СПОСОБ ГАЗОФАЗНОЙ ПОЛИМЕРИЗАЦИИ ОЛЕФИНОВ

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

СПОСОБ И УСТРОЙСТВО ДЛЯ ГАЗОФАЗНОЙ ПОЛИМЕРИЗАЦИИ

Изобретение относится к области полимеризации α-олефинов. Описан способ и устройство газофазной каталитической полимеризации, проводимой в двух взаимосвязанных зонах полимеризации, в которые подают один или нескольких мономеров в присутствии катализатора в условиях полимеризации и из которых выгружают полученный полимер. Растущие частицы полимера движутся вверх через первую зону полимеризации в условиях быстрого псевдоожижения, покидают указанную первую зону и входят в другую зону полимеризации, через которую они движутся в уплотненной форме под действием гравитации, покидают указанную вторую зону и вновь вводятся в первую зону полимеризации, обеспечивая тем самым циркуляцию полимера между двумя зонами полимеризации. Настоящее изобретение отличается тем, что состав газа, вводимого во вторую зону полимеризации, отличается от состава газа, присутствующего в первой зоне полимеризации, и избегают попадания газа, присутствующего в первой зоне полимеризации, во вторую зону полимеризации. Технический ...

УСТРОЙСТВО ДЛЯ УДАЛЕНИЯ ПОВЕРХНОСТНЫХ ВЕЩЕСТВ КАТАЛИЗАТОРА

Изобретение относится к устройству для удаления поверхностного вещества катализатора, присутствующего на поверхности катализатора, с катализатора путем приведения газового потока в контакт с катализатором, расположенным внутри основного корпуса устройства. Данное устройство включает: основной корпус; собирающее устройство для сбора катализатора, находящегося в верхней части основного корпуса; и возвратное устройство для возврата катализатора, соединенное с собирающим устройством. При этом возвратное устройство расположено так, что его нижний конец находится в контакте с данным газовым потоком, и часть катализатора, находящегося в контакте с газовым потоком внутри основного корпуса, собирается собирающим устройством и возвращается внутрь основного корпуса возвратным устройством, длина газового потока в направлении потока газа составляет 55 мм или больше, и средняя скорость потока газа составляет 80 м/с или больше и 500 м/с или меньше в расчете на линейную скорость при 15°C и 1 атм. Предлагаемое ...

СИСТЕМНЫЕ КОМПОНЕНТЫ СИСТЕМ РЕАКТОРА С ПСЕВДООЖИЖЕННЫМ КАТАЛИЗАТОРОМ

Группа изобретений относится к реакторным установкам для химической обработки, в частности к системе реактора с псевдоожиженным катализатором и системному компоненту системы реактора. Системный компонент содержит секцию отделения катализатора, содержащую стенки отделительной секции, образующие внутреннюю область секции отделения катализатора, выпускное отверстие для газа, отверстие стояка, отделительное устройство и выпускное отверстие для катализатора, стояк, проходящий через отверстие стояка секции отделения катализатора и содержащий основной внутренний сегмент стенки стояка, основной наружный сегмент стенки стояка и переходный сегмент стенки стояка, причем основной внутренний сегмент стенки стояка расположен по меньшей мере частично во внутренней области секции отделения катализатора и соединен по меньшей мере с переходным сегментом стенки стояка, а наружный сегмент стенки стояка расположен по меньшей мере частично за пределами секции отделения катализатора, и бак реактора, содержащий ...

СПОСОБ ПРЕВРАЩЕНИЯ КИСЛОРОДСОДЕРЖАЩИХ СОЕДИНЕНИЙ В ОЛЕФИНЫ И УСТРОЙСТВО ДЛЯ ЕГО ОСУЩЕСТВЛЕНИЯ

Изобретение относится к способу превращения кислородсодержащих соединений, имеющих по меньшей мере от 1 до 10 атомов углерода в олефины, характеризующемуся тем, что включает следующие стадии: а) контактирование в реакторе кислородсодержащих соединений с флюидизированным катализатором, содержащим ELAPO, с превращением указанных соединений в углеводороды, причем в реакторе имеются, по меньшей мере две зоны: первая зона, в которой газ движется с большей скоростью, чем во второй зоне, в которой газ движется с меньшей скоростью, и b) введение продувочного газа, содержащего некоторое количество инертного газа, во вторую зону отдельно от сырьевого потока. Также изобретение относится к устройству для осуществления настоящего способа. Применение настоящего изобретения позволяет предотвратить накопление нежелательных побочных продуктов в застойных зонах внутри реактора и уменьшает количество кокса, осажденного на катализаторе в застойных зонах или на поверхности внутри этих зон. 2 н. и 6 з.п. ф-лы ...

РЕАКТОР С КИПЯЩИМ СЛОЕМ И СПОСОБ ПОЛУЧЕНИЯ ПАРА-КСИЛОЛА И СОВМЕСТНОГО ПОЛУЧЕНИЯ НИЗШИХ ОЛЕФИНОВ ИЗ БЕНЗОЛА И МЕТАНОЛА И/ИЛИ ДИМЕТИЛОВОГО ЭФИРА

Изобретение относится к реакторам с кипящим слоем и их использованию для получения пара-ксилола и совместного получения низших олефинов из бензола и метанола и/или диметилового эфира. Описан реактор, содержащий первый и второй распределитель, через которые в реактор поступают материальные потоки A и В, причем первый распределитель расположен в нижней части кипящего слоя, а второй расположен в по меньшей мере одной зоне газового потока после первого распределителя; причем второй распределитель содержит впускную трубу, микропористую трубу и впускную кольцевую трубу; впускная труба соединена с газовым каналом микропористой трубы, причем газ подают через впускную трубу снаружи от кипящего слоя в микропористую трубу в кипящем слое; впускная кольцевая труба соединена с газовым каналом впускной трубы, причем впускная кольцевая труба расположена в плоскости, перпендикулярной направлению потока газа из первого распределителя; микропористая труба расположена на кольцевой впускной трубе и перпендикулярно ...

СПОСОБ ПОЛИМЕРИЗАЦИИ ОЛЕФИНОВ В ГАЗОФАЗНОМ РЕАКТОРЕ, ВКЛЮЧАЮЩЕМ РЕАКТОР ВОСХОДЯЩЕГО ПОТОКА И РЕАКТОР НИСХОДЯЩЕГО ПОТОКА

Изобретение относится к способу получения полимера этилена, включающему гомополимеризацию этилена или сополимеризацию этилена с одним или несколькими сомономерами в реакторе газофазной полимеризации. Реактор газофазной полимеризации имеет реактор восходящего потока, в котором растущие полимерные частицы движутся вверх в условиях псевдоожижения, быстрого псевдоожижения или других режимах транспортировки, и реактор нисходящего потока, в котором растущие частички полимера стекают вниз в уплотненной форме. В реакторе нисходящего потока остаточный объем полимерных частиц составляет 55- 80 мас.% от остаточного объема полимерных частиц в реакторе газофазной полимеризации. Технический результат – предотвращение и минимизация образования агломератов, комков или отложений на стенке реактора. 14 з.п. ф-лы, 1 ил., 1 табл., 3 пр.

СПОСОБ И УСТРОЙСТВО ДЛЯ ПОЛИМЕРИЗАЦИИ ПРОПИЛЕНА

... 1. Способ получения гетерофазных пропиленовых сополимеров путем полимеризации пропилена в присутствии катализатора полимеризации и водорода в качестве регулятора молекулярного веса, включающий следующие стадии: а) полимеризация пропилена в газовой или жидкой фазе, необязательно совместно с одним или более α-олефиновыми сомономерами, с получением фракции кристаллического полимера; b) сополимеризация этилена с пропиленом и/или 1-бутеном и необязательно одним или более альфа-олефиновыми сомономерами С5-С12 в газофазном реакторе с соединенными друг с другом зонами полимеризации, где растущие полимерные частицы перетекают снизу вверх через первую зону полимеризации (устройство с восходящим потоком) в условиях быстрого псевдоожижения или транспортирования, покидают упомянутое устройство с восходящим потоком и поступают во вторую зону полимеризации (устройство с нисходящим потоком), через которую они перетекают сверху вниз под действием силы тяжести, покидают упомянутое устройство с нисходящим ...

СМЕШИВАЮЩАЯ РАСХОДНАЯ РЕЗЕРВУАРНАЯ СИСТЕМА

... 1. Расходная резервуарная система для хранения суспензии, содержащая:резервуар для хранения, имеющий первый конец, второй конец и, по меньшей мере, одну стенку, окружающую внутренний объем между первым и вторым концами;впуск для суспензии в сообщении по текучей среде с внутренним объемом;выпуск в сообщении по текучей среде с внутренним объемом;впуск для рециркуляции в сообщении по текучей среде с внутренним объемом у первого конца резервуара для хранения;насос, имеющий всасывающую линию в сообщении по текучей среде с выпуском;клапан рециркуляции в сообщении по текучей среде с выпускной линией насоса и впуском для рециркуляции; ивыпускной клапан в сообщении по текучей среде с выпускной линией насоса.2. Система по п. 1, дополнительно содержащая дефлектор, расположенный в данном внутреннем объеме, и выполненный с возможностью перенаправления потока между впуском для суспензии и впуском для рециркуляции.3. Система по п. 1, в которой указанный первый конец наклонен в направлении впуска для рециркуляции ...

Reaktor zur Durchführung rascher stark exothermer Reaktionen und dessen Verwendung

The invention relates to a tube bundle reactor (1) for rapid highly exothermic reactions, consisting of a reactor housing (2) with a bundle (3) of tubes (6) as a reaction zone, said tubes being optionally interconnected radially in relation to their longitudinal extension, eduction pipes (4, 11), a product outlet (12) and a heat exchanger (5). The invention is characterised in that said eduction pipes (4) are configured as pipelines (4a, 4b, 4c, 4d) which are arranged in the tubes (6) of the bundle (3) and which are provided with a plurality of openings (7), said openings (7) in the pipelines (4a, 4b, 4c, 4d) being spread over the entire length of or a section of the length of the reaction zone.

