СПОСОБ ПОЛУЧЕНИЯ СИНТЕЗ-ГАЗА ПУТЕМ КОНВЕРСИИ С ВОДЯНЫМ ПАРОМ В РЕАКТОРЕ-ТЕПЛООБМЕННИКЕ

Изобретение относится к области химии. Синтез-газа получают из общей загрузки, содержащей углеводороды и возможно рециркулируемые соединения. Общая загрузка содержит первую загрузку, вторую загрузку и третью загрузку. Поток, содержащий первую загрузку с добавлением водяного пара, подвергают конверсии с водяным паром для получения по меньшей мере одной фракции синтез-газа в по меньшей мере одном мультитрубчатом реакторе-теплообменнике, имеющем множество реакционных труб, содержащих катализатор, и камеру, в которой находятся эти трубы. Первая загрузка с добавлением водяного пара циркулирует внутри множества труб в одном направлении. Реакционные трубы нагревают путем циркуляции в камере текучего теплоносителя снаружи по отношению к трубам, локально в режиме перекрестного потока, но в целом в режиме противотока всей первой загрузки, в котором текучий теплоноситель содержит по меньшей мере первый поток газа частичного или полного горения второй загрузки, который подвергают циркуляции в реакторе-теплообменнике ...

СПОСОБ ОБЕЗВРЕЖИВАНИЯ ОПАСНЫХ ИЛИ ОБЛАДАЮЩИХ ВЫСОКИМ ЭНЕРГЕТИЧЕСКИМ ПОТЕНЦИАЛОМ МАТЕРИАЛОВ, А ТАКЖЕ УСТРОЙСТВО ДЛЯ ОСУЩЕСТВЛЕНИЯ ЭТОГО СПОСОБА

Изобретение относится к обезвреживанию опасных или обладающих высоким энергетическим потенциалом материалов, а именно взрывчатых веществ, боеприпасов, а также других опасных веществ, которые с использованием определенных химикалий необходимо с помощью как экзотермических, так и эндотермических реакций превращать в целевые безопасные конечные продукты. Способ включает подачу сыпучего материала и обезвреживаемых материалов во внутреннее пространство прочного корпуса, в котором в контролируемых условиях инициируют реакцию этих обезвреживаемых материалов с образованием безопасных конечных продуктов. Из обезвреживаемых материалов и сыпучих материалов в прочном корпусе образуют перемещающийся сверху вниз подвижный слой, в котором подача сыпучего материала и обезвреживаемых материалов с одной стороны и выход смеси сыпучего материала с образовавшимися в результате реакции безопасными конечными продуктами с другой стороны находятся в динамическом равновесии, при этом реакцию инициируют внутри этого ...

ПРОТОЧНЫЙ РЕАКТОР С РАДИАЛЬНЫМ ПОТОКОМ И СПОСОБ ОБРАБОТКИ ЖИДКОГО ПОТОКА РЕАГЕНТОВ

Предложенный проточный реактор относится к химической промышленности и применяется для проведения каталитических процессов переработки углеводородов. Реактор снабжен несколькими кольцевыми зонами. Первая кольцевая зона с первым слоем катализатора расположена во внутреннем пространстве реактора и выполнена ограниченной концентрическими внутренней и внешней стенками первого слоя катализатора. Вторая кольцевая зона расположена радиально окружающей первую кольцевую зону. Реактор содержит теплообменные трубы, которые установлены в центральной зоне реактора, либо во второй кольцевой зоне, или в обеих зонах. Внутреннее пространство реактора выполнено с возможностью направления входящего внутрь реактора потока в радиальном направлении к первой кольцевой зоне и через первый слой катализатора во вторую кольцевую зону, а к выходному отверстию реактора - в осевом направлении. Предложен также способ использования данного аппарата для обработки жидкого потока реагентов. Данное изобретение позволяет эффективно ...

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 ...

УСТАНОВКА ДЛЯ ПОЛУЧЕНИЯ (МЕТ)АКРИЛОВОЙ КИСЛОТЫ И СПОСОБ ПОЛУЧЕНИЯ (МЕТ)АКРИЛОВОЙ КИСЛОТЫ

FIELD: chemistry. ^ SUBSTANCE: invention concerns aggregate for (met)acrylic acid obtainment, including: reactor for (met)acrylic acid obtainment by catalytic gas phase oxidation reaction of one, two or more source compounds including propane, propylene, isobutylene and (met)acrolein, in gas mix of source substances including one, two or more source compounds including propane, propylene, isobutylene and (met)acrolein, and oxygen; heat exchanger connected to reactor and intended for cooling of reaction gas mix including obtained (met)acrylic acid; and absorption column connected to heat exchanger and intended for contact absorbing fluid with reaction gas mix for (met)acrylic acid absorption, so that (met)acrylic acid is absorbed from reaction gas mix by absorbing fluid. Additionally the aggregate includes: bypass pipe connecting reactor and absorption column without the use of intermediary heat exchanger; and device for flow rate adjustment in reaction gas flow passing through bypass pipe in order to maintain almost constant flow rate of gas mix feed of source materials to reactor or almost constant pressure of gas mix of source materials at the reactor inlet. Also invention concerns improved method of (met)acrylic acid obtainment by extraction of (met)acrylic acid absorbed by absorbing fluid. ^ EFFECT: heat power tapping from reaction gas mix, stable and continuous process even in case of heat exchanger intended for heat power extraction is blocked. ^ 2 cl, 3 dwg, 1 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2 355 673 (13) C2 (51) МПК C07C C07C C07C C07C C07C C07C 51/215 51/235 51/25 51/42 57/05 57/055 (2006.01) (2006.01) (2006.01) (2006.01) (2006.01) (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ, ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (21), (22) Заявка: 2006147257/04, 07.09.2004 (24) Дата начала отсчета срока действия патента: 07.09.2004 (73) Патентообладатель(и): МИЦУБИСИ КЕМИКАЛ КОРПОРЕЙШН (JP) (43) Дата публикации заявки: 20. ...

СПОСОБ И УСТРОЙСТВО ДЛЯ ПОЛУЧЕНИЯ ФОСГЕНА

Изобретение относится к технологии получения фосгена. Фосген получают путем взаимодействия хлора и монооксида углерода в присутствии активированного угля в качестве катализатора в кожухотрубном реакторе, содержащем несколько реакционных трубок и окружающее их охлаждающее пространство, при этом реакционные трубки подвергают наружному испарительному охлаждению посредством охлаждающего пространства с водой и эксплуатируют под давлением, превышающим давление в охлаждающем пространстве. Монооксид углерода используют в молярном избытке по отношению к используемому количеству хлора, составляющем от 2 до 20%, а абсолютное давление в охлаждающем пространстве составляет от 0,1 до 0,8 бар. Кроме того, описывается устройство для получения фосгена, состоящее из кожухотрубного реактора 20, 60, который включает в себя несколько расположенных параллельно друг другу реакционных трубок 21, 61, окружающее реакционные трубки 21, 61 охлаждающее пространство 27, 67 для воды, по меньшей мере, с одним входным ...

КОНВЕРТЕРНАЯ СИСТЕМА С МАКСИМАЛЬНОЙ СКОРОСТЬЮ РЕАКЦИИ ДЛЯ ЭКЗОТЕРМИЧЕСКИХ РЕАКЦИЙ

Способ конверсии для синтеза аммиака включает: введение газообразного, обогащенного реагентами потока, содержащего смесь водорода и азота, при температуре подачи в теплообменный канал теплообменной реакционной зоны для подогрева обогащенного реагентами потока до температуры на входе, где теплообменная реакционная зона содержит кожухотрубный теплообменник, теплообменный канал представляет собой межтрубный канал через теплообменник, и реакционный канал содержит множество трубок, содержащих в себе катализатор, введение предварительно подогретого обогащенного реагентами потока при температуре на входе в противоточный, содержащий катализатор реакционный канал для экзотермической конверсии газа-реагента в получаемый газ с образованием обогащенной продуктом смеси из газа-реагента и получаемых газов, где реакционный канал содержит множество последовательных чередующихся, содержащих катализатор зон и зон, ограничивающих реакцию, косвенную передачу тепла от реакционного канала к теплообменному каналу ...

ВЕРТИКАЛЬНЫЙ АММИАЧНЫЙ КОНВЕРТЕР С РАЗДЕЛЬНЫМ ПОТОКОМ

Изобретение может быть использовано в химической промышленности. Вертикальный аммиачный конвертер с неподвижным слоем, в котором каталитическая зона неподвижного слоя расположена в двух механически разделенных объемах катализатора. В реакторе созданы два газовых потока, которые работают параллельно. Каждая каталитическая зона неподвижного слоя в настоящем изобретении может содержать катализатор в кольцевом пространстве, образованном между двумя концентрическими кожухами, размещенными вокруг кожухотрубного теплообменника. Трубы и трубопроводы расположены в слоях катализатора, кольцевые каналы вокруг слоя катализатора осуществляют параллельное разделение газового потока. Предложенное изобретение позволяет повысить эффективность аммиачного конвертера. 2 н. и 13 з.п. ф-лы, 3 ил.

СПОСОБ ПОЛУЧЕНИЯ ГРАНУЛ СЛОЖНОГО ПОЛИЭФИРА С НИЗКОЙ СТЕПЕНЬЮ ГИДРОЛИЗА ИЗ ВЫСОКОВЯЗКИХ РАСПЛАВОВ СЛОЖНОГО ПОЛИЭФИРА И УСТРОЙСТВО ДЛЯ ПОЛУЧЕНИЯ ГРАНУЛ СЛОЖНОГО ПОЛИЭФИРА

Изобретение относится к способу прямого получения гранулята полиэтилентерефталата с низкой степенью гидролиза из высоковязкого расплава полиэтилентерефталата и устройство для прямого получения гранулята полиэтилентерефталата с низкой степенью гидролиза. Способ прямого получения гранулята полиэтилентерефталата со степенью полимеризации СП от 132 до 165, при котором расплав после осуществления способа разрезания в горячем состоянии подвергают предварительной сушке и сушке/дегазации. Стадию разрезания в способе разрезания в горячем состоянии осуществляют при температурах воды от 70 до 95°С и при поддержании соотношения жидкости к твердому веществу - соотношения воды к гранулам/грануляту от 8:1 до 12:1, причем жидкость полностью удерживают до поступления в предварительную сушилку, а циркулирующую воду в предварительной сушилке отделяют в течение менее 10 с. Кроме того, изобретение относится к грануляту полиэтилентерефталата, полученному указанным способом, который имеет степень поликонденсации ...

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-ТЕПЛООБМЕННИК С БАЙОНЕТНЫМИ ТРУБАМИ, КОНСТРУКЦИЯ КОТОРОГО ПОЗВОЛЯЕТ ЕМУ РАБОТАТЬ С ПЕРЕПАДАМИ ДАВЛЕНИЯ ПОРЯДКА 100 БАР МЕЖДУ ТРУБОЙ И КАЛАНДРОМ

В изобретении представлен предназначенный для выполнения эндотермических реакций реактор-теплообменник, в состав которого входит каландр, внутри которого циркулирует текучий теплоноситель (11). Внутри каландра расположено множество параллельных труб (4). Внутри труб циркулирует среда, участвующая в технологическом процессе (5, 6). Трубы относятся к типу байонетных. Реактор не имеет трубчатой пластины. Техническим результатом изобретения является возможность работы реактора с перепадом давлений во внутритрубном пространстве и в каландровом пространстве, достигающим 100 бар. 5 н. и 4 з.п. ф-лы, 4 ил., 1 табл., 1 пр.

ГЕНЕРАТОР ВОДОРОДА И ИСТОЧНИК ЭНЕРГИИ С ТОПЛИВНЫМ ЭЛЕМЕНТОМ

Изобретения относятся к области химии. Генератор водорода включает в себя блок 7 испарения воды, в который подают сырьевой газ и воду, слой 9 катализатора риформинга, в который подают газовую смесь из блока 7 испарения воды, горелку 4, проток 16 для отходящего газа горения, который обеспечен на внутренней стороне блока 7 испарения воды, слой 10 катализатора конверсии, который располагают на внешней стороне блока 7 испарения воды, к которому подают реформируемый газ. Блок 7 испарения воды включает в себя двойные цилиндры 100 и 101 и спиральный круглый стержень, зажатый между цилиндрами 100 и 101. Нижнюю часть блока испарения воды выполняют с возможностью такой, что в величине теплообмена между протоком для отходящего газа горения и блоком испарения воды величина теплообмена между протоком для отходящего газа горения и нижней частью блока испарения воды становится больше, чем величина теплообмена между протоком для отходящего газа горения и частью блока испарения воды за исключением нижней ...

СПОСОБ ПОЛУЧЕНИЯ ГРАНУЛ СЛОЖНОГО ПОЛИЭФИРА С НИЗКОЙ СТЕПЕНЬЮ ГИДРОЛИЗА ИЗ ВЫСОКОВЯЗКИХ РАСПЛАВОВ СЛОЖНОГО ПОЛИЭФИРА И УСТРОЙСТВО ДЛЯ ПОЛУЧЕНИЯ ГРАНУЛ СЛОЖНОГО ПОЛИЭФИРА

... 1. Способ прямого получения гранулята сложного полиэфира с низкой степенью гидролиза из высоковязкого расплава сложного полиэфира со степенью полимеризации (СП) от 132 до 165, при котором расплав после осуществления способа разрезания в горячем состоянии подвергают предварительной сушке и сушке/дегазации, отличающийся тем, что ! стадию разрезания в способе разрезания в горячем состоянии осуществляют при температурах воды от 70 до 95°С и при поддержании соотношения жидкости к твердому веществу (соотношения воды к гранулам/грануляту) от 8:1 до 12:1, причем жидкость полностью удерживают до поступления в предварительную сушилку, а циркулирующую воду в предварительной сушилке отделяют в течение менее 10 с. ! 2. Способ по п.1, отличающийся тем, что 99% циркулирующей воды отделяют в предварительной сушилке, при этом в качестве предварительной сушилки предпочтительно применяют перемешивающую центрифугу, корпус которой выполнен в виде расширяющегося от основания вверх конуса или цилиндрических ступеней ...

СПОСОБ ВВЕДЕНИЯ В ЭКСПЛУАТАЦИЮ ПАРЦИАЛЬНОГО ГАЗОФАЗНОГО ОКИСЛЕНИЯ АКРОЛЕИНА В АКРИЛОВУЮ КИСЛОТУ ИЛИ МЕТАРОЛЕИНА В МЕТАКРИЛОВУЮ КИСЛОТУ НА ГЕТЕРОГЕННОМ КАТАЛИЗАТОРЕ

... 1. Способ введения в эксплуатацию газофазного парциального окисления на гетерогенном катализаторе акролеина в акриловую кислоту и метакролеина в метакриловую кислоту на фиксированном слое катализатора, который находится в кожухотрубном реакторе в реакционных трубках вертикально расположенного пучка реакционных трубок, заключенного в кожух реактора, когда оба конца каждой из реакционных трубок открыты и каждая реакционная трубка своим верхним концом плотно входит в сквозное отверстие плотно встроенной в верхнюю часть кожуха реактора верхней трубной решетки, а своим нижним концом плотно входит в сквозное отверстие плотно встроенной в нижнюю часть кожуха реактора нижней трубной решетки, при этом внешняя поверхность реакционных трубок, верхняя и нижняя трубная решетки, а также кожух реактора вместе ограничивают пространство, окружающее реакционные трубки, при этом также каждая из двух трубных решеток закрыта крышкой реактора с не менее чем одним отверстием, когда для введения в эксплуатацию ...

СПОСОБ КАТАЛИТИЧЕСКОГО ОКИСЛЕНИЯ В ПАРОВОЙ ФАЗЕ

... 1. Способ каталитического окисления в паровой фазе для получения газообразного реакционного продукта при использовании многотрубного реактора с неподвижным слоем теплообменного типа, образованного множеством реакционных труб и подачей исходного газообразного материала внутрь реакционных труб, набитых катализатором, при котором осуществляют регулирование потерь давления соответствующих реакционных труб таким образом, что потери давления соответствующих реакционных труб после набивки катализатора находятся в пределах ±20% от средней потери давления реакционных труб при набивке инертного вещества во впускную часть исходного газообразного материала реакционных труб или удалении набитого катализатора и повторной набивке катализатора для реакционной трубы, имеющей потерю давления меньше средней потери давления реакционных труб; и удалении набитого катализатора и повторной набивке катализатора для реакционной трубы, имеющей потерю давления больше средней потери давления реакционных труб. 2. Способ ...

