ТВЕРДОЖИДКОСТНАЯ РЕАКЦИЯ

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

СПОСОБ ПОВЫШЕНИЯ ПРОИЗВОДИТЕЛЬНОСТИ УСТАНОВКИ ДЛЯ ПОЛУЧЕНИЯ АММИАКА

Изобретение относится к области получения аммиака на основе риформинга углеводородов, в частности к способу повышения производительности установки для получения аммиака. Способ включает увеличение количества водорода, вырабатываемого секцией риформинга, посредством замены труб первичного риформера новыми трубами, имеющими меньшую толщину, для увеличения внутреннего диаметра труб, и установки источника кислорода для обогащения кислородом, поставляемым этим источником, воздуха, подаваемого на вторичный риформер, модернизацию воздушного компрессора посредством установки новых статорных и роторных частей, для увеличения расхода воздуха, подаваемого во вторичный риформер, при сохранении прежнего выходного давления, а также модернизацию секции удаления СО, компрессора синтез-газа, блока осушения синтез-газа и контура синтеза аммиака. Изобретение обеспечивает повышение производительности установки для получения аммиака. 7 з.п. ф-лы, 1 ил.

СПОСОБ АЛКИЛИРОВАНИЯ ИЗОБУТАНА В ТРЕХФАЗНОМ РЕАКТОРЕ С НЕПОДВИЖНЫМ СЛОЕМ КАТАЛИЗАТОРА

Изобретение относится к способу алкилирования изобутана в трехфазном реакторе с неподвижным слоем катализатора бутилены подают на каждый слой катализатора, а изобутан, взятый в избытке, в верхнюю часть реактора, проводят реакцию алкилирования, отделяют и возвращают на рецикл непрореагировавпшй изобутан и выводят полученный алкилбензин. Температуру и давление выбирают так, чтобы пары изобутана находились в состоянии насыщения, а дополнительное испарение жидкости в реакторе под действием тепла реакции обеспечивало изотермические условия процесса алкилирования. Жидкость стекает свободно без барботирования под действием силы тяжести при объемной скорости, составляющей не более W, равного,и не менее W, равного,где D - сечение слоя катализатора, м, ε - порозность слоя катализатора, ε- паросодержание в реакторе в условиях проведения реакции, ρ- плотность жидкости на входе в реактор, кг/м, ρ- плотность паров в реакторе в условиях проведения реакции, кг/м, - максимальная линейная скорость свободно ...

ТЕПЛООБМЕННЫЙ РЕАКТОР ДЛЯ ПРОИЗВОДСТВА ВОДОРОДА С ПОМОЩЬЮ ВСТРОЕННОГО ПУЧКА ПАРОГЕНЕРАТОРА

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

СПОСОБ ЗАСЫПКИ ПРОДОЛЬНОГО УЧАСТКА КОНТАКТНОЙ ТРУБЫ

Изобретение касается способа засыпки продольного участка контактной трубы единообразной частью твердого слоя катализатора. Способ засыпки продольного участка контактной трубы единообразной частью твердого слоя катализатора, активная масса которого представляет собой, по меньшей мере, один мультиэлементный оксид, который содержит a) элементы Мо, Fe и Bi, или b) элементы Мо и V, или c) элемент V, а также дополнительно Р и/или Sb, или активная масса которого содержит элементарное серебро на оксидном изделии-носителе, и который состоит из одного единственного сорта Sили из гомогенизированной смеси нескольких отличных друг от друга сортов Sкаталитически активных формованных изделий определенной геометрической формы или каталитически активных формованных изделий и инертных формованных изделий определенной геометрической формы, причем медиана максимальных продольных размеров L изделий определенной геометрической формы сорта Sхарактеризуется значением D , по меньшей мере, в пределах одного сорта ...

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

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

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

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

СПОСОБ РЕАЛИЗУЕМОГО В НЕПРЕРЫВНОМ РЕЖИМЕ ДЛИТЕЛЬНОГО ГЕТЕРОГЕННО КАТАЛИЗИРУЕМОГО ЧАСТИЧНОГО ДЕГИДРИРОВАНИЯ УГЛЕВОДОРОДОВ

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 ...

РЕАКТОР АВТОТЕРМИЧЕСКОГО РИФОРМИНГА ПРИРОДНОГО ГАЗА

Полезная модель относится к области газопереработки. Описан реактор автотермического риформинга для получения синтез-газа, характеризующийся тем, что содержит две последовательные секции, объединяющиеся газовым потоком, при этом нижняя секция состоит из камеры подачи исходных реагентов, матричных горелок и камеры сгорания, а верхняя секция представляет собой трубки, в которых загружен катализатор паровой конверсии метана и/или СО, а межтрубное пространство заполнено продуктовым синтез-газом. Технический результат - получение синтез-газа регулируемого состава основных компонентов в автотермическом режиме без использования энергии извне в одном реакторе. 1 ил.

СПОСОБ И УСТРОЙСТВО ДЛЯ ЗАГРУЗКИ ЧАСТИЦ В ТРУБУ ТРУБЧАТОГО РЕАКТОРА

Изобретение относится к способам и устройствам, предназначенным для загрузки сыпучих материалов, и может быть использовано в химической, нефтеперерабатывающей и других отраслях промышленности, например, в реакторах первичного риформинга. Изобретение решает задачу загрузки частиц в трубу с образованием однородного по высоте и одинакового для всех загружаемых труб слоя частиц при гарантированном обеспечении их сохранности в процессе загрузки при одновременном увеличении скорости загрузки. Поставленная задача решается тем, что применяют способ, при котором каждая частица свободно падает в трубе под воздействием силы гравитации и поступает на поверхность формируемого слоя с постоянной скоростью, одинаковой для всех частиц и меньшей, чем скорость падения, при которой частицы могут разрушиться от соударения с частицами формируемого слоя. Указанную скорость падения частиц в трубе устанавливают путем торможения встречным потоком газа, который подают в нижнюю часть не загруженной частицами внутренности ...

ИСПОЛЬЗОВАНИЕ ТРЕХМЕРНОГО ПЕРЕКРЕСТНОГО ДИВЕРТЕРАВ КАЧЕСТВЕ ЭЛЕМЕНТА ТРУБЫ, БАРАБАНА ИЛИ БАШНИ

... 1. Трехмерный перекрестный дивертер, используемый в качестве внутреннего элемента в трубе, барабане или башне, отличающийся тем, что один или множество ярусов трехмерных перекрестных дивертеров (2) размещено внутри корпуса (1) трубы, барабана или башни; каждый из указанных трехмерных перекрестных дивертеров (2) содержит четное количество (большее чем или равное четырем) конических полостей 2-1 с нестандартной формой профилировки, размещенных под углом, каждая коническая полость (2-1) с нестандартной формой профилировки имеет на наружном концевом участке увеличенный проход, а на внутреннем концевом участке - уменьшенный проход, все конические полости сходятся у средней точки на оси трехмерного перекрестно дивертера, которая также является центром трехмерного перекрестного дивертера, каждая коническая полость содержит две боковые поверхности (2-1-1), наружную поверхность (2-1-2) и внутреннюю поверхность (2-1-3), указанные боковые поверхности являются четырехугольными плоскими поверхностями ...

СПОСОБ ОКИСЛЕНИЯ ХЛОРИСТОГО ВОДОРОДА КИСЛОРОДОМ

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

МНОГОТРУБНЫЙ РАДИАЛЬНЫЙ КАТАЛИТИЧЕСКИЙ РЕАКТОР

НОСИТЕЛЬ КАТАЛИЗАТОРА, КАТАЛИЗАТОР И ЕГО ПРИМЕНЕНИЕ

... 1. Носитель катализатора, содержащий по меньшей мере 85 масс. процентов альфа-оксида алюминия, по меньшей мере 0,06 мас.% SiOи не более 0,04 мас.% NaO, обладающий водопоглощением не более 0,35 грамм воды/грамм носителя и отношением водопоглощения (грамм воды/грамм носителя) к площади поверхности (мносителя/грамм носителя) не более 0,50 грамм воды/мносителя.2. Носитель по п. 1, отличающийся тем, что содержание SiOне превышает 0,40 мас.%.3. Носитель по п. 1, отличающийся тем, что содержание SiOне превышает 0,30 мас.%.4. Носитель по п. 1, отличающийся тем, что содержание NaO не превышает 0,03 мас.%.5. Носитель по п. 1, отличающийся тем, что содержит по меньшей мере 0,15 мас.% SiO.6. Носитель по п. 1, отличающийся тем, что указанное отношение не превышает 0,45 г/м.7. Носитель по п. 1, отличающийся тем, что указанное отношение не превышает 0,40 г/м.8. Носитель по п. 1, отличающийся тем, что указанное водопоглощение не превышает 0,30 г/г.9. Носитель по п. 8, отличающийся тем, что указанная площадь ...

ПОЛУЧЕНИЕ СО-ОБОГАЩЕННОГО СИНТЕЗ-ГАЗА

ПРОТОЧНЫЙ ТРУБЧАТЫЙ РЕАКТОР ДЛЯ ПРЕВРАЩЕНИЯ ТЕТРАХЛОРИДА КРЕМНИЯ ДО ТРИХЛОРСИЛАНА

... 1. Способ получения трихлорсилана путем взаимодействия тетрахлорида кремния с водородом в реакторе гидродехлорирования (3), отличающийся тем, что реактор гидродехлорирования (3) эксплуатируют под давлением, причем он включает одну или несколько реакторных труб (3а, 3б, 3в), выполненных из керамического материала.2. Способ по п.1, отличающийся тем, что содержащий тетрахлорид кремния исходный газ (1) и/или содержащий водород исходный газ (2) в качестве потоков под давлением подают в эксплуатируемый под давлением реактор гидродехлорирования (3) и подвергают взаимодействию за счет подачи теплоты с получением содержащего трихлорсилан и HCl продуктового газа, выводимого из реактора гидродехлорирования (3) в качестве находящегося под давлением потока (4).3. Способ по п.2, отличающийся тем, что содержащий тетрахлорид кремния исходный газ (1) и содержащий водород исходный газ (2) подают в эксплуатируемый под давлением реактор гидродехлорирования (3) в качестве общего потока (1, 2).4. Способ по п ...

ВЫПОЛНЕНИЕ АВТОМАТИЗИРОВАННОЙ ПОДАЧИ КАТАЛИЗАТОРА И/ИЛИ ЧАСТИЦ ВЕЩЕСТВА К ЛЮБОМУ УСТРОЙСТВУ СИСТЕМЫ НАПОЛНЕНИЯ, ИСПОЛЬЗУЕМОМУ ДЛЯ НАПОЛНЕНИЯ ТРУБ

... 1. Устройство для автоматической подачи частиц вещества к трубе, помещенной в печи с вертикальными трубами, типа применяемой в установках для риформинга, содержащее: ! бункер, имеющий отверстие на нижнем конце, ! заслонку, установленную на бункере, выборочно выступающую над отверстием в бункере, ! ящик, установленный под бункером, ! основную загрузочную площадку, установленную в ящике, перекрывающую снизу отверстие в бункере, причем указанная основная загрузочная площадка имеет угол наклона и проходит до нижнего края ящика, при этом указанная основная загрузочная площадка содержит средство для обеспечения падения пыли и мелких фракций сквозь указанную основную загрузочную площадку, ! средство для транспортировки частиц вещества к переходнику загрузки трубы, которое присоединено к ящику вблизи одного конца указанной основной загрузочной площадки, ! средство для сбора пыли и мелких фракций, присоединенное к ящику, перекрывающее снизу указанную основную загрузочную площадку, ! причем переходник ...

КОМПАКТНЫЙ РЕДУКТОР РЕФОРМИНГА

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

ТРУБКИ ДЛЯ ВВОДА КАТАЛИЗАТОРА И/ИЛИ ДРУГОГО МАТЕРИАЛА В ВИДЕ ЧАСТИЦ

... 1. Устройство для загрузки материала в виде частиц, содержащее: ! приспособление для поворота указанного устройства, ! установочную поверхность, соединенную с указанным приспособлением для поворота, ! образующие препятствия элементы, закрепленные на установочной поверхности и расположенные последовательно с образованием спиральной конфигурации. ! 2. Устройство по п.1, в котором установочная поверхность присоединена под указанным приспособлением для поворота. ! 3. Устройство по п.1, в котором образующие препятствия элементы представляют собой цилиндрические пружины из нержавеющей стали. ! 4. Устройство по п.1, в котором образующие препятствия элементы представляют собой ответвления сплошного типа. ! 5. Устройство по п.1, в котором образующие препятствия элементы представляют собой ответвления щеточного типа, выполненные из нержавеющей стали. ! 6. Устройство по п.1, в котором указанные образующие препятствия элементы представляют собой элементы по меньшей мере двух разных типов, выбранных ...

КАТАЛИЗАТОР ПРЕВРАЩЕНИЯ СИНТЕЗ-ГАЗА В СПИРТЫ

СФОРМИРОВАННЫЕ КАТАЛИЗАТОРНЫЕ БЛОКИ

... 1. Катализаторный блок, пригодный для загрузки в трубу, включающий множество катализаторных частиц Фишера-Тропша, содержащих один или более восстанавливаемых металлов, выбираемых из Co или Fe в оксидной или восстановленной форме, расположенных в удаляемой матрице из воска или полимера, указанный блок имеет форму удлиненного тела, в котором частицы заполнены так, что объемная усадка после удаления удаляемой матрицы составляет ≤20%.2. Катализаторный блок по п.1, который имеет форму цилиндра с диаметром D в диапазоне от 1 до 15 см и с длиной в диапазоне от 0,75D до 20D.3. Катализаторный блок по п.2, в котором D находится в диапазоне от 1 до 5,5 см, а длина цилиндра находится в диапазоне от 10 до 200 см, предпочтительно, от 10 до 100 см, более предпочтительно, от 10 до 50 см.4. Катализаторный блок по п.2, в котором катализаторные частицы представляют собой пеллеты, гранулы или экструдаты с наибольшим размером в диапазоне от 0,04D до 0,2D.5. Катализаторный блок по п.1, в котором катализаторные ...

ТВЕРДО-ЖИДКОСТНАЯ РЕАКЦИЯ

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

Способ получения синтез-газа посредством неполного окисления горючего газа и реактор для его осуществления

Изобретение касается способа получения синтез-газа посредством неполного окисления горючего газа в снабженном роторным регенеративным трубчатым теплообменником реакторе, включающего разогрев до высокой температуры по меньшей мере части теплоизолированной реакционной камеры реактора; подачу в реактор двух газов-реагентов - горючего газа и кислородсодержащего газа-окислителя в недостаточном для полного окисления горючего газа количестве; смешение горючего газа и газа-окислителя в реакционной камере реактора; проведение реакции горючего газа и кислородсодержащего газа; выведение из реактора потока газообразных продуктов в виде синтез-газа. Процесс проводят посредством подачи горючего газа через каналы-трубы регенеративного трубчатого теплообменника, которые находятся в сечении газохода подачи горючего газа, и газа-окислителя через каналы-трубы регенеративного трубчатого теплообменника, которые находятся в сечении газохода подачи газа-окислителя, причем потоки горючего газа и газа-окислителя ...

Трубчатый реактор

Изобретение относится к конструкции трубчатого каталитического реактора, может быть использовано для получения окиси этилена и позволяет снизить процесс теплоотдачи за счет обеспечения низкотурбулентного режима. Реактор содержит корпус, внутри которого в трубных досках закреплены трубки с катализатором, и камеру охлаждения. Реактор снабжен распределительной камерой, размещенной под камерой охлаждения и выполненной в виде обечайки с двумя пластинами и закрепленными в них трубками, установленными соосно с трубками с катализатором. 2 ил.

VERFAHREN ZUR REFORMIERUNG UNREINEN METHANOLS UND VORRICHTUNG FUER SEINE ANWENDUNG.