Verfahren zur Durchführung von Stoffumwandlungen mit in Flüssigkeiten suspendierten Katalysatoren

Verfahren zur katalytischen Umwandlung von Kohlenwasserstoffen

Verfahren zur Herstellung von Acrylsaeurenitril und Methacrylsaeurenitril durch Umsetzung von Propylen oder Isobutylen mit Sauerstoff und Ammoniak

Verfahren und Anlage zur Wärmebehandlung von eisenoxidhaltigen Feststoffen

Verfahren zur Wärmebehandlung von eisenoxidhaltigen Feststoffen, bei dem feinkörnige Feststoffe in einem Reaktor (8) mit Wirbelbett auf eine Temperatur von 700 bis 1.150°C erhitzt werden, dadurch gekennzeichnet, dass ein erstes Gas oder Gasgemisch von unten durch wenigstens ein Gaszufuhrrohr (9) in einen Wirbelmischkammerbereich (15) des Reaktors (8) eingeführt wird, wobei das Gaszufuhrrohr (9) wenigstens teilweise von einer durch Zufuhr von Fluidisierungsgas fluidisierten, stationären Ringwirbelschicht (12) umgeben wird, und dass die Gasgeschwindigkeiten des ersten Gases oder Gasgemisches sowie des Fluidisierungsgases für die Ringwirbelschicht (12) derart eingestellt werden, dass die Partikel-Froude-Zahlen in dem Gaszufuhrrohr (9) zwischen 1 und 100, in der Ringwirbelschicht (12) zwischen 0,02 und 2 sowie in der Wirbelmischkammer (15) zwischen 0,3 und 30 betragen.

Manufacture of unsaturated aliphatic aldehydes

Unsaturated aliphatic aldehydes are made by reaction between formaldehyde and another saturated aliphatic aldehyde in the vapour phase in the presence of a finely-divided dehydrating catalyst maintained in the fluidized state in the reaction zone and circulated between the reaction zone and a zone in which it is regenerated while in the fluidized state by treatment with oxygen at an elevated temperature, the oxygen in the regeneration zone being used in the proportion of 0.02 to 0.15 mols, per mol. of aldehydes fed to the reaction zone in the same period of time. The catalyst specified is finely-divided silica gel impregnated with 0.1-5.0 per cent of an oxide of manganese, lead, zinc, or cadmium, and preferably passes a 50-120 mesh screen (U.S. units). Reaction temperature is 200-450 DEG C. and 1.0-3.0 mols. of formaldehyde per mol. of other aldehyde are used. The formaldehyde is preferably used as a 10-50 per cent aqueous solution. Temperatures specified for regeneration are 300-500 DEG ...

Method and system for cracking hydrocarbons

... 1,147,257. Catalytic cracking. MOBIL OIL CORP. 20 Sept., 1967, No. 42864/67. Heading C5E. A catalytic hydrocarbon conversion process comprises passing hydrocarbon vapour through an arranged series of dilute phase riser reactors through which series catalyst passes generally countercurrent to the flow of hydrocarbon vapours but concurrently with hydrocarbon vapour through any one reactor, the temperature at which vapour contacts catalyst in the individual reactors being progressively decreased in the direction of vapour flow through the series of reactors. The reactors may be followed by series of catalyst strippers and regenerators. The feed may be preheated by inert solid or partially pre-cracked by another catalyst in a preliminary stage which may also be provided with strippers and regenerators.

Improved process for the catalytic conversion of hydrocarbons

... In processes for the catalytic conversion of hydrocarbons in which the catalyst is cycled between a conversion and a regeneration zone, the conversion rate in volume per cent. is maintained substantially constant by increasing the ratio of catalyst to oil by weight passing through the conversion zone as the activity of the catalyst diminishes. A cracking plant of conventional arrangement comprising reactor 28 and regenerator 78 with associated separators 38, 52, 104, 92 and hoppers 44, 96 is described and the stand pipe 22 through which the regenerated catalyst is rtcycled to mix with the feed in line 18 is provided with a valve 24 by which the amount of catalyst mixed with the oil may be regulated. Examples are given in which the original catalyst/oil weight ratio of 1/1 is increased after about 100 hours running to 2/1 and later to 2.4/1 . In another example the ratio of 1.5/1 is increased first to 2.7/1 and finally to 5.5/1 .

Process and apparatus for contacting vaporized hydrocarbons with fluidised finely divided solid catalyst

In processes for the catalytic conversion of hydrocarbon vapours in presence of a fluidized solid catalyst, reduction in the size of the apparatus and improved conversion ratios are obtained by arranging the conventional cyclone catalyst separators inside the reaction or regeneration zones and discharging them by gravity by pipes dipping into a fluidized catalyst bed, the level of which is lower than that of the catalyst bed in the reactor or regenerator. The reactor 2 is divided by a sector plate 3 into reaction and stripping zones. Catalyst dust entrained in the gaseous reaction products is removed therefrom in a conventional two-stage cyclone separator 4, 5 and the separated catalyst is discharged by gravity through a pipe 8 into the catalyst bed in the stripping zone, the level of which is maintained lower than that in the reactor. The regenerator 1 is similarly constructed. The construction enables the height of the sector 3 to be increased, thus enabling the height ...

Process and plant for the thermal treatment of fine-grained solids

Improved apparatus for carrying out gaseous reactions at high temperatures

... An apparatus for controlling chemical reactions of short duration comprises in combination an elevated catalyst regeneration vessel 3, a reaction vessel 1 positioned below the regeneration vessel, a stand-pipe 4 connecting the regeneration vessel with the reaction vessel so as to conduct a natural flow of the fluidized catalyst from the regeneration vessel to the bottom inlet of the reaction vessel, means such as a pipe 20 and a distributing screen 21 for introducing a gasiform reactant into the bottom inlet of the reaction vessel so as to pick up and carry along in suspension through the reactor to its upper outlet the fluidized catalyst flowing from the stand-pipe, the outlet of the reactor being substantially below the level of fluidized catalyst in the regeneration vessel, a catalyst separating device 10, 10a at the outlet of the reaction vessel for directly receiving the catalyst suspension discharged from the reaction vessel and for separating centrifugally and ...

Improved method of regenerating a catalyst

... 552,334. Regenerating catalysts. STANDARD OIL DEVELOPMENT CO. June 16, 1941, Nos. 7617 and 7618. Convention dates, June 15, 1940, and July 16, 1940. Drawings to Specification. [Class 1 (i)] In the regeneration of catalysts contaminated with carbonaceous matter by burning this off, the temperature is controlled by mixing catalyst, which has been at least partly regenerated and then cooled, with the catalyst to be regenerated. The process is applicable either to granular or to finely divided catalyst. In the latter case this is suspended in a gas containing insufficient oxygen to effect complete regeneration, a part of the catalyst is separated from the gas after this treatment and recycled with a subsequent portion of catalyst, and the remainder is mixed with more oxygen and subjected to a second regeneration stage.

Process of roasting refractory gold ores

PROCEDURE FOR THE GASEOUS PHASE POLYMERIZATION OF OLEFINEN

IMPROVED DEEP CATALYTIC CRACKING PROCEDURE

PROCEDURE AND DEVICE FOR THE POLYMERIZATION OF PROPYLENE

PROCEDURE AND DEVICE FOR A THERMAL TREATMENT IN A FLUID BED

Wirbelschichtreaktorsystem

Die Erfindung betrifft ein Wirbelschichtreaktorsystem, umfassend einen oder mehrereWirbelschichtreaktoren (1, 2, 20) zur Durchführung chemischer oder physikalischerReaktionen, wovon zumindest ein Reaktor als schnell fluidisierter Reaktor zum Betriebals zirkulierende Wirbelschicht ausgeführt ist und am oberen Ende einen Fluidauslass(5, 6), einen Partikelabscheider (3, 4) und eine damit verbundene Partikelleitung(7, 8) zur Rückführung abgeschiedener Wirbelschichtpartikel in denselben odereinen weiteren Reaktor umfasst, wobei in zumindest einem schnell fluidisiertenReaktor ein oder mehrere Strömungsregler (18, 21) vorgesehen sind, um darin voneinandergetrennte Reaktionszonen (9, 10, 22) zu erzeugen, mit dem Kennzeichen,dass zur Regelung der Strömungsverhältnisse in den Reaktionszonen (9, 10, 22)einer oder mehrere der Strömungsregler (18, 21) von außerhalb des Systems gezieltverstellbar ist/sind. The invention relates to a fluidized-bed reactor system comprising one or more fluidized-bed reactors (1, 2, 20) for carrying out chemical reactions, at least one reactor being designed as a rapidly fluidized reactor for operation as a circulating fluidized bed and having a fluid outlet (5, 6) at the top Particle separator (3, 4) and associated particle line (7, 8) for recycling deposited fluidized bed particles into the same or a further reactor, wherein in at least one fast fluidized reactor one or more flow regulators (18, 21) are provided for separating reaction zones (18, 21) therebetween. 9, 10, 22), with the characteristic that for controlling the flow conditions in the reaction zones (9, 10, 22) one or more of the flow regulators (18, 21) is / are selectively adjustable from outside the system.

PROCEDURE AND DEVICE FOR THE GASEOUS PHASE POLYMERIZATION

Process for preparing ethylene and/or propylene

The present invention provides a process for preparing ethylene and/or propylene, wherein oxygenates and olefins are converted to ethylene and/or propylene over a zeolite-comprising catalyst, comprising the steps of: a) reacting in a first reactor an oxygenate feed over the zeolite-comprising catalyst at a temperature in the range of from 350 to 1000 °C and retrieving from the first reactor a first reactor effluent stream comprising gaseous products, including ethylene and/or propylene, and zeolite-comprising catalyst; b) reacting in a second reactor an olefin feed over the zeolite-comprising catalyst at a temperature in the range of from 500 to 700 °C and retrieving from the second reactor a second reactor effluent stream comprising gaseous products, including ethylene and/or propylene, and zeolite-comprising catalyst; c) providing the first and second reactor effluent stream to one or more gas/solid separators to retrieve zeolite-comprising catalyst from the first and second reactor effluent ...

Method and apparatus for oxidative coupling of methane

CONVERSION OF STACKED FCC UNIT

... "CONVERSION OF STACKED FCC UNIT" A stacked FCC reactor-regenerator arrangement is converted into an FCC riser unit having a two-stage regenerator. In this method, a stacked FCC unit having a bottom regeneration vessel, a superadjacent reactor vessel, and a stripping vessel laterally offset from and in open communication with the reactor vessel are used to make a two-stage regenerator having a lower first stage of regeneration, an upper second stage regeneration vessel, and a catalyst cooler for removing heat from the regenerated catalyst. This method involves modifying the vessels in the stacked reactor regenerator arrangement by converting the bottom regeneration into a first stage regeneration vessel, the upper reactor vessel into a second stage regeneration vessel and the stripping vessel into a regenerated catalyst cooler which operates as a downflow type catalyst cooler or a backmix type catalyst cooler. Therefore, apart from the addition of a new riser reactor only relatively minor ...

