КОЛЛЕКТОРНЫЙ ТРУБОПРОВОД ДЛЯ ТРУБЧАТЫХ ПЕЧЕЙ РИФОРМИНГА

Изобретение относится к коллекторному трубопроводу для трубчатых печей риформинга и трубчатой печи риформинга, содержащей один или несколько коллекторных трубопроводов. Коллекторный трубопровод для отвода горячих технологических газов в трубчатых печах риформинга содержит изнутри наружу, по меньшей мере, оба слоя: изоляционный слой из огнеупорного бетона или огнеупорной кладки, стенку металлической внешней трубы, и дополнительно содержит несколько патрубков, через которые реакционные трубы трубчатой печи риформинга имеют возможность соединения с коллекторным трубопроводом, который в направлении периметра имеет разные термические сопротивления. Изобретение обеспечивает предотвращение повреждений в трубопроводе и улучшенный коллекторный трубопровод. 2 н. и 7 з.п. ф-лы, 1 ил.

СПОСОБ ПОЛУЧЕНИЯ СИНТЕЗ-ГАЗА ИЗ ЖИДКИХ И ГАЗООБРАЗНЫХ УГЛЕВОДОРОДОВ

Изобретения относятся к области химии. Синтез-газ получают распылением и/или испарением потока жидкого углеводородного сырья при температуре от 50 до 500°С и давлении от 0,2 до 5 МПа. Распыление осуществляют при помощи газообразного пропеллента, возможно при добавлении СО2, выбираемого из пара и/или газообразного углеводорода. Распыленный и/или парообразный поток жидких углеводородов смешивают с окислительным потоком, возможно, с паром, возможно, с потоком газообразных углеводородов при температуре от 50 до 500°С и давлении от 0,2 до 5 МПа. Реакционную смесь пропускают, по меньшей мере, через первый структурированный каталитический слой с образованием смеси продуктов реакции, включающих H2 и СО. Указанный структурированный каталитический слой включает катализатор каталитического частичного окисления, размещенный в одной или более прослойках. Смесь продуктов реакции охлаждают. Установка включает впускную секцию I, устройство для распыления/испарения жидких потоков в смесительную секцию II ...

СПОСОБ ВТОРИЧНОГО РИФОРМИНГА И ГОРЕЛКА, ПРЕДНАЗНАЧЕННАЯ ДЛЯ ЕГО ОСУЩЕСТВЛЕНИЯ

Настоящее изобретение относится к способу проведения реакций вторичного реформинга для получения смесей газов, содержащих водород и моноксид углерода, например синтез-газов, используемых для производства аммиака и метанола. Способ получения вторичного реформинга включает подачу кислородсодержащего газа и поток содержащего углеводороды газа в камеру сгорания, получая в итоге поток газа, содержащий моноксид, углерода и водород, и который затем пропускают через слой катализатора, в котором проходит реакция реформинга с водяным паром. Поток содержащего кислород газа подают в камеру сгорания в виде множества отдельных струй, которые относительно направления подачи в камеру сгорания потока, содержащего углеводороды, расположены не одна над другой, а параллельно друг другу и имеют равную скорость, распределяют в камере сгорания множество струй кислородсодержащего газа в газообразном потоке углеводородов, перемешивая в одинаковом по всей камере сгорания соотношении поток кислородсодержащего газа ...

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.

АППАРАТ ДЛЯ ПОЛУЧЕНИЯ СИНТЕЗ-ГАЗА

... 1. Аппарат (1) для получения синтез-газа, содержащий по существу цилиндрическую оболочку (2), закрытую с противоположных сторон днищами (3, 4), по меньшей мере одно впускное отверстие (8) для подачи газового потока, содержащего кислород, по меньшей мере одно впускное отверстие (7) для газового потока, содержащего углеводороды, по меньшей мере одно выпускное отверстие для потока синтез-газа, и по меньшей мере одну горелку (9), сообщающуюся с реакционной камерой (15) для частичного окисления и(или) риформинга углеводородов с получением потока синтез-газа, отличающийся тем, что он содержит трубу (12) из керамического материала, проходящую внутри оболочки (2), при этом внутреннее пространство этой трубы (12) из керамического материала образует реакционную камеру (15). ! 2. Аппарат (1) по п.1, отличающийся тем, что труба (12) из керамического материала по существу коаксиальна с оболочкой (2). ! 3. Аппарат (1) по п.1, отличающийся тем, что толщина трубы (12) из керамического материала составляет ...

РЕАКТОР РИФОРМИНГА С НИЗКИМ ПЕРЕПАДОМ ДАВЛЕНИЯ

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

ТЕПЛОЗАЩИТНОЕ ПОКРЫТИЕ И СВЕРХВЫСОКОТЕМПЕРАТУРНЫЙ ХОЛОДНОСТЕННЫЙ РЕАКТОР ГИДРОГЕНИЗАЦИИ СЛОЯ СУСПЕНЗИИ, СОДЕРЖАЩИЙ ЭТО ПОКРЫТИЕ

Изобретение относится к теплозащитному покрытию и высокотемпературному холодностенному реактору гидрогенизации, содержащему такое покрытие. Теплозащитное покрытие содержит последовательно расположенные адгезивный слой, второй керамический слой и первый керамический слой. Второй керамический слой состоит из диоксида циркония, стабилизированного оксидом алюминия, с содержанием оксида алюминия до 30 мас.%. Первый керамический слой состоит из диоксида циркония, стабилизированного оксидом иттрия, с содержанием оксида иттрия 6-9 мас.%. Оксид циркония в обоих керамических слоях имеет тетрагональную кристаллическую структуру. Реактор содержит корпус, включающий внешнюю оболочку, слой наплавки из нержавеющей стали и теплозащитное покрытие, в котором адгезивный слой теплозащитного покрытия плотно прилегает к слою наплавки из нержавеющей стали. Изобретение обеспечивает улучшение теплостойкости и способности покрытия к деформации, эффективное поглощение и уменьшение теплового напряжения, возникающего ...

РЕАКТОР ДЛЯ ПАРЦИАЛЬНОГО ОКИСЛЕНИЯ УГЛЕВОДОРОДНЫХ ГАЗОВ

FIELD: power industry. SUBSTANCE: reactor includes an external housing with a reactor reaction products removal device and at least with one device for supply of raw material or components of raw material to a catalyst sleeve arranged inside the reactor with a gap with the external housing, filled with a catalyst and including devices for removal of products from its lower part. The catalyst sleeve is provided with a jacket adjacent at least to some part of the cylindrical wall of the catalyst sleeve, which in the adjoining area of the jacket has through openings; the reactor is provided with a device for supply to the jacket of a cooling agent cooling down the catalyst sleeve and supplied to the catalyst sleeve through the openings in its cylindrical wall. EFFECT: reduction of wall temperature of a catalyst sleeve; reduction of metal corrosion of the catalyst sleeve. 6 cl, 2 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 554 008 C1 (51) МПК C01B 3/38 (2006.01) B01J 8/04 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ (21)(22) Заявка: ИЗОБРЕТЕНИЯ К ПАТЕНТУ 2014100683/04, 13.01.2014 (24) Дата начала отсчета срока действия патента: 13.01.2014 (72) Автор(ы): Долинский Сергей Эрикович (RU), Дергачев Александр Александрович (RU) (45) Опубликовано: 20.06.2015 Бюл. № 17 R U (73) Патентообладатель(и): Общество с ограниченной ответственностью "Газохим Техно" (RU) Приоритет(ы): (22) Дата подачи заявки: 13.01.2014 (56) Список документов, цитированных в отчете о поиске: WO2011088982 A1, 28.07.2011 . 2 5 5 4 0 0 8 R U (54) РЕАКТОР ДЛЯ ПАРЦИАЛЬНОГО ОКИСЛЕНИЯ УГЛЕВОДОРОДНЫХ ГАЗОВ (57) Реферат: Изобретение относится к реактору для стенки катализаторной гильзы, которая в области парциального окисления углеводородного сырья. примыкания рубашки выполнена со сквозными Реактор включает внешний корпус со средством отверстиями, реактор снабжен средством ввода вывода продуктов реакции из реактора и с хотя в рубашку хладоагента, охлаждающего бы одним средством ...

КОМПАКТНЫЙ РЕДУКТОР РЕФОРМИНГА

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

УСТРОЙСТВО ДЛЯ ЭНДОТЕРМИЧЕСКОЙ РЕАКЦИИ

Эндотермическая реакционная печь 102 содержит одну или более удлиненных труб 110, разделяющих ее внутреннюю часть на проточный канал для реакционной среды и проточный канал для горючей среды для проведения эндотермической реакции. Проточный канал для горючей среды расположен так, что топливо и горючий воздух нагреваются отдельно внутри печи 102 до температуры, значительно превышающей их температуру самовоспламенения, до соединения в зоне 116 сгорания, где они смешиваются, самовоспламеняются и сгорают.

Wärmetauscheranordnung zur Übertragung von Reformatenergie an Dampf und Luft

Es ist eine Wärmetauscherkonstruktion zur optimalen Übertragung von Wärmeenergie zwischen einen Primärreaktor verlassendem Reformat und in den Primärreaktor eintretenden Dampf und Luft vorgesehen. Insbesondere umfasst eine Ausführungsform der vorliegenden Erfindung einen hauptflächengetreuen Gegenstrom-Wärmetauscher, der um den Primärreaktor herum positioniert ist.

WIRBELBETTREAKTORSYSTEM UND METHODE ZU DESSEN HERSTELLUNG

Hochtemperatur-Wärmetauscher

VORRICHTUNG ZUR DURCHFUEHRUNG EINER KATALYTISCHEN REAKTION

DUENNSCHICHTREAKTOREN ZUR UMSETZUNG VON METHAN.

SEKUNDÄR REFORMIERUNGSVERFAHREN UND BRENNER

SEKUNDÄR REFORMIERUNGSVERFAHREN UND BRENNER

Reaktor zur Herstellung von Synthesegas

Die vorliegende Erfindung betrifft einen Reaktor zur Herstellung von Synthesegas, der gegebenenfalls fluiddicht mit einem Wärmetauscher verbunden ist, sowie ein Verfahren zur Herstellung von Synthesegas, bevorzugt unter Hochdruck.

EINRICHTUNG FUER DIE KATALYTISCHE WIRBELSCHICHTSPALTUNG EINES KOHLENWASSERSTOFFEINSATZES.

Oxidationsreaktor mit differentiellem Druckverlust sowie seine Verwendung.

Waermebehandlungsanlage

VORRICHTUNG ZUR BEHANDLUNG VON FLÜSSIGKEITEN

Verfahren und Vorrichtung zur Behandlung von Perfluorkohlenstoff

REAKTOR FUER DIE ERZEUGUNG VON REAKTIONSGASEN

Dampfreformer

Die Erfindung betrifft einen Dampfreformer (A) mit einem über einen Brenner (S) beheizbaren Feuerraum (D) und einem im Feuerraum (D) angeordneten Behälter (E), der eine Eintrittsöffnung (M) zur Zuführung eines kohlenwasserstoffhaltigen Einsatzes und einer Austrittsöffnung (P) zur Abführung von Synthesegas aufweist und der einen Reformierungskatalysator (J) umschließt. Kennzeichnend für den Dampfreformer (A) ist, dass der Behälter (E) eine lichte Querschnittsfläche des Feuerraums (D) weitgehend vollständig ausfüllt, wobei er sich normal zu dieser Querschnittsfläche weniger als halb soweit erstreckt wie in jede der beiden dazu senkrechten Raumrichtungen.

Katalysatoranlage mit Durchlaufstrahlenabschirmung und Verfahren zur Herstellung von Blausäure mit derselben

WASSERDAMPFREFORMIERUNG MIT INTERNER WASSERSTOFFREINIGUNG

CATALYTIC EXHAUST GAS TREATMENT APPARATUS

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

APPARATUS FOR REFINING CRUDE LIQUID SULFUR

Isothermal reactor for partial oxidation of methane

Refining liquid sulphur

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

AN APPARATUS FOR REFINING CRUDE LIQUID SULFUR.

CATALYTIC REACTOR.

PURPOSE:To improve heat exchange efficiency and to suppress the pressure drop of a reaction fluid side and/or combustion gas side as far as possible so as to reduce required driving power for press feeding by providing a heat recovering means which projects from the inside surface on the inside surface of an inner cylindrical pipe. CONSTITUTION:The other end of the outer cylindrical pipe 9 of the concentrical double cylindrical pipe-shaped reaction apparatus 1 having an inlet 5 and outlet 23 for reaction fluid on the same one end is closed and the other end side, except a part of one end side is projected into a heating chamber. The reaction fluid is passed from the inlet 5 through the annular space which is delineated and formed of the outer cylindrical pipe 9 and the inner cylindrical pipe 11 and is packed with a catalyst; thereafter, the fluid is turned over at the other end and is then passed through the inside space of the inner cylindrical pipe 11 so as to be introduced to the outlet ...

Methanol steam reforming catalysts, steam reformers, and fuel cell systems incorporating the same

Furnaces

Improvements in or relating to contact apparatus for gas reactions

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

Method for the reprocessing of uranium-containing nuclear fuels

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

High temperature reactor

... 961,859. High temperature reactors. UNIVERSAL OIL PRODUCTS CO. July 6, 1961 [July 11, 1960], No. 24428/61. Heading B1F. A reactor for treating a process fluid stream at high temperatures in presence of solid particles and thereafter quenching said stream comprises a closed vessel 1 having an upper fluid inlet 3 and a lower fluid outlet 5, an insulating lining 11, perforate members 12, 14 spaced apart and overlying said outlet and a quenching liquid distributer 17 positioned between said perforate members. An expansible metallic lining 6 may also be provided. The insulating lining 11 may be of refractory concrete. Perforate members 12 and 14 are formed of metal or alloy wire screen, perforated alloy or metal, or may be non-metallic if for reactors operating in the lower ranges of temperature. The vessel contains a high temperature resistant material 15, e.g. ceramic balls, supporting a sub-divided solid catalyst 16 selected as required by the process, e.g. hydrocracking, hydrogenation or ...