Verfahren zur Durchführung von Stoffumwandlungen mit in Flüssigkeiten suspendierten Katalysatoren

Wasserstoffgenerator mit thermischem Siphonreaktor und thermischer Siphonreaktor

Thermischer Siphonreaktor, umfassend: ein Reaktionsrohr, in dem eine katalytische Reaktion einer Reaktionsquelle stattfindet; und eine Katalysatorschicht, die porös ist, und Gaserzeugung ermöglicht, indem sie mit der Reaktionsquelle in Kontakt steht und in dem Reaktionsrohr platziert ist, wobei in dem Reaktionsrohr ein Konvektionskanal, durch den ein Reaktionsprodukt ausgetragen wird, durch das Reaktionsrohr in Längsrichtung des Reaktionsrohrs durchläuft.

REAKTOR FUER EXOTHERME KATALYTISCHE VERFAHREN

Verfahren zur katalytischen Durchführung von Mehrphasenreaktionen, insbesondere Vinylierungen von Carbonsäuren

Die Erfindung betrifft ein Verfahren zur katalytischen Durchführung von Mehrphasenreaktionen in einem Rohrreaktor, wobei der Katalysator in der kontinuierlichen Phase und mindestens ein Edukt in einer dispergierten Phase enthalten ist und der Belastungsfaktor B des Rohrreaktors gleich oder größer 0,8 ist. DOLLAR A Das Verfahren ist besonders zur Herstellung von Vinylestern durch Reaktion von Carbonsäuren mit Acetylen geeignet. DOLLAR A Die Vinylester finden zur Herstellung von Homo- oder Copolymerisaten Verwendung.

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

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

Method for filling tubes of tube bundle reactor with bulk material e.g. tablets, involves determining dumping height of bulk material present in tubes of tube bundles reactor by laser, radar or ultrasonic

The method involves determining a dumping height (76) of a bulk material present in tubes (15) of a tube bundle reactor (10) by laser, radar or ultrasonic. The tubes are filled with the bulk material over a filler opening (19), and the dumping height of the bulk material is determined by measuring a distance of a surface of a fill to a reference point (64). A distance of the reference point to a base (17) of the tubes or to a surface of the material, present in the tube, is determined before filling the tubes. An independent claim is also included for a filling device for filling tubes of a tube bundles reactor with a bulk material, comprising a laser measuring device.

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

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

CATALYTIC EXHAUST GAS TREATMENT APPARATUS

... 1366061 Treating exhaust gas CHEMICAL CONSTRUCTION CORP 23 Jan 1973 3451/73 Heading F1B An apparatus for the catalytic treatment of exhaust gas comprises two co-axial cylindrical catalyst beds 14 and 30 mounted in a container with an inlet 7 for exhaust gas to the centre of the inner bed 14 and an inlet for air between the beds and a gas outlet external of the outer bed, the inner bed being a catalyst for the reduction of nitrogen oxides and the outer bed being a catalyst for the oxidation of hydrocarbons and carbon monoxide. Exhaust gas from an engine 3 is collected in manifold 4, to which air may be supplied at 5 so that the manifold operates as an after burner. The gases leaving the manifold enter pipe 7 and pass radially outwardly through slits 8 and through inner bed 14 which is contained by cylindrical baffle 16 having slits 15. The gases then flow parallel to the container axis to the inlet end of the apparatus, around the edge of an intermediate baffle 18 and enter outer bed 30 ...

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

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

CATALYTIC AMMONIA BURNER

... 1360782 Catalytic ammonia dissociation burner ALLIED CHEMICAL CORP 25. Aug 1971 [25 Sept 1970] 16334/73 Divided out of 1360781 Headings B1F and B1X [Also in Division F4] A dissociator-burner for use with an opentype refrigeration system comprises an insulated housing 29 defining a conduction chamber and contains apertures 30 for combustion air and vertical conduits 26 containing a catalyst, e.g. iron including activated iron promoter with Al 2 O 3 or other metal oxides for partially dissociating the ammonia vapour fed thereto through a manifold 25. The dissociated ammonia is discharged from the conduits to be burnt at 28 and the heat maintains the catalyst at an active temperature. Electrical heating elements 34 or a portable torch are used for start-up. In a modification the catalyst-containing conduit is horizontally positioned in the burner.

Steam reforming

A modular flow reactor

Improved reactor for catalytic reactions

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

A METHOD OF, AND APPARATUS FOR, EMPTYING PIPES

A method of emptying pipes, in particular catalyst-filled thin-walled vertical pipes 20, by means of a conveying fluid utilizes a probe, which discharges the conveying fluid, and is introduced from above into the catalyst pipes, the probe being moved continuously downwards to loosen the filling and to convey it away by suction through a coaxial connector 3. ...

A tubular reactor and process for supplying granular catalyst material and/or liquid into the tubes of the tubular reactor

The reactor tubes 8 of a tubular reactor are mounted in an upper tube plate 6 and are surrounded by a liquid coolant during operation. A vertically movable distributor plate 15 is disposed over the upper tube plate and is provided with distributor tubes 18, which extend into the top portions of the reactor tubes. Granular catalyst material is first supplied onto the distributor plate, and then through the tubes into the reactor tubes. The catalyst material on the distributor plate is then removed and the plate is raised so that the distributor tubes are emptied. The reactor tubes are thus filled except for an upper volume, which remains free of catalyst. The distributor plate may also be used to distribute liquid into the reactor tubes. ...

Monitoring device installation method and apparatus

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

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

Apparatus

CATALYTIC CONVERSION OF GAS/LIQUID

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

Heat exchange reactor seal apparatus

A tube seal device 20 for use in a heat exchange reactor comprises an inner tube 22 disposed within a seal tube 21 to provide an overlapping region. Within the overlapping region, the inner tube has: an interior constriction of reduced cross-sectional area forming a low-pressure region 32; an expansion region 33 adjacent the constriction and of cross-sectional area greater than that of the constriction; and one or more passages 34 through the wall of the inner tube connecting the low-pressure region to the exterior of the inner tube. The tube seal device further comprises one or more grooves 36 formed around an inner face of the seal tube in the overlapping region corresponding to the low-pressure region of the inner tube. One or more additional grooves 37 may be provided on an outer face of the inner tube or on an inner face of the seal tube in the overlapping region corresponding to the expansion region. The grooves disrupt the flow of gas through the tube seal device. A heat exchange ...

Vessel for containing catalyst in a tubular reactor.

Monolithic reactor

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

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

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

FISCHER-TROPSCH PROCESS IN A RADIAL REACTOR

MONOLITHIC REACTOR

Vessel for containing catalyst in a tubular reactor

Vessel for containing catalyst in a tubular reactor.

Monolithic reactor

Fischer-tropsch process in a radial reactor

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

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

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

Vessel for containing catalyst in a tubular reactor.

Monolithic reactor

PROCEDURE FOR FILLING INDIVIDUAL SOLIDS INTO PERPENDICULAR PIPES

REACTOR AND PROCEDURE FOR THE TREATMENT OF FLUIDS BY PHOTO CATALYSTS, WHICH ARE COUPLED WITH PHOSPHORESCING SOLIDS

PROCEDURE FOR THE CATALYTIC EXECUTION OF HYDROFORMYLIERUNGEN

LOAD DEVICE OF A CONTAINER WITH FIXED PARTICLES AND PROCEDURES, WITH WHICH THIS DEVICE IS USED

VERFAHREN ZUR HERSTELLUNG VON ACROLEIN UND ACRYLSAURE ODER METHACROLEIN UND METHACRYLSAURE

REAKTIONSAPPARAT ZUR DURCHFUEHRUNG KATALYTISCHER RAKTIONEN

COMBINATORIAL CATALYTIC REACTOR

BANK OF TUBES REACTOR WITH A HELIXFÖRMIG TRAINED CROSS SECTION

TOOL TO THE LOADING OF REACTOR PIPES

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

FILLING DEVICE FOR BANK OF TUBES REACTORS

COMPACT REFORMATION REACTOR

AUTOTHERMES PROCEDURE FOR THE PRODUCTION OF SYNTHESIS GAS AND DEVICE FOR THE EXECUTION OF THE PROCEDURE

PROCEDURE AND REACTOR FOR THE PRODUCTION OF METHANOL

PROCEDURE AND APPARATUS FOR THE SIMULTANEOUS REACTION AND DISTILLATION

CATALYTIC CONVERSION OF GAS OR LIQUID IN A PLURALROHRREAKTOR.

AUTOTHERMES VERFAHREN ZUR HERSTELLUNG VON SYNTHESEGAS UND VORRICHTUNG ZUR DURCHFUEHRUNG DES VERFAHRENS

PROCEDURE AND DEVICE FOR THE STEERED REACTION IN A REACTION MATRIX

ROHRBUNDELREAKTOR FUR THE CATALYTIC GASEOUS PHASE OXIDATION

SYNTHESIS GAS PRODUCTION BY STEAM REFORMING

CHEMICAL PROCEDURE

Reactor for the production of methanol

PROCEDURE AND DEVICE FOR FACILITATING FILLING VERTICAL PIPES WITH THE HELP OF A PARTIKELFÖRMIGEN MATERIAL

PROCEDURE AND DEVICE FOR THE HOMOGENEOUS FILLING OF CELEBRATIONS CATALYST PARTICLES INTO A TUBULAR REACTOR

A methanol synthesis process layout for large production capacity

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).

Commercial Fischer-Tropsch reactor

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

Reaction apparatus with a heat-exchanger

Reactor for the preparation of methanol

Improved design of a catalytic reactor for the production of methanol at equilibrium conditions whereby methanol as it is formed is separated from the gaseous phase into the liquid phase within the reactor, without reducing the catalytic activity of the methanol catalysts This is achieved by adjusting the boiling point of a liquid cooling agent being in indirect contact with the catalyst particles and by providing a specific ratio of catalyst bed volume to cooling surface area. Thereby, condensation of methanol as it is formed in the gaseous phase takes place at the cooling surface arranged evenly distributed within the reactor and within a very limited region of the catalyst bed.

Multi-structured reactor made of monolithic adjacent thermoconductive bodies for chemical processes with a high heat exchange

A multi-structured tubular element for producing a reactor for effecting exothermic/endothermic chemical reactions, comprises two or more monolithic thermoconductive bodies, assembled together so that each has a part of the side surface interfaced with the side surface of one or more monolithic thermoconductive bodies adjacent thereto, so as to form as a whole, a honeycomb structure containing a plurality of longitudinal channels extending from one end to the other of said tubular element, suitable for being filled with a granular catalytic solid.

Process for the ammonia production

Process and plant for the synthesis of ammonia from a hydrocarbon feedstock, comprising: primary reforming with steam and air-fired secondary reforming wherein primary reforming is performed at a temperature and pressure of at least 790 °C and 50 bar, and secondary reforming is carried out substantially in absence of excess air, the so obtained make-up synthesis gas having a H ...

OPEN CYCLE AMMONIA REFRIGERATION SYSTEM

Method and apparatus for controlled reaction in a reaction matrix

CATALYTIC VAPOR PHASE OXIDATION

Endothermic reaction apparatus

HALOCARBON PRODUCTION PROCESSES, HALOCARBON SEPARATION PROCESSES, AND HALOCARBON PRODUCTION SYSTEMS

APPARATUS FOR LOADING PARTICULATE CATALYTIC MATERIAL AND LOADING METHOD

PROCESS AND APPARATUS FOR LOADING A PARTICULATE SOLID INTO A VERTICAL TUBE

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

Реактор для получения углеродных наноматериалов газофазным химическим осаждением

Полезная модель относится к технологическому оборудованию для получения углеродных наноматериалов методом газофазного химического осаждения с использованием паров этанола в токе водорода. В реакторе для получения углеродных наноматериалов газофазным химическим осаждением, выполненным в виде предназначенной для размещения в устройстве нагрева кварцевой трубки, снабженной по торцам входным и выходным патрубками, по крайней мере один из которых выполнен съемным, кварцевая трубка выполнена с прямоугольным проходным сечением, оптимально кварцевую трубку выполнять со скругленными углами в прямоугольном проходном сечении. Технический результат - повышение производительности процесса за счет повышения эффективности синтеза УНМ. 1 з.п.ф-лы, 3 ил. РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 191 901 U1 (51) МПК B01J 8/06 (2006.01) B82B 3/00 (2006.01) C01B 32/15 (2017.01) B82Y 40/00 (2011.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ПОЛЕЗНОЙ МОДЕЛИ К ПАТЕНТУ (52) СПК C01B 32/15 (2018.05); B82B 3/0019 (2018.05); B82Y 40/00 (2018.05); B01J 8/062 (2018.05); B01J 8/065 (2018.05) (21)(22) Заявка: 2017139513, 14.11.2017 14.11.2017 Дата регистрации: Приоритет(ы): (22) Дата подачи заявки: 14.11.2017 (45) Опубликовано: 28.08.2019 Бюл. № 25 Адрес для переписки: 127055, Москва, ГСП-4, Вадковский пер., 1, ФГБОУ ВО "МГТУ "СТАНКИН", УИС U 1 1 9 1 9 0 1 R U (54) Реактор для получения углеродных наноматериалов газофазным химическим осаждением (57) Реферат: Полезная модель относится к входным и выходным патрубками, по крайней технологическому оборудованию для получения мере один из которых выполнен съемным, углеродных наноматериалов методом кварцевая трубка выполнена с прямоугольным газофазного химического осаждения с проходным сечением, оптимально кварцевую использованием паров этанола в токе водорода. трубку выполнять со скругленными углами в В реакторе для получения углеродных прямоугольном проходном сечении. Технический наноматериалов газофазным химическим результат - ...

Process for quenching the effluent gas of a furnace

The present invention relates to a process for quenching the effluent gas of a furnace comprising: a) providing a furnace comprising a radiant zone enclosure means having a plurality of tubes disposed therein, an inlet means for introducing the process fluid into the tubes, means for exposing the external surface of the tubes to radiant heat for heating said process fluid and thereby produce an effluent gas, b) providing a quench zone having a plurality of quench tubes in which the effluent gas is passed and such as the inlet of one quench tube is connected to the outlet of one or more tubes of the radiant zone, c) recovering the effluent gas after it has been cooled in the quench tubes, wherein, at least a part of the quench tubes and advantageously all the quench tubes are tubes having means inside of it, on all the length or a part of the length, to promote turbulent flow by breaking the boundary film on the internal surface of the tube. The present invention also relates to a quench exchanger to carry out the above process.

Reformer tube apparatus having variable wall thickness and associated method of manufacture

The present invention provides a reformer tube apparatus, including: an axially aligned tubular structure including a flange section, a top section, a middle section, and a bottom section; wherein the top section of the axially aligned tubular structure includes a first portion having a first wall thickness; wherein the top section of the axially aligned tubular structure includes a second portion having a second wall thickness; and wherein the top section of the axially aligned tubular structure includes a third portion having a transitioning wall thickness that joins the first portion to the second portion. The flange section includes a concentric flange disposed about a top portion thereof. The bottom section of the tubular structure includes a plurality of concentric wedge structures disposed about the interior thereof. The bottom section of the tubular structure also includes a recess disposed about the exterior thereof. The axially aligned tubular structure further includes a secondary flange section coupled to the flange section, wherein the secondary flange section includes a concentric flange disposed about a top portion thereof. Optionally, the reformer tube apparatus is disposed within a reformer used in a direct reduction process.

Hydrogenation Process for Fluorocarbons

Disclosed is a process and apparatus for the catalytic hydrogenation of fluoro-olefins to fluorocarbons where the reaction is carried out in a multi-tube shell and tube reactor. Reactions involving hydrogenation of fluoro-olefins are typically exothermic. In commercial processes where a fluoro-olefin C n H 2n-x F x to C n H 2n-x2 F x is hydrogenated (e.g., hexafluoropropylene to 236ea, 1225ye to 245eb, and the like), inadequate management or control of heat removal may induce excess hydrogenation, decomposition and hot spots resulting in reduced yields and potential safety issues. In the hydrogenation of fluoro-olefins, it is therefore necessary to control the reaction temperature as precisely as practical to overcome challenges associated with heat management and safety.

