СПОСОБ ГАЗОФАЗНОЙ ПОЛИМЕРИЗАЦИИ ОЛЕФИНОВ

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

ТВЕРДОЖИДКОСТНАЯ РЕАКЦИЯ

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

РЕАКТОР ДЛЯ ПРОВЕДЕНИЯ ТРЕХФАЗНОЙ РЕАКЦИИ ЖИДКОЙ И ГАЗООБРАЗНОЙ ФАЗ В НЕПОДВИЖНОМ СЛОЕ КАТАЛИЗАТОРА

Изобретение относится к реактору для осуществления трехфазной реакции жидкой и газообразной фаз в неподвижном слое катализатора, способу осуществления трехфазной реакции и их применению для селективной гидрогенизации фракций углеводородов. Реактор содержит слой катализатора, смесительное и распределительное устройство над слоем катализатора, через которое сверху вниз направляется равномерным потоком жидкая фаза и газообразная фаза. Смесительное и распределительное устройство включает лотковый распределитель с имеющими форму лотков каналами и отводными трубочками для жидкой фазы, а также распределительную тарелку, расположенную под лотковым распределителем с вертикальными насадками. Лотковый распределитель имеет отверстия для впуска газообразной фазы и расположенные под ними отверстия для поступления жидкой фазы. Причем количество и размер отверстий для поступления жидкой фазы рассчитаны так, что при заданном притоке жидкости уровень жидкости на распределительной тарелке устанавливается ...

УПРАВЛЕНИЕ РЕАКТОРОМ АММОКСИДИРОВАНИЯ

Изобретение относится к вариантам способа аммоксидирования. Согласно одному из предлагаемых способов вводят поток реагентов в реактор аммоксидирования, причем поток реагентов содержит аммиак, кислородсодержащий газ и углеводород, выбранный из группы, состоящей из пропана, пропилена, изобутена, изобутилена и их смесей; вводят пар в змеевики, расположенные в реакторе аммоксидирования, с получением рабочей температуры реактора от 350°C до 480°C. При этом регулируют количество кислорода, вводимого в реактор, и температуру пара с поддержанием линейной скорости, отнесенной к сечению реактора, от 0,5 м/с до 1,5 м/с. Предлагаемые способы позволяют управлять процессом аммоксидирования и сократить отклонения температуры реактора. 3 н. и 31 з.п. ф-лы, 2 ил.

ОРГАНИЗАЦИЯ ХИМИЧЕСКИХ ЦИКЛОВ

Изобретение относится к способу организации химических циклов. Способ осуществления химической реакции, включающий передачу элемента или группы X от одной молекулы к другой в реакторе с неподвижным слоем, содержащим нестехиометрическое соединение, которое имеет формулу MX, где n и p обозначают целые числа, требующиеся для стехиометрического соединения между М и X, и 0q>-1, и которое способно содержать величины q в интервале, а М может обозначать один элемент или смесь более одного элементов, включает пропускание химической частицы Р через реактор, причем частица Р поступает из первого положения во второе положение в реакторе, и извлечение полученного химического соединения PXиз второго положения, затем пропускание химического соединения QXчерез реактор, причем соединение QXпоступает из второго положения в первое положение в реакторе, и извлечение полученного химического соединения из первого положения, причем Р и Q представляют собой химические частицы, которые выбирают таким ...

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 ...

СПОСОБ РАБОТЫ РЕАКТОРА С РУТЕНИЕВЫМ КАТАЛИЗАТОРОМ

Изобретение относится к области химии. Заполняют реакционный резервуар каталитического реактора рутениевым катализатором. Уровень высоты заполнения катализатором устанавливают выше уровня высоты подачи текучего материала. В качестве текучего материала подают смешанный газ, содержащий, главным образом, углеводород, 1-кислородсодержащий газ и пар. Получают синтез-газ, содержащий водород и моноксид углерода. Выполняют мониторинг мольного отношения (С/O) углерода, содержащегося в углеводородном газе, и кислорода, содержащегося в кислородсодержащем газе, которые подают в реакционный резервуар, и останавливают подачу кислородсодержащего газа в реакционный резервуар до того, как мольное отношение С/Oснизится ниже критического мольного отношения, при котором возникает рассеивание рутения в рутениевом катализаторе. Изобретение позволяет заблаговременно предотвратить рассеивание рутениевого катализатора и стабилизировать процесс. 2 н. и 3 з.п. ф-лы, 7 ил.

СПОСОБ ПОЛИМЕРИЗАЦИИ

Описывается способ непрерывной газофазной полимеризации в псевдоожиженном слое олефинового мономера, выбранного из (а) этилена, (б) пропилена, (в) смесей этилена с пропиленом и (г) смесей (а), (б) или (в) с одним или несколькими другими альфа-олефинами в реакторе с псевдоожиженным слоем посредством непрерывной рециркуляции газообразного потока, содержащего по меньшей мере некоторое количество этилена и/или пропилена, через псевдоожиженный слой в указанном реакторе в присутствии полимеризационного катализатора при реакционных условиях, причем по меньшей мере часть указанного газообразного потока, отведенного из указанного реактора, охлаждают до температуры, при которой из него конденсируется жидкость, отличающийся тем, что по крайней мере часть сконденсированной жидкости выделяется из газообразного потока и по крайней мере часть этой выделенной жидкости вводится непосредственно в псевдоожиженный слой в точку или выше точки, в которой газообразный поток, проходящий через псевдоожиженный слой ...

ПРОТОЧНОЕ ЛАБОРАТОРНОЕ УСТРОЙСТВО ДЛЯ ГИДРИРОВАНИЯ И ЛАБОРАТОРНЫЙ СПОСОБ ГИДРИРОВАНИЯ С ИСПОЛЬЗОВАНИЕМ ЭТОГО УСТРОЙСТВА

... 1. Проточное лабораторное устройство (100; 200; 300) для гидрирования введенных образцов ниже значений надкритических давлений, включающее резервуар (104; 204), подающий насос (102; 202), собирательный элемент (108; 208) с двумя входами и выходом, реактор (110; 210; 310-1,..., 310-m) гидрирования и узел (112; 212) регулирования давления, все соединенные в линию потока, а также источник (126; 226) водорода и клапан (120; 220), направляющий поток газа в одном единственном направлении и расположенный между источником (126; 226) водорода и вторым входом собирательного элемента (108; 208), где узел (112; 212) регулирования давления расположен на линии потока после реактора (110; 210; 310-1,..., 310-m) гидрирования, отличающееся тем, что подающий насос (102; 202) представляет собой насос, создающий постоянную объемную скорость, а резервуар (104; 204) в качестве исходного раствора содержит по меньшей мере растворитель для образца, который нужно гидрировать, где реактор (110; 210; 310-1,..., 310 ...

НЕПРЕРЫВНЫЙ СПОСОБ КОНВЕРСИИ ЛИГНИНА В СОЕДИНЕНИЯ, ПОДХОДЯЩИЕ ДЛЯ ПРИМЕНЕНИЯ

... 1. Непрерывный способ конверсии лигнинового сырья, содержащего лигнин, причем указанный способ включает:дезоксигенирование лигнина до совокупности продуктов конверсии лигнина в реакторе для конверсии лигнина, содержащем содержимое реактора, содержащее жидкую композицию, содержащую по меньшей мере одно соединение, являющееся жидкостью при 1 бар и 25°C; и при этом одновременное непрерывное выведение по меньшей мере части совокупности продуктов конверсии лигнина из реактора;где конверсию лигнина проводят путем приведения лигнина в контакт с водородом и первым катализатором; иконверсию лигнина проводят при температуре конверсии лигнина и давлении конверсии лигнина, где температура конверсии лигнина находится в интервале выше температуры кипения указанной жидкой композиции при атмосферном давлении и ниже критической температуры жидкой композиции, а давление конверсии лигнина выше давления в пузырьке указанной жидкой композиции при температуре конверсии лигнина, при этом давление конверсии лигнина ...

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

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

КАТАЛИТИЧЕСКИЙ РЕАКТОР С НИСХОДЯЩИМ ПОТОКОМ

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

СПОСОБ КРЕКИРОВАНИЯ УГЛЕВОДОРОДНОГО СЫРЬЯ

... 1. Способ крекирования углеводородного сырья в реакторном агрегате, содержащем: ! реакторный аппарат; ! вход для твердого катализатора, через который вводят катализатор, и выход для твердого катализатора, через который катализатор выводят из реакторного аппарата; ! множество подающих сопел, с помощью которых сырье вводят у днища аппарата; ! выход для продукта, предназначенный для вывода продуктовой смеси газа и твердого катализатора в верхней части реакторного аппарата; и ! по меньшей мере одну перегородочную плиту, которая разделяет внутреннюю полость реакторного аппарата на два или более отделения, и при этом перегородочная плита пересекает вход для твердого катализатора. ! 2. Способ по п.1, в котором отделения создают с помощью перегородочных плит, расположенных по существу перпендикулярно к днищу реакторного аппарата. ! 3. Способ по п.2, в котором реакторный агрегат дополнительно содержит трубопровод для транспортирования смеси продуктов из выхода для продукта к сепаратору газ/твердые ...

КОНТРОЛЬ ТЕМПЕРАТУРЫ РЕАКТОРА АММОКСИДИРОВАНИЯ

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 ...

ТВЕРДО-ЖИДКОСТНАЯ РЕАКЦИЯ

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

Способ получения олигоимидов

Verfahren zur Herstellung von Produkten unter wechselnden Lastbedingungen

Die Erfindung betrifft ein Verfahren und eine Vorrichtung zur Synthese eines Produktgases aus einem ersten Eduktgas und einem zweiten Eduktgas, wobei Produktgas ausgeschleust und nicht umgesetztes Eduktgas im Kreislauf geführt wird, und wobei der Volumenstrom des ersten Eduktgases, des zweitem Eduktgas und/oder des ausgeschleusten Produktgases während des Verfahrens variiert wird. Auf diese Weise kann die pro Zeiteinheit gebildete Menge an Produktgas vorübergehend gedrosselt (Teillast-Betrieb) oder dessen Synthese vorübergehend vollständig eingestellt werden (Stand-by-Betrieb), ohne dass die Anlage, auf der das Verfahren durchgeführt wird, vollständig heruntergefahren werden muss. So können temporäre Engpässe bei der Verfügbarkeit von Energie bzw. von Eduktgas überbrückt werden. Das Verfahren kann kurzfristig wieder auf optimierte Synthesebedingungen hochgefahren werden (Volllast-Betrieb), wenn die Verfügbarkeit von Energie bzw. von Eduktgas wieder hergestellt ist. Die beiden Eduktgase ...

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 ( ...

VERFAHREN ZUR DURCHFÜHRUNG VON STARK EXOTHERMEN OXIDATIONSREAKTIONEN UNTER PSEUDO-ISOTHERMISCHEN BEDINGUNGEN

Brennstoffpatrone mit Reaktionskammer

Verfahren zur Durchfuehrung von exothermen Reaktionen zwischen einem Gas und einer Fluessigkeit

WASSERDAMPFREFORMIERUNG MIT INTERNER WASSERSTOFFREINIGUNG

Wasserstoffgenerator

Ein Wasserstoffseparierungsfilter schließt eine Vielzahl von Wasserstoffextraktionsschichten, eine Vielzahl von Separierungsschichten mit Wasserstoffseparierungsfilmen und eine Vielzahl von reformierten Gasschichten, welche aufeinanderfolgend in der Reihenfolge der Extraktionsschicht, der Separierungsschicht, der reformierten Gasschicht und der Separierungsschicht gelegt werden, um eine Laminatstruktur zu bilden. Die jeweiligen Schichten sind aus einem porösen keramischen Material zusammengesetzt, um die benötigte Festigkeit bzw. Zähigkeit sicherzustellen. Die Richtung des Gasstromes in den reformierten Gasschichten und diejenige in den Extraktionsschichten sind jeweils fixiert, um die Gaseinspeisung und Entladungsstruktur zu vereinfachen. Der Wasserstoffseparierungsfilter wird mit einer Umhüllung über ein Pufferelement bedeckt, um die ausreichende Festigkeit bzw. Zähigkeit und benötigen Versiegelungseigenschaften sicherzustellen. Ein Methanisierungskatalysator, der die Methanisierung von ...

Improved process for contacting fluids with powdered solid particles

... 578,962. Catalytic apparatus. STANDARD OIL DEVELOPMENT CO. April 30, 1943, No. 6842. Convention date, Aug. 26, 1942. Drawings to Specification. [Class 1 (i)] In contacting gases or vapours with a fluidized mass or solid catalyst particles, wherein most of the catalyst is withdrawn from the bottom of the reactor but a minor amount is entrained in the exit gases, this entrainment is reduced to a minimum by maintaining the level of the fluidized mass some distance below the top of the contact zone. The distance varies with the gas velocity and may be 15 ft. for a velocity of 1.5 ft. per second and 5 ft. for 1 ft. per second. The invention is applicable to the conversion of hydrocarbons and the regeneration of catalysts.

METHOD OF REMOVING HEAT GENERATED IN THE POLYMERIZATION OF MONOMERS IN THE GAS PHASE

... 1354020 Polymerization BADISCHE ANILIN- & SODA-FABRIK AG 7 Oct 1971 [9 Oct 1970] 46671/71 Heading C3P Heat is removed from polymerization reactions of monomers in the gaseous phase by a process in which gaseous or liquid monomer and optionally heat transfer agent is introduced into the polymerization zone and polymer is removed -therefrom and gaseous monomer, optionally together with heat-transfer agent, is removed from the polymerization zone, at least partially liquefied by cooling under the pressure prevailing in the polymerization zone and reintroduced in the liquid state into the polymerization zone, the polymerization temperature being kept constant by regulating the rate of reintroduction of the condensate which is stored as necessary after condensation and before reintroduction. The process may be applied to the polymerization of C 2 -C 6 olefins in the prescence of titanium halide/aluminium alkyl catalysts and vinyl chloride in the presence of peroxides or azo compounds. Apparatus ...

CONVERSION OF HYDROCARBONS

... 1438795 Cracking TEXACO DEVELOPMENT CORP 11 June 1973 27775/73 Heading C5E In a catalytic cracking process in which the product is fractionated and an intermediate gas oil fraction is collected on a trap tray for recycle, the addition of catalyst to the reaction zone is controlled by means responsive to the level of oil on the trap tray. The recycle rate can then be used to control the distribution of product between light gas oil and lighter hydrocarbons. As shown, the fresh and recycle feeds are cracked in separate risers (12 and 22), receiving catalyst from standpipes 11 and 23, controlled by slide valves 19 and 53. Valve 19 is controlled by means 15 responsive to the temperature in the riser, whereas valve 53 is controlled by means 70 responsive to the level of liquid on the trap tray 67.

Actively cooled reactor for exothermic reaktions

Nozzle

PROCESS FOR REGENERATING A COKE-CONTAMINATED FLUID CATALYTIC CRACKING CATALYST AND CATALYTIC CONVERSION OF CO TO CO

Hydrocarbon synthesis reaction apparatus, start-upprocess thereof and hydrocarbon synthesis reactio n system

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

HYDROCARBON SYNTHESIS REACTION APPARATUS, START-UP PROCESS THEREOF, AND HYDROCARBON SYNTHESIS REACTION SYSTEM

Hydrocarbon synthesis reaction apparatus, start-upprocess thereof and hydrocarbon synthesis reactio n system

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

Hydrocarbon synthesis reaction apparatus, start-upprocess thereof and hydrocarbon synthesis reactio n system

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

HEISGASREAKTOR AND PROCEDURES FOR ITS USE

PROCEDURE FOR THE CONTROLLING OF THE POLYMER RIVER DURING A POLYMERIZATION PROCESS

POLYOLEFIN TREATMENT FOR THE SEPARATION OF VOLATILE MATERIAL

FLUIDIZED BED DEVICE MODULE AND PROCEDURE FOR THE EXCHANGE OF A FIRST MODULE AGAINST A SECOND MODULE IN FLUIDIZED BED DEVICES

PROCESS ACCOMPLISHED IN THE CONDENSATION MODE IN THE GASEOUS PHASE FLUIDIZATION, WITH LIQUID PHASE ENRICHMENT AND GASEOUS PHASE FLUIDIZED BED INJECTION

PROCEDURE FOR THE GASEOUS PHASE POLYMERIZATION OF OLEFINEN

IMPROVED DEEP CATALYTIC CRACKING PROCEDURE

REAKTIONSAPPARAT ZUR DURCHFUHRUNG MEHRSTUFIGER KATALYTISCHER REAKTIONEN

PROCEDURE AND DEVICE FOR A THERMAL TREATMENT IN A FLUID BED

REACTION APPARATUS TO DURCHFUHRUNG MULTI-LEVEL CATALYTIC REACTIONS

Wirbelschichtreaktorsystem

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

DEVICE AND PROCEDURE FOR PROPORTIONING SOLID FROM A FLUID BED, AVAILABLE IN A GAS/CSOLID STREAM.

HYDROGENATION PROCEDURE.

DEVICE AND PROCEDURE FOR PROPORTIONING SOLID FROM A FLUID BED, AVAILABLE IN A GAS/CSOLID STREAM

POLYMERIZATION PROCEDURE

CONTINUOUS GASEOUS PHASE PROCEDURE FOR THE COATING OF POLYMERIZATION CATALYSTS

PROCEDURE FOR THE PRODUCTION OF HYDROCARBONS

PROCESS FOR PRODUCTION OF ETHYLENE FROM ETHANE

Method and apparatus for treating high pressure particulate material

SOLIDS FLOW REGULATOR

REGENERATING COKE CONTAMINATED FLUID CATALYST

Wireless monitoring and profiling of reactor conditions using plurality of sensor-enabled RFID tags and multiple transceivers

Disclosed is a system and method for wirelessly monitoring 5 process conditions within a reactor vessel. A plurality of sensor-enabled radio frequency identification (RFID) tags are disposed at unspecified or random locations throughout a catalyst bed of a vessel and are used to measure various conditions within the vessel. The sensor-enabled RFID tags are encoded with individual identification codes and are wirelessly linked to multiple 10 transceivers. The use of multiple transceivers allows for the application of triangulation methods to identify the location of each of the sensor-enabled RFID tags in threedimensional space and for the interrogation of each sensor-enabled RFID tag to receive responsive transponder signals that carry information representative of the sensed condition within the reactor.

Gas distributor for a reactor

Fixed-bed catalytic reactor

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

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

PROCESS FOR HYDROGENATING AN UNSATURATED ORGANIC COMPOUND

A continuous reaction device for synthesizing polyoxymethylene dimethyl ethers

Abstract The present invention pertains to the technical field of energy resource chemical industry, and in particular relates to a continuous reaction device and process for synthesizing 5 polyoxymethylene dimethyl ethers by using paraformaldehyde and methylal as feedstock or using trioxane and methylal as feedstock in the presence of an acidic catalyst. The continuous reaction device comprises multiple slurry bed stirred tank reactors connected in series or in combination of series connection and parallel connection, and also comprises an on-line solid-liquid separation device to perform separation of the reaction mixture from the 0 catalyst. Each of the tank reactors is provided with an axial-flow stirring paddle having 2-6 blades per layer, to ensure sufficient mixing of the reactants with the catalyst. By using a distributed control pattern of reaction temperature and feedstock supplying to enhance the process and to optimize the operation, the reaction device of the present invention ...