Multi-zone process and reactor for cracking heavy hydrocarbon feeds

In a multiple-zone fluidized bed conversion process and apparatus for producing light distillate liquid and fuel gas products from heavy hydrocarbon feedstocks, the feedstock is introduced into an upper fluidized bed cracking zone 14 maintained at a temperature of 482-760 DEG C (900-1400 DEG F) for cracking reactions, and resulting tars and coke are deposited on and within a particulate carrier material 17 therein. The carrier material descends through a stripping zone 18 to remove tars and then into a lower fluidized bed gasification zone 20, which is maintained at a temperature of 927-1093 DEG C (1700-2000 DEG F) by O2-containing gas and steam introduced therein at 22 to gasify the coke and produce a reducing gas. The stripping zone 18 contains coarse packing material 19 which is supported by a refractory annular- shaped grid 34. The decoked hot particulate carrier is recirculated by a transport gas supplied at 24, upwardly through a central refractory-lined conduit 28 to the upper bed ...

A new or improved furnace, more particularly for treating hydrocarbons

A furnace for treating hydrocarbons, e.g. for cracking or reforming, comprises a cylindrical cluster of tubes 8 arranged adjacent the wall 3 of a vessel 1 . . . 3, an axial burner 5 whose flame is directed parallel with the tubes 8, and burners 17 on the wall 3 which direct their flames to lick the wall 3. The burners 17 may be star burners, and the wall 3 preferably has ribs 18 to assist heat radiation towards the tubes 8, which may contain catalyst. The tubes 8 are connected by flexible hose 12, 15 to outlet and inlet ring manifolds 13, 16 respectively, and the tubes 8 have removable plugs 11. Additional burners may be provided on the hearth 1 and/or on the roof 2.

DESIGN FOR COMBINED TUBULAR PRIMARY & SECONDARY REFORMER

CATALYTIC STEAM REFORMING OF HYDROCARBONS

GENERATION OF SYNTHESIS GAS

Process and apparatus for executing catalytic conversions with regenerative contact masses

... 557,211. Catalytic apparatus and processes. SHELL DEVELOPMENT CO. March 24, 1942, No 3904. Convention date, March 3, 1941. [Class 1 (i)] In the simultaneous and alternate execution of catalytic endothermic and exothermic reactions in separate, contiguous reaction zones, the reactants in each zone are passed in indirect heat exchange through the other zone at a plurality of points along the length of the zones. The invention is particularly applicable to the conversion of hydrocarbons and the regeneration of the catalyst. In one form of apparatus each reactor comprises a series of superposed compartments 10-12, 13-15 respectively, each containing a catalyst bed 4 on a perforated support 5. Adjacent compartments of each series are connected by pipe coils 16-19 respectively each passing through two adjacent compartments of the opposite series. The coils may be embedded in the catalyst layers, or in the spaces above and below them as shown.

Fluidised-bed reactor

A shaft furnace for reacting two gases, e.g. metal halides and oxygen, in a fluidized bed of inert solid particles, is provided at its base with separate sets of passageways for the individual reactant gases which fluidize the bed, each passageway containing a constriction such that the pressure drop thereacross is equal to at least half that from bottom to top of the bed when fluidized. The constrictions are preferably in the form of removable discs having a central orifice. The passageways are so arranged in the base that the separate gases intermingle in the bed. The inert solid has a particle size of 40-1000m and the furnace has a diameter of at least 15 inches. Specific reference is made to the production of titanium dioxide from titanium tetrachloride and oxygen and aluminium trioxide from aluminium trichloride and oxygen according to the process described and claimed in Specification 919,019, Fig. 1 shows furnace 1 having a heat insulating base through which the fluidizing reactant ...

Electric reactors for catalytic gas reactions at high temperatures, and process for the endothermic production from methane and amonia, of both hydrocyanic acid and hydrogen

... A combined heating and catalytic body comprises a resistor 1 which may be metallic or non-metallic and may be made of rods or tubes or granules which is supplied by current through insulated and shielded nipples 8 and 81. The resistor is enclosed by a fireproof dielectric layer 2 preferably of porcelain, alumina or quartz, and this layer is coated with a thin catalytic layer, preferably of a metal, such as a platinum group metal or alloy. The complex body may possess at least one axis of symmetry so that the heat developed flows uniformly from the resistor to the catalytic layer. The complex body is arranged in a chamber 3 whose internal wall is coated with a catalytic layer similar to that on the fireproof layer. The reaction chamber is arranged in a metallic case 4 containing thermal insulator 5 with inlet 6 and outlet 7 for the reaction gases. The gap between chamber 3 and heater 2 comprises a reaction chamber. The reeactor may contain more than one heating body.

An electrical induction heating assembly

An electrical induction heating assembly

Apparatus of reaction for the treatment of fluids at high temperature.

DRIVE DEVICE WITH ENGINE AND TRANSMISSION PART FOR FROM PLAY COMPONENT SYSTEM ELEMENTS ZUSAMMENGE ONES SET TOY MODELS

PROCEDURE FOR ELKTROINDUKTIVEN THE HEATING UP OF FLUID BED LAYERS AND DEVICE FOR THE BY FUEHRUNG THE PROCEDURE

DEVICE FOR THE PRODUCTION OF SYNTHESIS GAS

COMPACT REFORMATION REACTOR

REACTOR TO METHANISIERUNG THE CARBON MONOXIDE EN UNREINIGUNGEN IN AN AMMONIA SYNTHESIS GAS

PROCEDURES AND DEVICE FOR THE PYROLYSIS OF FLUIDS EFFLUENTEN

REACTOR

PROCEDURE AND DEVICE FOR THE TRANSPORT OF CELEBRATIONS PARTICLES BETWEEN AREAS

DEVICE FOR THE CATALYTIC SHIFTING OF GASES.

PROCEDURE FOR THE TRANSFORMATION KARBOMETALLI OELE INTO LOW SIMMERING PRODUCTS.

HYDROGENATION PROCEDURE.

PROCEDURE AND DEVICE FOR THE ENTERPRISE OF A SYSTEM WITH CIRCULATING FLUIDISED BED

HEAT EXCHANGE MORE REFORMER WITH LOW PRESSURE LOSS

PROCEDURE FOR THE PRODUCTION OF SYNTHESIS GAS OF MEANS OF CATALYTIC PARTIAL OXIDATION

METHOD AND DEVICE FOR CIRCULATING SOLID IN A WIRBELSCHICHTREAKTOR

PROCEDURE AND DEVICE FOR THE ENTERPRISE OF A REACTOR SYSTEM WITH CIRCULATING FLUIDISED BED

FURNACE WITH A CIRCULAR FLUID FLOW HEATING ZONE

GAS DISTRIBUTOR FOR OXYGEN INJECTION INTO A WIRBELSCHICHTREAKTOR

Burner exhaust gas collection assembly for a catalytic reformer

FLUIDIZED BED WITH VERTICAL HEAT EXCHANGER COILS

APPARATUS AND METHOD FOR PRODUCING UNIFORM, FINE BORON-CONTAINING CERAMIC POWDERS

STEAM REFORMING HYDROCARBONS

METHOD FOR PRODUCING HYDROGEN AND APPARATUS FOR SUPPLYING HYDROGEN

CATALYTIC GAS REFORMER

Syngas reactor with ceramic membrane

Inhibiting of erosion of vessels

GASIFICATION OF SOLID FUEL

Inhibition of carbon deposition on fuel gas steam reformer walls

Endothermic reaction apparatus

APPARATUS AND METHOD FOR PRODUCING UNIFORM, FINE BORON-CONTAINING CERAMIC POWDERS

Fluidized bed reactor with gas distributor and baffle

Integrated reactor

CATALYTIC DEVICE WITH INTERNAL HEAT EXCHANGE

The invention relates to a catalytic device with internal heat exchange that among other things can be used for vehicles with an internal combustion engine or for stationary engines where there is a certain amount of unburned gas components in the exhaust that can be converted in the catalyst. By the invention it is obtained that the maximum temperature in the catalyst is always nearly constant whatever the inlet temperature. Hereby, the catalyst can be designed to work at a very specific temperature, by which it is possible, partly to ensure a better and safer burnout of the unburned components, and partly to save expenses for catalyst materials. The exhaust gas is guided through the catalyst (1) by at least three passage sections that have a mutual internal heat exchange. In the main reaction passage section (3) there are catalytic materials (4) of one or several kinds, in which the gas can react, and in which the gases heat exchange with the succeeding main heat transfer passage section ...

METHOD AND APPARATUS FOR UPGRADING BITUMINOUS MATERIAL

The present invention consists of an improved method and apparatus to upgrade bitumen in various forms which comprises four main components; namely, a fractionator equipped with a condenser, a heavy gas oil catalytic treater, a catalyst regenerator/gasifier and a gas cleanup assembly. In operation, the bitumen in liquid form is fed to the fractionator for initial separation of fractions with the bulk of the bitumen leaving the bottom of the fractionator in the form of a heavy gas oil which is pumped to the catalytic treater and sprayed on a hot catalyst to crack the heavy gas oil (an endothermic reaction) to release lighter hydrocarbons in the form of H2 rich volatile matter while depositing carbon on the catalyst. The volatile matter from the treater is directed to the fractionator where the condensable fractions are separated from the non-condensable H2 rich gas, a valuable primary gas. The carbon containing catalyst from the treater is recycled to the regenerator/ gasifier, and the catalyst ...

APPARATUS AND PROCESS FOR THE PRODUCTION OF HYDROGEN

Disclosed is a new process and apparatus for steam reforming of any vaporizable hydrocarbon to produce H2 and CO2, with minimal CO, and no CO in the H2 stream, using a membrane steam reforming (MSR) reactor and flame-less distributed combustion (FDC) which provides great improvements in heat exchange efficiency and load following capabilities to drive the steam reforming reaction. The invention also pertains to a zero emission hybrid power system wherein the produced hydrogen is used to power a high-pressure internally manifolded molten carbonate fuel cell. In addition, the design of the FDC-MSR powered fuel cell makes it possible to capture good concentrations of CO2 for sequestration or use in other processes.

MULTI-ZONE PROCESS AND REACTOR FOR CRACKING HEAVY HYDROCARBON FEEDS

A multiple-zone fluidized bed conversion process and apparatus for producing light distillate liquid and fuel gas products from heavy hydrocarbon feedstocks. The feedstock is introduced into an upper fluidized bed cracking zone maintained at a temperature of 900-1400.degree.F for cracking reactions, and resulting tars and coke are deposited on and within a particulate carrier material therein. The carrier material descends through a stripping zone to remove tars and then into a lower fluidized bed gasification zone, which is maintained at a temperature of 1700--2000.degree.F by 02-containing gas and steam introduced therein to gasify the coke and produce a reducing gas. The stripping zone contains coarse packing material which is supported by a refractory annular-shaped grid. The decoked hot particulate carrier is recirculated by a transport gas upwardly through a central refractory-lined conduit to the upper bed. Such recycle of the carrier solids is controlled by a refractory-lined gas-cooled ...

GASIFICATION OF SOLID FUEL

Solid fuel is acted on by a gasifying medium in a fluidised bed W. The resulting gas enters a cyclone 20 having an outlet for solid particles connected to a gasification chamber 30 in which the particles are gasified by a separate stream of gasifying medium supplied by an injector 25.

THERMAL REACTOR

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 ...

THIN BED REACTORS FOR METHANE CONVERSION

The invention relates to the conversion of methane to higher hydrocarbons by reaction of methane and gaseous oxidant under adiabatic conditions in a thin bed reactor, and to reactors for carrying out this reaction.

CONTINUOUS CATALYST UNLOADING DEVICE

A conveyance system in Fig. 1 for removing particulate catalyst from the fluidized bed of a regenerator vessel 5 with a downwardly directed discharge conduit 9 which leads from the lower portion of said vessel and is connected at its lower end to a vertical, refractory lined pipe 17, which is aligned with a fluidization means for conveying particulate catalyst through said refractory lined pipe. The discharge conduit is of a relatively large diameter in order to prevent catalyst plugging of the conveyance system. A gate valve located within this conduit is used to close the conveyance system during shutdown of said system. Control of catalyst flow is performed by the fluidization means aligned with the vertical refractory lined pipe, while the pressure level of the system is maintained by the reduced internal diameter of the pipe created by the refractory lining 19. The refractory lined pipe is connected at its downstream end to appropriate conduits which transport the catalyst to a spent ...

CATALYTIC REACTOR WITH IMPROVED BURNER

Catalytic Reactor With Improved Burner To more uniformly distribute heat to the plurality of catalyst tubes in a catalytic reaction furnace, the burner disposed in the furnace above the tops of the tubes includes concentric primary and secondary annular fuel and air outlets. The fuel-air mixture from the primary outlet is directed towards the tubes adjacent the furnace wall, and the burning secondary fuel-air mixture is directed horizontally from the secondary outlet and a portion thereof is deflected downwardly by a slotted baffle toward the tubes in the center of the furnace while the remaining portion passes through the slotted baffle to another baffle disposed radially outwardly therefrom which deflects it downwardly in the vicinity of the tube between those in the center and those near the wall of the furnace.

PLASMA INJECTED FLUIDISED BED METHOD AND HEATING INSTALLATION, ITS USES FOR NITROUS OXYDE SYNTHESIS, COAL GASIFICATION AND ORE REDUCTION

BREVET D 'INVENTION PROCEDE ET INSTALLATION DE CHAUFFAGE D'UN LIT FLUIDISE PAR INJECTION DE PLASMA, ET APPLICATIONS A LA SYNTHESE DES OXYDES D'AZOTE, A LA GAZEIFICATION D'UNE SUBSTANCE CARBONEE ET A LA REDUCTION DES MINERAIS Invention de : Jacques AMOUROUX Siméon CAVADIAS ELECTRICITE de FRANCE (Service National) Une substance à traiter est amenée dans une colonne de traitement (10) et maintenue en suspension (11) dans celle-ci par injection (A), en partie basse de la colonne, d'un gaz de fluidisation. Selon l'invention, on injecte (D) un plasma dans la colonne dans au moins une direction comprise dans un plan radial par rapport à la colonne. De préférence, le plasma est produit par induction haute fréquence et injecté à une pression voisine de la pression atmosphérique, de manière à ne pas perturber la fluidisation du lit et à permettre une bonne interpénétration des différentes veines gazeuses. Applications à la synthèse des oxydes d'azote, à la gazéification d'une substance carbonée et ...