Shaped catalyst units

A catalyst unit suitable for loading into a tube in a reactor includes a plurality of catalyst particles incorporated within a removable solid matrix, said unit in the form of an elongate body in which the particles are packed together such that the volume shrinkage upon removal of the removable matrix is ≦20%. The catalyst particles preferably comprise one or more metals selected from the group consisting of Fe and Co in oxidic or reduced form. The units are particularly suitable for loading catalyst into tubes in a Fischer-Tropsch reactor.

Stackable structural reactors

A reactor for carrying out catalytic reactions. The reactor includes a reactor component optionally arranged on a central rod in a reactor tube. The reactor component can have fluid ducts for directing fluid flow through the reactor. The fluid ducts are effective for increasing heat transfer in the reactor. The reactor component can further have a washer attached to a top or bottom surface for directing fluid flow.

Device for unloading catalyst from a reactor vessel

A device and method for automatic unloading of particles from the vertical tubes of a chemical reactor automatically feeds a fish tape into the bottom of the vertical tube to contact and dislodge the particles and automatically retracts the fish tape to allow the particles to fall out of the tube.

Vessel For Containing Catalyst In A Tubular Reactor

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.

Method of Producing Gaseous Products Using a Downflow Reactor

Reactor systems and methods are provided for the catalytic conversion of liquid feedstocks to synthesis gases and other noncondensable gaseous products. The reactor systems include a heat exchange reactor configured to allow the liquid feedstock and gas product to flow concurrently in a downflow direction. The reactor systems and methods are particularly useful for producing hydrogen and light hydrocarbons from biomass-derived oxygenated hydrocarbons using aqueous phase reforming. The generated gases may find used as a fuel source for energy generation via PEM fuel cells, solid-oxide fuel cells, internal combustion engines, or gas turbine gensets, or used in other chemical processes to produce additional products. The gaseous products may also be collected for later use or distribution.

Tunable catalytic gasifiers and related methods

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

Apparatus and method for hydroconversion

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

Method Of Operating A Fluid Bed Reactor

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

SEPARATION OF CARBON DIOXIDE (CO2) FROM GAS MIXTURES BY CALCIUM BASED REACTION SEPARATION (CaRS-CO2) PROCESS

A reaction-based process developed for the selective removal of CO2 from a multicomponent gas mixture to provide a gaseous stream depleted in CO2 compared to the inlet CO2 concentration. The proposed process effects the separation of CO2 from a mixture of gases by its reaction with metal oxides. The Calcium based Reaction Separation for CO2 (CaRS-CO2) process consists of contacting CO2 laden gas with CaO in a reactor such that CaO captures CO2 by the formation of CaCO3. CaCO3 is regenerated by calcination leading to the formation of fresh CaO sorbent and the evolution of a concentrated stream of CO2. The “regenerated” CaO is then recycled for the further capture of CO2. This carbonation-calcination cycle forms the basis of the CaRS-CO2 process. This process also may use a mesoporous CaCO3 structure that attains >90% conversion over multiple carbonation and calcination cycles. 1. A facility separating carbon dioxide and sulfur dioxide from a flow of gas comprising carbon dioxide and sulfur dioxide , comprising:a gas-solid contact reactor receiving said flow of gas;a sorbent within said gas-solid reactor, comprising a metal oxide, said sorbent reacting with said carbon dioxide and said sulfur dioxide so as to convert at least a portion of said sorbent to a metal carbonate and at least a portion of said sorbent to a metal sulfate; anda calcinator, said calcinator receiving said at least a portion of said metal carbonate, said calcinatory calcining said metal carbonate to form said metal oxide and carbon dioxide,wherein said sorbent is replenished in said gas-solid reactor with said metal oxide formed in said calcinatory.2. The facility of claim 1 , further comprising a cyclone claim 1 , said cyclone separating said metal carbonate from said flow of gas.3. The facility of claim 1 , wherein said gas-solid reactor is operated at between about 600° to about 650° Celsius to facilitate the reaction between said carbon dioxide and said sulfur dioxide with said sorbent.4. The ...

STACKED CATALYST BED FOR FISCHER-TROPSCH

The present invention pertains to a reactor tube comprising a fixed bed of Fischer-Tropsch catalyst particles, wherein the catalyst particles in 5% to 40% of the fixed bed volume at the upstream end have an average outer surface to volume ratio (S/V) of between 3.0 to 4.5 mm, and the catalyst particles in the remaining fixed bed volume have an average S/V of between 4.5 to 8.0 mm, and wherein the difference between the average S/V of the particles at the upstream end and the average S/V of the particles in the remaining fixed bed volume is at least 0.5 mm. The weight of catalytically active metal per volume unit in 5% to 33% of the fixed bed volume at the upstream end is 59% to 69% lower than the weight of catalytically active metal per volume unit in the remaining fixed bed volume. 1. A reactor tube comprising a fixed bed of Fischer-Tropsch catalyst particles , wherein the catalyst particles in 5% to 33% of the fixed bed volume at the upstream end have an average outer surface to volume ratio (S/V) in the range of between 3.0 to 4.5 mmand the catalyst particles in the remaining fixed bed volume have an average outer surface to volume ratio (S/V) in the range of between 4.5 to 8.0 mm , and wherein the difference between the average S/V of the particles at the upstream end and the average S/V of the particles in the remaining fixed bed volume is at least 0.5 mm , and wherein the weight of catalytically active metal per volume unit in 5% to 33% of the fixed bed volume at the upstream end , is 59% to 69% lower than the weight of catalytically active metal per volume unit in the remaining fixed bed volume.2. A reactor tube comprising a fixed bed of Fischer-Tropsch catalyst particles , wherein the catalyst particles in 7% to 25% of the fixed bed volume at the upstream end , have an average outer surface to volume ratio (S/V) in the range of between 3.0 to 4.5 mm , and the catalyst particles in the remaining fixed bed volume have an average outer surface to volume ratio ( ...

STEAM REFORMER TUBE ASSEMBLY AND METHOD OF ASSEMBLING OR RETROFITTING SAME

A steam reformer tube assembly includes a reformer tube including a wall defining an interior space for receiving fluid delivered into the reformer tube, a plug at least partially positioned in an opening in the interior space such that a gap is defined between the plug and the wall of the reformer tube, and a sealing member positioned in the gap to either limit or prevent the passage of fluid toward the opening in the interior space of the reformer tube and along the gap that is defined between the exterior surface of the plug and the interior wall of the reformer tube. A method of assembling a steam reformer tube assembly is also provided. 1. A steam reformer tube assembly , comprising:a reformer tube including a wall defining an interior space for receiving fluid delivered into the reformer tube;a plug at least partially positioned in an opening in the interior space of the reformer tube such that a gap is defined between an exterior surface of the plug and the interior wall of the reformer tube; anda sealing member positioned in the gap to either limit or prevent the passage of fluid toward the opening in the interior space of the reformer tube and along the gap that is defined between the exterior surface of the plug and the interior wall of the reformer tube.2. The steam reformer tube assembly of claim 1 , wherein a blind flange of the plug is mounted to a flange of the reformer tube.3. The steam reformer tube assembly of claim 2 , further comprising a gasket mounted between the blind flange of the plug and the flange of the reformer tube claim 2 , wherein the gasket is positioned in fluid communication with the gap that is defined between the exterior surface of the plug and the interior wall of the reformer tube.4. The steam reformer tube assembly of claim 1 , wherein the sealing member is positioned in a recess that is formed on an exterior surface of the plug claim 1 , and the sealing member is sized and shaped to contact the interior wall of the reformer ...

ADVANCED FISCHER TROPSCH SYSTEM

A Fischer Tropsch (“FT”) unit that includes an FT tube that is packed with a catalyst. The catalyst is designed to catalyze an FT reaction to produce a hydrocarbon. An insert that is positioned within the FT tube. The insert comprises at least one cross-piece that contacts an inner surface of the FT tube and at least one cross-fin extending from the cross-piece. There may be a corresponding second cross-fin adjacent each cross-fin. Both the cross-fins and the second cross-fins may be disposed radially outwardly such that the edge of the cross-fins are closer to the inner surface of the FT tube than is the base of the cross-fins. 1. A Fischer Tropsch (“FT”) unit comprising:an FT tube; at least one cross-piece that contacts an inner surface of the FT tube; and', 'at least one cross-fin extending from the cross-piece., 'an insert that is positioned within the FT tube, the insert comprising2. The FT unit as in claim 1 , wherein the insert comprises three cross-pieces claim 1 , wherein each cross-piece contacts the inner wall of the FT tube claim 1 , wherein the three cross-pieces generally form a “snowflake” configuration.3. The FT unit as in claim 2 , wherein the end of each cross-piece comprises a pad claim 2 , wherein each pad contacts the inner surface of the FT tube.4. The FT unit as in claim 3 , wherein there is a corresponding second cross-fin that is positioned adjacent each cross-fin.5. The FT unit as in claim 4 , wherein each cross-fin and each corresponding second cross-fin are disposed towards the inner surface of the FT tube.6. The FT unit as in claim 5 , wherein each cross-piece comprises two cross-fins and two corresponding second cross-fins.7. The FT unit as in claim 1 , further comprising a thermocouple in communication with the insert.8. The FT unit as in claim 6 , wherein a thermocouple opening is positioned at the center of the insert.9. The FT unit as in claim 1 , wherein the insert is made of a heat conductive metal.10. The FT unit as in claim 9 , ...

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

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

CATALYTIC SYSTEMS FOR CONTINUOUS CONVERSION OF SILICON TETRACHLORIDE TO TRICHLOROSILANE

The invention relates to an improved method for converting silicon tetrachloride having hydrogen in a hydrodechlorination reactor comprising a catalyst. The invention further relates to a catalytic system for such a hydrodechlorination reactor. 1. A process comprising reacting , in a hydrodechlorination reactor , silicon tetrachloride with hydrogen to obtain trichlorosilane , wherein a coating on an inner wall of the reactor catalyzes the reaction.2. The process of claim 1 , comprising reacting a silicon tetrachloride-comprising reactant gas and a hydrogen-comprising reactant gas in the hydrodechlorination reactor by supplying heat claim 1 , to obtain a product gas comprising trichlorosilane and HCl.3. The process of claim 2 , wherein the silicon tetrachloride-comprising reactant gas and the hydrogen-comprising reactant gas pass into the hydrodechlorination reactor in a combined stream.4. The process of claim 1 , wherein the hydrodechlorination reactor comprises a reactor tube claim 1 , the coating is disposed on an inner wall of the reactor tube claim 1 , and the reactor tube comprises a ceramic material.5. The process of claim 4 , wherein the ceramic material is selected from the group consisting of AlO claim 4 , AlN claim 4 , SiN claim 4 , SiCN and SiC.6. The process of claim 5 , wherein the ceramic material is selected from the group consisting of Si-infiltrated SiC claim 5 , isostatically pressed SiC claim 5 , hot isostatically pressed SiC claim 5 , and SiC sintered under ambient pressure (SSiC).7. The process of claim 4 , wherein the reactor tube comprises SiC sintered under ambient pressure (SSiC).8. The process of claim 2 , wherein (i) the silicon tetrachloride-comprising reactant gas claim 2 , (ii) hydrogen-comprising reactant gas claim 2 , or both (i) and (ii) pass into the hydrodechlorination reactor as pressurized streams or as a pressurized combined stream claim 2 , the reactor is pressurized claim 2 , and the product gas passes out of the ...

Metal passivation of heat-exchanger exposed to synthesis gas

A process for passivation of surfaces of heat exchange apparatus exposed to a synthesis gas containing carbon monoxide, includes the steps of: adding arsine to the synthesis gas to provide a total As concentration in the synthesis gas in range 0.001 to 10 ppmv, (ii) exposing the mixture of hot synthesis gas and arsine to the shell-side surfaces of said heat exchange apparatus to reduce the interaction between the carbon monoxide present in said gas and metals in said surfaces, (iii) recovering a cooled synthesis gas from the shell-side of said apparatus, and (iv) passing the cooled synthesis gas, optionally after further cooling, through a sorbent bed to remove arsenic compounds from the synthesis gas.

Tube bundle reactor having a structured packing

A tubular reactor for carrying out a catalytically supported, homogeneous chemical reaction in the gas phase at an elevated temperature and a subsequent cooling, wherein the reactor is arranged upright, and therefore the tubes extend vertically and the as flows downward through the tubes. The tubes are filled with a catalyst bed in the upper part thereof extending in the reaction zone of the reactor and are filled with a structured packing in the lower part, the cooling zone of the reactor.

Shell-and-tube reactor for carrying out catalytic gas phase reactions

A tube bundle reactor for carrying out catalytic gas phase reactions, particularly methanation reactions, has a bundle of catalyst-filled reaction tubes through which reaction gas flows and around which heat carrier flows during operation. In the region of the catalyst filling, the reaction tubes run through at least two heat carrier zones which are separated from one another, the first of which heat carrier zones extends over the starting region of the catalyst filling. The reaction tubes each have a first reaction tube portion with a first hydraulic diameter of the catalyst filling and, downstream thereof in flow direction of the reaction gas, at least a second reaction tube portion with a second hydraulic diameter of the catalyst filling that is greater than the first hydraulic diameter of the catalyst filling.

Process and Apparatus for Continuous High Temperature Short-Time Alkoxylation (Ethoxylation, Propoxylation) of Chemical Substances with Active Hydrogen Atoms

Disclosed is a process for continuously reacting liquid alkylene oxide with a liquid substance including an organic compound with active hydrogen atoms and a catalyst in a reactor. 130-. (canceled)31. A process for continuously reacting liquid alkylene oxide with a liquid substance comprising an organic compound with one or more active hydrogen atoms and a catalyst selected from alkali metal hydroxides and alkali metal alcoholates , in a reactor selected from(a) a tubular reactor comprising at least one reaction tube providing a reaction space inside of said tube, and(b) an annular-gap reactor comprising an outer tube and an inner tube, longitudinally inserted into said outer tube, which form an annular reaction gap extending between the inner surface of the outer tube, which forms the outer boundary of the reaction gap, and the outer surface of the inner tube, which forms the inner boundary of the reaction gap,wherein(1) the supply of liquid alkylene oxide to the reactor is controlled by a single mass flow controller, the liquid alkylene oxide is fed to said reactor (a) or (b) via a single inlet socket which is connected with a source of liquid alkylene oxide via said mass flow controller and the alkylene oxide is split before entering the reaction space or gap into a first and a second part,(2) said first part of alkylene oxide enters the reaction space or gap of said reactor (a) or (b) at a first location,(3) the liquid organic substance is supplied to the interior of the reaction space of said tubular reactor (a) or to the interior of the reaction gap of said annular gap reactor (b) at a second location of the reactor, located at or downstream of said first location, and is intermingled with the liquid alkylene oxide to form a liquid reaction mixture, which moves downstream towards the end of the reactor,(4) the liquid alkylene oxide enters the reactor at said first location and over the entire-cross sectional area of the reaction space or gap at said location,( ...

Catalyst loading system

A reformer tube processing and filling system is provided for ensuring uniformity of reformer tube flow rates and reactivity. The disclosed invention provides a system for detecting and removing tube obstructions, as well as an automated process for verifying the flow rate for each tube and identifying tubes with abnormal flow rates to remove a source of human error and conserve labor costs. An automated tube filling system provides a calibrated fill mechanism coordinated with a calibrated loading rope withdrawal mechanism to ensure loading consistency. A lack of vibrating parts ensures a low dust count, and what little dust is present is removed via a built-in vacuum outlet in the loader.

