separation zone is directed to a high pressure knockout drum and the liquid separated within the vapor/liquid separation zone is directed to a stripping section and then the lower zone. The lower zone comprises at least one lower catalyst bed. Preferably, the stripping section is configured and arranged for removing hydrogen sulfide and ammonia from the gas.

Подробнее
12-01-2017 дата публикации

PROCESS FOR PRODUCING BTX FROM A C5-C12 HYDROCARBON MIXTURE

Номер: US20170009158A1
Принадлежит:

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

Подробнее
27-01-2022 дата публикации

METHODS OF CO-PROCESSING PETROLEUM DISTILLATES AND BIO-BASED MATERIAL THROUGH A REACTION SERIES

Номер: US20220025279A1
Принадлежит:

Methods of processing bio-based material feed (“bio-feed”) and a petroleum feed, using combinations of hydrotreating beds, dewaxing beds, post-treatment beds, and liquid quenching zones. Some methods comprise processing the petroleum feed through first hydrotreating reactor beds; then processing the output with a bio-feed together through second hydrotreating reactor beds; then processing the output through the plurality of dewaxing beds to create a dewaxed stream; and, processing the dewaxed stream through the plurality of post-treatment beds to create a product stream. Other methods comprise processing the petroleum feed through the plurality of first hydrotreating reactor beds; then processing the output through the plurality of dewaxing beds to create a dewaxed stream; and, processing the dewaxed stream and the bio-feed together through the plurality of liquid quenching beds zones to create a mixed stream; and, processing the mixed stream through the plurality of post-treatment beds to create a product stream. 1. A method of processing a bio-based material feed (“bio-feed”) and a petroleum feed , the method comprising: a plurality of first hydrotreating reactor beds;', 'a plurality of second hydrotreating reactor beds;', 'a plurality of dewaxing beds; and', 'a plurality of post-treatment beds; and, 'providing one or more reactors comprising, in seriesprocessing the petroleum feed through the plurality of first hydrotreating reactor beds to create a first hydrotreated stream;processing the first hydrotreated stream and the bio-feed together through the plurality of second hydrotreating reactor beds to create a second hydrotreated stream;processing the second hydrotreated stream through the plurality of dewaxing beds to create a dewaxed stream; and,processing the dewaxed stream through the plurality of post-treatment beds to create a product stream.2. The method of wherein first hydrotreating reactor beds and the second hydrotreating reactor beds each receive a ...

Подробнее
10-01-2019 дата публикации

SYSTEMS AND METHODS FOR CARBON MONOXIDE PRODUCTION BY REDUCTION OF CARBON DIOXIDE WITH ELEMENTAL SULFUR

Номер: US20190010058A1
Принадлежит:

Thermoneutral systems and methods for producing carbon monoxide (CO) and sulfur dioxide (SO) are disclosed. The systems can include a first reaction zone and a second reaction zone, where heat generated in the first reaction zone is sufficient to drive a carbon dioxide gas (CO(g)) and elemental sulfur gas (S(g)) reaction to produce a product stream that includes CO(g) and SO(g). 1. A system for producing carbon monoxide (CO) and sulfur dioxide (SO) , the system comprising:(a) a first reaction zone configured to produce heat from an exothermic reaction of a first reaction mixture and a first product stream;{'sub': 2', '2, '(b) a second reaction zone comprising a gaseous reaction mixture of carbon dioxide (CO(g)) and elemental sulfur and configured to receive the produced heat from the first reaction zone in an amount sufficient to heat the gaseous reaction mixture and produce a second product stream comprising CO and SO;'}(c) a first outlet in fluid communication with the first reaction zone and configured to remove the first product stream from the first reaction zone; and{'sub': '2', '(d) a second outlet in fluid communication with the second reaction zone and configured to remove the second product stream comprising CO and SOfrom the second reaction zone.'}2. The system of claim 1 , wherein exothermic first reaction mixture comprises carbonyl sulfide (COS) and oxygen source oxygen (O) and the first product stream comprises COand SO.3. The system of claim 1 , wherein the second reaction zone encompasses the first reaction zone.4. The system of claim 3 , wherein the first reaction zone and the second reaction zone form a concentric reactor claim 3 , and wherein the first reaction zone is the annulus of the concentric reactor.5. The system of claim 1 , wherein the first product stream absorbs heat from the exothermic reaction claim 1 , and the system further comprises a heat exchanging unit in fluid communication with the first outlet and the second reaction zone and ...

Подробнее
09-01-2020 дата публикации

CO-PRODUCTION OF METHANOL AND AMMONIA

Номер: US20200010333A1
Принадлежит: Haldor Topsoe A/S

Process for the co-production of methanol and ammonia from a hydrocarbon feed without venting to the atmosphere carbon dioxide captured from the methanol or ammonia synthesis gas and without using expensive air separation units and water gas shift. 1. Process for co-producing methanol and ammonia from a hydrocarbon feedstock , said process comprising the steps of: 'from a second methanol processes, comprising a second reforming step and a second methanol conversion step obtaining a second effluent comprising methanol and a second gas effluent comprising hydrogen, nitrogen and unconverted carbon oxides', 'a) from a first methanol process, comprising a first reforming step and first methanol conversion step obtaining a first effluent comprising methanol and a first gas effluent comprising hydrogen, nitrogen and unconverted carbon oxides, and'}{'sub': '2', 'b) producing an ammonia synthesis gas from the first and/or second gas effluent in a common catalytic methanation stage and withdrawing said ammonia synthesis gas preferably having a H:N2 molar ratio of 3:1;'}c) catalytically converting the nitrogen and hydrogen of the ammonia synthesis gas in a common ammonia synthesis stage and withdrawing an effluent comprising ammonia and a purge-gas stream comprising hydrogen, nitrogen and/or methane.2. Process according to claim 1 , wherein in each of the first and second methanol processes claim 1 , the following steps are carried out:1) producing a methanol synthesis gas containing hydrogen, carbon oxides and nitrogen by steam reforming the hydrocarbon feedstock in a reforming section comprising a primary and a secondary reforming stage;2) catalytically converting the carbon oxides and hydrogen of the methanol synthesis gas in a once-through methanol synthesis stage and withdrawing an effluent comprising methanol and a gas effluent comprising nitrogen, hydrogen and unconverted carbon oxides.3. Process according to claim 2 , wherein the secondary reforming stage is an air- ...

Подробнее
19-01-2017 дата публикации

System and method for producing hydrogen

Номер: US20170015553A1
Принадлежит: Chiyoda Corp

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

Подробнее
21-01-2016 дата публикации

PROCESS AND APPARATUS FOR THE PRODUCTION OF SYNTHESIS GAS

Номер: US20160016793A1
Принадлежит:

Reactive diluent fluid () is introduced into a stream of synthesis gas (or “syngas”) produced in a heat-generating unit such as a partial oxidation (“PDX”) reactor () to cool the syngas and form a mixture of cooled syngas and reactive diluent fluid. Carbon dioxide and/or carbon components and/or hydrogen in the mixture of cooled syngas and reactive diluent fluid is reacted () with at least a portion of the reactive diluent fluid in the mixture to produce carbon monoxide-enriched and/or solid carbon depleted syngas which is fed into a secondary reformer unit () such as an enhanced heat transfer reformer in a heat exchange reformer process. An advantage of the invention is that problems with the mechanical integrity of the secondary unit arising from the high temperature of the syngas from the heat-generating unit are avoided.

Подробнее
17-01-2019 дата публикации

PROCESS AND SYSTEM FOR PRODUCING DIMETHYL ETHER

Номер: US20190016656A1

The invention relates to an improved process and system for the synthesis of dimethyl ether (DME) from a feedstock comprising Hand CO, wherein x=1-2. The process according to the invention comprises (a) subjecting the gaseous mixture comprising synthesis gas originating from step (c) to DME synthesis by contacting it with a catalyst capable of converting synthesis gas to DME to obtain a gaseous mixture comprising DME; (b) subjecting a gaseous mixture comprising the gaseous mixture originating from step (a) to a separation-enhanced reverse water gas shift reaction; and (c) subjecting the gaseous mixture originating from step (b) to DME/synthesis gas separation to obtain DME and a gaseous mixture comprising synthesis gas, which is recycled to step (a). Herein, the feedstock is introduced in step (a) or step (b) and the molar ratio of Hto COin the gaseous mixture which is subjected to step (b) is at least (x+0.8). Also a system for performing the reaction according to the invention is disclosed. 116-. (canceled)18. The process according to claim 17 , wherein the feedstock comprises CO claim 17 , wherein x is 1.5-2 and the feedstock is introduced in step (b).19. The process according to claim 17 , wherein the feedstock comprises CO claim 17 , wherein x is 1.9-2 and the feedstock is introduced in step (b).20. The process according to claim 19 , wherein the feedstock comprises CO claim 19 , wherein x is 1-1.5 and the feedstock is introduced in step (a).21. The process according to claim 20 , wherein the feedstock comprises CO claim 20 , wherein x is 1-1.2 and the feedstock is introduced in step (a).22. The process according to claim 17 , wherein the molar ratio of Hto COin the feedstock is in the range of (x+1) to (x+10).23. The process according to claim 17 , wherein step (a) and/or step (b) is performed in a separation-enhanced DME synthesis (SEDMES) reaction zone.24. The process according to claim 23 , wherein the SEDMES reaction zone is sorption-enhanced and comprises ...