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

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

POLYMERISATION OF VINYL CHLORIDE

Syngas reactor with ceramic membrane

SUPPORTED MICROPOROUS CERAMIC MEMBRANES

Catalyst-downcomer-tray for chemical process tower

A NON-MECHANICAL RATE CONTROLLER FOR A SOLID FLOW ESTABLISHED BETWEEN TWO FLUIDIZED MEDIA

IMPROVED DISTRIBUTOR SYSTEM FOR DOWNFLOW REACTORS

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

CARRYING OUT GAS/LIQUID EXOTHERMIC REACTIONS

OPTIMIZING THE PRODUCTION RATE OF SLURRY BUBBLE REACTORS BY USING LARGE GAS FLOW RATES AND MODERATE SINGLE PASS CONVERSION

A gas-agitated multiphase reactor system that is effective for enabling maximum reactor productivity or minimizing reactor volume comprising at least two stages with or without recycle, wherein inlet gas superficial velocity is at least 20 cm/sec at Fischer-Tropsch synthesis, yielding a total syngas conversion of greater than about 90%, while syngas conversion in each reactor is less than 60%. More specifically, the total reactor volume is held to a minimum such that minimum reactor volume is less than 0.02 cubic meters total reactor volume/(kg C5+/hr production).

METHOD AND APPARATUS FOR TREATING HIGH PRESSURE PARTICULATE MATERIAL

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

PROCESS FOR INITIATING AND CONTROLLING DENSE-BED OXIDATION OF COKE AND CATALYZED OXIDATION OF CO TO CO2 IN CC REGENERATION ZONE

A process for initiating and controlling the regeneration of spent fluid catalytic cracking catalyst containing catalytically effective amounts of a C0 conversion promotor and for the essentially complete catalytic conversion of C0 to C02 both in a dense bed of catalyst maintained in an FCC regeneration zone. The process comprises (a) passing to a dense-phase catalyst bed in a regeneration zone said catalyst and fresh regeneration gas at a first flow rate sufficient to oxidize coke to produce partially spent regeneration gas, (b) oxidizing coke at first oxidizing conditions including a catalyst bed first temperature of from 399.degree.C to 677.degree.C to produce regenerated catalyst and partially spent regeneration gas containing C0, (c) increasing the catalyst bed temperature from said first temperature to a second temperature of from 677.degree.C to 760.degree.C, (d) passing to the catalyst bed fresh regeneration gas at a second flow rate stoichiometrically sufficient to essentially ...

AIR FLOW MEASUREMENT DEVICE FOR FLUIDIZED BED REACTOR

AIR FLOW MEASUREMENT DEVICE FOR FLUIDIZED BED REACTOR A fluidized bed reactor in which an air distribution plate is disposed within an enclosure for supporting a bed of particulate material including fuel. The air distribution plate includes a plurality of vertically disposed nozzles extending therethrough for receiving air from an air plenum and discharging the air in an upward direction into the bed at a velocity sufficient to fluidize the bed material and support the combustion or gasification of the fuel. A first pressure sensing device is disposed within at least one of said nozzles and a second pressure sensing device is disposed within the air plenum, whereby the rate of air flow into the bed of particulate material can be measured. ld-8369U ...

DEVICE FOR DISTRIBUTING FLOWING MEDIA OVER A FLOW CROSS SECTION

REGULATING FLUIDIZED BEDS

FUEL CARTRIDGE AND REACTION CHAMBER

A fuel cartridge in accordance with one of the present inventions includes a fuel reservoir (102), a reaction chamber (104), and a passive structure (128, 130) adapted to resist fluid flow from the fuel reservoir (102) to the reaction chamber (104). A reaction chamber in accordance with one of the present inventions includes an external housing (178), defining a first reactant inlet (179), a liquid outlet (181) and a gas outlet (194), and a substantially gas permeable/substantially liquid impermeable structure (182) that separates the first reactant inlet (179) and the liquid outlet (181) from the gas outlet (194).

OXYGEN REDUCTION SYSTEM WITH A UNIVERSALLY COMPATIBLE FRONT-END FOR COUPLING WITH VARIOUS DIFFERENT GAS SOURCES

Disclosed herein are various examples of systems, methods and devices for an oxygen reduction system with a universally compatible, adaptive front end that can be coupled with various different gas sources, wherein the oxygen reduction system determines its operations separate and independent from any signal lines from any upstream components or systems. In one example, the oxygen reduction system determines its functions, operations, and operational states from parameters that it measures from the input gas stream and other internal measurements. In this manner, installation of an oxygen reduction system is simplified, time-efficient and universal, and embodiments of the present disclosure provide for oxygen reduction systems that can be installed in a variety of different environments, applications, and with new or existing natural gas productions sites.

PROCESS

A process for the production of propylene glycol from a lactate ester is disclosed. The process comprisessupplying a feed comprising a C3-6 alkyl lactate ester. The feed is contacted with a stream of hydrogen containing gas and subjected to hydrogenation in the vapour phase in the presence of a catalyst at a temperature of from about 130°C to about 185°C, a pressure of from about 20 bar to about 60 bar, and a weight hourly space velocity greater than about 0.3 h-1. The catalyst is a reduced copper catalyst selected from copper alumina, optionally comprising manganese, copperchromite, copper zinc oxide and Raney copper.

CATALYTIC OXIDATION PROCESS WITH FLOW CONTROL SYSTEM

A process for the catalytic oxidation of a hydrocarbonaceous fuel (1) into a conversion product, wherein a feed mixture comprising the fuel and an oxygen- containing gas (2) is contacted with a catalyst bed (3), which process further comprises the steps of: (a) setting the flow rate of the fuel and flow rate of the oxygen-containing gas, preferably in accordance with the demand of conversion product and a pre-determined value of the oxygen/carbon ratio in the feed mixture; (b) determining the actual temperature (10) of the upstream surface of the catalyst bed by means of a quick response device; (c) generating an output signal (13) that is a function of the difference between the actual temperature and a set point for the temperature; and (d) using the output signal to adjust the flow rate of the fuel (6) and/or of the oxygen- containing (7) gas, preferably the flow rate of the fuel.

FABRICATION DU STYRENE

REACTOR FOR USE IN UPGRADING HEAVY OIL ADMIXED WITH A HIGHLY ACTIVE CATALYST COMPOSITION IN A SLURRY

The instant invention relates to a reactor useful in upgrading heavy oils admixed with a catalyst composition in a slurry. The liquid recirculating reactor of this invention employs a dispersed bubble flow regime, which requires a high liquid to gas ratio. A dispersed bubble flow regime results in more even flow patterns, increasing the amount of liquid that can be upgraded in a single reactor.

FLUIDIZED BED REACTOR SYSTEM

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

GAS JET INJECTOR REACTOR FOR CATALYTIC FAST PYROLYSIS

Methods and systems utilizing gas jets to carry biomass into a biomass conversion reactor are described. Reactor configurations and conditions for carrying out processes utilizing the gas jets are also described. The use of gas jets has been found to be especially desirable for operation with pyrolysis of biomass in catalytic fluidized bed reactors. A feed system for introducing biomass into a pyrolysis reactor, such as a catalytic fast pyrolysis (CFP) fluid bed reactor, that employs a jet stream of gas or vapor to inject the biomass particles into the fluid bed is disclosed. The biomass is kept relatively cool, can be metered upstream of a gas jet, and can be injected far into the fluid bed. Good mixing between the relatively cooler biomass with the hot catalyst and other materials in the fluid bed can be insured by adjustment of the number, size, angle, position, and flow rate of the multiple injector ports in larger reactors.

HYDROCARBON SYNTHESIS REACTION APPARATUS, START-UP PROCESS TEHREOF, AND HYDROCARBON SYNTHESIS REACTION SYSTEM

This hydrocarbon synthesis reaction device comprises: a synthetic gas supply passage for supplying a synthetic gas compressed by a first compressor; a reaction vessel for containing a catalyst slurry; a gas-liquid separator for gas-liquid separating unreacted synthetic gas and hydrocarbon derived from the reaction vessel; a first recirculation passage for recirculating the unreacted synthetic gas after the gas-liquid separation compressed by a second compressor to the reaction vessel; and a second recirculation passage for recirculating the rest of the unreacted synthetic gas after the gas-liquid separation to a suction side of the first compressor at the time of start up operation when the introduction amount of the synthetic gas is gradually increased.

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 ADDING STARTING MATERIAL SLURRY AND SULFURIC ACID TO AUTOCLAVE IN HIGH PRESSURE ACID LEACHING PROCESS AND AUTOCLAVE

An autoclave (100) of a high pressure acid leaching process in which heated and pressurized starting material slurry and sulfuric acid are stirred by stirrers (30A, 30B...) provided in respective divided chambers (20A, 20B...) in an autoclave that is multiply divided using partition walls (10A, 10B...) to promote the leaching and the slurry is transferred from the upstream divided chambers to the downstream divided chambers and leaching is promoted successively. The mixing of the starting material slurry and sulfuric acid is promoted and the control value for the free sulfuric acid concentration after discharge is reduced by: alternately disposing starting material slurry-supplying tubes (41, 42), which have starting material slurry discharging ports (41A, 42A), and sulfuric acid-supplying tubes (51, 52), which have sulfuric acid-supplying ports (51A, 52A), around the stirring blades (31A) of the stirrer (30A) provided in the divided chamber (20A) at the upstream end; and adding the starting ...

EXOTHERMIC PROCESS WITH POROUS MEANS TO CONTROL REACTION RATE AND EXOTHERMIC HEAT

An exothermic process for forming a product which may be in a liquid phase is disclosed wherein a first reactant (3), preferably a liquid reactant, is directly fed into a reaction zone (10) containing mounting elements (12, 58) and which comprises a first compartment (10) of a reactor (2, 40). A second reactant, which is maintained at a higher pressure, is fed into a second compartment (20) of the reactor (2, 40) separated from the first compartment (10) by a porous wall (32, 52). The second reactant (4) passes through this porous wall (32, 52) into the reaction zone to react with the first reactant (3). The process thereby controls rates of the reactions and the exothermic heats generated by the reactions. Pulsatile flow in one or both reaction compartments improves mixing. An evaporator for a portion of the production improves product quality and permits higher reaction temperatures in the reactor.

Method and Apparatus for Controlling Introduction of Catalysts Into FCC Units

METHOD AND APPARATUS FOR STOPPING REACTION IN A GAS PHASE POLYMERIZATION REACTOR SYSTEM

PASSIVE ACOUSTICS PROCESS TO MONITOR TRANSFER LINES OF A REACTOR

The present invention is a method for the non-intrusive determination of average particle velocity and average particle mass density from the mass flux and RMS acceleration in a gas/particle transfer line. The method includes the steps of determining the RMS acceleration of the wall of said transfer line at one or more positions along the length of said transfer line, determining the average mass flux through the transfer line, and from both quantities determining the average particle mass density or the average particle velocity from the RMS acceleration and the average mass flux.

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.

AUTOCLAVE HAVING HIGH OXYGEN TRANSFER RATE TO METAL-CONTAINING SOLUTIONS

The autoclave of the present invention includes an impeller having a conduit to recirculate or introduce an oxygen-containing gas into the slurry. The outlets for the gas can be located in the blades of the impeller for thorough dispersion of the gas bubbles in the slurry.

Verfahren zur Steuerung der Wasserstoffbildung aus einer Kohlenwasserstoff-Beschickung

Verfahren zur kontinuierlichen Herstellung von Hexachlorbenzol und Anlage zur Durchführung des Verfahrens

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

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

Tunable catalytic gasifiers and related methods

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

Bi-Modal Radial Flow Reactor

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

Catalytic oxidation method and method for producing conjugated diene

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

Hydrogen gas generating system and method with buffer tank

A hydrogen gas generating system that heats a liquid reactant such as water, then channeling the resultant heated reactant to a reaction chamber containing a solid hydride. The chemical reaction between the heated liquid reactant and solid hydride forming hydrogen gas. This hydrogen gas is then filtered and regulated before being stored in a buffer tank. Hydrogen gas from the buffer tank can then be supplied to a fuel cell to produce electricity as and when needed, such as when a battery goes below a predetermined level. The pressure of the buffer tank is measured and used to ascertain when the hydrogen gas generation should start and stop. A pressure and temperature of the reaction chamber is measured as a safety precaution, whereby the reaction will be stopped if the pressure and temperature exceeds predetermined values.

FLUID CATALYTIC CRACKING PROCESSES AND APPARATUS

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

Inherently safe oxygen/hydrocarbon gas mixer

Provided herein is a gas mixer for the safe mixing of a hydrocarbon containing gas with a gaseous oxidant. The gas mixer and method for mixing described includes a closed mixing vessel where bubbles of gas injected at the bottom of the vessel are mixed during their rise to the top of the vessel, forming a homogeneous mixture that can safely be removed. This simple design and method allows for safe mixing of gases and is applicable to catalytic oxidative processes such as oxidative dehydrogenation of paraffins where there is a risk of thermal runaway of reactions.

SYSTEMS AND METHODS FOR PREDICTING AND CONTROLLING THE PROPERTIES OF A CHEMICAL SPECIES DURING A TIME-DEPENDENT PROCESS

Devices and methods for controlling the properties of chemical species during time-dependent processes. A device includes a reactor for containing one or more chemical species of a time-dependent process, an extraction pump for automatically and continuously extracting an amount of the one or more chemical species from the reactor, one or more detectors for measuring property changes of the one or more extracted chemical species and generating a continuous stream of data related to the one or more property changes to the one or more chemical species during a time interval, and a process controller configured to fit the continuous stream of data to a mathematical function to predict one or more properties of the one or more chemical species at a future time point and make one or more process decisions based on the prediction of one or more properties at the future time point. 131-. (canceled)32. A method comprising:introducing, in a reactor, one or more chemical species to be monitored during a time-dependent process;detecting, using one or more detectors, one or more property changes to the one or more chemical species over a time interval;receiving, from the one or more detectors, a continuous stream of data related to the one or more property changes to the one or more chemical species during the time interval;fitting, using a process controller, the continuous stream of data to a mathematical function to predict one or more properties of the one or more chemical species at a future time point; andmaking, by the process controller, one or more process decisions based on the prediction of one or more properties at the future time point.33. The method of claim 32 , wherein the one or more process decisions comprise any one of terminating of the time-dependent process claim 32 , recovering the reactor contents claim 32 , proceeding to a subsequent reaction or processing stage in the same or a different reactor.34. The method of claim 32 , further comprising fitting ...

Hydrogen generator

A hydrogen generator includes a container having a gas outlet that is configured to contain a soluble chemical fuel that reacts with a catalyst to generate hydrogen. A control cylinder is attached to the container and comprises a piston configured to travel axially within the control cylinder, a pole attached to the piston and extending into the container, a catalyst holder provided within the container and connected to the pole, resilient means biasing the catalyst holder towards a bottom of the container, and a gas inlet port. A gas flow line is in fluid communication with the gas outlet and has a first end in fluid communication with the gas inlet port, a second end configured to feed hydrogen to a hydrogen-consuming device, and a two-way valve provided to allow fluid communication between the first and second ends of the gas flow line to be selectably established or cut off.

Catalyst Transfer Pipe Plug Detection

Apparatuses and methods are disclosed for detecting catalyst transfer pipe plugging in a chemical plant or petrochemical plant or refinery. The catalyst transfer pipe may extend from a reactor to a catalyst collector and enable the flow of catalyst from the reactor to the catalyst collector. Specifically, one or more sensors affixed to a catalyst transfer pipe may collect sensor data for analysis. Based on one or more detected changes in the sensor data outside a range, a data collection platform may send one or more alerts and/or send one or more signals to a control platform to adjust a flow rate, a pressure differential, or perform another action to clear a developing catalyst buildup and thereby attempt to avoid a catalyst transfer pipe from becoming plugged. 1. A system for detecting catalyst-transfer-pipe plugging , the system comprising:a reactor configured for a dehydrogenation process, wherein the reactor is configured for use with a solid catalyst;a catalyst collector comprising a valve, the catalyst collector configured to collect the solid catalyst;a catalyst transfer pipe extending from the reactor to the catalyst collector, the catalyst transfer pipe configured to enable flow of the solid catalyst from the reactor to the catalyst collector;one or more sensors affixed to an outside of the catalyst transfer pipe; and one or more processors; and', receive sensor data collected by the one or more sensors affixed to the catalyst transfer pipe;', 'analyze the sensor data to determine a flow rate through the catalyst transfer pipe; and', 'based on analyzing the sensor data to determine the flow rate through the catalyst transfer pipe, transmit a command to adjust the flow rate through the catalyst transfer pipe by adjusting the valve of the catalyst collector., 'non-transitory computer-readable memory storing executable instructions that, when executed, cause the computing device to], 'a computing device comprising2. The system of claim 1 , wherein the ...

Process of Removing Heat

The present invention provides an improved process for removing heat from an exothermic reaction. In particular, the present invention provides a process wherein heat can be removed from multiple reaction trains using a common coolant system.

APPARATUS AND PROCESS FOR THE PRODUCTION OF FORMALDEHYDE

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

METHOD AND GENERATOR FOR HYDROGEN PRODUCTION

A hydrogen generator and methods of generating hydrogen are described in which a hydride is hydrolysed in a reaction chamber in an exothermic reaction by the addition of liquid water to be vaporized in the reaction chamber, and/or the added water is controlled in relation to the hydrogen generated according to a value x defined by equations, which, for a divalent metal, reads: 1. A hydrogen generator , comprising:a reaction chamber having an interior, a water supply inlet in communication with the reaction chamber and a hydrogen outlet in communication with the reaction chamber, wherein, within the interior of the reaction chamber, a metal hydride in the form of a granular material is positioned, and wherein, in series with the hydrogen outlet, within the interior of the reaction chamber, a porous material that is permeable to hydrogen but is not permeable to the hydride is positioned;a water feed pump;a water line coupled to the water supply inlet and the water feed pump;a temperature sensor in communication with the interior of the reaction chamber;a control unit in electrical communication with the water feed pump and the temperature sensor; [{'br': None, 'i': x', 'x', 'x, 'MH+H2O→(1-)M2O+(2-1)MOH+H2,'}, {'br': None, 'M symbolizing a 1-valent metal, x being in the interval of 0.51 to 0.9,'}, {'br': None, 'i': +x', 'x, 'MH2H2O→(2-x)MO+(-1)M(OH)2+2H2,'}, {'br': None, 'M symbolizing a divalent metal, x being in the interval of 1.02 to 1.8,'}, {'br': None, 'i': +x', 'x', 'x, 'MH3H2O→(1⅓)M2O3+(⅔-1)M(OH)3+3H2,'}, {'br': None, 'M symbolizing a 3-valent metal, x being in the interval of 1.5 to 3,'}, {'br': None, 'i': +x', 'x', 'x, 'MH4H2O→(2½)MO2+(½-1)M(OH)4+4H2,'}, {'br': None, 'M symbolizing a 4-valent metal, x being in the interval of 2.04 to 3.6.'}], 'wherein the metal hydride can be the hydride of a 1-valent metal, or a 2-valent metal, or a 3-valent metal, or a 4-valent metal, a stoichiometric factor x in the following equations being controlled within the below ...