РЕАКТОР-ТЕПЛООБМЕННИК С БАЙОНЕТНЫМИ ТРУБАМИ, КОНСТРУКЦИЯ КОТОРОГО ПОЗВОЛЯЕТ ЕМУ РАБОТАТЬ С ПЕРЕПАДАМИ ДАВЛЕНИЯ ПОРЯДКА 100 БАР МЕЖДУ ТРУБОЙ И КАЛАНДРОМ

... 1. Реактор-теплообменник состоит из закрытого сверху колпаком, а снизу днищем каландра цилиндрической формы, внутри которого циркулирует текучий теплоноситель, причем: указанный каландр содержит внутри себя множество параллельных труб, оси которых ориентированы практически в вертикальном направлении, внутри которых циркулирует среда, участвующая в технологическом процессе; причем указанные трубы относятся к типу байонетных и плотность их установки находится в диапазоне от 2 и 12 штук на м2 сечения реактора; интервал установки байонетных труб, или их межосевое расстояние превышает по величине в 2-5 раз внутренний диаметр наружной трубы (6); причем входной и выходной торцы каждой байонетной трубы выходят за пределы реактора; текучий теплоноситель получается путем сжигания топлива непосредственно в самом рассматриваемом аппарате, в горелках (8) удлиненной формы, устанавливаемых с образованием трехстороннего шага в промежутках между байонетными трубами; межосевое расстояние установки горелок ...

РЕАКТОР РИФОРМИНГА С НИЗКИМ ПЕРЕПАДОМ ДАВЛЕНИЯ

... 1. Теплообменник риформинга синтез-газа, содержащий: !сосуд, содержащий удлиненную оболочку, имеющую относительно высокотемпературный и относительно низкотемпературный концы; ! впуск текучей среды межтрубного пространства, смежный с высокотемпературным концом, для приема порции горячего газа; ! впуск текучей среды трубного пространства, смежный с низкотемпературным концом для приема порции газового реагента; ! выпуск текучей среды межтрубного пространства, флюидно изолированный от впуска текучей среды трубного пространства посредством трубной решетки, смежного с низкотемпературным концом, для выпуска охлажденного газа; ! трубный пучок, содержащий множество труб, одну или несколько продольно-разнесенных поперечных кольцевых перегородок, и одну или несколько продольно-разнесенных трубных направляющих, причем трубы имеют впускной конец, прикрепленный к трубной решетке, для приема порции смеси, и выпускной конец, смежный с впуском текучей среды межтрубного пространства, для выпуска получаемого ...

ТРУБЧАТЫЙ ТЕПЛООБМЕННЫЙ УЗЕЛ ДЛЯ ИСПОЛЬЗОВАНИЯ ВНУТРИ ТЕПЛООБМЕННИКОВ ИЛИ РЕАКТОРОВ

КОНВЕРТЕРНАЯ СИСТЕМА С МАКСИМАЛЬНОЙ СКОРОСТЬЮ РЕАКЦИИ ДЛЯ ЭКЗОТЕРМИЧЕСКИХ РЕАКЦИЙ

... 1. Способ конверсии для синтеза аммиака, включающий введение газообразного, обогащенного реагентами потока при температуре подачи в теплообменный канал теплообменной реакционной зоны для подогрева обогащенного реагентами потока до температуры на входе, введение предварительно подогретого обогащенного реагентами потока при температуре на входе в противоточный, содержащий катализатор реакционный канал для экзотермической конверсии газа-реагента в получаемый газ с образованием обогащенной продуктом смеси из газа-реагента и получаемого газов, косвенную передачу тепла от реакционного канала к теплообменному каналу со скоростью, эффективной для поддержания температуры смеси газов ниже равновесной температуры, и отвод выходящего потока, обогащенного получаемым газом, от выхода из реакционного канала при температуре выпуска. 2. Способ по п.1, при котором обогащенная продуктом смесь имеет равновесную концентрацию продукта, которая увеличивается с уменьшением температуры, и коэффициент скорости реакции ...

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 ...

ОКИСЛИТЕЛЬНОЕ ДЕГИДРИРОВАНИЕ АЛКАНОВ (ОД)

Tube bundle reactor for catalytic gas phase reactions, automatically bypasses recirculated heating medium in cold, viscous state, during start up

During reactor (2) start up, heat exchange medium bypass (22) throughput, corresponds with a comparatively-cold and viscous state. In this case, the reactor vessel (8) is partially bypassed. During steady-state reactor operation, flow is automatically controlled as a function of the instantaneous heating power required in the reactor. In this case, heat exchange medium passes through the reactor at an essentially constant flow rate. Preferred Features: Control functions are carried out in a common unit. Bypassing is controlled on temperature and ranges of bypass ratio are specified for start-up and running conditions. Annular channels and openings form inlets and outlets for the heat exchange medium. A heater (30) is provided for the medium, and is used during start up. It is in e.g. a valved, auxiliary circuit in a location unrelated to the main medium inlet and outlet. An external heating medium is employed in a heater. Further details of the bypass, its valving and circulating pump (12) connections and disposition are provided. A mixer may be included. Conventional thermal expansion and de-gasification provisions are made. An additional pump mitigates against cavitation in the circulation pump. The design is further detailed.

Verfahren zur Herstellung von Monosilan

Anlage zur kontinuierlichen Herstellung von Monosilan und Tetrachlorsilan durch katalytische Dismutierung von Trichlorsilan bei einer Betriebstemperatur und einem Druck von 1 bis 50 bar basierend auf folgenden Einheiten • einem Gegenstromreaktor (1) mit Doppelmantel (2), • mindestens ein im Gegenstromreaktor (1) angeordnetes und mit Katalysator (3) bestücktes Katalysatorbett (4), • einem Kondensator (5) am Kopf des Gegenstromreaktors (1), • einer Verdampfereinheit (6) am Sumpf des Gegenstromreaktors (1), • mindestens einer Trichlorsilanzuführung (A) für die Aufgabe von Trichlorsilan (7.1, 7.2) in den Gegenstromreaktor (1), • einem Wärmetauscher (7), wobei das Trichlorsilan zunächst mittels Leitung (7.1, 7.2) über den Wärmetauscher (7) geführt und dort vorgewärmt wird und dazu Sumpfprodukt mittels Leitung (6.1, 6.2) aus der Verdampfereinheit (6) über den Wärmetauscher (7) dem Doppelmantel (2) auf einer Höhe im unteren Teil des Gegenstromreaktors (1) zugeführt und auf einer Höhe im oberen ...

Double heat exchanger for exothermic reactions - has set of tubes contg. catalyst which act as reactor tubes, with bundle above and below, having heat transfer medium around tubes

Tubular reactor is for carrying out gas phase catalytic reactions. Two tube bundles are used above and below a common inlet branch (or outlet). The gas stream divides and flows out from either end of the vessel. On the cooling side, distributor plates are used to give uniform coolant flow along the walls of the tubes. The apertures on these increase towards the centre. A further baffle is used in the cooling side at the level of max. heat release. Used for strongly exothermic gas phase catalytic reaction. Can also be used on endothermic reactions. The capacity is not limited by the heat transfer factors nor by the construction.

Verfahren zu katalytischen Gasphasenoxidation von Propen zu Acrolein

Verfahren zur katalytischen Dampfphasenoxidation und Röhrenkesselreaktor

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

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

CATALYTIC 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 ...

Steam reforming

Isothermal reactor for partial oxidation of methane

A multiple contact bed converter

... A multiple contact bed converter for the catalytic conversion of So2-containing gases into So3, comprises at least three contact beds and an intermediate heat exchanger annularly surrounding the first contact bed and directly adjacent thereto and so arranged that when the converter is in operation, the gases leaving the first bed flow through the heat exchanger to the second bed. As shown, So2 gases having been conventionally preheated to approximately 320 DEG C. by heat exchange with So3 gases leaving the converter through an outlet opening 13, enter an annular chamber 2 through an inlet 1. From this chamber they pass into a heat exchanger 21 which annularly surrounds the contact beds 4, 6 and being guided by baffles 22 sweep around a U-shaped flow path defined by hairpin tubes of the heat exchanger in cross flow. The temperature of the So2 gases having thus been raised to 440 DEG C., they then pass through a preliminary catalyst bed 4 via opening 5. The precatalyzed ...

A method of carrying on catalytic molecular association of organic compounds

... 306,883. Selden Co., (Assignees of Jaeger, A. O.) Feb. 27, 1928, [Convention date]. Esters; aldehydes.-In a process for effecting the molecular association of organic compounds the reacting vapours are passed through heatexchanging elements at least partly embedded in a catalyst layer, the vapour being in indirect heat-exchanging relation with the catalyst; the flow is then reversed and the vapour passed in direct heat-exchanging relation with the catalyst and with the incoming gas; and finally the vapour passes after another reversal of flow through the catalyst layer. In the illustrated modification the vapours pass down through the tubes 9, up through the surrounding tubes 11, and down through the catalyst. In a modification the passages are in the form of concentricannuli instead of separate tubes. A portion of the gas may be admitted directly to the catalyst, e.g. by the pipe 14. A part or all of the reaction mixture may be recirculated through the converter either with or without ...

CATALYTIC CONVERSION OF GAS/LIQUID

Catalytic apparatus

... 331,468. Selden Co., (Assignees of Jaeger, A. O.). Dec. 22, 1928, [Convention date]. Catalytic apparatus. - Apparatus for carrying out exothermic catalytic gas reactions comprises one or more layers of catalyst which are cooled by means of the reaction gases, followed by one or more layers of catalyst which are cooled by means of a medium other than the reaction gas issuing from the first layer or layers. The .cooling medium for the second layer may be the reaction gas before passing through the first layer or it may be an independent medium. The cooling means in the first layer are preferably of the double counter-current type and the cooling means in the second layer may also be of the same kind. In the embodiment shown in Fig. 1, closed tubes 4 extend through the catalyst layer 3 and for some distance below it and the reaction gas is fed to the bottoms of these tubes by the inner tubes 5 so that it undergoes indirect and direct heat exchange with the .catalyst before passing through ...

Flow reactors for chemical conversions with heterogeneous catalysts.

Flow reactors for chemical conversions with heterogeneous catalysts.

A apparatus for use in process systems which include exothermic chemical conversions of organic compounds to value added products is disclosed mote particularly, flow reactors for exothermic chemical conversions using a fixed heterogeneous catalyst with means for control of the exortherm. Flow reactors of the invention comprise a plurality of walled conduits (3) each having an outer surface disposed for contact with a heat-transfer medium, an inlet distribution manifold (2) adapted for flow communication with a downstream manifold (4) through channels formed by heterogeneous catalytic material disposed within each conduit during operation in a sequence of zones for catalyst having the same or different length along the longitudinal coordinate of the conduit and within each zone essentially uniform cross-section of the conduit measured in a plane perpendicular to the longitudinal coordinate thereby defining volume of the zone, and the sequence of zones comprising of at least two zones (5 ...

Flow reactors for chemical conversions with heterogeneous catalysts.

Flow reactors for chemical conversions with heterogeneous catalysts.

PROCEDURE OF THE START-UP OF A HETEROGENEOUSLY CATALYZED PARTIAL ONE GASEOUS PHASE OXIDATION OF ACROLEIN TO ACRYLIC ACID OR OF METHACROLEIN TOO METHACRYLSÄURE

PROCEDURE FOR THE CHANGE OF TEMPERATURE OF A BANK OF TUBES REACTOR

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

CATALYTIC CONVERSION OF GAS OR LIQUID IN A PLURALROHRREAKTOR.

ROHRBUNDELREAKTOR FUR THE CATALYTIC GASEOUS PHASE OXIDATION

HEAT EXCHANGE MORE REFORMER WITH LOW PRESSURE LOSS

CHEMICAL REACTOR WITH HEAT EXCHANGER

Procedure and device for the Gasführung with catalytic high pressure synthesis reactors, in particular for the ammonia synthesis

Fixed-bed catalytic reactor

Reaction apparatus with a heat-exchanger

CATALYTIC VAPOR PHASE OXIDATION

Integrated reactor

REACTION APPARATUS AND REACTION METHOD

A reaction apparatus comprising a heat exchanger 5 and a reactor 1 with a heater 2, which are enclosed in an outer casing 6, the top of the heat exchanger 5 being connected to the reactor 1, the other end part of the heat exchanger 5 and the bottom of the outer casing 6 being fixed to each other by a flange 4, and a double piping 7 for introducing a gas to be treated and discharging the treated gas being connected to the other end part of the heat exchanger 5, such that the gas passes through the heat exchanger 5, the reactor 1 and the heat exchanger 5 during the process from introducing gas through one of the inner tube and the outer tube in the double piping to discharging the gas through the other tube, and reaction method using the apparatus. Using the apparatus of the present invention, the temperature distribution inside the reactor can be kept uniform and efficiency in energy recovery is enhanced.

A REACTOR SYSTEM, AND A PROCESS FOR PREPARING AN OLEFIN OXIDE, A 1,2-DIOL, A 1,2-DIOL ETHER, A 1,2-CARBONATE AND AN ALKANOLAMINE

The present invention provides an epoxidation reactor system for preparin g an olefin oxide comprising: - one or more purification zones comprising on e or more purification vessels containing an absorbent comprising copper and zinc; and - a reaction zone comprising one or more reactor vessels containi ng an epoxidation catalyst, wherein the reaction zone is positioned downstre am from the one or more purification zones; a process for preparing an olefi n oxide; and a process for preparing a 1,2-diol, a 1,2-diol ether, a 1,2-car bonate, and an alkanolamine.

PROCESS AND APPARATUS FOR REFORMING HYDROCARBONS

The invention relates to a process and apparatus for the production of synthesis gas from a hydrocarbon feedstock in a heat exchanger reformer, wherein a cooling medium is added to the heat exchange reformer.

REACTOR CONSTRUCTION AND USAGE

Apparatus and method for first mixing continuously at a prechosen flow rate a less dense fluid with a more dense fluid, the fluids being at least partially immiscible, so as to achieve a constant weight ratio of one fluid to the other per prechosen unit of mixed fluid volume transversely across the path of such mixed fluid followed by charging the resulting mixed fluid simultaneously to a multiplicity of tubes in a tubular reactor under conditions of substantially plug flow. At least one of the fluids is a liquid at all times.

FLUIDIZED BED REACTOR WITH GAS COOLER

A new reactor apparatus that can be used to carry out chemical reactions in a fluidized catalyst bed at high temperatures with reduced afterburning or other undesirable downstream side reactions. One application is the manufacture of acrylonitrile.

REACTION APPARATUS WITH A HEAT-EXCHANGER

A reaction apparatus comprising a heat exchanger 5 and a reactor 1 with a heater 2, which are enclosed in an outer casing 6, the top of the heat exchanger 5 being connected to the reactor 1, the other end part of the heat exchanger 5 and the bottom of the outer casing 6 being fixed to each other by a flange 4, and a double piping 7 for introducing a gas to be treated and discharging the treated gas being connected to the other end part of the heat exchanger 5, such that the gas passes through the heat exchanger 5, the reactor 1 and the heat exchanger 5 during the process from introducing gas through one of the inner tube and the outer tube in the double piping to discharging the gas through the other tube, and reaction method using the apparatus. Using the apparatus of the present invention, the temperature distribution inside the reactor can be kept uniform and efficiency in energy recovery is enhanced.

TWO-STAGE REACTOR FOR EXOTHERMAL AND REVERSIBLE REACTIONS AND METHODS THEREOF

The present invention relates a two-stage reactor for exothermal, reversible reactions. In particular, the reactor contains a first semi-isothermal stage followed by a second cooling stage. The reactor allows for high conversion of products in an exothermal, reversible reaction.

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

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

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

A method for the synthesis of anhydrous hydrogen halide fluids from organic halide fluids, such as perfluorocarbon fluids and refrigerant fluids, and anhydrous hydrogen and anhydrous carbon dioxide; and the synthesis of anhydrous carbon dioxide and anhydrous from carbon monoxide and water for the environmentally safe disposition thereof.

METHOD FOR PRODUCTION OF ETHYLENE OXIDE

The production of ethylene oxide by the catalytic vapor phase oxidation of ethylene with a molecular oxygencontaining gas is effected in a reactor provided with a preheating zone, a reaction zone, a cooling zone, a partition plate separating the first two portions from the third portion, and a multiplicity of reaction tubes piercing the two separated sections by a method which comprises supplying hot water to the cooling zone of the reactor, forwarding zone of the hot water discharged from the cooling zone to a gas-liquid separation tank, circulating the remainer of the hot water in conjunction with the cooling hot water to the cooling zone, supplying the hot water separated in the gas-liquid separation tank to the reaction zone to remove the heat of the oxidation reaction, and circulating the hot water extracted in the form of a gasliquid mixed phase to the gas-liquid separation tank. The method is excellent to prevent isomerization of ethylene oxide to acetaldelyde which is impurity, ...

CERAMIC MEMBRANE FOR ENDOTHERMIC REACTIONS

Syngas, a mixture of hydrogen and carbon monoxide, is an intermediate in the conversion of methane to liquid fuels. For certain applications, it is desirable to maintain an H2/CO molar ratio of about 3. This molar ratio is achieved by steam reforming of methane in accordance with: CH4 + H2O ~ 3H2 + CO. To provide the heat required to drive the endothermic steam reforming reaction, a low grade fuel is combusted in a reactor and the heat of combustion conducted to the endothermic reaction. By using an oxygen selective ion transport membrane element to transport the oxygen required for combustion, the formation of undesirable NOx compounds is minimized.