PROCESS FOR CHARGING A LONGITUDINAL SECTION OF A CATALYST TUBE

A process for charging a longitudinal section of a catalyst tube with a homogeneous fixed catalyst bed section whose active composition is at least one multielement oxide or comprises elemental silver on an oxidic support body and whose geometric shaped catalyst bodies and shaped inert bodies have a specific inhomogeneity of their longest dimensions. 113-. (canceled)15: A process for heterogeneously catalyzed partial gas phase oxidation of an organic compound in a tube bundle reactor claim 14 , wherein the tube bundle reactor is a tube bundle reactor according to .16: The process according to claim 15 , wherein the heterogeneously catalyzed partial gas phase oxidation is that of propylene to acrolein and/or that of acrolein to acrylic acid.17. (canceled)18: A tube bundle reactor comprising at least one catalyst tube which has been charged by a process for charging a catalyst tube with a fixed catalyst bed which consists of a plurality of successive and mutually different catalytically active fixed catalyst bed sections claim 15 , each of which is intrinsically homogeneous claim 15 , and where the active composition of all fixed catalyst bed sections comprises at least one multielement oxide which comprisesa) the elements Mo, Fe and Bi, orb) the elements Mo and V, orc) the element V and additionally P and/or Sb,{'sup': i', 'i', 'i, 'or whose active composition comprises elemental silver on an oxidic support body, and the individual fixed catalyst bed section consists of a single type Sor of a homogenized mixture of a plurality of mutually distinguishable types Sof geometric shaped catalyst bodies and geometric shaped inert bodies, wherein, in each individual fixed catalyst bed section, all types Sof geometric shaped bodies present therein in each case satisfy the proviso M that'}{'sup': i', 'i, 'sub': 's', 'claim-text': {'br': None, 'i': ·D', '≦L', '·D, 'sub': s', 's', 's, 'sup': i', 'i', 'i, '0.98≦1.02,'}, 'from 40 to 70% of the total number of geometric shaped ...

BAYONET CATALYTIC REACTOR

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 , ...

Catalytic oxidation method and method for producing conjugated diene

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.

Method for producing carbonates

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.

PILOT PLANT FOR CHEMICAL LOOPING HYDROGEN GENERATION USING SINGLE-COLUMN PACKED BED AND HYDROGEN GENERATION METHOD

A pilot plant for chemical looping hydrogen generation using a single-column packed bed and hydrogen generation method. The plant has a feeding system, reaction system, tail gas treatment and analysis system, and auxiliary system. The reaction system has a packed bed reactor, inside which a thermal storage layer, oxygen carrier layer and supporting layer are arranged successively from top to bottom. The feeding system has a delivery pipe, metering pump, mass flow controller and fuel mixer. The tail gas treatment and analysis system has a cooler, gas-liquid separator, mass flow meter, gas analyzer and tail gas pipe. The packed bed reactor is subjected to fuel reduction, purge, steam oxidation, purge, air combustion and purge stages successively under control of the feeding system. The pilot plant enables evaluation for oxygen carriers and identification for technological difficulties and can generate high-purity hydrogen without using complex gas purification devices. 1. A pilot plant for chemical looping hydrogen generation using a single-column packed bed , wherein the plant comprises a feeding system , a reaction system and an tail gas treatment and analysis system;wherein the feeding system comprises at least one raw material delivery pipe, at least one raw material mass flow controller and a fuel mixer, wherein at least one outlet of the raw material mass flow controller is connected with an inlet of the fuel mixer, and other remaining outlets of the raw material mass flow controller are connected with an inlet of the reaction system;the reaction system is composed of a packed bed reactor, inside which a thermal storage layer, an oxygen carrier layer and a supporting layer are arranged successively from top to bottom, and the packed bed reactor is continuously subjected to fuel reduction, first purge, steam oxidation, second purge, air combustion and third purge stages successively under the control of the feeding system; andthe tail gas treatment and analysis ...

Air Lance for Removing Pellets from Tubes

An air lance for removing pellets from tubes includes a conduit body having an inlet end and a bottommost discharge opening, and a poker fixed relative to the conduit body and projecting beyond the bottommost discharge opening to serve as a spacer and poker; wherein a rigid member extends along said conduit body, such that that a hammering force applied to said rigid member where it extends outside of the tube will be transmitted through said rigid member to said poker for dislodging and breaking pellets.

CATALYST BED COMPRISING SILVER CATALYST BODIES AND PROCESS FOR THE OXIDATIVE DEHYDROGENATION OF OLEFINICALLY UNSATURATED ALCOHOLS

The present invention relates to a catalyst bed comprising silver catalyst bodies and a reactor comprising such a catalyst bed. Further, the invention relates to the use of the catalyst bed and the reactor for gas phase reactions, in particular for the oxidative dehydrogenation of organic compounds under exothermic conditions. In a preferred embodiment, the present invention relates to the preparation of olefinically unsaturated carbonyl compounds from olefinically unsaturated alcohols by oxidative dehydrogenation utilizing a catalyst bed comprising metallic silver catalyst bodies. 118.-. (canceled)19. A process for the preparation of an olefinically unsaturated carbonyl compound in a tubular reactor comprising a plurality of reactor tubes , comprising reacting an olefinically unsaturated alcohol with oxygen in the presence of a catalyst bed , comprising full-metallic silver catalyst bodies , wherein the catalyst bed has a packing density of the full-metallic silver catalyst bodies in the range of 3.0 g/cmto 10.0 g/cm.20. The process according to claim 19 , wherein the catalyst bed has a packing density of the full-metallic silver catalyst bodies in the range of 5.5 g/cmto 10.0 g/cm.21. The process according to claim 19 , wherein the catalyst bed has a void space ratio in the range of 5% to 70% claim 19 , based on the volume of the catalyst bed not occupied by the catalyst bodies per volume of the catalyst bed.22. The process according to claim 19 , wherein the full-metallic silver catalyst bodies have a mean particle size of 0.5 mm to 5.0 mm.23. The process according to claim 19 , wherein the full-metallic silver bodies have a cylindrical shape or spherical shape or sphere-like shape or combinations thereof.24. The process according to claim 19 , wherein the full-metallic silver bodies have a geometric surface area in the range of 100 mm/g to 600 mm/g.25. The process according to claim 19 , wherein the catalyst bed is located in a tube reactor.26. The process ...

CATALYST SYSTEM FOR OXIDIZING O-XYLOL AND/OR NAPHTHALENE INTO PHTHALIC ANHYDRIDE

The present invention relates to a catalyst system for oxidation of o-xylene and/or naphthalene to phthalic anhydride (PA), comprising a plurality of catalyst zones arranged in succession in the reaction tube, which have been produced using antimony trioxide comprising a noticeable proportion of senarmontite wherein some of the primary crystallites have a size of less than 200 nm. The present invention further relates to a process for gas phase oxidation, in which a gas stream comprising at least one hydrocarbon and molecular oxygen is passed through a catalyst system which comprises a plurality of catalyst zones arranged in succession in the reaction tube and which has been produced using an antimony trioxide comprising a noticeable proportion of senarmontite wherein some of the primary crystallites have a size of less than 200 nm. 19-. (canceled)10. A catalyst system for oxidation of o-xylene and/or naphthalene to phthalic anhydride , comprising a plurality of catalyst zones is arranged in succession in the reaction tube , which is produced using an antimony trioxide having a senarmontite content of at least 20% by weight and where the senarmontite primary crystallites have a polymodal size distribution , wherein between 10% and 80% by weight have a primary crystallite size of <200 nm and a median primary crystallite size of <150 nm.11. The catalyst according to claim 10 , wherein an antimony trioxide having a senarmontite content of at least 50% by weight is used.12. The catalyst according to claim 10 , wherein the senarmontite primary crystallites have a bimodal size distribution.13. The catalyst according to claim 10 , wherein between 10% and 80% by weight of the senarmontite primary crystallites have a primary crystallite size of <200 nm and a median primary crystallite size of <100 nm.14. The catalyst according to claim 10 , wherein between 10% and 50% by weight of the senarmontite primary crystallites have a primary crystallite size of <200 nm and a median ...

CATALYST SYSTEM FOR OXIDATION OF O-XYLENE AND/OR NAPHTHALENE TO PHTHALIC ANHYDRIDE

The present invention relates to a catalyst system for oxidation of o-xylene and/or naphthalene to phthalic anhydride (PA), comprising a plurality of catalyst zones arranged in succession in the reaction tube, which has been produced using antimony trioxide consisting predominantly of the senarmontite modification of which all primary crystallites have a size of less than 200 nm. The present invention further relates to a process for gas phase oxidation, in which a gas stream comprising at least one hydrocarbon and molecular oxygen is passed through a catalyst system which comprises a plurality of catalyst zones arranged in succession in the reaction tube and which has been produced using an antimony trioxide consisting predominantly of the senarmontite modification with a median primary crystallite size of less than 200 nm. 112.-. (canceled)13. A catalyst system for oxidation of o-xylene and/or naphthalene to phthalic anhydride , comprising a plurality of catalyst zones arranged in succession in the reaction tube , which is produced using an antimony trioxide with at least 95% by weight in the senarmontite modification with a median primary crystallite size of less than 200 nm.14. The catalyst system according to claim 13 , wherein an antimony trioxide with at least 99% by weight in the senarmontite modification is used.15. The catalyst system according to claim 13 , wherein the senarmontite primary crystallites have a bimodal or polymodal size distribution.16. The catalyst system according to claim 13 , wherein the senarmontite primary crystallites have a median primary crystallite size of less than 150 nm.17. The catalyst system according to claim 13 , wherein the senarmontite claim 13 , primary crystallites have a median primary crystallite size of less than 100 nm.18. The catalyst system according to claim 13 , which is produced using pure senarmontite with a median primary crystallite size of less than 100 nm.19. A process for production of a catalyst system ...

Modular flow reactor

A modular flow reactor is formed of a plurality of modules, wherein each module comprises a body having at least one conduit passing therethrough, and wherein a plurality of said modules are aligned along a longitudinal axis such that said conduits of said modules are aligned to form a passage for fluid, wherein each module has a length along said longitudinal axis which is less than the length of the module perpendicular to the longitudinal axis. The modules are “slices” rather than “tubes” and a plurality of said modules can be aligned linearly so that the conduits form a tube.

Reactor with stripping zone

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.

CATALYST PARTICLE SHAPE

A catalytic system is provided which comprises a tubular reactor and at least one catalyst particle located within the tubular reactor. The catalyst particles have a particular geometric form which promotes heat transfer with the tubular reactor. Certain specific catalyst particles are also provided. 1. A catalytic system comprising:a. a tubular reactor having a cylindrical form around an axis A-A; the internal surface of said tubular reactor having an internal diameter D and an internal radius of curvature R, defined in a plane perpendicular to the axis A-A; a first end-face and a second end-face being arranged perpendicular to said primary axis L at least in the region in which they meet said primary axis L, and', 'first and second sidewalls extending between the first and second end-faces, each of said sidewalls having a curved profile in a cross-section perpendicular to the primary axis L, wherein said first and second sidewalls each independently have an external radius of curvature R1, R2 in said plane being 0.4-0.99 times the internal radius of curvature R of the tubular reactor,', 'and wherein the maximum width D1 of the catalyst particle, measured in a plane defined perpendicular to the primary axis L, is less than 0.25 times the internal diameter D of the tubular reactor,', 'and wherein 2×R1 is greater than D1; and 2×R2 is greater than D1., 'b. at least one catalyst particle located in said tubular reactor, wherein the catalyst particle has a three-dimensional form with a primary length axis L, wherein each catalyst particle comprises2. The catalytic system claim 1 , wherein the external radii of curvature R1 claim 1 , R2 of each of the first and second sidewalls are the same.3. The catalytic system claim 1 , wherein said catalyst particle consists of opposing first and second sidewalls extending between the first and second end-faces claim 1 , and opposing third and fourth sidewalls extending between the first and second sidewalls and said first and ...

System and method for producing hydrogen

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.

STEAM REFORMERS, MODULES, AND METHODS OF USE

The present disclosure is directed to steam reformers for the production of a hydrogen rich reformate, comprising a shell having a first end, a second end, and a passage extending generally between the first end and the second end of the shell, and at least one heat source disposed about the second end of the shell. The shell comprises at least one conduit member comprising at least one thermally emissive and high radiant emissivity material, at least partially disposed within the shell cavity. The shell further comprises at least one reactor module at least a portion of which is disposed within the shell cavity and about the at least one conduit member and comprises at least one reforming catalyst. The disclosure is also directed to methods of producing a hydrogen reformate utilizing the steam reformers, comprising the steps of combusting a combustible mixture in a burner to produce a combustion exhaust that interacts with the steam reactor module(s) through surface to surface radiation and convection heat transfer, and reforming a hydrocarbon fuel mixed with steam in the steam reformers to produce a hydrogen-containing reformate. The present disclosure is further directed to reactor modules for use with the above steam reformers and methods of producing a hydrogen reformate. 1. A reactor module , comprising: a catalyst bed disposed within the cavity to receive heat conducted by the thermally conductive shell, the catalyst bed comprising at least one reforming catalyst;', 'a first channel configured to provide a reactant stream to at least a portion of the catalyst bed;', 'a second channel configured to receive a product stream from at least a portion of the catalyst bed, and', 'a partition wall interposed between at least a portion of the first channel and at least a portion of the second channel through which heat is exchanged between at least a portion of the product stream and at least a portion of the reactant stream;, 'a thermally conductive shell having a ...

APPARATUS AND PROCESS FOR THE PRODUCTION OF FORMALDEHYDE

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

MULTI-TUBULAR STEAM REFORMER AND PROCESS FOR CATALYTIC STEAM REFORMING OF A HYDROCARBONACEOUS FEEDSTOCK

A multi-tubular steam reformer is disclosed, which comprises a steam reforming zone heated by an external heat source and contains a plurality of parallel steam reforming tubes (each comprising a gas supply inlet); a fixed bed of steam reforming catalyst; and a solid, inert insert having an upstream end and a downstream end and is placed in the tube downstream of the gas supply inlet and upstream of the catalyst bed The insert has a tortuous free fluid flow path and the upstream end of the catalyst bed is adjacent to the downstream end of the insert. The ratio of the length of the insert and the length of the catalyst bed is in the range of from 0.05 to 0.5. The invention further relates to a process for catalytic steam reforming of a hydrocarbonaceous feedstock comprising an oxygenated hydrocarbonaceous compound in such multi-tubular steam reformer. 114-. (canceled)15. A multi-tubular steam reformer , comprising a steam reforming zone heated by an external heat source , which steam reforming zone comprises:(a) a plurality of parallel steam reforming tubes, each tube comprising a gas supply inlet;(b) a fixed bed of steam reforming catalyst; and(c) a solid, inert insert having an upstream end and a downstream end which insert is placed in the steam reforming tubes downstream of the gas supply inlet and upstream of the catalyst bed,wherein the insert defines a tortuous-free fluid flow path through the tubes between the upstream end and the downstream end of the insert,wherein the catalyst bed has an upstream end and a downstream end, the upstream end of the catalyst bed being adjacent to the downstream end of the insert, andwherein the ratio of the length of the insert and the length of the catalyst bed is between 0.05 to 0.5.16. The multi-tubular steam reformer according to claim 15 , wherein the ratio of the length of the insert and the length of the catalyst bed is between 0.1 to 0.3.17. The multi-tubular steam reformer according to claim 15 , wherein the tortuous ...

Ozonization continuous reaction device and a working method thereof

The invention discloses an ozonization continuous reaction device, comprising a raw material inlet, a raw material distributing device, one or plurality of single reaction tubes, a product outlet and an air vent. The first end of the raw material distributing device is communicated with the raw material inlet; the first end of one or plurality of single reaction tubes is communicated with the second end of the raw material distributing device; the product outlet is communicated with the second end of the single reaction tube; ozone is conveyed to the single reaction tube via the air vent. The ozonization continuous reaction device provided by the invention realizes the large-scale and continuous production of the ozonization reaction on the basis of guaranteeing security; as the single reaction tube is arranged, the ozone amount and the liquid raw material existing in the single reaction tube in unit time become fewer, the reaction security is greatly improved; in addition, the liquid raw material and the ozone are continuously fed into the reaction device, the exhaust gas and the products are continuously discharged from the reaction device, the accumulation of the ozone is prevented, the security is greatly guaranteed, and the production capacity also can be improved to a higher level.

PSEUDO-ISOTHERMAL REACTOR

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 , ...