Подробнее
16-01-2020 дата публикации

APPARATUS AND PROCESS FOR THE PRODUCTION OF FORMALDEHYDE

Номер: US20200016560A1
Принадлежит:

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

Подробнее
21-01-2021 дата публикации

USE OF TREATING ELEMENTS TO FACILITATE FLOW IN VESSELS

Номер: US20210018022A1
Принадлежит: CRYSTAPHASE PRODUCTS, INC.

A method for facilitating the distribution of the flow of one or more streams within a bed vessel is provided. Disposed within the bed vessel are internal materials and structures including multiple operating zones. One type of operating zone can be a processing zone composed of one or more beds of solid processing material. Another type of operating zone can be a treating zone. Treating zones can facilitate the distribution of the one or more streams fed to processing zones. The distribution can facilitate contact between the feed streams and the processing materials contained in the processing zones. 1. A method of improving flow distribution of one or more streams in a process vessel comprising:passing the one or more streams through more than one processing zone within the process vessel, wherein each processing zone contains processing materials; andpassing the one or more streams through a redistribution treating zone located within the processing vessel and between an upstream processing zone and a downstream processing zone, wherein the redistribution treating zone comprises at least one layer of fixed material which provides porous structures to facilitate stream flow redistribution by laterally dispersing the one or more streams to provide improved contact between the one or more streams and the downstream processing materials within the processing vessel,wherein there is no space between the upstream processing zone and the redistribution treating zone, andwherein the redistribution zone is located adjacent to both the upstream processing zone and the downstream processing zone.2. The method of claim 1 , wherein a bed zone is disposed upstream of the upstream processing zone.3. The method of claim 1 , wherein certain of the processing materials from the upstream processing zone mix into the redistribution treating zone to create a combo-zone having both processing zone functionality and treating zone functionality.4. The method of claim 1 , wherein the ...

Подробнее
26-01-2017 дата публикации

PSEUDO-ISOTHERMAL REACTOR

Номер: US20170021322A1
Принадлежит: Haldor Topsoes A/S

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

Подробнее
28-01-2016 дата публикации

FUEL REFORMER AND FUEL CELL

Номер: US20160023899A1
Принадлежит: Sumitomo Precision Products Co., Ltd.

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

Подробнее
28-01-2016 дата публикации

Multi-Stage Oxidative Dehydrogenation Process with Inter-Stage Cooling

Номер: US20160023963A1
Принадлежит:

A method of oxidatively dehydrogenating a dehydrogenation reactant includes providing a first gaseous feed stream to a first adiabatic, catalytic reaction zone with less than a stoichiometric amount of oxygen and superheated steam, oxidatively dehydrogenating dehydrogenation reactant in said first adiabatic, catalytic reaction zone and subsequently cooling the effluent, adding additional oxygen and reacting the effluent stream in at least one subsequent adiabatic reaction zone. The deydrogenation system enables higher conversion and yield per pass and in some cases greatly reduces steam usage and energy costs. In a preferred integrated process, ethylene is converted to n-butene which is then oxidatively dehydrogenated to butadiene. 1. A method of oxidatively dehydrogenating a dehydrogenation reactant comprising:(a) providing a first gaseous feed stream to a first adiabatic, catalytic reaction zone at a first-stage inlet temperature, the first feed stream including a dehydrogenation reactant, oxygen and superheated steam, wherein the molar ratio of superheated steam to dehydrogenation reactant is from 0.5:1 to 20:1;(b) oxidatively dehydrogenating dehydrogenation reactant in said first adiabatic, catalytic reaction zone to provide a first-stage effluent stream enriched in said dehydrogenated product at a first-stage effluent temperature above said first-stage inlet temperature;(c) cooling the first-stage effluent stream in a first heat transfer zone to a second-stage inlet temperature lower than said first-stage effluent temperature to provide a second gaseous feed stream comprising superheated steam, dehydrogenation reactant and dehydrogenated product;(d) feeding said second gaseous feed stream at said second-stage inlet temperature to a second adiabatic, catalytic reaction zone along with additional oxygen;(e) oxidatively dehydrogenating dehydrogenation reactant in said second adiabatic, catalytic reaction zone to provide a second stage effluent stream further ...

Подробнее
28-01-2016 дата публикации

OLEFIN CONVERSION PROCESS

Номер: US20160023964A1
Принадлежит: LUMMUS TECHNOLOGY INC.

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

Подробнее
26-01-2017 дата публикации

Reactor Components

Номер: US20170022426A1
Принадлежит:

The present disclosure relates to reactor components and their use, e.g., in regenerative reactors. A process and apparatus for utilizing different wetted areas along the flow path of a fluid in a pyrolysis reactor, e.g., a thermally regenerating reactor, such as a regenerative, reverse-flow reactor, is described. 1. A hydrocarbon conversion method comprising: {'sub': v1', 'v2', 'v2', 'v1, 'the regenerative reactor has a first portion having a first plurality of flow passages with a wetted area aand a second portion having a second plurality of flow passages with a second wetted area a, wherein the ratio of the second wetted area ato the first wetted area ais ≦0.75; and'}, 'passing a first mixture comprising hydrocarbons to a regenerative reactor, wherein'}reacting at least a portion of the hydrocarbons within the regenerative reactor to produce{'sub': '2', 'a second mixture comprising Cunsaturates.'}2. The method of claim 1 , wherein the ratio of the second wetted area ato the first wetted area ais ≦0.5.3. The method of claim 1 , wherein the ratio of the second wetted area ato the first wetted area ais in the range of 0.05 to 0.75.4. The method of claim 1 , wherein the ratio of the second wetted area ato the first wetted area ais in the range of 0.1 to 0.5.5. The method of claim 1 , comprising: [{'br': None, 'i': R', '=a', '/a', '=X, 'sub': 21', 'v2', 'v1, 'sup': (T', {'sub2': '2'}, '-T', {'sub2': '1'}, ')/300}, {'sub': 21', '2', '1, 'wherein Ris the ratio, Tis the zone temperature of the second portion in units of ° C., Tis the zone temperature of the first portion in units of ° C., and the X parameter is between 0.1 and 0.9;'}], 'calculating the ratio by the following equation{'sub': '21', 'obtaining the first portion and the second portion based on the determined ratio R; and'}disposing the first portion and second portion within the regenerative reactor.6. The method of claim 5 , wherein the X parameter is in the range of 0.25 to 0.75.7. The method of claim 1 , ...

Подробнее
25-01-2018 дата публикации

Operation Method for Hydrogen Production Apparatus, and Hydrogen Production Apparatus

Номер: US20180022605A1
Принадлежит:

A hydrogen production apparatus including a desulfurized, a reformer, a CO transformer a gas flow path, and a purge gas supply path which is provided where a purge gas is supplied to an upstream side of a pressure feeding apparatus in the gas flow path, prior to a stopping operation, a purging step of replacing gas within the gas flow path with the purge gas and filling the purge gas into the gas flow path is performed, and in a start-up operation in which a heating means is operated to increase the temperature of the gas within the gas flow path, which is performed prior to a hydrogen purification operation, a pressure increasing step of supplying the purge gas from the purge gas supply path to the closed circulation circuit and increasing the pressure within the closed circulation circuit is performed. 16.-. (canceled)7. An operation method for a hydrogen production apparatus , the hydrogen production apparatus comprising a desulfurizer that desulfurizes a source gas , a reformer that heats the desulfurized source gas in a state mixed with steam with a heating means and obtains a reformed gas , a CO transformer that causes carbon monoxide in the reformed gas to react with steam , and a hydrogen purification unit that separates impurities other than hydrogen from transformed gas after processing by the CO transformer to purify hydrogen gas , the operation method comprising:providing a gas flow path that allows gas to flow to the desulfurizer, the reformer, the CO transformer, and the hydrogen purification unit, and providing a pressure feeding apparatus that causes gas to flow in the gas flow path,providing a hydrogen purification operation for driving the heating means and the pressure feeding apparatus to supply the source gas to the gas flow path, and a stopping operation for stopping driving of the heating means and the pressure feeding apparatus, being performed in order,providing in the gas flow path a closed circulation circuit that returns and circulates ...