Float valve for a chemical reactor

A float valve for a chemical reactor has a central pipe which glides around a liquid transfer pipe when a liquid level rises and falls, thereby opening for fluid transfer through liquid transfer apertures in the transfer pipe when the liquid level is rising and shutting off for fluid transfer when the float lowers and seals against a sealing ring placed on the transfer pipe below the liquid transfer apertures.

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

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

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

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

METHOD OF SIMULTANEOUSLY PREPARING 1,1,1-TRIFLUORO-2-CHLOROPROPENE AND 1,1,1,2-TETRAFLUOROPROPENE USING GAS PHASE CATALYST

Disclosed is a method of simultaneously preparing 1,1,1-trifluoro-2-chloropropene and 1,1,1,2-tetrafluoropropene, the method including i) a step of elevating a temperature of a reactor charged with a gas phase catalyst up to a reaction temperature; ii) a step of feeding 1,1,1-trifluoro-2,3-dichloropropane and 2-chloro-1,1,1,2-tetrafluoropropane into the reactor, the temperature of which has been elevated; iii) a step of performing dehydrochlorination while maintaining the temperature of the reactor; and iv) a step of performing washing and distillation after the dehydrochlorination. In accordance with the present disclosure, a high-efficient gas-phase process of continuously, simultaneously preparing 1,1,1-trifluoro-2-chloropropene and 1,1,1,2-tetrafluoropropene is provided. 1. A method of simultaneously preparing 1 ,1 ,1-trifluoro-2-chloropropene and 1 ,1 ,1 ,2-tetrafluoropropene , the method comprising:i) elevating a temperature of a reactor charged with a gas phase catalyst up to a reaction temperature;ii) feeding 1,1,1-trifluoro-2,3-dichloropropane and 2-chloro-1,1,1,2-tetrafluoropropane into the reactor, the temperature of which has been elevated;iii) performing dehydrochlorination while maintaining the temperature of the reactor; and 'wherein the gas phase catalyst is a catalyst in which a metal is supported on a support, the support is selected from activated carbon, activated alumina, or a molecular sieve, and the metal is selected from the group consisting of Zn, Pd, Pt, Sb, V, Sn, and Bi.', 'iv) performing washing and distillation after the dehydrochlorination: and'}2. (canceled)3. (canceled)4. (canceled)5. The method according to claim 1 , wherein the metal is Zn.6. The method according to claim 5 , wherein a Zn content in the gas phase catalyst is 1 to 20% by weight.7. The method according to claim 1 , wherein a reaction temperature of the reactor is 300 to 400° C.8. The method according to claim 1 , wherein an inflow rate of 1 claim 1 ,1 claim 1 ,1- ...

PROCESS FOR PREPARING CHLORSILANES

The present disclosure relates to a process for producing chlorosilanes in a fluidized bed reactor by reaction of a hydrogen and silicon tetrachloride-containing reaction gas with a particulate contact mass containing silicon and a catalyst. The chlorosilanes have the general formula HSiCland/or HClSi. The reactor design is described by an index K1, the constitution of the contact mass is described by an index K2 and the reaction conditions are described by an index K3. 118-. (canceled)20. The process of claim 19 , wherein K1 has a value of 3 to 18 claim 19 , preferably of 4 to 16 claim 19 , or particularly preferably of 6 to 12.21. The process of claim 19 , wherein K2 has a value of 0.005 to 100 claim 19 , preferably of 0.01 to 25 claim 19 , or particularly preferably of 0.02 to 15.22. The process of claim 19 , wherein K3 has a value of 0.5 to 10 000 claim 19 , preferably of 3 to 3000 claim 19 , or particularly preferably of 5 to 1000.23. The process of claim 19 , wherein the effective reactor volume Vis 5 to 200 m claim 19 , preferably 10 to 150 m claim 19 , or particularly preferably 20 to 100 m.24. The process of claim 19 , wherein the hydraulic plant diameter dis 0.75 to 2m or preferably 0.8 to 1.5m.25. The process of claim 19 , wherein the pressure drop over the fluidized bed pis 30 claim 19 ,000 to 150 claim 19 ,000 kg/m*sor preferably 50 claim 19 ,000 to 120 claim 19 ,000 kg/m*s.26. The process of claim 19 , wherein the particle Sauter diameter dis 50 to 1500 μm claim 19 , preferably 100 to 1000 μm claim 19 , or particularly preferably 200 to 800 μm.27. The process of claim 19 , wherein the breadth of the particle size distribution of the contact mass Bis 100 to 1000 μm or preferably 300 to 800 μm.28. The process of claim 19 , wherein the relative catalyst distribution in the contact mass δis 0.005 to 5 or preferably 0.01 to 2.5.290. The process of claim 19 , wherein the catalyst is selected from the group of Fe claim 19 , Al claim 19 , Ca claim 19 , Ni ...

CO2 HYDROGENATION IN REVERSE FLOW REACTORS

Systems and methods are provided for hydrogenation of COin a reverse flow reactor environment via a reverse water gas shift reaction. A reverse flow reactor environment is suitable for performing endothermic reactions at high temperatures, where a reactant flow is passed into the reactor in a first portion of the cycle in a first flow direction while a combustion or heating flow is passed into the reactor during a second portion of the reaction cycle from the opposite direction. This can allow for efficient heating of surfaces within the reactor to provide heat for the endothermic reverse water gas shift reaction while reducing or minimizing incorporation of combustion products into the desired reaction products. 1. A method for performing a reaction in a reverse flow reactor , comprising:{'sub': '2', 'reacting a fuel mixture comprising fuel, 0.1 vol % or more of O, and a diluent under combustion conditions in a combustion zone within a reverse flow reactor to form a flue gas and to heat a conversion zone to an average conversion zone temperature of 400° C. or more, the conversion zone comprising a catalyst composition; and'}{'sub': 2', '2', '2', '2', '2, 'exposing a reactant stream comprising 5.0 vol % to 50 vol % CO, 20 vol % or more H, and a ratio of Hto COof 2.0 or more, to the catalyst composition in the conversion zone under reverse water gas shift reaction conditions to form a product stream comprising HO and CO, a direction of flow for the reactant stream within the reaction zone being reversed relative to a direction of flow for the fuel mixture.'}2. The method of claim 1 , wherein the reactant stream comprises a ratio of Hto COof 3.0 or more.3. The method of claim 1 , wherein the reactant stream comprises 10 vol % or more CO.4. The method of claim 3 , the method further comprising:{'sub': 2', '2, 'mixing a synthesis gas feed comprising 10 vol % or more COwith an H-containing stream to form the reactant stream.'}5. The method of claim 1 , wherein the ...

Catalytic Alkane Conversion and Olefin Separation

Disclosed is a hydrocarbon conversion process that is less energy intensive than comparable processes. The hydrocarbon conversion process is particularly desirable for converting alkanes, such as methane into C 2+ olefins, such as ethylene and propylene, particularly with increasing selectivity to ethylene production. It is also desirable for effectively removing a C 2 composition (i.e., ethane, ethylene and/or acetylene) produced from the catalytic conversion of hydrocarbon comprised of C 2+ olefins. In addition, the hydrocarbon process is desirable for providing a substantially non-cryogenic separation of the desired C 2 compositions from the hydrocarbons (e.g., methane) present in the reaction mixture.

Process of Removing Heat

The present invention provides an improved process for removing heat from an exothermic reaction. In particular, the present invention provides a process wherein heat can be removed from multiple reaction trains using a common coolant system. 120-. (canceled)21. A method of starting up an exothermic reaction comprising:(a) providing at least two separate reaction trains each comprising at least one reactor;(b) providing a common coolant circulation system which comprises a single common reservoir comprising a coolant which is fed into each reaction train;(c) starting circulation of the coolant to each reaction train;(d) increasing the pressure the reactors to a desired reaction pressure;(e) feeding a reactant feedstream into each reaction train;(f) increasing the temperature of the single common reservoir while adjusting the GHSV of the reactant feedstreams through each reaction train to obtain the desired extent of exothermic reaction.2226-. (canceled)27. A method of starting up an exothermic reaction in a start-up reactor comprised in a reaction train , said method comprisinga) providing multiple reaction trains each comprising at least one reactor;b) providing a common coolant circulation system which comprises a single common reservoir comprising a first coolant which is fed into each reaction train except the reaction train comprising the start-up reactor in which the exothermic reaction is to be started up;c) providing a second coolant circulation system associated with a second coolant reservoir comprising a second coolant which is fed into the reaction train comprising the start-up reactor;d) increasing the pressure in the start-up reactor to a desired reaction pressure;e) feeding a reactant feedstream into the reaction train comprising the start-up reactor;f) running the process until the operating conditions of the start-up reactor are such that the coolant exiting the start-up reactor may be reintroduced to the common coolant circulation system; andg) ...

PROCESS OF REMOVING HEAT

The present invention provides an improved process for removing heat from an exothermic reaction. In particular, the present invention provides a process wherein heat can be removed from multiple reaction trains using a common coolant system. 1. (canceled)2. (canceled)3. (canceled)4. (canceled)5. (canceled)6. (canceled)7. (canceled)8. (canceled)9. (canceled)10. (canceled)11. (canceled)12. (canceled)13. (canceled)14. (canceled)15. (canceled)16. (canceled)17. (canceled)18. (canceled)19. (canceled)20. (canceled)21. (canceled)22. A method of isolating a reaction train from an exothermic reaction process circuit which comprises multiple reaction trains to which a first coolant is fed from a common first coolant reservoir and wherein each reaction train comprises a reactor to which a reactant substream is fed , comprising:performing the exothermic reaction in the reactor to produce reaction products and first coolant to which heat has been transferred;providing a second coolant circulation system associated with a second coolant reservoir;redirecting the first coolant to which heat has been transferred from the reaction train to be isolated to the second coolant reservoir; and thenstopping the feed of the first coolant to the reaction train to be isolated while simultaneously initiating the feed of the second coolant from the second coolant reservoir to the reaction train to be isolated.23. The method according to claim 22 , wherein the first coolant and the second coolant are the same.24. The method according to claim 22 , wherein the first coolant and the second coolant are different.25. A method of reintroducing a reaction train which has been isolated from an exothermic reaction process circuit which comprises multiple reaction trains to which a first coolant is fed from a common coolant reservoir claim 22 , wherein each reaction train comprises a reactor to which a reactant substream is fed and wherein:an exothermic reaction is performed in the reactor of each ...

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

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

Method for Reducing Temperature Spread in Reformer

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

Hydrocarbon Dehydrocyclization

The invention relates to hydrocarbon dehydrocyclization to produce products such as aromatic hydrocarbon, to equipment and materials useful for dehydrocyclization, to processes for carrying out dehydrocyclization, and to the use of dehydrocyclization for, e.g., natural gas upgrading. The dehydrocyclization is carried out in a catalytic reaction zone of a reverse-flow reactor. 1. A hydrocarbon dehydrocyclization process , the process comprising:{'sub': '2+', '(a) providing a feed comprising C non-aromatic hydrocarbon;'}(b) providing an oxidant and a gaseous fuel; (i) a pre-heated reaction zone, and', '(ii) a dehydrocyclization catalyst located in the reaction zone, the dehydrocyclization catalyst comprising a molecular sieve component and a dehydrogenation component;, '(c) providing a reverse-flow reactor, the reverse-flow reactor including'} (i) establishing a forward flow of the feed to the reaction zone,', '(ii) transferring heat from the reaction zone to the feed to produce a heated feed and a cooled reaction zone,', {'sub': '2+', "(iii) reacting at least a portion of the heated feed flow's C non-aromatic hydrocarbon in the presence of the dehydrocyclization catalyst under dehydrocyclization conditions which include a temperature a temperature ≧400° C. and a pressure ≧0 psi gauge (psig) (101 kPa) to produce a forward flow of a reaction product comprising molecular hydrogen and aromatic hydrocarbon,"}, '(iv) depositing coke on or proximate to the dehydrocyclization catalyst,', '(v) conducting the forward flow of reaction product from the reaction zone and away from the reverse-flow reactor, and', '(vi) decreasing the feed flow to the reaction zone; and, '(d) during a first time interval,'} (i) establishing a reverse flow of the fuel and a reverse flow of the oxidant toward the reverse-flow reactor, the oxidant flow comprising first and second portions of the oxidant,', '(ii) combusting the first portion of the oxidant flow under combustion conditions with at least ...

Polymerization Using a Spiral Heat Exchanger

This invention relates to a polymerization process for forming polymer comprising: contacting (typically in a solution or slurry phase), a monomer and a catalyst system in a reaction zone comprising at least one spiral heat exchanger and recovering polymer, wherein the monomer, the catalyst system and the polymer flow through the at least one spiral heat exchanger in a cross-flow direction relative to spirals of the at least one spiral heat exchanger.

ENABLING SECURED DEBUG OF AN INTEGRATED CIRCUIT

Secured debug of an integrated circuit having a test operation mode and a secure mission operation mode. The integrated circuit has a processing unit, a test interface through which the test operation mode is controllable, an on-chip memory which is accessible in the test operation mode and in the secure mission operation mode, and one or more protected resources inaccessible in the test operation mode. The processing unit is configured, in the test operation mode, to receive an authenticated object through the test interface, and store the received authenticated object in the on-chip memory. The processing unit is moreover configured, upon reset into the secure mission operation mode, to execute a boot procedure to determine that the authenticated object is available in the on-chip memory, authenticate the authenticated object, and—upon successful authentication—render the more protected resources accessible to a debug host external to the integrated circuit. 1. An integrated circuit having a test operation mode and a secure mission operation mode , the integrated circuit comprising:a processing unit;a test interface through which the test operation mode is controllable;an on-chip memory, the on-chip memory being accessible in the test operation mode and in the secure mission operation mode;at least one protected resource, the at least one protected resource being inaccessible in the test operation mode; receive an authenticated object through the test interface; and', 'store the received authenticated object in the on-chip memory; and, 'the processing unit being configured, in the test operation mode, to determine that the authenticated object is available in the on-chip memory;', 'authenticate the authenticated object; and', 'upon successful authentication, render the at least one protected resources accessible to a debug host external to the integrated circuit., 'the processing unit being configured, upon reset into the secure mission operation mode, to execute ...

METHOD AND DEVICE FOR PRODUCING LITHIUM TRANSITION METAL OXIDE

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

EFFICIENT IN-SITU CATALYST SULFIDING METHODS AND SYSTEMS

A system and method is disclosed for efficiently sulfiding metal catalyst resident in a reactor vessel comprises a sulfiding module and a hydrogen sulfide detection module and a remote computer all arranged and configured to communicate wirelessly and to allow remote control and monitoring of the modules and sulfiding process. 1. A system for sulfiding a metal catalyst , comprising: a sulfur product inlet and outlet,', 'a sulfur product measurement device,', 'a sulfur product pressurization device having a variably controllable output,', 'a controller in electrical communication with at least the measurement device and pressurization device, and', 'a first communication device configured to transmit information between the module and an external site;, 'a mobile sulfur supply module comprising'} an inlet and outlet,', 'a hydrogen sulfide concentration detection device located between the inlet and outlet,', 'a hydrogen gas concentration detection device located between the inlet and the outlet,', 'and', 'a second communication device configured to transmit information between the hydrogen sulfide detection device and the external site and between the hydrogen gas detection device and the external site., 'a mobile detection module comprising'}2. The system of claim 1 , wherein the external site is a laptop computer.3. The system of claim 1 , wherein the external site is a website on the Internet.4. The system of claim 1 , wherein the pressurization device comprises a pump.5. The system of claim 4 , wherein the pump comprises an AC motor and a variable frequency drive.6. The system of claim 1 , wherein the pressurization device comprises a compressor.7. The system of claim 6 , wherein the compressor comprises an AC motor and a variable frequency drive.8. The system of claim 1 , wherein the sulfur product measurement device comprises a multi-parameter fluid measurement device.9. The system of claim 8 , wherein the fluid measurement device is configured to determine ...

ESTIMATION OF CYCLONE LIFE BASED ON REMAINING ABRASION RESISTANT LINING THICKNESS

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

Process for Producing Paraxylene by Methylation of Benzene and/or Toluene

A process is described for producing paraxylene, in which an aromatic hydrocarbon feedstock comprising benzene and/or toluene is contacted with an alkylating reagent comprising methanol and/or dimethyl ether in an alkylation reaction zone under alkylation conditions in the presence of an alkylation catalyst to produce an alkylated aromatic product comprising xylenes. The alkylation catalyst comprises a molecular sieve having a Constraint Index≤5, and the alkylation conditions comprise a temperature less than 500° C. Paraxylene may then be recovered from the alkylated aromatic product.

Fluidized bed reactor with pinching fittings for producing polysilicon granulate, and method and use for same

Control of the flow of granular polysilicon granules is effected by employing an elastomeric pinch sleeve valve. The flow control by this method is especially useful for controlling the flow of silicon seed particles and granular polysilicon product in the fluidized bed method for producing polysilicon. The flow may be stopped without gas leakage, and is suitable for use over long operating campaigns.

FEED GAS REFORMING SYSTEM AND METHOD OF CONTROLLING THE SAME

A feed gas reforming system is provided. The system includes a reformer configured to receive feed gas and supply water and to produce and discharge mixed gas including hydrogen, a pressure swing absorber (PSA) configured to receive the mixed gas and to refine and discharge hydrogen gas, a feed gas supply unit configured to control the supply amount of feed gas, a supply water supply unit configured to control the supply amount of supply water, a hydrogen gas supply unit configured to control the amount of hydrogen gas, and a control unit configured to control the flow rate of hydrogen gas, to control the feed gas supply unit based on the pressure of the discharged hydrogen gas, and to control the supply water supply unit based on the flow rate of feed gas. 1. A feed gas reforming system comprising: receive feed gas and supply water; and', 'produce and discharge mixed gas including hydrogen;, 'a reformer configured to receive the mixed gas from the reformer; and', 'refine and discharge hydrogen gas;, 'a pressure swing absorber (PSA) configured toa feed gas supply unit configured to control a supply amount of the feed gas;a supply water supply unit configured to control a supply amount of the supply water;a hydrogen gas supply unit configured to control an amount of the hydrogen gas discharged from the PSA; and control a flow rate of the hydrogen gas discharged through the hydrogen gas supply unit;', 'control the feed gas supply unit based on a pressure of the discharged hydrogen gas; and', 'control the supply water supply unit based on a flow rate of the feed gas discharged through the feed gas supply unit., 'a control unit configured to2. The feed gas reforming system according to claim 1 , wherein the control unit further comprises: control the hydrogen gas supply unit based on a flow rate or pressure of the hydrogen gas discharged from the PSA; and', 'control the hydrogen gas supply unit according to a signal transmitted from outside., 'a hydrogen gas controller ...