Verfahren zur Durchführung exothermer Reaktionen unter Druck und Vorrichtung zur Durchführung des Verfahrens.

Glasdachsprosse mit Eisenbeton-Tragkörper und kittloser Befestigungsvorrichtung der Glastafeln mittels Verschraubung.

Verfahren zur Durchführung katalytischer Reaktionen in der Gasphase in Kontaktöfen.

Verfahren zur Regenerierung eines Katalysators in einem Rohrkonverter

Wärmetauschvorrichtung

FURNACE AND METHOD OF STEAM REFORMING

СПОСОБ ПАРОВОГО РИФОРМИНГА С УЛУЧШЕННЫМ ПОТОКОМ ДЫМОВОГО ГАЗА

Настоящее изобретение относится к способу парового риформинга углеводородов в риформинг-печи, включающему по меньшей мере одну камеру сгорания, имеющую по меньшей мере две вертикальных стенки (1, 2), находящихся друг напротив друга и изготовленных из огнеупорного материала, содержащую по меньшей мере один ряд труб (3) риформинг-печи, расположенных вертикально на середине расстояния между находящимися друг напротив друга вертикальными огнеупорными стенками, с горелками (4), расположенными на каждой из двух находящихся друг напротив друга вертикальных огнеупорных стенок (1, 2), указанные горелки способны производить радиальное пламя, параллельное поверхности стенки (1, 2); и по меньшей мере одну трубу для высвобождения газов горения, расположенную на верхнем краю печи, только на одной из боковых стенок. (1). В соответствии с настоящим изобретением труба для высвобождения газов имеет уровень, связанный с отражателем, с выходом на соединение между трубой и стенкой (1), этот отражатель изменяет ...

ПРОТОЧНЫЕ РЕАКТОРЫ ДЛЯ ХИМИЧЕСКИХ ПРЕВРАЩЕНИЙ С ИСПОЛЬЗОВАНИЕМ ГЕТЕРОГЕННЫХ КАТАЛИЗАТОРОВ

В изобретении предлагается устройство, предназначенное для использования в технологических системах, в которых проводят экзотермические химические превращения органических соединений в продукты с добавленной стоимостью. Более конкретно, предлагаются проточные реакторы для экзотермических химических превращений с использованием неподвижного гетерогенного катализатора со средством для управления экзотермой. Проточные реакторы в соответствии с настоящим изобретением содержат множество трубопроводов (3), каждый из которых имеет наружную поверхность, предназначенную для контакта с теплоносителем, впускной распределительный коллектор (2), приспособленный для жидкостного сообщения с расположенным ниже по течению коллектором (4) через каналы, образованные из гетерогенного каталитического материала, заключенного внутри каждого трубопровода в процессе работы в последовательности зон для катализатора, имеющих одинаковую или различную длину вдоль продольной оси трубопровода, причем внутри каждой зоны ...

УСТРОЙСТВО ДЛЯ РАЗДЕЛЕНИЯ СТУПЕНЕЙ КОНВЕРТЕРА

Опорное кольцо для размещения элемента типа плиты в сосуде, в частности, полки (8) или разделительной плиты (9) в конвертере (1) для производства SO3 из газа, содержащего SO2; элемент типа плиты опирается на кронштейн (11), прикрепленный к стенке (10) сосуда (1). Кронштейн (11) имеет верхнюю опорную поверхность (12), которая наклонена вниз относительно горизонтали.

OXIDATIVE DEHYDROGENATION OF (ODG) ETHANE

Parallelized jet loop reactors

The present invention relates to a device and a method for the continuous conversion of a liquid and a second fluid, wherein the device has at least two jet loop reactors connected parallel to each other and a common outer liquid circulation.

Catalytic oxidation reactor with enhanced heat exchanging system

METHOD AND APPARATUS FOR REFORMING LOW PRESSURE OILS WITH HEATING BY MEANS OF THE FLUE GAS

Réacteur pour réactions chimiques à catalyseurs.

L'invention a pour objet un réacteur pour réactions chimiques à catalyseurs du type comportant un faisceau de tubes de réactions parallèles débouchant, à leurs extrémités, dans des coiffes d'extrémité par des orifices ménagés respectivement dans des plaques tubulaires perpendiculaires aux dits tubes, et dans lequel un agent échangeur de chaleur dirigé au moyen d'une pompe extérieure, suivant un parcours cyclique, est amené et évacué radialement par des conduits annulaires extérieurs entourant le réacteur et reliés à l'intérieur de celui-ci par des ouvertures réparties sur sa périphérie. Selon l'invention, il comporte, dans des espaces vides ménagés dans le faisceau de tubes de réaction (2), des tubes de dérivation (40) clos, parallèles aux tubes de réaction (2), et percés à différents niveaux de trous (41) de communication avec l'intérieur du réacteur.

ARRANGEMENT OF A HEATING UNIT IN REACTION APPARATUS

Exchanging reactor to carry out steam reforming reactions, comprises an enclosure, a distribution unit to distribute a charge through a fixed-bed catalytic zone, and a collection unit to collect an effluent from the catalytic zone

L'invention concerne un réacteur échangeur (1) comprenant : - une enceinte (2) - des moyens de distribution d'une charge à travers une zone catalytique en lit fixe (10), - des moyens de collecte (6) de l'effluent issu de la zone catalytique (10), - des moyens de chauffage de la zone catalytique (10), dans lequel lesdits moyens de collecte (6) comportent des conduits traversant la zone catalytique (10) de part en part, et dans lequel les moyens de chauffage de la zone catalytique comportent au moins un zone de combustion (13) située à proximité de la zone catalytique (10), des moyens d'alimentation de ladite zone de combustion en mélange gazeux oxydant (15) et en combustible gazeux (17) et des moyens d'évacuation (14) de l'effluent gazeux issu de la combustion.

REACTOR

ENGINE

Improvements brought to the apparatuses to transmit heat of a gas to another through metal walls

LOW PRESSURE DROP HEAT EXCHANGE REFORMER

PURPOSE: Reforming exchangers with catalyst tubes having a relatively low ratio of inside tube diameter to catalyst particle size are provided. CONSTITUTION: The syngas reforming exchanger(100) comprises an elongated shell(108) having relatively high and low temperature ends(110,112); a shell side fluid inlet(104) adjacent the high temperature end(110) for receiving a hot gas feed; a tube side fluid inlet(102) adjacent the low temperature end for receiving a feed mixture of hydrocarbon and steam; a shell side fluid outlet(106) fluidly isolated from the tube side fluid inlet(102) by a tube sheet(114) adjacent the low temperature end(112) for discharging cooled gas; a tube bundle(116) comprising a plurality of tubes(118) and one or more longitudinally-spaced transverse baffle plates(120), wherein the tubes(118) have an inlet end(122) secured to the tube sheet(114) for receiving the feed mixture and an outlet end(124) adjacent the shell side fluid inlet(104) for discharging reformed gas into ...

METHODS FOR THE CATALYTIC OXTDAÇÃO IN PHASE VAPOR AND TO COMPACT A CATALYSER

HYDROGEN GENERATOR AND FUEL CELL POWER GENERATOR

Provided is a hydrogen generator which prevents the supply of droplets to a reforming catalyst layer and has stable performance, wherein the generator has a water vaporizer (7) which supplies raw material gas and water, a reforming catalyst layer (9) which supplies the gas mixture from the water vaporizer (7), a burner (4) which mixes the fuel gas with air and combusts, a combustion exhaust gas flow path (16) which is provided on the inner side of the water vaporizer (7) for the flow of the combustion exhaust gas, and a spiral round rod (18) which has a transformation catalyst layer (10), which is placed on the outside of the water vaporizer (7) and supplies the reforming gas, and inserts the water vaporizer (7) between two cylinders (100) and (101). The pitch of the spiral round rod (18) is small compared to the other location in the downstream part of the water vaporizer (7).

HEAT EXCHANGER AND METHOD OF PERFORMING CHEMICAL PROCESSES

A heat exchanger including a passageway having an internal passage adapted to form a first flow path, and an array of conduits having internal passages that collectively form a second flow path. The conduits extend through the internal passage of the passageway, and a first conduit of the array is provided with a lower total heat exchange surface area per unit volume therein than a second conduit of the array. A method of performing chemical processes is provided that includes providing a catalyst bed within the second flow path, and minimizing a temperature differential between a maximum temperature of a fluid in the second flow path and a minimum temperature of the fluid in the second flow path.

TUBULAR REACTOR FOR CATALYTIC REACTIONS

The invention relates to a tubular reactor (2) for catalytic reactions, which inside its reactor mantle (10) has a contact tube bundle (8) around which a heat carrying medium circulates. The tube bundle extends between a tube base on the reaction gas entry side and a tube base on the reaction gas exit side (4, 6; 60; 82). The invention also comprises gas entry and gas exit domes (12, 14) which span the two tube bases across their faces, and reaction-inhibiting means in the area of the tube base on the gas entry side. The invention is characterized in that the reaction-inhibiting means wholly or partly consist of a heat insulating layer (46; 50; 64; 80) which does not cover the tube in its cross-section and is situated on at least one side of the corresponding tube base (4; 60; 82). In this way either the corresponding tube base (4; 60; 82) is insulated against the hot heat carrying medium or the reaction gas entering the reactor is prevented from coming into contact with the relatively ...

CHEMICAL REACTOR WITH HEAT EXCHANGER

A reactor of the staged adiabatic reactor type, comprises at least one heat exchanger panel, preferably a printed circuit heat exchange (PCHE) panel (90), interposed between adiabatic beds of catalyst (81), wherein the facial area of the panels and the superficial facial area of the corresponding catalyst are substantially similar, and the panels include means defining discrete passages for handling of reactants and heat transfer media, wherein the means defining passages for heat transfer media provide for at least two differing flow path directions for the heat transfer media through the said heat exchanger panel whereby the occurrence of temperature bias or differentials is reduced.

Carrying out exothermic catalytic gas reactions

Fuel reformer

Provided is a fuel reforming apparatus wherein vacuum reforming tubes ( 13 ) are accommodated in a flow path ( 12 ) between an inner cylinder ( 9 a) of a heat-insulating vessel ( 9 ) and a furnace flue ( 11 ) arranged in the inner cylinder ( 9 a). Formed between the furnace flue ( 11 ) and a guide cylinder ( 21 ) accommodated in the furnace flue ( 11 ) is a gap though which combustion gas ( 28 ) generated in a combustor ( 10 ) is raised. A helical plate ( 22 ) is arranged in the flow path ( 12 ) such that the combustion gas ( 28 ) lowered in the flow path ( 12 ) flows across the reforming tubes ( 13 ). Thus, red heating of the furnace flue can be sufficiently conducted to sufficiently heat the reforming tubes through radiation heat transfer. As a result, heat transfer areas of the reforming tubes may be made smaller to reduce in size the reforming tubes. Since upper ends of the reforming tubes are not exposed to high temperature and the combustion gas lowered between the inner cylinder ...

Method for the production of polyester granulates from highly viscous polyester melts and also device for the production of the polyester granulates

The invention relates to a method and device for the direct production of polyester granulate from a highly viscous polyester melt with a polymerization degree of 132 to 165, as well as the granulates formed thereform. In the method, the highly viscous polyester melt is subjected to a pre-drying and drying/degassing after a hot cutting method. Hot cutting is implemented at water temperatures of 70° C. to 95° C. and with a liquid to solid ratio of 8 to 12:1.

Annular distributor having guide vane to improve flow rate distribution

Disclosed is an annular distributor having: an annular slit layer that is mounted on an inner circumferential surface of the annular distributor and has at least one slit discharging or introducing a fluid; at least one opening that is formed on an outer circumferential surface of the annular distributor and is connected with any one of a fluid supply duct and a fluid discharge duct; and at least one guide vane selected from three types of guide vanes that are installed in the annular distributor, and splits a flow rate of the fluid supplied from the duct or collects a flow rate of the fluid discharged to the duct. And disclosed are a reactor or heat exchanger has the annular distributor, and a method of producing unsaturated aldehyde or unsaturated acid from olefin by catalytic gas phase oxidation in the reactor.

COMPACT STEAM REFORMER

Shell and tube type heat exchanger

Reformer with low fired duty per unit of feedstock

METHOD FOR PRODUCING SYNTHESIS GAS BY STEAM REFORMING AND PARTIAL OXIDATION

PROBLEM TO BE SOLVED: To provide a method for producing a synthesis gas, which is high-performance from the viewpoint of energy and requires equipment of a reduced size and limited investoment cost. SOLUTION: A method for producing a synthesis gas SG from a hydrocarbon feedstock etc., is described. A first feedstock F1 supplied with steam is subjected to steam reforming in a multi-tubular reactor heat exchanger R containing a plurality of reaction tubes 38 containing a steam reforming catalyst and a shell containing the tubes 38 to produce a first synthesis gas SG1; the reaction tubes 38 are mainly heated by heat-transfer from a hot fluid HF recirculated through the outsides of the tubes 38 to produce a second synthesis gas SG2, and the hot fluid HF is a stream of the multistage partial oxidation of a second feedstock F2 with oxygen of pressure of 0.5 to 12 MPa; and a synthesis gas SG is produced by mixing the synthesis gas SG1 with the synthesis gas SG2. COPYRIGHT: (C)2007,JPO&INPIT ...

КОМПАКТНЫЙ РЕАКТОР РЕФОРМИНГА

Изобретение относится к области химии и может быть использовано при получении водорода. Реактор реформинга для превращения исходной жидкости в водород включает секцию 4 реформинга, находящуюся в закрытом объеме, секцию 3 кипения и секцию 2 горения. Секция реформинга содержит одну или несколько катализаторных трубок 20. Секция 3 кипения имеет один или несколько сквозных каналов 11 для прохождения газообразных продуктов горения 12 из секции 2 горения, и секция горения снабжена не менее чем одной горелкой 16. 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 закрытом объеме, и при этом по крайней мере часть закрытого объема находится внутри названной секции кипения. Изобретение позволяет легко обеспечить достижение и поддержание рабочей температуры. 8 з.п. ф-лы, 2 ил.

СПОСОБ ПОЛУЧЕНИЯ СИНТЕЗ-ГАЗА ПУТЕМ КОНВЕРСИИ С ВОДЯНЫМ ПАРОМ В РЕАКТОРЕ-ТЕПЛООБМЕННИКЕ

Изобретение относится к области химии. Поток, содержащий первую загрузку с добавлением водяного пара, подвергают конверсии с водяным паром в по меньшей мере одном мультитрубчатом реакторе-теплообменнике, имеющем множество реакционных труб, содержащих катализатор конверсии с водяным паром, и камеру, в которой находятся эти трубы, для получения первого синтез-газа. Реакционные трубы нагревают главным образом посредством конвекции путем циркуляции в камере текучего теплоносителя HF снаружи по отношению к трубам, в котором HF представляет собой поток газа, по существу не содержащий азота, частичного окисления кислородом второй загрузки для получения второго синтез-газа. Текучий теплоноситель содержит по меньшей мере первый поток частичного окисления кислородом первой части, который циркулирует в реакторе-теплообменнике для нагревания реакционных труб, который затем смешивают в по меньшей мере одной дополнительной зоне частичного окисления с по меньшей мере второй частью и кислородом, вводимыми ...

КАТАЛИТИЧЕСКАЯ УСТАНОВКА

Изобретение относится к каталитической установке, пригодной для использования в трубчатом реакторе, в сочетании с зернистым катализатором, в частности, с катализаторами, пригодными для использования в процессах каталитического потокового риформинга. Описана каталитическая установка, расположенная в вертикальной реакционной трубке. Установка содержит структурированный катализатор в верхней части реакционной трубки. Зернистый катализатор под упомянутым структурированным катализатором в нижней части упомянутой реакционной трубки. Устройство носителя катализатора расположено между структурированным катализатором и зернистым катализатором. Причем устройство носителя катализатора содержит цилиндрическое тело, имеющее первый конец, адаптированный для соединения со структурированным катализатором, и второй конец. Цилиндрическое тело обладает диаметром, составляющим 70-90% от внутреннего диаметра трубки, и соотношением длина/диаметр в диапазоне 0,5-2,5. Изобретение обеспечивает снижение нежелательного ...

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.

Heat exchanger reformer

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

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.

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.

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 ...

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 ...

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 ...