FLUIDIZED BED SYSTEM

A fluidized bed system is a single unitary modular system that packages a circulation fan, a fluidized bed, and a dust collection system within a same structure. The structure is formed to include internal ducts to provide fluid communication between the circulation fan, the fluidized bed, and the dust collection system. The fan provides a flow of air via a pressure duct to the fluidized bed. Particulate is separated from particles included on the fluidized bed by the flow of air being uniformly distributed to the fluidized bed. Particulate separated in a disengagement area and suspended in the flow of air is conducted through a particulate clearance space surrounding the dust collection system. The particulate is captured by the dust collection system and conveyed to a location external to the system.

FLUIDIZED BED REACTOR SYSTEM

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

PROCESS FOR CONVERTING A SOLID BIOMASS MATERIAL

A process for converting a solid biomass material, comprising contacting the solid biomass material with a catalytic cracking catalyst at a temperature of more than 400°C in a riser reactor to produce one or more cracked products, wherein the riser reactor is an internal riser reactor.

FLUIDIZED BED REACTOR AND PROCESS FOR PRODUCING OLEFINS FROM OXYGENATES

The present invention provides a fluidized bed reactor and its use for producing olefins from oxygenates, the fluidized bed reactor comprises: a reaction zone located in the lower portion of the fluidized bed reactor and comprising a lower dense phase zone and an upper riser, wherein the dense phase zone and the riser are connected with each other transitionally; a separation zone located in the upper portion of the fluidized bed reactor and comprising a settling chamber, a fast gas-solid separation means, a cyclone and a gas collecting chamber, wherein the riser extends upwardly into the separation zone and is connected at its outlet with the inlet of the fast gas-solid separation means, the fast gas-solid separation means is connected at its outlet with the inlet of the cyclone via a fast gas passage, the cyclone is connected at its outlet with the gas collecting chamber, and the gas collecting chamber is located below the reactor outlet and connected therewith; and a catalyst recycle ...

PROCESS AND REACTOR FOR CARRYING OUT CONVERSIONS WITH CATALYSTS SUSPENDED IN LIQUIDS, AND REACTOR FOR THIS PURPOSE

Catalytic reactions are carried out in a reactor which contains a liquid phase in which at least one catalyst is suspended, and which may additionally contain a gas phase, by a process in which the liquid phase and , if present, also the gas phase are fed, at least partly, through an apparatu s having orifices or channels in the reactor, the hydraulic diameter of which orifices or channels is from 0.5 to 20 mm, preferably from 1 to 10 mm, particularly preferably from 1 to 3 mm.

Verfahren zur Durchführung katalytischer Reaktionen.

Procédé de craquage d'hydrocarbures et appareil pour la mise en oeuvre de ce procédé

Verfahren zur Herstellung ungesättigter Nitrile

METHOD AND DEVICE FOR HEAT TREATMENT OF SOLID MATERIALS, CONTAINING IRON OXIDE, USING FLUIDIZED BED REACTOR

УСТАНОВКА ДЛЯ ТЕРМИЧЕСКОЙ ОБРАБОТКИ ТВЕРДЫХ МАТЕРИАЛОВ, СОДЕРЖАЩИХ ОКСИД ЖЕЛЕЗА, С ИСПОЛЬЗОВАНИЕМ РЕАКТОРА С ПСЕВДООЖИЖЕННЫМ СЛОЕМ

Настоящее изобретение относится к установке для термической обработки твердых материалов, содержащих оксид железа, на которой мелкозернистые твердые материалы нагреваются до температуры от 700 до 1150°С в реакторе с псевдоожиженным слоем (8). С целью улучшения использования энергии предлагается вводить первый газ или газовую смесь снизу через по меньшей мере одну газоподводящую трубу (9) в область смесительного пространства (15) реактора (8), причем газоподводящая труба (9), по крайней мере, частично окружена стационарным кольцевым псевдоожиженным слоем (12), который псевдоожижается подаваемым псевдоожижающим газом. Объемные скорости первого газа или газовой смеси и псевдоожижающего газа для кольцевого псевдоожиженного слоя регулируют таким образом, чтобы число Фруда для частиц в газоподводящей трубе (9) было в пределах от 1 до 100, в кольцевом псевдоожиженном слое (12) от 0,02 до 2 и в смесительном пространстве (15) от 0,3 до 30.

СПОСОБ И УСТАНОВКА ДЛЯ ТЕРМИЧЕСКОЙ ОБРАБОТКИ В ПСЕВДООЖИЖЕННОМ СЛОЕ

Настоящее изобретение относится к установке для термической обработки мелкозернистых твердых материалов, в частности гипса, в которой мелкозернистые твердые материалы нагревают до температуры от 50 до 1000°С в реакторе с псевдоожиженным слоем (1). С целью улучшения использования энергии предлагается вводить первый газ или газовую смесь снизу через расположенную преимущественно по центру газоподводящую трубу (3) в смесительное пространство (21) реактора (1), причем газоподводящая труба (3), по крайней мере, частично окружена стационарным кольцевым псевдоожиженным слоем (2), который псевдоожижается подводимым псевдоожижающим газом, и регулировать объемные скорости первого газа или газовой смеси, а также псевдоожижающего газа для кольцевого псевдоожиженного слоя (2) таким образом, чтобы число Фруда для частиц в газоподводящей трубе было в пределах от 1 до 100, в кольцевом псевдоожиженном слое от 0,02 до 2 и в смесительном пространстве от 0,3 до 30.

УСТАНОВКА ДЛЯ УДАЛЕНИЯ ГАЗООБРАЗНЫХ ЗАГРЯЗНИТЕЛЕЙ ИЗ ОТХОДЯЩИХ ГАЗОВ

Настоящее изобретение относится к устройству для удаления газообразных загрязнителей из отходящих газов, в котором газообразные загрязнители реагируют с мелкозернистым реагентом с образованием в реакторе с псевдоожиженным слоем (2) твердых материалов. С целью низких концентраций загрязнителя в чистом газе при почти стехиометрическом расходе реагента предлагается введение отходящего газа снизу через расположенную преимущественно по центру газоподводящую трубу (20) в смесительное пространство (21) реактора (2), причем газоподводящая труба (20), по крайней мере, частично окружена стационарным кольцевым псевдоожиженным слоем (22) реагента, который псевдоожижается подводимым псевдоожижающим газом и в котором объемные скорости отходящего газа и псевдоожижающего газа для кольцевого псевдоожиженного слоя регулируют таким образом, чтобы число Фруда для частиц было в газоподводящей трубе (20) в пределах от 1 до 100, в кольцевом псевдоожиженном слое (22) от 0,02 до 2 и в смесительном пространстве ...

СПОСОБ И УСТАНОВКА ДЛЯ ТЕРМИЧЕСКОЙ ОБРАБОТКИ МЕЛКОЗЕРНИСТЫХ ТВЕРДЫХ ЧАСТИЦ

Настоящее изобретение относится к способу химической и/или физической обработки псевдоожижаемых материалов в реакторе (1, 1'), включающему предпочтительно подачу топлива и воздуха горения предпочтительно в камеру сгорания (4), находящуюся выше по потоку от реактора, и сжигание при температуре в интервале приблизительно от 1000 до 1500°С. Горячий газ вводят во внутренний объем (2) реактора через центральную трубу (3). Горячий газ и центральную трубу (3) охлаждают с помощью хладагента. Кроме того, настоящее изобретение относится к установке для осуществления указанного способа.

УСТАНОВКА ДЛЯ ТЕРМИЧЕСКОЙ ОБРАБОТКИ ТВЕРДЫХ МАТЕРИАЛОВ, СОДЕРЖАЩИХ ОКСИД ЖЕЛЕЗА, С ИСПОЛЬЗОВАНИЕМ РЕАКТОРА С ПСЕВДООЖИЖЕННЫМ СЛОЕМ

Настоящее изобретение относится к установке для термической обработки твердых материалов, содержащих оксид железа, на которой мелкозернистые твердые материалы нагреваются до температуры от 700 до 1150°С в реакторе с псевдоожиженным слоем (8). С целью улучшения использования энергии предлагается вводить первый газ или газовую смесь снизу через по меньшей мере одну газоподводящую трубу (9) в область смесительного пространства (15) реактора (8), причем газоподводящая труба (9), по крайней мере, частично окружена стационарным кольцевым псевдоожиженным слоем (12), который псевдоожижается подаваемым псевдоожижающим газом. Объемные скорости первого газа или газовой смеси и псевдоожижающего газа для кольцевого псевдоожиженного слоя регулируют таким образом, чтобы число Фруда для частиц в газоподводящей трубе (9) было в пределах от 1 до 100, в кольцевом псевдоожиженном слое (12) от 0,02 до 2 и в смесительном пространстве (15) от 0,3 до 30.

СПОСОБ И УСТАНОВКА ДЛЯ ТЕРМИЧЕСКОЙ ОБРАБОТКИ В ПСЕВДООЖИЖЕННОМ СЛОЕ

Настоящее изобретение относится к способу термической обработки мелкозернистых твердых материалов, в частности гипса, в котором мелкозернистые твердые материалы нагревают до температуры от 50 до 1000°С в реакторе с псевдоожиженным слоем (1), и к соответствующей установке. С целью улучшения использования энергии предлагается вводить первый газ или газовую смесь снизу через расположенную преимущественно по центру газоподводящую трубу (3) в смесительное пространство (21) реактора (1), причем газоподводящая труба (3), по крайней мере, частично окружена стационарным кольцевым псевдоожиженным слоем (2), который псевдоожижается подводимым псевдоожижающим газом, и регулировать объемные скорости первого газа или газовой смеси, а также псевдоожижающего газа для кольцевого псевдоожиженного слоя (2) таким образом, чтобы число Фруда для частиц в газоподводящей трубе было в пределах от 1 до 100, в кольцевом псевдоожиженном слое - от 0,02 до 2 и в смесительном пространстве - от 0,9 до 30.