DECLINED BED CONTACTOR

DECLINED BED CONTACTOR An apparatus for contacting solids with gases, preferably a needle coke preheater, which includes an elongated housing having an entrance and an exit and means for introducing solids into the entrance of the housing. A bed support divides the housing into an upper chamber and a lower chamber and is declined from the horizontal at an angle such that the solids introduced into the entrance of the housing slide down the bed support toward the exit of the housing. The bed support contains a plurality of openings distributed between two solid rectangular borders which serve as the two long parallel sides of the bed support. The openings are sufficiently large so that gases can flow from the lower chamber in contact with the solids and then into the upper chamber. The solid rectangular borders prevent preferential flow of the gases up the walls of the housing by forcing the gases to flow toward the center of the bed support. The apparatus also contains means for introducing ...

EROSION RESISTANT, CERAMIC FIBER LINING

Simply stated, the present invention contemplates the use of a ceramic fiber insulation material which is impregnated with an agent capable of stiffening the blanket and reducing erosion of the insulation material under conditions of use. The invention is especially applicable to the internal insulation of reactor vessels, where severe reaction conditions render the lining susceptible to cracking and separation from the reactor walls and also to erosion and corrosion by the reactants in the vessel.

APPARATUS AND METHOD FOR PRODUCING UNIFORM, FINE BORON-CONTAINING CERAMIC POWDERS

Uniform, fine ceramic powder is prepared using an apparatus comprising a cooled reactant transport member that includes an annular gas--flow space through which a sweep gas flows thereby inhibiting contact of reactants with internal reactor chamber surfaces; a reactor chamber (16); a heating means (40); and a cooling chamber (42). The reactor chamber defines a reaction zone heated by a heating means positioned to maintain an area of the reaction zone, positions adjacent to the reactant transport member at a desired temperature. The cooling chamber defines a cooling zone that communicates with the reactor chamber. The transport member temperature and the cooling chamber temperature are below that of the reactor chamber. The apparatus may be used to produce, via rapid carbothermal reduction, boron-containing ceramic powders by (1) feeding a mixture of boric oxide or a hydrate thereof and a carbon source into the reactor chamber described above through the cooled reactant transport member ...

THERMAL REACTOR

METHOD AND APPARATUS FOR DECOMPOSING CONCENTRATED AQUEOUS ALUMINUM NITRITE SOLUTIONS

PROCESS FOR CONVERSION OF DIMETHYL SULFIDE TO METHYL MERCAPTAN

Disclosed herein are systems and processes involving the catalyzed cleavage reaction of dimethyl sulfide to methyl mercaptan. The catalyzed cleavage reaction can be a standalone system or process, or can be integrated with a methyl mercaptan production plant.

PROCESS AND APPARATUS FOR PRODUCTION OF GRANULAR POLYCRYSTALLINE SILICON

The invention relates to a process for producing granular polycrystalline silicon in a fluidized bed reactor comprising a reactor tube and a heating apparatus outside the reactor tube, in which silicon seed particles are fluidized in the reactor tube by means of a gas flow in a fluidized bed which is heated up by means of the heating apparatus, and polycrystalline silicon is deposited by means of pyrolysis on the hot silicon seed particles by addition of a silicon-containing reaction gas to the fluidized bed, and the granular polycrystalline silicon thus formed is removed from the reactor tube, wherein the reactor tube has a fluidized bed region and an unheated region above the fluidized bed, and the reactor tube has a silicon coating on its inner wall, characterized in that the unheated region of the reactor tube above the fluidized bed has a wall temperature that has the effect that the silicon coating over the entire reactor tube has a maximum silicon layer thickness in a ratio of 7: ...

REFORMER TUBE HAVING A STRUCTURED CATALYST AND IMPROVED HEAT BALANCE

A reformer tube for producing synthesis gas by steam reforming of hydrocarbon- containing feed gases, in which a structured stream reforming catalyst is used, is proposed. According to the invention, a heat exchanger tube is arranged in the interior of the structured catalyst, with the feed gas stream flowing firstly through the structured catalyst and subsequently in countercurrent through the heat exchanger tube. This improves the heat exchange between the synthesis gas product stream and the structured catalyst and the feed gas stream flowing through it, especially in the radial direction.

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.

Hydrogen generation assemblies and hydrogen purification devices

Hydrogen generation assemblies, hydrogen purification devices, and their components, and methods of manufacturing those assemblies, devices, and components are disclosed. In some embodiments, the assemblies may include a vaporization region with packing material configured to transfer heat from a heated exhaust stream to a liquid-containing feed stream, and/or an insulation base adjacent a combustion region and configured to reduce external temperature of an enclosure. In some embodiments, the assemblies may include a cooling block configured to maintain an igniter assembly in thermal communication with a feed stream conduit, an igniter assembly including a catalytic coating, and/or a fuel stream distribution assembly. In some embodiments, the assemblies may include a heat conducting assembly configured to conduct heat from external heaters to an enclosure portion. In some embodiments, the devices may include frames with membrane support structures and/or may include a microscreen structure configured to prevent intermetallic diffusion.

STEAM REFORMERS, MODULES, AND METHODS OF USE

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

Reactor Components

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

EFFICIENT OXIDATIVE COUPLING OF METHANE PROCESSES AND SYSTEMS

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

Reactors and systems for oxidative coupling of methane

In an aspect, the present disclosure provides a method for the oxidative coupling of methane to generate hydrocarbon compounds containing at least two carbon atoms (C 2+ compounds). The method can include mixing a first gas stream comprising methane with a second gas stream comprising oxygen to form a third gas stream comprising methane and oxygen and performing an oxidative coupling of methane (OCM) reaction using the third gas stream to produce a product stream comprising one or more C 2+ compounds.

PROCESS AND APPARATUS FOR PRODUCTION OF GRANULAR POLYCRYSTALLINE SILICON

Prolonged operation campaigns in a fluidized bed reactor for producing granular polysilicon by deposition of silicon onto silicon seed particles from a silicon-containing precursor gas is made possible by employing a silicon-coated reaction tube which is not insulated above a region of the fluidized bed and as a result has a lower temperature such that the ratio of the thickness of the silicon on the reactor tube adjoining the fluidized bed to the coating thickness over the total reactor tube is from 7:1 to 1.5 to 1 after production campaign of from 15 to 500 days. 16.-. (canceled)7. In a process for producing granular polycrystalline silicon in a fluidized-bed reactor comprising a reactor tube and a heating device outside the reactor tube , in which silicon nucleus particles (seed) are fluidized in the reactor tube by means of a gas stream in a fluidized bed which is heated by means of the heating device and polycrystalline silicon is deposited by means of pyrolysis on the hot silicon nucleus particles by introduction of a silicon-containing reaction gas into the fluidized bed and the granular polycrystalline silicon formed in this way is removed from the reactor tube , where the reactor tube has a fluidized bed region and an unheated region above the fluidized bed , an intermediate space between an interior wall of the vessel and an outer wall of the reactor tube containing an insulation material and the reactor tube has a silicon coating on its interior wall , the improvement comprising:reducing the deposition of silicon on an interior of the unheated region of the reactor tube above the fluidized bed by establishing a wall temperature of the unheated region of the reactor tube which is lower than the wall temperature of the reactor tube in the region of the fluidized bed, where, owing to the lower wall temperature, the deposition of silicon above the fluidized bed is reduced, and setting a defined axial temperature gradient in the reactor tube in the region ...

PROCESS FOR PRODUCING PURE HYDROGEN WITH LOW STEAM EXPORT

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

Reactor for producing synthesis gas

The present invention relates to a reactor for production of synthesis gas that optionally has a fluid-tight connection to a heat exchanger, and to a process for producing synthesis gas, preferably under high pressure.

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 ...

Cold-Wall Reactor for Suspension-Bed Hydrogenation

The present invention provides a cold-wall reactor for suspension-bed hydrogenation, comprising a reactor body, which is provided with a reaction product outlet arranged at the top thereof, a cold hydrogen gas inlet arranged on a side wall thereof and a feed inlet arranged at bottom thereof, and the reactor body comprises, in a sequence from external to internal, a housing, a surfacing layer and a thermal insulation liner, and an inner liner cylinder, which is fixedly arranged inside the reactor body and is provided with an outlet on top thereof and an inlet on bottom thereof, wherein the outlet of the inner liner cylinder is connected with the reaction product outlet in a sealing manner, and the inlet of the inner liner cylinder is communicated with the feed inlet, wherein a side wall of the inner lining cylinder and an inner side wall of the reactor body define a cavity serving as a first circulation channel, wherein a second circulation channel is arranged on the side wall of the inner lining cylinder, and wherein an interior of the inner lining cylinder is communicated with the first circulation channel through the second circulation channel; by using the cold-wall reactor for suspension-bed hydrogenation, the material temperature is more uniform and reaction efficiency is improved, materials coking is reduced. In addition the falling and damaging of the thermal insulation liner is prevented, and the temperature of the outer wall of the reactor body is lower than the temperature of the medium. 1. A cold-wall reactor for suspension-bed hydrogenation , comprising{'b': 1', '2', '3', '4', '5', '18', '17, 'a reactor body (), which is provided with a reaction product outlet () arranged at the top thereof, a cold hydrogen gas inlet () arranged on a side wall thereof and a feed inlet () arranged at bottom thereof, and comprises, in a sequence from outside to inside thereof, a housing (), a surfacing layer () and a thermal insulation liner (), and'}{'b': 6', '1', '7', '8 ...

Chemical Reactor with Integrated Heat Exchanger, Heater, and High Conductance Catalyst Holder

A chemical reactor that combines a pressure vessel, heat exchanger, heater, and catalyst holder into a single device is disclosed. The chemical reactor described herein reduces the cost of the reactor and reduces its parasitic heat losses. The disclosed chemical reactor is suitable for use in ammonia (NH 3 ) synthesis.

CATALYTIC SYSTEM FOR CATALYTIC PARTIAL OXIDATION PROCESSES WITH A SHORT CONTACT TIME

The present invention relates to a catalytic system comprising at least two catalytic zones of which at least one zone exclusively contains one or more noble metals selected from the group consisting of Rhodium, Ruthenium, Iridium, Palladium and Platinum and at least another zone contains Nickel, said catalytic system characterized in that at least one zone exclusively containing noble metals selected from the group consisting of Rhodium, Ruthenium, Iridium, Palladium and Platinum is always distinct but in contact with at least one zone containing Nickel. 1. (canceled)2. A process of catalytic partial oxidation for the production of synthesis Gas and , with further steps , of hydrogen , using a catalytic system comprising at least two catalytic zones whose at least one zone contains exclusively one or more noble metals selected in the group consisting of Rhodium , Ruthenium , Iridium , Palladium and Platinum and at least the other zone contains Nickel , said catalytic system characterized in that at least one zone containing exclusively noble metals selected in the group consisting of Rhodium , Ruthenium , Iridium , Palladium and Platinum is always distinct but in contact with at least one zone containing Nickel; [{'sub': n', '2', 'n', '2, 'hydrocarbons and/or oxygenated compounds which are either liquid or gaseous at the inlet temperature and pressure of at least one reaction equipment, wherein the liquid hydrocarbons are selected from naphtha, gas oils, heavy gas oils such as Light Cycle Oils, deasphalted oils and mixtures thereof, wherein the oxygenated compounds are selected from ethanol, ethylene glycol, triglycerides of fatty acids, glycerine and carbohydrates with formula C(HO)Hand mixture thereof, wherein the gaseous hydrocarbons are selected from methane, Natural Gas, Refinery Fuel Gas, liquefied petroleum gas and mixture thereof;'}, 'air, enriched air with oxygen at any volumetric percentage ranging from 21% to 100%, or pure oxygen;', 'optionally steam and ...

BASKET-LIKE DEVICE HAVING WALL INSULATION

A device D accommodated in a reactor R and containing a gas- and/or liquid-permeable bottom B, in the peripheral region of which is arranged a lateral boundary W which completely surrounds the bottom B and forms a volume V which is partially or completely filled with catalytic and/or non-catalytic moldings, there optionally being located on the side facing the bottom B in the upstream direction at least one noble metal and/or non-noble metal fabric, wherein a thermal insulation layer S is located on at least part of the surface of the inner side of the lateral boundary W of the device D, the material for the thermal insulation layer S being selected from the group consisting of ceramic material, microporous material and silicate fibers. 115.-. (canceled)16. A device that can be accommodated in a reactor , the device comprising:a gas- and/or liquid-permeable bottom;a peripheral region arranged as a lateral boundary that completely surrounds the bottom and forms a volume, the volume which is partially or completely filled with catalytic and/or non-catalytic moldings;a thermal insulation layer positioned on at least part an inner side surface of the lateral boundary of the device, the thermal insulation layer being a microporous, silicatic material that includes highly dispersed silica and opacifiers, and which exhibits no decomposition in a temperature range from 700 to 1100° C., and has a thermal conductivity in a range from 0.04 to 0.09 W/m/K; andoptionally at least one noble metal and/or non-noble metal fabric located on a side facing the bottom in the upstream direction.17. The device of claim 16 , wherein the thermal insulation layer covers 30% to nearly 100% of the inner side surface of the lateral boundary.18. The device of claim 16 , wherein the thermal insulation layer covers at least the lower 30% of the inner side surface of the lateral boundary.19. The device of claim 16 , wherein the cross-section of the bottom is essentially round.20. The device of claim ...

HYDROGEN GENERATION ASSEMBLIES AND HYDROGEN PURIFICATION DEVICES

Hydrogen generation assemblies, hydrogen purification devices, and their components, and methods of manufacturing those assemblies, devices, and components are disclosed. In some embodiments, the devices may include an insulation base having insulating material and at least one passage that extends through the insulating material. In some embodiments, the at least one passage may be in fluid communication with a combustion region. 1. A steam reforming hydrogen generation assembly configured to receive at least one feed stream and generate a reformate stream containing hydrogen gas as a majority component and other gases , comprising:an enclosure;a hydrogen-producing region contained within the enclosure and including a reforming catalyst, the hydrogen-producing region being configured to produce, via a steam reforming reaction, the reformate stream from the at least one feed stream;a heating assembly configured to receive at least one air stream and at least one fuel stream and to combust the at least one fuel stream within a combustion region contained within the enclosure producing a heated exhaust stream for heating at least the hydrogen-producing region to at least a minimum hydrogen-producing temperature; andan insulation base configured to reduce external temperature of the enclosure, the insulation base being adjacent to the combustion region, wherein the enclosure is supported on the insulation base and the insulation base includes insulating material and at least one passage that extends through the insulating material, the at least one passage being in fluid communication with the combustion region.2. The assembly of claim 1 , wherein the insulation base further includes at least one cavity within the insulating material claim 1 , and wherein the at least one cavity is (a) sized to at least partially receive an air blower configured to produce at least a portion of the at least one air stream (b) in fluid communication with the at least one passage.3. The ...