REACTOR INLET VAPOR VELOCITY EQUALIZER AND DISTRIBUTOR

The invention relates to distributing feed vapor more evenly across the interior space of a reactor vessel utilizing a distributor pipe at the inlet end that initially directs the flow of reactants through a flange plate and a series of ring plates. The ring plates are physical spaced such that vapor along the wall of the inlet is mildly obstructed by the flange plate and the ring plates cause the vapor to alter course temper down any diverse velocities that may create hot spots within the catalyst bed. At the end of the distributor pipe is a deflector which directs the feed vapor upwardly and outwardly in the head space of the reactor vessel. 1. A reactor system comprising:a) a reactor vessel including a closed shell defining a relatively large interior space inside the shell for conducting a fixed bed catalytic reaction, an inlet into the interior space of the shell for the admission of feed vapor, an outlet at the opposite end thereof to allow products of the catalytic reaction to exit the reactor vessel, a bed of catalyst between the inlet and the outlet and a head space between the inlet and the catalyst bed, wherein the inlet includes a generally cylindrical neck having a smaller internal cross sectional dimension than a comparable internal cross sectional dimension of the relatively large interior space within the shell of the reactor vessel;b) a generally cylindrical distributor pipe extending down through the generally cylindrical neck and into the head space of the reactor vessel, wherein the generally cylindrical distributor pipe has a peripheral wall, a first end through which feed vapor is received and an opposite end that is positioned in the head space of the reactor vessel, wherein the feed vapor is arranged to exit the generally cylindrical distributor pipe through openings extending radially outwardly through the peripheral wall of the distributor pipe adjacent the opposite end of the distributor pipe and into the headspace and further wherein the ...

SYSTEMS AND METHODS FOR THE OXIDATIVE COUPLING OF METHANE

The present disclosure provides systems and methods for producing olefins via an oxidative coupling of methane (OCM) process. The systems and methods may comprise the use of a staged process comprising at least one non-adiabatic section that is in thermal communication with a heat transfer medium and at least one substantially adiabatic section. The systems and methods may also comprise the use of a diluent stream which may improve methane conversion in an OCM reactor and an ethylene/ethane ratio in a post-bed cracking unit. The methods and systems may further comprise injecting oxygen (O) and a paraffin into a gas stream containing a radical transfer agent to provide a reaction mixture. The reaction mixture may be held in a vessel for a time period greater than an auto-ignition delay time (AIDT), such that the reaction mixture may ignite to liberate heat and convert to a product mixture comprising olefins. 1. A method for producing an olefin , the method comprising:{'sub': 4', '2, '(a) producing a gas stream comprising methane (CH), oxygen (O), and a diluent; and'}{'sub': 4', '2+, '(b) passing the gas stream over an oxidative coupling of methane (OCM) catalyst at a pressure of at least 2 bar(g) to convert at least some of the CHinto hydrocarbon compounds having two or more carbon atoms (C compounds),'}wherein a ratio of diluent molecules to carbon atoms in the gas stream is at least 0.1:1.2. The method of claim 1 , wherein the diluent comprises water (HO).3. The method of claim 1 , wherein the diluent comprises carbon dioxide (CO).4. The method of claim 1 , wherein the diluent comprises HO and CO.5. The method of claim 1 , wherein the ratio of diluent molecules to carbon atoms in the gas stream is at least 0.5:1.6. The method of claim 1 , wherein the ratio of diluent molecules to carbon atoms in the gas stream is at most 20:1.7. The method of claim 1 , wherein the ratio of diluent molecules to carbon atoms in the gas stream is from 0.1:1 to 5:1.8. The method of ...

New catalyst system for producing maleic anhydride by means of the catalytic oxidation of n-butane

The invention relates to a catalyst system for producing maleic anhydride by means of the catalytic oxidation of n-butane, comprising at least one reactor tube, which has two catalyst layers consisting of different catalyst particles, characterized in that the geometric surface area per catalyst particle is greater in the catalyst layer that is first in the gas flow direction than in the second catalyst layer. The invention further relates to a process for producing maleic anhydride by means of the catalytic oxidation of n-butane, wherein a mixture of oxygen and n-butane is fed through the catalyst system according to the invention and the at least one reactor tube is at elevated temperature.

SYSTEMS AND METHODS FOR IMPROVING YIELDS OF HYDROCARBON FUELS FROM ALCOHOLS

Systems and methods are provided that permit temperature control of a catalyst bed for conversion of alcohols to fuel hydrocarbons by modulating the water content of the alcohol feed stream provided to the catalyst bed. Heat generated by exothermic reactions in the catalyst bed can be utilized to pre-heat the alcohol feed stream. In some embodiments a secondary catalyst bed is provided for the conversion of light hydrocarbons found in the initial hydrocarbon product to fuel hydrocarbons that are liquid at ambient temperature and pressure. 135.-. (canceled)36. A method for controlling temperature in a catalyst bed comprising:providing a catalyst bed configured to process alcohol to a fuel hydrocarbon mixture;providing a first flow of a first stream comprising the alcohol;directing a second flow of a second stream comprising water into the first stream to produce a third stream, wherein the third stream is directed to the catalyst bed; andmodulating the first flow or the second flow to modulate water content of the third stream to maintain temperature of the catalyst bed within a desired temperature range.37. The method of claim 36 , further comprising the step of generating temperature data characterizing temperature of the catalyst bed.38. The method of claim 37 , further comprising the steps of:providing the temperature data to a controller;within the controller, using an algorithm to determine a flow rate of either the first flow or the second flow necessary to maintain temperature of the catalyst bed within a desired range; andtransmitting an instruction from the controller to a flow control device to modulate flow rate of either the first flow or the second flow.39. The method of claim 36 , wherein a mean temperature within the desired temperature range is from 200° C. to 600° C. claim 36 , and wherein the mean temperature is surrounded by a temperature range selected from the group consisting of ±20° C. claim 36 , ±30° C. claim 36 , ±40° C. claim 36 , ±50° C. ...

Flex-Fuel Hydrogen Reformer for IC Engines and Gas Turbines

An on-board Flex-Fuel Hreforming apparatus provides devices and the methods of operating these devices to produce Hand CO from hydrocarbons and bio-fuels. One or more parallel autothermal reformers are used to convert the fuels into Hover the Pt group metal catalysts without external heat and power. The produced reformate is then cooled and the dry gas is compressed and stored in vessels at a pressure between 1 to 100 atmospheres. For this system, the pressure of the storage vessels and the flow control curves are used directly to control the amount of the reformers' reformate output. 1): An on-board Flex-Fuel HReforming apparatus provides devices comprising:{'sub': '2', 'a). Providing one or more parallel autothermal (ATR) reformers for producing Hand CO from hydrocarbons and/or bio-fuels over supported and/or unsupported Pt group catalysts;'}b). Providing one automatic control system comprising a control computer and/or microprocessors, flow meters/controllers, valves, pumps, sensors and thermocouples;c). Providing a stream of the ATR reformer's inlet fuel mixture comprising at least one oxidant, at least one fuel and at least one water/steam, wherein the reactants are selected from the reactant supply group consisting of liquid fuel loop, gas fuel loop, water supply loop, air supply loop, water electrolyzer loop, exhaust gas recycle (EGR) loop, water recycle loop and reformate recycle loop;{'sub': 2', '2', '2', '2, "d). Reacting said stream of the inlet fuel mixture over said catalysts inside the ATR reformer to produce a reformate containing Hand CO from said fuels, and simultaneously controlling said fuel mixture's O/C, HO/C and CO/C ratios within a given range so that the maximum ATR reaction temperature is kept constantly below 1200° C.;"}e). Providing one or more vessels/manifolds for storing the condensed water for the reformers and also storing said dry reformate produced from the ATR reformers at a pressure between 1 to 100 atmospheres, which is used by ...

FLOW BYPASS DEVICE FOR A VESSEL CONTAINING SOLID PARTICLES

Disclosed is a flow bypass device, a reactor system containing the flow bypass device; a method for operating a fixed bed of solid particles in which gas is re-routed to an interior of the fixed bed, for example, the flow bypass device is used to bypass a portion of the solid particles; and a method for loading solid particles and a flow bypass device into a vessel. The methods and systems can use a single flow bypass device or multiple flow bypass devices that are stacked on top of one another. 1. A flow bypass device comprising:a pipe portion having a first flow channel formed therein and extending from a first end of the pipe portion to a second end of the pipe portion;a distributor portion connected to the second end of the pipe portion, wherein the distributor portion has a second flow channel formed therein that is fluidly connected to the first flow channel of the pipe portion and to an opening formed in a bottom of the distributor portion, wherein a longitudinal axis of the opening is parallel to a longitudinal axis of the pipe portion; anda rupture disk coupled to the first end of the pipe portion,wherein the pipe portion has no perforations.2. The flow bypass device of claim 1 , further comprising:a top assembly containing the rupture disk and connected to the first end of the pipe portion; anda cap coupled to the top assembly, to the pipe portion, or to both the top assembly and the pipe portion,wherein the rupture disk is positioned between the cap and the first end of the pipe portion.3. The flow bypass device of claim 2 , wherein the cap comprises:a cover; andat least two arms, each of the at least two arms being configured to couple the cover to the top assembly, to the pipe portion, or to both the top assembly and the pipe portion.4. The flow bypass device of claim 3 , wherein each of the at least two arms has an end connected to an underside of the cover and an opposite end connected to the top assembly claim 3 , to the pipe portion claim 3 , or to ...

Method for preventing the fluidization of a catalytic fixed bed in a tubular upward-flow reactor of a steam methane reformer

The present invention relates to a method to prevent the fluidization of a catalytic fixed bed present in a tubular reactor operated in upward-flow configuration by estimating a pressure drop margin remaining before fluidization of the catalytic bed and adjusting the reactant gas flow in response. It relates also to a method to operate safely a furnace suitable for performing endothermic reactions containing a plurality of catalytic fixed bed reactors operated in upward-flow configuration, and to a method to debottleneck safely a catalytic fixed bed reactor involving a gas flowing in up flow direction.

METHOD AND REACTION EQUIPMENT FOR PREPARING DIMETHYL ETHER AND OLEFIN FROM METHANOL

The present invention relates to a method for preparing dimethyl ether from methanol which is carried out in a reaction device arranged with a plurality of catalyst bed layers connected in series, and comprises: dividing the reactant stream that contains methanol into n substreams, and feeding these different substreams into the reaction device through top feed ports or side feed ports between the catalyst bed layers of the reaction device for methanol-to-dimethyl ether reaction; wherein, the temperature T1 of the substream fed into the first catalyst bed layer is controlled within the following range: 290−50K1≦T1≦150K1−271K1+397.5; where, 1>K1≧0.5, and T1 is in unit of ° C. 2. The method for preparing dimethyl ether from methanol according to claim 1 , wherein 2≦n≦8.3. The method for preparing dimethyl ether from methanol according to claim 1 , wherein 0.95≧K1≧0.6.4. The method for preparing dimethyl ether from methanol according to claim 1 , wherein 1>K1≧0.6.5. The method for preparing dimethyl ether from methanol according to claim 1 , wherein the allocation proportion Ki of the reactant in the substream i is Ki≧(1−ΣK)×50% claim 1 , wherein i≠1.6. The method for preparing dimethyl ether from methanol according to claim 1 , wherein the number of the catalyst bed layers is greater than or equal to n.7. The method for preparing dimethyl ether from methanol according to claim 1 , wherein the reaction device comprises one or more fixed bed reactors claim 1 , with said a plurality of catalyst bed layers arranged in the one or more fixed bed reactors.8. A reaction apparatus for preparing dimethyl ether from methanol claim 1 , comprising a feeding device claim 1 , a flow control device claim 1 , a heating device claim 1 , and a reaction device claim 1 , wherein the reaction device is arranged with a plurality of catalyst bed layers therein claim 1 , the feeding device is configured to provide a methanol-containing gas-phase material to at least two of the catalyst bed ...

OXIDATIVE COUPLING OF METHANE SYSTEMS AND METHODS

Systems and methods conducive to the formation of one or more alkene hydrocarbons using a methane source and an oxidant in an oxidative coupling of methane (OCM) reaction are provided. One or more vessels each containing one or more catalyst beds containing one or more catalysts each having similar or differing chemical composition or physical form may be used. The one or more catalyst beds may be operated under a variety of conditions. At least a portion of the catalyst beds may be operated under substantially adiabatic conditions. At least a portion of the catalyst beds may be operated under substantially isothermal conditions. 115.-. (canceled)16. A system for generating hydrocarbons having two or more carbon atoms (C hydrocarbons) , comprising:a methane source that provides methane;an oxidant source that provides an oxidant;{'sub': '2+', 'a reaction unit in fluid communication with said methane source and said oxidant source, said reaction unit comprising a catalyst bed that includes at least one oxidative coupling of methane (OCM) catalyst, wherein said OCM catalyst facilitates an OCM reaction using said methane from said methane source and said oxidant from said oxidant source to generate said C hydrocarbons, and wherein said catalyst bed has an inlet zone that is contacted by a bulk gas mixture formed upon entry of said methane from said methane source and said oxidant from said oxidant source into said reaction unit; and'} (a) maintain a thermal profile across said catalyst bed during said OCM reaction, which thermal profile is characterized by (i) a temperature of said inlet zone being less than about 550° C., and (ii) a maximum temperature within said catalyst bed being greater than about 800° C.;', '(b) maintain a pressure within said reaction unit greater than about 15 pounds per square inch gauge (psig); and', {'sub': '2+', '(c) maintain said OCM reaction within said catalyst bed at a methane conversion of at least about 6% and a C hydrocarbon ...

HIGH-PRESSURE POLYMERIZATION PROCESS OF ETHYLENICALLY UNSATURATED MONOMERS

A process for polymerizing or copolymerizing ethylenically unsaturated monomers at pressures in the range of from 110 MPa to 500 MPa in a production line comprising a continuously operated polymerization reactor, wherein the process comprises monitoring the surrounding of the production line with respect to an occurrence of a leakage of monomers or of reaction mixture by an IR point detector arrangement of at least three groups of IR point detectors which are capable of detecting hydrocarbons and the groups of IR point detectors are operating according to a voting logic and starting automatically an emergency pressure release program when a group of IR point detectors of the IR point detector arrangement detects the presence of hydrocarbons. 1. A process for polymerizing or copolymerizing one or more ethylenically unsaturated monomers at temperatures from 100° C. to 350° C. and pressures in the range of from 110 MPa to 500 MPa in a continuously operated polymerization reactor ,wherein the polymerization is carried out in a production line in which the monomers are brought to the polymerization pressure by one or more compressors in a sequence of compression stages in which the compressed gas mixture is cooled after each compression stage by a compression stage cooler, the compressed monomers are optionally passed through a pre-heater or a pre-cooler and transferred into the polymerization reactor which is optionally cooled by cooling jackets, a reaction mixture obtained by the polymerization is leaving the reactor through a pressure control valve and optionally cooled by an post reactor cooler, the reaction mixture is separated into polymeric and gaseous components in two or more stages, where the gaseous components separated off in a first stage at an absolute pressure of from 15 MPa to 50 MPa are recycled to the one or more compressors via a high-pressure gas recycle line, and the gaseous components separated off in a second stage at an absolute pressure in the ...

Multiple downcomer trays

Multiple downcomer trays having increased active area for vapor-liquid contact and separation are described. The increased active area of the tray is achieved by adding raised bubble promoters surrounded by perforated vertical contactors on the tray deck. The bubble promoters and surrounding vertical contactors are located under the downcomers from the tray above. The bubble promoter and surrounding vertical contactor promote uniform fluid flow and contact.

Continuous Preparation of Calcined Chemically-Treated Solid Oxides

The present invention discloses a continuous calcination vessel which can be used to prepare calcined chemically-treated solid oxides from solid oxides and chemically-treated solid oxides. A process for the continuous preparation of calcined chemically-treated solid oxides is also provided. Calcined chemically-treated solid oxides disclosed herein can be used in catalyst compositions for the polymerization of olefins. 1. A continuous calcination vessel comprising:(a) a fluidized bed vessel having a slope from horizontal in a range from about 5 degrees to less than about 15 degrees;(b) a particulate material inlet capable of introducing inlet particulate material into the fluidized bed vessel;(c) a fluidizing gas inlet capable of introducing a fluidizing gas into the fluidized bed vessel;(d) a fluidizing gas path capable of directing the fluidizing gas from the fluidizing gas inlet into the fluidized bed vessel to fluidize the inlet particulate material;(e) a heating zone within the fluidized bed vessel; and(f) an outlet capable of removing outlet particulate material from the fluidized bed vessel.2. The continuous calcination vessel of claim 1 , wherein the inlet particulate material comprises a solid oxide claim 1 , a chemically-treated solid oxide claim 1 , or a combination thereof.3. The continuous calcination vessel of claim 1 , wherein the outlet particulate material comprises a calcined chemically-treated solid oxide.4. The continuous calcination vessel of claim 1 , wherein the heating zone comprises at least one baffle claim 1 , and wherein the fluidized bed vessel contains sufficient baffles to cause a substantially plug flow profile through the fluidized bed vessel.5. The continuous calcination vessel of claim 1 , further comprising a filter apparatus adapted to remove a portion of the inlet particulate material and/or the outlet particulate material entrained in the fluidizing gas.6. The continuous calcination vessel of claim 1 , further comprising a ...

GAS DECOMPOSITION REACTOR FEEDBACK CONTROL USING RAMAN SPECTROMETRY

A gas decomposition reactor for the decomposition of a gas into a mixture of solid and gaseous by-products is disclosed. The gas decomposition reactor includes a reactor vessel, a Raman spectrometer, and a processor. The reactor vessel has an inlet for receiving inlet gas and an exhaust outlet for releasing exhaust gas. The Raman spectrometer is connected with the exhaust outlet for determining a chemical conversion within the reactor chamber and generating a corresponding signal. The processor is connected with the Raman spectrometer to receive the signal from the Raman spectrometer. The processor is capable of comparing the signal with a set of values and calculating differences between the signal and the set of values. The processor is connected with the inlet to regulate a flow of the inlet gas. 1. A gas decomposition reactor for the decomposition of a gas into a mixture of solid and gaseous by-products , the gas decomposition reactor comprising:a reactor vessel having an inlet for receiving an inlet gas and an exhaust outlet for releasing an exhaust gas;a Raman spectrometer connected with the exhaust outlet for determining a chemical conversion within the reactor vessel and generating a corresponding signal; anda processor connected with the Raman spectrometer to receive the signal from the Raman spectrometer, the processor being capable of comparing the signal with a set of values and calculating differences between the signal and the set of values, the processor is connected with the inlet to regulate a flow of the inlet gas.2. The gas decomposition reactor of claim 1 , further comprising a feeder tube for providing particles to the reactor vessel.3. The gas decomposition reactor of claim 1 , wherein the Raman spectrometer is connected with the inlet for determining a chemical composition of the inlet gas and generating a corresponding inlet signal.4. The gas decomposition reactor of claim 3 , wherein the set of values used by the processor to calculate ...