PROCESS FOR GENERATING A MIXED MULTICOMPONENT VAPOR FOR PREPARATION OF MONOALKYL ETHERS OF DIPHENOLS

A process and a system thereof include apparatuses for developing multi-component vapor mixture by heating of solution of reactants comprising one or more of diphenols, or diphenol derivatives, and an organic compound. Upon reacting in a vapor state in presence of a catalyst with diphenols, or diphenol derivatives, the organic compound produces a monoalkyl ether of a dihydric phenolic compound. The entire solution of reactants completely transforms into a super-heated multi-component vapor using heaters without the use of thin film evaporator. The complete transformation of the entire solution of the reactants in to super-heated multicomponent vapor is achieved by heating the entire solution firstly by a pre-heater followed by further heating by a super-heater. The unevaporated or condensed high boilers and tar are removed to drain. The superheated vapor is subjected to vapor phase reaction mediated by catalyst to get monoalkyl ether of a dihydric phenolic compound. 1. A system for developing multi-component vapor mixture by heating of solution of reactants comprising one or more of diphenols , or diphenol derivatives , and an organic compound , wherein the organic compound is one which upon reacting in a vapor state in presence of a catalyst with diphenols , or diphenol derivatives , produces a monoalkyl ether of a dihydric phenolic compound; whereinthe entire solution of reactants completely transforms into a super-heated multi-component vapor using heaters without the use of thin film evaporator.2. The system of comprising:a. a stainless steel reactor under a nitrogen atmosphere for making a solution of a diphenol or a diphenol derivative in the organic compound at room temperature and heating the same to about 50-50-70° C.,b. a pre-heater to heat the solution to get vapors and a super-heater to heat the vapors to get super-heated vapors multicomponent mixture from the said solution,c. a jacketed section/vessel for receiving superheated steam at its top and ...

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. A process of making acrylic acid comprising:a) providing a mixed feed gas comprising propylene to a first shell-and-tube reaction stage, wherein the first shell-and-tube reaction stage comprises a mixed metal oxide catalyst;b) oxidizing the propylene in the first shell-and-tube reaction stage to produce a process gas comprising acrolein;c) cooling the process gas to a temperature ranging from 240° C. to 280° C. in an interstage heat exchanger;d) passing the cooled process gas through an open interstage region;e) passing the process gas to a second shell-and-tube reaction stage, wherein the tubes of the second shell-and-tube reaction stage have an internal diameter greater than 22.3 mm and wherein the second shell-and-tube reaction stage comprises a mixed metal oxide catalyst;f) oxidizing the acrolein in the second shell-and-tube reaction stage to produce a product gas comprising acrylic acid; andg) transferring the product gas between a reactor outlet and downstream collection and purification equipment using large diameter exit piping having an outlet diameter ratio, Ko, of 0.08 or more.2. The process of claim 1 , wherein the second reactor stage comprises a conical outlet reactor head.3. The process of claim 1 , wherein the open interstage region is at least partially filled with at least one inert material.4. The process of claim 1 , wherein passing the cooled process gas ...

Two-stage reactor for exothermal and reversible reactions and methods thereof

The present invention relates a two-stage reactor for exothermal, reversible reactions. In particular, the reactor contains a first semi-isothermal stage followed by a second cooling stage. The reactor allows for high conversion of products in an exothermal, reversible reaction.

CATALYST TUBE FOR REFORMING

The inventions is directed to a new design for catalyst tubes, which makes it possible to apply the concept of regenerative reforming into steam reformers having catalyst tube inlets and outlets at opposite sides of the furnace chamber. The catalyst tube comprises an inlet for process gas to enter the catalyst tube and an outlet for process gas to exit the catalyst tube, which inlet and outlet are located at opposite ends of the catalyst tube. The catalyst tube further comprises a first annular channel comprising the catalyst, a second annular channel for process gas to flow countercurrently or co-currently to the process gas flowing through the first annular channel. 1. A catalyst tube for regenerative catalytic conversion of process gas in an industrial furnace comprisinga catalyst tube inlet for process gas to enter the catalyst tube and a catalyst tube outlet for process gas to exit the catalyst tube, which inlet and outlet are located at opposite ends of the catalyst tube;{'b': 1', '11, 'an outer reactor tube (,);'}{'b': 5', '15', '1', '11, 'an inner tube (,) that extends coaxially inside the outer reactor tube (,);'}{'b': 3', '13', '1', '11', '5', '15, 'a boundary (,) located between the inner wall of the outer reactor tube (,) and the outer wall of the inner tube (,);'}{'b': 1', '11', '3', '13, 'a first annular channel for catalytically converting process gas, which channel is defined by the inner wall of the outer reactor tube (,) and the outer wall of the boundary (,), which channel is loaded with catalyst material;'}{'b': 3', '13', '5', '15, 'a second annular channel for process gas to flow countercurrently or co-currently to the process gas flowing through the first annular channel, which second annular channel is defined by the inner wall of the boundary (,) and the outer wall of the inner tube (,);'}{'b': 4', '14', '1', '11', '5', '15, 'an inlet barrier (,) at the inlet end of the catalyst tube for preventing process gas to exit the outer reactor tube ...

OXIDATIVE DEHYDROGENATION (ODH) OF ETHANE

Processes and associated reaction systems for the oxidative dehydrogenation of ethane are provided. In particular, a process is provided that comprises supplying a feed gas comprising ethane and oxygen to a multitubular fixed-bed reactor, allowing the ethane and oxygen to react in the presence of an oxidative dehydrogenation catalyst to yield a reactor effluent comprising ethylene; supplying a coolant to an upstream region of an interior shell space of the reactor in a flow pattern that is counter-current with the flow of the feed gas; and withdrawing the coolant from the upstream region and supplying at least a portion of the coolant withdrawn from the upstream region to the downstream region in a flow pattern that is co-current with the flow of the feed gas. 1. A process for the oxidative dehydrogenation of ethane to ethylene comprising:providing a multitubular fixed-bed reactor comprising a reactor inlet, an interior shell space, a perforated partition that divides the interior shell space into an upstream region and a downstream region, and a plurality of reactor tubes, wherein the plurality of reactor tubes comprise a catalyst bed that comprises an oxidative dehydrogenation catalyst;supplying a feed gas comprising ethane and oxygen to the reactor inlet and allowing the ethane and oxygen to react in the presence of the oxidative dehydrogenation catalyst to yield a reactor effluent comprising ethylene;supplying a coolant to the upstream region in a flow pattern that is counter-current with the flow of the feed gas through the plurality of reactor tubes; andwithdrawing the coolant from the upstream region and supplying at least a portion of the coolant withdrawn from the upstream region to the downstream region in a flow pattern that is co-current with the flow of the feed gas through the plurality of reactor tubes.2. The process of claim 1 , wherein the coolant is supplied to the upstream region at an upstream coolant inlet at an upstream inlet coolant ...

Gasoline production device

Provided is a gasoline production device capable of effectively using heat of reaction generated in the synthesis of gasoline and also capable of readily cooling heat generated by synthesizing gasoline. A device 30 for producing gasoline from methanol includes a plurality of reaction tubes 34 configured to synthesize gasoline from methanol and a duct 36 configured to allow air to flow outside the reaction tubes, and heat exchange is carried out between synthesis heat generated within the reaction tubes 34 and the air which flows through the duct 36.

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 steam reformer for the production of a hydrogen reformate , comprising:a cylindrical shell defining a cavity having a bottom portion comprising an opening;a heat source configured to heat a fluid supplied to the cavity;a silicon carbide hollow conduit comprising openings at both ends, a first end of the conduit is disposed within the cavity and opens into the cavity and a second end of the conduit is attached to the bottom portion of the shell and opens to the shell exterior, wherein the heat source is in fluid communication with the second end, and the silicon carbide hollow conduit guides the heated fluid from the heat source to the cavity;a plurality of cylindrical reactor modules as ...

SHELL-AND-MULTI-TRIPLE CONCENTRIC-TUBE REACTOR AND HEAT EXCHANGER

The present disclosure relates to a shell-and-multi-triple concentric-tube reactor and a shell-and-multi-triple concentric-tube heat exchanger, and to a shell-and-multi-triple concentric-tube reactor and a shell-and-multi-triple concentric-tube heat exchanger which provide a new type of reactor and heat exchanger, thereby maximizing catalyst performance and improving performance of the reactor by optimizing heat exchange efficiency and a heat flow, uniformly distributing a reactant, and increasing a flow rate of the reactant, and accordingly making the reactor and the heat exchanger compact. 1. A shell-and-multi-triple concentric-tube reactor comprising:a shell side heating medium flow zone in which a shell side heating medium flows along a route formed by a baffle in a shell;a catalytic reaction zone in which a reactant is distributed to respective catalytic reaction flow paths by a reactant distributing unit, and the reactant performs a catalytic reaction with a catalyst positioned in the catalytic reaction flow paths, the catalytic reaction zone including a product capturing unit which captures a product produced by a heat exchange between the shell side heating medium and an inner heating medium and an unreacted material which is not reacted; andan inner heating medium flow zone in which the inner heating medium is distributed to inner heating medium inlet tubes inserted into the catalytic reaction flow paths by an inner heating medium distributing unit, and the inner heating medium, which exchanges heat with the catalytic reaction flow paths, is discharged to an inner heating medium capturing unit through inner heating medium discharge tubes,wherein one end of the inner heating medium inlet tube inserted into the catalytic reaction flow path is configured to be closed,the inner heating medium discharge tube includes a configuration that is inserted into the inner heating medium inlet tube and opened, such that the inner heating medium flowing into the inner ...

Oxidative dehydrogenation (odh) of ethane

Processes and associated reaction systems for the oxidative dehydrogenation of ethane are provided. In particular, a process is provided that comprises supplying a feed gas comprising ethane and oxygen to a multitubular fixed-bed reactor and allowing the ethane and oxygen to react in the presence of an oxidative dehydrogenation catalyst to yield a reactor effluent comprising ethylene; and supplying a coolant to an interior shell space of the multitubular fixed-bed reactor in a flow pattern that is co-current with the flow of the feed gas through reactor.

Reactor apparatus for loading a carrier medium with hydrogen and/or unloading it therefrom and plant comprising a reactor apparatus of this kind

A reactor apparatus for loading a carrier medium with hydrogen and/or unloading it therefrom includes a reactor housing chargeable with carrier medium and having a carrier medium feed orifice, having a carrier medium removal orifice, having a base and having a hydrogen gas orifice. The reactor apparatus further includes at least one heat transfer element for supplying heat into the reactor housing. Catalyst has been provided in the reactor housing.

REACTOR APPARATUS FOR DEHYDROGENATING A CARRIER MEDIUM

A reactor apparatus for dehydrogenating a carrier medium includes a reactor housing, an interior space which is enclosed by the reactor housing and includes a preliminary space, which has an inflow opening for inflow of loaded carrier medium into the preliminary space and at least one first connecting opening for outflow of the carrier medium from the preliminary space, and includes a reaction space connected via the at least one first connecting opening to the preliminary space. The reactor apparatus additionally has a heat transfer space which is arranged between the reactor housing and the reaction space and contains a heat transfer medium for transfer of heat from the heat transfer medium to the carrier medium. 1. A reactor apparatus for dehydrogenating a carrier medium , the reactor apparatus comprising:a reactor housing, wherein the reactor housing encloses an interior space, the interior space comprising a preliminary space, which has an inflow opening for inflow of loaded carrier medium into the preliminary space and at least one first connecting opening for outflow of the carrier medium from the preliminary space, the interior space further comprising a reaction space connected via the at least one first connecting opening to the preliminary space;a heat transfer space arranged between the reactor housing and the reaction space and the heat transfer space containing a heat transfer medium for transfer of heat from the heat transfer medium to the carrier medium.2. The reactor apparatus as claimed in claim 1 , further comprising a plurality of reaction tubes claim 1 , each of the plurality of the reaction tubes having a reaction space and each of the plurality of reaction tubes being connected via a first connecting opening to the preliminary space.3. The reactor apparatus as claimed in claim 1 , wherein the at least one first connecting opening has an internal diameter which is less than an internal diameter of a reaction tube connected thereto.4. The ...

REFORMING FURNACE COMPRISING REFORMING TUBES WITH FINS

A reforming furnace for producing hydrogen is provided. The reforming furnace includes a plurality of reforming tubes that allow a flow of hydrocarbons and at least one fluid inside the tubes, from top to bottom, and have, on at least part of the upper half of the outer surface at least one fin that has a thickness of between 1 and 30 mm, a width of between 3 and 100 mm, and a length of between 1 m and an length equivalent to the height of the furnace. 17.-. (canceled)8. A reforming furnace for the production of hydrogen , comprising a plurality of reforming tubes allowing a flow of hydrocarbons and of at least one fluid inside the tubes from the top downward , and having , on their exterior surfaces , one or more fins , the majority of which is situated on at least part of the upper half , with the fins having a thickness comprised between 1 and 30 mm , a width comprised between 3 mm and 100 mm , and a length comprised between 1 m and a length equivalent to the height of said furnace.9. The reforming furnace of claim 8 , wherein the number of fins per tube is comprised between 1 and 50.10. The reforming furnace of claim 8 , wherein the fin may have the shape of a plate in the form of a rectangle claim 8 , a trapezium claim 8 , a triangle claim 8 , a corrugated plate or a chamfered plate.11. The reforming furnace of claim 8 , wherein the fins are installed vertically.12. The reforming furnace of claim 8 , wherein the fluid flowing with the hydrocarbons inside the tubes is steam.13. The reforming furnace of claim 8 , wherein the reforming tubes are installed in a combustion chamber.14. The use of a reforming furnace of for the production of hydrogen. This application is a 371 of International PCT Application PCT/FR2015/052503 filed Sep. 18, 2015 which claims priority to French Patent Application No. 1460107 filed Oct. 21, 2014, the entire contents of which are incorporated herein by reference.The invention relates to a steam reforming furnace for the production of ...

Tube heat exchange unit for internals of heat exchangers reactors

Tube-bundle heat exchange unit (1) for internals of heat exchangers or reactors, comprising: at least one tube bundle (2); a plurality of baffles (3) associated with said tube bundle and defining through-openings according to a predefined arrangement, each opening being passed through by one of more tubes of the tube bundle, and a shell (6) which surrounds said tube bundle and said baffles, wherein the assembly of the tube bundle and the shell can be disassembled and the shell is structurally collaborating with the tube bundle through said baffles.

Method for producing a gaseous fuel comprising hydrogen from kinetic and/or potential energy recovered from a vehicle powered by a four stroke diesel engine fitted with an engine braking mechanism and system useful to implement such method

A method for producing a hydrogen gaseous fuel from kinetic and/or potential energy recovered from a vehicle powered by a four stroke Diesel engine fitted with a Jacobs engine brake during a deceleration stage. Such a method comprises the following steps: a) providing a preheated steam flow; b) providing a gas flow from at least one chemical species used as preheated carbon and hydrogen source; c) mixing the gas flow from at least one chemical species used as carbon and hydrogen source from step a) with the steam flow from step b); d) reacting the mixture from step c) in the catalytic bed of a reforming reactor, heated by high temperature air from the compression stage of the Diesel engine acting as engine brake upon deceleration, producing an outlet synthesis gas flow which contains hydrogen; e) causing water to condense in the outlet synthesis gas flow which contains hydrogen, producing a water-free synthesis gas flow, and f) storing the synthesis gas flow obtained at step e) in a reservoir for its subsequent use during an acceleration stage of the vehicle. A system useful to implement the method for recovering kinetic and/or potential energy from a vehicle powered by a four stroke Diesel engine fitted with a Jacobs engine brake during a deceleration stage.

HEAT EXCHANGE APPARATUS

Heat exchange apparatus and, particularly, heat exchangers having a baffled cooling jacket are disclosed. Methods for using the exchangers including methods that involve cooling an effluent gas produced from a fluidized bed reactor for producing polycrystalline silicon are also disclosed. 1. A heat exchange apparatus for transferring heat between a first process stream and a second process stream , the heat exchange apparatus comprising:a shell;a tube within the shell, the tube having a vertical portion and a horizontal portion transverse to the vertical portion, the shell and tube forming an annular chamber between the shell and tube; anda baffle within the annular chamber.2. The heat exchange apparatus as set forth in wherein the baffle is helical.3. The heat exchange apparatus as set forth in wherein the helical baffle has an outer edge and an inner edge claim 2 , the outer edge contacting the shell and the inner edge contacting the tube.4. The heat exchange apparatus as set forth in wherein the vertical portion and the horizontal portion of the tube form a joint claim 1 , at least one of the vertical portion and the horizontal portion of the tube comprising a substrate and a protective liner disposed on the substrate for reducing erosion at the joint.5. The heat exchange apparatus as set forth in wherein the liner comprises graphite claim 4 , tungsten claim 4 , carbide or cobalt-chromium alloys.6. The heat exchange apparatus as set forth in wherein the vertical portion of the tube comprises an upper segment and a lower segment claim 1 , the upper segment and lower segment being connected by an expansion joint.7. The heat exchange apparatus as set forth in comprising a single tube.8. The heat exchange apparatus as set forth in wherein the shell comprises a plurality of segments claim 1 , each segment having an inlet and an outlet.9. The heat exchange apparatus as set forth in wherein the shell comprises a vertical segment and a horizontal segment claim 8 , the ...