Подробнее
10-02-2022 дата публикации

PROCESS FOR PRODUCING 1-(4-ISOBUTYLPHENYL)ETHANOL BY HYDROGENATION OF 1-(4-ISOBUTYL-PHENYL)ETHANONE IN THE PRESENCE OF A CATALYST COMPOSITION COMPRISING COPPER

Номер: US20220041533A1
Принадлежит:

Described is a process for producing 1-(4-isobutylphenyl)ethanol by reacting 1-(4-isobutyl-phenyl)ethanone with hydrogen in the presence of a catalyst composition comprising cop-per and one or more metals other than copper, and a use of a respective composition and/or of a pre-composition, the pre-composition comprising a mixture of oxides of copper and oxides of one or more metals other than copper, in a catalytic hydrogenation process for producing 1-(4-isobutylphenyl)ethanol from 1-(4-isobutylphenyl)ethanone. 1. A process for producing 1-(4-isobutylphenyl)ethanol comprising 'wherein the catalyst composition comprises the copper in a total amount in a range of from 30 mass-% to 98 mass-%, relative to a total mass of metals present in the catalyst composition.', 'S3) reacting 1-(4-isobutylphenyl)ethanone with hydrogen in the presence of a catalyst composition comprising copper and one or more metals other than copper,'}2. The process according to claim 1 , wherein the catalyst composition comprises the copper in a total amount in the range of from 45 mass-% to 98 mass-% relative to the total mass of metals present in the catalyst composition.3. The process according to claim 1 , wherein the catalyst composition comprises in addition to the copper: 'wherein a total amount of aluminium, silicon, zirconium and carbon in the catalyst composition, relative to the total mass of copper present in the catalyst composition, is in a range of from 2.5 mass-% to 60.0 mass-%;', 'c2) a carrier component comprising one or more substance selected from the group consisting of aluminium, aluminium compounds, silicon, silicon compounds, zirconium, zirconium compounds, carbon, and carbon compounds,'}and/or 'wherein the total amount of the one or more metal different from the group consisting of copper, aluminium, and zirconium in the catalyst composition, relative to the total mass of metals present in the catalyst composition, is in the range of from 0.1 mass-% to 55.0 mass-%.', 'c3) ...

Подробнее
23-01-2020 дата публикации

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

Номер: US20200023330A1
Автор: Rizzi Enrico
Принадлежит: Casale SA

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

Подробнее
10-02-2022 дата публикации

Use of treating elements to facilitate flow in vessels

Номер: US20220042528A1
Принадлежит: Crystaphase International Inc

A method for facilitating the distribution of the flow of one or more streams within a bed vessel is provided. Disposed within the bed vessel are internal materials and structures including multiple operating zones. One type of operating zone can be a processing zone composed of one or more beds of solid processing material. Another type of operating zone can be a treating zone. Treating zones can facilitate the distribution of the one or more streams fed to processing zones. The distribution can facilitate contact between the feed streams and the processing materials contained in the processing zones.

Подробнее
24-01-2019 дата публикации

PROCESS FOR CONVERTING MIXED HYDROCARBON STREAMS TO LPG AND BTX

Номер: US20190024000A1
Автор: Dittrich Christoph
Принадлежит:

The present invention relates to a process for converting a feed comprising C5-C12 hydrocarbons to higher BTX, LPG and methane in the presence of hydrogen in n reaction zones operated in series, wherein m reaction zones are not participating in the conversion process and only (n−m) reaction zones are operated under reaction conditions sufficient to convert at least a portion of said a feed comprising C5-C12 hydrocarbons to an effluent having said BTX. An object of the present invention is to provide a process for converting C5-C12 hydrocarbons to LPG, optionally BTX, and methane in the presence of hydrogen wherein coke formation on the catalyst is controlled and the physical movement of particulate catalyst is avoided. 1. A process for converting a mixed C5-C12 hydrocarbons stream to BTX , LPG and methane in the presence of hydrogen in n reaction zones operated in series , wherein m reaction zones are not participating in the conversion process and only (n−m) reaction zones are operated under reaction conditions sufficient to convert at least a portion of said C5-C12 hydrocarbon stream to an effluent having said BTX , wherein each reaction zone is initially numbered serially with a designator from 1 to n , the process comprising:(a) providing a quantity of catalytic material within each reaction zone;(b) providing to the reaction zone designated as 1 a hydrocarbon feedstock containing C5-C12 hydrocarbons and hydrogen;(c) cooling at least a portion of the effluent of the said reaction zone designated as 1 to the inlet temperature of the reaction zone designated as 2, and more generally, cooling at least a portion of the effluent of each reaction zone with a designator equal or smaller than (n−m−1) to the inlet temperature of the reaction zone with a designator larger by one than that of the reaction zone from which said effluent originates;(d) transferring said at least portion of said effluent of the said reaction zone designated as 1 to said reaction zone ...

Подробнее
28-01-2021 дата публикации

EFFICIENT OXIDATIVE COUPLING OF METHANE PROCESSES AND SYSTEMS

Номер: US20210024438A1
Принадлежит:

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

Подробнее
01-02-2018 дата публикации

Chemical Synthesis And Synthesis Reactors

Номер: US20180028996A1
Принадлежит: SIEMENS AKTIENGESELLSCHAFT

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

Подробнее
01-02-2018 дата публикации

Catalyst System and Use in Heavy Aromatics Conversion Processes

Номер: US20180029025A1
Принадлежит: ExxonMobil Chemical Patents Inc

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

Подробнее
17-02-2022 дата публикации

Process For Recovering Heat At High Temperatures In Plasma Reforming Systems

Номер: US20220048003A1
Принадлежит:

A heat recovery system for plasma reformers is comprised of a cascade of regenerators and recuperators that are arranged to transfer in stages the heat at high temperatures for storage, transport, and recirculation. Recirculation of heat increases the efficiency of plasma reformers and heat exchanging reduces temperature of the product for downstream applications. 1. A thermal reformer with heat recovery for the conversion of one or more reactants into products , comprising:a pre-heater where reactants are heated to temperatures greater than their incoming temperature;a heat source where said reactants are further heated to a temperature where a portion of the reactants are reformed into products;and a heat exchanging unit where a portion of the sensible heat is removed from the products;wherein the heat provided in the pre-heater was recovered from the heat exchanging unit;wherein the products have a molecular composition different from that of the reactants; andwherein said pre-heater and said heat exchanging unit are comprised of at least two different fixed-bed regenerators, such that said thermal reformer periodically switches between a first mode wherein said reactants flow into at least a first of said at least two different fixed-bed regenerators while said products flow through a second of said at least two different fixed-bed regenerators, and a second mode wherein said reactants flow into at least said second of said at least two different fixed-bed regenerators while said products flow through said first of said at least two different fixed-bed regenerators.27-. (canceled)8. The thermal reformer of claim 1 , further comprising at least two high temperature valves;wherein at least one of said high temperature valves is configured such that said reactants flow into at least said first of said at least two different fixed-bed regenerators, and at least one other of said at least two high temperature valves is configured such that said products flow into at ...

Подробнее
31-01-2019 дата публикации

METHODS FOR FLUID CONTACTING IN A DOWNFLOW VESSEL

Номер: US20190030495A1
Принадлежит:

A contacting device and method are presented for the collection, contacting, and distribution of fluids between particulate beds of a downflow vessel, which may operate in co-current flow. By one approach, the contacting device includes a liquid collection tray, a mixing channel in fluid communication with the liquid collection tray, and a liquid distribution zone. 1. A method for fluid contacting in a downflow vessel , the method comprising:collecting liquid on a liquid collection tray;passing at least a portion of the liquid through an inlet of an enclosed mixing channel of a mixing device and downstream through the mixing channel; andpassing at least a portion of vapor through a vapor inlet of the mixing channel downstream of the liquid inlet and across the liquid stream flowing through the mixing channel to contact the vapor and liquid in the mixing channel.2. The method of claim 1 , wherein passing at least a portion of the vapor through the mixing channel vapor inlet further comprises passing at least a portion of the vapor into a lower portion of the mixing channel into the liquid flowing through the mixing channel.3. The method of claim 1 , wherein passing at least a portion of the vapor through the mixing channel vapor inlet further comprises passing at least a portion of the vapor obliquely downstream into the mixing channel to facilitate the flow and contact of the liquid and vapor in the downstream direction.4. The method of claim 1 , wherein passing at least a portion of the vapor through the mixing channel vapor inlet further comprises passing at least a portion of the vapor through an upper chimney opening of a vapor chimney surrounding the vapor inlet and passing the vapor downwardly through the chimney to the mixing channel vapor inlet.5. The method of claim 4 , further comprising passing at least another portion of the vapor through a second vapor inlet of the mixing channel at a different downstream distance from the liquid inlet than the first ...