EQUALIZING VAPOR VELOCITY FOR REACTOR INLET

The invention relates to distributing reactants more evenly across the interior space of a reactor vessel utilizing a distributor at the inlet end that initially directs the flow of reactants through a flange plate and a series of ring plates. The ring plates are physical spaced such that vapor along the wall of the inlet is mildly obstructed by the flange plate and the ring plates cause the vapor to alter course temper down any diverse velocities that may create hot spots within the catalyst bed. 1. A process for damping down higher velocity vapor flows that are concentrated asymmetrically across a generally cylindrical inlet to a reactor vessel caused by one or more bends within a conduit conveying vapor to the generally cylindrical inlet of the reaction vessel , wherein the generally cylindrical inlet comprises a peripheral wall with a length from the conduit to the reactor vessel , the process comprising:a) providing a first obstruction generally transverse within the generally cylindrical inlet of the reactor vessel at a first position along the length of the generally cylindrical inlet and near the peripheral wall of the generally cylindrical inlet and having a generally circular opening wherein the size of the first obstruction and the size of the circular opening create a pressure drop of no more than 0.25 pounds for the vapor passing through the generally cylindrical inlet;b) providing a top, ring-like obstruction spaced inwardly from the peripheral wall of the generally cylindrical inlet at a second position along the length of the generally cylindrical inlet wherein the size and shape of the top, ring-like obstruction create a pressure drop of no more than 0.25 pounds for the vapor passing through the generally cylindrical inlet;c) providing a middle, ring-like obstruction spaced further inwardly from the peripheral wall of the generally cylindrical inlet as compared to the top, ring-like obstruction at a third position along the length of the generally ...

AMMOXIDATION REACTOR CONTROL

A process is provided for control of an ammoxidation reactor. More specifically, the process includes controlling an amount of oxygen added to the reactor, steam temperature and linear velocity to minimize reactor temperature deviations. 1. An ammoxidation process comprising:introducing a flow of a reactant stream into an ammoxidation reactor, wherein the reactant stream includes ammonia, an oxygen containing gas, a hydrocarbon selected from the group consisting of propane, propylene, isobutene, isobutylene and mixtures thereof; andproviding steam to coils disposed in the ammoxidation reactor to provide a reactor operating temperature of about 350° C. to about 480° C.,wherein an amount of the oxygen added to the reactor and the steam temperature are controlled to maintain a superficial reactor linear velocity.2. The process of wherein the superficial reactor linear velocity is maintained between about 0.5 m/s to about 1.5 m/s.3. The process of wherein the superficial reactor linear velocity is maintained between about 0.7 m/s to about 1.0 m/s.4. The process of wherein the superficial reactor linear velocity is maintained between about 0.75 m/s to about 0.80 m/s.5. The process of wherein reactor temperature deviations are maintained at about 10° C. or less during changes in a heat transfer area of the coils.6. The process of wherein the steam is superheated steam and the coils are superheat coils.7. The process of wherein the superheated steam is provided with a temperature of about 355° C. to about 400° C.8. The process of wherein a reactor top pressure is maintained at about 3.8 psig to about 5.0 psig.9. The process of wherein a total available superheat coil area per reactor cross sectional area (ft/ft) is about 1 to about 7.10. The process of wherein the superheat coil area (ft) per heat removed by the superheat coils (Kcal) per metric ton of acrylonitrile produced is about 275 claim 9 ,000 to about 475 claim 9 ,000.11. The process of wherein the reactant stream ...

Beta-Mercaptoethanol Synthesis

A process includes reacting, in a reactor having a fixed bed containing a solid catalyst which contains a heterogeneous ion exchange resin, hydrogen sulfide and ethylene oxide in the presence of the solid catalyst to yield a reaction product which contains beta-mercaptoethanol. A reactor system includes the reactor, an ethylene oxide stream, a hydrogen sulfide stream, a fixed bed containing the solid catalyst placed in the reactor, and an effluent stream containing the reaction product. During steady state operation of the reactor in the process and the reactor system, the hydrogen sulfide and the ethylene oxide are present in a mole ratio in a range of about 9:1 to about 20:1. 1. A process comprising:reacting, in a reactor having a fixed bed containing a solid catalyst comprising a heterogeneous ion exchange resin, hydrogen sulfide and ethylene oxide in the presence of the solid catalyst to yield a reaction product comprising beta-mercaptoethanol, wherein during steady state operation of the reactor, the hydrogen sulfide and the ethylene oxide are present in a mole ratio in a range of about 9:1 to about 20:1, wherein an effluent of the reactor comprises the reaction product, wherein the reaction product in the effluent further comprises less than about 0.5 wt. % thiodiglycol.2. The process of claim 1 , further comprising:converting, in the reactor, at least a portion of the hydrogen sulfide from a liquid phase to a vapor phase to absorb a heat of reaction created in the step of reacting.3. The process of claim 2 , wherein the step of reacting and the step of converting occur about simultaneously.4. The process of claim 1 , wherein no internal and/or external cooling source is used to cool the reactor.5. (canceled)6. The process of claim 5 , wherein the reaction product in the effluent consists essentially of the beta-mercaptoethanol and the thiodiglycol.7. The process of claim 1 , wherein no detectable amount of ethanedithiol is present in the reaction product when ...

SYSTEMS AND METHODS FOR PREDICTING AND CONTROLLING THE PROPERTIES OF A CHEMICAL SPECIES DURING A TIME-DEPENDENT PROCESS

Devices and methods for controlling the properties of chemical species during time-dependent processes. A device includes a reactor for containing one or more chemical species of a time-dependent process, an extraction pump for automatically and continuously extracting an amount of the one or more chemical species from the reactor, one or more detectors for measuring property changes of the one or more extracted chemical species and generating a continuous stream of data related to the one or more property changes to the one or more chemical species during a time interval, and a process controller configured to fit the continuous stream of data to a mathematical function to predict one or more properties of the one or more chemical species at a future time point and make one or more process decisions based on the prediction of one or more properties at the future time point. 131-. (canceled)32. A method comprising:introducing, in a reactor, one or more chemical species to be monitored during a time-dependent process;detecting, using one or more detectors, one or more property changes to the one or more chemical species over a time interval;receiving, from the one or more detectors, a continuous stream of data related to the one or more property changes to the one or more chemical species during the time interval;fitting, using a process controller, the continuous stream of data to a mathematical function to predict one or more properties of the one or more chemical species at a future time point; andmaking, by the process controller, one or more process decisions based on the prediction of one or more properties at the future time point;wherein the continuous stream of data comprises one or more of UV absorption, visible absorption, infra-red absorption, Raman scattering, fluorescence, reduced viscosity, intrinsic viscosity, dynamic light scattering, static light scattering, Mie scattering, and evaporative light scattering.33. The method of claim 32 , wherein the ...

Hydrogen purification/storage apparatus and method using liquid organic hydrogen carrier

The present disclosure relates to a hydrogen purification/storage apparatus and method using a liquid organic hydrogen carrier (LOHC).

PUMPS, PUMP ASSEMBLIES, AND METHODS OF PUMPING FLUIDS

The present disclosure relates to a system and method for pumping a feedstock slurry through a device. The system includes a pressure pump, a first sensor, a second sensor, a controller, and a control valve. The pressure pump includes a plunger configured to pressurize the slurry to a first pressure prior to the slurry entering the device. The first sensor is configured to sense a second pressure of the slurry entering the device. The second sensor is configured to sense the position of the plunger. The controller is configured to determine a change of position of the plunger based on the sensed position of the plunger and to control the movement of the plunger by setting a plunger mode based on the second pressure of the slurry and the change of position of the plunger. The control valve is configured to control the flow rate of the slurry through the device. 1. An apparatus configured to pump slurry into a device , the apparatus comprising:a plunger configured to pressurize the slurry to a first pressure prior to the slurry entering the device;a first sensor configured to sense a second pressure of the slurry entering the device;a second sensor configured to sense the position of the plunger; anda controller configured to 1) determine a change of position of the plunger based on the sensed position of the plunger, and 2) control the movement of the plunger based on the second pressure of the slurry and the change of position of the plunger.2. The apparatus of claim 1 , wherein the movement of the plunger is controlled by setting a plunger mode claim 1 , wherein the plunger mode includes a steady mode and a clearing mode claim 1 , and wherein the plunger mode is set to the clearing mode when the second pressure is greater than a predetermined pressure threshold for a predetermined amount of time and there is substantially no change of position of the plunger.3. The apparatus of claim 2 , wherein in the clearing mode the plunger travels a first distance between ...

GAS DISTRIBUTION NOZZLE

The invention relates to a gas distributor nozzle () comprising a gas feed () directed vertically upwards and a float () with which an outlet orifice out of the gas feed () may be closed if no gas is flowing, wherein the float () has a center of gravity which is below a point of force application of the gas flow. The invention further comprises a reactor with a solid bed and at least one gas distributor nozzle (). 1113113. A gas distributor nozzle comprising a gas feed () directed vertically upwards and a float () with which an outlet orifice out of the gas feed () may be closed if the gas velocity falls below a given value , no gas is flowing or a pressure reversal occurs , wherein the float () has a center of gravity which is below a point of force application of the gas flow.2131. The gas distributor nozzle according to claim 1 , wherein the float () has a constantly narrowing diameter on the side facing towards the gas feed ().313. The gas distributor nozzle according to or claim 1 , wherein the float () comprises a cavity on its side remote from the gas feed.413171917. The gas distributor nozzle according to one of to claim 1 , wherein the float () takes the form of a hollow cone () claim 1 , the tip () of the cone () being solid.51315. The gas distributor nozzle according to one of to claim 1 , wherein the float () comprises a guide rod ().6151917. The gas distributor nozzle according to and claim 1 , wherein the guide rod () is formed at the tip () of the hollow cone ().7157. The gas distributor nozzle according to or claim 1 , wherein the guide rod () is guided in a guide ring ().821157. The gas distributor nozzle according to claim 7 , wherein a guide stop () is provided on the guide rod () which comes to a stop against the guide ring () in the open state.9133331131313. The gas distributor nozzle according to one of to claim 7 , wherein the float () is guided in a sleeve () claim 7 , said sleeve () comprising a limit stop () on which the float () rests in ...

Hydrocarbon Conversion to Ethylene

The invention relates to a hydrocarbon conversion process and a reactor configured to carry out the hydrocarbon conversion process. The hydrocarbon conversion process is directed to increasing the overall equilibrium production of ethylene from typical pyrolysis reactions. The hydrocarbon conversion process can be carried out by exposing a hydrocarbon feed to a peak pyrolysis gas temperature in a reaction zone in the range of from 850° C. to 1200° C.

Continuous production of titanium tetrachloride from titanium-bearing slags

This disclosure relates to an improved method to produce titanium tetrachloride continuously from titanium-bearing materials containing high concentrations of alkaline earth metal impurities through fluidized-bed carbochlorination. Agglomerated heavy particles in a reaction are taken out continuously from a chlorination reactor without clogging and stopping. The reactors and related methods disclosed apply to the chlorination of titanium slag containing high content of alkaline earth metal oxides of up to 15% by weight.

CONTINUOUS REACTION DEVICE FOR SYNTHESIZING POLYOXYMETHYLENE DIMETHYL ETHERS

The present invention pertains to the technical field of energy resource chemical industry, and in particular relates to a continuous reaction device and process for synthesizing polyoxymethylene dimethyl ethers by using paraformaldehyde and methylal as feedstock or using trioxane and methylal as feedstock in the presence of an acidic catalyst. The continuous reaction device comprises multiple slurry bed stirred tank reactors connected in series or in combination of series connection and parallel connection, and also comprises an on-line solid-liquid separation device to perform separation of the reaction mixture from the catalyst. Each of the tank reactors is provided with an axial-flow stirring paddle having 2-6 blades per layer, to ensure sufficient mixing of the reactants with the catalyst. By using a distributed control pattern of reaction temperature and feedstock supplying to enhance the process and to optimize the operation, the reaction device of the present invention can effectively achieve large-scale continuous production of polyoxymethylene dimethyl ethers, and both the yield rates and the distribution of the reaction product are better than those of prior art. 1. A continuous reaction device for synthesizing polyoxymethylene dimethyl ethers , the reaction using paraformaldehyde and methylal as feedstock or using trioxane and methylal as feedstock and being carried out in the presence of an acidic catalyst , wherein ,the continuous reaction device comprises multiple reactors connected in series or in combination of series connection and parallel connection, and also comprises an on-line solid-liquid separation device to perform solid-liquid separation of the reaction mixture from the catalyst;each of the tank reactors is independently controlled at a pressure of 1.0-4.0 MPa and a temperature of 50-120° C.; a molar ratio of paraformaldehyde or trioxane, metered in mole number of formaldehyde contained therein, to methylal in the feedstock is 0.5-5.0; ...

PROCESS FOR START-UP OF A MULTIZONE CIRCULATING REACTOR

A process for starting a multizone circulating reactor containing no polyolefin particles, comprising the steps of conveying gas through the reactor and the gas recycle line, feeding a particulate material comprising a polymerization catalyst and optionally polyolefin into the reactor, controlling the gas flow in a vertical reactor zone equipped with a throttling valve at the bottom so that the upwards gas velocity in the bottom part of this reaction zone is lower than the terminal free-fall velocity of the particulate material fed into the reactor, and, after the weight of the particulate polyolefin in this reactor zone is higher than the drag force of the upward moving gas, controlling the circulation rate of the polymer particles within the multizone circulating reactor by adjusting the opening of the throttling valve and adjusting the flow rate of a dosing gas. 1. A process for starting a gas-phase olefin polymerization reaction for producing a particulate polyolefin by polymerizing one or more olefins in a multizone circulating reactor , a vertical first reactor zone and', 'a vertical second reactor zone, which is equipped with a throttling valve at the bottom, a line for discharging polymer, and, in the upper part, means which allow measuring the level of a settled bed of polyolefin particles into the second reactor zone, and', 'the upper region of the first reactor zone is connected with the upper region of the second reactor zone by a first connecting part and', 'the lower region of the second reactor zone is connected with the lower region of the first reactor zone by a second connecting part; and, 'wherein the multizone circulating reactor comprises'} a gas recycle line, which is equipped with a compressor and a heat exchanger for removing the heat of polymerization and which connects the top of the first reactor zone, the top of the second reactor zone or the first connecting part with at least', 'a riser gas introduction point for feeding a riser gas at ...

Efficient in-situ catalyst sulfiding methods and systems

A system and method is disclosed for efficiently sulfiding metal catalyst resident in a reactor vessel comprises a sulfiding module and a hydrogen sulfide detection module and a remote computer all arranged and configured to communicate wirelessly and to allow remote control and monitoring of the modules and sulfiding process.

Gas decomposition reactor feedback control using raman spectrometry

A gas decomposition reactor for the decomposition of a gas into a mixture of solid and gaseous by-products is disclosed. The gas decomposition reactor includes a reactor vessel, a Raman spectrometer, and a processor. The reactor vessel has an inlet for receiving inlet gas and an exhaust outlet for releasing exhaust gas. The Raman spectrometer is connected with the exhaust outlet for determining a chemical conversion within the reactor chamber and generating a corresponding signal. The processor is connected with the Raman spectrometer to receive the signal from the Raman spectrometer. The processor is capable of comparing the signal with a set of values and calculating differences between the signal and the set of values. The processor is connected with the inlet to regulate a flow of the inlet gas.

PROCESS FOR THE LARGE-SCALE MANUFACTURE OF ZEOLITE-TEMPLATED CARBON

A method for the large-scale synthesis of a zeolite-templated carbon (ZTC). The method includes the steps of: introducing a bed material comprising a zeolite to a fluidized bed reactor and heating the bed material to a temperature between 550° C. and 800° C.; fluidizing the bed material with a fluidizing gas and maintaining the temperature of the bed material between 550° C. and 800° C.; introducing an organic carbon precursor while fluidizing the zeolite for a period of time such that carbon is deposited on the zeolite by chemical vapor deposition to produce a zeolite-carbon composite; and treating the zeolite-carbon composite with an acid solution such that the zeolite template is dissolved and the ZTC is obtained. 1. A method for large-scale synthesis of a zeolite-templated carbon (ZTC) , the method comprising the steps of:introducing a bed material comprising a zeolite to a fluidized bed reactor and heating the bed material to a first temperature between 550 degrees Celsius (° C.) and 800° C.;fluidizing the bed material with a fluidizing gas and maintaining the temperature of the bed material between 550° C. and 800° C.;introducing an organic carbon precursor while fluidizing the zeolite for a first period of time such that carbon is deposited on the zeolite by chemical vapor deposition to produce a zeolite-carbon composite;treating the zeolite-carbon composite with an acid solution such that the zeolite is dissolved and the ZTC is obtained.2. The method of claim 1 , wherein at least 100 grams of the ZTC is obtained.3. The method of claim 1 , wherein the fluidizing gas has an average gas velocity in the fluidized bed reactor that is between 5 centimeters per second (cm/s) and 25 cm/s.4. The method of claim 1 , wherein the step of fluidizing the bed material further comprises introducing the fluidizing gas such that the bed material is fluidized in a bubbling fluidization regime.5. The method of claim 1 , wherein the zeolite is a bead-type zeolite having a ...

FLUIDIZED BED REACTOR

A fluidized bed reactor includes: a reactor body; a dispersion plate mounted within the reactor body to partition the inside of the reactor body in a traverse direction and having a plurality of holes through which a reaction gas passes; a nozzle unit mounted on one surface of the dispersion plate to receive an inert gas from outside the reactor and inject the inert gas so as to crush deposits on the dispersion plate; a sensing unit configured to sense the deposits on the dispersion plate; and a control unit configured to control operation of the nozzle unit according to information sensed in the sensing unit. 1. A fluidized bed reactor for manufacturing carbon nanotubes , comprising:a longitudinally-extending reactor body;a dispersion plate mounted within the reactor body to partition the inside of the reactor body in a traverse direction and having a plurality holes; through which a reaction gas passes;a nozzle unit mounted on one surface of the dispersion plate to receive an inert gas from outside the reactor body and inject the inert gas so as to crush deposits on the dispersion plate;a sensing unit configured to sense the deposits on the dispersion plate; anda control unit configured to control an operation of the nozzle unit according to information sensed by the sensing unit.2. The fluidized bed reactor of claim 1 , comprising a plurality of nozzle units claim 1 , spaced apart from each other along a circumference of the dispersion plate.3. The fluidized bed reactor of claim 2 , wherein the nozzle units each comprise:a housing fixed to one surface of the dispersion plate on which the deposits area supply line configured to supply the inert gas from the outside into the housing; andan injection part provided in the housing to inject the inert gas.4. The fluidized bed reactor of claim 3 , wherein two or more injection parts are provided in the housing to inject the inert gas in different directions.5. The fluidized bed reactor of claim 4 , wherein at least one ...