Production method for trichlorosilane, and pipe

To prevent solidified aluminum chloride from adhering to and accumulating on a pipe and also prevent stress-corrosion cracking in the pipe, a method for producing trichlorosilane includes a cooling step of cooling a discharge gas that is discharged from a fluidized-bed reactor and that contains the trichlorosilane, the cooling step involving causing a fluid to flow through a space ( 4 ) inside a side wall ( 3 ) of a pipe ( 10 ), the pipe being a pipe for discharging the discharge gas from the fluidized-bed reactor, in such a manner that the side wall ( 3 ) has a surface ( 1 a ) having a temperature of not lower than 110° C.

Process for the production of polymers using a loop reactor

A polymer can be prepared using a loop reactor and process including feeding a process stream through the loop reactor and maintaining the loop reactor at a steady state by controlling a flow of coolant fluid to maintain a temperature in the loop reactor at a preset point. The temperature in the loop reactor may be maintained at a preset point by using a coolant fluid flow controller and valve unit having a substantially linear response over the normal operating range of the controller and valve unit. The normal operating range of the controller and valve unit may be sufficient to provide a flow range not limiting to the throughput of the loop reactor.

Process for the production of polymers using a loop reactor

A polymer can be prepared using a loop reactor and process including feeding a process stream through the loop reactor and maintaining the loop reactor at a steady state by controlling a flow of coolant fluid to maintain a temperature in the loop reactor at a preset point. The temperature in the loop reactor may be maintained at a preset point by using a coolant fluid flow controller and valve unit having a substantially linear response over the normal operating range of the controller and valve unit. The normal operating range of the controller and valve unit may be sufficient to provide a flow range not limiting to the throughput of the loop reactor.

Process for the production of polymers using a loop reactor

A polymer can be prepared using a loop reactor and process including feeding a process stream through the loop reactor and maintaining the loop reactor at a steady state by controlling a flow of coolant fluid to maintain a temperature in the loop reactor at a preset point. The temperature in the loop reactor may be maintained at a preset point by using a coolant fluid flow controller and valve unit having a substantially linear response over the normal operating range of the controller and valve unit. The normal operating range of the controller and valve unit may be sufficient to provide a flow range not limiting to the throughput of the loop reactor.

Design of vertical reactor with tube bundle and indirect heat exchange for catalytic gas phase reactions, specifies configuration to control flow conditions

Design of vertical reactor with tube bundle and indirect heat exchange for catalytic gas phase reactions, specifies configuration to control flow conditions which are distributed over the outer and/or inner circumference of the tube bundle. Design of vertical reactor with tube bundle and indirect heat exchange for catalytic gas phase reactions, specifies configuration to control flow conditions which are distributed over the outer and/or inner circumference of the tube bundle (6). Pipe bundle distribution and/or dimensions are varied in all radial directions over the reactor circumference, for control of flow resistance. A radial dimension of at least one type of baffle sheet (22) is varied over the circumference to control flow conditions approaching the tubes. Cross sections of flow openings in baffles are varied to control flow conditions.

Annular channel for external supply and return of heat exchange medium to vertical tube reactor, has openings equipped with flow controls

Opening(s) (34) are equipped with flow controls. Preferred Features: The opening height is 0.05 x to 1 x the available height, i.e. the height of the annular channel or spacing between tube bases and the adjacent deflection baffle (22). Individual openings along the reactor circumference are most preferably 0.5-0.65 times the opening interval along it. Opening (34) geometry varies around the circumference. Opening(s) near the inlet are small, becoming larger and then smaller, further away from it. Flow control is by deflection baffles. Connections for valves and a circulation pump are provided. An expansion joint runs around the reactor casing.

Reactor for catalytic gas phase oxidation

The temperature distribution of a heating medium in the reactor is allayed and the occurrence of hot spots is repressed. In a shell-and-tube type reactor provided with donut type (202) and disc type baffle plates (203), reaction tubes (204) are disposed even in the holes formed in the donut type baffle plates (202) and an empty space devoid of a configuration of the reaction tubes is formed at the center of the shell. According to this invention, (meth)acrylic acid and/or (meth) acrolein can be produced at a low energy by catalytic gas phase oxidation of propylene- or isobutylene-containing gas.

Method for catalytic gas phase oxidation

In the reaction of catalytic gas phase oxidation by means of a shell-and-tube type reactor adapted to circulate a heating medium (10a) to the shell (1) of the reactor through the medium of a circulation device (30) connecting an annular conduit connected thereto, a method for the catalytic gas phase oxidation characterized by subjecting a part of the heating medium extracted from the shell (1) of the reactor to heat exchange, introducing the heating medium (10a) resulting from the heat exchange into the proximity of a heating medium circulation inlet (31) on the inlet side of the circulation device or the annular conduit on the outlet side of the reactor. The flow rate of the heating medium after the heat exchange is preferred to be in the range of 2 - 40 vol.% based on the flow rate of the heating medium within the shell of the reactor and the temperature difference of the heating medium at the inlet and the outlet to be in the range of 15 - 150°C. According to this invention, it is made possible to reduce evenly the hot spots in the reaction tubes, improve the yield of the product aimed at, and implement a reaction of catalytic gas phase oxidation of propylene or isobutylene.

Method for modifying the temperature of a multi-tube reactor

Procedure for varying the temperature of a tube bundle reactor (1) for catalytic gas-phase reactions during start-up and shut-down of the reactor, comprises (a) changing the temperature of the heat transfer liquid during the circulation of the heat transfer liquid through a heat exchanger, and (b) passing a temperature-altering gas through the reaction tubes, at least when the heat transfer liquid is not yet or not any longer circulated. Procedure for varying the temperature of a tube bundle reactor (1) for catalytic gas-phase reactions during start-up and shut-down of the reactor, comprises (a) changing the temperature of the heat transfer liquid during the circulation of the heat transfer liquid through a heat exchanger, and (b) passing a temperature-altering gas through the reaction tubes, at least when the heat transfer liquid is not yet or not any longer circulated, where: the temperature of the temperature-altering gas (55) is limited at its entry into the reaction tubes (8) to be above a minimum value during the start-up process and to be below a maximum value during the shut-down process and/or the volume flow of the temperature-altering gas is also limited to be above a minimum value in such a manner that over each time period that begins with the first feeding of the temperature-altering gas, the time-averaged temperature alteration velocity of the temperature-altering gas does not exceed 30[deg] C/hour during its exit from the reaction tubes; and the tube bundle reactor exhibits a primary reactor part with a bundle of vertically arranged reaction tubes, an upper and a lower tube plate, which are tightly connected with the upper and the bottom ends of the reaction tubes, and a reactor jacket that encloses the tube bundle (9), and where in normal operation mode, the outer sides of the reaction tubes are flowed through by a heat transfer fluid that exhibits a melting point in the range of 100-450[deg] C and is circulated in at least a cycle through the ...

fluidized bed reactor and replaceable insert.

REACTOR FOR TESTING CATALYST SYSTEMS

Process of producing methanol

METHANOL IS CATALYTICALLY PRODUCED FROM A SYNTHESIS GAS CONTAINING HYDROGEN AND CARBON OXIDES ON COPPER-CONTAINING CATALYSTS AT PRESSURES IN THE RANGE FROM 20 TO 120 BAR AND TEMPERATURES IN THE RANGE FROM 130 TO 350?C. THE SYNTHESIS GAS IS FIRST OF ALL PASSED THROUGH A FIRST SYNTHESIS REACTOR, IN WHICH THE CATALYST IS PROVIDED IN TUBES SURROUNDED BY WATER AS A COOLANT WHICH IS BOILING AT AN ELEVATED PRESSURE. FROM THE FIRST REACTOR A FIRST MIXTURE CONTAINING GASES AND METHANOL IS WITHDRAWN AND PASSED THROUGH A SECOND SYNTHESIS REACTOR. IN THE SECOND REACTOR THE CATALYST IS COOLED WITH SYNTHESIS GAS.

Reactor apparatus

A reactor apparatus is provided with an outer jacket surrounding the reaction vessel. The jacket is formed by a plurality of baffles having triangular cross-section. At least some of the baffles are provided with adjustable deflectors. Heat exchanging fluid is admitted into the space between the jacket and the vessel outer wall. The triangular cross-section of the baffles and adjustable deflectors allow optimum regulation of reaction conditions, for example reaction temperature and in effect increase reactor productivity.

Air-cooled heat exchangers

A plant or refinery may include equipment such as reactors, heaters, heat exchangers, regenerators, separators, or the like. Types of heat exchangers include shell and tube, plate, plate and shell, plate fin, air cooled, wetted-surface air cooled, or the like. Operating methods may impact deterioration in equipment condition, prolong equipment life, extend production operating time, or provide other benefits. Mechanical or digital sensors may be used for monitoring equipment, and sensor data may be programmatically analyzed to identify developing problems. For example, sensors may be used in conjunction with one or more system components to detect and correct maldistribution, cross-leakage, strain, pre-leakage, thermal stresses, fouling, vibration, problems in liquid lifting, conditions that can affect air-cooled exchangers, conditions that can affect a wetted-surface air-cooled heat exchanger, or the like. An operating condition or mode may be adjusted to prolong equipment life or avoid equipment failure.

Shell-and-tube type reactor for catalytic gas phase reactions

催化气相氧化反应器

本发明能够减小载热体在反应器中的温度分布，并且抑制过热点的出现。在管壳式反应器中安装有圆环形和圆盘形挡板，反应管均匀地设置在圆环形挡板上形成的孔中，在壳体中心形成一个没有配置反应管的空区。根据本发明，通过含丙烯或异丁烯的气体的催化气相氧化，能够在低能耗的情况下生产(甲基)丙烯酸和/或(甲基)丙烯醛。

Method and apparatus for reducing by-product content in carbonaceous material

본 발명은 탄소질 물질을 처리하여 이로부터 부산물을 제거하기 위한 각종 장치 및 방법에 관한 것이다. 더욱 구체적으로 말해서, 본 발명은 불활성 가스를 진공하에 탄소질 물질 중으로 주입하거나, 진공을 통제된 방식으로 적용하거나 적용하지 않고 증기를 탄소질 물질 중으로 주입하여 탄소질 물질의 충진물을 더욱 일관되게 처리함에 의한 탄소질 물질의 처리방법에 관한 것이다. The present invention relates to various apparatuses and methods for treating carbonaceous materials to remove by-products therefrom. More particularly, the present invention relates to a method of injecting an inert gas into a carbonaceous material under vacuum, or injecting the vapor into a carbonaceous material without applying or applying the vacuum in a controlled manner to more consistently treat the filler of the carbonaceous material To a method for treating a carbonaceous material.

Reactor system, absorbent and method of conducting reaction in fed material

FIELD: process engineering. SUBSTANCE: invention relates to reactor system, absorbent, and method of conducting reaction in fed material. Reactor system comprises cleaning zone containing absorbent and reaction zone comprising catalyst and located downstream of cleaning zone. Proposed method of conducting reaction in fed material containing hydrocarbon comprises the steps whereat material components are brought in contact with absorbent to reduce amount of impurities in said material and in contact with catalyst to make reaction products. Absorbent for removal of said impurities contains silver, alkaline or alkali-earth metal in amount of 50 mmol/kg and substrate layer from aluminium oxide with surface area of 75 m 2 /g. EFFECT: higher catalyst efficiency. 23 cl, 2 dwg, 1 tbl, 3 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2 474 470 (13) C2 (51) МПК B01J B01J B01J B01D C07D 8/06 (2006.01) 20/04 (2006.01) 23/54 (2006.01) 53/04 (2006.01) 301/10 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (21)(22) Заявка: 2009147028/05, 15.05.2008 (24) Дата начала отсчета срока действия патента: 15.05.2008 (73) Патентообладатель(и): ШЕЛЛ ИНТЕРНЭШНЛ РИСЕРЧ МААТСХАППИЙ Б.В. (NL) R U Приоритет(ы): (30) Конвенционный приоритет: 18.05.2007 US 60/938,890 (72) Автор(ы): МАТУШ Марек (US) (43) Дата публикации заявки: 27.06.2011 Бюл. № 18 2 4 7 4 4 7 0 (45) Опубликовано: 10.02.2013 Бюл. № 4 (56) Список документов, цитированных в отчете о поиске: ЕР 1121977 А2, 08.08.2001. WO 2004/039496 A1, 13.05.2004. US 2004/0220414 A1, 04.11.2004. RU 2126296 C1, 20.02.1999. 2 4 7 4 4 7 0 R U (86) Заявка PCT: US 2008/063722 (15.05.2008) C 2 C 2 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 18.12.2009 (87) Публикация заявки РСТ: WO 2008/144402 (27.11.2008) Адрес для переписки: 129090, Москва, ул. Б. Спасская, 25, стр.3, ООО "Юридическая фирма Городисский и Партнеры" (54) РЕАКТОРНАЯ СИСТЕМА, АБСОРБЕНТ И СПОСОБ ОСУЩЕСТВЛЕНИЯ РЕАКЦИИ В ПОДАВАЕМОМ ...

Vapor-phase catalytic oxidation process

FIELD: industrial organic synthesis. SUBSTANCE: invention relates to a process of catalytic oxidation in vapor phase, which prevents emergence of non-controllable reaction and premature poisoning of catalyst in (meth)acrylic acid synthesis. Vapor-phase catalytic oxidation process, wherein feed gas is supplied for oxidation to reaction tubes of multi-tubular reactor provided with multiple, disposed in reactor shell, reaction tubes filled with catalyst and multiple deflectors serving to modify direction of heat-carrier stream introduced into reactor shell. Temperature is measured in catalyst, which is placed in a reaction tube and is not connected with at least one deflector, as well as temperature in catalyst, which is placed in a reaction tube and is connected with all deflectors. EFFECT: ensured continuous production of (meth)acrylic acid with high yield and for a long period of time. 12 cl, 6 dwg, 4 ex ÐÎÑÑÈÉÑÊÀß ÔÅÄÅÐÀÖÈß RU (19) (11) 2 295 383 (13) C2 (51) ÌÏÊ B01J 8/06 (2006.01) C07C 27/14 (2006.01) C07C 47/22 (2006.01) ÔÅÄÅÐÀËÜÍÀß ÑËÓÆÁÀ ÏÎ ÈÍÒÅËËÅÊÒÓÀËÜÍÎÉ ÑÎÁÑÒÂÅÍÍÎÑÒÈ, ÏÀÒÅÍÒÀÌ È ÒÎÂÀÐÍÛÌ ÇÍÀÊÀÌ (12) ÎÏÈÑÀÍÈÅ ÈÇÎÁÐÅÒÅÍÈß Ê ÏÀÒÅÍÒÓ (21), (22) Çà âêà: 2004130289/15, 11.03.2003 (24) Äàòà íà÷àëà îòñ÷åòà ñðîêà äåéñòâè ïàòåíòà: 11.03.2003 (30) Êîíâåíöèîííûé ïðèîðèòåò: 11.03.2002 (ïï.1-12) JP 2002-64620 (73) Ïàòåíòîîáëàäàòåëü(è): ÌÈÖÓÁÈÑÈ ÊÅÌÈÊÀË ÊÎÐÏÎÐÅÉØÍ (JP) (43) Äàòà ïóáëèêàöèè çà âêè: 10.04.2005 R U (72) Àâòîð(û): ÑÀÊÀÊÓÐÀ ßñóþêè (JP), ßÄÀ Ñóõåé (JP), ÄÇÈÍÍÎ Êèìèêàöó (JP), ÕÎÑÀÊÀ Õèðîòèêà (JP), ÑÓÇÓÊÈ Éîñèðî (JP) (45) Îïóáëèêîâàíî: 20.03.2007 Áþë. ¹ 8 2 2 9 5 3 8 3 (56) Ñïèñîê äîêóìåíòîâ, öèòèðîâàííûõ â îò÷åòå î ïîèñêå: ÅÐ 1080780 À1, 07.03.2001. US 5821390 À, 13.10.1998. WO 0142184 À1, 14.06.2001. RU 2180266 C1, 13.11.2000. RU 2198868 Ñ2, 20.02.2003. (85) Äàòà ïåðåâîäà çà âêè PCT íà íàöèîíàëüíóþ ôàçó: 11.10.2004 2 2 9 5 3 8 3 R U (87) Ïóáëèêàöè PCT: WO 03/076373 (18.09.2003) C 2 C 2 (86) Çà âêà PCT: JP 03/02855 (11.03.2003) Àäðåñ äë ïåðåïèñêè: 129010, ...