СПОСОБ И УСТРОЙСТВО ДЛЯ ТЕРМИЧЕСКОЙ ОБРАБОТКИ В ПСЕВДООЖИЖЕННОМ СЛОЕ

Данное изобретение относится к способу термической обработки твердых частиц, в частности, термического разложения солей, в котором твердые частицы нагревают до температуры от 200 до 1400°С в реакторе (1) с псевдоожиженным слоем, и к соответствующей установке. Для улучшения использования энергии и разложения солей предлагается вводить первый газ или смесь газов снизу через предпочтительно центральную трубу (3) подачи газа в смесительную камеру (7) реактора, при этом труба (3) подачи газа, по меньшей мере, частично окружена неподвижным кольцевым псевдоожиженным слоем (10), который псевдоожижается посредством подачи газа псевдоожижения, и скорость первого газа или смеси газов и скорость псевдоожижающего газа для кольцевого псевдоожиженного слоя (10) регулируют так, что число Фруда для частиц в трубе (3) подачи газа находится от 1 до 100, в кольцевом псевдоожиженном слое (10) от 0,02 до 2 и в смесительной камере (7) от 0,3 до 30.

СПОСІБ ТА УСТАНОВКА ДЛЯ ТЕРМІЧНОЇ ОБРОБКИ ТВЕРДИХ МАТЕРІАЛІВ, ЩО МІСТЯТЬ ОКСИД ЗАЛІЗА

Винахід належить до чорної металургії. Спосіб термічної обробки твердих матеріалів, що містять оксид заліза, включає нагрівання дрібнозернистих твердих матеріалів до температури від 700 до 1150 °С в реакторі із псевдозрідженим шаром за допомогою двох потоків газу або газових сумішей, причому перший потік газу або газової суміші вводять знизу в область змішувального простору реактора через щонайменше одну газопідвідну трубу, причому газопідвідну трубу принаймні частково оточують стаціонарним кільцевим псевдозрідженим шаром, який зріджують другим потоком газу, який є зріджувальним газом, або газовою сумішшю, що подають в реактор, при цьому об’ємні швидкості першого потоку газу або газової суміші, а також другого потоку газу або газової суміші, яким зріджують кільцевий псевдозріджений шар, регулюють таким чином, щоб число Фруда для дрібнозернистого твердого матеріалу становило в газопідвідній трубі від 1 до 100, у кільцевому псевдозрідженому шарі - від 0,02 до 2 і у змішувальному просторі ...

СПОСОБ И УСТАНОВКА ДЛЯ УДАЛЕНИЯ ГАЗООБРАЗНЫХ ЗАГРЯЗНИТЕЛЕЙ ИЗ ОТХОДЯЩИХ ГАЗОВ

Настоящее изобретение относится к способу удаления газообразных загрязнителей из отходящих газов, в котором газообразные загрязнители реагируют с мелкозернистым реагентом с образованием в реакторе с псевдоожиженным слоем (2) твердых материалов, и к соответствующей установке. С целью низких концентраций загрязнителя в чистом газе при почти стехиометрическом расходе реагента предлагается введение отходящего газа снизу через преимущественно по центру расположенную газоподводящую трубу (20) в смесительное пространство (21) реактора (2), причем газоподводящая труба (20), по крайней мере, частично окружена стационарным кольцевым псевдоожиженным слоем (22) реагента, который псевдоожижается подводимым псевдоожижающим газом и в котором объемные скорости отходящего газа и псевдоожижающего газа для кольцевого псевдоожиженного слоя регулируют таким образом, чтобы число Фруда для частиц было в газоподводящей трубе (20) в пределах от 1 до 100, в кольцевом псевдоожиженном слое (22) от 0,02 до 2 и в смесительном ...

A PROCESS FOR THE GAS-PHASE POLYMERIZATION AND AN APPARATUS FOR REALIZING THE SAME

METHOD AND PLANT FOR HEAT TREATMENT IN FLUIDIZED BED

THERMOLYTIC FRAGMENTATION OF SUGARS

METHOD AND SYSTEM THERMAL PROCESSING OF GRANULATED SOLID SUBSTANCES

METHODS FOR CONVERSION OF METHANE IN SYNTHESIS GAS-

METHOD AND DEVICE FOR POLYMERIZATION OF OLEFINS IN GAS PHASE

СПОСОБ И УСТАНОВКА ДЛЯ ТЕРМИЧЕСКОЙ ОБРАБОТКИ МЕЛКОЗЕРНИСТЫХ ТВЕРДЫХ ЧАСТИЦ

Настоящее изобретение относится к способу химической и/или физической обработки псевдоожижаемых материалов в реакторе (1, 1'), включающему предпочтительно подачу топлива и воздуха горения предпочтительно в камеру сгорания (4), находящуюся выше по потоку от реактора, и сжигание при температуре в интервале приблизительно от 1000 до 1500°С. Горячий газ вводят во внутренний объем (2) реактора через центральную трубу (3). Горячий газ и центральную трубу (3) охлаждают с помощью хладагента. Кроме того, настоящее изобретение относится к установке для осуществления указанного способа.

OLEFIN POLYMERIZATION PROCESS IN A GAS-PHASE REACTOR COMPRISING A RISER UNIT AND A DOWNCOMER

α-烯烃的气相聚合法及所用装置

在二个相连的聚合反应区内进行的气相聚合法，在反应条件下的催化剂存在下，将一种或多种α-烯烃CH 2 ＝CHR加入上述聚合反应区中，而产生的聚合物则从上述反应区中流出。本方法的特征在于生成的聚合物在快速流态化状态下流经第一聚合反应区，流出第一区后进入第二聚合反应区，此时，聚合物在重力作用下呈稠密状流过该区，流出第二区后又重新进入第一聚合反应区，这样便在二个聚合反应区之间建立了一个聚合物循环。这种新奇的方法允许用气相法聚合烯烃，并具有高的单位反应器容积的生产量，而又不会遇到当前已知的流化床技术所出现的问题。

Catalytic process of treatment of hydrocarbons

Catalytic gas conversion

Process and fluid device of catalysis

PROCESS AND DEVICE Of INTRODUCTION OF CATALYST PARTICLES INTO CATALYTIC UNREACTEUR OF CRACKING AT the FLUID STATE

A method for the treatment by gases of granular solids

GUILLOTINE VALVE FOR REGULATING FLOW IN A FLUID CATALYTIC CRACKING UNIT

DEVICE AND METHOD FOR ROTARY FLUIDIZED BED IN A SUCCESSION OF CYLINDRICAL CHAMBERS

The invention concerns a device and a method for rotary fluidized bed for catalytic polymerization, drying and other treatments of solid particles or for catalytic transformation of fluids, wherein a cylindrical reactor (1), in which the fluids are injected (7) tangentially to its cylindrical wall, is divided into a succession of cylindrical chambers (Z1, Z2, Z3) by hollow discs (3), which are fixed to its cylindrical wall, which have central openings through which the fluids circulating in rotation inside the cylindrical chambers are sucked (10), which have lateral openings through which said fluids are evacuated through the cylindrical wall of the reactor and which have passages (27) for transferring the suspended solid particles in the rotary fluidized bed from one chamber to the next through said discs (3). © KIPO & WIPO 2007 ...

reator de leito fluidificado circulante

PROCESO PARA LA CONVERSIÓN DE HIDROCARBUROS Y EQUIPAMIENTO PARA REALIZAR REACCIONES QUÍMICAS UTILIZADO EN EL MISMO

Los procesos y sistemas para la conversión de hidrocarburos en la presente pueden incluir separar un efluente de un reactor de lecho móvil, el efluente que incluye el producto de reacción, primer catalizador particulado, y segundo catalizador particulado. La separación puede recuperar una primera corriente que incluye el producto de reacción y el primer catalizador particulado y una segunda corriente que incluye el segundo catalizador particulado. La segunda corriente se puede mezclar con una corriente de catalizador regenerado que incluye tanto el primero como el segundo catalizador particulado a una temperatura elevada. La mezcla puede producir un catalizador mixto a una temperatura relativamente uniforme menor que la temperatura elevada del catalizador regenerado, donde la temperatura es más ventajosa para el contacto de la nafta liviana y la nafta pesada dentro del reactor de lecho móvil para producir el efluente que incluye el producto de reacción, el primer catalizador particulado ...

PROCESS AND APPARATUS FOR THE GAS-PHASE POLYMERIZATION OF ALPHA-OLEFINS

Process for gas-phase polymerization carried out in two interconnected polymerization zones, to which one or more -olefins CH2=CHR are in the presence of catalyst under reaction conditions and from which the polymer product is disharged. The process is characterized in that the growing polymer flows through a first polymerization zone under fast fluidization conditions, leaves said first zone and enters a second polymerization zone through which it flows in a densified form under the action of gravity, leaves said second zone and is reintroduced into the first polymerization zone, thus establishing a circulation of polymer around the two polymerization zones. The novel process allows olefins to be polymerized in the gas phase with high productivity per unit volume of the reactor without incurring the problems of the fluidized-bed technologies of the known state of the art.

METHOD AND APPARATUS FOR HEAT TREATMENT IN A FLUIDIZED BED

The present invention relates to a method for the heat treatment of fine-grained solids, in particular gypsum, in which the solids are heated to a temperature of 50 to 1000 °C in a fluidized bed reactor (1), and to a corresponding plant. To improve the energy utilization, it is proposed to introduce a first gas or gas mixture from below through a preferably central gas supply tube (3) into a mixing chamber (21) of the reactor (1), the gas supply tube (3) being at least partly surrounded by a stationary annular fluidized bed (2) which is fluidized by supplying fluidizing gas, and to adjust the gas velocities of the first gas or gas mixture as well as of the fluidizing gas for the annular fluidized bed (2) such that the particle Froude numbers in the gas supply tube (3) are between 1 and 100, in the annular fluidized bed (2) between 0.02 and 2 and in the mixing chamber (21) between 0.3 and 30.

Process for producing polyolefin grafted copolymers

A gas phase process for producing olefin polymer graft copolymers, including providing a reaction apparatus having first and second reaction zones operatively connected to each other into which particles of an olefin polymer and a free-radical polymerizable monomer are fed while maintaining free-radical polymerization conditions and a substantial non-oxidizing environment in said zones and from which the grafted copolymer product is discharged. An apparatus suitable for practicing this process is also disclosed.

Hydrogenation of carbon oxides

Method and reactor for carrying out the conversion of substances using catalysts suspended in liquids

Catalytic process for e.g. oxidation and hydration of liquids In carrying out reactions in a reactor containing a liquid phase in which a catalyst is suspended, and where a gaseous phase may be present, the liquid and gas phases pass, at least partly, through a device having openings or passages whose hydraulic diameter is 0.5-20 (1-3) mm. Also claimed is the reactor including a device having openings or passages in it built so that liquid or gas flow through it during the reaction.