Reactor for the Conversion of Carbon Dioxide

The present invention concerns a reactor for the conversion of carbon dioxide or carbon monoxide into hydrocarbon and/or alcohol comprising a support made from an electrically and thermally conductive material, forming the wall or walls of at least one longitudinal channel that passes through the support and also acting as the cathode of the reactor, at least one wire electrode forming an anode of the reactor, and extending within each longitudinal channel, and being arranged at a distance from the wall or walls of the longitudinal channel, each wire electrode optionally being covered with an electrically insulating layer along the part of the wire electrode extending within the longitudinal channel, a catalyst capable of catalysing a conversion reaction for the conversion of carbon dioxide or carbon monoxide into hydrocarbon and/or alcohol, the catalyst being situated between the wire electrode and the wall or walls of each longitudinal channel. 11. A reactor () for conversion of carbon dioxide or carbon monoxide into hydrocarbon and/or alcohol , comprising:{'b': 2', '2', '3', '2', '1, 'a support () made of electrically and thermally conductive material, said support () forming the wall or walls of at least one longitudinal channel () which passes through the support () and also acts as cathode of the reactor ()'}{'b': 4', '1', '4', '3', '3', '3', '4', '5', '4', '3, 'at least one wire electrode () forming an anode of the reactor (), each wire electrode () extending within each longitudinal channel (), along said longitudinal channel (), and being arranged at a distance from the wall or walls of said longitudinal channel (), each wire electrode () being optionally covered by an electrically insulating layer () along the part of the wire electrode () extending within said longitudinal channel (),'}{'b': 6', '6', '4', '3, 'a catalyst () adapted to catalyse a conversion reaction of carbon dioxide or carbon monoxide into hydrocarbon and/or alcohol, the catalyst () being ...

Method and Apparatus for Producing a Hydrogen-Containing Product

Process and apparatus for producing a hydrogen-containing product by steam-hydrocarbon reforming of multiple hydrocarbon feedstocks in a production facility utilizing a prereformer in addition to the primary reformer. The temperature of the reactant mixture introduced into the prereformer is controlled depending on the composition of the reactant mixture fed to the prereformer. 2. The process of wherein during the first time period the process further comprises:passing the second fraction of the first reactant gas mixture from the bypass conduit to the catalyst-containing reactor, introducing the second fraction of the first reactant gas mixture into the catalyst-containing reactor as at least another portion of the feed to the catalyst-containing reactor, reacting the second fraction of the first reactant gas mixture in the catalyst-containing reactor, wherein the effluent from the catalyst-containing reactor is also formed from the second fraction of the first reactant gas mixture.3. The process of wherein during the second time period the process further comprises:passing the second fraction of the second reactant gas mixture from the heat exchanger to the catalyst-containing reactor, introducing the second fraction of the second reactant gas mixture into the catalyst-containing reactor as at least another portion of the feed to the catalyst-containing reactor, reacting the second fraction of the second reactant gas mixture in the catalyst-containing reactor, wherein the effluent from the catalyst-containing reactor is also formed from the second fraction of the second reactant gas mixture .4. The process ofwherein the first fraction or all of the first reactant gas mixture is cooled in the heat exchanger by indirect heat exchange with boiler feed water.5. The process ofwherein when passing the first fraction or all of the first reactant gas mixture from the heat exchanger to the catalyst-containing reactor, the first fraction or all of the first reactant gas ...

METHOD FOR ACTIVATING A CATALYST, REACTOR, AND METHOD OF OBTAINING HYDROCARBONS IN FISCHER-TROPSCH PROCESS

The invention relates to Fischer-Tropsch synthesis in a compact version. A compact reactor comprises a housing, rectangular reaction channels inside the housing, which are filled with a cobalt catalyst, synthesis gas injection nozzles in the number determined by the ratio of the number of channels to the number of synthesis gas injection nozzles, an input and output nozzle for heat transfer medium on which a pressure controller installed, and an assembly for withdrawing synthetic hydrocarbons. The cobalt catalyst is activated by passing hydrogen through it. Synthetic hydrocarbons are produced by passing synthesis gas through the reaction channels filled with the activated cobalt catalyst. The space velocity of synthesis gas is increased every 300-500 h, followed by returning to the initial process conditions. This provides a high-molecular-weight hydrocarbon output per unit mass of the reactor. 1. A compact reactor for the production of synthetic hydrocarbons in a Fischer-Tropsch process , comprising a housing with reaction channels filled with a cobalt catalyst , wherein the channels have a thickness of 1 to 5 mm and a rectangular cross section; synthesis gas injection nozzles; input and output nozzles for heat transfer medium; and an assembly for withdrawing synthetic hydrocarbons , wherein the reactor is characterized in that a pressure controller is installed on the output nozzle for heat transfer medium , the outer surface of the wall of the reaction channels with the catalyst has a roughness of 1.6 to 25 μm , a distance between the nearest reaction channels is 1 to 5 mm , a thickness of the wall of the reaction channel is 1 to 3 mm , a width-to-thickness ratio of the reaction channel is 2 to 100 , and a height-to-thickness ratio of the reaction channel is from 20 to 2000 , wherein a ratio of the number of reaction channels to the number of synthesis gas injection nozzles is from 1 to 50.2. The reactor according to claim 1 , characterized in that a ratio of the ...

PRODUCTION OF OXIDIZED OLEFINS

The present disclosure includes a system and method for the production of oxidized olefins. Two or more reactors include a number of reaction tubes each having a first surface defining a first side and a second surface defining a second of each of the tubes side are provided. A catalyst for catalytic oxidation of olefins can be located on the first side of the number of reaction tubes is included. A common supply line supplies inlets to each reactor that provide a mixture comprising olefins and oxygen to the catalyst. Product outlet streams of each reactor receive at least the oxidized olefin product and are joined to a single product stream. Coolant fluid passes through the reactors to remove heat from the number of reaction tubes and flows into a single coolant drum connected to the two or more reactors. The single coolant drum receives the coolant fluid from a number of coolant fluid outlet streams of each of the reactors. The single coolant drum supplies the coolant fluid at a common temperature to a number of coolant fluid inlet streams of each reactor. 1. A system for producing oxidized olefins , comprising:two or more reactors, each of the two or more reactors including a number of reaction tubes each including a first surface defining a first side and a second surface opposite the first surface that defines a second side of each of the number of reaction tubes;a catalyst for catalytic oxidation of olefins on the first side of the number of reaction tubes;an inlet to each of the two or more reactors that supplies a mixture comprising olefins and oxygen to the catalyst, where a common supply line supplies the mixture to each inlet of the two or more reactors;a product outlet from each of the two or more reactors that receives a product stream comprising the oxidized olefins, where each product outlet joins to a single common product stream comprising the oxidized olefins; andonly one coolant drum connected to the two or more reactors, where coolant fluid ...

BOILING WATER REACTOR

The invention relates to a boiling water reactor for an exothermal reaction. The reactor comprises reactant by-pass inserts arranged on top of the upper tube sheet to provide for a catalyst layer on top of the upper tube sheet and also a cooling stream of reactant by-passing the upper layer of catalyst and cooling the upper tube sheet from the temperature rise due to the exothermal reaction taking place in the upper layer of catalyst. 2. Boiling water reactor according to claim 1 , wherein said at least one reactant by-pass insert comprises a plurality of single tube inserts with a lower end diameter smaller than the inner diameter of the top end of the reaction tubes and means for fixing said tube inserts to the top end of the reaction tubes.3. Boiling water reactor according to claim 2 , wherein said fixing means comprises a top part of the tube inserts with an outer dimension larger than the inner diameter of the top end of the reaction tubes claim 2 , whereby the tube inserts are fixed to the top end of the reaction tubes by means of gravity.4. Boiling water reactor according to claim 2 , wherein said fixing means comprises a plurality of bulges.5. Boiling water reactor according to claim 2 , wherein the top part of the tube inserts is hexagon in shape.6. Boiling water reactor according to claim 1 , wherein said at least one reactant by-pass insert comprises a tray of assembled tube inserts for holding catalyst and insertion into the top end of the reaction tubes and apertures in the tray for by-pass of the reactant.7. Boiling water reactor according to claim 1 , wherein the area of the annulus between the lower end of the at least one reactant by-pass insert and the top of the upper tube sheet is adapted to control the amount of reactant by-pass into the reaction tubes.8. Boiling water reactor according to claim 1 , further comprising insertion rings for mounting around the lower end of the at least one reactant by-pass insert claim 1 , wherein said insertion ...

SYSTEMS, METHODS, AND APPARATUSES FOR FISCHER-TROPSCH REACTOR CASCADE

Methods, systems and apparatuses are disclosed for a Fischer-Tropsch (“FT”) operation including a first FT stage comprising at least one FT reactor having a first FT catalyst and a first heat transfer surface area to catalyst volume configured to receive a first feed comprising synthesis gas and to convert a first portion of the synthesis gas in the first feed into first FT products. The disclosure also provides for a separation apparatus configured to separate the first FT products into first liquid FT hydrocarbons and first FT tail gas comprising unreacted syngas and for a second FT stage comprising at least one second FT reactor, having a second FT catalyst and a second heat transfer surface area to catalyst volume different from the first heat transfer surface area to catalyst volume, and configured to receive a second feed comprising the first FT tail gas and to convert at least a portion of the second feed into a second FT products. 1. A Fischer-Tropsch (“FT”) reactor system , the system comprising:a. a first FT reactor having a first FT catalyst and a first heat transfer surface area to catalyst volume ratio, the first FT reactor configured to receive a first feed comprising synthesis gas and, operating at first FT conditions, to convert a first portion of the synthesis gas in the first feed into first FT products comprising FT hydrocarbons and leave unconverted a second portion of the synthesis gas;b. a first separation apparatus configured to receive the first FT products as at least part of its feed and to separate the first FT products into first liquid FT hydrocarbons and first FT tail gas stream comprising unreacted syngas; andc. a second FT reactor, having a second FT catalyst and a second heat transfer surface area to catalyst volume ratio that is different from the first heat transfer surface area to catalyst volume ratio, in series with the first FT reactor and configured to receive a second feed comprising the first FT tail gas stream and, ...

Device for Filling a Tube with Particulate Filling Material

The present invention relates to a device for gently and uniformly filling a tube, in particular a tubular reactor, with particulate filling material, in particular catalyst particles; wherein the device comprises specially designed fall arrester elements and also comprises means which reduce the wear of the fall arrester elements; and method for filling a tube using these articles. 1. A device for filling a tube with particulate filling material , comprising at least one fall arrester element that is fastened to a carrier and is introducible together with the carrier into the tube to be filled; wherein the at least one fall arrester element carries a net structure that is permeable to the filling-material particles , wherein the net structure comprises a multiplicity of elastic net elements and the filling-material deflector is arranged above the net structure; and wherein the net structure comprises a central body which carries the net elements;characterized in that,above the at least one fall arrester element, a filling-material deflector radially enclosing the carrier is arranged, the outside diameter of said filling-material deflector being less than the inside diameter of the tube to be filled, wherein the filling-material deflector is formed as an umbrella-like, substantially radially symmetric structure with a lateral surface that drops substantially uniformly toward the outside, and protects the central region of the at least one fall arrester element from being struck directly by filling-material particles during a filling operation, wherein the central region comprises the body and the inner portion of the net elements, via which the latter are fastened to the body.2. The device as claimed in claim 1 , wherein the central region has 90 to 10% of the radial diameter (d) of the fall arrester element.3. The device as claimed in claim 1 , wherein the central region has 40 to 20% of the radial diameter (d) of the fall arrester element.4. The device as claimed ...

REACTOR PACKING WITH PREFERENTIAL FLOW CATALYST

The present invention relates to reactor tubes packed with a catalyst system employed to deliberately bias process gas flow toward the hot tube segment and away from the cold segment in order to reduce the circumferential tube temperature variation. 1. A method of producing synthesis gas within a tubular reformer , comprising:introducing a process gas, where the process gas comprises steam and at least one hydrocarbon at an inlet of one or more tubes disposed in the reformer, contacting the process gas with a catalyst in the interior of the one or more tubes, wherein at least a portion of the catalyst has a structural element that circumferentially biases a process gas flow toward at least one tube wall side of greater incident heat flux thereby reducing the maximum tube wall temperature, andremoving a reformed process gas at an outlet of the one or more tubes wherein the reformed process gas is a synthesis gas containing predominantly hydrogen, carbon monoxide, carbon dioxide, and water.2. The method of claim 1 , wherein the structural element biases the process gas flow toward the at least one tube wall side of greater incident heat flux and away from the tube wall sides of lesser incident heat flux claim 1 , thereby reducing the circumferential variation in the tube wall temperature.3. The method of claim 1 , wherein the structural element is utilized in at least a portion of the tube.4. The method of claim 3 , wherein the type and/or elevation of the structural element is predetermined by analysis of the reformer tube wall incident heat flux profile.5. The method of claim 1 , wherein the structural element has a configuration that varies over the length of the tube.6. The method of claim 1 , wherein one or more types of structured elements are utilized in one or more tubes within the tubular reformer7. A catalyst with a structural element disposed in the interior of one or more tubes within a tubular reformer claim 1 , comprising: a structural element that ...

STEAM BOILER FOR A STEAM REFORMER

Embodiments are disclosed that relate to a compact steam boiler which may provide steam to a steam reformer in a fuel cell system. For example, one disclosed embodiment provides a steam boiler including an outer shell and a first inner tube and a second inner tube within the outer shell, the first and second inner tubes spaced away from one another. The steam boiler further includes a twisted ribbon positioned inside each of the first and second inner tubes. 1. A steam reformer , comprising:a cylindrical reaction chamber;an exhaust heat exchanger positioned around an upper portion of the reaction chamber; anda steam boiler wrapped around the heat exchanger and including an outer shell, a first inner tube and a second inner tube within the outer shell, and a twisted ribbon positioned inside each of the first and second inner tubes.2. The steam reformer of claim 1 , wherein the first and second inner tubes are spaced away from one another claim 1 , the reformer further including an exterior shell which surrounds a lower portion of the reaction chamber and includes adjacent angled fins which extend away from an inner surface of the exterior shell and toward the bottom of the steam reformer.3. The steam reformer of claim 2 , wherein the first inner tube is wrapped with a first wire in a first direction and the second inner tube is wrapped with a second wire in a second direction claim 2 , and wherein the first wire and the second wire cross once per revolution along a length of the first and second inner tubes to space the first and second inner tubes away from one another.4. The steam reformer of claim 2 , further comprising a third inner tube and a fourth inner tube spaced away from one another and spaced away from the first and second inner tubes via a third wire wrapped around the third inner tube in a second direction and a fourth wire wrapped around the fourth inner tube in a first direction claim 2 , and a twisted ribbon positioned inside each of the third and ...

Method and system for the production of hydrogen

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

Cooled reactor for the production of dimethyl ether from methanol

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.

METHODS FOR SELECTING A LOADING PRESSURE DROP TOLERANCE SPECIFICATION FOR A MULTITUBULAR FIXED-BED REACTOR

A method for a selecting a loading pressure drop tolerance specification for a plurality of tubes in a multitubular fixed-bed reactor, wherein the plurality of tubes comprise a packed bed of epoxidation catalyst, the method comprising: defining a first loading pressure drop tolerance range for the plurality of tubes based on a desired maximum variation in outlet oxygen concentration, relative to the mean, for the plurality of tubes; defining a second loading pressure drop tolerance range for the plurality of tubes based on a desired maximum number of tube corrections for the plurality of tubes; and selecting the loading pressure drop tolerance specification for the plurality of tubes such that the entirety of the loading pressure drop tolerance specification falls within the first loading pressure drop tolerance range and the second loading pressure drop tolerance range. 1. A method for a selecting a loading pressure drop tolerance specification for a plurality of tubes in a multitubular fixed-bed reactor , wherein the plurality of tubes comprise a packed bed of epoxidation catalyst , the method comprising:defining a first loading pressure drop tolerance range for the plurality of tubes based on a desired maximum variation in outlet oxygen concentration, relative to the mean, for the plurality of tubes;defining a second loading pressure drop tolerance range for the plurality of tubes based on a desired maximum number of tube corrections for the plurality of tubes; andselecting the loading pressure drop tolerance specification for the plurality of tubes such that the entirety of the loading pressure drop tolerance specification falls within the first loading pressure drop tolerance range and the second loading pressure drop tolerance range.2. The method of wherein the desired maximum variation in the outlet oxygen concentration is no more than ±0.4 mol %.3. The method of wherein the desired maximum variation in the outlet oxygen concentration is no more than ±0.2 mol ...