Подробнее
31-01-2019 дата публикации

LIQUID PLASMA DISCHARGE DEVICE AND METHOD FOR BIODIESEL SYNTHESIS USING SAME

Номер: US20190030509A1
Автор: Deng Shaobo, Wu Xiao, ZHU Jun
Принадлежит:

A process comprises feeding a stream of reactant compounds to a reactor and discharging a liquid plasma into the reactant stream in the reactor, wherein the plasma initiates or accelerates a reaction of the reactant compounds to form a product composition. The reactor can comprise one or more chambers, a high-voltage electrode positioned at a first portion of the one or more chambers, a ground electrode positioned at a second portion of the one or more chambers, and a dielectric plate between the ground electrode and the high-voltage electrode that comprises openings through which the reactant stream can pass from the first portion to the second portion or from the second portion to the first portion. Discharging the plasma can include supplying electrical power to the high-voltage electrode such that plasma is discharged where the reactant stream flows through the openings. 1. A plasma reactor for the generation of a stable plasma discharge , the plasma reactor comprising:a housing defining one or more interior chambers;a high-voltage electrode positioned at least partially in or proximate to a first portion of the one or more chambers;a first ground electrode positioned at least partially in or proximate to a second portion of the one or more chambers, wherein the second portion is located on a first side of the high-voltage electrode;a first dielectric plate between the first ground electrode and the high-voltage electrode, the first dielectric plate comprising one or more first openings through which a reaction stream can pass from the first portion to the second portion or from the second portion to the first portion;a feed inlet for feeding the reaction am into the one or more chambers; anda product outlet for withdrawing e reaction stream from the one or more chambers.2. A plasma reactor according to claim 1 , wherein the first portion is at a middle position in the one or more chambers and the second port s at a first outer position in the one or more ...

Подробнее
17-02-2022 дата публикации

Method for producing butadiene from ethanol with optimised in situ regeneration of the catalyst of the second reaction step

Номер: US20220048833A1

The present invention relates to a process for producing butadiene from ethanol, in two reaction steps, comprising a step a) of converting ethanol into acetaldehyde and a step b) of conversion into butadiene, said step b) simultaneously implementing a reaction step and a regeneration step in (n+n/2) fixed-bed reactors, n being equal to 4 or a multiple thereof, comprising a catalyst, said regeneration step comprising four successive regeneration phases, said step b) also implementing three regeneration loops.

Подробнее
17-02-2022 дата публикации

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

Номер: US20220048834A1
Принадлежит:

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

Подробнее
30-01-2020 дата публикации

ISOTHERMAL REACTOR

Номер: US20200030765A1
Принадлежит:

A reactor () for thermochemical reactions is provided comprising a reactor shell () having an inlet () and an outlet (). Solid catalyst () is provided in reaction zones () in which at least a portion of reactants entering the reactor () undergo a thermochemical reaction. A heat exchange medium is provided in heat exchange zones such that heat is exchanged between the reaction zones () and the heat exchange medium. One or more hollow inserts () at least partially extend through the reaction zones (). The hollow inserts () are configured to form a flow path to either: divert a portion of the reactants from the reactor inlet () or from one reaction zone to a different reaction zone; or divert a portion of the heat exchange medium from one heat exchange zone to a different heat exchange zone. 1. A reactor for thermochemical reactions , comprising:a reactor shell having an inlet for receiving reactants into the reactor and an outlet for the removal of products from the reactor;a plurality of reaction zones comprising a solid catalyst in which at least a portion of the reactants undergo a thermochemical reaction and form a reaction mixture of products and reactants;a plurality of heat exchange zones comprising a heat exchange medium;a plurality of tubes for housing the reaction zones or the heat exchange medium, wherein heat is exchanged between the reaction zones and the heat exchange medium through walls of the tubes; and form a flow path to divert a portion of the reactants or reaction mixture from the reactor inlet or from one reaction zone to a different reaction zone; or', 'form a flow path to divert a portion of the heat exchange medium from one heat exchange zone to a different heat exchange zone., 'one or more hollow inserts at least partially extending through one or more reaction zones thereby to displace solid catalyst in the reaction zone and reduce temperature variation across the reaction zone, wherein each hollow insert comprises an inlet and an outlet, ...

Подробнее
04-02-2021 дата публикации

PRODUCING C5 OLEFINS FROM STEAM CRACKER C5 FEEDS

Номер: US20210031164A1
Принадлежит: LUMMUS TECHNOLOGY LLC

Producing C5 olefins from steam cracker C5 feeds may include reacting a mixed hydrocarbon stream comprising cyclopentadiene, C5 olefins, and C6+ hydrocarbons in a dimerization reactor where cyclopentadiene is dimerized to dicyclopentadiene. The dimerization reactor effluent may be separated into a fraction comprising the C6+ hydrocarbons and dicyclopentadiene and a second fraction comprising C5 olefins and C5 dienes. The second fraction, a saturated hydrocarbon diluent stream, and hydrogen may be fed to a catalytic distillation reactor system for concurrently separating linear C5 olefins from saturated hydrocarbon diluent, cyclic C5 olefins, and C5 dienes contained in the second fraction and selectively hydrogenating C5 dienes. An overhead distillate including the linear C5 olefins and a bottoms product including cyclic C5 olefins are recovered from the catalytic distillation reactor system. Other aspects of the C5 olefin systems and processes, including catalyst configurations and control schemes, are also described. 1. A process for producing C5 olefins from a C5 feed , comprising linear C5 olefins , branched C5 olefins , C5 dienes , including cyclopentadiene , and one or more C5 paraffins , the process comprising:feeding the C5 feed, a saturated hydrocarbon diluent stream, and hydrogen to a fixed bed selective hydrogenation unit to selectively hydrogenate the C5 dienes, including cyclopentadiene, producing a partially hydrogenated stream comprising linear C5 olefins, branched C5 olefins, and remaining C5 dienes;feeding the partially hydrogenated stream to a catalytic distillation reactor system, wherein the partially hydrogenated stream is introduced below a first catalyst zone; separating the C5 olefins from the saturated hydrocarbon diluent; and', 'selectively hydrogenating at least a portion of the remaining C5 dienes to form additional linear C5 olefins and branched C5 olefins; and, 'concurrently in the catalytic distillation reactor systemrecovering linear ...

Подробнее
30-01-2020 дата публикации

Heavy Aromatics Conversion Processes and Catalyst Compositions Used Therein

Номер: US20200031740A1
Принадлежит:

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

Подробнее
05-02-2015 дата публикации

Cooled reactor for the production of dimethyl ether from methanol

Номер: US20150038745A1

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

Подробнее
11-02-2016 дата публикации

Boroaluminosilicate Molecular Sieves and Methods for Using Same for Xylene Isomerization

Номер: US20160039726A1
Автор: Amelse Jeffrey A.
Принадлежит: BP CORPORATION NORTH AMERICA INC.

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

Подробнее
24-02-2022 дата публикации

POLYMERISATION METHOD AND APPARATUS THEREFOR

Номер: US20220055003A1
Принадлежит:

A method of assembling and/or operating apparatus for undertaking a chemical reaction. The apparatus includes a housing in which a precursor of a receptacle is arranged. A fluid (F1) may be introduced into said precursor to cause the precursor to inflate. 132-. (canceled)33. A method of assembling and/or operating apparatus for carrying out a chemical reaction , the method comprising the steps of:(i) selecting a housing in which a precursor of a receptacle is arranged; and(ii) introducing a fluid (F1) into said precursor of said receptacle to cause the precursor to distend (e.g. inflate) to define a distended receptacle for receiving reagents for reaction in the apparatus.34. The method according to claim 33 , wherein claim 33 , in step (i) claim 33 , the precursor of said receptacle is substantially flaccid.35. The method according to claim 33 , wherein said housing has a volume in which said precursor of the receptacle is arranged wherein claim 33 , in the combination described in step (i) claim 33 , said precursor of the receptacle occupies less than 70% claim 33 , preferably less than 5% claim 33 , of said volume.36. The method according to claim 33 , wherein:said housing supports said precursor of said receptacle and/or said distended receptacle;said housing is elongate and, in the combination described in step (i), length (L) of the precursor of the receptacle extends at least 60% (or at least 90%) along the elongate extent of an internal region of the housing in which said precursor of said receptacle is arranged; andsaid housing is elongate and includes securement means for releasably securing said precursor and/or distended receptacle in position.37. The method according to claim 33 , wherein claim 33 , in the combination described in step (i) claim 33 , said precursor of the receptacle is secured in position relative to the housing and said precursor of said receptacle comprises a plastic material which comprises optionally-substituted alkylene units.38. ...