Process for the conversion in a fluidized bed of a feed consisting mainly of an oxygenated compound

Process for catalytic conversion of a feed stock containing a major part of at least one oxygen-containing compound into olefinic hydrocarbons. This process comprises a thermal control of the fluidised catalyst beds with the aid of a heat exchanger. The catalyst circulates essentially from the base of a vessel (1) into a heat exchanger (6) comprising an internal separating partition which defines two elongate and adjacent compartments communicating via their lower part. In the compartment where the catalyst flows downwards the rate of fluidisation is between 0.1 cm/s and 2 m/s, while in the compartment where the catalyst rises in the heat exchanger (6) the fluidisation velocity is between 0.1 and 6 m/s. ...

PROCESS AND APPARATUS FOR THE GAS-PHASE POLYMERISATION

A process for the gas-phase catalytic polymerisation carried out in two interconnected polymerisation zones, to which one or more monomers are fed in the presence of a catalyst under polymerisation conditions and from which the produced polymer is discharged. The growing polymer particles flow through a first polymerisation zone under fast fluidisation conditions, leave said first zone and enter a second polymerisation zone through which they flow in a densified form under the action of gravity, leave said second zone and are reintroduced into the first polymerisation zone, thus establishing a circulation of polymer between the two polymerisation zones. The present invention is characterised in that a gas of composition different from that present in the first polymerisation zone is introduced into the second polymerisation zone and it is avoided that the gases present in the first polymerisation zone are introduced into the second polymerisation zone. The process is particularly suited for obtaining in-reactor made blends of olefin polymers having different compositions.

СПОСОБ И УСТРОЙСТВО ДЛЯ ГАЗОФАЗНОЙ ПОЛИМЕРИЗАЦИИ АЛЬФА-ОЛЕФИНОВ

Изобретение относится к способу газофазной полимеризации, осуществляемому в двух взаимосоединенных зонах полимеризации, в которые подаются один или более α-олефинов общей формулы СН2=СНR в присутствии катализатора в реакционных условиях и из которых выгружается полимерный продукт. В способе изобретения растущие полимерные частицы проходят через первую зону полимеризации в условиях быстрого псевдоожижения, выходят из указанной первой зоны и поступают во вторую зону полимеризации. Через вторую зону полимеризации они проходят в уплотненном виде под действием силы тяжести и повторно вводятся в первую зону полимеризации, создавая таким образом циркуляцию полимера через две зоны полимеризации. Способ позволяет полимеризовать олефины в газовой фазе с высокой продуктивностью на единицу объема реактора без проблем, связанных с технологией псевдоожиженного слоя. При этом достигается гибкость процесса, параметры могут быть оптимизированы на основе характеристик катализатора и продукта и не ограничиваются ...

УСТРОЙСТВО И СПОСОБ ГЛУБОКОГО КАТАЛИТИЧЕСКОГО КРЕКИНГА УГЛЕВОДОРОДНОГО СЫРЬЯ

Изобретения относятся к устройству и способу глубокого каталитического крекинга углеводородного сырья. Устройство содержит первую вертикальную секцию крекинга с радиусом х, вторую вертикальную секцию крекинга с радиусом у, вертикальную производственную трубу и разделительный сосуд. Величина отношения у:х имеет значение в интервале 1,1:1-5,0:1. В нижней части первой секции расположены средства подачи углеводородного сырья и средства подачи катализатора крекинга для селективного каталитического крекинга сырья в газолин. Вторая секция крекинга соединена с первой с помощью переходной секции с первым диаметром для селективного каталитического крекинга газолина, превращаемого в первой вертикальной секции в олефины. Вертикальная производственная труба имеет входящее отверстие, которое в рабочем состоянии соединено со второй вертикальной секцией крекинга с помощью переходной секции второго диаметра, и выходное отверстие, которое в рабочем состоянии соединено с приспособлениями для разделения катализатора ...

РЕАКТОРНАЯ СИСТЕМА И СПОСОБ ЕЕ ИСПОЛЬЗОВАНИЯ

Способ полимеризации олефинов включает: подачу олефина и катализатора полимеризации в реактор полимеризации с получением полиолефина, содержащий область с псевдоожиженным слоем, имеющую верхнюю и нижнюю части, и область с подвижным слоем, причем с одного своего конца область с подвижным слоем сообщается по текучей среде с верхней частью области с псевдоожиженным слоем, с другого своего конца область с подвижным слоем сообщается по текучей среде с нижней частью области с псевдоожиженным слоем, а диаметр области с псевдоожиженным слоем больше диаметра области с подвижным слоем; циркуляцию по меньшей мере части олефина, катализатора и полиолефина через область с псевдоожиженным слоем и область с подвижным слоем; поддержание псевдоожиженного слоя в плотнофазном состоянии в области с псевдоожиженным слоем; отвод полиолефина из области с псевдоожиженным слоем. Изобретение позволяет избежать образования таких явлений, как полимерные слои и поверхностные оболочки. 2 н. и 11 з.п. ф-лы, 3 табл., ...

ИНТЕГРИРОВАННЫЙ СПОСОБ ДЕГИДРИРОВАНИЯ C3-C4 УГЛЕВОДОРОДОВ

Изобретение относится к интегрированному способу получения олефинов С3-С4 или С4-диолефинов, включающему следующие стадии: (1)(а) приведение в контакт в реакторе дегидрирования с псевдоожиженным слоем (i) C3-C4-углеводородного сырья и (ii) потока катализатора, содержащего катализатор; в условиях, обеспечивающих образование смеси продуктов стадии (1)(а), содержащей целевой С3-С4-олефин или целевой С4-диолефин, водород и непрореагировавшее С3-С4-углеводородное сырье; и осаждение кокса на указанном катализаторе и по меньшей мере частичное дезактивирование указанного катализатора таким образом, что он образует по меньшей мере частично дезактивированный катализатор; и (b) перенос смеси продуктов стадии (1)(а) и указанного по меньшей мере частично дезактивированного катализатора из указанного реактора дегидрирования с псевдоожиженным слоем в систему циклонной сепарации и в условиях, обеспечивающих преобразование указанной смеси продуктов стадии (1)(а) с получением смеси продуктов стадии (1)(b ...

УСТРОЙСТВО С КИПЯЩИМ СЛОЕМ И СПОСОБ ПОЛУЧЕНИЯ ПАРА-КСИЛОЛА И СОВМЕСТНОГО ПОЛУЧЕНИЯ НИЗШИХ ОЛЕФИНОВ ИЗ МЕТАНОЛА И/ИЛИ ДИМЕТИЛОВОГО ЭФИРА И БЕНЗОЛА

Изобретение относится к устройству и способу получения пара-ксилола (РХ) и совместного получения низших олефинов. Представлен реактор с турбулентным кипящим слоем для получения пара-ксилола и совместного получения низших олефинов из метанола и/или диметилового эфира и бензола, причем указанный реактор с турбулентным кипящим слоем включает распределитель первого сырья для реактора и множество распределителей второго сырья для реактора, и распределитель первого сырья для реактора и множество распределителей второго сырья для реактора расположены последовательно снизу вверх в реакционной зоне реактора с турбулентным кипящим слоем; при этом количество распределителей второго сырья для реактора составляет от 2 до 10, при этом реактор с турбулентным кипящим слоем включает первый сепаратор твёрдой и газовой фаз реактора, при этом первый сепаратор твёрдой и газовой фаз реактора расположен в зоне разбавленной фазы или за пределами корпуса реактора, при этом первый сепаратор твердой и газовой фаз ...

УСТРОЙСТВО И СПОСОБ ПОЛУЧЕНИЯ ПАРА-КСИЛОЛА И СОВМЕСТНОГО ПОЛУЧЕНИЯ НИЗШИХ ОЛЕФИНОВ ИЗ МЕТАНОЛА И/ИЛИ ДИМЕТИЛОВОГО ЭФИРА И БЕНЗОЛА

Изобретение относится к реактору с быстрокипящим слоем для получения пара-ксилола и совместного получения низших олефинов из метанола и/или диметилового эфира и бензола, где нижняя часть реактора с быстрокипящим слоем представляет собой реакционную зону и верхняя часть реактора с быстрокипящим слоем представляет собой зону разбавленной фазы. При этом указанный реактор с быстрокипящим слоем включает корпус реактора, распределитель первого сырья для реактора и множество распределителей второго сырья для реактора, при этом и указанный распределитель первого сырья для реактора и указанное множество распределителей второго сырья для реактора расположены последовательно снизу вверх в реакционной зоне. Также указанный реактор с быстрокипящим слоем включает первый сепаратор твердой и газовой фаз реактора, при этом указанный первый сепаратор твердой и газовой фаз реактора расположен в зоне разбавленной фазы или за пределами корпуса реактора. Причем указанный первый сепаратор твердой и газовой фаз ...

ПЕРЕРАБОТКА РАЗЛИЧНЫХ ТИПОВ ИСХОДНОГО СЫРЬЯ В УСТАНОВКЕ ДЛЯ КАТАЛИТИЧЕСКОГО КРЕКИНГА С ПСЕВДООЖИЖЕННЫМ СЛОЕМ КАТАЛИЗАТОРА

... 1. Способ каталитического крекинга с псевдоожиженным слоем катализатора, предназначенный для увеличения выходов С3 и С4 углеводородов, включающий: (а) ввод основного исходного сырья, содержащего углеводороды, характеризующиеся температурами кипения в диапазоне от 400°F (204°С) до 1150°F (621°С), в реактор с восходящим потоком аппаратуры каталитического крекинга с псевдоожиженным слоем катализатора через комплект инжекторов для основного исходного сырья и (b)ввод легкого исходного сырья, содержащего углеводороды, характеризующиеся температурами кипения, которые не превышают приблизительно 440°F (227°С), в упомянутую аппаратуру каталитического крекинга с псевдоожиженным слоем катализатора через множество инжекторов для легкого исходного сырья, на технологической схеме расположенных до упомянутых инжекторов для основного исходного сырья, поблизости от позиций, в которых поток катализатора изменяет направление. 2. Способ по п.1, где упомянутое легкое исходное сырье вводят в канальную часть ...