REACTORS AND SYSTEMS FOR OXIDATIVE COUPLING OF METHANE

In an aspect, the present disclosure provides a method for the oxidative coupling of methane to generate hydrocarbon compounds containing at least two carbon atoms (C compounds). The method can include mixing a first gas stream comprising methane with a second gas stream comprising oxygen to form a third gas stream comprising methane and oxygen and performing an oxidative coupling of methane (OCM) reaction using the third gas stream to produce a product stream comprising one or more C compounds. 110.-. (canceled)11. A method for the oxidative coupling of methane to generate hydrocarbon compounds containing at least two carbon atoms (C compounds) , comprising:(a) mixing a first gas stream comprising methane with a second gas comprising oxygen to form a third gas stream comprising methane and oxygen, wherein said third gas stream has a composition that is selected such that at most 5% of said oxygen in said gas stream auto-ignites; and{'sub': '2+', '(b) performing an oxidative coupling of methane (OCM) reaction in an OCM reactor containing an OCM catalyst using said third gas stream to produce a product stream comprising one or more C compounds,'}wherein mixing the first gas stream comprising methane with the second gas stream comprising oxygen is performed upstream of the OCM reactor.12. The method of claim 11 , wherein the third gas stream has a composition that is selected such that at most 1% of said oxygen in said third gas stream auto-ignites.13. The method of claim 11 , wherein the third gas stream has a composition that is selected such that at most 0.1% of said oxygen in said third gas stream auto-ignites.14. The method of claim 11 , wherein the third gas stream has a composition that is selected such that substantially no oxygen in said third gas stream auto-ignites.15. The method of claim 11 , further comprising separating said product stream into at least a fourth stream and a fifth stream claim 11 , wherein said fourth stream has a lower C concentration ...

PROCESS FOR PRODUCING 2,3,3,3-TETRAFLUOROPROPENE, AND REACTOR FOR CARRYING OUT SAID PROCESS

A process for producing 2,3,3,3-tetrafluoropropene comprises the steps: i) in a first adiabatic reactor comprising a fixed bed composed of an inlet and an outlet, bringing 2-chloro-3,3,3-trifluoropropene into contact with hydrofluoric acid in the gas phase in the presence of a catalyst to produce a stream A comprising 2,3,3,3-tetrafluoropropene, HF and unreacted 2-chloro-3,3,3-trifluoropropene; and ii) in a second adiabatic reactor comprising a fixed bed composed of an inlet and an outlet, bringing hydrofluoric acid into contact in the gas phase, optionally in the presence of a catalyst, with at least one chlorinated compound to produce a stream B comprising 2-chloro-3,3,3-trifluoropropene. The stream A obtained in step i) feeds said second reactor. The inlet temperature of the fixed bed of one of said first or second reactors is between 300° C. and 400° C. The longitudinal temperature difference between the inlet and the outlet of the fixed bed in question is less than 20° C. 115-. (canceled)16. A process for producing 2 ,3 ,3 ,3-tetrafluoropropene , comprising the steps:i) in a first adiabatic reactor comprising a fixed bed composed of an inlet and an outlet, bringing 2-chloro-3,3,3-trifluoropropene into contact, in the gas phase in the presence of a catalyst, with hydrofluoric acid in order to produce a stream A comprising 2,3,3,3-tetrafluoropropene, HF and unreacted 2-chloro-3,3,3-trifluoropropene; andii) in a second adiabatic reactor comprising a fixed bed composed of an inlet and an outlet, bringing hydrofluoric acid into contact, in the gas phase in the presence or absence of a catalyst, with at least one chlorinated compound selected from the group consisting of 1,1,1,2,3-pentachloropropane, 2,3-dichloro-1,1,1-trifluoropropane, 2,3,3,3-tetrachloropropene and 1,1,2,3-tetrachloropropene, in order to produce a stream B comprising 2-chloro-3,3,3-trifluoropropene, the stream A obtained in step i) feeds said second reactor used for step ii), and', 'the temperature ...

STEAM METHANE REFORMER TUBE OUTLET ASSEMBLY

The present invention relates a steam methane reformer tube outlet assembly and a method of assembling or retrofitting same. More specifically, it relates to an exposed flanged tube outlet of a reformer designed to mitigate metal dusting corrosion, dew point condensation-related metal fatigue and cracking, and over-temperature induced metal failures such as hydrogen attack. 1. A flanged tube outlet assembly of a steam methane reformer assembly comprising:at least one or more reformer tubes having an inlet for allowing a process gas to be introduced into said tube outlet assembly for the removal of said process gas, wherein said process gas exiting an outlet port is syngas,said tube outlet assembly is disposed outside the confines of the reformer and includes a reformer tube having an interior space accommodating an internal insulation can therein wherein said insulation can is fitted in the interior space of the reformer tube, and the exterior of said reformer tube is covered with insulation extending in close proximity to the tube-flange weld neck;the outlet port disposed upstream of the distal end of said insulating can for delivering said syngas to downstream process units, andsaid insulation can is connected to a blind flange and extends into the reformer tube toward the outlet port, wherein the gap between the can and the interior of said reformer tube is larger at the distal end than at the blind flange end.2. The flanged tube outlet assembly of claim 1 , wherein the internal insulation can is selected from the group consisting of a fully tapered can claim 1 , a partially tapered can claim 1 , a fully stepped can or a partially stepped can.3. The flanged tube outlet assembly of claim 2 , wherein the internal can has an angled or curved distal end.4. The flanged tube outlet assembly of claim 1 , wherein the insulation can disposed in the interior of said reformer tube is designed to maintain areas of the tube outlet upstream of the distal end of the insulation ...

Steam methane reformer tube outlet assembly

The present invention relates a steam methane reformer tube outlet assembly and a method of assembling or retrofitting same. More specifically, it relates to an exposed flanged tube outlet of a reformer designed to mitigate metal dusting corrosion, dew point condensation-related metal fatigue and cracking, and over-temperature induced metal failures such as hydrogen attack.

DEVICE AND METHOD FOR CLEANING PRODUCER GAS USING A MICROWAVE INDUCED PLASMA CLEANING DEVICE

A device and method for cleaning producer gas includes a filter bed housing and a microwave chamber. The filter bed housing comprises an inlet for carbon-based material and a spent carbon outlet. The microwave chamber comprises a permeable top and wave guides around the perimeter through which microwaves can be introduced into the device using magnetrons. The method comprises using the device by filling the filter bed housing with carbon-based material, introducing microwaves into the microwave chamber using the magnetrons and wave guides, passing the gas through carbon-based material in the filter bed chamber, the microwave chamber, the gas permeable top and the gas outlet. 2. The device of claim 1 , wherein the conduit is in the shape of a sideways “T′.3. The device of claim 1 , wherein the conduit is a wave guide.4. The device of claim 1 , further comprising a wave guide connected to the conduit.5. The device of claim 1 , further comprising an unobstructed path for microwaves to enter the microwave chamber from the magnetron claim 1 , wherein the conduit is a sideways T-shaped conduit so that when the device is operated claim 1 , the first catalytic chamber is outside the path of microwaves being directed through the conduit.6. The device of claim 1 , further comprising at least one elbow shaped wave guide attached to the conduit that allows for the magnetron to be positioned horizontally with respect to a vertical orientation of the microwave chamber.7. The device of claim 1 , further comprising multiple wave guides connected to the conduit.8. The catalytic chamber of claim 1 , further comprising microwave absorbing material in the catalytic chamber.9. The device of claim 8 , wherein the microwave absorbing material of the catalytic chamber comprises ceramic tiles impregnated with a material that catalyzes conversion of microwave energy into heat energy.10. The catalytic chamber of claim 1 , further comprising ceramic tiles vertically aligned claim 1 , parallel ...

Efficient oxidative coupling of methane processes and systems

The present disclosure provides oxidative coupling of methane (OCM) systems for small scale and world scale production of olefins. An OCM system may comprise an OCM subsystem that generates a product stream comprising C 2+ compounds and non-C 2+ impurities from methane and an oxidizing agent. At least one separations subsystem downstream of, and fluidically coupled to, the OCM subsystem can be used to separate the non-C 2+ impurities from the C 2+ compounds. A methanation subsystem downstream and fluidically coupled to the OCM subsystem can be used to react H 2 with CO and/or CO 2 in the non-C 2+ impurities to generate methane, which can be recycled to the OCM subsystem. The OCM system can be integrated in a non-OCM system, such as a natural gas liquids system or an existing ethylene cracker.

STEAM REFORMERS, MODULES, AND METHODS OF USE

The present disclosure is directed to steam reformers for the production of a hydrogen rich reformate, comprising a shell having a first end, a second end, and a passage extending generally between the first end and the second end of the shell, and at least one heat source disposed about the second end of the shell. The shell comprises at least one conduit member comprising at least one thermally emissive and high radiant emissivity material, at least partially disposed within the shell cavity. The shell further comprises at least one reactor module at least a portion of which is disposed within the shell cavity and about the at least one conduit member and comprises at least one reforming catalyst. The disclosure is also directed to methods of producing a hydrogen reformate utilizing the steam reformers, comprising the steps of combusting a combustible mixture in a burner to produce a combustion exhaust that interacts with the steam reactor module(s) through surface to surface radiation and convection heat transfer, and reforming a hydrocarbon fuel mixed with steam in the steam reformers to produce a hydrogen-containing reformate. The present disclosure is further directed to reactor modules for use with the above steam reformers and methods of producing a hydrogen reformate. 1. A steam reformer for the production of a hydrogen reformate , comprising:a cylindrical shell defining a cavity having a bottom portion comprising an opening;a heat source configured to heat a fluid supplied to the cavity;a silicon carbide hollow conduit comprising openings at both ends, a first end of the conduit is disposed within the cavity and opens into the cavity and a second end of the conduit is attached to the bottom portion of the shell and opens to the shell exterior, wherein the heat source is in fluid communication with the second end, and the silicon carbide hollow conduit guides the heated fluid from the heat source to the cavity;a plurality of cylindrical reactor modules as ...

SYSTEMS AND METHODS FOR MAKING CERAMIC POWDERS

Systems and methods for making ceramic powders configured with consistent, tailored characteristics and/or properties are provided herein. In some embodiments a system for making ceramic powders, includes: a reactor body having a reaction chamber and configured with a heat source to provide a hot zone along the reaction chamber; a sweep gas inlet configured to direct a sweep gas into the reaction chamber and a sweep gas outlet configured to direct an exhaust gas from the reaction chamber; a plurality of containers, within the reactor body, configured to retain at least one preform, wherein each container is configured to permit the sweep gas to flow therethrough, wherein the preform is configured to permit the sweep gas to flow there through, such that the precursor mixture is reacted in the hot zone to form a ceramic powder product having uniform properties. 1. A method for carbothermically producing a ceramic powder , the method comprising: (i) wherein the at least one preform comprises a mixture, wherein the mixture comprises a carbon source and at least one of (a) a metal oxide and (b) boric acid; and', '(ii) wherein the at least one preform comprises at least one gas channel;, 'a) preheating at least one container in a staging zone, wherein the at least one container comprises at least one preform;'}b) moving the at least one container into a reactor body, wherein the reactor body comprises a reaction zone;c) carbothermically reacting the at least one preform in the reaction zone thereby producing a ceramic powder, wherein the carbothermically reacting comprises reducing, via the carbon of the at least one preform, at least one of the metal oxide and the boric acid of the at least one preform to form the ceramic powder, wherein the ceramic powder comprises ceramic particles, wherein the ceramic particles are selected from the group consisting of metal carbide particles, metal boride particles, metal nitride particles, and combinations therefor; andd) moving the ...

Centrifugal aluminum chloride generator

A metal chloride generator is provided. The metal chloride generator is a metal chloride centrifugal reactor that can be operated under conditions sufficient to cause metal particles and chlorine in the generator to be brought into contact with one another and react using centrifugal force to form metal chloride. A process for manufacturing titanium dioxide that utilizes the metal chloride generator is also provided.

REFORMER TUBE HAVING A STRUCTURED CATALYST AND IMPROVED HEAT BALANCE

A reformer tube for producing synthesis gas by steam reforming of hydrocarbon-containing feed gases, in which a structured stream reforming catalyst is used, is proposed. According to the invention, a heat exchanger tube is arranged in the interior of the structured catalyst, with the feed gas stream flowing firstly through the structured catalyst and subsequently in countercurrent through the heat exchanger tube. This improves the heat exchange between the synthesis gas product stream and the structured catalyst and the feed gas stream flowing through it, especially in the radial direction. 112-. (canceled)13. A reformer tube for converting a hydrocarbon-containing feed into a synthesis gas product containing carbon oxides and hydrogen under steam reforming conditions , the reformer tube comprising:(a) a reaction chamber comprising an outer, pressure-bearing casing tube, which is configured to receive heat from the outside, wherein the casing tube is demarcated at a first end from an adjacent outlet chamber by means of a separating plate and is closed at a second end by means of a closure device;(b) at least one structured packing disposed in the reaction chamber and containing a catalyst which is active for steam reforming;(c) an inlet for a feed gas stream comprising the hydrocarbon-containing feed arranged on the reaction chamber, where the inlet is disposed at an end of the reaction chamber closest to the separating plate and is in fluid communication with a gas inlet into the structured packing;(d) a heat exchanger tube disposed within the reaction chamber and within the structured packing and having a heat exchanger inlet end that is in fluid communication with a gas outlet from the structured packing, wherein the heat exchanger tube further comprises a heat exchanger outlet end that is in fluid communication with the outlet chamber, where the feed gas stream flows, after entry into the reaction chamber, firstly through the structured packing and subsequently ...