Purified Silicon, Devices and Systems for Producing Same

The present disclosure provides devices and systems that utilize concurrent and countercurrent exchange platforms to produce purified silicon. 1. A device for purifying silicon comprising:a vessel having a top end, an opposing bottom end, and a plurality of concentric columns, the columns in fluid communication with each other;a central column comprising a silicon inlet at a top portion of a first column for introducing molten silicon into a bed of a plurality of silica particles to form a slurry;a first channel in fluid communication with a bottom portion of the central column adapted for receiving glassy particles, which are less dense than molten silicon, by floatation thereby separating the impurity-laden glassy particles from the slurry, leaving the molten silicon, the impurity-laden glassy particles upwardly flowing in the first channel;a second channel in fluid communication with the first channel for receiving the molten silicon separated from the slurry, the silicon downwardly flowing in the second channel.2. The device of wherein the silica particles are fracking sand.3. The device of wherein the slurry comprises an additive selected from the group consisting of CaSOor NaSO claim 1 , NaO and HO.4. A device for purifying silicon comprising:a vessel having a top end, an opposing bottom end, and a sidewall extending between the opposing ends and defining a chamber;a silicon inlet at a top portion of the vessel for introducing silicon particles into the chamber, the silicon particles having a temperature greater than 1350° C.;an injection structure at a bottom portion of the vessel, the injection structure having at least one orifice for introducing a molten salt composition into the chamber, the molten salt composition having a temperature greater than 1350° C. and comprising an oxidizer dissolved in the molten salt,a countercurrent exchange section located between the silicon inlet and the injection structure, the countercurrent exchange section comprising(1 ...

IN-LINE MANUFACTURE OF CARBON NANOTUBES

Mass production of carbon nanotubes (CNT) are facilitated by methods and apparatus disclosed herein. Advantageously, the methods and apparatus make use of a single production unit, and therefore provide for uninterrupted progress in a fabrication process. Embodiments of control systems for a variety of CNT production apparatus are included. 1. A method of producing an aggregate of vertically aligned carbon nanotubes , the method comprising:(a) loading a base material into a controlled environment;(b) disposing a catalyst onto the base material to provide a substrate in an environment having an oxygen concentration low enough to substantially prevent oxidation of the substrate;(c) subjecting the substrate to a carbonaceous raw material gas and heating at least one of the raw material gas and the substrate for growing the aggregate onto the substrate; and(d) cooling the aggregate in an environment having an oxygen concentration low enough to substantially prevent oxidation of the aggregate during the cooling;wherein steps (a) to (d) are performed in the controlled environment comprising chambers sequentially connected in a manner that limits the exposure of the base material and any catalyst, substrate, and aggregate disposed thereon to contamination between each step.2. The method of claim 1 , further comprising disposing a carburizing prevention layer on at least one of the base material and the catalyst.3. The method of claim 1 , wherein disposing the catalyst comprises using at least one of sputtering evaporation claim 1 , cathodic arc deposition claim 1 , sputter deposition claim 1 , ion beam assisted deposition claim 1 , ion beam induced deposition and electrospray ionization.4. The method of claim 1 , further comprising treating the substrate with a plasma.5. The method of claim 1 , further comprising subjecting the substrate to a catalyst activation material during the growing of the aggregate.6. The method of claim 5 , further comprising adding the catalyst ...

Double Loop Technology

The present invention relates to an apparatus and process for polymerizing olefins. One embodiment comprises polymerizing at least one monomer in a first loop reactor in the presence of a catalyst to produce a first polyolefin fraction. A portion of the first polyolefin fraction is transferred to a second loop reactor, connected in series with the first loop reactor. The process further comprises polymerizing in the second loop reactor at least one monomer in the presence of a catalyst to produce a second polyolefin fraction in addition to the first polyolefin fraction. The combination of the first and second polyolefin fractions can produce a polymer resin fluff having bimodal molecular weight distribution. 1. An apparatus for controlling the injection of catalyst slurry in a polymerization reactor wherein polyethylene is prepared , comprising:one or more storage vessels for storing catalyst slurry including solid catalyst in a hydrocarbon diluent, whereby each storage vessel is provided with means for transferring said catalyst slurry from said storage vessels to one or more mixing vessels,wherein each mixing vessel is connected with one of the one or more storage vessels by means of said transferring means, for diluting said catalyst slurry to a suitable concentration,one or more conduits connecting said one or more mixing vessels to a polymerization reactor for transferring said diluted catalyst slurry from said mixing vessel to said polymerization reactor, whereby each conduit is provided with a pumping means for pumping said catalyst slurry to said polymerization reactor, andthe dilution being adapted to the pumping means.2. The apparatus according to claim 1 , wherein the pumping means is a membrane pump.3. The apparatus according to wherein the dilution being adapted to the pumping means comprises the solid catalyst diluted with the hydrocarbon diluent to a concentration between 0.1 and 1.5% by weight.4. The apparatus according to wherein said catalyst is a ...

CHEMICAL LOOPING

This invention relates to a method of chemical looping using non-stoichiometric materials with a variable degree of non-stoichiometry. One application of these methods is in the water gas shift reaction for Hproduction. The methods of the invention can overcome limitations, e.g. those associated with chemical equilibria, which prevent chemical processes from proceeding with complete conversion of starting materials to products. 2. A method of claim 1 , wherein greater than 50% of both QXand P are converted to Q and PXrespectively3. A method of claim 1 , wherein the non-stoichiometric material is a solid.4. A method of claim 1 , wherein P is passed through the reactor in step A) as a mixture with other components.5. A method of claim 1 , wherein QXis passed through the reactor in step B) as a mixture with other components.6. A method of claim 1 , wherein P claim 1 , PX claim 1 , Q and QXare all gases within the temperature range of the reaction.7. A method of claim 1 , wherein X is an element.8. A method of claim 7 , wherein X is a non-metal.9. A method of claim 8 , wherein X is oxygen.10. A method of claim 9 , wherein Q is Hand QXis HO.11. A method of claim 10 , wherein P is selected from: CO claim 10 , H claim 10 , at least one organic molecule or a mixture thereof.12. A method of claim 1 , wherein P is CO claim 1 , PXis CO claim 1 , Q is Hand QXis HO.13. A method of claim 1 , wherein P is a mixture of Hand CO claim 1 , PXis a mixture of HO and CO claim 1 , Q is Hand QXis HO.14. A method of claim 13 , the method comprising a step F before step A claim 13 , step F comprising forming the mixture of Hand CO by reforming a hydrocarbon.15. A method of claim 1 , wherein P is at least one organic molecule claim 1 , PXis a mixture of CO and H claim 1 , Q is Hand QXis HO.16. A method of claim 15 , wherein the mixture of Hand CO obtained in step A is subsequently further oxidised to COor HO and the heat which is generated during said oxidation is extracted and transferred to ...

SYSTEMS AND METHODS FOR PROCESSING FLUOROPOLYMER MATERIALS AND RELATED WORKPIECES

A method for removing perfluorinated compounds from a fluoropolymer material is provided. The method includes the steps of: (a) providing the fluoropolymer material in a chamber; (b) providing an anaerobic environment in the chamber; and (c) providing a fluorination gas in the chamber, thereby exposing the fluoropolymer material to the fluorination gas. The method results in the removal the perfluorinated compounds from the fluoropolymer material. 2. The method of claim 1 , wherein the fluoropolymer material comprises the perfluorinated compounds used in the manufacture of the fluoropolymer material.3. The method of claim 1 , wherein the amount of the perfluorinated compounds in the processed fluoropolymer material is less than 1.1% the amount of the perfluorinated compounds in the fluoropolymer material.4. The method of claim 1 , wherein the perfluorinated compounds comprise perfluorooctanoic acid (PFOA) and an amount of the PFOA in the processed fluoropolymer material is less than 1.1% the amount of PFOA in the fluoropolymer material.5. The method of claim 1 , wherein the fluoropolymer material is a fluoropolymer micropowder claim 1 , the perfluorinated compounds comprise PFOA claim 1 , and the amount of PFOA in the processed fluoropolymer material is less than 100 ppt.6. The method of claim 1 , wherein the fluoropolymer material is a PTFE micropowder claim 1 , the perfluorinated compounds comprise PFOA claim 1 , and the amount of PFOA in the processed fluoropolymer material is less than 100 ppt.7. The method of claim 1 , further comprising the step of heating the chamber to a temperature in a range of 25° C. to 325° C. claim 1 , and wherein the fluoropolymer material is exposed to the fluorination gas at a chamber pressure in a range of 5 PSIA to 55 PSIA.8. The method of claim 1 , wherein the fluoropolymer material is exposed to the fluorination gas for a time period in a range of 1 hour to 1000 hours claim 1 , and wherein the fluorination gas comprises 1 vol % ...

Process, reactor and system for catalytic cracking of hydrocarbon oils

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

METHOD, TUBE BUNDLE REACTOR AND REACTOR SYSTEM FOR CARRYING OUT CATALYTIC GAS PHASE REACTIONS

A method for carrying out catalytic gas phase reactions including providing a tube bundle reactor which has a bundle of reaction tubes that are filled with a catalyst charge and are cooled by a heat transfer medium, conveying a reaction gas through the catalyst charge, the reaction gas flowing into each reaction tube divided into two part flows introduced in the axial direction of the reaction tube at different points in the catalyst charge the catalyst charge has at least two catalyst layers of different activity, wherein the activity of the first catalyst layer, in the flow direction of the reaction gas, is lower than the activity of the at least one other catalyst layer and in step a first part flow is introduced into the first catalyst layer and each further part flow is introduced past the first catalyst layer into the at least one further catalyst layer. 120.-. (canceled)21. A method for carrying out catalytic gas phase reactions which include methanation reactions , comprising:a) providing a tube bundle reactor that has a bundle of reactor tubes filled with a catalyst charge and are cooled by a heat transfer medium; andb) conveying a reaction gas through the catalyst charge, wherein the reaction gas flowing into each reaction tube is divided into at least two partial flows that are introduced into the catalyst charge in an axial direction of the reaction tube at different points,wherein the catalyst charge has at least two catalyst layers of different activity,wherein an activity of a first catalyst layer in a flow direction of the reaction gas is set to 5% to 90% of an activity of at least one second catalyst layer; andintroducing a first partial flow into the first catalyst layer and each further partial flow is introduced past the first catalyst layer into at least one second catalyst layer.22. The method according to claim 21 , wherein the activity of the first catalyst layer is set to 10% to 40% claim 21 , of the activity of the at least one second ...

METHOD AND APPARATUS FOR PRODUCING CARBON MONOXIDE

A method and apparatus for producing carbon monoxide, wherein the carbon monoxide is formed from a gaseous feed which includes at least carbon dioxide. The method includes supplying oxygen to a carbon dioxide stream for forming a carbon dioxide based mixture, supplying the carbon dioxide based mixture to a hydrogen based stream to form the gaseous feed, supplying a hydrocarbon containing stream to the hydrogen based stream before the supply of the carbon dioxide based mixture, feeding the gaseous feed into a reactor which includes at least one catalyst, treating the gaseous feed by partial oxidation in the reactor so that carbon dioxide reacts with hydrogen in the reactor in presence of oxygen and heat is formed during the reaction, and recovering a product composition including at least carbon monoxide and hydrogen from the reactor. 1. A method for producing carbon monoxide , wherein the carbon monoxide is formed from a gaseous feed which comprises at least carbon dioxide , wherein the method comprisessupplying oxygen to a carbon dioxide stream for forming a carbon dioxide based mixture,supplying the carbon dioxide based mixture to a hydrogen based stream to form the gaseous feed,supplying a hydrocarbon containing stream to the hydrogen based stream before the supply of the carbon dioxide based mixture,feeding the gaseous feed into a reactor which comprises at least one catalyst,treating the gaseous feed by means of a partial oxidation in the reactor so that carbon dioxide reacts with hydrogen in the re-actor in presence of oxygen and heat is formed during the reaction, andrecovering a product composition comprising at least carbon monoxide and hydrogen from the reactor.2. The method according to claim 1 , wherein the gaseous feed is fed with high velocity to the reactor such that the velocity of the gas stream is ≥0.5 m/s.3. The method according to claim 1 , wherein a treatment temperature is 800-1500° C. in the reactor.4. The method according to claim 1 , wherein ...

REACTOR AND FEED DISTRIBUTION ASSEMBLY

Embodiments include a reactor and feed distribution assembly. The reactor and feed distribution assembly can include a reactor vessel, a gaseous feed conduit, a catalyst feed conduit, a catalyst feed conduit housing, and a catalyst backflow diverter. 1. A reactor and feed distribution assembly comprising: the bottom has an inner surface and an outer surface,', 'the gaseous feed distribution assembly has a first surface that faces the inner surface, a second surface that is spaced apart from and faces away from the first surface, and an outer plate surface having a portion that is normal to the first surface and the second surface, wherein the gaseous feed distribution assembly defines a plurality of gas passageways, each of the plurality of gas passageways being in fluid communication with the first surface and the second surface via first apertures and second apertures, the second apertures having a greater cross-sectional area than the first apertures, and wherein distribution assembly insulation packing is disposed between a lower portion of refractory-lined inner wall surface that is nearer to where the refractory-lined inner wall surface connects to the bottom than to where the refractory-lined inner wall surface connects to the top,', 'the mounting plate having a first end, which is operatively connected to the bottom, and a second end, wherein the first end and the second end are spaced apart from one another and there between define an outer planar surface that is spaced apart from an inner planar surface, the outer planar surface being spaced apart from the refractory-lined inner wall surface, the outer plate surface being operatively connected to a portion of the inner planar surface proximate to the second end and apart from the first end,, 'a reactor vessel having a refractory-lined inner wall surface, an outer wall surface, a bottom, a top, a gaseous feed distribution assembly, and a mounting plate, whereina gaseous feed conduit that is operatively ...

Fluidized bed reactor and method for producing granular polysilicon

Granular polysilicon is produced in a fluidized-bed reactor by fluidizing silicon particles by means of a gas flow in a fluidized bed heated to a temperature of 850-1100° C., adding a silicon-containing reaction gas by means of a nozzle and depositing of silicon on the silicon particles, wherein, in at least 56% of an axially symmetric region around a nozzle opening of the nozzle, the reaction gas concentration is greater than 75% of the maximum concentration of the reaction gas (10 to 50 mol %), the fluidized-bed temperature is greater than 95% of the fluidized-bed temperature outside the axially symmetric region (850-1100° C.) and the solids concentration is greater than 85% of the solids concentration at the edge of the fluidized bed (55 to 90% by volume).

In-situ Catalyst Sulfiding, Passivating and Coking Systems and Methods

A system and method for efficiently treating metal catalyst resident in a reactor vessel comprises a sulfiding module, a sulfur source, an ammonia source, and/or a coking source, a hydrogen sulfide detection module, a hydrogen gas detection module, a pH detection module, an ammonia gas detection module and a remote computer all arranged and configured to communicate wirelessly and to allow remote control and monitoring of the modules and process so that catalyst may be sulfided, passivated and/or soft-coked in situ. 1. A system for in situ treatment of a metal catalyst , comprising: a module inlet and outlet,', 'a sulfur-containing product measurement device,', 'a sulfur product pressurization device having a variably controllable output,', 'a nitrogen-containing product pressurization device having a variably controllable output,', 'a controller in electrical communication with at least the measurement device and the sulfur and nitrogen pressurization devices, and', 'a first communication device configured to transmit information between the module and an external site;, 'a mobile sulfiding module comprising'} an inlet and outlet,', 'a hydrogen sulfide concentration detection device located between the inlet and outlet,', 'a hydrogen gas concentration detection device located between the inlet and the outlet, and', 'a second communication device configured to transmit information between the hydrogen sulfide detection device and the external site and between the hydrogen gas detection device and the external site; and, 'a mobile detection module comprising'}an ammonia gas detection module having a communication device configured to transmit information between the ammonia detector detection device and the external site.2. The system of claim 1 , wherein the external site is a laptop computer.3. The system of claim 1 , wherein the external site is a website on the Internet.4. The system of claim 1 , wherein the pressurization devices comprise pumps.5. The system of ...

HYDROPROCESSING METHOD WITH HIGH LIQUID MASS FLUX

In a method of hydroprocessing, hydrogen gas for the hydroprocessing reaction is combined with a liquid feed composition comprising a feedstock to be treated and a diluent to form a feed stream, at least a portion of the hydrogen gas being dissolved in the liquid feed composition of the feed stream, with non-dissolved hydrogen gas being present in the feed stream in an amount of from 1 to 70 SCF/bbl of the liquid feed composition. The feed stream is contacted with a hydroprocessing catalyst, within a reactor while maintaining a liquid mass flux within the reactor of at least 5000 lb/hr·ftto form a hydroprocessed product. 1. A method of hydroprocessing comprising:combining hydrogen gas for the hydroprocessing reaction with a liquid feed composition comprising a feedstock to be treated and a diluent to form a feed stream, at least a portion of the hydrogen gas being dissolved in the liquid feed composition of the feed stream, with non-dissolved hydrogen gas being present in the feed stream in an amount of from 1 SCF to 70 SCF per bbl of the liquid feed composition; and{'sup': '2', 'contacting the feed stream with a hydroprocessing catalyst within a reactor while maintaining a liquid mass flux within the reactor of at least 5000 lb/hr·ftto form a hydroprocessed product.'}2. The method of claim 1 , wherein:the feedstock comprises at least one of a petroleum feedstock, a non-petroleum feedstock, a bio oil, a pyrolysis oil, a high-contaminant feedstock, and a high-olefinic feedstock.3. The method of claim 1 , wherein:the feed stream is contacted with a hydroprocessing catalyst contained in at least two catalyst beds within the reactor.4. The method of claim 1 , wherein:the non-dissolved hydrogen gas in the feed stream is present in an amount of from 1 SCF to 50 SCF per bbl of the liquid feed composition.5. The method of claim 1 , wherein:{'sup': 2', '2, 'the liquid mass flux within the reactor is maintained at from 5000 lb/hr·ftto 100,000 lb/hr·ft.'}6. The method of claim ...