УСТРОЙСТВО С КИПЯЩИМ СЛОЕМ И СПОСОБ ПОЛУЧЕНИЯ ПАРА-КСИЛОЛА И СОВМЕСТНОГО ПОЛУЧЕНИЯ НИЗШИХ ОЛЕФИНОВ ИЗ МЕТАНОЛА И/ИЛИ ДИМЕТИЛОВОГО ЭФИРА И БЕНЗОЛА

Изобретение относится к устройству и способу получения пара-ксилола (РХ) и совместного получения низших олефинов. Представлен реактор с турбулентным кипящим слоем для получения пара-ксилола и совместного получения низших олефинов из метанола и/или диметилового эфира и бензола, причем указанный реактор с турбулентным кипящим слоем включает распределитель первого сырья для реактора и множество распределителей второго сырья для реактора, и распределитель первого сырья для реактора и множество распределителей второго сырья для реактора расположены последовательно снизу вверх в реакционной зоне реактора с турбулентным кипящим слоем; при этом количество распределителей второго сырья для реактора составляет от 2 до 10, при этом реактор с турбулентным кипящим слоем включает первый сепаратор твёрдой и газовой фаз реактора, при этом первый сепаратор твёрдой и газовой фаз реактора расположен в зоне разбавленной фазы или за пределами корпуса реактора, при этом первый сепаратор твердой и газовой фаз ...

УСТРОЙСТВО ВЫВОДА СЫПУЧЕГО КАТАЛИЗАТОРА И СПОСОБЫ ЕГО ИСПОЛЬЗОВАНИЯ

ГАЗОФАЗНАЯ ПОЛИМЕРИЗАЦИЯ АДЬФА-ОЛЕФИНА

... 1. Способ газофазной полимеризации альфа-олефина, включающий стадии:подачи циркуляционного газа, содержащего один или большее число альфа-олефинов и инертный газ, в реактор полимеризации;полимеризации альфа-олефина до полиолефина в двух разделенных зонах полимеризации в реакторе полимеризации иудаления полученного полиолефина из реактора полимеризации,в котором реактор полимеризации разделен на две зоны полимеризации отводной трубой и внутренняя часть отводной трубы формирует стояк, в котором растущие полимеры полиолефина поднимаются при быстром псевдоожижении, а внешняя часть отводной трубы образует кольцевой зазор, в котором полимеры полиолефина, прошедшие по стояку опускаются под действием гравитации, и полимеры полиолефина, прошедшие кольцевой зазор, снова вводятся в нижнюю часть стояка так, что полимеры полиолефина полимеризуются во время циркуляции между стояком и кольцевым зазором.2. Способ газофазной полимеризации по п.1, в котором циркуляционный газ подают в нижнюю часть отводной ...

СИСТЕМНЫЕ КОМПОНЕНТЫ СИСТЕМ РЕАКТОРА С ПСЕВДООЖИЖЕННЫМ КАТАЛИЗАТОРОМ

КОЛОННЫ ПОДАЧИ ОТРАБОТАВШЕГО КАТАЛИЗАТОРА

УСТРОЙСТВО И СПОСОБ ГЛУБОКОГО КАТАЛИТИЧЕСКОГО КРЕКИНГА УГЛЕВОДОРОДНОГО СЫРЬЯ

... 1. Устройство для каталитического крекинга углеводородного сырья, включающее: (a) первую более узкую вертикальную реакторную секцию с радиусом х, средства подачи углеводородного сырья и средства подачи катализатора крекинга, расположенные в нижней части секции; (b) вторую более широкую вертикальную реакторную секцию с радиусом у, причем величина отношения у:х имеет значение в интервале 1,1:1-5,0:1, соединенную с указанной первой более узкой вертикальной реакторной секцией с помощью переходной секции с первым диаметром; (c) вертикальную производственную трубу, входящее отверстие которой в рабочем состоянии соединено со второй расширенной вертикальной реакторной секцией с помощью переходной секции второго диаметра, а выходное отверстие которой в рабочем состоянии соединено с приспособлениями для разделения катализатора и продуктов крекинга; и (d) разделительный сосуд, содержащий верхнюю разреженную фазу и плотную нижнюю фазу, причем верхняя разреженная фаза предназначена для приема газообразных ...

APPARATUR ZUR BEHANDLUNG VON PARTIKELFÖRMIGEM GUT

Katalytisches Verfahren zur Herstellung von Olefinen

Verfahren und Vorrichtung zum katalytischen Cracken von Kohlenwasserstoffen

Method for transferring subdivided solids

... 917,793. Proportionate mixing of solids with liquids. PHILLIPS PETROLEUM CO. March 9, 1961 [March 28, 1960], No. 8624/61. Class 86. [Also in Group XXVIII] In a method for transferring subdivided solids, e.g. a catalyst, a wet compacted mass of the solids is formed in a confined zone 22 and then forced upwardly by fluid-pressure, via a conduit 47, into a stream of liquid 42 flowing at an angle to the flow of the solids, so as to form a slurry. A contact-flow orifice 44 is provided in liquid conduit 42. The flow of forcing fluid is regulated by a valve 49. Specifications 790,195 and 845,319 are referred to.

Catalytic cracking of hydrocarbon oils

... Hydrocarbon oils such as gas oil are cracked by passing a suspension of hot catalyst particles in the hydrocarbon vapours upwards through a reactor 10 at a velocity of at least 6 feet per second and separating the cracked products from the spent catalyst. The carbonaceous deposit is burned off the spent catalyst by passing it with oxygen-containing gas through regenerator 40 at a velocity of at least 6 feet per second; a major proportion of the hot regenerated catalyst is recycled to the inlet of the regenerator, and the remainder is mixed with fresh hydrocarbon feed flowing to the reactor. Because the hydrocarbon vapours expand in volume as cracking proceeds, reactor 10 is made in the shape of a slender inverted cone. The catalyst may be synthetic silica-alumina, silica-magnesia boria-alumina or natural clay, and preferably has a particle size of 20 to 100 microns. Gas oil, preheated to about 675 DEG F., is introduced into the system through conduit 13, and is vaporized ...

An improved process for the catalytic treatment of hydrocarbon oils

... 548,134. Catalytic conversion of hydrocarbon oils. KELLOGG CO., M. W. March 12, 1940, No. 4629. Convention date, May 20, 1939. [Classes 1 (i) and 32] In processes for the catalytic conversion of hydrocarbon oils of the kind in which the catalyst is passed in suspension in the hydrocarbon vapours through the reaction zone, and after separation therefrom regenerated by passage in suspension in an oxygen-containing gas through a regenerating zone and returned to the reaction zone, the catalyst and hydrocarbons are fed through the reaction zone in such proportions that at least half the heat generated in the regeneration zone is absorbed by the catalyst, the ratio by weight of catalyst to hydrocarbons passed through the reaction zone being maintained in conformity with the formula where C represents the fraction of charged hydrocarbon converted to form carbonaceous deposit on the catalysts; H, the heat of combustion of the carbonaceous material in B.T.U.s per lb.; S, the specific heat of the ...

PARTICULATE SOLIDS REGENERATION

PRODUCTION OF VINYL CHLORIDE

... 1,256,245. Oxychlorination catalysts; separating gas mixtures by absorption; cooling fluidised bed. PRINCETON CHEMICAL RESEARCH Inc. 25 Oct., 1968 [27 Dec., 1967; 10 June, 1968 (2)], No. 50892/68. Headings BIE, B1F; B1L and B1X. [Also in Divisions C2 and C5] Oxychlorination catalysts comprise an iron oxide and (a) at least one Group IIIA, Group IV A, Rare Earth or Actinide metal oxide, and (b) at least one Group I or II metal oxide. The catalysts may be supported on conventional carriers, e.g. diatomaceous earth, quartz, silica glass, alumina, pumice, silica gel, mullite or silicon carbide, and prepared by impregnation with a soluble salt followed by its decomposition, or may be unsupported and prepared by pelletising or other agglomerating techniques, or by spray drying. The separation of organic chlorides and hydrogen chloride from an ethylene-containing gas stream is effected by scrubbing the stream with liquid dimethyl formamide. Apparatus for conducting a fluidised bed oxychlorination ...

Wirbelschichtreaktorsystem

Die Erfindung betrifft ein Wirbelschichtreaktorsystem, umfassend einen oder mehrereWirbelschichtreaktoren (1, 2, 20) zur Durchführung chemischer oder physikalischerReaktionen, wovon zumindest ein Reaktor als schnell fluidisierter Reaktor zum Betriebals zirkulierende Wirbelschicht ausgeführt ist und am oberen Ende einen Fluidauslass(5, 6), einen Partikelabscheider (3, 4) und eine damit verbundene Partikelleitung(7, 8) zur Rückführung abgeschiedener Wirbelschichtpartikel in denselben odereinen weiteren Reaktor umfasst, wobei in zumindest einem schnell fluidisiertenReaktor ein oder mehrere Strömungsregler (18, 21) vorgesehen sind, um darin voneinandergetrennte Reaktionszonen (9, 10, 22) zu erzeugen, mit dem Kennzeichen,dass zur Regelung der Strömungsverhältnisse in den Reaktionszonen (9, 10, 22)einer oder mehrere der Strömungsregler (18, 21) von außerhalb des Systems gezieltverstellbar ist/sind. The invention relates to a fluidized-bed reactor system comprising one or more fluidized-bed reactors (1, 2, 20) for carrying out chemical reactions, at least one reactor being designed as a rapidly fluidized reactor for operation as a circulating fluidized bed and having a fluid outlet (5, 6) at the top Particle separator (3, 4) and associated particle line (7, 8) for recycling deposited fluidized bed particles into the same or a further reactor, wherein in at least one fast fluidized reactor one or more flow regulators (18, 21) are provided for separating reaction zones (18, 21) therebetween. 9, 10, 22), with the characteristic that for controlling the flow conditions in the reaction zones (9, 10, 22) one or more of the flow regulators (18, 21) is / are selectively adjustable from outside the system.

EQUIPMENT FOR THE TREATMENT OF PARTIKELFÖRMIGEM PROPERTY

Process and apparatus for mixing two streams of catalyst

A process and apparatus for mixing streams of regenerated and carbonized catalyst involves passing a catalyst stream into and out of a chamber in a lower section of a riser. The chamber fosters mixing of the catalyst streams to reduce their temperature differential before contacting hydrocarbon feed.