DOWN-FIRED BURNER WITH A PERFORATED FLAME HOLDER

A down-fired flame burner includes a flame holder positioned below the burner. The flame holder includes a plurality of perforations that collectively confine a combustion reaction of the burner to the flame holder. 1. A down-fired burner comprising:a down-fired fuel nozzle configured to output fuel in a downward direction;an oxidant source configured to output an oxidant; and an input surface facing the down-fired fuel nozzle;', 'an output surface opposite the fuel nozzle; and', 'a plurality of perforations extending from the input surface to the output surface and collectively configured to promote a combustion reaction of the fuel and oxidant within the perforations., 'a flame holder positioned below the down-fired fuel nozzle, the flame holder including2. The down-fired burner of claim 1 , wherein the flame holder is configured to contain a majority of the combustion reaction within the perforations.3. The down-fired burner of claim 1 , wherein the flame holder is configured to contain 80% or more of the combustion reaction within the perforations.4. The down-fired burner of claim 1 , wherein the flame holder is a refractory material.5. The down-fired burner of claim 1 , wherein the flame holder is an integral structure.6. The down-fired burner of claim 1 , wherein the flame holder is configured to initiate the combustion reaction.7. The down-fired burner of claim 1 , comprising a preheating mechanism configured to heat the flame holder prior to starting the combustion reaction.8. The down-fired burner of claim 7 , wherein the preheating mechanism comprises a second fuel nozzle configured to generate a flame adjacent to the flame holder.9. The down-fired burner of claim 7 , wherein the preheating mechanism comprises a laser configured to irradiate the flame holder.10. The down-fired burner of claim 7 , wherein the down-fired fuel nozzle is an adjustable nozzle and the preheating mechanism is configured to move the fuel nozzle closer to the flame holder during a ...

ENHANCED EFFICIENCY ENDOTHERMIC REACTOR FOR SYNGAS PRODUCTION WITH FLEXIBLE HEAT RECOVERY TO MEET LOW EXPORT STEAM GENERATION

An apparatus for carrying out endothermic reactions including a plurality of catalytic vessels, immersed in a combustion chamber having a contiguous overlaid convection chamber enclosing a top portion of the catalytic vessels wherein heat is recovered at a lower temperature level from the flue gases from the combustion chamber. The catalytic vessels may contain internal and coaxial heat recovery tubes creating an annular space filled in with a catalytic device. Both the external heat recovery through the catalyst tube outer surface and the internal heat recovery through the inner tube surface can be maximized by an enhanced catalytic device acting also as a heat transfer promoter in the process gas region. The apparatus provides enhanced and flexible heat recovery that permits to meet the request of minimum or none export steam production in one single apparatus, avoiding the need of a pre-reforming section and/or of a convective reformer downstream. 114-. (canceled)15. An apparatus for conducting endothermic reactions able to meet the heat balance with a null or limited amount of export steam , through a flexible heat recovery , comprising:a combustion chamber having a closed bottom end, an open top end, two opposite end walls, and two opposite side walls;an upper convection chamber, in communication with said combustion chamber through said open top end, allowing the flow of flue gas through a plurality of convection channels in flow communication with a top plenum chamber connected to an outlet flue gas channel;a plurality of catalytic vessels arranged at a distance and disposed in line or staggered along the centerline of the combustion and convection chamber in such a way that the bottom portion is immersed in the combustion chamber and the remaining top portion is immersed in the convection chamber wherein the portion of the catalytic vessel immersed in the combustion chamber is such that the flue gas temperature at its exit and inlet of the convection chamber ...

Reactor and Process for the Hydrogenation of Carbon Dioxide

The present invention is directed to a membrane reactor for the hydrogenation of carbon dioxide, said membrane reactor comprising a reaction compartment () comprising a catalyst bed, a permeate compartment () and a membrane separating the reaction compartment and the permeate compartment, wherein said permeate compartment comprises a condensing surface. 1. A membrane reactor for the hydrogenation of carbon dioxide ,said membrane reactor comprising a reaction compartment comprising a catalyst bed, a permeate compartment and a water-permeable membrane separating the reaction compartment and the permeate compartment, wherein said permeate compartment comprises a condensing surface and a means for cooling that is connected to said condensing surface such that during operation of the reactor, water can condense on the condensing surface.2. The membrane reactor in accordance with claim 1 , wherein the means for cooling comprises an active-cooling device.5. The membrane reactor in accordance with claim 1 , wherein said permeate compartment and means for cooling comprise an active-cooling device which active-cooling device is disconnected from the inner wall.6. The membrane reactor in accordance with claim 3 , wherein said inner wall and outer wall are tubular and the outer wall is at least partially co-axially arranged around said inner wall.7. The membrane reactor in accordance with claim 1 , wherein the condensing surface comprises protruding surface elements.8. The membrane reactor in accordance with claim 1 , wherein said water-permeable membrane comprises a hydrophilic membrane.9. The membrane reactor in accordance with claim 1 , wherein said catalyst bed comprises copper claim 1 , zinc oxide claim 1 , zirconia claim 1 , palladium claim 1 , cerium(IV) oxide or combinations thereof.10. The process for the hydrogenation of carbon dioxide claim 1 , wherein said process comprises reacting carbon dioxide with hydrogen to form methanol and/or dimethyl ether claim 1 , and ...

Process for the ammonia production

Process and plant for the synthesis of ammonia from a hydrocarbon feedstock, comprising: primary reforming with steam and air-fired secondary reforming wherein primary reforming is performed at a temperature and pressure of at least 790° C. and 50 bar, and secondary reforming is carried out substantially in absence of excess air, the so obtained make-up synthesis gas having a H 2 to N 2 molar ratio in the range 2.5 to 3.

Epoxidation process

A method for the oxidation of ethylene to form ethylene oxide which comprises: providing an aqueous stream containing ethylene glycol and impurities; introducing the aqueous stream in a first ion exchange treatment bed to reduce the content of these impurities; determining whether an outlet of the first ion exchange treatment bed has a conductivity greater than about 5 μS/cm; upon determining that the outlet of the first ion exchange treatment bed has a conductivity greater than about 5 μS/cm, introducing the outlet of the first ion exchange treatment bed into a second ion exchange treatment bed; and upon determining that the outlet of the first ion exchange treatment bed has a conductivity greater than about 60 μS/cm, redirecting the introduction of the aqueous stream to the second ion exchange treatment bed and regenerating the first ion exchange bed.

COMPACT AND MAINTAINABLE WASTE REFORMATION APPARATUS

Methods and apparatus for compact and easily maintainable waste reformation. Some embodiments include a rotary oven reformer adapted and configured to provide synthesis gas from organic waste. Some embodiments include a rotary oven with simplified operation both as to reformation of the waste, usage of the synthesized gas and other products, and easy removal of the finished waste products, preferably in a unit of compact size for use in austere settings. Yet other embodiments include Fischer-Tropsch reactors of synthesized gas. Some of these reactors include heat exchanging assemblies that provide self-cleaning effects, efficient utilization of waste heat, and ease of cleaning.

Process And Reactor Comprising A Plurality Of Catalyst Receptacles

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

Method for manufacturing carbon nanotube, method for manufacturing carbon nanotube assembled wire, method for manufacturing carbon nanotube assembled wire bundle, carbon nanotube manufacturing apparatus, carbon nanotube assembled wire manufacturing apparatus, and carbon nanotube assembled wire bundle manufacturing apparatus

A method for manufacturing a carbon nanotube includes: a growing step of growing a carbon nanotube from a catalyst particle by supplying a carbon-containing gas to the catalyst particle in a suspended state; and a drawing step of drawing the carbon nanotube by applying a tensile force to the carbon nanotube in a suspended state.

HIGH PRESSURE STRIPPERS FOR USE IN UREA PLANTS

Shell-and-tube strippers for stripping a urea/carbamate mixture, related systems, methods, and uses. The stripper includes a shell, a plurality of tubes disposed within the shell, and a heating fluid distributor for homogenizing the flow of a heating fluid near a heating fluid inlet. The heating fluid distributor includes an edge wall and a laterally disposed heating fluid distribution plate. Related systems, methods, and uses are also provided.

METHOD TO OBTAIN METHYLENE MALONATE VIA BIS(HYDROXYMETHYL) MALONATE PATHWAY

Method to obtain methylene malonate and related monomers following a bis(hydroxymethyl) malonate pathway. A bis(hydroxymethyl) malonate intermediary is subsequently reacted (i.e., subjected to thermolysis) to provide a methylene malonate monomer species. A source of formaldehyde (e.g., formalin) is provided in the presence of a basic catalyst (e.g., calcium hydroxide), to which a malonate (e.g., diethyl malonate) is added under suitable reaction conditions to obtain the desired intermediary (e.g., dialkyl bis(hydroxymethyl) malonate). The intermediary is reacted (i.e., subjected to thermolysis) under suitable conditions in the presence of a suitable catalyst (e.g., a zeolite) to obtain a methylene malonate monomer. In an exemplary embodiment, the thermolysis reaction includes the addition of the bis(hydroxymethyl) malonate intermediary onto a heated catalyst. The reaction product is collected and purified. The disclosed methods may be performed in a continuous operation. Discrete steps may be performed by using modular units within a plant. 162-. (canceled)63. A plant for producing a methylene malonate monomer comprising:at least one diol production unit comprising a diol reactor apparatus capable of reacting a dialkyl malonate ester and a source of formaldehyde in the presence of a catalyst,at least one diol purification unit,at least one monomer production unit comprising a plurality of catalyst columns and at least one heating apparatus for maintaining the temperature of the plurality of catalyst columns, andat least one monomer purification unit comprising a condensation apparatus, a fractional distillation apparatus, or both;wherein the at least one diol production unit is in communication with the at least one diol purification unit, and the at least one diol purification unit is in communication with the at least one monomer production unit, and the at least one monomer production unit is in communication with the at least one monomer purification unit.6473-. ...

Hydrocarbon Pyrolysis

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 ...

Manufacture of Methylolalkanes with Augmented Heat Transfer and Improved Temperature Control

A multistage tubular reaction system and method for preparing methylol derivatives of an aldehyde includes a tubular reaction system with a plurality of successive reactor stages comprising a plurality of jacketed reaction tubes provided with a cooling system adapted to control flow of a cooling medium through said jacketed reaction tubes. The cooling medium flow is controlled independently in different stages in response to temperature measurements in the reaction system to regulate temperature. In order to further reduce temperature spikes and byproduct generation, aldehyde is stepwise added to the production stream at a plurality of feed ports proximate to reaction tubes equipped with tube inserts to enhance mixing and heat transfer. 2. The method according to claim 1 , wherein the production stream is fed to a plurality of tubular reaction sections provided with tube inserts following addition of the Cor higher condensable aldehyde and/or base.3. The method according to claim 2 , wherein said tube inserts are displacement flow inserts.4. The method according to claim 3 , wherein said tube inserts are wire-wrapped tube inserts.6. The method according to claim 1 , wherein there is provided a cooling control system adapted to control temperature and flow of a cooling medium claim 1 , and the flow of the cooling medium is independently controlled in different stages of the reaction system in response to temperature measurements in respective stages.7. The method according to claim 6 , wherein said tubular reaction system with a plurality of reaction stages includes tubular reaction sections jacketed with a cooling medium.8. The method according to claim 1 , wherein the methylolalkane is trimethylolpropane and the aldehyde which is condensable with formaldehyde is n-butyraldehyde.9. The method according to claim 1 , wherein the methylolalkane is neopentyl glycol and the aldehyde which is condensable with formaldehyde is isobutyraldehyde.10. The method according to ...

REACTOR AND HEATER CONFIGURATION SYNERGIES IN PARAFFIN DEHYDROGENATION PROCESS

An apparatus for heating a process fluid is presented. The apparatus is for improving the foot-print of a fired heater and to reduce the fired heater volume. The apparatus includes a W-shaped process coil to provide for a smaller single-cell fired heater, and a fired heater with a lower profile, providing flexibility in positioning relative to downstream reactors. 1. An apparatus for reducing hot transfer volume , comprising:a radiant fired heater having a single cell, at least one process coil, burners, and a flue gas outlet; andat least one outlet manifold having an inlet in fluid communication with the process coils outlets and at least one manifold outlet;wherein each process coil has a configuration of three tubes in a parallel orientation, with two semi-circular tubular sections connecting the ends of the tubes, such that the tubes and tubular sections form a generalized W-shaped coil, with the central tube having one end connected to the outlet port, and the two outer tubes having one end connected to an inlet port.2. The apparatus of further comprising a convection bank having an inlet in fluid communication with the flue gas outlet claim 1 , and heating tubes claim 1 , wherein the heating tubes have an inlet and an outlet.3. The apparatus of claim 2 , wherein the convection bank is above or below the fired heater.4. The apparatus of claim 2 , wherein the convection bank is positioned to the side of the fired heater.5. The apparatus of claim 2 , wherein the heating tubes are for steam generation.6. The apparatus of further comprising:a moving bed reactor having a process stream inlet disposed above the reactor moving bed, a process fluid outlet, a catalyst inlet, a catalyst collector at the bottom of the reactor, and a catalyst outlet at the bottom of the catalyst collector.7. The apparatus of claim 6 , wherein the radiant fired heater is elevated to provide for that the moving bed reactor process stream inlet is disposed within 0.3 m elevation of the outlet ...

Vaporisation in Oxidation to Phthalic Anhydride

In the production of phthalic anhydride by the oxidation of ortho-xylene with air, the ortho-xylene loading is increased without increasing the likelihood of explosion by insulating the system to avoid cold spots to keep the ortho-xylene at a temperature above its dew point; in addition the system may be electrically interconnected and grounded to reduce the risk of spark initiated explosions or deflagrations. 133.-. (canceled)34. An apparatus for the production of phthalic anhydride which comprises a reaction section comprising a fixed bed tubular catalytic reactor , and a raw material preparation section comprising(i) separate raw material delivery sections for a liquid and for a gaseous raw material,(ii) a raw material mixing section comprising a system for spraying the liquid raw material into the gaseous raw material to form a mixture of vaporised liquid and gas, and 'said apparatus further comprising', '(iii) a mixture delivery section for delivering the mixture of vaporised liquid and gas to the fixed bed catalytic reactor,'}at least one rupture disk on the raw material preparation section and/or on the reaction section, andwherein the raw material delivery sections each comprise a raw material heater, and wherein the external surfaces of the equipment nozzles, which are provided for connecting the individual elements of the process equipment in the raw material preparation section and/or in the reaction section up to the inlet tubesheet of the tubular reactor, and which are in contact with the mixture of vaporised liquid and gas, are thermally insulated.35. The apparatus according to wherein an insulating blanket is provided on the external surface of the rupture disc.36. The apparatus according to wherein the rupture disc is provided with a relief stack comprising a foam cap.37. The apparatus according to further comprising means for heating the thermal insulation.38. The apparatus according to wherein the heating means is electrical tracing and/or steam ...

ALKANE OXIDATIVE DEHYDROGENATION (ODH)

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, ...

ETHYLENE-TO-LIQUIDS SYSTEMS AND METHODS

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 ...

Process for performing an endothermic reaction

Process for performing an endothermic reaction in a reactor containing catalyst tubes, the catalyst tubes containing a catalyst promoting the endothermic reaction, the process comprising the steps of, a. contacting the catalyst contained in the catalyst tubes with a feed flow passing through the channels from an entrance end to an exit end, b. contacting an outer surface of the catalyst tubes with a flow of a heating medium having an initial heating temperature and flowing co-currently with the flow of feeds to heat the surface by convection, c. mixing at least part of the heating medium after having been contacted with the catalyst tubes with a flow of fresh heating medium having a start temperature higher than the initial heating temperature to form the co-current heating medium having the initial heating temperature and reactor for carrying out the process.