制造甲醇的方法

在20-120巴压力及130-350℃温度下，含氢气及氧化碳的合成气在含铜催化剂上被催化生成甲醇。首先将合成气通过其中催化剂被装入管中的第一合成反应器中，此管用在高压下沸腾的水冷却剂环绕，从第一反应器，抽出含气体及甲醇蒸汽的第一混合物，并使之通过第二合成反应器。在第二反应器中，催化剂用合成气进行冷却。

Catalytic gas phase oxidation method

열매체를 환상도관을 접속하는 순환장치를 통해 반응기 쉘에 순환시키는 다관식 반응기에 의한 접촉기상산화반응에 있어서, 반응기쉘로부터 인출한 열매체의 일부를 열교환하고, 또한 상기 열교환후의 열매체를 도입하는 열매체도입구가, 상기 순환장치의 열매체순환구 근방 또는 환상도관인 것을 특징으로 하는 접촉기상산화방법이다. 상기 열교환후의 열매체량은 반응기 쉘내의 열매체량의 2∼40용량%의 범위이고, 또한 열매체의 입구와 출구와의 온도차는 15∼150℃인 것이 바람직하다. 본 발명에 의하면, 균일하게 반응관의 열점을 감소할 수 있으며, 이에 따라 원하는 생성물을 효과적으로, 프로필렌 또는 이소부틸렌의 접촉기상산화반응을 행할 수 있다. In the catalytic gas phase oxidation reaction of a multi-pipe reactor in which a heat medium is circulated to a reactor shell through a circulation device connecting an annular conduit, a heat medium for heat-exchanging a part of the heat medium withdrawn from the reactor shell, and also introducing the heat medium after the heat exchange. A contact gas phase oxidation method is characterized in that the inlet is in the vicinity of the heat medium circulation port of the circulation device or an annular conduit. The heat medium amount after the heat exchange is in the range of 2 to 40% by volume of the heat medium amount in the reactor shell, and the temperature difference between the inlet and the outlet of the heat medium is preferably 15 to 150 ° C. According to the present invention, it is possible to uniformly reduce the hot spot of the reaction tube, whereby the desired product can be effectively subjected to catalytic gas phase oxidation of propylene or isobutylene.

Fluidized bed reactor with gas cooler

A new reactor apparatus that can be used to carry out chemical reactions in a fluidized catalyst bed at high temperatures with reduced afterburning or other undesirable downstream side reactions. One application is the manufacture of acrylonitrile.

Reactor apparatus

A new reactor apparatus that can be used to carry out chemical reactions in a fluidized catalyst bed at high temperatures with reduced afterburning or other undesirable downstream side reactions.

Fluidized bed reactor with gas cooler

A new reactor apparatus that can be used to carry out chemical reactions in a fluidized catalyst bed at high temperatures with reduced afterburning or other undesirable downstream side reactions. One application is the manufacture of acrylonitrile.

带有气体冷却器的流化床反应器

一种新的反应装置，可用于在高温下在流化催化剂床中进行化学反应，并可减少二次燃烧或其它不合需要的下游副反应。一种应用是生产丙烯腈。

Reactor apparatus

A NEW REACTOR APPARATUS THAT CAN BE USED TO CARRY OUT CHEMICAL REACTIONS IN A FLUIDIZED CATALYST BED AT HIGH TEMPERATURES WITH REDUCED AFTERBURNING OR OTHER UNDESIRABLE DOWNSTREAM SIDE REACTIONS.

Реакторное устройство

Изобретение относится к химической промышленности и может быть использовано для проведения химических реакций в псевдоожиженном слое катализатора при высоких температурах и в газовой фазе с пониженным выгоранием или иными нежелательными побочными реакциями. В зоне плотного слоя реакторного устройства на решетке реакторного устройства находится слой порошкового катализатора. Над решеткой расположена система распределения газа. Зона выделения катализатора расположена над зоной плотного слоя. Зона разбавленной фазы расположена над зоной выделения. Внутри зоны разбавленной фазы размещен газовый холодильник. Внутри реакционного сосуда расположено устройство для отделения катализатора и средство для возврата отделенного катализатора в зону плотного слоя. Изобретение обеспечивает снижение степени неконтролируемого окисления и уменьшение потерь продуктов и исходных материалов. 17 з.п. ф-лы, 11 ил. РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2 359 747 (13) C2 (51) МПК B01J 8/18 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ, ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (21), (22) Заявка: 2005134690/12, 06.05.2004 (24) Дата начала отсчета срока действия патента: 06.05.2004 (43) Дата публикации заявки: 10.04.2006 2 3 5 9 7 4 7 R U (85) Дата перевода заявки PCT на национальную фазу: 09.11.2005 C 2 C 2 (56) Список документов, цитированных в отчете о поиске: US 4158036 А, 12.06.1979. FR 937899 А, 30.08.1948. GB 2075360 А, 18.11.1981. ЕР 0446379 A1, 18.09.1991. GB 1121909 A, 31.07.1968. EP 1202017 A2, 02.05.2002. EP 0546677 A1, 16.06.1993. SU 1554202 A1, 20.06.1996. (73) Патентообладатель(и): ИНЕОС ЮЭсЭй ЭлЭлСи (US) (86) Заявка PCT: US 2004/014403 (06.05.2004) (87) Публикация PCT: WO 2004/101136 (25.11.2004) Адрес для переписки: 119034, Москва, Пречистенский пер., 14, стр.1, 4 этаж, "Гоулингз Интернэшнл Инк.", В.Н.Дементьеву (54) РЕАКТОРНОЕ УСТРОЙСТВО (57) Реферат: Изобретение относится к химической промышленности и может быть использовано для проведения ...

Reactor apparatus

Fluidized bed reactor with gas cooler

Reactor apparatus

A new reactor apparatus that can be used to carry out chemical reactions in a fluidized catalyst bed at high temperatures with reduced afterburning or other undesirable downstream side reactions.

Fluidized bed reactor with gas cooler

A new reactor apparatus that can be used to carry out chemical reactions in a fluidized catalyst bed at high temperatures with reduced afterburning or other undesirable downstream side reactions. One application is the manufacture of acrylonitrile.

用于测试催化剂体系的反应器

本文介绍了一种用于测试催化剂体系的反应器，该反应器内部具有多个相互平行排列催化剂管(2)，管的末端焊入管板。该反应器每个末端还装有顶盖(3)，且各顶盖划定了顶盖空间(4)的范围。流动的反应介质(5)经一个顶盖空间(4)供入催化剂管(2)，流经催化剂管(2)并经另一个顶盖空间(4)排出。该反应器还装配有换热介质回路。在该回路中换热介质(6)从反应器的一端供入，流经催化剂管(2)之间的中间区域，从反应器的另一末端流出。在该反应器中将催化剂管(2)分布在温度互不相同的两个或者更多催化剂管区(7)。

Fixed-bed catalytic reactor

FIELD: chemistry. SUBSTANCE: invention relates to chemical industry and can be used particularly for synthesising ammonia, methanol, formaldehyde or styrene. Catalyst layers are put on the axis of a cylindrical body of a radial reactor. The layers have inlet sides, through which gaseous reagents enter, and outlet sides through which a reaction mixture comes out, and several heat exchangers distributed on the circular part of the layers. In the first catalyst layer heat exchangers are only placed on the part of this layer near its outlet side. In the second layer heat exchangers are only placed on the part of this second catalyst layer near its inlet side. In the method of catalytic synthesis, gaseous reagents are passed through the first adiabatic zone in the first catalyst layer, and then through the first pseudoisothermal zone in the first catalyst layer, through the second pseudoisothermal zone in the second catalyst layer and, finally, through the second adiabatic zone in the second catalyst layer. EFFECT: increased conversion output of reactors with simultaneous reduction of energy consumption, capital expenditure and expenses on servicing and repair. 7 cl, 8 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2 361 657 (13) C2 (51) МПК B01J 8/04 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ, ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (30) Конвенционный приоритет: 29.07.2004 EP 04017905.3 (73) Патентообладатель(и): МЕТАНОЛ КАСАЛЕ С.А. (CH) (43) Дата публикации заявки: 10.09.2008 (45) Опубликовано: 20.07.2009 Бюл. № 20 (85) Дата перевода заявки PCT на национальную фазу: 28.02.2007 2 3 6 1 6 5 7 R U (87) Публикация PCT: WO 2006/010565 (02.02.2006) Адрес для переписки: 101000, Москва, М.Златоустинский пер., 10, кв.15, "ЕВРОМАРКПАТ", пат.пов. И.А.Веселицкой, рег. № 11 (54) РЕАКТОР С НЕПОДВИЖНЫМ СЛОЕМ КАТАЛИЗАТОРА расположены только в части этого второго (57) Реферат: слоя катализатора ближе к его входной Изобретение относится к химической ...

Reactor for catalytic gas phase oxidation

본 발명의 반응기에서 열매체의 온도 분포가 완화되고 핫 스팟의 발생이 억제된다. 도넛형과 원반형 배플판이 구비된 다관식 반응기에서, 반응 튜브는 도넛형 배플판에 형성된 기공에 균등하게 분포되고, 상기 반응 튜브의 배열이 없는 빈 공간이 쉘의 중앙에 형성된다. 본 발명에 따르면, (메타)아크릴산 및/또는 (메타)아크롤레인이 프로필렌 또는 이소부틸렌을 함유하는 기체의 접촉 기상 산화에 의해 낮은 에너지로 생산될 수 있다. In the reactor of the present invention, the temperature distribution of the heat medium is relaxed and the occurrence of hot spots is suppressed. In a multi-tubular reactor with donut and disc baffle plates, the reaction tubes are evenly distributed in the pores formed in the donut baffle plates, and an empty space without an arrangement of the reaction tubes is formed in the center of the shell. According to the invention, (meth) acrylic acid and / or (meth) acrolein can be produced at low energy by catalytic gas phase oxidation of a gas containing propylene or isobutylene.

Fixed bed catalytic reactor

Hydrogen purifying apparatus

본 발명은, CO를 산화시키는 촉매층을 갖는 촉매반응부와, 이산화탄소, CO 및 주성분인 수소가스를 포함하는 개질가스를 원료가스공급로를 지나서 상기 반응부에 공급하는 원료가스공급부와, 상기 원료가스공급로의 도중에서 상기 개질가스에 산화제가스를 공급하는 산화제가스공급부를 구비하고, 상기 개질가스 중의 CO를 산화 및 제거하는 수소정제장치에 관한 것이다. 그리고, 상기 촉매층의 상류측 부분을 냉각하는 수단과, 하류측 부분의 가열하는 수단을 구비함으로써, 일산화탄소를 선택적으로 산화하는 촉매의 능력을 충분히 발휘시키고 온도, 공급공기량 및 일산화탄소처리량 등의 사용조건이 변화하더라도, 안정되게 개질가스 중의 일산화탄소농도를 저하시킬 수 있다. The present invention provides a catalytic reaction unit having a catalyst layer for oxidizing CO, a raw material gas supply unit for supplying a reforming gas containing carbon dioxide, CO, and hydrogen gas as a main component to the reaction unit via a source gas supply path, and the source gas An oxidant gas supply unit for supplying an oxidant gas to the reformed gas in the middle of a supply path, and relates to a hydrogen purification device for oxidizing and removing CO in the reformed gas. And means for cooling the upstream portion of the catalyst layer and means for heating the downstream portion, thereby fully exhibiting the ability of the catalyst to selectively oxidize carbon monoxide and providing conditions for use such as temperature, supply air amount and carbon monoxide treatment amount. Even if it changes, the concentration of carbon monoxide in the reformed gas can be stably lowered.

Internal combustion heat exchange reactor for endothermic reaction in fixed bed

FIELD: process engineering. ^ SUBSTANCE: invention relates to reactors used in steam reforming reactions. Proposed reactor comprises chamber, appliances to feed charge via catalytic zone in fixed bed, appliances to collect gas wastes flowing out of catalytic zone and appliances to heat said zone. Appliances to collect gas wastes have channels penetrating through catalytic zone and distributed therein and arranged between heating appliances. Heating appliances are contained in shells, in section immersed in catalytic zone. Shells are closed at one ends and closed on opposite ends. Open end is secured to top tubular plate that confines collection chamber arranged above catalytic zone. Heating appliances comprises combustion zone arranged nearby catalytic zone, appliances to feed combustion zone with oxidising gas mix and combustible gas, and appliances to discharge combustion gas wastes. ^ EFFECT: optimum heat distribution. ^ 23 cl, 6 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2 424 847 (13) C2 (51) МПК B01J 8/02 (2006.01) C01B 3/26 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ, ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (21)(22) Заявка: 2008141143/05, 16.03.2007 (24) Дата начала отсчета срока действия патента: 16.03.2007 (73) Патентообладатель(и): ИФП (FR) 2 4 2 4 8 4 7 (43) Дата публикации заявки: 27.04.2010 Бюл. № 12 (45) Опубликовано: 27.07.2011 Бюл. № 21 (56) Список документов, цитированных в отчете о поиске: US 3909299 А, 30.09.1975. ЕР 1505036 А2, 09.02.2005. ЕР 1516663 А2, 23.03.2005. RU 2265480 С2, 10.12.2005. 2 4 2 4 8 4 7 R U (86) Заявка PCT: FR 2007/000466 (16.03.2007) C 2 C 2 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 17.10.2008 (87) Публикация заявки РСТ: WO 2007/118950 (25.10.2007) Адрес для переписки: 129090, Москва, ул.Б.Спасская, 25, стр.3, ООО "Юридическая фирма Городисский и Партнеры", пат.пов. А.В.Мицу, рег.№ 364 (54) ТЕПЛООБМЕННЫЙ РЕАКТОР ВНУТРЕННЕГО СГОРАНИЯ ДЛЯ ЭНДОТЕРМИЧЕСКОЙ РЕАКЦИИ В ...

Apparatus for synthesis of anhydrous hydrogen halide and anhydrous carbon dioxide

FIELD: chemistry. SUBSTANCE: system for treatment and/or decomposition of organic halide fluids comprises a dual reactor unit having a first reactor within a first heat sink vessel, a second reactor within a second heat sink vessel and a third heat sink balance vessel. The first reactor and the second reactor are hydraulically connected such that a product of a reaction that occurs in one reactor is fed into the other reactor. The dual reactor unit has a first heat sink vessel having a first reactor, a second heat sink vessel having a second reactor, a third heat sink balance vessel and a circulator. The first heat sink vessel is hydraulically connected to the second heat sink vessel, the third heat sink balance vessel and the circulator. EFFECT: invention provides efficient treatment of fluids and reduces environmental pollution. 20 cl, 2 dwg, 6 tbl, 6 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (51) МПК B01J 8/04 (11) (13) 2 529 232 C1 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ (21)(22) Заявка: ИЗОБРЕТЕНИЯ К ПАТЕНТУ 2013142581/05, 12.12.2011 (24) Дата начала отсчета срока действия патента: 12.12.2011 (72) Автор(ы): ТАРАНКОН III Грегорио (US) (73) Патентообладатель(и): Мидуэст Рефриджерентс, ЭлЭлСи (US) Приоритет(ы): (30) Конвенционный приоритет: R U 12.04.2011 US 61/474,657; 04.05.2011 US 13/100,942 (45) Опубликовано: 27.09.2014 Бюл. № 27 3445292 A, 20.05.1969. US 4282339A, 04.08.1981. RU 2282492 C2, 27.08.2006 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 12.11.2013 (86) Заявка PCT: US 2011/064365 (12.12.2011) 2 5 2 9 2 3 2 (56) Список документов, цитированных в отчете о поиске: US 2007/0049781 A1, 01.03.2007. US 2 5 2 9 2 3 2 R U WO 2012/141750 (18.10.2012) Адрес для переписки: 191036, Санкт-Петербург, а/я 24, "НЕВИНПАТ" (54) УСТРОЙСТВО ДЛЯ СИНТЕЗА БЕЗВОДНОГО ГАЛОИДА ВОДОРОДА И БЕЗВОДНОГО ДИОКСИДА УГЛЕРОДА (57) Реферат: Изобретение относится к устройству для реактора содержит первый теплопоглощающий синтеза текучих сред ...

Реакторная система для получения газообразных продуктов

1. Прямоточный реактор с нисходящими потоками для превращения жидкого исходного сырья в неконденсирующийся газообразный продукт с использованием гетерогенного катализатора, включающий ! реакционную камеру, содержащую по меньшей мере одну реакционную трубку, содержащую гетерогенный катализатор; ! входное отверстие, давление в котором равно Pi, выполненное с возможностью подавать жидкий питающий поток в верхнюю часть реакционной камеры; ! выходное отверстие, давление в котором равно Ро, выполненное с возможностью выпускать неконденсирующийся газообразный продукт и жидкий выходящий поток из нижней части реакционной камеры; и ! в котором Pi больше, чем Ро. ! 2. Реактор по п.1, в котором реакционная камера включает ряд реакционных трубок, каждая из которых содержит катализатор, внешнюю оболочку, выполненную с возможностью заключать в себе по меньшей мере часть реакционных трубок, и систему нагрева, выполненную с возможностью вводить теплоноситель внутрь оболочки для осуществления нагревания реакционных трубок. ! 3. Реактор по п.1, в котором катализатор включает по меньшей мере один металл группы VIIIВ, и в котором исходное сырье включает воду и по меньшей мере один растворимый в воде кислородсодержащий С2+ углеводород. ! 4. Реактор по п.3, в котором металл группы VIIIB выбирают из группы, состоящей из платины, никеля, палладия, рутения, родия, иридия, железа, их сплавов и их смесей, и в котором кислородсодержащий углеводород представляет собой кислородсодержащий С2-6 углеводород. ! 5. Реактор по п.4, в котором катализатор дополнительно включает второй каталитический материал, выбранный из группы, состоящей из металлов групп� РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2009 121 628 (13) A (51) МПК B01J 8/06 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ, ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21)(22) Заявка: 2009121628/05, 20.12.2007 (71) Заявитель(и): Вайрент Энерджи Системз, Инк. (US) Приоритет(ы): (30) Конвенционный приоритет: 20.12.2006 US 60/876 ...