PROCESSES AND SYSTEMS FOR USING SILICA PARTICLES IN FLUID BED REACTOR

The present disclosure relates to fluid bed processes that utilize silica particles as a fluidization aid. The process comprises reacting one or more reactants in a reactor comprising a fluid bed to form a product. The fluid bed comprises a catalyst composition comprising a catalyst and an inert additive composition comprising silica particles from 0.5 wt % to 30 wt %, based on the total weight of the catalyst composition. The silica particles are discrete, inert particles that are mixed with the catalyst in the fluid bed. 1. A process comprising:reacting one or more reactants in a reactor comprising a fluid bed to form a product;wherein the fluid bed comprises a catalyst composition comprising a catalyst and an inert additive composition comprising from 0.5 wt % to 30 wt % of silica particles, based on the total weight of the catalyst composition,wherein the silica particles have an equivalent median particle diameter ranging from 10 microns to 500 microns.2. The process of claim 1 , wherein the catalyst comprises one or more of antimony claim 1 , uranium claim 1 , iron claim 1 , bismuth claim 1 , vanadium claim 1 , molybdenum claim 1 , nickel claim 1 , potassium claim 1 , cobalt claim 1 , oxides thereof claim 1 , or salts thereof.3. The process of claim 1 , wherein the catalyst has an equivalent median diameter ranging from 1 microns to 125 microns.4. The process of claim 1 , wherein the silica particles have a real density ranging from 1.8 g/cmto 2.8 g/cm claim 1 , and wherein the difference between the density of the silica particles and the catalyst is less than 75%.5. The process of claim 1 , wherein the silica particles have a surface area less than 50 m/g claim 1 , and wherein the silica particles have a hardness ranging from 500 to 720 as measured by ASTM E384 (2018).6. The process of claim 1 , wherein the silica particles have a sphericity ranging from 60% to 99.9%7. The process of claim 1 , wherein the catalyst composition further comprises alumina ...

FLUID CATALYTIC CRACKING PROCESSES AND APPARATUS

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

PROCESS AND APPARATUS FOR REACTING FEED WITH A FLUIDIZED CATALYST OVER A TEMPERATURE PROFILE

A fluidized catalytic reactor utilizes an ascending temperature profile. The apparatus and process deliver cooler spent catalyst to a first catalyst distributor and a hotter regenerated catalyst to a second catalyst distributor that are spaced apart from each other. The reactant stream first encounters the first stream of catalyst and then encounters the second stream of catalyst. The process and apparatus stage the addition of hot catalyst to the reactant stream. The process and apparatus may be particularly advantageous in an endothermic reaction because the hotter catalyst will encounter reactants that have cooled due to the progression of endothermic reactions. 1. A reactor for contacting a reactant stream with a catalyst comprising:a reactant distributor for distributing the reactant stream to the reactor;a first catalyst inlet for feeding a first stream of catalyst to the reactor;a second catalyst inlet for feeding a second stream of catalyst to the reactor, the first catalyst inlet being closer to the reactant distributor than the second catalyst inlet;a product outlet for discharging product from the reactor, the second catalyst distributor being closer to the reactant distributor than the product outlet.2. The reactor of further comprising a regenerated catalyst pipe connected to said second catalyst inlet claim 1 , the regenerated catalyst pipe having an inlet connected to a catalyst regenerator.3. The reactor of further comprising a reaction chamber containing said first catalyst inlet and said second catalyst inlet and a separation chamber comprising a primary catalyst separator for separating catalyst from product gases claim 1 , said primary catalyst separator being located closer to the second catalyst inlet than the product outlet.4. The reactor of further comprising a recycle catalyst pipe connected to said first catalyst inlet claim 3 , the recycle catalyst pipe having an inlet in the separation chamber.5. The reactor of further comprising a ...

Multiple Reactor and Multiple Zone Polyolefin Polymerization

Apparatuses and processes that produce multimodal polyolefins, and in particular, polyethylene resins, are disclosed herein. This is accomplished by using two reactors in series, where one of the reactors is a multi-zone circulating reactor that can circulate polyolefin particles through two polymerization zones optionally having two different flow regimes so that the final multimodal polyolefin has improved product properties and improved product homogeneity. 1. A trimodal polyethylene resin having a low molecular weight (LMW) component , an intermediate molecular weight (IMW) component , and a high molecular weight (HMW) component; wherein the LMW component is present in an amount of from about 20 wt. % to about 75 wt. %; wherein the IMW component is present in an amount of from about 5 wt. % to about 40 wt. %; wherein the LMW component has a weight average molecular weight of from about 20 kg/mol to about 150 kg/mol; wherein the IMW component has a weight average molecular weight of from about 85 kg/mol to about 350 kg/mol; wherein the weight average molecular weight of the IMW component is greater than the weight average molecular weight of the LMW component; wherein the weight average molecular weight of the HMW component is greater than the weight average molecular weight of the IMW component; wherein the trimodal polyethylene resin has a Young's modulus (E) of equal to or greater than about 900 MPa , when tested in accordance with ASTM D638; and wherein the trimodal polyethylene resin has a density of equal to or greater than about 0.952 g/cc , when tested in accordance with ASTM D1505.2. The trimodal polyethylene resin of claim 1 , wherein the trimodal polyethylene resin has a melt index of less than about 1 g/10 min claim 1 , when tested in accordance with ASTM D1238 under a force of 2.16 kg.3. The trimodal polyethylene resin of claim 1 , wherein the trimodal polyethylene resin has a density of equal to or greater than about 0.955 g/cc claim 1 , when tested ...

Fluidized bed reactor and process for producing olefins from oxygenates

The present invention provides a fluidized bed reactor and its use for producing olefins from oxygenates, the fluidized bed reactor comprises: a reaction zone located in the lower portion of the fluidized bed reactor and comprising a lower dense phase zone and an upper riser, wherein the dense phase zone and the riser are connected with each other transitionally; a separation zone located in the upper portion of the fluidized bed reactor and comprising a settling chamber, a fast gas-solid separation means, a cyclone and a gas collecting chamber, wherein the riser extends upwardly into the separation zone and is connected at its outlet with the inlet of the fast gas-solid separation means, the fast gas-solid separation means is connected at its outlet with the inlet of the cyclone via a fast gas passage, the cyclone is connected at its outlet with the gas collecting chamber, and the gas collecting chamber is located below the reactor outlet and connected therewith; and a catalyst recycle line for recycling the catalyst from the settling chamber back to the dense phase zone, a catalyst withdrawl line for withdrawing the deactivated catalyst from the settling chamber and/or the dense phase zone to the catalyst regeneration means, and a catalyst return line for returning the regenerated catalyst from the catalyst regeneration means to the dense phase zone.

CONVERSION OF A CRUDE OIL IN A FLUIDISED BED COMPRISING ZONES WITH DIFFERENT CONTACT TIMES

The present invention relates to a device and to a process for the fluidized bed catalytic cracking of a hydrocarbon feedstock, in which: a first feedstock () is cracked in a dense fluidized bed reactor () in the presence of a catalyst () to produce a first effluent; and at least one second feedstock () is cracked in a transport fluidized bed reactor () in the presence of the catalyst () supplied by the dense fluidized bed reactor () to produce a second effluent, the second feedstock () being a heavier feedstock than the first feedstock (). 112334. A device for the fluidized bed catalytic cracking of a hydrocarbon feedstock , comprising: a dense fluidized bed reactor () suitable for at least partially cracking a first hydrocarbon feedstock () in the presence of a catalyst () to produce a first effluent , and at least partially feeding with catalyst () a transport fluidized bed reactor (); and{'b': 4', '10', '3, 'the transport fluidized bed reactor () suitable for at least partially cracking at least one second hydrocarbon feedstock () in the presence of the catalyst () to produce a second effluent,'}{'b': 10', '2, 'the second hydrocarbon feedstock () being a heavier feedstock than the first hydrocarbon feedstock ().'}21443. The device as claimed in claim 1 , in which the dense fluidized bed reactor () is directly connected to the transport fluidized bed reactor () in order to directly feed the transport fluidized bed reactor () with catalyst ().31. The device as claimed in claim 1 , in which the dense fluidized bed reactor () is an ebullating or turbulent fluidized bed reactor.44. The device as claimed in claim 1 , in which the transport fluidized bed reactor () is an upward or downward gas-solid cocurrentwise fluidized bed reactor.54. The device as claimed in claim 1 , in which the transport fluidized bed reactor () is an upward gas-solid cocurrentwise fluidized bed reactor.614. The device as claimed in claim 1 , in which the dense fluidized bed reactor () is ...

DEVICE AND METHOD FOR PREPARING PARA-XYLENE AND CO-PRODUCING LIGHT OLEFINS FROM METHANOL AND/OR DIMETHYL ETHER AND BENZENE

A fast fluidized bed reactor, device and method for preparing para-xylene and co-producing light olefins from methanol and/or dimethyl ether and benzene, resolving or improving the competition problem between an MTO reaction and an alkylation reaction during the process of producing para-xylene and co-producing light olefins from methanol and/or dimethyl ether and benzene, and achieving a synergistic effect between the MTO reaction and the alkylation reaction. By controlling the mass transfer and reaction, competition between the MTO reaction and the alkylation reaction is coordinated and optimized to facilitate a synergistic effect of the two reactions, so that the conversion rate of benzene, the yield of para-xylene, and the selectivity of light olefins are increased. 124-. (canceled)25. A fast fluidized bed reactor for preparing para-xylene and co-producing light olefins from methanol and/or dimethyl ether and benzene , wherein the fast fluidized bed reactor comprises a first reactor feed distributor and a plurality of second reactor feed distributors , the first reactor feed distributor and the plurality of second reactor feed distributors are sequentially arranged along the gas flow direction in the fast fluidized bed reactor.26. The fast fluidized bed reactor of claim 25 , wherein the number of the second reactor feed distributors is in a range from 2 to 10.27. The fast fluidized bed reactor of claim 25 , wherein the fast fluidized bed reactor comprises a first reactor gas-solid separator and a second reactor gas-solid separator claim 25 , the first reactor gas-solid separator is placed in a dilute phase zone or outside a reactor shell claim 25 , and the second reactor gas-solid separator is placed in the dilute phase zone or outside the reactor shell;the first reactor gas-solid separator is provided with a regenerated catalyst inlet, a catalyst outlet of the first reactor gas-solid separator is placed at the bottom of a reaction zone, and a gas outlet of the ...