Подробнее
24-02-2022 дата публикации

PROCESS FOR PRODUCING BUTADIENE FROM ETHANOL WITH IN SITU REGENERATION OF THE CATALYST OF THE SECOND REACTION STEP

Номер: US20220055969A1
Принадлежит:

The present invention relates to a process for producing butadiene from ethanol, in two reaction steps, comprising a step a) of converting ethanol into acetaldehyde and a step b) of conversion into butadiene, said step b) simultaneously implementing a reaction step and a regeneration step in (n+n/2) fixed-bed reactors, n being equal to 2 or a multiple thereof, comprising a catalyst, said regeneration step comprising four successive regeneration phases, said step b) also implementing a regeneration loop for the inert gas and at least one regeneration loop for the gas streams comprising oxygen. 1. A process for producing butadiene from ethanol , comprising at least the following steps:a) a step of converting ethanol into acetaldehyde, to produce an ethanol/acetaldehyde effluent, comprising at least one reaction section (A) fed with a stream comprising ethanol and operated in the presence of a catalyst (Ca);b) a butadiene conversion step comprising at least one reaction-regenerative section in which are simultaneously performed a reaction step and a regeneration step in (n+n/2) fixed-bed reactors, n being an integer equal to 2 or a multiple thereof, said (n+n/2) fixed-bed reactors each comprising at least one fixed bed of a catalyst (Cb), said (n+n/2) fixed-bed reactors functioning in parallel and in sequence so that said reaction step starts in each of said reactors with a time shift equal to half of the catalytic cycle time of said catalyst (Cb), said reaction-regenerative section comprising a regeneration loop for inert gas and at least one regeneration loop for a gas stream comprising oxygen, and so that, at each instant:b1) said reaction step is operated in n of said fixed-bed reactors, n being an integer equal to 2 or a multiple thereof, fed at least with a fraction of said ethanol/acetaldehyde effluent obtained from step a), at a temperature of between 300 and 400° C., at a pressure of between 0.1 and 1.0 MPa, for a time equal to the catalytic cycle time of said ...

Подробнее
07-02-2019 дата публикации

HIGH PURITY HYDROGEN PRODUCTION DEVICE AND HIGH PURITY HYDROGEN PRODUCTION METHOD

Номер: US20190039890A1
Принадлежит:

A hydrogen production device is provided. The device comprises: a dry reforming reaction unit for directly reacting methane and carbon dioxide in biogas to produce a synthesis gas containing hydrogen; and a gas shift unit for reacting carbon monoxide in the synthesis gas produced in the dry reforming reaction unit with water vapor to produce carbon dioxide and hydrogen, and for capturing the produced carbon dioxide. 1. A hydrogen production device comprising: a dry reforming reaction unit for directly reacting methane and carbon dioxide in biogas to produce a synthesis gas containing hydrogen; anda gas shift unit for reacting carbon monoxide in the synthesis gas produced in the dry reforming reaction unit with water vapor to produce carbon dioxide and hydrogen, and for capturing the produced carbon dioxide.2. The hydrogen production device according to claim 1 ,wherein the carbon dioxide captured in the gas shift unit is supplied to the dry reforming reaction unit to be recycled in the reaction with methane in biogas.3. The hydrogen production device according to claim 1 ,wherein the gas shift unit comprises a hydrogen production catalyst and an adsorbent for capturing carbon dioxide, andwherein the weight ratio of the hydrogen production catalyst and the adsorbent for capturing carbon dioxide is 1:9 to 9:1.4. The hydrogen production device according to claim 1 ,wherein the hydrogen production catalyst comprises at least one transition metal selected from the group consisting of Cu, Ni, and Fe.5. The hydrogen production device according to claim 1 ,wherein the adsorbent for capturing carbon dioxide comprises an alkali metal double salt-based adsorbent or a hydrotalcite-based adsorbent.6. The hydrogen production device according to claim 5 ,wherein the alkali metal double salt-based adsorbent is an adsorbent prepared by coprecipitation or impregnation process of an alkaline earth metal carbonate, and [{'br': None, 'i': 'x', 'sub': '2', '(1−)M(OH)\u2003\u2003Formula 1 ...

Подробнее
06-02-2020 дата публикации

MULTIPLE-BED CATALYTIC REACTOR COMPRISING A MIXING DEVICE

Номер: US20200038816A1
Принадлежит: Haldor Topsoe A/S

The present invention relates to multi-bed catalytic reactor with a cylindrical shape comprising a mixing device mounted between two catalyst beds in the reactor, said mixing device has a circular outer rim which corresponds to the inner wall of the reactor, the mixing device comprises; collecting means disposed in a collecting section for collecting fluid from an up¬stream catalytic bed, mixing means disposed in a mixing section for mixing the collected fluid comprising guide vanes and guide ramps, and discharging means disposed in a discharging section for discharging the mixed fluid to a down-stream catalytic bed; wherein the collecting section, the mixing section and the discharging section are disposed outside the center of the circular cross-section of the reactor, as well as associated methods for mixing and the use of such a mixing device in catalytic reactors. 1. A multi-bed catalytic reactor with a cylindrical shape comprising a mixing device mounted between two catalyst beds in said reactor , said mixing device has a circular outer rim adapted to fit within the inner wall of the reactor , the mixing device comprises;collecting means disposed in a collecting section for collecting fluid from an up-stream catalytic bed,mixing means disposed in a mixing section comprising a floor, a ceiling and inner and outer walls for mixing the collected fluid, anddischarging means disposed in a discharging section for discharging the mixed fluid to a down-stream catalytic bed;wherein the mixing device has a donut shape and the collecting section, the mixing section and the discharging section are disposed outside the centre of the circular cross-section of the reactor and wherein said mixing means comprise guide vanes with a first and a second end, guide ramps with a first and a second end or comprises said guide vanes and said guide ramps.2. A multi-bed catalytic reactor with a cylindrical shape comprising a mixing device according to claim 1 , wherein the floor of said ...

Подробнее
24-02-2022 дата публикации

SYSTEM FOR PRE-PURIFICATION OF A FEED GAS STREAM

Номер: US20220057137A1
Принадлежит:

A system and method of pre-purification of a feed gas stream is provided that is particularly suitable for pre-purification of a feed air stream in cryogenic air separation unit. The disclosed pre-purification systems and methods are configured to remove substantially all of the hydrogen, carbon monoxide, water, and carbon dioxide impurities from a feed air stream and is particularly suitable for use in a high purity or ultra-high purity nitrogen plant. The pre-purification systems and methods preferably employ two or more separate layers of hopcalite catalyst with the successive layers of the hopcalite separated by a zeolite adsorbent layer that removes water and carbon dioxide produced in the hopcalite layers. Alternatively, the pre-purification systems and methods employ a hopcalite catalyst layer and a noble metal catalyst layer separated by a zeolite adsorbent layer that removes water and carbon dioxide produced in the hopcalite layer. 1. A method of purifying a gas stream to remove the hydrogen and carbon monoxide impurities present in the gas stream , the method comprising:(a) passing the gas stream substantially free of carbon dioxide and water through a first catalyst layer comprising a mixture manganese and copper oxides configured to remove at least some of the carbon monoxide and hydrogen from the gas stream and produce a first intermediate effluent;(b) passing the first intermediate effluent through an adsorbent layer disposed downstream of the first catalyst layer, the adsorbent layer configured to remove water and carbon dioxide from the intermediate effluent and produce a second intermediate effluent; and(c) passing the second intermediate effluent through a second catalyst layer disposed downstream of the adsorbent layer, the second catalyst layer configured to remove at least hydrogen from the second intermediate effluent to yield an intermediate purified stream.2. The method of claim 1 , wherein the intermediate purified stream is substantially ...