MOULDED INSULATION BODIES

Moulded insulation bodies, processes for the production thereof and use thereof consisting essentially of ceramic material comprising SiOfibers and AlOfibers which has been produced using AlOsol as a binder and kilned at a temperature of above 800° C. for insulation of the ends of cracking tubes of a tubular reactor for performing a steam reforming process for generating synthesis gas which project out of the reactor heating space. 17-. (canceled)8. A process for producing self-supporting moulded insulation bodies from a ceramic material comprising SiOfibres and AlOfibres , the process comprising the steps of:{'sub': 2', '2', '3', '2', '3, 'a) providing a flowable mixture comprising SiOfibres and AlOfibres and a binder comprised of an AlOsol;'}b) producing a preform by filling the flowable mixture into a hollow mould;c) kilning the preform at a temperature of at least 800° C.9. A moulded insulation body obtained by the process according to .10. The moulded insulation body according to claim 9 , wherein the moulded insulation body has a circular arc profile.11. The moulded insulation body according to claim 10 , wherein the moulded insulation body is in a shape selected from the group consisting of a half shell claim 10 , a quarter shell claim 10 , and cylindrical.12. Use of a moulded insulation body according to as insulation material in cracking tubes of a tubular reactor for performing a steam reforming process for generating synthesis gas.13. The use according to claim 12 , wherein an inlet for reactants and an outlet for products are arranged at opposite ends of the cracking tube which project out of a heating space of the tubular reactor claim 12 , wherein the inlet region and/or the outlet region of the cracking tube are fitted with internal moulded insulation bodies having a circular arc profile.14. The use according to claim 12 , wherein the inlet for the reactants and the outlet for the products are arranged at the same end of the cracking tube which ...

CORROSION-PROTECTED REFORMER TUBE WITH INTERNAL HEAT EXCHANGE

A reformer tube for producing synthesis gas by steam reforming of hydrocarbon-containing input gases is proposed where 110-. (canceled)11. A reformer tube for converting hydrocarbon-containing input materials , preferably natural gas , into a synthesis gas product comprising carbon oxides and hydrogen under steam reforming conditions , comprisinga. an outer, pressurized shell tube, wherein the shell tube is divided into a reaction chamber and an exit chamber by means of a separating tray, so that it is possible to set a different, preferably lower, pressure in the exit chamber than in the reaction chamber, and wherein the reaction chamber is externally heated,b. a dumped bed of a steam-reforming-active solid catalyst arranged in the reaction chamber,c. an entry for the input gas stream comprising the input material, arranged in the region of the reaction chamber, wherein the entry for the input gas stream is in fluid connection with the dumped catalyst bed,d. at least one helically coiled heat exchanger tube arranged inside the reaction chamber and inside the dumped catalyst bed, whose entry end is in fluid connection with the dumped catalyst bed and whose exit end is in fluid connection with the exit chamber, wherein the input gas stream after entry into the reaction chamber initially flows through the dumped catalyst bed and subsequently flows through the heat exchanger tube in countercurrent, and wherein the heat exchanger tube is in a heat exchange relationship with the dumped catalyst bed and the input gas stream flowing therethrough,e. a collection conduit for the synthesis gas product, which is in fluid connection with the exit chamber,wherein, in the region of the exit chamber:the exit end of the heat exchanger tube is fed through the separating tray and opens into an inner tube which is arranged in the interior of the shell tube and is in fluid connection with the collection conduit, so that the synthesis gas product is able to pass from the reaction ...

HYDROGEN GENERATION ASSEMBLIES AND HYDROGEN PURIFICATION DEVICES

Hydrogen generation assemblies, hydrogen purification devices, and their components, and methods of manufacturing those assemblies, devices, and components are disclosed. In some embodiments, the devices may include an insulation base having insulating material and at least one passage that extends through the insulating material. In some embodiments, the at least one passage may be in fluid communication with a combustion region.

System of product gas collection conduits for a steam reformer

A system of product gas collecting conduits for a steam reformer, containing a plurality of reaction tubes within a reformer housing, for the production of synthesis gas, comprising: a) a product gas collecting conduit arranged outside the reformer housing of the steam reformer, b) several port tubes arranged along the length of the conduit for connecting one reaction tube each to the product gas collecting conduit, c) at least one windshield for the protection of the product gas collecting conduit against wind and draft.

INDUCTION HEATER SYSTEM FOR A FLUIDIZED BED REACTOR

A system for the production of a polycrystalline silicon product is disclosed. The system includes a reaction chamber, a susceptor, an induction unit, and a plurality of energy sources. The reaction chamber has a reactor wall, and the susceptor encircles the reactor wall. The induction heater surrounds the susceptor, and has multiple induction coils for producing heat in the susceptor. The coils are grouped into a plurality of zones. The plurality of energy sources supply electric current to the coils. Each energy source is connected with the coils of at least one zone. 1. A system for producing a polycrystalline silicon product , the system comprising:a reaction chamber having a reactor wall;a susceptor encircling the reactor wall;an induction unit surrounding the susceptor, the induction unit having multiple induction coils for producing heat in the susceptor, the coils grouped into a plurality of zones; anda plurality of energy sources for supplying an electric current to the coils, each energy source connected with the coils of at least one zone.2. The system of claim 1 , further comprising insulation between the induction unit and the susceptor for preventing heat loss from the susceptor to ambient.3. The system of claim 1 , further comprising a high-pressure fluidized bed reactor.4. The system of claim 1 , wherein the reactor wall has a diameter of at least 20 inches.5. The system of claim 1 , wherein the coils of each zone being divided into multiple sub-zones claim 1 , at least one sub-zone from each zone connected with the same energy source.6. The system of claim 1 , further comprising an enclosure surrounding the induction unit for masking a stray magnetic field generated by the coils.7. The system of claim 1 , wherein the coils have passages therethrough for circulating deionized water to cool the coils.8. A method for producing a polycrystalline silicon product in a reactor having multiple induction coils grouped into multiple zones and a plurality of ...

HEAT INTEGRATED REFORMER WITH CATALYTIC COMBUSTION FOR HYDROGEN PRODUCTION

A heat integrated steam reformer, which incorporates a catalytic combustor, which can be used in a fuel processor for hydrogen production from a fuel source, is described. The reformer assembly comprises a reforming section and a combustion section, separated by a wall. Catalyst () able to induce the reforming reactions is placed in the reforming section, either in the form of pellets or in the form of coating on a suitable structured catalyst substrate such as fecralloy sheets. Catalyst () able to induce the combustion reactions is placed in the combustion section in the form of coating on suitable structured catalyst substrate such as fecralloy sheet. A steam and fuel mixture () is supplied to the reforming section () where it is reformed to produce hydrogen. A fuel and an oxygen () containing gas mixture is supplied to the combustion section where it is catalytically combusted to supply the heat for the reformer. The close placement of the combustion and reforming catalysts facilitate efficient heat transfer. Multiple such assemblies can be bundled to form reactors of any size. The reactor made of this closely packed combustion and reforming sections is very compact. 110-. (canceled)11. An integrated steam reformer/combustor assembly for use in a fuel processing system that supplies a steam and a reformer fuel mixture to a reformer to produce a reformate of primarily hydrogen , the assembly comprising:a multitude of tubular sections where an inside of each tubular section is a combustor and an internal wall of each tube is contacted with a structured catalyst support coated with a catalyst to induce combustion reactions in the combustor,a. at least two tube sheets supporting and spacing the multitude of tubular sections;b. a cylindrical wall enclosing the multitude of tubular sections which are connected to the tube sheets and having flow passages for feeding reforming reactants and removing reforming products and containing a reforming catalyst in close contact ...

Reactors and systems for oxidative coupling of methane

In an aspect, the present disclosure provides a method for the oxidative coupling of methane to generate hydrocarbon compounds containing at least two carbon atoms (C2+ compounds). The method can include mixing a first gas stream comprising methane with a second gas stream comprising oxygen to form a third gas stream comprising methane and oxygen and performing an oxidative coupling of methane (OCM) reaction using the third gas stream to produce a product stream comprising one or more C2+ compounds.

Efficient oxidative coupling of methane processes and systems

The present disclosure provides oxidative coupling of methane (OCM) systems for small scale and world scale production of olefins. An OCM system may comprise an OCM subsystem that generates a product stream comprising C 2+ compounds and non-C 2+ impurities from methane and an oxidizing agent. At least one separations subsystem downstream of, and fluidically coupled to, the OCM subsystem can be used to separate the non-C 2+ impurities from the C 2+ compounds. A methanation subsystem downstream and fluidically coupled to the OCM subsystem can be used to react H 2 with CO and/or CO 2 in the non-C 2+ impurities to generate methane, which can be recycled to the OCM subsystem. The OCM system can be integrated in a non-OCM system, such as a natural gas liquids system or an existing ethylene cracker.

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 (O2) 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.

流化床反应器的空气流量测量装置

一种流态化床反应器，在该反应器的壳体内装有空气分配板，用于支撑颗粒材料(包括燃料)床。空气分配板上有许多垂直布置的喷嘴穿过该板延伸，这些喷嘴用来接收来自空气通风装置中的空气，并使空气以足以使颗粒材料流态化，并可支持燃料燃烧或使其气化的流动速度排出到颗粒材料床内。第一压力检测装置置于至少一个喷嘴内，第二压力检测装置装在空气通风室内，因而就可测出颗粒材料床内的空气流量。

Tubular reactor for carrying out catalytic gas-phase reactions and method for operating said reactor

Catalytic reactor for endothermic reactions

Sistema continuo mejorado de descarga de catalizador

Catalytic reactor

Fluidizing a population of catalyst particles having a low catalyst fines content

The present invention relates to processes for fluidizing a population of catalyst particles that are depleted of catalyst fines. In one embodiment, the process includes providing a plurality of catalyst particles in the reactor, wherein the catalyst particles have a d2 value of greater than about 40 microns. The catalyst particles are contacted with a fluidizing medium under conditions effective to cause the catalyst particles to behave in a fluidized manner and form a fluidized bed. The particles are contacted with one or more primary obstructing members while in the fluidized bed. By fluidizing the catalyst particles in this manner, the catalyst particles can be maintained at an axial gas Peclet number of from about 10 to about 20.

Fluidizing a population of catalyst particles having a low catalyst fines content

The present invention relates to processes for fluidizing a population of catalyst particles that are depleted of catalyst fines. In one embodiment, the process includes providing a plurality of catalyst particles in the reactor, wherein the catalyst particles have a d 2 value of greater than about 40 microns. The catalyst- particles are contacted with a fluidizing medium under conditions effective to cause the catalyst particles to behave in a fluidized manner and form a fluidized bed. The particles are contacted with one or more primary obstructing members while in the fluidized bed. By fluidizing the catalyst particles in this manner, the catalyst particles can be maintained at an axial gas Peclet number of from about 10 to about 20.

Fluidizing a population of catalyst particles having a low catalyst fines content

A process and apparatus for fluidizing a population of catalyst particles having a low catalyst fines content includes a fluidized bed reactor which includes a plurality of catalyst particles in the reactor wherein the catalyst particles having a d 2 value of greater than about 40 microns. The catalyst particles are contacted with a fluidizing medium under conditions to fluidize the particles, the reactor includes a continuous reaction zone and separation zone and the fluidized of the catalyst particles are situated within the reaction and both the reaction zone and the separation zone include obstructing members which obstruct the flow of particles such that the catalyst particles can be maintained at an axial gas Peclet number from about 10 to about 20.

Fluidizing a population of catalyst particles having a low catalyst fines content

The present invention relates to processes for fluidizing a population of catalyst particles that are depleted of catalyst fines. In one embodiment, the process includes providing a plurality of catalyst particles in the reactor, wherein the catalyst particles have a dvalue of greater than about 40 microns. The catalyst particles are contacted with a fluidizing medium under conditions effective to cause the catalyst particles to behave in a fluidized manner and form a fluidized bed. The particles are contacted with one or more primary obstructing members while in the fluidized bed. By fluidizing the catalyst particles in this manner, the catalyst particles can be maintained at an axial gas Peclet number of from about 10 to about 20.

Fluidizing A Population of Catalyst Particles Having A Low Catalyst Fines Content

The present invention relates to processes for fluidizing a population of catalyst particles that are depleted of catalyst fines. In one embodiment, the process includes providing a plurality of catalyst particles in the reactor, wherein the catalyst particles have a d 2 value of greater than about 40 microns. The catalyst particles are contacted with a fluidizing medium under conditions effective to cause the catalyst particles to behave in a fluidized manner and form a fluidized bed. The particles are contacted with one or more primary obstructing members while in the fluidized bed. By fluidizing the catalyst particles in this manner, the catalyst particles can be maintained at an axial gas Peclet number of from about 10 to about 20.

Fluidizing a population of catalyst particles having a low catalyst fines content

The present invention relates to processes for fluidizing a population of catalyst particles that are depleted of catalyst fines. In one embodiment, the process includes providing a plurality of catalyst particles in the reactor, wherein the catalyst particles have a d 2 value of greater than about 40 microns. The catalyst- particles are contacted with a fluidizing medium under conditions effective to cause the catalyst particles to behave in a fluidized manner and form a fluidized bed. The particles are contacted with one or more primary obstructing members while in the fluidized bed. By fluidizing the catalyst particles in this manner, the catalyst particles can be maintained at an axial gas Peclet number of from about 10 to about 20.

Reactors and systems for oxidative coupling of methane

메탄의 산화적 커플링를 위한 시스템 및 방법

본 개시는 메탄의 산화적 커플링(OCM) 공정을 통해 올레핀을 제조하는 시스템 및 방법을 제공한다. 상기 시스템 및 방법은 열 전달 매질과 열적으로 연통하는 적어도 하나의 비-단열 구획 및 적어도 하나의 실질적 단열 구획을 포함하는 단계식 공정의 이용을 포함할 수 있다. 상기 시스템 및 방법은 OCM 반응기에서 메탄 전환을 개선할 수 있고 포스트-층 분해 유닛에서 에틸렌/에탄 비를 개선할 수 있는 희석제 스트림의 사용도 포함할 수 있다. 상기 방법 및 시스템은 산소(O 2 ) 및 파라핀을, 라디칼 전달제를 함유하는 가스 스트림에 주입하여 반응 혼합물을 제공하는 단계를 추가로 포함할 수 있다. 상기 반응 혼합물은 자가점화 지연 시간(AIDT)보다 더 긴 시간 동안 용기에 보유될 수 있으므로, 상기 반응 혼합물은 점화하여 열을 방출할 수 있고 올레핀을 포함하는 생성물 혼합물로 전환될 수 있다.