Polymerization Using a Spiral Heat Exchanger

This invention relates to a polymerization process for forming polymer comprising: contacting (typically in a solution or slurry phase), a monomer and a catalyst system in a reaction zone comprising at least one spiral heat exchanger and recovering polymer, wherein the monomer, the catalyst system and the polymer flow through the at least one spiral heat exchanger in a cross-flow direction relative to spirals of the at least one spiral heat exchanger. 1. A polymerization process for forming polymer comprising:contacting a monomer and a catalyst system in a reaction zone comprising at least one spiral heat exchanger and recovering polymer,wherein the monomer, the catalyst system and polymer flow through the at least one spiral heat exchanger in a cross-flow direction relative to spirals of the at least one spiral heat exchanger.225.-. (canceled)26. The polymerization process of claim 1 , wherein the catalyst system comprises a catalyst compound and an activator.27. The polymerization process of claim 26 , wherein the catalyst compound is selected from the group consisting of a pyridyldiamido compound claim 26 , a metallocene compound [8 commercial catalysts].28. The polymerization process of claim 1 , further comprising contacting a scavenger with the monomer and the catalyst system in the reaction zone.29. The polymerization process of claim 28 , wherein the scavenger is present at a molar ratio less than 10:1.30. The polymerization process of claim 28 , wherein scavenger is present at 0 mol %.31. The polymerization process of claim 28 , wherein the scavenger is water.32. The polymerization process of claim 1 , wherein polymer is produced at a rate of at least about 600 grams per liter of reactor volume.33. The polymerization process of claim 1 , wherein the polymerization process is conducted at a temperature from about 50° C. to about 220° C.34. The polymerization process of claim 1 , wherein the at least one spiral heat exchanger removes heat at a rate of about ...

ROTARY BOTTOM ASH REGENERATION SYSTEM

A rotary bottom ash regenerating (RBAR) system [ comprises a cylindrical body [] that receives ash [ containing reactant particles [ that are partially reacted limestone compounds having unreacted cores [ from a furnace. Sensors [ sense physical parameters within the cylindrical body [ A controller [ receives the output of the sensors [ and information indicating the amount of unreacted core [ and causes a fluid actuator [ to spray a proper amount of regeneration fluid regulator [ from a plurality of spray nozzles [ to different locations within the cylindrical body [ to regulate the temperature and to cause the reactant particles [ to have a require content of regeneration fluid. This causes the reactant particles [ to be regenerated and reused. This results in a lower limestone costs and less overheating of ash handling systems. 1. (canceled)2. (canceled)3. (canceled)4. (canceled)5. (canceled)6. (canceled)7. (canceled)8. (canceled)9. (canceled)10. (canceled)11. A rotary bottom ash regeneration (RBAR) system for processing bottom ash having partially reacted reactant particles of a circulating fluidized bed furnace comprising:a cylindrical body adapted to receive said bottom ash at an inlet end and rotate;at least one sensor disposed within the cylindrical body adapted to measure a physical conditions, and create at least one output signal representing the measured physical conditions;at least one spray nozzle adapted to receive a regeneration fluid and spray the regeneration fluid onto the bottom ash in the cylindrical body;a fluid actuator coupled to the at least one spray nozzle adapted to spray a specified amount of regeneration fluid in the cylindrical body when activated; receive the sensor output signal,', 'calculate amounts of regeneration fluid to be provided to the cylindrical body, and', 'activate the fluid actuator to provide the calculated amount of regeneration fluid to the bottom ash in the cylindrical body thereby regenerating the reactant particles ...

FLUIDIZED BED REACTION SYSTEM AND METHOD OF PRODUCING TITANIUM TETRACHLORIDE

This disclosure relates to a fluidized bed reaction system and method for continuous production of titanium tetrachloride from titanium-bearing materials containing high concentrations of alkaline earth metal impurities. Agglomerated heavy particles in a reaction are taken out continuously from a chlorination reactor without clogging and stopping. The reactors and related methods disclosed apply to the chlorination of titanium slag containing high content of alkaline earth metal oxides of up to 15% by weight. 1. A fluidized bed reaction system comprising:a reaction vessel lined with a refractory material configured for running an exothermic reaction therein;a baseplate providing a base for the reaction vessel and comprising a first surface, a second surface lower than the first surface, and a side surface interconnecting between the first and second surfaces, the side surface comprising a portion that is not parallel to either of the first and second surfaces;a collection zone comprising a space under a level of the first surface and defined by the second surface and the side surface for collecting agglomerated particles from the reaction while running the reaction in the reaction vessel;a reaction zone comprising a space above the collection zone and further above the first surface, in which the reaction is occurring primarily within the reaction vessel;a plurality of first nozzles formed through the first surface of the baseplate and configured for supplying fluidizing gas directly into the reaction zone;a plurality of second nozzles formed through the second surface and configured for supplying fluidizing gas into the reaction zone via the collection zone; anda gas flow control configured for controlling flow of the fluidizing gas to the plurality of first nozzles and to the plurality of second nozzles such that a linear fluidizing velocity of the fluidizing gas supplied through the plurality of second nozzles is substantially lower than a linear fluidizing ...

System and Method for On Stream Catalyst Replacement

A system of reforming reactors comprises a plurality of reactors coupled by flow lines, a feed header coupled to the plurality of reactors by a plurality of feed lines, an effluent header coupled to the plurality of reactors by a plurality of effluent lines, and a plurality of valves disposed in the flow lines, the feed lines, and the effluent lines. Each reactor comprises a reforming catalyst, and the plurality of valves are capable of being dynamically operated to create a first serial flow path through the plurality of reactors. The plurality of valves is further configured to dynamically reconnect the plurality of reactors to create a second serial flow path through the plurality of reactors. A first reactor of the plurality of reactors is adjacent to a second reactor of the plurality of reactors in the first serial flow path, and the first reactor is not adjacent to the second reactor in the second serial flow path. 1. A system comprising:a plurality of reactors coupled by flow lines, wherein each reactor comprises a reforming catalyst;a feed header coupled to the plurality of reactors by a plurality of feed lines;an effluent header coupled to the plurality of reactors by a plurality of effluent lines; anda plurality of valves disposed in the flow lines, the feed lines, and the effluent lines,wherein the plurality of valves are capable of being dynamically operated to create a first serial flow path through the plurality of reactors, wherein a first reactor of the plurality of reactors is adjacent to a second reactor of the plurality of reactors in the first serial flow path,wherein the plurality of valves are further configured to dynamically reconnect the plurality of reactors to create a second serial flow path through the plurality of reactors, wherein the first reactor is not adjacent to the second reactor in the second serial flow path.2. The system of claim 1 , wherein the plurality of valves are further configured to bypass at least one reactor of the ...

FLUID CATALYTIC REACTORS WHICH INCLUDE FLOW DIRECTORS

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

CATALYST FEED CONTROL DURING CATALYST TRANSITION PERIODS

Techniques are provided for operating a reactor during a catalyst transition period. The instantaneous reaction rate during a catalyst transition period can be determined using real-time measured process variables, and material balance calculations to provide an instantaneous reaction rate in approximately real time. According to certain embodiments, a material balance can be performed on the reactor system using a continuous ideal stirred tank reactor to determine the fractions of each type of catalyst that are present in the reactor, as well as the overall weight percent of catalyst in the reactor. A controller can then calculate the overall instantaneous reaction rate based on the respective catalyst fractions and the overall weight percent of catalyst in the reactor. The catalyst feed rate can then be adjusted based on the determined instantaneous reaction rate to maintain the instantaneous reaction rate within desired limits during a catalyst transition period. 1. A reactor system , comprising:a reactor configured to polymerize monomer into polymer solids;a monomer feed system configured to feed the monomer to the reactor;a catalyst feed system configured to feed a first catalyst and a second catalyst to the reactor; anda control system configured to perform a material balance on the reactor to determine respective fractions of the first catalyst and the second catalyst in the reactor during a catalyst transition period, and configured to determine an overall instantaneous reaction rate based on the respective fractions, wherein the material balance is based at least on an effluent rate of the polymer solids exiting the reactor.2. The reactor system of claim 1 , wherein the control system comprises a workstation configured to display the overall instantaneous reaction rate claim 1 , and wherein the control system is configured to receive a user input that adjusts a feed rate for the second catalyst based on the overall instantaneous reaction rate.3. The reactor ...

METHODS OF MONITORING AND CONTROLLING THE MELT INDEX OF A POLYOLEFIN PRODUCT DURING PRODUCTION

Methods for producing polyolefin polymers may use a predictive melt index regression to estimate the melt index of the polyolefin during production based on the composition of the gas phase and, optionally, the concentration of catalyst in the reactor or reactor operating conditions. Such predictive melt index regression may include multiple terms to account for concentration of ICA in the reactor, optionally concentration of hydrogen in the reactor, optionally concentration of comonomer in the reactor, optionally the catalyst composition, and optionally reactor operating conditions. One or more terms may independently be represented by a smoothing function that incorporates a time constant. 124.-. (canceled)25. A method comprising:contacting in a fluidized bed gas phase reactor an olefin monomer with a catalyst system in the presence of an induced condensing agent (ICA) and optionally hydrogen to produce a polyolefin having a melt index;monitoring a reactor ICA concentration, optionally a reactor hydrogen concentration, and the melt index of the polyolefin;calculating a predictive melt index regression based on an effect of the concentration of the ICA in the reactor and optionally an effect of the hydrogen in the reactor on the melt index of the polyolefin, wherein at least one term of the predictive melt index regression associated with the concentration of the ICA or the concentration of the hydrogen is independently represented by a smoothing function that incorporates a time constant;calculating a predicted melt index using the predictive melt index regression based on a change in the reactor ICA concentration; andadjusting the reactor ICA concentration based on the predicted melt flow index to maintain the melt index within or move the melt index to within a melt index threshold range.26. The method of claim 25 , wherein terms of the predictive melt index regression associated with the concentration of the ICA and the concentration of the hydrogen are each ...

FLUIDIZED BED REACTOR SYSTEM

A fluidized bed reactor system with one or more fluidized bed reactors for carrying out chemical or physical reactions, at least one reactor thereof being a rapidly fluidized reactor to be operated as a circulating fluidized bed and having, at the upper end, a fluid outlet, a particle separator, and a particle line connected thereto for the purpose of feeding back separated fluidized bed particles into the same or a further reactor, wherein, at least one rapidly fluidized reactor has one or more flow control devices producing reaction zones that are separate from one another, and in order to control the flow conditions into the reaction zones, one or more of these flow control devices are specifically adjustable from outside of the system. 1. A fluidized-bed reactor system , comprising:a fast fluidized bed reactor configured to carry out chemical or physical reactions,wherein the fast fluidized bed reactor is configured to be operated as a circulating fluidized bed,wherein the fast fluidized bed reactor comprises, at the upper end, a fluid outlet, a particle separator, and a particle line connected so as to feed back separated fluidized-bed particles into the same or another reactor,wherein one or more flow controllers are provided in at least one fast fluidized reactor in order to create separate reaction zones therein, andwherein one or more of the flow controllers are accurately adjustable from outside of the system to control flow conditions in the reaction zones.2. The system of claim 1 , wherein a horizontal cross-sectional area of the at least one fast fluidized reactor at a height of an accurately adjustable flow controller claim 1 , is changeable by adjusting the flow controller.3. The system of claim 1 , wherein at least one of the accurately adjustable flow controllers can be adjusted by hand.4. The system of claim 1 , wherein at least one of the accurately adjustable flow controllers is driven by a motor.5. The system of claim 1 , wherein the accurately ...

Co-production of methanol, ammonia and urea

A process and plant for the co-production of methanol and ammonia together with urea production from a hydrocarbon feed without venting to the atmosphere carbon dioxide captured from the methanol or ammonia synthesis gas and without using expensive air separation units and water gas shift. Carbon dioxide is removed from flue gas from reforming section and used to convert partially or fully all ammonia into urea.

SYSTEM AND METHOD FOR POLYMERIZATION

Techniques are provided for polymerization. A polymerization method may include polymerizing a monomer in a polymerization reactor to produce a slurry comprising polyolefin particles and a diluent, flowing the slurry out of the polymerization reactor through an outlet of the polymerization reactor, receiving the slurry from the outlet into a slurry handling system, conveying a first mixture from the slurry handling system to a diluent and monomer recovery system, and injecting steam into the first mixture downstream of the slurry handling system using a steam injection system. 130.-. (canceled)31. A system , comprising:a loop slurry polymerization reactor configured to polymerize a monomer into polyolefin particles;a slurry handling system configured to receive a slurry comprising the polyolefin particles suspended in a liquid diluent from the polymerization reactor and to provide the slurry to a diluent and monomer recovery system downstream of the slurry handling system; anda steam injection system configured to inject steam into the slurry such that the steam interacts with the slurry downstream of the loop slurry polymerization reactor to substantially prevent further polymerization of the monomer.32. The system of claim 31 , wherein the steam injection system comprises a steam control valve and a mass flow meter to control the amount of steam injected into the slurry claim 31 , and wherein the mass flow meter is an inertial flow meter claim 31 , a Coriolis meter claim 31 , a thermodynamic meter claim 31 , or a combination thereof.33. The system of claim 31 , comprising a feed system configured to provide a catalyst to the loop slurry polymerization reactor claim 31 , such that the slurry comprises the catalyst claim 31 , and wherein the catalyst is a chromium-based catalyst claim 31 , a Ziegler-Natta catalyst claim 31 , a metallocene catalyst claim 31 , a vanadium-based catalyst claim 31 , a nickel-based catalyst claim 31 , or a combination thereof.34. The ...

OXIDATIVE COUPLING OF METHANE SYSTEMS AND METHODS

Systems and methods conducive to the formation of one or more alkene hydrocarbons using a methane source and an oxidant in an oxidative coupling of methane (OCM) reaction are provided. One or more vessels each containing one or more catalyst beds containing one or more catalysts each having similar or differing chemical composition or physical form may be used. The one or more catalyst beds may be operated under a variety of conditions. At least a portion of the catalyst beds may be operated under substantially adiabatic conditions. At least a portion of the catalyst beds may be operated under substantially isothermal conditions. 115.-. (canceled)16. A system for generating hydrocarbons having two or more carbon atoms (C hydrocarbons) , comprising:a methane source that provides methane;an oxidant source that provides an oxidant;{'sub': '2+', 'a reaction unit in fluid communication with said methane source and said oxidant source, said reaction unit comprising a catalyst bed that includes at least one oxidative coupling of methane (OCM) catalyst, wherein said OCM catalyst facilitates an OCM reaction using said methane from said methane source and said oxidant from said oxidant source to generate said C hydrocarbons, and wherein said catalyst bed has an inlet zone that is contacted by a bulk gas mixture formed upon entry of said methane from said methane source and said oxidant from said oxidant source into said reaction unit; and'}a control unit operably coupled to said reaction unit, wherein said control unit is programmed to:(a) maintain a thermal profile across said catalyst bed during said OCM reaction, which thermal profile is characterized by (i) a temperature of said inlet zone being less than about 600° C., and (ii) a maximum temperature within said catalyst bed being greater than about 800° C.;(b) maintain a pressure within said reaction unit greater than about 15 pounds per square inch gauge (psig); and{'sub': '2+', '(c) maintain said OCM reaction within ...

BI-MODAL RADIAL FLOW REACTOR

A bi-modal radial flow reactor comprising: a cylindrical outer housing surrounding at least five cylindrical, concentric zones, including at least three annulus vapor zones including an outer annulus vapor zone, a middle annulus vapor zone, and a central annulus vapor zone, and at least two catalyst zones, including an outer catalyst zone and an inner catalyst zone, wherein the outer catalyst zone is intercalated with the outer annulus vapor zone and the middle annulus vapor zone, and wherein the inner catalyst zone is intercalated with the middle annulus vapor zone and the central annulus vapor zone; and a manifold configured to introduce a feed vertically into a bottom end of each of one or two of the at least three annulus vapor zones, and remove a product from a bottom end of each of the one or two remaining of the at least three annulus vapor zones. 1. A bi-modal radial flow reactor comprising:a cylindrical outer housing surrounding at least five cylindrical, concentric zones, including at least three annulus vapor zones and at least two catalyst zones, wherein the at least two catalyst zones comprise an outer catalyst zone and an inner catalyst zone, and wherein the at least three annulus vapor zones comprise an outer annulus vapor zone, a middle annulus vapor zone, and a central annulus vapor zone, wherein the central annulus vapor zone extends along a centerline of the bi-modal radial flow reactor, and wherein the outer catalyst zone is intercalated with the outer annulus vapor zone and the middle annulus vapor zone, and wherein the inner catalyst zone is intercalated with the middle annulus vapor zone and the central annulus vapor zone,wherein each of the at least five cylindrical, concentric zones has a top end and a bottom end; and(a) wherein each of the at least three annulus vapor zones has an opening at the bottom end thereof, operable as an inlet or an outlet of the bi-modal radial flow reactor; or (b) wherein (i) the middle annulus vapor zone has an ...

FUEL REFORMING SYSTEM

Provided is a fuel reforming system that can convert gasoline into alcohol in a vehicle. Provided is a fuel reforming system () equipped with a reformer () having a reforming catalyst () that uses air to reform gasoline to produce alcohol, a mixer () which mixes gasoline and air and supplies the mixture to the reformer (), and a condenser () which separates the gas produced in the reformer () into a gas phase and a condensed phase of which reformed fuel is the primary constituent; wherein the fuel reforming system () is characterized in that the reforming catalyst () is configured including a main catalyst for extracting hydrogen atoms from the hydrocarbons in the gasoline to produce alkyl radicals, and a catalytic promoter for reducing alkyl hydroperoxides produced from the alkyl radicals to produce alcohol. 1. A fuel reforming system comprising:a reformer that includes a reforming catalyst which reforms hydrocarbons in fuel consisting of gasoline or gasoline that contains alcohol using air to produce alcohols;a mixer that is provided upstream of the reformer, and mixes the fuel and air and supplies to the reformer; anda condenser that is provided downstream of the reformer, and separates product gas generated by the reformer into a condensed phase with reformed fuel as a main constituent and a gas phase,wherein the reforming catalyst is configured to include a primary catalyst which abstracts hydrogen atoms from hydrocarbons in the fuel to produce alkyl radicals, and an auxiliary catalyst which reduces alkyl hydroperoxides generated from the alkyl radicals and oxygen to produce alcohols, andwherein the reformed fuel has a higher octane rating than the fuel.2. The fuel reforming system according to claim 1 , wherein the primary catalyst is an N-hydroxyimide group-containing compound.3. The fuel reforming system according to claim 1 , wherein the auxiliary catalyst is a transition metal compound.4. The fuel reforming system according to claim 1 , wherein the ...

IN-LINE TRIMMING OF DRY CATALYST FEED

A process for polymerizing polyethylene is disclosed. The process comprises contacting ethylene and at least one comonomer with a catalyst system to produce a polyolefin. The first catalyst and at least a portion of the second catalyst are co-supported to form a commonly-supported catalyst system. The catalyst system is introduced to a line as a dry-feed. The line is coupled with a polymerization reactor. A carrier fluid is added to the line to form a slurry. The slurry is introduced to the polymerization reactor. 1. A method for producing a polyolefin comprising:contacting a dry-feed composition and a solution composition in a line to form a slurry composition, the dry-feed composition comprising a contact product of a first catalyst, a second catalyst, a support, and a first activator, and the solution composition comprising a contact product of an activator, a diluent, and the first catalyst or the second catalyst;introducing a carrier gas to the line;introducing the slurry composition from the line into a gas-phase fluidized bed reactor;exposing the slurry composition to polymerization conditions; andobtaining a polyolefin.2. The method of claim 1 , wherein the carrier gas is selected from nitrogen claim 1 , argon claim 1 , ethane claim 1 , propane claim 1 , and mixtures thereof.3. The method of claim 1 , wherein the carrier gas is nitrogen.4. The method of claim 3 , wherein the carrier gas is introduced at a rate of from 0.4 kg/hr to 45 kg/hr.5. The method of claim 1 , wherein the diluent is an alkane.6. The method of claim 5 , wherein the diluent is isopentane or isohexane.7. The method of claim 1 , wherein the solution composition is free of a support.8. The method of claim 1 , wherein the dry-feed composition is free of a nucleating agent.9. The method of claim 8 , further comprising mixing the slurry composition in a static mixer or agitated vessel before introducing the slurry composition to the reactor.10. The method of claim 9 , wherein mixing the slurry ...