氢精制装置

本发明的氢精制装置具备以下3部分：即具有使CO氧化的催化剂层的催化剂反应部分；将含有二氧化碳、CO及作为主成分的氢气的转化气体经过原料气体供给通道导入前述反应部分的原料气体供给部分；设置在前述原料气体供给通道中的向前述转化气体提供氧化剂气体的氧化剂气体供给部分。由于具备冷却前述催化剂层上游侧部分的装置和加热下游侧部分的装置，所以可使催化剂的选择性氧化CO的能力充分发挥，即使温度、供气量及CO处理量等条件发生变化，也能稳定降低转化气体中的CO浓度。

Каталитический реактор для экзотермических процессов, протекающих в газ-твердой фазе с невысокой разностью температур

Catalyst arrangement

Катализаторная трубка для риформинга

РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2019 115 952 A (51) МПК C01B 3/38 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21)(22) Заявка: 2019115952, 25.10.2017 (71) Заявитель(и): ТЕКНИП ФРАНС (FR) Приоритет(ы): (30) Конвенционный приоритет: 25.10.2016 EP 16195490.4 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 27.05.2019 R U (43) Дата публикации заявки: 27.11.2020 Бюл. № 33 (72) Автор(ы): ФАРАЧЕ, Антонио (NL), ВАЛЬСПУРГЕР, Стефан (NL) (86) Заявка PCT: (87) Публикация заявки PCT: WO 2018/077969 (03.05.2018) R U (54) КАТАЛИЗАТОРНАЯ ТРУБКА ДЛЯ РИФОРМИНГА (57) Формула изобретения 1. Катализаторная трубка для регенеративной каталитической конверсии технологического газа в производственной печи, содержащая - впуск катализаторной трубки для введения технологического газа в катализаторную трубку и выпуск катализаторной трубки для выведения технологического газа из катализаторной трубки, причем указанные впуск и выпуск расположены на противоположных концах катализаторной трубки; - наружную реакторную трубку (1, 11); - внутреннюю трубку (5, 15), коаксиально простирающуюся внутри наружной реакторной трубки (1, 11); - границу (3, 13) раздела, расположенную между внутренней стенкой наружной реакторной трубки (1, 11) и наружной стенкой внутренней трубки (5, 15); - первый кольцевой канал для каталитической конверсии технологического газа, ограниченный между внутренней стенкой наружной реакторной трубки (1, 11) и наружной стенкой границы (3, 13) раздела, причем указанный канал загружен каталитическим материалом; - второй кольцевой канал для технологического газа, проходящего противоточно или прямоточно технологическому газу, проходящему по первому кольцевому каналу, ограниченный между внутренней стенкой границы (3, 13) раздела и наружной стенкой внутренней трубки (5, 15); Стр.: 1 A 2 0 1 9 1 1 5 9 5 2 A Адрес для переписки: 101000, Москва, ул. Мясницкая, 13, стр. 5, ООО "Союзпатент", С.Б. Фелициной 2 0 1 9 1 1 5 9 5 2 EP ...

[UNK]

Method and device for injecting oxygen into a reaction gas flowing through a synthesis reactor

Die Erfindung betrifft einen Synthesereaktor, der eine Vorrichtung zur Eindüsung von sauerstoffhaltigem Gas in ein Reaktionsgas umfasst, wobei in Strömungsrichtung des Reaktionsgases vor der Einrichtung zur Aufnahme einer Katalysatorfüllung ein Sauerstoffverteilelement aus zwei Rohrböden und einer Vielzahl von Gasführungsrohren zur Durchleitung des Einsatzgases vorgesehen ist und der Sauerstoff dem Zwischenraum um und zwischen den Gasführungsrohren zuführbar ist. Dabei ist vertikal zu den Gasführungsrohren mindestens ein Leitblech angeordnet, welches den Zwischenraum in mindestens zwei Verteilerräume teilt, wobei die Verteilerräume fluidisch durch eine oder mehrere Öffnungen miteinander verbunden sind oder ineinander übergehen. Weiterhin führt eine Gasleitung in den ersten Unterraum, über welche der Sauerstoff zuführbar ist, und der in Strömungsrichtung der untere Rohrboden ist und mit einer Vielzahl von Öffnungen in Form von Düsen, Bohrungen oder dergleichen sehen ist, über welche der Sauerstoff den Zwischenraum verlassen kann und in einer unterhalb des unteren Rohrbodens vorgesehene feststofffreie Gasmischzone geleitet werden kann. The invention relates to a synthesis reactor comprising a device for injecting oxygen-containing gas into a reaction gas, wherein in the flow direction of the reaction gas upstream of the means for receiving a catalyst filling an oxygen distribution element of two tube sheets and a plurality of gas guide tubes for the passage of the feed gas is provided and the oxygen the space around and between the gas guide tubes can be fed. In this case, at least one baffle is arranged vertically to the gas guide tubes, which divides the intermediate space into at least two distribution spaces, wherein the distribution spaces are fluidly interconnected by one or more openings or merge into one another. Furthermore, a gas line into the first subspace, via which the oxygen is supplied, and which is in the flow direction of the lower tube sheet and is ...

Method and apparatus for the fluidized catalytic treatment of fluid reactants

Reactor for catalytic gas phase oxidation.

Carbon monoxide conversion process and reactor.

Tube bundle reactor, useful for catalytic gas phase reactions, comprises bundle of vertically arranged reaction tubes, a reactor shell, deflecting plate, reverse opening, bypass openings arranged in deflecting plate and adjusting device

Tube bundle reactor comprises: a bundle of vertically arranged reaction tubes, an upper and a lower tube sheet tightly connected to the upper and lower ends of the reaction tubes and lead through the reaction tubes in gas supply- and gas discharge devices; and a reactor shell enclosing tube bundle; at least one deflecting plate; a reverse opening (5) for releasing heat transfer medium, so that transfer medium flows in meander-form through tube bundle in the longitudinal direction, and bypass openings arranged in at least one deflecting plate in its piping region; and an adjusting device. Tube bundle reactor comprises: a bundle of vertically arranged reaction tubes, an upper and a lower tube sheet tightly connected to the upper and lower ends of the reaction tubes and lead through the reaction tubes in gas supply- and gas discharge devices; and a reactor shell enclosing the tube bundle, which is connected pressure tightly to the tube sheets, and together with the tube sheets, the reactor shell forms a pressure chamber (18), in which the reaction tubes are washed in the operation of a heat transfer medium (8); at least one deflecting plate, which extends across through the tube bundle and imposes a cross-flow to the heat transfer medium; a reverse opening (5) for releasing the heat transfer medium, so that the transfer medium flows in meander-form through the tube bundle in the longitudinal direction, and bypass openings arranged in at least one deflecting plate in its piping region; and an adjusting device (4) for adjusting the flow resistance in the reverse opening or at least one part of the bypass openings, where the adjusting device of a first position, in which the flow resistance allows a meander-form reverse of the flow direction of a partial flow quantity of heat transfer medium and is movable in at least one second position, where the flow resistance is increased, such that the partial flow quantity is reduced, or at least one tube-free region is formed in ...

Temperature control device and method for controlling the temperature of a tube bundle reactor

Temperiervorrichtung zum Temperieren eines Rohrbündelreaktors für katalytische Reaktionen, mittels eines Temperiergases, wobei der Rohrbündelreaktor einen Katalysatorraum und einen an diesen angrenzenden, aber von diesem getrennten Wärmeträgerraum aufweist, und wobei die Temperiervorrichtung mit einem Wärmeträgereinlass und einem Wärmeträgerauslass des Wärmeträgerraums in Strömungsverbindung bringbar ist und das Temperiergas die Temperiervorrichtung und den Wärmeträgerraum im Kreislauf durchströmt, mit einer Druckgasversorgung, einer Heizeinrichtung für das Temperiergas und einer Fördereinrichtung für das Temperiergas, dadurch gekennzeichnet, dass die Druckgasversorgung (125) einen Druck im Bereich von 5 bis 100 bar sicherstellt und die Temperiervorrichtung (102) einen so geringen Bauraum einnimmt, dass sie transportierbar ist. Temperature control device for tempering a tube bundle reactor for catalytic reactions, by means of a tempering, wherein the tube bundle reactor has a catalyst space and adjacent thereto, but separated from this heat transfer space, and wherein the temperature control device can be brought into fluid communication with a heat transfer inlet and a heat transfer outlet of the heat transfer space and the temperature control gas flows through the temperature control device and the heat transfer chamber in the circuit, with a pressurized gas supply, a heating device for the tempering gas and a conveying device for the tempering gas, characterized in that the compressed gas supply (125) ensures a pressure in the range of 5 to 100 bar and the temperature control device (102) occupies such a small installation space that it can be transported.

Use of foam bodies in oxidation reactors for the production of unsaturated carboxylic acids

Ein Verfahren zur Herstellung von ungesättigten Carbonsäuren durch heterogene, katalytische Gasphasenoxidation von ungesättigten oder gesättigten Kohlenwasserstoffen, beinhaltend die Verfahrensschritte:i) Bereitstellung eines Gasgemisches mindestens beinhaltend einen gesättigten Kohlenwasserstoff und katalytische Gasphasendehydrierung des mindestens einen gesättigten Kohlenwasserstoffs unter Erhalt eines einen ungesättigten Kohlenwasserstoff enthaltenen Gasgemisches in einem ein Dehydrier-Katalysatormaterial aufweisenden Dehydrier-Reaktor; oderii) Bereitstellung eines Gasgemisches mindestens beinhaltend Sauerstoff und mindestens einen ungesättigten Kohlenwasserstoff;iii) katalytische Gasphasenoxidation des in Verfahrensschritt i) erhaltenen oder des in Verfahrensschritt ii) bereitgestellten ungesättigten Kohlenwasserstoffs unter Erhalt eines einen ungesättigten Aldehyd enthaltenen Gasgemisches in einem ersten, ein erstes Oxidations-Katalysatormaterial aufweisenden Oxidations-Reaktor;iv) katalytische Gasphasenoxidation des im Verfahrensschritt iii) erhaltenen, ungesättigten Aldehyds unter Erhalt eines eine ungesättigte Carbonsäure enthaltenen Gasgemisches in einem zweiten, ein zweites Oxidations-Katalysatormaterial aufweisenden Oxidations-Reaktor; wobei mindestens einer der Reaktoren ausgewählt aus dem Dehydrier-Reaktor, dem ersten Oxidations-Reaktor und dem zweiten Oxidations-Reaktor mindestens einen Schaumkörper beinhaltet, wobei der Schaumkörper ein offenzelliger metallischer Schaum aus Stahl, Edelstahl oder Kupfer ist, und wobei mindestens ein Teil der Oberfläche des Schaumkörpers mit dem Dehydrier-Katalysatormaterial, dem ersten Oxidations-Katalysatormaterial, dem zweiten Oxidations-Katalysatormaterial oder einem Katalysatormaterial, welches die Direktoxidation eines gesättigten Kohlenwasserstoffs zu einer ungesättigten Carbonsäure katalysiert, belegt ist. A process for preparing unsaturated carboxylic acids by heterogeneous, catalytic gas-phase oxidation of ...

System for improved hydrogen generation by steam reforming of hydrocarbons and integrated chemical reactor for producing hydrogen from hydrocarbons

本発明は、下記構成を備えたリアクタを提供する：入口（１）及び出口（８）を有し、一体的に構成されたシェル・アセンブリ；シェル・アセンブリ（１０）内で前記入口（１）から前記出口（８）へ伸びる流路、この流路は、第一の触媒（５）を備えた水蒸気改質セクション、及び第二の触媒（５０）を備えた水性ガス転化リアクタ・セクションを有し、前記水蒸気改質セクションは前記水性ガス転化リアクタ・セクションの上流側に位置している；シェル・アセンブリ（１０）の中にあり、前記水蒸気改質セクションを加熱するように構成された加熱セクション；シェル・アセンブリ（１０）の中にあり、前記水性ガス転化リアクタ・セクションを冷却するように構成された冷却セクション。本発明はまた、単純化された水素製造システムを提供する。当該システムは、接触水蒸気改質、それに続く低硫黄の（質量含有率１００ｐｐｍ未満）炭化水素燃料の高温水性ガス転化、それに続く圧力スイング吸着（ＰＳＡ）による水素の精製を含む。

Теплообменный реактор для производства водорода с помощью встроенного пучка парогенератора

1. Теплообменный реактор, предназначенный для проведения эндотермических реакций, содержащий множество байонетных труб (4), подвешенных к верхнему своду (2) упомянутого реактора и простирающихся до уровня нижнего дна (3), при этом байонетные трубы (4) используются для проведения одной или нескольких эндотермических химических реакций и заключены в кожух (1), содержащий впускной патрубок (Е) для горячих дымовых газов, передающих тепло байонетным трубам (4), и, по меньшей мере, один выпускной патрубок (S) для отвода дымовых газов, охлажденных после теплообмена, причем теплообменный реактор содержит пучок парогенератора, образованный множеством вертикальных труб (5), также подвешенных к верхнему своду (2) теплообменного реактора и заключенных в периферийное пространство между внутренней перегородкой, по существу, параллельной вертикальной стенке кожуха (1), и упомянутой вертикальной стенкой, при этом упомянутая внутренняя перегородка (Bi) содержит, по меньшей мере, одно отверстие (Oi) для прохода дымовых газов из середины реактора к периферийному пространству, причем вертикальные трубы (5) служат для генерации пара и питаются водой из нижнего распределителя (9), расположенного в нижней части периферийного пространства (8), а пароводяная смесь, выходящая из вертикальных труб (5), собирается в верхнем коллекторе (7), расположенном над верхним сводом (2) теплообменного реактора, причем нижняя линия (14) связывает жидкую фазу сепараторного резервуара (6) с верхним коллектором (7), а верхняя линия (13) связывает верхний коллектор (7) с паровой фазой сепараторного резервуара (6).2. Теплообменный реактор по п.1, в котором каждая труба (5) парогене РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (51) МПК B01J 8/00 (11) (13) 2012 136 474 A (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21)(22) Заявка: 2012136474/05, 24.08.2012 (71) Заявитель(и): ИФП ЭНЕРЖИ НУВЕЛЛЬ (FR) Приоритет(ы): (30) Конвенционный приоритет: 26.08.2011 FR 11/02602 Адрес для ...

Method and device to force oxygen into reaction gas flowing through synthesis reactor

FIELD: process engineering. ^ SUBSTANCE: invention relates to synthesis reactor. Proposed synthesis reactor comprises device to feed oxygen into reaction gas. Note here that oxygen and reaction gas feature different temperatures. Note also that distributing element is arranged in direction of reaction gas flow ahead of catalyst pack device and comprises distributor case, two tube plates and multiple reaction gas pipes. One guide partition is arranged perpendicular to gas pipes to divide intermediate space into two distributing chambers. One gas feed line runs into distribution chamber, the first one along the gas flow, to feed oxygen. Bottom tube plate with multiple injector-like holes to feed oxygen into intermediate space are arranged along the gas flow. Zone of mixing gases not containing solid substances is arranged under bottom tube plate. Method of forcing oxygen into reaction gas consists in that oxygen escapes from separate nozzle at the rate of, at least, 60 m/s, preferably, of, at least, 100 m/s, and more preferably, of, at least, 140 m/s. ^ EFFECT: synthesis reactor of simple and reliable design. ^ 16 cl, 3 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2 417 833 (13) C2 (51) МПК B01J B01J 8/02 4/00 (2006.01) (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ, ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (21)(22) Заявка: 2009122697/05, 05.11.2007 (24) Дата начала отсчета срока действия патента: 05.11.2007 (73) Патентообладатель(и): УДЕ ГМБХ (DE) R U Приоритет(ы): (30) Конвенционный приоритет: 16.11.2006 DE 102006054415.3 (72) Автор(ы): ХАЙНРИТЦ-АДРИАН Макс (DE), ХАМЕЛЬ Штефан (DE), ЗЕМРАУ Лотар (DE) (43) Дата публикации заявки: 27.12.2010 Бюл. № 36 2 4 1 7 8 3 3 (45) Опубликовано: 10.05.2011 Бюл. № 13 (56) Список документов, цитированных в отчете о поиске: US 3706534 A, 19.12.1972. EP 1382382 A1, 21.01.2004. WO 2007/045457 A1, 26.04.2007. RU 2296003 C2, 27.03.2007. 2 4 1 7 8 3 3 R U (86) Заявка PCT: EP 2007/009551 (05.11.2007) C 2 C 2 ...