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 2 ) 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.

Reactors and systems for oxidative coupling of methane

In an aspect, the present disclosure provides a method for the oxidative coupling of methane to generate hydrocarbon compounds containing at least two carbon atoms (C2+ compounds). The method can include mixing a first gas stream comprising methane with a second gas stream comprising oxygen to form a third gas stream comprising methane and oxygen and performing an oxidative coupling of methane (OCM) reaction using the third gas stream to produce a product stream comprising one or more C2+ compounds.

Reactors and systems for oxidative coupling of methane

In an aspect, the present disclosure provides a method for the oxidative coupling of methane to generate hydrocarbon compounds containing at least two carbon atoms (C 2+ compounds). The method can include mixing a first gas stream comprising methane with a second gas stream comprising oxygen to form a third gas stream comprising methane and oxygen and performing an oxidative coupling of methane (OCM) reaction using the third gas stream to produce a product stream comprising one or more C 2+ compounds.

Efficient oxidative coupling of methane processes and systems

The present disclosure provides oxidative coupling of methane (OCM) systems for small scale and world scale production of olefins. An OCM system may comprise an OCM subsystem that generates a product stream comprising C 2+ compounds and non-C 2+ impurities from methane and an oxidizing agent. At least one separations subsystem downstream of, and fluidically coupled to, the OCM subsystem can be used to separate the non-C 2+ impurities from the C 2+ compounds. A methanation subsystem downstream and fluidically coupled to the OCM subsystem can be used to react H 2 with CO and/or CO 2 in the non-C 2+ impurities to generate methane, which can be recycled to the OCM subsystem. The OCM system can be integrated in a non-OCM system, such as a natural gas liquids system or an existing ethylene cracker.

Efficient oxidative coupling of methane processes and systems

The present disclosure provides oxidative coupling of methane (OCM) systems for small scale and world scale production of olefins. An OCM system may comprise an OCM subsystem that generates a product stream comprising C 2+ compounds and non-C 2+ impurities from methane and an oxidizing agent. At least one separations subsystem downstream of, and fluidically coupled to, the OCM subsystem can be used to separate the non-C 2+ impurities from the C 2+ compounds. A methanation subsystem downstream and fluidically coupled to the OCM subsystem can be used to react H 2 with CO and/or CO 2 in the non-C 2+ impurities to generate methane, which can be recycled to the OCM subsystem. The OCM system can be integrated in a non-OCM system, such as a natural gas liquids system or an existing ethylene cracker.

Efficient oxidative coupling of methane processes and systems

The present disclosure provides oxidative coupling of methane (OCM) systems for small scale and world scale production of olefins. An OCM system may comprise an OCM subsystem that generates a product stream comprising C 2+ compounds and non-C 2+ impurities from methane and an oxidizing agent. At least one separations subsystem downstream of, and fluidically coupled to, the OCM subsystem can be used to separate the non-C 2+ impurities from the C 2+ compounds. A methanation subsystem downstream and fluidically coupled to the OCM subsystem can be used to react H 2 with CO and/or CO 2 in the non-C 2+ impurities to generate methane, which can be recycled to the OCM subsystem. The OCM system can be integrated in a non-OCM system, such as a natural gas liquids system or an existing ethylene cracker.

System for the continuous conveyance of catalyst from a fluidized bed in a regenerator

A conveyance system for removing particulate catalyst from a fluidized bed in a regenerator vessel (5) comprises a downwardly directed discharge conduit (9) extending below the top level (7) of catalyst in the vessel (5) and connected at its lower end to a vertical, refractory lined pipe (17), which is aligned with a fluidization means (14, Fig. 2) for conveying particulate catalyst upwardly into the bottom end of the refractory lined pipe (17) and through to the top end thereof. The discharge conduit (9) is of a relatively large diameter in order to prevent catalyst plugging of the conveyance system. A gate valve (11) located within the discharge conduit (9) is used to close the conveyance system during shutdown of said system. Control of catalyst flow is performed by the fluidization means (14) aligned with the vertical refractory lined pipe (17), while the pressure level of the system is maintained by the reduced internal diameter of the lined pipe (17) created by the refractory lining 19. The refractory lined pipe (17) is connected at its upper end (21) to appropriate conduits (23, 25), which transport the catalyst to a catalyst hopper (27) for recirculation to the hydrocarbon reactor.

Catalyst reactor

APPARATUS FOR CATALYTIC CRACKING IN A FLUIDIZED BED OF A HYDROCARBON LOAD

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

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

Установка дл проведени эндотермических реакций

УСТАНОВКА ДЛЯ ПРОВЕДЕНИЯ ЭНДОТЕРМИЧЕСКИХ РЕАКЦИЙ, содержаща  печь, камеру сгорани , вертикально установленные по концентрическим окружност м цилиндрические реакторы, снабженные перегородками дл  равномерного распределени  греющих газов, и устройства дл  подачи горючего газа и окислител , отличающа с   тем, что, с целью упрощени  конструкции и уменьшени  металлоемкости, под камерой сгорани  размещены реакторы , над которыми установлены уст ройства дл  подачи горючего и окислител , при этом реакторы, расположенные вблизи стенок камеры сгорани , I снабжены экранами. СО

Lämpöä kuluttavien reaktioiden katalyyttinen reaktori

Tube and shell reactor with oxygen selective ion transport ceramic reaction tubes

A reactor comprising: a hollow shell defining a hermetic enclosure; a plurality of tube sheets disposed within said hermetic enclosure, a first one of said plurality of tube sheets defining a first chamber; at least one reaction tube each having a first end and an opposing second end, said first end being fixedly attached and substantially hermetically sealed to one end of said plurality of tube sheets and opening into said first chamber, the second end being axially unrestrained; each of said reaction tubes is comprised of an oxygen selective ion transport membrane with an anode side wherein said oxygen selective ion transport membrane is formed from a mixed conductor metal oxide that is effective for the transport of elemental oxygen at elevated temperatures and at least a portion of said first and second heat transfer sections are formed of metal; each of said reaction tubes includes first and second heat transfer sections and a reaction section, said reaction section disposed between said first and second heat transfer sections; a reforming catalyst disposed about said anode side of said oxygen selective ion transport membrane; a first process gas inlet; a second process gas inlet; and, a plurality of outlets.

FLUID BED REACTOR

Fluidized bed process heater

A fluidized bed process heater with a reaction chamber of toroidal configuration is provided with radially-oriented bed coils in the reaction chamber in which steam is generated or other process fluids are heated. The inner wall of the toroidal reaction chamber is water-cooled and the bed coils in the reaction chamber are removable. The return bends of the coils are protected against erosion from particulate bed solids.

Fluid bed heat recovery apparatus

A fluid bed reactor including a first, upstream reaction zone having a fluidized bed of particles and a second, downstream heat recovery zone having a fluidized bed of particles. The reactor is designed adjacent the heat recovery zone to withdraw heat from the heat recovery zone at a temperature lower than the temperature in the reaction zone. In operation, the particles in the heat recovery zone cool and quench the effluent from the reaction zone so as to remove fines and volatile elutriates therefrom, rendering the effluent less corrosive and preventing back or side reactions.

Sparger for oxygen injection into a fluid bed reactor

A sparger includes a conduit for conducting an oxygen feed, a nozzle connected to the conduit for passage of the oxygen feed from the conduit to the outside of the sparger, the nozzle including an orifice and a shroud, and insulation surrounding the conduit and also the shroud substantially the full length of the shroud. A method is provided for producing acrylonitrile via propane ammoxidation, comprising introducing propane and ammonia feeds into a fluid bed of a fluid bed reactor, and introducing an oxygen feed into the fluid bed through at least one insulated and jacketed sparger nozzle for reacting with at least one of the propane feed and ammonia feed in the presence of a fluid bed catalyst.

Patent JPH0221860B2

Fluidized-Bed Reactor For The Thermal Treatment Of Fluidizable Substances In A Microwave-Heated Fluidized Bed

The present invention relates to a fluidized-bed reactor for the thermal treatment of fluidizable substances, comprising at least one means for feeding microwave radiation into the fluidized-bed reactor and a metallic reactor wall defining the reactor and having a thermal insulation coating. To increase the energy utilization of such reactors, it is proposed in accordance with the invention that the thermal insulation coating is provided on the inside of the reactor wall and has an outer layer as seen from the reactor wall, which comprises refractory brick and/or refractory concrete as well as an inner layer comprising light-weight refractory brick and/or insulating concrete.

Fast fluidized bed reactor

In a fast fluidized bed reactor having, in a lower region, downwardly and inwardly inclined walls, a change in the direction of the wall surface or a ledge or protrusion is provided to change the direction of the particles flowing downwardly adjacent the wall for directing the particles inwardly away from the wall and into the region acted on by the nozzles providing the fluidizing gas. The change of direction, abutment or projection is preferably provided along the refractory wall surface at an elevation 200-1100 mm above the grid plate. In this manner, clogging of the nozzles is prevented and more efficient and effective fluidization and combustion processes occur.

Precise regulation of pyrocarbon coating

Deposition of a pyrocarbon coating of precise thickness onto one or more substrates being levitated along with a bed of particles in a fluidized bed coating enclosure is accomplished by varying the amount of hydrocarbon supplied to the bed as a part of an upward levitating flow to compensate for changes which are detected in the size of the fluidized bed. Increases and decreases in the size of the bed are detected by monitoring either the differential pressure above and below the bed or the weight of the bed, and compensating changes are made to return the bed to its desired size by changing the flow rate of hydrocarbon. For example, when a growth in bed size is detected that is not attributable to an aberration in either particle supply or withdrawal, the amount of hydrocarbon being supplied to the bed is decreased so as to cause the size of the bed to gradually return to its desired value.

System and method for flameless thermal oxidation at optimized equivalence ratios

A diptube assembly for a flameless thermal oxidizer having a matrix bed of media is provided. The diptube assembly comprises a fuel conduit at least partially positioned within the matrix bed for delivering fuel. An oxidizing agent conduit is at least partially positioned within the matrix bed for delivering oxidizing agents, wherein the oxidizing agent conduit is separate from the fuel conduit. At least one mixing conduit is positioned within the matrix bed and configured to receive fuel from the fuel conduit and the oxidizing agent from the oxidizing agent conduit. The mixing conduit is positioned to deliver the combination of fuel and oxidizing agents into the matrix bed of media.

Fluidised bed reactor

FIELD: machine building. SUBSTANCE: reactor includes a head part, the first housing located below the above mentioned head part and connected to the above mentioned head part, inside which there is a reaction chamber, the second housing located below the above mentioned first housing and connected to the above mentioned first housing, inside which there is the second reaction chamber, a bottom located below the above mentioned second housing and connected to the above mentioned second housing, in which there mounted is a liquefying gas supply branch pipe, a reaction gas supply branch pipe, as well as a heater and electrodes; at that, the above liquefying gas supply branch pipe includes an end flange located perpendicular to length of the above liquefying gas supply branch pipe; the above bottom has a hole into which the above liquefying gas supply branch pipe is placed; reactor has the first shock absorber and the second shock absorber, which are located from above and from below the above flange and turning the above liquefying gas branch pipe. EFFECT: simpler erection, installation, operation and repair of a reactor. 19 cl, 6 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2 490 576 (13) C2 (51) МПК F27B 15/00 (2006.01) B01J 8/18 (2006.01) C01B 33/00 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (21)(22) Заявка: 2011139608/02, 29.09.2011 (24) Дата начала отсчета срока действия патента: 29.09.2011 (73) Патентообладатель(и): СИЛИКОН ВЭЛЬЮ ЛЛС. (KR) (43) Дата публикации заявки: 10.04.2013 Бюл. № 10 2 4 9 0 5 7 6 (45) Опубликовано: 20.08.2013 Бюл. № 23 Адрес для переписки: 129090, Москва, пр-кт Мира, 6, ППФ "ЮС", С.В. Ловцову C 2 C 2 (56) Список документов, цитированных в отчете о поиске: US 2008/0299291 A1, 04.12.2008. RU 2285046 С2, 10.10.2006. WO 2007012027 А2, 25.01.2007. US 20020102850 A1, 01.08.2002. RU 2397953 С2, 10.10.2006. RU 2397952 С2, 10.10.2006. R U 2 4 9 0 5 7 6 (54) РЕАКТОР КИПЯЩЕГО СЛОЯ (57) Реферат: ...

Wirbelschichtreaktor zum thermischen Behandeln von wirbelfähigen Substanzen in einem mikrowellenbeheizten Wirbelbett

Die vorliegende Erfindung betrifft einen Wirbelschichtreaktor zum thermischen Behandeln von wirbelfähigen Substanzen mit wenigstens einer Einrichtung zum Einspeisen von Mikrowellenstrahlung in den Wirbelschichtreaktor und einer den Reaktor begrenzenden sowie eine thermische Isolierbeschichtung aufweisenden metallischen Reaktorwand. Um die Energieausnutzung derartiger Reaktoren zu erhöhen, wird erfindungsgemäß vorgeschlagen, dass die thermische Isolierbeschichtung an der Innenseite der Reaktorwand vorgesehen ist und eine, von der Reaktorwand aus gesehen, äußere Schicht, umfassend Schamottestein und/oder Feuerbeton, sowie eine innere Schicht, umfassend Feuerleichtstein und/oder Isolierbeton, aufweist.

System and method for flameless thermal oxidation at optimized equivalance ratios

A diptube assembly for a flameless thermal oxidizer having a matrix bed of media is provided. The diptube assembly comprises a fuel conduit at least partially positioned within the matrix bed for delivering fuel. An oxidizing agent conduit is at least partially positioned within the matrix bed for delivering oxidizing agents, wherein the oxidizing agent conduit is separate from the fuel conduit. At least one mixing conduit is positioned within the matrix bed and configured to receive fuel from the fuel conduit and the oxidizing agent from the oxidizing agent conduit. The mixing conduit is positioned to deliver the combination of fuel and oxidizing agents into the matrix bed of media.