Подробнее
07-02-2019 дата публикации

PROCESS FOR CONVERTING LPG TO HIGHER HYDROCARBON(S)

Номер: US20190040324A1
Автор: Dittrich Christoph
Принадлежит:

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

Подробнее
18-02-2021 дата публикации

Oxycombustion with co2 capture in reverse flow reactors

Номер: US20210047181A1
Принадлежит: ExxonMobil Research and Engineering Co

Systems and methods are provided for using oxycombustion to provide heat within a reverse flow reactor environment. The oxygen for the oxycombustion can be provided by oxygen stored in an oxygen storage component in the reactor. By using an oxygen storage component to provide the oxygen for combustion during the regeneration step, heat can be added to a reverse flow reactor while reducing or minimizing addition of diluents and while avoiding the need for an air separation unit. As a result, a regeneration flue gas can be formed that is substantially composed of CO2 and/or H2O without requiring the additional cost of creating a substantially pure oxygen-containing gas flow.

Подробнее
03-03-2022 дата публикации

Process And Reactor Comprising A Plurality Of Catalyst Receptacles

Номер: US20220064000A1
Автор: Gray Julian Stuart
Принадлежит:

A reactor having a shell comprising one or more reactor tubes located within the shell, said reactor tube or tubes comprising a plurality of catalyst receptacles containing catalyst; means for providing a heat transfer fluid to the reactor shell such that the heat transfer fluid contacts the tube or tubes; an inlet for providing reactants to the reactor tubes; and an outlet for recovering products from the reactor tubes; wherein the plurality of catalyst receptacles containing catalyst within a tube comprises catalyst receptacles containing catalyst of at least two configurations.

Подробнее
14-02-2019 дата публикации

USE OF TREATING ELEMENTS TO FACILITATE FLOW IN VESSELS

Номер: US20190048903A1
Принадлежит: CRYSTAPHASE PRODUCTS, INC.

A method for facilitating the distribution of the flow of one or more streams within a bed vessel is provided. Disposed within the bed vessel are internal materials and structures including multiple operating zones. One type of operating zone can be a processing zone composed of one or more beds of solid processing material. Another type of operating zone can be a treating zone. Treating zones can facilitate the distribution of the one or more streams fed to processing zones. The distribution can facilitate contact between the feed streams and the processing materials contained in the processing zones. 1passing the one or more streams through an upstream processing zone and a downstream processing zone within the process vessel, the upstream processing zone and downstream processing zone each containing one or more beds of processing materials;passing the one or more streams through a redistribution treating zone located between the upstream processing zone and downstream processing zone, wherein the redistribution treating zone comprises a single layer of a fixed, form-fit fibrous mesh material conforming to the interior dimensions of the process vessel; andlaterally dispersing the one or streams with the fibrous mesh material to provide improved contact between the one or more streams and the processing materials in the downstream processing zone.. A method of improving flow distribution of one or more streams in a process vessel comprising: This application is a continuation application and claims the benefit, and priority benefit, of U.S. patent application Ser. No. 15/720,751, filed Sep. 29, 2017, which is a continuation and claims the benefit, and priority benefit, of U.S. patent application Ser. No. 15/676,603, filed Aug. 14, 2017, which claims the benefit and priority benefit of U.S. patent application Ser. No. 15/265,405, filed Sep. 14, 2016, which claims the benefit and priority benefit of U.S. Provisional Patent Application Ser. No. 62/314,069, filed Mar. ...

Подробнее
13-02-2020 дата публикации

Hydrocarbon Pyrolysis

Номер: US20200048163A1
Принадлежит:

The invention relates to hydrocarbon pyrolysis, to equipment and materials useful for hydrocarbon pyrolysis, to processes for carrying out hydrocarbon pyrolysis, and to the use of hydrocarbon pyrolysis for, e.g., hydrocarbon upgrading. 124-. (canceled)25. A reactor for pyrolysing a hydrocarbon feed under predetermined pyrolysis conditions , the reactor comprising{'sub': 'R', '(a) an elongated tubular vessel having (i) an internal volume which includes first and second regions and (ii) opposed first and second openings in fluidic communication with the internal volume, the first and second openings being separated by a reactor length (L), and'}{'sub': s', 'p, 'sup': '3', 'claim-text': [ (A) a first aperture, the first aperture being proximate to the first opening and in fluidic communication with the first opening,', '(B) at least one internal channel in fluidic communication with the first aperture, and', {'sub': 1', '1', 'R, '(C) a second aperture, the second aperture being in fluidic communication with the first aperture via a flowpath Lthrough the channel, Lbeing ≥0.1*L; and'}], '(i) the first channeled thermal mass includes, [{'br': None, 'i': t', '*C', '*R*T', '*ΔT', '*X*ΔH*P, 'sub': R', 's', 'p', 'av', 'av', 'P, 'sup': '−1', '([OFA-1]/OFA)=(*ρ)*(t), wherein,'}, "(A) R is the feed's Gas Constant and", {'sub': R', 'av', 'p', 'p', 'av', 'P', 'av, '(B) the predetermined pyrolysis conditions include a residence time in the channel (t)≤1 sec., a feed conversion (X)≥50%, an average total pressure in the channel (P)≥1 bar, an average bulk gas temperature in the channel (T)≤1500° C. at the start of the pyrolysis, a peak gas temperature (T) located in the channel, T>T, a pyrolysis step time tin the range of from 0.001 sec. to 50 sec., and a change in average bulk gas temperature during the pyrolysis (ΔT)≤100° C.'}], '(ii) the OFA is determined from the formula], '(b) a channeled thermal mass located in the first region, wherein the first channeled thermal mass has a ...

Подробнее
03-03-2016 дата публикации

APPARATUS AND METHOD FOR CRACKING GASES

Номер: US20160059197A1
Принадлежит:

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

Подробнее
03-03-2016 дата публикации

Method and Catalyst System for the Production of Para-Xylene

Номер: US20160059224A1
Принадлежит:

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

Подробнее
21-02-2019 дата публикации

ALKANE OXIDATIVE DEHYDROGENATION (ODH)

Номер: US20190055177A1
Принадлежит:

Processes and associated reaction systems for the oxidative dehydrogenation of an alkane containing 2 to 6 carbon atoms, preferably ethane or propane, more preferably ethane, are provided. In particular, a process is provided that comprises supplying a feed gas comprising the alkane and oxygen to a reactor vessel that comprises an upstream and downstream catalyst bed; contacting the feed gas with an oxidative dehydrogenation catalyst in the upstream catalyst bed, followed by contact with an oxidative dehydrogenation/oxygen removal catalyst in the downstream catalyst bed, to yield a reactor effluent comprising the alkene; and supplying an upstream coolant to an upstream shell space of the reactor vessel from an upstream coolant circuit and a downstream coolant to a downstream shell space of the reactor vessel from a downstream coolant circuit. 1. A process for the oxidative dehydrogenation of an alkane containing 2 to 6 carbon atoms , preferably ethane or propane , more preferably ethane , to an alkene containing 2 to 6 carbon atoms , preferably ethylene or propylene , more preferably ethylene , comprising:supplying a feed gas comprising the alkane and oxygen to an inlet of a reactor vessel, the reactor vessel comprising a reactor shell, a plurality of reactor tubes disposed within an interior of the reactor shell, and a perforated partition that divides the interior of the reactor vessel into an upstream region and a downstream region, wherein the plurality of reactor tubes comprise:(i) an upstream catalyst bed positioned within the upstream region that comprises an oxidative dehydrogenation catalyst comprising tellurium, and(ii) a downstream catalyst bed positioned with the downstream region that comprises an oxidative dehydrogenation/oxygen removal catalyst;contacting the feed gas with the oxidative dehydrogenation catalyst in the upstream catalyst bed, followed by contact with the oxidative dehydrogenation/oxygen removal catalyst in the downstream catalyst bed, ...

Подробнее
01-03-2018 дата публикации

OLEFIN CONVERSION PROCESS

Номер: US20180057424A1
Принадлежит: LUMMUS TECHNOLOGY INC.

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

Подробнее
03-03-2016 дата публикации

Methods and apparatuses for hydroprocessing hydrocarbons

Номер: US20160060548A1
Принадлежит: UOP LLC

Methods and apparatuses for hydroprocessing a hydrocarbon stream are provided herein. In an embodiment, a method of hydroprocessing the hydrocarbon stream includes hydrocracking the hydrocarbon stream in a first hydrocracking stage in the presence of a first hydrocracking catalyst to produce a first conversion stream. Components from the first conversion stream are treated in a downstream processing stage in the presence of a downstream resid hydrotreating catalyst to produce a second conversion stream.