Parallel reforming in chemical plant

A chemical plant including: a reforming section arranged to receive a feed gas comprising hydrocarbons and provide a combined synthesis gas stream, wherein the reforming section includes: an electrically heated reforming reactor housing a first catalyst, an autothermal reforming reactor in parallel with the electrically heated reforming reactor, wherein the reforming section is arranged to output a combined synthesis gas stream including at least part of the first and/or second synthesis gas streams, an optional post processing unit downstream the reforming section, a gas separation unit arranged to separate a synthesis gas stream into a water condensate and an intermediate synthesis gas, and a downstream section arranged to receive the intermediate synthesis gas and to process the intermediate synthesis gas to a chemical product and an off-gas. Also, a process for producing a chemical product from a feed gas comprising hydrocarbons.

METHOD FOR PRE-REFORMING HYDROCARBONS

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 ...

Method for Preparing Cyclododecene and Synthesis Device Therefor

A method for preparing cyclododecene and a synthesis device therefor, of the present invention, remarkably increase the conversion ratio of cyclododecatriene and selectivity of cyclododecene, can minimize the costs required for equipment and processing, are practical, reduce processing time, and are industrially advantageous to mass production in comparison with a conventional method and device. 1. A method for synthesizing cyclododecene , comprising a hydrogenation step of partially hydrogenating cyclododecatriene to synthesize cyclododecene ,wherein cyclododecatriene and hydrogen sequentially pass through a continuous stirred-tank reactor and a tubular reactor and react with each other in the continuous stirred-tank reactor and the tubular reactor to synthesize cyclododecene.2. The method of claim 1 , wherein the following Expression 1 is satisfied claim 1 ,{'br': None, 'sub': 1P', '1C, '1≤τ/τ≤9\u2003\u2003[Expression 1]'}{'sub': 1C', '1P, '(in Expression 1, τis a residence time of a reactant or a product in the continuous stirred-tank reactor, and τis a residence time of a reactant or a product in the tubular reactor).'}3. The method of claim 1 , wherein the continuous stirred-tank reactor is obtained by sequentially connecting a first continuous stirred-tank reactor and a second continuous stirred-tank reactor.4. The method of claim 3 , wherein the following Expression 2 is satisfied claim 3 ,{'br': None, 'sub': 2C', '1C, '0.1≤τ/τ≤0.9'}{'br': None, 'sub': 1P', '1C, '1≤τ/τ≤9\u2003\u2003[Expression 2]'}{'sub': 1C', '2C, '(in Expression 2, τand τare a residence time of a reactant or a product in the first continuous stirred-tank reactor and a residence time of a reactant or a product in the second continuous stirred-tank reactor, respectively, and Tip is a residence time of a reactant or a product in the tubular reactor).'}5. The method of claim 1 , wherein the cyclododecene is synthesized by hydrogenation to the cyclododecatriene in a solvent containing ethanol ...

APPARATUS AND METHOD FOR HYDROCONVERSION

An apparatus is disclosed for the hydroconversion of hydrocarbon feedstock with a hydrogen gas at elevated temperature and pressure with the use of a catalyst. The apparatus is a reactor vessel with a grid plate distributor for improved gas liquid distribution. The distributor comprises a grid plate and a bubble cap assembly with a plurality of tubular risers extending through the grid plate. Each tubular riser has an upper section above the grid plate and a lower section below the grid plate, the lower section terminated with an open bottom end for ingress of the hydrogen gas and hydrocarbon feedstock, the upper section having a closed top terminated with a housing cap. Each tubular riser has at least a vertical slot and a least a laterally placed opening sufficiently sized such that in operation, the liquid level in the zone below the grid plate is above the vertical slot and below the laterally placed opening. 1. A grid plate assembly for use in a hydroconversion reactor in which a hydrocarbon feedstock is mixed with a hydrogen gas and at least one catalyst at elevated temperature and pressure , comprising:a grid plate having a top and a bottom dividing the hydroconversion reactor into a zone above the grid plate top and a zone below the grid plate bottom;a plurality of tubular risers extending through the grid plate, wherein each tubular riser comprises an upper section extending above the grid plate top and closed with a bubble cap and a lower section extending below the grid plate bottom and having an open end, at least one laterally placed vertical slot and at least one laterally placed opening;wherein each tubular riser is placed in the grid plate assembly such that an inclined liquid level in the zone below the grid plate bottom is maintained between the laterally placed vertical slot and the at least one laterally placed opening.2. The grid plate assembly of claim 1 , wherein the laterally placed opening has a shortest dimension ranging from 1/16 to ½ of ...

REFORMER TUBE HAVING INTERNAL HEAT EXCHANGE

A reformer tube for producing synthesis gas by steam reforming of hydrocarbon-containing feed gases, preferably natural gas, includes one or more helically coiled heat exchanger tubes which are arranged within a catalyst bed of a reforming catalyst and are helically coiled over part of their length located within the catalyst bed and are otherwise straight are present, where the straight proportion of the heat exchanger tubes and/or the helix pitch of the helically coiled part alters within the catalyst bed and matching to requirements of the pressure drop, the heat exchange properties, and the corrosion resistance. 1. A reformer tube for converting a hydrocarbonaceous feedstock into a synthesis gas product comprising a carbon oxide and hydrogen under steam reforming conditions , the reformer tube comprising:(a) an outer tube comprising an open tube end, a closed tube end, and a bed of a solid catalyst active suitable for steam reforming, wherein the outer tube is configured to be heated from outside;(b) a feed gas stream inlet, configured to feed in the feedstock, wherein the feed gas stream inlet is arranged at the open tube end and is in fluid connection with the catalyst bed;(c) a helically-coiled heat exchanger tube arranged within the catalyst bed, wherein a helically-coiled heat exchanger tube inlet end is in fluid connection with the catalyst bed and a helically-coiled heat exchanger tube outlet end is in fluid connection with a synthesis gas product stream outlet, and wherein the helical-coiled heat exchanger tube is in heat exchanging relationship with the catalyst bed and the feed gas stream flowing through the catalyst bed; and(d) a synthesis gas product stream outlet arranged at the open tube end and in fluid connection with the outlet end of the helically-coiled heat exchanger tube, but not in fluid connection with the inlet for the feed gas stream,wherein the feed gas stream initially flows through the catalyst bed and subsequently in counterflow ...

NOZZLE, SOLID MATTER UNLOADING DEVICE, SOLID MATTER UNLOADING SYSTEM, AND SOLID MATTER UNLOADING METHOD

A nozzle includes: a flow path allowing gas to flow; tip opening portion(s) formed on a tip side of the flow path; a base end opening portion formed on a base end side of the flow path; and side hole(s) which is formed on the base end side from the tip opening portion and allows a part of the gas flowing through the flow path to be discharged toward the base end side. The tip opening portion(s) is formed in a direction of the flow path. The side hole(s) is formed along a circumferential direction of the flow path. When the gas is supplied from the base end opening portion, a ratio (Q1/Q1) of a flow rate (Q1) of the gas discharged from the tip opening portion(s) and a flow rate (Q1) of the gas discharged from the side hole(s) is 0.05 to 0.7. 1. A nozzle which is connectable to a conduit for supplying gas to a tubular body filled with granular solid matters , the nozzle comprising:a flow path which allows the gas to flow;a tip opening portion which is formed on a tip side of the flow path;a base end opening portion which is formed on a base end side of the flow path; anda side hole which is formed on the base end side from the tip opening portion and allows a part of the gas flowing through the flow path to be discharged toward the base end side, whereinthe one or more tip opening portions are formed in a direction of the flow path,the one or more side holes are formed along a circumferential direction of the flow path, andwhen the gas is supplied from the base end opening portion, a ratio (Q1a/Q1b) of a flow rate (Q1a) of the gas discharged from the one or more tip opening portions and a flow rate (Q1b) of the gas discharged from the one or more side holes is 0.05 to 0.7.2. The nozzle according to claim 1 , whereinthe side hole is open toward a base end side of the nozzle at an angle of 30° or more and less than 90° with respect to an axis along a longitudinal direction of the flow path.3. The nozzle according to claim 1 , whereinthe two or more side holes are formed ...

PROCESS FOR PRODUCING PURE HYDROGEN WITH LOW STEAM EXPORT

A process is proposed for producing pure hydrogen by steam reforming of a feed gas comprising hydrocarbons, preferably natural gas or naphtha, with a simultaneously low and preferably adjustable export steam flow rate. The process includes the steam reforming of the feed gas, for which the heat of reaction required is provided by combustion of one or more fuel gases with combustion air in a multitude of burners arranged within the reformer furnace. According to the invention, the combustion air, before being introduced into the burners, is heated by means of at least one heat exchanger in indirect heat exchange with the hot flue gas to temperatures of at least 530° C. 1. A process for producing a pure hydrogen product gas by steam reforming of a feed gas containing hydrocarbons , comprising:(a) providing the feed gas comprising hydrocarbons,{'claim-text': ['(b1) a prereformer,', {'claim-text': ['(b21) a multitude of reformer tubes filled with steam reforming catalyst, wherein the reformer tubes have a feed gas inlet for a feed gas mixture on a first side of the reformer furnace and a product gas outlet for a crude synthesis gas on a second side of the reformer furnace, wherein the second side is opposite the first side, and further comprising', '(b22) a multitude of burners,'], '#text': '(b2) a steam reforming plant with a reformer furnace, comprising'}, '(b3) a CO conversion plant,', '(b4) a hydrogen purification plant,'], '#text': '(b) providing a hydrogen production plant comprising'}(c) adding steam to the feed gas to obtain a steam-feed gas mixture having an overall SIC ratio,(d) introducing the steam-feed gas mixture into the prereformer, prereforming the steam-feed gas mixture under prereforming conditions to give a prereformed feed gas comprising hydrogen, carbon oxides, methane and higher hydrocarbons, discharging the prereformed feed gas,(e) introducing the prereformed feed gas into the feed gas inlet of the reformer tubes of the steam reforming plant, ...

CONTINUOUS PRODUCTION OF METHYL PENTENONE USING CATION EXCHANGE RESIN IN A FIXED BED REACTOR

Provided herein is a method for producing methyl pentenone (MPO) in high yield in a continuous mode in a fixed bed reactor having a plurality of sidewall injecting ports by reacting excess methyl ethyl ketone (MEK) with acetaldehyde in presence of a cation exchange resin catalyst, wherein the acetaldehyde is injected from the plurality of sidewall injecting ports of the reactor. The method is also effective in reducing the complete consumption of the catalyst during the course of the reaction. 1. A method for producing methyl pentenone (MPO) in a continuous mode in high yield , the method comprising a reaction between methyl ethyl ketone (MEK) and acetaldehyde in presence of a heterogeneous catalyst in a fixed bed reactor having a plurality of sidewall injecting ports , wherein MEK is fed in a bed of the heterogeneous catalyst in the reactor and acetaldehyde is injected from the plurality of sidewall injecting ports and wherein the concentration of acetaldehyde to methyl ethyl ketone is from 1:3 to 1:18 (feed molar ratio).2. The method as claimed in claim 1 , wherein the heterogeneous catalyst is a cation exchange resin catalyst.3. The method as claimed in claim 2 , wherein the cation exchange resin catalyst is selected from the group consisting of Polystyrene sulphonated cation resin claim 2 , a Polymeric resin claim 2 , a solid catalyst supported on clay claim 2 , a solid acid catalyst supported on polymeric resin claim 2 , solid aluminophosphate claim 2 , Amberlyst-15 claim 2 , Amberlyst-35 claim 2 , Langson dry Lewatit K2620 catalyst claim 2 , Dry NKC claim 2 , Dry purolite claim 2 , Zinc acetate claim 2 , zinc acetate dehydrate claim 2 , and aluminium phosphate.4. The method as claimed in claim 1 , wherein the reaction takes place at a temperature of 343-363 K.5. The method as claimed in claim 1 , wherein the reaction takes place at a residence time of 295-345 min.6. The method as claimed in claim 1 , wherein injection of acetaldehyde from the plurality of ...

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

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 ...

ETHYLENE-TO-LIQUIDS SYSTEMS AND METHODS

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 ...

Continuous process for the preparation of thiocarboxylate silane

The invention is directed to a process for the preparation of thiocarboxylate silane comprising reacting an aqueous solution of a salt of a thiocarboxylic acid with a haloalkylalkoxysilane in the presence of a solid supported catalyst. The invention is also directed to a process for the preparation of an aqueous solution of a salt of a thiocarboxylic acid which comprises reacting an aqueous solution of a sulfide and/or hydrosulfide with a carboxylic acid halide and/or acid anhydride.

Method for Reducing Temperature Spread in Reformer

The invention is directed to a method for heating a process gas in a top or bottom fired reformer, a method for improving the temperature spread over a top or bottom fired reformer, and to a top or bottom fired reformer wherein these methods can applied. This can be achieved by the lane flow rate of at least one outer tube lane being different from the lane flow rate of at least one inner tube lane.

SHELL AND TUBE OXIDATION REACTOR WITH IMPROVED RESISTANCE TO FOULING

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 ...

USE OF TOP DIVIDING WALL IN ISOMERIZATION UNIT

The invention is directed to a combined naphtha hydrotreating (NHT) and isomerization process scheme, which includes dividing wall columns (DWC) that replace multiple distillation columns and allow optimized heat integration within the system. The disclosed design provides reductions in both capital and energy costs compared to conventional schemes. 1. An isomerization unit comprising: a first side configured as a stabilizer column; and', 'a second side configured as naphtha splitter column;, 'a first dividing wall column comprising a first side configured as a depentanizer column; and', 'a second side configured as a deisohexanizer column., 'a second dividing wall column;'}2. The isomerization unit of claim 1 , further comprising:a deisopentanizer column coupled to the first dividing wall column configured to receive a light naphtha overhead stream from the second side of the first dividing wall column;an isomerization reactor coupled to the deisopentanizer column and configured to receive a bottoms stream from the deisopentanizer column; anda stabilizer column coupled to the isomerization reactor and configured to receive a stream comprising unstable isomerate from the isomerization reactor and to feed stable isomerate to the second dividing wall column.3. The isomerization unit of claim 1 , wherein the first dividing wall column comprises a first condenser and a second condenser claim 1 , the first condenser configured to reflux a portion of an overheads stream from the first side of the first dividing wall column to an overheads section of the first side of the first dividing wall column claim 1 , and the second condenser configured to reflux a portion of an overheads stream from the second side of the first dividing wall column to an overheads section of the second side of the first dividing wall column.4. The isomerization unit of claim 1 , wherein the second dividing wall column comprises a first condenser and a second condenser claim 1 , the first condenser ...

PROCESS AND APPARATUS FOR STEAM REFORMING

A process and an apparatus for generating a hydrogen- and/or carbon monoxide-comprising gas product, wherein a hydrocarbon feed formed from a hydrocarbons-containing starting material is supplied together with superheated steam to a steam reforming proceeding at elevated pressure to obtain a hydrogen- and carbon monoxide-containing crude synthesis gas from which the gas product is derived are disclosed. The boiler feed water is supplied at a pressure higher than its critical pressure with heat to obtain supercritical water of which subsequently at least a portion is employed as propelling medium in a steam jet ejector by means of which the hydrocarbon feed and/or a substance employed for the formation thereof are compressed. 1. A process for generating a hydrogen- and/or carbon monoxide-comprising gas product , wherein a hydrocarbon feed formed from a hydrocarbons-containing starting material is supplied together with superheated steam to a steam reforming proceeding at elevated pressure to obtain a hydrogen- and carbon monoxide-containing crude synthesis gas from which the gas product is derived , characterized in that boiler feed water is supplied at a pressure higher than its critical pressure with heat to obtain supercritical water of which subsequently at least a portion is employed as propelling medium in a steam jet ejector by means of which the hydrocarbon feed and/or a substance employed for the formation thereof are compressed.2. The process according to claim 1 , characterized in that during compression of the hydrocarbon feed in the steam jet ejector a substance mixture is formed which meets the requirements of steam reforming on account of its composition and/or has a pressure allowing supply to the steam reforming without further compression.3. The process according to claim 1 , characterized in that the boiler feed water is heated in indirect heat exchange against flue gas from which heat is removed beforehand for the steam reforming.4. The process ...