Method of catalytic oxidation in vapour phase implemented in multiple-tubular reactor

FIELD: heating. SUBSTANCE: invention concerns improved method of catalytic oxidation in vapour phase which supplies effective removing of reactionary heat, excludes hot spot formation, and supplies effective receipt of base product. Method of catalytic oxidation is disclosed in the vapour phase (a) of propylene, propane or isobutene by the instrumentality of molecular oxygen for receiving (meth)acrolein, and/or oxidation (b) of (meth)acrolein by molecular oxygen for receiving (meth)acryl acid, by the instrumentality of multiple-tubular reactor, contained: cylindrical reactor vessel, outfitted by initial material supply inlet hole and discharge hole for product, variety of reactor coolant pipes, located around the cylindrical reactor vessel and used for insertion the heat carrier into cylindrical reactor vessel or for removing the heat carrier from it, circulator for connection of variety loop pipeline to each other, variety of reaction tube, mounted by the instrumentality of tube reactor lattices, with catalyst. Also multiple-tubular reactor contains: variety of partitions, located lengthways of reaction tubes and used for changing heat carrier direction, inserted into reactor vessel. According to this heat carrier coolant flow is analysed and there are defined zones in reactor which have heat-transfer coefficient of heat carrier less than 1000 W/(m 2 ·K); also reaction of catalytic oxidation is averted in the vapour phase in mentioned zones of reactor and reaction of catalytic oxidation is implemented in the vapour phase in reactor. EFFECT: receiving of improved method catalytic oxidation in vapour phase which supplies effective removing of reactionary heat, excludes hot spot formation, and supplies effective receipt of base product. 3 cl, 6 dwg, 2 ex ÐÎÑÑÈÉÑÊÀß ÔÅÄÅÐÀÖÈß (19) RU (11) 2 331 628 (13) C2 (51) ÌÏÊ C07C C07C C07C C07C C07C ÔÅÄÅÐÀËÜÍÀß ÑËÓÆÁÀ C07C ÏÎ ÈÍÒÅËËÅÊÒÓÀËÜÍÎÉ ÑÎÁÑÒÂÅÍÍÎÑÒÈ,C07C ÏÀÒÅÍÒÀÌ È ÒÎÂÀÐÍÛÌ ÇÍÀÊÀÌ B01J (12) 45/33 (2006.01) 45/35 (2006.01) ...

Heat exchange reactor

본 고안은, 반응기 내의 열 전달 튜브의 지지부에 고정된 바닥과 정상의 슬라이딩에 의한 고온 반응에 대한 개선된 유체 밀봉과, 열 전달 튜브의 밀봉된 지지부를 이용하여, 흡열 촉매 반응 또는 발열 촉매 반응을 실행하는 열 교환 반응기에 관한 것이다.

Method for producing trichlorosilane

固化した塩化アルミニウムの配管への固着・堆積、および配管の応力腐食割れを防止する。トリクロロシランの製造方法であって、流動床方式反応装置から排出された、トリクロロシランを含む排出ガスを冷却する冷却工程では、流動床方式反応装置から排出ガスを排出するための配管（１０）内において、当該配管（１０）の側壁（３）の表面（１ａ）の温度が１１０℃以上となるように側壁（３）の内部に形成された空間（４）に流体を流して、排出ガスを冷却する。 Prevents solidified aluminum chloride from sticking to and depositing on pipes and stress corrosion cracking of pipes. In the cooling process for cooling the exhaust gas containing trichlorosilane discharged from the fluidized bed type reactor, the pipe (10) for discharging the exhaust gas from the fluidized bed type reactor In this case, a fluid is caused to flow through the space (4) formed in the side wall (3) so that the temperature of the surface (1a) of the side wall (3) of the pipe (10) is 110 ° C. or higher, and the exhaust gas is discharged. Cooling.

Reactor for catalytic gas phase oxidation and method for producing (meth) acrylic acid using the same

Catalytic unit

本申请公开了一种布置在竖直反应管(50)内的催化装置，所述装置包括：结构催化剂(52)，该结构催化剂在反应管的上部部分中；颗粒催化剂(56)，该颗粒催化剂在所述结构催化剂(52)下面在所述反应管的下部部分中；以及催化剂支承装置，该催化剂支承装置布置在结构催化剂(52)和颗粒催化剂(56)之间，其中，催化剂支承装置包括圆柱形本体(72)，该圆柱形本体有用于与结构催化剂连接的第一端以及第二端，该圆柱形本体的直径为管的内径的70‑90％，且长度/直径在0.5‑2.5范围内。

Process For Producing (Meth)Acrolein Or (Meth)Acrylic Acid

The object of the invention is to provide a method for producing (meth)acrolein or (meth)acrylic acid by gas phase catalytic oxidation reaction, which can perform smooth temperature control of the heat medium, can prevent hot spot effectively and can be handled easily, and an apparatus. The invention are a method for producing (meth)acrolein or (meth)acrylic acid by carrying out gas phase catalytic oxidation reaction of propane, propylene, isobutylene or (meth)acrolein with an oxygen-containing gas using an inorganic salt as a reaction temperature adjusting heat medium, characterized in that the material of a gland packing member which seals body part of a regulating valve arranged on a heat medium feeder and controlling supply and circulation velocity of the heat medium and a rotation axis that interfits to the body part, in such a manner that they can perform sliding, is a mica-based material, and a production apparatus.

Method for producing ethylene oxide

Catalytic gas phase oxidation method and multitubular reactor

Single reactor process for preparing acrylic acid from propylene having improved capacity

This invention relates to an improved process for preparing acrylic acid from propylene using a single reactor utilizing an increased amount of propylene reactant thereby providing increased capacity and throughput.

Reactor arrangement for carrying out catalytic gas phase reactions

Reaktoranordnung zur Durchführung katalytischer Gasphasenreaktionen, mit einem Mantelrohrreaktor, der ein von einem Mantel umgebenes Rohrbündel mit einer Anzahl katalysatorgefüllter Reaktionsrohre aufweist, wobei das Reaktionsrohrbündel senkrecht zur Längsachse der Reaktionsrohre eine berohrte Querschnittsfläche belegt, und mit einem separaten, direkt nachgeschalteten Nachkühler, der ein von einem Mantel umgebenes Rohrbündel mit Kühlrohren aufweist, deren Anzahl geringer ist als die der Reaktionsrohre, wobei das Kühlrohrbündel senkrecht zur Längsachse der Kühlrohre ebenfalls eine berohrte Querschnittsfläche belegt, dadurch gekennzeichnet, daß die berohrte Querschnittsfläche (27) im Nachkühler (3) im wesentlichen deckungsgleich ist mit der (26) im Mantelrohrreaktor (2) und daß beide berohrte Querschnittsflächen (26, 27) in eine Vielzahl paarweise einander gegenüberliegender und paarweise gleich großer Teilflächen (39, 40) mit im wesentlichen gleichem Verhältnis von Durchströmungsquerschnitt der Kühlrohre (21) zum Durchströmungsquerschnitt der Reaktionsrohre (7) unterteilbar sind. reactor assembly to carry out catalytic Gas phase reactions, with a jacket tube reactor, the one of a Sheath surrounded tube bundle with a number of catalyst-filled Reaction tubes, wherein the reaction tube bundle vertically to the longitudinal axis the reaction tubes occupy a drilled cross-sectional area, and with a separate, directly aftercooler, having a sheath surrounded by a tube bundle with cooling tubes whose number is less than that of the reaction tubes, wherein the cooling tube bundle vertically to the longitudinal axis the cooling pipes as well a drilled cross-sectional area occupied, characterized in that the drilled cross-sectional area (27) in aftercooler (3) is substantially congruent with (26) in the jacket tube reactor (2) and that both drilled cross-sectional areas (26, 27) in a plurality of pairs opposite each other and pairs of equally sized partial surfaces (39, 40) with ...

Tube bundle reactor for gas phase, particularly exothermic, processes has improved efficiency and operational stability by its construction from tubes of similar close tolerance internal diameter and wall thickness

Tube bundle reactors for exothermic and endothermic gas phase processes are constructed from tubes having the same consistent nominal internal diameter, and where the manufacturing tolerance basis for the tube is related to its internal diameter. Particularly, tube bundle reactors with internal diameter tolerances of +-0.45 to +-1.35% are claimed.

Partial gas phase oxidation of acrolein to acrylic acid or methacrolein to methacrylic acid, useful e.g. as monomer to prepare polymers, comprises using a tube bundle reactor in reaction tube of a vertically arranged reaction tubes

Process for implementing a heterogeneously catalyzed partial gas phase oxidation of acrolein to acrylic acid or methacrolein to methacrylic acid in a solid catalyst bed comprises using a tube bundle reactor in reaction tube of a vertically arranged bundle of reaction tubes (9), which are closed by a reactor jacket; where: the both ends of the individual reaction tubes are open and each reaction tubes terminate with its upper end in a passage of a top tube plate sealed above in reactor jacket and with its lower end in a passage of a down tube plate (5) sealed below in reactor jacket. Process for implementing a heterogeneously catalyzed partial gas phase oxidation of acrolein to acrylic acid or methacrolein to methacrylic acid in a solid catalyst bed comprises using a tube bundle reactor in reaction tube of a vertically arranged bundle of reaction tubes (9), which are closed by a reactor jacket; where: the both ends of the individual reaction tubes are open and each reaction tubes terminate with its upper end in a passage of a top tube plate sealed above in reactor jacket and with its lower end in a passage of a down tube plate (5) sealed below in reactor jacket; the exterior of the reaction tubes, the top and the down tube plate, and the reactor jacket differentiate conjointly to the reaction tube surrounding chamber, and each of the two tube plates is spanned by at least a reactor cover (6) having an opening, with which, in order to set start-up in several respects, to the reaction tubes of the tube bundle reactor, at least an opening (3) in one of the both reactor covers supplies a reaction gas inlet mixture (1) containing >= 3 vol.% of acrolein or methacrolein and additionally molecular oxygen; at least an opening of the other reactor cover discharges by partial gas phase oxidation of the acrolein to acrylic acid or methacrolein to methacrylic acid, where the passage of the product gas mixture (2) containing acrylic acid or methacrylic acid results in the solid ...

Process for the production of polymers using a loop reactor

Processes to make neopentane using shell and tube reactors

Processes for producing neopentane are disclosed herein. Processes comprise demethylating a C 6 -C 8 alkane within a shell and tube reactor to produce a demethylation product including at least 10 wt % neopentane based on the weight of the demethylation product.

Use of foam bodies in oxidation reactors for preparing unsaturated aldehydes or carboxylic acids

本发明涉及通过不饱和或饱和烃的多相催化气相氧化制备不饱和醛或不饱和羧酸的方法，其包括下列工艺步骤：i)提供至少包含饱和烃的气体混合物并在具有脱氢催化剂材料的脱氢反应器中在气相中催化脱氢所述至少一种饱和烃以获得包含不饱和烃的气体混合物；或ii)提供至少包含氧和至少一种不饱和烃的气体混合物；iii)在具有第一氧化催化剂材料的第一氧化反应器中在气相中催化氧化工艺步骤i)中获得的或工艺步骤ii)中提供的不饱和烃以获得包含不饱和醛的气体混合物；iv)任选地，在具有第二氧化催化剂材料的第二氧化反应器中在气相中催化氧化工艺步骤iii)中获得的不饱和醛以获得包含不饱和羧酸的气体混合物；其中选自脱氢反应器、第一氧化反应器和第二氧化反应器的至少一种反应器包含至少一种泡沫体。本发明还涉及制备基于不饱和羧酸的聚合物的方法、制备不饱和羧酸或基于不饱和羧酸的聚合物的装置，和装置的用途。

Flow reactors for chemical conversions with heterogeneous catalysts

Exothermic process and apparatus therefor

Method for producing a gaseous fuel comprising hydrogen from kinetic and/or potential energy recovered from a vehicle powered by a four stroke diesel engine fitted with an engine braking mechanism and system useful to implement such method

一种用于从减速阶段的由装配有Jacobs(皆可博)发动机制动器的四冲程柴油机驱动的车辆回收的动能和/或势能生产氢气体燃料的方法。所述方法包括以下阶段：a)提供预加热的蒸汽流；b)提供来自于至少一种用作预加热碳源和氢源的化学物质的气流；c)将阶段a)的来自于至少一种用作碳源和氢源的化学物质的气流与阶段b)的蒸汽流混合。

Steam reforming

FIELD: technological processes. SUBSTANCE: present invention relates to a method for steam reforming hydrocarbons to produce synthesis gas and to an apparatus for carrying out the method. Apparatus for steam reforming hydrocarbons is disclosed, comprising a steam reformer comprising a plurality of externally-heated vertical tubes, each tube having an inlet for a feed gas mixture comprising hydrocarbon and steam, and an outlet for a reformed gas mixture, wherein the tubes contain a particulate steam reforming catalyst adjacent the outlet, and a structured steam reforming catalyst adjacent the inlet. Method for steam reforming hydrocarbons using said apparatus is also described. EFFECT: creating a compact apparatus for steam reforming hydrocarbons and reducing undesirable overheating of the walls of the reaction tube. 19 cl, 3 dwg, 1 tbl РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 673 527 C2 (51) МПК B01J 8/06 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК B01J 8/06 (2018.08); C01B 3/00 (2018.08) (21)(22) Заявка: 2016138792, 17.02.2015 (24) Дата начала отсчета срока действия патента: (73) Патентообладатель(и): ДЖОНСОН МЭТТИ ПАБЛИК ЛИМИТЕД КОМПАНИ (GB) Дата регистрации: 27.11.2018 (56) Список документов, цитированных в отчете о поиске: EP 1930293 A1, 11.06.2008. RU 04.03.2014 GB 1403787.3 (43) Дата публикации заявки: 05.04.2018 Бюл. № 10 (45) Опубликовано: 27.11.2018 Бюл. № 33 (86) Заявка PCT: C 2 C 2 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 04.10.2016 113729 U1, 27.02.2012. WO 2011048361 A1, 18.04.2011. WO 2012146904 A1, 01.11.2012. RU 2570004 C2, 10.12.2015. RU 2455068 C2, 10.07.2012. US 7906079 B2, 15.03.2011. DE 3744265 A1, 13.07.1989. GB 472629 A1, 24.09.1937. GB 2015/050447 (17.02.2015) (87) Публикация заявки PCT: 2 6 7 3 5 2 7 WO 2015/132555 (11.09.2015) R U 2 6 7 3 5 2 7 Приоритет(ы): (30) Конвенционный приоритет: R U 17.02.2015 (72) Автор(ы): ХЛАПИК Кеннет (US), ФАРНЕЛЛ Питер ...

Method for synthesis of anhydrous hydrogen halide and anhydrous carbon dioxide

FIELD: chemistry. SUBSTANCE: method of treating and/or decomposing fluid media of organic halides includes, in a first reactor, reaction of one or more organic halides, anhydrous hydrogen and anhydrous carbon dioxide to obtain carbon monoxide and one or more anhydrous hydrogen halides. At least a portion of the anhydrous hydrogen halides is collected and carbon monoxide is fed in a stream into a second reactor. In the second reactor, the carbon monoxide reacts with water to obtain hydrogen and carbon dioxide. Further, water is removed from the hydrogen and the carbon dioxide to obtain anhydrous hydrogen and anhydrous carbon dioxide and the hydrogen and carbon dioxide are returned to the first reactor. EFFECT: invention reduces the amount of environmentally hazardous emissions while also reducing the temperature of treating organic halides. 19 cl, 2 dwg, 6 tbl, 6 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 530 357 C1 (51) МПК C01B 7/00 (2006.01) C01B 3/16 (2006.01) C01B 31/20 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ (21)(22) Заявка: ИЗОБРЕТЕНИЯ К ПАТЕНТУ 2013142582/05, 30.03.2012 (24) Дата начала отсчета срока действия патента: 30.03.2012 (72) Автор(ы): ТАРАНКОН III Грегорио (US) (73) Патентообладатель(и): Мидуэст Рефриджерентс, ЭлЭлСи (US) Приоритет(ы): (30) Конвенционный приоритет: R U 12.04.2011 US 61/474,659; 04.05.2011 US 13/100,951 (45) Опубликовано: 10.10.2014 Бюл. № 28 A1, 15.04.1983; . RU 2136581 C1, 10.09.1999. US 5547653 A, 20.08.1996. JP 2004105864 A, 08.04.2004. (85) Дата начала рассмотрения заявки PCT на национальной фазе: 12.11.2013 (86) Заявка PCT: 2 5 3 0 3 5 7 (56) Список документов, цитированных в отчете о поиске: US 4982039 A, 01.01.1991. SU 1011503 2 5 3 0 3 5 7 R U (87) Публикация заявки PCT: C 1 C 1 US 2012/031418 (30.03.2012) WO 2012/141918 (18.10.2012) Адрес для переписки: 191036, Санкт-Петербург, а/я 24, "НЕВИНПАТ" (54) СПОСОБ СИНТЕЗА БЕЗВОДНОГО ГАЛОИДА ВОДОРОДА И БЕЗВОДНОГО ДИОКСИДА УГЛЕРОДА (57) Реферат: ...