Подробнее
01-03-2018 дата публикации

MIXING DEVICE FOR A DOWN-FLOW HYDROPROCESSING REACTOR

Номер: US20180057757A1
Принадлежит:

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

Подробнее
20-02-2020 дата публикации

ETHYLENE-TO-LIQUIDS SYSTEMS AND METHODS

Номер: US20200055796A1
Принадлежит:

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

Подробнее
22-05-2014 дата публикации

Improvements in Hydrogen Generators

Номер: US20140140903A1
Принадлежит: QINETIQ LIMITED

A pyrolytic hydrogen generator comprising a pressure vessel containing a plurality of cardboard receptacles for the thermally decomposable hydrogen generating material and an associated ignition system. Also, a modular pellet tray assembly for use in the generator comprises a plurality of trays having pellet holders and associated igniters and held in a stack by support rods that also provide electrical connectivity to the trays. 1. A modular pellet tray assembly for use in a pyrolytic hydrogen generator comprising a plurality of pellet holder trays mounted on top of each other by means of a plurality of support rods to form a stack , wherein each tray comprises a plurality of pellet holders and associated ignitors for igniting any pellets loaded , in use , into the respective pellet holders , and wherein the support rods also provide electrical connectivity within the stack.2. An assembly according to claim 1 , wherein the support rods provide the electrical connectivity to operate the ignitors.3. An assembly according to claim 1 , wherein the support rods form columns of support rods extending throughout the length of the stack.4. An assembly according to claim 3 , wherein each column is formed from a single support rod roughly the same length as the stack.5. An assembly according to claim 1 , wherein the assembly is formed from complete trays that include a set of pellet holders and a set of support rods that are roughly the same length as the pellet holders whereby the stack has been assembled by stacking each complete tray on top of the one below.6. An assembly according to claim 1 , wherein the support rods are received within conducting bores or channels located in each tray.7. An assembly according to claim 1 , wherein pellet holders of the respective trays are aligned throughout the stack to form columns of pellet holders.8. An assembly according to claim 1 , wherein the pellet holders each comprise a cardboard housing.9. A pyrolytic hydrogen generator ...

Подробнее
17-03-2022 дата публикации

UPFLOW REACTOR

Номер: US20220080375A1
Принадлежит:

An upflow reactor (), comprising a housing (), a catalyst bed layer () and a pressing device (). The housing () is internally provided with a reaction chamber (), a reaction material inlet () and a reaction material outlet () which are in communication with the reaction chamber () are provided on the housing (); the catalyst bed layer () is provided within the reaction chamber (), the pressing device () is provided within the reaction chamber () and located above the catalyst bed layer (), and at least a part of the pressing device () is provided to be movable up and down, so that the at least a part of the pressing device () can be pressed against the catalyst bed layer (). 1. An upflow reactor , comprising:a housing provided with a reaction chamber therein, and provided with a reaction material inlet and a reaction material outlet thereon, which are in communication with the reaction chamber;a catalyst bed layer arranged in the reaction chamber; anda pressing device arranged in the reaction chamber and located above the catalyst bed layer, wherein at least a part of the pressing device is arranged to be movable up and down, so that the at least a part of the pressing device is able to be pressed against the catalyst bed layer.2. The upflow reactor of claim 1 , wherein the upflow reactor comprises a plurality of catalyst bed layers and a plurality of pressing devices claim 1 , the plurality of catalyst bed layers and the plurality of pressing devices are disposed alternately in the vertical direction claim 1 , and each of the pressing devices is able to be pressed against one of the catalyst bed layers; optionally claim 1 , the plurality of catalyst bed layers are in height incremented in the material feeding direction.3. The upflow reactor of claim 1 , wherein the catalyst bed layer comprises an upper catalyst section and a lower catalyst section claim 1 , wherein the upper catalyst section is positioned above the lower catalyst section claim 1 , and the pressing ...

Подробнее
28-02-2019 дата публикации

Systems for selective naphtha reforming

Номер: US20190062650A1
Принадлежит: Phillips 66 Co

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

Подробнее
27-02-2020 дата публикации

METHOD AND DEVICE FOR CARRYING OUT ENDOTHERMIC GAS PHASE-SOLID OR GAS-SOLID REACTIONS

Номер: US20200061565A1
Принадлежит: BASF SE

The present invention relates to a process for conducting endothermic gas phase or gas-solid reactions, wherein the endothermic reaction is conducted in a production phase in a first reactor zone, the production zone, which is at least partly filled with solid particles, where the solid particles are in the form of a fixed bed, of a moving bed and in sections/or in the form of a fluidized bed, and the product-containing gas stream is drawn off from the production zone in the region of the highest temperature level plus/minus 200 K and the product-containing gas stream is guided through a second reactor zone, the heat recycling zone, which at least partly comprises a fixed bed, where the heat from the product-containing gas stream is stored in the fixed bed, and, in the subsequent purge step, a purge gas is guided through the production zone and the heat recycling zone in the same flow direction, and, in a heating zone disposed between the production zone and the heat recycling zone, the heat required for the endothermic reaction is introduced into the product-containing gas stream and into the purge stream or into the purge stream, and then, in a regeneration phase, a gas is passed through the two reactor zones in the reverse flow direction and the production zone is heated up; the present invention further relates to a structured reactor comprising three zones, a production zone containing solid particles, a heating zone and a heat recycling zone containing a fixed bed, wherein the solid particles and the fixed bed consist of different materials. 1: A process for conducting endothermic gas phase or gas-solid reactions , the process comprising:conducting an endothermic reaction in a production step in a first reactor zone, a production zone, which is at least partly filled with solid particles, where the solid particles are in the form of a fixed bed, of a moving bed and in sections or in the form of a fluidized bed, anddrawing off a product-containing gas stream ...

Подробнее
10-03-2016 дата публикации

METHOD FOR PRE-REFORMING HYDROCARBONS

Номер: US20160068391A1

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

Подробнее
09-03-2017 дата публикации

REACTOR FOR A CATALYTIC PROCESS

Номер: US20170065955A1
Автор: Bergstrom Jesper
Принадлежит: Haldor Topsoe A/S

A reactor for a catalytic process comprising one or more catalyst beds has catalyst bed supports constructed as a grid comprising a plurality of cassettes (), which are covered with easily removable screens (). The down-time and service costs for the reactor are thereby lowered. 1. Reactor for a catalytic process with one or more catalyst beds of catalyst pellets , comprising a bottom support for each of said catalyst beds , the support is constructed as a grid comprising a plurality of cassettes , each cassette is covered by a permeable screen with apertures large enough to allow flow through of process fluid , but small enough to retain the catalyst pellets , wherein said screen is removable fastened to said cassette.2. Reactor according to claim 1 , wherein the apertures of the screen each has an area of between 500 mmand 0.1 mm.3. Reactor according to claim 1 , wherein the apertures of the screen each has an area of between 100 mmand 1 mm.4. Reactor according to claim 1 , wherein the screen is made by woven wire mesh.5. Reactor according to claim 1 , wherein the screen is made by welded wires and rods.6. Reactor according to claim 1 , wherein the screen is made by a flat printed pattern.7. Reactor according to claim 1 , wherein the weight of the screen is below 100 kg.8. Reactor according to claim 1 , wherein the weight of the screen is below 25 kg.9. Reactor according to claim 1 , wherein the screen is fixed to the cassette by means of quick release means claim 1 , enabling the screen to be fixed to or detached from the cassette by hand or by hand tools in less than 30 minutes.10. Reactor according to claim 1 , wherein the screen is fixed to the cassette by means of quick release means claim 1 , enabling the screen to be fixed to or detached from the cassette by hand or by hand tools in less than 5 minutes.11. Reactor according to claim 1 , wherein a majority of the screens in the reactor are rectangular and each is fixed to a cassette in each of its four ...

Подробнее
12-03-2015 дата публикации

SYSTEMS FOR PYROLYSIS VAPOR UPGRADING

Номер: US20150071836A1
Принадлежит: Phillips 66 Company

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

Подробнее
17-03-2016 дата публикации

Apparatus And Method For Heterogeneous Catalytic Reactions

Номер: US20160074824A1
Принадлежит:

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

Подробнее
15-03-2018 дата публикации

COMPACT COMBINED MIXING AND DISTRIBUTION DEVICE

Номер: US20180071703A1
Принадлежит: IFP ENERGIES NOUVELLES

A device for mixing and distributing fluids for a downward flow catalytic reactor, said device comprising: 1. A device for mixing and distributing fluids for a downward flow catalytic reactor , said device comprising:{'b': '5', 'at least one collection zone (A) comprising at least one collection means ();'}{'b': 7', '5', '8', '7, 'at least one substantially vertical collection conduit () adapted to receive a reaction fluid collected by said collection means () and at least one injection means () opening into said collection conduit () to inject a quench fluid;'}{'b': 5', '9', '7', '10, 'at least one mixing zone (B) disposed downstream of the collection means () in the direction of flow of the fluids, said mixing zone (B) comprising at least one mixing chamber () connected to said collection conduit () and an outlet end () for discharge of the fluids; and'}{'b': '12', 'at least one distribution zone (C) disposed downstream of said mixing zone (B) in the direction of flow of the fluids comprising a distribution plate () supporting a plurality of chimneys;'}{'b': 16', '17', '17, 'i': a', 'b, 'characterised in that said mixing zone (B) is disposed at the same level as the distribution one (C), said mixing zone (B) and said distribution zone (C) being delimited by at least one annular wall () comprising at least one lateral passage section (, ) adapted for the passage of the fluids from said mixing zone (B) to said distribution zone (C).'}21516. A device according to characterised in that said mixing zone (B) is included in an annular enclosure () comprising said annular wall ().316. A device according to characterised in that said annular wall () internally delimits said distribution zone (C).41622. A device according to characterised in that said annular wall () is positioned at a spacing d from the enclosure of the reactor claim 1 , the spacing d varying from 2% to 20% of the diameter of the reactor.5911. A device according to characterised in that said mixing chamber ...