Fluidized-bed-type reactor, and method for manufacturing trichlorosilane

A fluidized-bed reactor (1A) includes a reaction vessel (10A) configured to contain metallurgical grade silicon powder and a hydrogen chloride gas, and a portion of a side wall (w) which portion extends along at least 80% of a height extending from a gas feed opening (21), which is provided in a lower part of the reaction vessel (10A), to a top face of a fluid bed (40) has such a tapered shape that a cross section of the reaction vessel (10A) which cross section is taken perpendicular to a height direction of the reaction vessel (10A) increases in area in an upward direction.

Flex-Fuel Hydrogen Reformer for IC Engines and Gas Turbines

An on-board Flex-Fuel Hreforming apparatus provides devices and the methods of operating these devices to produce Hand CO from hydrocarbons and bio-fuels. One or more parallel autothermal reformers are used to convert the fuels into Hover the Pt group metal catalysts without external heat and power. The produced reformate is then cooled and the dry gas is compressed and stored in vessels at a pressure between 1 to 100 atmospheres. For this system, the pressure of the storage vessels and the flow control curves are used directly to control the amount of the reformers' reformate output. 1): An on-board Flex-Fuel HReforming apparatus provides devices comprising:{'sub': '2', 'a). Providing one or more parallel autothermal (ATR) reformers for producing Hand CO from hydrocarbons and/or bio-fuels over supported and/or unsupported Pt group catalysts;'}b). Providing one automatic control system comprising a control computer and/or microprocessors, flow meters/controllers, valves, pumps, sensors and thermocouples;c). Providing a stream of the ATR reformer's inlet fuel mixture comprising at least one oxidant, at least one fuel and at least one water/steam, wherein the reactants are selected from the reactant supply group consisting of liquid fuel loop, gas fuel loop, water supply loop, air supply loop, water electrolyzer loop, exhaust gas recycle (EGR) loop, water recycle loop and reformate recycle loop;{'sub': 2', '2', '2', '2, "d). Reacting said stream of the inlet fuel mixture over said catalysts inside the ATR reformer to produce a reformate containing Hand CO from said fuels, and simultaneously controlling said fuel mixture's O/C, HO/C and CO/C ratios within a given range so that the maximum ATR reaction temperature is kept constantly below 1200° C.;"}e). Providing one or more vessels/manifolds for storing the condensed water for the reformers and also storing said dry reformate produced from the ATR reformers at a pressure between 1 to 100 atmospheres, which is used by ...

SYSTEMS AND METHODS FOR IMPROVING FLOW IN RADIAL FLOW REACTOR

A radial flow distribution system, a radial flow reactor, and components thereof, including one or more of a scallop, center pipe, and/or outer basket. Each of the scallop, the center pipe, and the outer basket has openings formed therein. wherein the sizes or the shapes of the openings vary along the length or the width of the reactor components such that the openings define a pattern in configured to manipulate and optimize the distribution of flow of feedstock out of the components and through the reactor to maximize the efficiency of the catalyst reaction thereof. 1. A scallop for use in a radial flow reactor , comprising:an elongated flow distribution conduit having a top end and an opposing bottom end, a length extending between the top and bottom ends, opposing sides, and a width extending between the opposing sides;a plurality of openings formed in the conduit through a thickness thereof, each of the plurality of openings having a size and a shape,wherein the sizes or the shapes of the plurality of openings vary along the length or the width of the conduit such that the plurality of openings define a pattern in the conduit configured to manipulate and optimize the distribution of flow of feedstock out of the scallop and through the reactor to maximize the efficiency of the catalyst reaction thereof.2. The scallop of claim 1 , wherein the sizes of the plurality of openings vary along the length and the width of the conduit.3. The scallop of claim 1 , wherein the shapes of the plurality of openings vary along the length and the width of the conduit.4. The scallop of claim 1 , wherein the sizes and the shapes of the plurality of openings vary along the length of the conduit.5. The scallop of claim 1 , wherein the sizes and the shapes of the plurality of openings vary along the width of the conduit.6. The scallop of claim 1 , wherein the sizes and the shapes of the plurality of openings vary along the length and width of the conduit.7. The scallop of claim 1 , ...

PROCESS FOR PRODUCING A MULTIFUNCTIONAL PRODUCT AND THE DEVICE FOR APPLYING SAID PROCESS

A process by which the raw material, a gas comprising mainly hydrogen, carbon monoxide and carbon dioxide, is introduced into a first reactor together with a catalyst, in which one or more reactions take place that produce methanol or dimethyl ether or both, which are then introduced into a second reactor adding oxygen and a catalyst and producing formaldehyde and a minority of dimethyl ether, and where there may be an excess of water, such water being extracted from the process and the remaining products being introduced into the third reactor with, optionally, an additive, and such raw material is exposed to catalysts and under an atmosphere at medium temperature and pressure, in order to produce three or four groups of chemical reactions that, after extracting most of the water that is generated as a residue during the process, produces as a result a liquid multifunctional product that can be used as a solvent, a foaming agent or an oxygenated fuel; said product, normally a fluid, comprises polyoxymethylene dimethyl ethers with molecular formula CH3O(CH2O)nCH3 wherein n has a value between 1 and 7. 1. PROCESS FOR PRODUCING A MULTIFUNCTIONAL PRODUCT , characterized in that it comprises.a prior phase of preparation of the raw material at a temperature between 200° and 300° C. and at a pressure between 18 and 60 bar, preferably between 30 and 50 bar and more preferably between 37 and 43 bar, the raw material being a gas comprising hydrogen, carbon monoxide and carbon dioxide.1. A first phase , comprising the reactions caused by at least one of these two catalysts:a. A catalyst C1, preferably based on CuO/ZnO/Al2O3, thus giving rise to the first group of reactions comprising the reaction CO+2H2→CH3OH producing methanol.a. A catalyst C2, preferably based on aluminum oxide and CuO/ZnO/Al2O3, thus giving rise to the second group of reactions comprising the reaction 3CO+3H2→CH3OCH3+CO2, producing dimethyl ether.2. A second phase in which at least one of the products ...

A METHOD OF OPERATING A SLURRY BUBBLE COLUMN REACTOR

A method for starting a slurry bubble column reactor that includes a reactor vessel holding a settled or slumped bed of particles and a liquid phase from which the particles have settled includes introducing a flow of a re-suspension liquid into the settled or slumped bed to loosen the settled or slumped bed. The introduction of the re-suspension liquid takes place before the introduction of any gas into the settled or slumped bed, or together with feeding of gas into the settled or slumped bed, provided that, if gas is fed together with the re-suspension liquid into the settled or slumped bed before the settled or slumped bed has been loosened, the gas has a superficial gas velocity in the reactor below 10 cm/s. Once the settled or slumped bed has been loosened by at least the re-suspension liquid, gas is passed at a superficial gas velocity above 10 cm/s through the liquid phase. 115-. (canceled)16. A method for starting a slurry bubble column reactor that includes a reactor vessel holding a settled or slumped bed of particles and a liquid phase from which the particles have settled , the method including:introducing a flow of a re-suspension liquid into the settled or slumped bed to loosen the settled or slumped bed, the introduction of the re-suspension liquid taking place before the introduction of any gas into the settled or slumped bed, or together with feeding of gas into the settled or slumped bed, provided that, if gas is fed together with the re-suspension liquid into the settled or slumped bed before the settled or slumped bed has been loosened, the gas has a superficial gas velocity in the reactor below 10 cm/s; andonce the settled or slumped bed has been loosened by at least the re-suspension liquid, passing gas at a superficial gas velocity above 10 cm/s through the liquid phase.17. The method according to claim 16 , wherein the slurry bubble column reactor is used for Fischer-Tropsch synthesis and wherein the particles include solid Fischer-Tropsch ...

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

A method is provided of shutting down an operating three-phase slurry bubble column reactor () having downwardly directed gas distribution nozzles () submerged in a slurry body () of solid particulate material suspended in a suspension liquid contained inside a reactor vessel (), with the gas distribution nozzles () being in flow communication with a gas feed line () through which gas is being fed to the gas distribution nozzles () by means of which the gas is injected downwardly into the slurry body (). The method includes abruptly stopping flow of gas from the gas feed line () to the gas distribution nozzles () to trap gas in the gas distribution nozzles () thereby to inhibit slurry ingress upwardly into the gas distribution nozzles (). 1. A method of shutting down an operating three-phase slurry bubble column reactor having downwardly directed gas distribution nozzles submerged in a slurry body of solid particulate material suspended in a suspension liquid contained inside a reactor vessel , with the gas distribution nozzles being in flow communication with a gas feed line through which gas is being fed to the gas distribution nozzles by means of which the gas is injected downwardly into the slurry body , the method includingabruptly stopping flow of gas from the gas feed line to the gas distribution nozzles to trap gas in the gas distribution nozzles thereby to inhibit slurry ingress upwardly into the gas distribution nozzles.2. The method as claimed in claim 1 , wherein abruptly stopping flow of gas from the gas feed line to the gas distribution nozzles involves activating a fast response valve in the gas feed line to close off the gas feed line from the gas distribution nozzles.3. The method as claimed in claim 2 , wherein the fast response valve has a response time of between 1 and 10 seconds.4. The method as claimed in any of to claim 2 , wherein the gas distribution nozzles have outlets that are at the same elevation.5. The method as claimed in any of to ...

FLUIDIZED BED REACTION SYSTEM AND METHOD OF PRODUCING TITANIUM TETRACHLORIDE

This disclosure relates to a fluidized bed reaction system and method for continuous production of titanium tetrachloride from titanium-bearing materials containing high concentrations of alkaline earth metal impurities. Agglomerated heavy particles in a reaction are taken out continuously from a chlorination reactor without clogging and stopping. The reactors and related methods disclosed apply to the chlorination of titanium slag containing high content of alkaline earth metal oxides of up to 15% by weight. 1. A fluidized bed reaction system comprising:a reactor base comprising a center and a rim, wherein the center is recessed relative to the rim;at least one reactor wall defining, together with the reactor base, an enclosed space comprising a collection zone and a reaction zone, wherein the collection zone comprises a space within the recessed center of the reactor base, wherein the reaction zone comprises a space above the center and the rim of the reactor base such that the reaction zone is above the collection zone;a plurality of center nozzles formed through the recessed center of the reactor base and configured to supply fluidizing gas to the reaction zone via the collection zone;a plurality of rim nozzles formed through the rim of the reactor base and configured to supply fluidizing gas directly to the reaction zone;a gas flow control configured to control flow of the fluidizing gas to the plurality of center nozzles and to the plurality of rim nozzles such that a linear fluidizing velocity of the fluidizing gas supplied through the plurality of center nozzles is substantially lower than a linear fluidizing velocity of the fluidizing gas supplied through the plurality of rim nozzles.2. A method of producing titanium tetrachloride , the method comprising:{'sub': '2', 'introducing TiO-containing slag into a reaction zone of a reactor;'} {'br': None, 'sub': 2', '2', '4', '2, 'TiO+2Cl+C→TiCl+CO/CO,'}, 'supplying fluidizing gas comprising chlorine gas to the ...

EFFICIENT IN-SITU CATALYST SULFIDING METHODS AND SYSTEMS

A system and method is disclosed for efficiently sulfiding metal catalyst resident in a reactor vessel comprises a sulfiding module and a hydrogen sulfide detection module and a remote computer all arranged and configured to communicate wirelessly and to allow remote control and monitoring of the modules and sulfiding process. 1. A system for sulfiding a metal catalyst , comprising: a sulfur product inlet and outlet,', 'a sulfur product measurement device,', 'a sulfur product pressurization device having a variably controllable output,', 'a controller in electrical communication with at least the measurement device and pressurization device, and', 'a first communication device configured to transmit information between the module and an external site;, 'a mobile sulfur supply module comprising'} an inlet and outlet,', 'a hydrogen sulfide concentration detection device located between the inlet and outlet,', 'a hydrogen gas concentration detection device located between the inlet and the outlet,', 'and', 'a second communication device configured to transmit information between the hydrogen sulfide detection device and the external site and between the hydrogen gas detection device and the external site., 'a mobile detection module comprising'}2. The system of claim 1 , wherein the external site is a laptop computer.3. The system of claim 1 , wherein the external site is a website on the Internet.4. The system of claim 1 , wherein the pressurization device comprises a pump.5. The system of claim 4 , wherein the pump comprises an AC motor and a variable frequency drive.6. The system of claim 1 , wherein the pressurization device comprises a compressor.7. The system of claim 6 , wherein the compressor comprises an AC motor and a variable frequency drive.8. The system of claim 1 , wherein the sulfur product measurement device comprises a multi-parameter fluid measurement device.9. The system of claim 8 , wherein the fluid measurement device is configured to determine ...

APPARATUS AND PROCESS FOR CATALYZED REACTIONS CARRIED OUT IN A TUBULAR REACTOR

In a reactor tube in which a plurality of catalyst carriers are disposed, each catalyst carrier is an annular container having a perforated inner wall defining a tube, a perforated outer wall, a top surface closing the annular container and a bottom surface closing the annular container. A surface closes the bottom of the tube and a skirt extends upwardly from the perforated outer wall of the annular container from a position at or near the bottom surface of the container. A seal is located at or near the top surface and extends outward from the container beyond an outer edge of the skirt. The reactor tube additionally includes a temperature measuring device configured to measure the temperature in two or more catalyst carriers within the reactor tube. 1. A reactor tube comprising a plurality of catalyst carriers , each of said catalyst carriers comprising:an annular container for holding catalyst in use, said container having a perforated inner wall defining a tube, a perforated outer wall, a top surface closing the annular container and a bottom surface closing the annular container;a surface closing the bottom of said tube formed by the inner wall of the annular container;a skirt extending upwardly from the perforated outer wall of the annular container from a position at least one of at and near the bottom surface of said container, the skirt having a circumferential outer edge;a seal located at or near the top surface and extending outward from the container beyond the circumferential outer edge of the skirt, the skirt extending upward to a position below the seal;characterised in that the reactor tube additionally includes a temperature measuring device configured to measure the temperature in two or more of said catalyst carriers; said temperature measuring device being located at least one of between the catalyst carrier outer wall and the skirt, external of the skirt and in the interior space of the annular container.2. The reactor tube according to wherein ...

Radial-parallel catalytic reactor

The present invention comprises an axial radial catalytic reactor with a shell (as gas tight seal to maintain process gas flows within it) and a feed tube (passing from a source of process gas flow through the shell and into it do deliver feed gas to one or more levels of two annularly sequential catalyst beds), where one end of the feed tube is used as an inlet for feeding reaction mass. In one embodiment of the invention, an interior end of the feed tube is sealed.

SYSTEMS AND METHODS FOR PROCESSING FLUOROPOLYMER MATERIALS AND RELATED WORKPIECES

A method for removing perfluorinated compounds from a fluoropolymer material is provided. The method includes the steps of: (a) providing the fluoropolymer material in a chamber; (b) providing an anaerobic environment in the chamber; and (c) providing a fluorination gas in the chamber, thereby exposing the fluoropolymer material to the fluorination gas. The method results in the removal the perfluorinated compounds from the fluoropolymer material. 2. The method of claim 1 , further comprising the steps of(d) withdrawing the fluorination gas from the chamber; and(e) withdrawing the processed fluoropolymer from the chamber.3. The method of claim 1 , further comprising the step of heating the chamber to a temperature in a range of 25° C. to 325° C. claim 1 , and wherein the fluoropolymer material is exposed to the fluorination gas at a chamber pressure in a range of 5 PSIA to 55 PSIA.4. The method of claim 1 , wherein the fluoropolymer material is expose to the fluorination gas for a time period in a range of 1 hour to 1000 hours.5. The method of claim 1 , wherein the fluorination gas comprises 1 vol % to 100 vol % fluorine.6. The method of claim 1 , wherein the fluorination gas comprises 99 vol % to 0 vol % of an inert gas claim 1 , wherein the inert gas comprises nitrogen.7. The method of claim 5 , wherein an amount of the fluorine exposed to the fluoropolymer material ranges from 0.1 pounds of fluorine per 1000 pounds of fluoropolymer material to 20.0 pounds of fluorine per 1000 pounds of the fluoropolymer material.8. The method of claim 1 , wherein providing the fluorination gas of step (c) includes providing a continuous flow of the fluorination gas into and/or out of the chamber.9. The method of claim 1 , wherein the fluoropolymer material is provided in a bulk material form.10. The method of claim 1 , wherein the fluoropolymer material is provided as part of a workpiece.11. The method of claim 1 , wherein the fluoropolymer material is a virgin fluoropolymer ...

Apparatus And Process For The Production Of Formaldehyde

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

Continuous Preparation of Calcined Chemically-Treated Solid Oxides

The present invention discloses a continuous calcination vessel which can be used to prepare calcined chemically-treated solid oxides from solid oxides and chemically-treated solid oxides. A process for the continuous preparation of calcined chemically-treated solid oxides is also provided. Calcined chemically-treated solid oxides disclosed herein can be used in catalyst compositions for the polymerization of olefins. 120-. (canceled)21. A continuous calcination vessel comprising:(a) a fluidized bed vessel comprising at least one zone dividing wall for dividing the fluidized bed into a plurality of heating zones capable of independent temperature control and independent fluidizing gas control;(b) a particulate material inlet capable of introducing inlet particulate material into the fluidized bed vessel;(c) a fluidizing gas inlet capable of introducing a fluidizing gas into the fluidized bed vessel;(d) a fluidizing gas path capable of directing the fluidizing gas from the fluidizing gas inlet into the fluidized bed vessel to fluidize the inlet particulate material; and(e) an outlet capable of removing outlet particulate material from the fluidized bed vessel; wherein:each heating zone comprises at least one baffle;the fluidized bed vessel contains sufficient baffles to cause a substantially plug flow profile through the fluidized bed vessel; andthe fluidized bed vessel has a slope from horizontal of less than about 15 degrees.22. The continuous calcination vessel of claim 21 , wherein the inlet particulate material comprises a solid oxide claim 21 , a chemically-treated solid oxide claim 21 , or a combination thereof.23. The continuous calcination vessel of claim 21 , wherein the outlet particulate material comprises a calcined chemically-treated solid oxide.24. The continuous calcination vessel of claim 21 , wherein each baffle contains apertures located on alternating opposite edges of the baffles to cause a serpentine flow profile through the fluidized bed vessel ...