Process

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

METHOD FOR PRODUCING ACROLEIN AND/OR ACRYLIC ACID FROM GLYCEROL

The invention relates to the production of acrolein and/or acrylic acid from glycerol, and more particularly to a method for continuous production of a stream comprising acrolein by dehydration of glycerol, comprising cycles of reaction and regeneration of a dehydration catalyst. 2. The installation as claimed in comprising a single device for withdrawing gas mixture.3. The installation as claimed in claim 2 , wherein each of the reactor zones has fluidic connection to a device for withdrawing gas mixture.410204020. The installation as claimed in claim 1 , wherein the reactor R is a multiple-tube reactor comprising tubes () fixed by tube plates () and comprising at least one plate () positioned between the reactor dome and the tube plates (). This application is a divisional application of U.S. Ser. No. 14/395,128, filed Oct. 17, 2014 which is a national stage application under 35 U.S.C. §371 of PCT/FR2013/050730, filed Apr. 3, 2013, which claims benefit to French patent application FR 1253557, filed Apr. 18, 2012, Patented; Patent No. FR 2989684 B1 on Oct. 31, 2014.The work leading to the present invention received financial support from the seventh framework program of the European Community FP7/2007-2013 based on subsidy agreement No. 228867.The present invention relates to the production of acrolein and/or acrylic acid from glycerol, and relates more particularly to a method for continuous production of a stream comprising acrolein by dehydration of glycerol, comprising cycles of reaction and regeneration of the dehydration catalyst.It also relates to a plant for producing this continuous stream of acrolein efficiently in terms of energy consumption and productivity, without high capital costs and in good conditions of safety.TECHNOLOGICAL BACKGROUNDResources of fossil origin, such as petroleum cuts, for the chemical industry will be exhausted some decades from now. That is why, for some years, industrial corporations have oriented their research and development ...

UREA REACTOR TRAY, REACTOR, AND PRODUCTION PROCESS

A urea reactor tray having a base plate; and a number or quantity of hollow cup-shaped members, which project vertically from the base plate along respective substantially parallel axes perpendicular to the base plate, and have respective substantially concave inner cavities communicating with respective openings formed in the base plate; the tray having a number or quantity of first cup-shaped members, each of which extends axially between an open top end having the opening, and a closed bottom end, and has a lateral wall with through holes substantially crosswise to the axis, and a bottom wall which closes the closed bottom end and has no holes. 123-. (canceled)24. A urea reactor tray comprising:a base plate; and a lateral wall which defines a plurality of through circulation holes substantially crosswise to the axis of said first cup-shaped member, said circulation holes including a plurality of first circulation holes predominantly configured for throughflow of a gaseous phase, and a plurality of second circulation holes predominantly configured for throughflow of a liquid phase, the plurality of first circulation holes being located closer to the open top end of the first cup-shaped member than the plurality of second circulation holes, and the plurality of first circulation holes being smaller than the plurality of second circulation holes; and', 'a bottom wall attached to the lateral wall and which does not define any circulation holes., 'a first cup-shaped member which projects in a downward direction from a bottom face of the base plate along an axis transverse to the base plate, and which defines a substantially concave inner cavity communicating with an opening defined by the base plate, and which extends axially between an open top end defined by the opening defined by the base plate and a closed bottom end, said first cup-shaped member including25. The urea reactor tray of claim 24 , wherein the plurality of first circulation holes are located in a top ...

Ceramic oxygen transport membrane array reactor and reforming method

A commercially viable modular ceramic oxygen transport membrane reforming reactor for producing a synthesis gas that improves the thermal coupling of reactively-driven oxygen transport membrane tubes and catalyst reforming tubes required to efficiently and effectively produce synthesis gas.

EXHAUST SYSTEM FOR A STEAM REFORMER AND BEARING THEREFOR

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

PROCESS FOR OPERATING A HIGHLY PRODUCTIVE TUBULAR REACTOR

The present technology is directed to processes for conversion of synthesis gas in a tubular reactor to produce a synthetic product that utilizes high activity carbon monoxide hydrogenation catalysts and a heat transfer structure that surprisingly provides for higher per pass conversion with high selectivity for the desired synthetic product without thermal runaway. 114-. (canceled)15. A tubular reactor comprising:one or more reactor tubes including a tube inlet;a tube outlet located downstream of the tube inlet;an inner tube wall defining an interior of the one or more reactor tubes;an outer tube wall defining an exterior of the one or more reactor tubes;a volume of a catalyst provided in at least one section within the interior of the one or more reactor tubes; anda heat transfer structure provided within the interior of the one or more reactor tubes, the heat transfer structure being in conductive thermal contact with a portion of the catalyst and in at least partial conductive thermal contact with the inner tube wall throughout a surface area of the inner tube wall in the at least one section containing the catalyst;a reactor inlet in fluid communication with the one or more reactor tubes; anda reactor outlet located downstream of the reactor inlet and in fluid communication with the one or more reactor tubes,wherein the tubular reactor satisfies at least one of the following conditions:{'sub': eff', 'cat, 'a ratio of an effective thermal conductivity of the heat transfer structure and the catalyst with the inner tube wall to a thermal conductivity of the catalyst (k/k) is at least 50:1, or'}{'sup': 2', '3', '2', '3, 'a total combined surf ace area of the heat transfer structure and inner tube wall containing the catalyst per volume of the catalyst (the “SA/V”) is about 500 m/mto about 4000 m/m.'}16. The tubular reactor of claim 15 , wherein at least about 5% of the surface area of the inner tube wall containing the carbon monoxide hydrogenation catalyst is in ...

Sabatier process and apparatus for controlling exothermic reaction

A Sabatier process involving contacting carbon dioxide and hydrogen in a first reaction zone with a first catalyst bed at a temperature greater than a first designated temperature; feeding the effluent from the first reaction zone into a second reaction zone, and contacting the effluent with a second catalyst bed at a temperature equal to or less than a second designated temperature, so as to produce a product stream comprising water and methane. The first and second catalyst beds each individually comprise an ultra-short-channel-length metal substrate. An apparatus for controlling temperature in an exothermic reaction, such as the Sabatier reaction, is disclosed.

INDUCTIVE HEATING OF A STEAM REFORMER FURNACE

A furnace and method for steam reforming of a hydrocarbon-containing feed stream, which particularly comprises methane, with: a combustion chamber, at least one reactor tube, which in portions extends in the combustion chamber and is designed for receiving a catalyst and for passing the feed stream through, and at least one burner, which is designed to burn a fuel in the combustion chamber for heating the at least one reactor tube is disclosed. It is provided that the at least one reactor tube has a portion of tube running above and outside the combustion chamber, an inductor which is designed for inductively heating the portion of tube being arranged on the portion of tube. 2. The furnace according to claim 1 , characterized in that the inductor has a coil claim 1 , which is wound around the said portion of tube.3. The furnace according to claim 1 , characterized in that the said portion of tube is designed to receive the catalyst claim 1 , or in that the portion of tube is filled with the catalyst.5. The method according to claim 4 , characterized in that the at least one reactor tube has a portion of tube running above and outside the combustion chamber.6. The method according to claim 4 , characterized in that the inductor has a coil claim 4 , which is wound around the said portion of tube.7. The method according to claim 4 , characterized in that the said portion of tube is designed to receive the catalyst claim 4 , or in that the portion of tube is filled with the catalyst. This application claims priority from German Patent Application DE 102015013071.4 filed on Oct. 8, 2015.The invention relates to a furnace, for example for carrying out steam reforming of a hydrocarbon-containing feed gas stream, and also to a corresponding method.Steam reforming, in particular of methane, is a widely used, established technology for producing synthesis gas. Steam reforming is also currently preferred over other methods, in particular for producing hydrogen.Steam reforming ...

CATALYST LOADING TOOL

There is provided a loading tray for loading particulate material into a catalytic reactor comprising an upper tubesheet and an array of reaction tubes extending downward from the tubesheet; wherein the loading tray comprises: a loading template comprising one or more loading openings; one or more supports for spacing the loading template above the tube-sheet to form a volume between the loading template and the upper tube-sheet; and a vacuum outlet for application of suction to the volume between the loading template and the upper tubesheet. 1. A loading tray for loading particulate material into a catalytic reactor comprising an upper tubesheet and an array of reaction tubes extending downward from the tubesheet;wherein the loading tray comprises:a loading template comprising one or more loading openings;one or more supports for spacing the loading template above the tubesheet to form a volume between the loading template and the upper tubesheet; anda vacuum outlet for application of suction to the volume between the loading template and the upper tubesheet.2. A catalyst loading tray according to which claim 1 , when placed above the tubesheet for catalyst loading use claim 1 , substantially closes the volume between the loading template and the upper tubesheet for airflow claim 1 , except for the catalyst loading openings claim 1 , reactor tube openings in the tubesheet claim 1 , and the vacuum outlet.3. A catalyst loading tray according to wherein the catalyst loading template is elongate.4. A catalyst loading tray according to wherein the catalyst loading openings are disposed in a single row.5. A catalyst loading tray according to wherein the catalyst loading template comprises from 2 to 40 catalyst loading openings.6. A catalyst loading tray according to wherein at least one of the catalyst loading openings is provided with a filler sleeve claim 1 , the filler sleeve comprising:an upper portion having a catalyst loading orifice and an engagement member;a ...

PROCESS FOR THE EPOXIDATION OF PROPENE

During start-up of a continuous epoxidation of propene with hydrogen peroxide in a methanol solvent with a shaped titanium silicalite catalyst in a tube bundle reactor with a cooling jacket, cooling medium is fed at the rate for full load of the reactor with a constant entry temperature of from 20° C. to 50° C., methanol solvent is fed at a rate of from 50 to 100% for full load of the reactor, hydrogen peroxide is fed at a rate that starts with no more than 10% of the rate for full load and is increased continuously or stepwise to maintain a maximum temperature in the fixed bed of no more than 60° C. and a difference between the maximum temperature in the fixed bed and the cooling medium entry temperature of no more than 20° C., and propene is fed at a rate of from 20 to 100% of the rate for full load, increasing the feeding rate when the molar ratio of propene to hydrogen peroxide reaches the molar ratio for full load. 16-. (canceled)7. A process for the epoxidation of propene by continuously reacting propene with hydrogen peroxide in a methanol solvent and in the presence of a shaped titanium silicalite catalyst; wherein:a) the reaction is in a tube bundle reactor comprising a multitude of parallel reaction tubes and a cooling jacket enclosing the reaction tubes;b) the catalyst is arranged as a fixed bed in the reaction tubes;c) the molar ratio of propene to hydrogen peroxide is in the range of from 2.5:1 to 6:1 at full load of the reactor; i) cooling medium is fed to the cooling jacket at a constant rate for full load of the reactor, the entry temperature of the cooling medium being kept essentially constant at a value in the range of from 20° C. to 50° C.;', 'ii) methanol solvent is fed to the reaction tubes at a feeding rate of from 50 to 100% of a feeding rate for full load of the reactor;', 'iii) hydrogen peroxide is fed to the reaction tubes at a feeding rate that starts with no more than 10% of a feeding rate for full load of the reactor and is increased ...

Hydrogen Generators

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.

Organic waste disposal plant and method

The treatment plant comprises: a reactor for the sublimation of organic material in order to obtain a syngas; a filtration assembly for filtering the syngas in order to obtain a filtered gas, and a motor-generator assembly for producing electrical energy by means of the combustion of the filtered gas and thereby producing burnt gas; characterized in that said plant also comprises a methanation assembly, comprising: a catalyst that can extract carbon dioxide and nitrogen from the burnt gas; an electrolyzer that can separate water into oxygen and hydrogen by means of electrolysis; and a methanation reactor, which can produce methane by means of the Sabatier reaction using hydrogen and carbon dioxide originating from the electrolyzer and from the catalyst; the catalyst comprising a catalysis layer consisting of stone wool and nickel nanospheres, a plurality of steel microtubes containing copper microfilaments, and a system for controlling the reaction conditions.

CATALYST FOR C2 OXYGENATE SYNTHESIS, DEVICE FOR MANUFACTURING C2 OXYGENATE, AND METHOD FOR MANUFACTURING C2 OXYGENATE

The present invention relates to a catalyst for C2 oxygenate synthesis in which a hydrogenated active metal is supported on a porous carrier to synthesize a C2 oxygenate from a mixed gas containing hydrogen and carbon monoxide, wherein the porous carrier has an average pore diameter of 0.1 to 20 nm. 1. A catalyst for C2 oxygenate synthesis in which a hydrogenated active metal is supported on a porous carrier to synthesize a C2 oxygenate from a mixed gas containing hydrogen and carbon monoxide , wherein the porous carrier has an average pore diameter of 0.1 to 20 nm.2. The catalyst for C2 oxygenate synthesis according to claim 1 , wherein the average pore diameter is 0.1 to 8 nm.3. The catalyst for C2 oxygenate synthesis according to claim 1 , wherein the average pore diameter is 2 to 20 nm.4. The catalyst for C2 oxygenate synthesis according to claim 1 , wherein the hydrogenated active metal is one or more substances selected from the group consisting of alkali metals and elements belonging to groups 7 to 10 of the periodic table.5. A device for manufacturing a C2 oxygenate claim 1 , the device including a reaction tube packed with the catalyst for C2 oxygenate synthesis according to claim 1 , a supply unit for supplying the mixed gas into the reaction tube claim 1 , and a discharge unit for discharging the product from the reaction tube.64. A method for manufacturing a C2 oxygenate claim 1 , wherein the C2 oxygenate is obtained by bringing a mixed gas containing hydrogen and carbon monoxide into contact with the catalyst for C2 oxygenate synthesis according to .7. The catalyst for C2 oxygenate synthesis according to claim 2 , wherein the hydrogenated active metal is one or more substances selected from the group consisting of alkali metals and elements belonging to groups 7 to 10 of the periodic table.8. The catalyst for C2 oxygenate synthesis according to claim 3 , wherein the hydrogenated active metal is one or more substances selected from the group consisting ...

A catalyst for converting synthesis gas to alcohols

A catalyst for converting a synthesis gas, said catalyst comprising a first catalyst component and a second catalyst component, wherein the first catalyst component comprises, supported on a first porous oxidic substrate, Rh, Mn, an alkali metal M and Fe, and wherein the second catalyst component comprises, supported on a second porous oxidic support material, Cu and a transition metal other than Cu.

ETHYLENE-TO-LIQUIDS SYSTEMS AND METHODS

The present disclosure provides petrochemical processing methods and systems, including ethylene conversion processes and systems, for the production of higher hydrocarbon compositions, for example liquid hydrocarbon compounds, with reduced amount of unsaturated hydrocarbons. 1. A method for generating hydrocarbon compounds with eight or more carbon atoms (C compounds) , comprising:{'sub': 2+', '2+', '3+, '(a) directing a feed stream comprising unsaturated C hydrocarbon compounds into an oligomerization unit that permits at least a portion of said unsaturated C hydrocarbon compounds to react in an oligomerization process to yield an effluent comprising unsaturated C hydrocarbon compounds; and'}{'sub': 3+', '8+, '(b) directing at least a portion of said effluent from said oligomerization unit and a stream comprising isoparaffins into an alkylation unit downstream of and separate from said oligomerization unit, which alkylation unit permits at least a portion of said unsaturated C hydrocarbon compounds and said isoparaffins to react in an alkylation process to yield a product stream comprising said C compounds.'}2. The method of claim 1 , further comprising: directing methane and an oxidizing agent into an oxidative coupling of methane (OCM) unit that facilitates an OCM reaction to generate an OCM product stream comprising ethylene (CH) claim 1 , and wherein at least a portion of said feed stream is provided by the OCM product stream.3. The method of claim 1 , wherein the oligomerization unit comprises a dimerization unit and the oligomerization process comprises a dimerization process claim 1 , and wherein the dimerization process operates at a temperature of 20° C. to 200° C. and a pressure of 100 psia to 400 psia.4. The method of claim 1 , wherein the product stream is an alkylate stream comprising an alkylate product comprising saturated C hydrocarbon compounds claim 1 , isomers thereof claim 1 , or both saturated C hydrocarbon compounds and isomers thereof.5. The ...