Подробнее
15-03-2018 дата публикации

ETHANE RECOVERY PROCESS AND ALKYLATION PROCESS WITH ETHANE RECOVERY

Номер: US20180072640A1
Принадлежит: LUMMUS TECHNOLOGY INC.

Processes and systems for the production of ethylbenzene using a dilute ethylene feed and subsequent recovery of ethane in the alkylation vent gas. 1. A process for the recovery of ethane , comprising:feeding a first stream comprising methane, ethane, and ethylene to a reboiled absorber column;contacting the first stream with an absorbent-reactant in the reboiled absorber column to absorb essentially all of the ethane and ethylene, producing a rich oil bottoms stream comprising the absorbent-reactant, ethylene, and ethane, and a vapor stream comprising methane;reacting the ethylene and the absorbent-reactant in a reaction zone, producing a reaction zone effluent comprising ethane and a reaction product;stripping the effluent in a stripper to produce a lean oil bottoms stream and an overhead vapor stream comprising ethane.2. The process of claim 1 , wherein the first stream and the vapor stream each further comprise one or more of nitrogen claim 1 , hydrogen claim 1 , carbon monoxide claim 1 , and carbon dioxide.3. The process of claim 1 , further comprising:operating the reboiled absorber column at a bottoms temperature in the range from about 150° C. to about 220° C.;operating the stripper at a bottoms temperature in the range from about 200° C. to about 280° C.4. The process of claim 1 , further comprising recycling at least a portion of the lean oil bottoms steam from the stripper to the reboiled absorber column as the absorbent-reactant.5. The process of claim 4 , further comprising introducing the absorbent-reactant proximate an upper end of the reboiled absorber column at a temperature in the range from about −20° C. to about 50° C.6. The process of claim 1 , wherein the reboiled absorber column comprises multiple reboilers configured to sequentially extract heat from the lean oil bottoms stream from the stripper.7. The process of claim 6 , wherein the multiple reboilers comprise one or more side reboilers.8. The process of claim 6 , further comprising ...

Подробнее
24-03-2022 дата публикации

CATALYTIC PYROLYSIS OF POLYSTYRENE INTO AROMATIC RICH LIQUID PRODUCT USING SPHERICAL CATALYST

Номер: US20220089831A1
Принадлежит: INDIAN OIL CORPORATION LIMITED

The present invention provides a process of catalytic depolymerization of polystyrene involving a spherical catalyst, an apparatus for carrying out the depolymerization, recovering the aromatic rich liquid product and recycling the catalyst without any decrease in the catalytic performance. Further, the present invention provides that the aromatic rich liquid product includes styrene, xylene, benzene, ethyl benzene, with styrene content greater than 65%. Additionally, the catalyst involved in the depolymerization process is a spherical catalyst that is easily recovered from coke/char formed during the process and is recycled and reused without any decrease in the catalytic performance. 1. A process of catalytic depolymerization of polystyrene , the process comprising:(a) adding a polystyrene feed and a catalyst into a reactor, wherein the catalyst and the feed are added together, or the feed is added first followed by the catalyst, or the feed is added into the reactor containing the catalyst; wherein the catalyst is a spherical catalyst;(b) mixing of the feed with the catalyst in the reactor to obtain a mixture and heating the mixture at a rate ranging from 3 to 20° C./min in an inert atmosphere for generating vapor;(c) passing the vapor from the reactor to a condenser to obtain a condensate, wherein a heating tape is connected to a temperature controller in the reactor to prevent condensation of the vapor before entering the condenser; and(d) routing the condensate from the condenser to a liquid product collection flask and passing un-condensable gases from the condenser through a scrubber; wherein the liquid product is present in an amount ranging from 85% to 90% by weight comprising styrene in an amount ranging from 65% to 71% by weight of the liquid product.2. The process as claimed in claim 1 , wherein the feed is a styrene rich polymer waste comprising styrene in an amount ranging from 20% to 100% by weight claim 1 , wherein the styrene rich polymer is ...

Подробнее
05-03-2020 дата публикации

ETHYLENE-TO-LIQUIDS SYSTEMS AND METHODS

Номер: US20200071242A1
Принадлежит:

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

Подробнее
18-03-2021 дата публикации

MULTI-BED CATALYTIC CONVERTER WITH INTER-BED COOLING

Номер: US20210077968A1
Принадлежит:

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

Подробнее
14-03-2019 дата публикации

Methods and apparatus for fluid contacting in a downflow vessel

Номер: US20190076806A1
Принадлежит: UOP LLC

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

Подробнее
22-03-2018 дата публикации

SHELL AND TUBE OXIDATION REACTOR WITH IMPROVED RESISTANCE TO FOULING

Номер: US20180078919A1
Принадлежит:

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

Подробнее
26-03-2015 дата публикации

REACTIVE RECTIFICATION COLUMN FOR PERFORMING CHEMICAL REACTIONS

Номер: US20150086430A1

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

Подробнее
23-03-2017 дата публикации

Inherently safe odh operation

Номер: US20170081261A1
Принадлежит: Nova Chemicals International SA

In the operation of an oxidative dehydrogenation (ODH) process, it is desirable to remove oxygen in the product stream for a number of reasons, including to reduce oxidation of the product. This may be achieved by having several pre-reactors upstream of the main reactor having a catalyst system containing labile oxygen. The feed passes through one or more reactors saturated with labile oxygen. When the labile oxygen is consumed through a valve system, the pre-reactor accepts product from the main reactor and complexes reactive oxygen in the product stream until the catalyst system is saturated with labile oxygen. Then the reactor becomes a pre-reactor and another pre-reactor becomes a scavenger.

Подробнее
12-06-2014 дата публикации

METHOD FOR CARRYING OUT EXOTHERMIC CATALYTIC REACTIONS AND A REACTOR FOR USE IN THE METHOD

Номер: US20140163260A1
Автор: THORHAUGE Max
Принадлежит: Haldor Topso A/S

Method and a reactor for performing exothermic catalytic reactions. The method comprises the steps of providing a feed gas stream comprising reactants for the exothermic catalytic reaction to a fixed bed catalytic reactor comprising one or more catalyst beds each with catalyst particles filled sections with a catalyst volume; providing a feed gas bypass inside the reactor by arranging within at least one of the catalyst beds a number of bypass passageways without catalytic active particles inside the passageways and having a cooling surface area; passing a part of the feed gas stream through the bypass passageways and reminder of the stream through the catalyst particles filled sections; and removing heat from the feed gas stream being passed through the catalyst filled sections by indirect heat transfer to the part of the feed gas stream being passed through the bypass passageways. 2. The method of claim 1 , wherein the ratio of the catalyst volume to the cooling surface VCAT/ACOOL is between 0.01 m and 0.04 m claim 1 , and wherein the total superficial area (Ab)of the bypass passageways is adjusted to result in a value M of between 0.9 and 1.2.3. The method according to claim 1 , wherein the feed gas stream is passed in series through at least two catalyst beds provided with the bypass passageways.4. The method according to claim 1 , wherein the feed gas stream being withdrawn from the at least one catalyst bed is cooled by heat exchange or by quench cooling with a feed gas stream prior to further conversion.6. The catalytic reactor according to claim 5 , wherein the ratio of the catalyst volume (VCAT) to the cooling surface (ACOOL) is between 0.01 m and 0.04 m claim 5 , and the total superficial area (Ab) of the bypass passageways has a value M of between 0.9 and 1.2.7. The catalytic reactor of claim 5 , comprising at least two catalyst beds arranged in series and each provided with the bypass passageways.8. The catalytic reactor according to claim 5 , further ...

Подробнее
12-03-2020 дата публикации

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

Номер: US20200079710A1
Принадлежит:

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

Подробнее