Fluidized bed gas distributor system for elevated temperature operation

A method and apparatus for the debonding and sand core removal of sand cores from cast parts, the heat treating of metal parts and the removal of organic contamination from metal parts, which is utilizing a fluid bed furnace having an improved fluidizing gas distributor which discharges fluidized gas in a downward direction away from the parts in the fluidized bed.

Perfectionnements aux procédés de traitement en fluidisation et dispositif de mise en oeuvre

Method for production of synthesis gas for production of ammonia and shaft reactor for its realization

Изобретение относитс  к получению синтез-газа дл  производства аммиака и устройствам , осуществл ющим эти процессы, С целью экономии энергосырьевых ресурсов и снижени  энергозатрат в способе получени  синтез газа дл  производства аммиака, включающем паровую конверсию природного газа в трубчатой печи и паровоздушную доконверсию метана в шахтном реакторе с байпасной подачей природного газа, природный газ, подаваемый по бай- пэсной линии в шахтный реактор, дел т на два потока, один из которых в соотношении 1:7 с исходным количеством газа, прошедшего сероочистку, подают в гомогенную зону реактора на сжигание, а другой в соотношении 1:2 с количеством сжигаемого газа направл ют на конверсию. Шахтный реактор дл  получени  синтез-газа, содержащий металлический корпус, изнутри футерованный жаропрочным бетоном, снабженный вод ной рубашкой, смесителем воздуха с топливным газом, радиальным вводом парогазовой смеси и осевым вводом воздуха, он снабжен каналами дл  ввода природного газа и пара, расположенными коаксмально осевому вводу воздуха, а патрубки дл  истечени  природного гаээ и пара выполнены конусообразными. По сравнению со способом прототипом в изобретении 1000 мЗ/ч природного газа образуетс  больше водорода наА 5% больше оксида углерода, а использование устройства дл  осуществлени  способа позвол ет на 15% обеспечить экономию пара. 2 с п. ф-лы, 1 табл., 1 ил. сл С X СЯ Ј е The invention relates to the production of synthesis gas for the production of ammonia and the devices carrying out these processes in order to save energy resources and reduce energy costs in the method for producing synthesis gas for ammonia production, including steam reforming of natural gas in a tube furnace and vapor-air re-conversion of methane in a shaft reactor With the bypass supply of natural gas, the natural gas supplied via the bypass line to the shaft reactor is divided into two streams, one of which in a 1: 7 ratio with the initial quantity g for passing desulfurization, is fed into the ...

生产粒状多晶硅的方法和设备

本发明涉及在流化床反应器中生产粒状多晶硅的方法，该流化床反应器包含反应器管以及在反应器管外部的加热装置，其中在反应器管中通过气流使硅核心颗粒(晶种)在借助加热装置加热的流化床中流化，并通过将含硅的反应气体引入流化床中通过热解而在热的硅核心颗粒上沉积多晶硅，并将以此方式形成的粒状多晶硅由反应器管排出，其中所述反应器管具有流化床区域及在流化床上方的未加热区域，反应器管在其内壁上具有硅涂层，其特征在于，反应器管在流化床上方的未加热区域的壁温使得在由15至500天的运行持续时间之后在总反应器管中硅涂层的最大硅层厚度与在流化床区域中的平均硅层厚度的比例为由7:1至1.5:1。

Corrosion resistant reformer tube with internal heat exchange

탄화수소-함유 투입 가스의 증기 개질에 의해 합성 가스를 제조하기 위한 개질기 튜브가 제안되며, - 외부 쉘 튜브는 분리 트레이에 의해 반응 챔버와 출구 챔버로 나누어지고, - 증기-개질-활성 고형 촉매의 덤핑된 베드는 반응 챔버 내에 배열되고, - 적어도 하나의 열 교환기 튜브는 반응 챔버 내측 및 덤핑된 촉매 베드 내측에 배열되고, 열 교환기 튜브의 입구 단부는 덤핑된 촉매 베드와 유체 연결되고, 열 교환기 튜브의 출구 단부는 출구 챔버와 유체 연결되고, - 열 교환기 튜브의 출구 단부는 분리 트레이를 관통하고, 쉘 튜브의 내부에 배치되고 합성 가스 생성물을 위한 수집 도관과 유체 연결되는 부식 방지 내부 튜브 내로 개방되며, - 가스 투과성 단열 층이 쉘 튜브의 내벽과 내부 튜브의 외벽 사이에 배열된다. A reformer tube for the production of synthesis gas by steam reforming of a hydrocarbon-containing input gas is proposed, the outer shell tube being divided into a reaction chamber and an outlet chamber by a separation tray, - dumping of the steam-reforming-active solid catalyst the exhausted bed is arranged within the reaction chamber, wherein at least one heat exchanger tube is arranged inside the reaction chamber and inside the dumped catalyst bed, the inlet end of the heat exchanger tube being in fluid communication with the dumped catalyst bed, the outlet end is in fluid communication with the outlet chamber, the outlet end of the heat exchanger tube passing through the separation tray and opening into the corrosion resistant inner tube disposed inside the shell tube and in fluid communication with a collection conduit for the synthesis gas product; - a gas permeable insulating layer is arranged between the inner wall of the shell tube and the outer wall of the inner tube;

蒸汽甲烷重整器管出口组件

本发明涉及一种蒸汽甲烷重整器管出口组件及其组装或改装方法。更具体地，本发明涉及重整器的暴露的凸缘管出口，其被设计成减轻金属尘化腐蚀、露点冷凝相关的金属疲劳和开裂、以及过温引起的金属失效诸如氢蚀。

Method and apparatus for the production of granular polycrystalline silicon

본 발명은 반응기 튜브 및 상기 반응기 튜브의 외부에 존재하는 가열 장치를 포함하는 유동층 반응기 내에서 과립형 다결정질 실리콘의 제조 방법에 관한 것이며, 여기서, 실리콘 시드(seed) 입자를 반응기 튜브 내에서, 가열 장치에 의해 가열되는 유동층 내의 기체 유동에 의해 유동화시키고, 실리콘-함유 반응 기체를 유동층 내에 첨가함으로써 다결정질 실리콘을 가열된 실리콘 시드 입자 상에서 열분해에 의해 증착시키고, 이러한 방식으로 형성된 과립형 다결정질 실리콘을 반응기 튜브로부터 제거하며, 이때, 반응기 튜브는 유동층 영역, 및 상기 유동층 상의 비가열되는 영역을 가지고, 반응기 튜브는 이의 내벽 상에 실리콘 코팅을 가지며, 유동층 상의 반응기 튜브의 상기 비가열되는 영역은, 15일 내지 500일의 작동 기간 후, 전체 반응기 튜브 내 최대 실리콘 층 두께 : 유동층 영역 내 평균 실리콘 층 두께의 비율을 7:1 내지 1.5:1로 갖는 실리콘 코팅을 초래하는 벽 온도를 갖는 것을 특징으로 한다. The present invention relates to a method for producing granular polycrystalline silicon in a fluidized bed reactor comprising a reactor tube and a heating device external to the reactor tube, wherein the silicon seed particles are heated in the reactor tube Fluidized by gas flow in a fluidized bed heated by the apparatus, polycrystalline silicon is deposited by thermal decomposition on heated silicon seed particles by adding a silicon-containing reaction gas into the fluidized bed, and the granular polycrystalline silicon formed in this way is deposited. Removed from the reactor tube, wherein the reactor tube has a fluidized bed area, and a non-heated area on the fluidized bed, the reactor tube has a silicone coating on its inner wall, and the non-heated area of the reactor tube on the fluidized bed is 15 After an operating period of 1 to 500 days, the maximum in the entire reactor tube Silicon layer thickness characterized by having a wall temperature resulting in a silicone coating with a 1: the ratio of the average thickness of the silicon layer fluidized bed region 7: 1 to 1.5.

Inhibiting of erosion of vessels

A method of inhibiting erosion of an interior surface of a process vessel by solid objects carried in a fluid passing over the interior surface includes providing at least one formation at or in close proximity to the interior surface to interfere with the flow of the fluid over the interior surface, and to interfere with the movement of the solid objects by the fluid. The invention extends to a process vessel (10) which includes a body (16) defining an interior vessel surface (20), a catalyst bed (12) in the body (16), retaining means (22) on the catalyst bed for retaining the catalyst bed in position, and at least one formation (26) at or in close proximity to the interior vessel surface above the retaining means for interfering with fluid flow above the retaining means.

Способ и устройство для получения синтез-газа

1. Способ получения синтез-газа путем каталитического превращения метана посредством пропускания реагентов через неподвижный слой катализатора, отличающийся тем, что в качестве неподвижного слоя катализатора используют кольцевой слой катализатора, в котором реагенты пропускают от внутренней к наружной поверхности кольцевого слоя катализатора, в качестве реагентов используют смесь метана с газообразными реагентами, дополнительно содержащую продукты плазмохимического распада газообразных реагентов или их смеси, тепловой режим процесса обеспечивают путем смешивания продуктов плазмохимического распада со смесью метана с газообразными реагентами, а, по крайней мере, часть реагентов подают непосредственно в плазмохимическую зону.2. Способ получения синтез-газа по п.1, отличающийся тем, что в качестве газообразных реагентов используют углекислый газ или водяной пар или кислород.3. Реактор для получения синтез-газа путем каталитического превращения метана, включающий неподвижный слой катализатора и устройство нагрева реагентов и катализатора, отличающийся тем, что слой катализатора выполнен в форме кольца, в котором движение реагентов осуществляется от внутренней к наружной поверхности кольцевого слоя катализатора, устройство нагрева реагентов и катализатора выполнено в виде плазматрона, потребляющего рабочий газ и расположенного в центральной части реактора в плазмохимической зоне, имеющей огнеупорную термоизоляцию, между плазмохимической зоной и слоем катализатора расположена буферная зона, в которой происходит перемешивание реагентов и продуктов плазмохимического распада рабочего газа пла� РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2013 138 470 A (51) МПК C01B 3/34 (2006.01) C01B 3/38 (2006.01) B01J 19/08 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21)(22) Заявка: 2013138470/05, 18.02.2011 (71) Заявитель(и): Вощинин Сергей Александрович (RU) Приоритет(ы): (22) Дата подачи заявки: 18.02.2011 (43) Дата публикации заявки: 27.02. ...

Catalytic reactor

Patent DE3532413C2

流動層合成装置のガス分散板

(57)【要約】本公報は電子出願前の出願データであるた め要約のデータは記録されません。

带有陶瓷膜的合成气体反应器

放热反应和吸热反应在一反应器中进行热结合，该反应器具有至少一个氧选择性离子迁移膜，该膜用含氧气体如空气中的氧提供放热反应。吸热反应的热需要量由放热反应来满足。根据所采用的反应器设计，放热反应和吸热反应可以气态地结合。

Tube furnace for catalytic splitting of hydrocarbons

FIELD: tube furnaces for catalytic splitting of hydrocarbons in production of synthesis gas. SUBSTANCE: heater tube furnace has many tunes in furnace chamber and containing catalyst. Produced in tubes is synthesis gas containing, first of all, hydrogen, carbon monoxide and dioxide. There is hazard of formation of carbide (metal dusty corrosion) on external sides of ends of tube throats. To prevent corrosion supplied to external section of ends of tube throats is gas or vapor protective medium which contains no carbon monoxide. EFFECT: improved design. 3 cl, 2 dwg Ос оОгс ПЧ ГЭ РОССИЙСКОЕ АГЕНТСТВО ПО ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ (19) ВИ "” 2102 310. 13) СЛ 50 М С 01 В 3/26 12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ РОССИЙСКОЙ ФЕДЕРАЦИИ (21), (22) Заявка: 94038428/25, 12.08.1994 (30) Приоритет: 13.08.1993 ОЕ Р 4327176.6 (46) Дата публикации: 20.01.1998 (56) Ссылки: ГЕ, заявка, 3329435, кл. С 01 В 3/26, 1984. (71) Заявитель: Металлгезельшафт АГ (0Е) (72) Изобретатель: Фридрих Хоманн[0Е], Вернер Релльы[ОЕ], Ханс Гюнтер Мертель[0ОЕ] (73) Патентообладатель: Металлгезельшафт АГ (0Е) С1 (54) ТРУБЧАТАЯ ПЕЧЬ ДЛЯ КАТАЛИТИЧЕСКОГО РАСЩЕПЛЕНИЯ УГЛЕВОДОРОДОВ (57) Реферат: Трубчатая печь предназначена для каталитического расщепления углеводородов в целях производства синтез-газа. Сущность изобретения: трубчатая калориферная печь имеет многочисленные трубы, расположенные в топочной камере и содержащие катализатор. В трубах производят синтез-газ, содержащий прежде всего водород, окись и двуокись углерода. На внешних сторонах концов горловин труб есть опасность карбидообразования (пыльная коррозия металла). Чтобы предотвратить коррозию, на внешний участок концов горловин труб подают газо- или парообразную защитную среду, не содержащую окись углерода. 3 з.п. Ф-лы, 2 ил. 3 2102310 КО Ос оОгс ПЧ ГЭ КУЗЗАМ АСЕМСУ ГОК РАТЕМТ$ АМО ТКАОЕМАКК$ (19) 12) АВЗТКАСТ ОЕ 1МУЕМТОМ ВИ "” 2102 310. (51) 1пЕ. С1.6 13) Сл С О1В 3/26 (21), (22) АррИсаНоп: 94038428/25, 12.08.1994 (30) Рпошу: 13.08.1993 ОЕ Р 4327176 ...

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

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

CATALYST AND PROCEDURE FOR THE OLIGOMERIZATION OF OLEFINE

Synthesis gas production apparatus

FIELD: process engineering. ^ SUBSTANCE: invention can be used to produce gas mixes containing hydrogen, carbon monoxide and, if required, nitrogen. Proposed apparatus has cylindrical case closed on opposite sides by bottoms. It comprises also one oxygen-containing gas flow feed hole at least one hydrocarbon-containing gas flow feed hole, and at least one synthesis gas flow discharge hole. At least, one burner communicates with reaction chamber for partial hydrocarbon oxidation and/or reforming to produce synthesis gas flow. Apparatus casing houses ceramic material tube. ^ EFFECT: ease of manufacture, higher efficiency. ^ 15 cl, 1 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2 407 585 (13) C2 (51) МПК B01J 8/00 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ, ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (21), (22) Заявка: 2008132805/21, 22.12.2006 (24) Дата начала отсчета срока действия патента: 22.12.2006 (72) Автор(ы): ЦАНИКЕЛЛИ Лука (IT), ФЕРРИНИ Кристина (CH) (43) Дата публикации заявки: 20.02.2010 2 4 0 7 5 8 5 (45) Опубликовано: 27.12.2010 Бюл. № 36 (56) Список документов, цитированных в отчете о поиске: US 5856585 A, 05.01.1999. RU 2065866 C1, 27.08.1996. RU 2114718 C1, 10.07.1998. DE 4140063 A1, 09.06.1993. EP 1419812 A1, 19.05.2004. RU 2180317 C1, 10.03.2002. EP 0124226 A2, 07.11.1984. 2 4 0 7 5 8 5 R U (86) Заявка PCT: EP 2006/012429 (22.12.2006) C 2 C 2 (85) Дата перевода заявки PCT на национальную фазу: 11.08.2008 (87) Публикация PCT: WO 2007/079954 (19.07.2007) Адрес для переписки: 101000, Москва, М.Златоустинский пер., 10, кв.15, "ЕВРОМАРКПАТ", пат.пов. И.А.Веселицкой, рег. № 11 (54) АППАРАТ ДЛЯ ПОЛУЧЕНИЯ СИНТЕЗ-ГАЗА (57) Реферат: Изобретение может быть использовано для получения газовых смесей, содержащих водород, моноксид углерода и, при необходимости, азот. Аппарат имеет цилиндрическую оболочку, закрытую с противоположных сторон днищами. А также по меньшей мере одно впускное отверстие для подачи газового потока, содержащего ...

SYSTEMS AND METHODS FOR OXIDATIVE COMBINATIONS OF METHANE

РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2020 102 298 A (51) МПК C07C 2/84 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21)(22) Заявка: 2020102298, 09.07.2018 (71) Заявитель(и): ЛЮММУС ТЕКНОЛОДЖИ ЛЛС (US) Приоритет(ы): (30) Конвенционный приоритет: (43) Дата публикации заявки: 10.08.2021 Бюл. № 22 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 07.02.2020 US 2018/041322 (09.07.2018) (87) Публикация заявки PCT: A WO 2019/010498 (10.01.2019) Адрес для переписки: 190900, BOX 1125, Санкт-Петербург, Нилова Мария Иннокентьевна R U (57) Формула изобретения 1. Способ получения олефина, включающий: а) обеспечение реактора, имеющего изотермическую секцию, причем указанная изотермическая секция содержит катализатор, способный стимулировать реакцию окислительного сочетания метана (ОСМ), и находится в тепловом контакте с теплопередающей средой; и б) введение газовой смеси в изотермическую секцию реактора, причем указанная газовая смесь содержит кислород (O2) и метан (CH4), в результате чего по меньшей мере примерно 75 мол. % O2 вступает в реакцию с CH4 с образованием выходящего потока, содержащего углеводородные соединения, имеющие два или более атомов углерода (соединения C2+), и не содержащие соединения C2+ примеси. 2. Способ по п. 1, в котором реакция ОСМ имеет селективность по соединениям C2+ по меньшей мере примерно 50% при 700°C. 3. Способ по п. 1, в котором реакция ОСМ имеет селективность по соединениям C2+ по меньшей мере примерно 60% при 750°C. 4. Способ по п. 1, в котором реакция ОСМ имеет селективность по соединениям C2+ по меньшей мере примерно 65% при 800°C. Стр.: 1 A 2 0 2 0 1 0 2 2 9 8 (54) СИСТЕМЫ И СПОСОБЫ ОКИСЛИТЕЛЬНОГО СОЧЕТАНИЯ МЕТАНА 2 0 2 0 1 0 2 2 9 8 (86) Заявка PCT: (72) Автор(ы): ЦИЦЕРОН, Джоэль (US), ШЕРИДАН, Дэвид (US), ТЮРК, Грегори Дж. (US), ЛАКХАПАТРИ, Сатиш (US), ФЭНЬ, Жун (US), РАДЕЛЛИ, Гвидо (US), МАРТЕНС, Францискус Дж.А. (CA), МАККОРМИК, Джарод (US), РОЗЕНБЕРГ, Дэниел (US), ЦУРКЕР, ...

Heat exchange reactor

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

Apparatus for the catalytic oxidation of hydrocarbons

Process and device for the gasification of materials and or for reforming a gas, plus a high-temperature heat-exchanger for carrying out the process

내용 없음. No content.

CASE PIPE REACTOR FOR APPLICATION OF CATALYTIC GAS STAGE REACTIONS AND METHOD FOR CARRYING OUT AN APPLICATION.

Buluş, patent istemi 1'in giriş kısmına göre bir mahfazalı boru reaktörü ve bu tür bir reaktörün çalıştırılmasına yönelik kullanımlar ve bir yönteme ilişkindir. The invention relates to a housing tube reactor according to the preamble of patent claim 1, and a method and uses for operating such a reactor.

Fluidized bed reactor apparatus and related gasification system

A process and pressurized, gasification reactor apparatus for converting combustible carbon containing materials such as coal char and other carbonaceous solids or carbonaceous solids/heavy oil combinations to an intermediate heating value fuel gas. The gasification reactor includes an insulated fluidized bed reactor chamber, an upper reactor housing for a freely suspended bayonet bundle type heat exchanger for (a) superheating incoming saturated steam and (b) cooling outgoing high temperature product gas, and a lower reactor housing structure which includes a free-floating, conically-shaped perforated plenum chamber. The superheated steam and oxygen are premixed with the plenum chamber before being pressure directed into the fluidized bed reactor chamber for mixture and combustion with the incoming combustible carbon containing materials such as coal char. After reaction of the superheated steam, oxygen and coal char in the fluidized bed reactor at temperatures ranging from 900° F. to 1750° F., the product fuel gases and associated particulate matter are cooled by steam flowing through the bayonet heat exchanger, the steam being superheated by this exchange. After discharge from the heat exchanger, the fuel gas product containing particulate matter is pressure directed into a conventional cyclone separator for (a) separation of the desired product gases and (b) return of the particulate matter for further recycling in the reactor chamber. Undesirable ash clinkers are gravitationally and pressure directed out of the reactor chamber through a central ash withdrawal pipe.

DEVICE AND METHOD FOR CATALYTIC GAS-PHASE REACTIONS, AND ALSO THEIR APPLICATION

1. Реактор для каталитических экзотермических газофазных реакций конверсии сырьевого газа в продуктовый газ, включающий в направлении потока сырьевого газа входную зону (1), реакционную зону (2), содержащую по меньшей мере один катализатор (4), и зону выхода (3) продуктового газа, где сырьевая газовая смесь вводится во входную зону (1), в области входной зоны (1) или в области входной зоны (1) и реакционной зоны (2) предусмотрена по меньшей мере одна изолирующая оболочка (6), которая изолирует внутренний объем реактора от реакторной рубашки (5) на высоте входной зоны (1) или на высоте входной зоны (1) и реакционной зоны (2), и/или где предусмотрено по меньшей мере одно устройство для проведения охлаждающей среды в область входной зоны (1) или в область входной зоны (1) и реакционной зоны (2), причем эти средства снижают теплоперенос из реакционной зоны (2) во входную зону (1), и/или причем внутренние стенки реактора в области входной зоны (1) или в области входной зоны (1) и реакционной зоны (2) состоят из инертного материала. ! 2. Реактор по п.1, отличающийся тем, что в области входной зоны (1) и реакционной зоны (2) предусмотрены средства для снижения теплопереноса из реакционной зоны (2) во входную зону (1). ! 3. Реактор по п.1, отличающийся тем, что в области входной зоны (1) или в области входной зоны (1) и реакционной зоны (2) предусмотрены средства, которые уменьшают теплоперенос из реакционной зоны (2) во входную зону (1), и тем, что внутренние стенки реактора в области входной зоны (1) или в области входной зоны (1) и реакционной зоны (2) состоят из инертного материала. ! 4. Реактор по п.1, отличающийся тем, что устройство для проведения охлаждающей среды находи РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2009 149 317 (13) A (51) МПК B01J 8/00 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ, ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21)(22) Заявка: 2009149317/05, 28.05.2008 (71) Заявитель(и): УДЕ ГМБХ (DE) Приоритет(ы): (30) Конвенционный ...

Reactor for realization of the non-adiabatic reactions

FIELD: chemical industry; devices for realization of the non-adiabatic reactions. SUBSTANCE: the invention is pertaining to the field of chemical industry, in particular, to the reactor for realization of the non-adiabatic reactions. The reactor consists of the metallic ingot and contains, at least, one reactionary passage made through the ingot and designed for maintaining the catalyst for the non-adiabatic transformation of the reactants flow. The reactor contains the inlet channels for introduction of the stream of the reactants into the reactionary passage and the outlet channels for withdrawal of the reacted stream of the reactants; and also the heating-up or cooling device intended for maintaining the catalytic non-adiabatic transformation of the torrent of the reactants. The invention provides, that the mentioned inlet and outlet channels are made in the ingot and are located mainly perpendicularly to the reactionary passages and in parallel connect the reactionary passages. The technical result of the invention is the possibility to use of the reactor for the small-scale production works. EFFECT: the invention ensures the possibility to use of the reactor for the small-scale production works. 9 cl, 1 dwg ÐÎÑÑÈÉÑÊÀß ÔÅÄÅÐÀÖÈß RU (19) (11) 2 299 093 (13) C2 (51) ÌÏÊ B01J 8/02 (2006.01) B01J 19/24 (2006.01) B01L 5/00 (2006.01) ÔÅÄÅÐÀËÜÍÀß ÑËÓÆÁÀ ÏÎ ÈÍÒÅËËÅÊÒÓÀËÜÍÎÉ ÑÎÁÑÒÂÅÍÍÎÑÒÈ, ÏÀÒÅÍÒÀÌ È ÒÎÂÀÐÍÛÌ ÇÍÀÊÀÌ (12) ÎÏÈÑÀÍÈÅ ÈÇÎÁÐÅÒÅÍÈß Ê ÏÀÒÅÍÒÓ (21), (22) Çà âêà: 2001131921/12, 27.11.2001 (72) Àâòîð(û): ÉÎÐÍ Ýðíñò (DK), ËÅÃÑÒÅÄ-ÍÈËÜÑÅÍ Ýðèê (DK) (24) Äàòà íà÷àëà îòñ÷åòà ñðîêà äåéñòâè ïàòåíòà: 27.11.2001 (73) Ïàòåíòîîáëàäàòåëü(è): ÕÀËÜÄÎÐ ÒÎÏÑÅÝ À/Ñ (DK) R U (30) Êîíâåíöèîííûé ïðèîðèòåò: 28.11.2000 DK PA200001789 (43) Äàòà ïóáëèêàöèè çà âêè: 20.07.2003 (45) Îïóáëèêîâàíî: 20.05.2007 Áþë. ¹ 14 2 2 9 9 0 9 3 (56) Ñïèñîê äîêóìåíòîâ, öèòèðîâàííûõ â îò÷åòå î ïîèñêå: WO 98/50147 A1, 12.11.1998. US 5958091 A, 28.09.1999. US 4973777 A, 27.11.1990. RU 2078611 C1, 10.05.1997. ...

Method for sustainable preparation of polycrystalline silicon using fluidized bed reactor

본 발명은 유동층 반응기를 이용한 다결정 실리콘 제조방법에 관한 것으로서, 특히 다결정 실리콘의 제조장치에서 반응관 내벽면에 형성되는 실리콘 퇴적물을 효과적으로 제거하면서 실리콘 입자를 제조할 수 있게 하는 다결정 실리콘의 지속 가능한 제조방법에 관한 것이다. 입자형태의 다결정 실리콘을 제조함에 있어서, 본 발명은, 반응관 내부에서 형성된 실리콘 입자들의 층이 유동하는 상태에서 실리콘 석출이 일어날 수 있도록 실리콘 원소를 함유한 반응가스를 공급하는 반응가스주입수단의 반응가스 출구가 상기 실리콘 입자들의 층 내부에 위치하고, 상기 출구의 높이를 기준으로 할 때 출구의 상측과 하측이 반응가스에 의해 실리콘 석출반응이 진행되는 반응영역과 실리콘 입자들의 가열을 위한 가열영역으로 각각 구분되는 입자형태의 다결정 실리콘을 제조하기 위한 유동층 반응기를 이용하되, 상기 반응가스주입수단에 의해 상기 반응가스를 공급함으로써 반응가스와 접촉하는 실리콘 입자들의 표면에 실리콘이 석출됨과 동시에 상기 반응영역을 에워싸는 반응관의 내벽면에 실리콘 퇴적물이 누적되는 실리콘 입자들 제조 단계와; 상기 반응가스를 공급하는 것을 중단한 다음, 상기 반응관 내부에 잔류하는 실리콘 입자들의 잔류층의 높이가 상기 출구의 높이를 초과하지 않도록 실리콘 입자들의 일부를 상기 유동층 반응기의 외부로 배출시키는 실리콘 입자들 부분 배출 단계와; 상기 실리콘 퇴적물과 반응하여 기상의 실리콘 화합물을 생성시킬 수 있는 에칭가스를 상기 반응영역의 공간으로 공급함으로써 실 리콘 퇴적물을 제거하는 실리콘 퇴적물 제거 단계;를 포함한다. 이러한 본 발명에 의하면, 유동층 반응기를 안정적으로 지속 가능하게 운전할 수 있고, 또한 상기 실리콘 입자들 제조 단계, 실리콘 입자들 부분 배출 단계, 실리콘 퇴적물 제거 단계, 실리콘 입자들 보충 단계가 순서대로 진행되는 실리콘 석출 운전 사이클을 반복하면서 유동층 반응기를 해체하지 않고 다결정 실리콘 입자를 제조하는 것이 가능하다. 다결정, 실리콘, 석출, 퇴적물, 유동층 반응기, 반응관, 에칭