BULK CATALYST WITHDRAWAL SYSTEM AND METHODS FOR THE USE THEREOF

A method for processing a chemical stream includes contacting a feed stream with a catalyst in a reactor portion of a reactor system causing a reaction which forms a product stream. The method includes separating the product stream from the catalyst, passing the catalyst to a catalyst processing portion of the reactor system, processing the catalyst in the catalyst processing portion, and passing a portion of the catalyst from the catalyst processing portion of the reactor system into a catalyst withdrawal system that includes a catalyst withdrawal vessel and a transfer line coupling the catalyst withdrawal vessel to the catalyst processing portion. Each of the catalyst withdrawal vessel and the transfer line include an outer metallic shell and an inner refractory lining. The method further includes cooling the catalyst in the catalyst withdrawal vessel from greater than or equal to 680° C. to less than or equal to 350° C. 1. A method for processing a chemical stream , the method comprising:contacting a feed stream with a catalyst in a reactor portion of a reactor system, wherein the reactor system comprises the reactor portion and a catalyst processing portion and the contacting of the feed stream with the catalyst causes a reaction which forms a product stream;passing the catalyst to the catalyst processing portion of the reactor system;processing the catalyst in the catalyst processing portion of the reactor system;passing at least a portion of the catalyst from the catalyst processing portion of the reactor system into a catalyst withdrawal system comprising a catalyst withdrawal vessel and a transfer line coupling the catalyst withdrawal vessel to the catalyst processing portion, each of the catalyst withdrawal vessel and the transfer line comprising an outer metallic shell and an inner refractory lining; andcooling the catalyst in the catalyst withdrawal vessel from greater than or equal to 680° C. to less than or equal to 350° C.2. The method of claim 1 , ...

MINIMIZING COKE FORMATION IN A REACTOR STRIPPER

The presently disclosed subject matter relates to systems and methods for catalyst regeneration. In particular, the presently disclosed subject matter provides for an integrated fluidized bed reactor and catalyst regeneration system to minimize hydrocarbon accumulation. In one embodiment, the presently disclosed subject matter provides for a fluidized bed reactor unit including a catalyst riser having a partially perforated surface in close proximity to a reactor stripper. 1. A catalyst reaction and regenerator system , comprising:a fluidized bed reactor comprising: 'a reactor stripper in close proximity to the partially perforated surface of the catalyst riser; and', 'a catalyst riser having a partially perforated surface; and'}a catalyst regenerator having at least two transfer lines to the fluidized bed reactor.2. The system of claim 1 , wherein one of the transfer lines connects the catalyst riser to the catalyst regenerator.3. The system of claim 1 , wherein one of the two transfer lines connects the reactor stripper and the catalyst regenerator.4. The system of claim 1 , wherein the perforated surface of the catalyst riser does not allow more than about 5% to about 10% of a catalyst to flow inside the catalyst riser from the reactor stripper.5. The system of claim 1 , wherein the partially perforated surface of the catalyst riser minimizes coke formation.6. The system of claim 1 , wherein the system further comprises a second reactor.7. The system of claim 6 , wherein the second reactor is connected to the fluidized bed reactor by a transfer line.8. A method of regenerating catalyst claim 6 , comprising: generating a chemical product in the presence of a catalyst in the catalyst riser;', 'separating the chemical product from the catalyst in the catalyst riser;', 'feeding the catalyst from the catalyst riser to the reactor stripper;', 'transferring the catalyst from the reactor stripper to a catalyst regenerator through a transfer line; and, 'feeding a ...

FLUIDIZED BED DEVICE AND METHOD FOR PREPARING PARA-XYLENE AND CO-PRODUCING LIGHT OLEFINS FROM METHANOL AND/OR DIMETHYL ETHER AND BENZENE

A turbulent fluidized bed reactor, device and method for preparing para-xylene and co-producing light olefins from methanol and/or dimethyl ether and benzene, resolving or improving the competition problem between an MTO reaction and an alkylation reaction during the process of producing para-xylene and co-producing light olefins from methanol and/or dimethyl ether and benzene, and achieving a synergistic effect between the MTO reaction and the alkylation reaction. By controlling the mass transfer and reaction, competition between the MTO reaction and the alkylation reaction is coordinated and optimized to facilitate a synergistic effect of the two reactions, so that the conversion rate of benzene, the yield of para-xylene, and the selectivity of light olefins are increased. The turbulent fluidized bed reactor includes a first reactor feed distributor and a number of second reactor feed distributors; the first reactor feed distributor and the plurality of second reactor feed distributions are sequentially arranged. 126-. (canceled)27. A turbulent fluidized bed reactor for preparing para-xylene and co-producing light olefins from methanol and/or dimethyl ether and benzene , the turbulent fluidized bed reactor comprising a first reactor feed distributor and a plurality of second reactor feed distributors , the first reactor feed distributor and the plurality of second reactor feed distributors are sequentially arranged along the gas flow direction in the turbulent fluidized bed reactor; andthe number of the second reactor feed distributors is in a range from 2 to 10.28. The turbulent fluidized bed reactor of claim 27 , the turbulent fluidized bed reactor further comprises a first reactor gas-solid separator and a second reactor gas-solid separator claim 27 , the first reactor gas-solid separator is placed in a dilute phase zone or outside a reactor shell claim 27 , and the second reactor gas-solid separator is placed in the dilute phase zone or outside the reactor ...

THERMOLYTIC FRAGMENTATION OF SUGARS

A process for large scale and energy efficient product on of oxygenates from sugar is disclosed in which a sugar feedstock is introduced into a thermolytic fragmentation reactor comprising a fluidized stream of heat carrying particles. The heat carrying particles may be separated from the fluidized stream prior to cooling the fragmentation product and may be directed to a reheater to reheat the particles and recirculate the heated particles to the fragmentation reactor. 1. A process for thermolytic fragmentation of a sugar into C-Coxygenates , said process comprising the steps of:a. providing particles carrying heat and suitable for fluidization;b. providing a fluidized bed fragmentation reactor comprising a riser and suitable for conducting thermolytic fragmentation and suitable for fluidizing a stream of particles;c. providing a feedstock solution comprising a sugar;d. introducing the particles into the reactor at a rate sufficient to maintain a temperature of at least 250° C., such as at least 300 350, 400 or 450° C., after the thermolytic fragmentation has taken place, and sufficient to obtain a fluidized stream of particles;e. introducing the feedstock into the fluidized stream of particles to obtain thermolytic fragmentation of the sugar to produce a particle dense fragmentation product; thenf. separating a fraction of the particles from the particle dense fragmentation product to produce a particle lean fragmentation product;g. quenching the particle lean fragmentation product at least 50° C. such that from introducing the feedstock into the particle containing fluidization stream to the quench is performed, the mean residence time of the gas is maximum 5, such as maximum 3 seconds, such as maximum 2, 1, 0.8 or 0.6 seconds;h. recovering the crude fragmentation product,i. transferring the particles separated in step f) to a reheater for heating; andj. recirculating the heated particles to the fragmentation reactor.2. The process according to claim 1 , wherein ...

APPARATUSES FOR DEHYDROGENATION OF ALKANES

The present disclosure relates to circulating fluidized bed apparatuses for dehydrogenation of alkanes to alkenes with higher yield and selectivity. The apparatus includes a riser-type reactor, a separator section, a regenerator and a withdrawal well disposed downstream to the regenerator. The apparatus includes a transfer line to receive hot regenerated catalyst free of oxygen from the withdrawal well, and to pre-treat the catalyst with a reducing gas to regulate-oxidation state of metals on the catalyst before reintroducing the catalyst to the riser-type reactor. The transfer line is formed in an elongated U-shaped pipe such that the oxidation state of the metals on the catalyst is regulated by the time the pre-treated catalyst reaches the bottom of the riser-type reactor. 1. A circulating fluidized bed apparatus for dehydrogenation of alkanes comprising a riser-type reactor , a separator coupled to the riser-type reactor , a regenerator coupled to the separator and a withdrawal well disposed downstream to the regenerator , and a transfer line connecting the withdrawal well with the riser-type reactor , the transfer line adapted to:receive hot regenerated catalyst free of oxygen from the withdrawal well; andpre-treat the catalyst with a reducing gas to regulate the oxidation state of metals on the catalyst before reintroducing the catalyst to the bottom of the riser-type reactor, wherein the transfer line is formed in an elongated U-shaped pipe such that the oxidation state of the metals on the catalyst is regulated by the time the catalyst reaches the bottom of the riser-type reactor.2. The circulating fluidized bed apparatus as claimed in claim 1 , wherein the riser-type reactor is adapted to accommodate a pre-heated alkane feed stream and a catalyst for dehydrogenation reaction.3. The circulating fluidized bed apparatus as claimed in claim 1 , wherein the separator comprising:a riser termination device for disengaging the catalyst and hydrocarbons;a set of ...

SINGLE AND MULTIPLE TURBULENT/FAST FLUIDIZED BED REACTORS IN NCC PROCESS FOR MAXIMIZING AROMATICS PRODUCTION

Systems and methods for producing aromatics are disclosed. A feed stream comprising naphtha is flowed into a reaction unit comprising a fast fluidized bed reactor coupled to and in fluid communication with a riser reactor. The fast fluidized bed reactor is adapted to enable backmixing therein to maximize the production of aromatics. The effluent from the fast fluidized bed reactor is further flowed to the riser reactor. The lift gas, which can comprise nitrogen, methane, flue gas, or combinations thereof, is injected in the reaction unit via a sparger. The effluent of the riser reactor is separated in a product separation unit to produce a product stream comprising light olefins and spent catalyst. The spent catalyst is further stripped by a stripping gas comprising methane, nitrogen, flue gas, or combinations thereof. The stripped spent catalyst is regenerated to produce regenerated catalyst, which is subsequently flowed to the fast fluidized bed reactor. 1. A method of producing an aromatic , the method comprising:contacting, in a fast fluidized bed reactor, naphtha with catalyst particles of a fast-fluidized bed having a superficial gas velocity (SGV) in a range of 1 to 6.5 m/s and under first reaction conditions sufficient to produce a first product comprising one or more aromatics;flowing effluent of the fast fluidized bed reactor to a riser reactor, the effluent of the fast fluidized bed reactor comprising (1) unreacted hydrocarbons of the naphtha, (2) the first product, and (3) the catalyst particles; andcontacting, in the riser reactor, the unreacted hydrocarbons of the naphtha, the first product, and the at least some of the catalyst particles under second reaction conditions sufficient to produce a second product comprising one or more aromatics.2. The method of claim 1 , wherein the first reaction conditions include a reaction temperature in the fast fluidized bed reactor of 690 to 710° C.3. The method of claim 1 , wherein the first reaction conditions ...

Method and synthesis reactor for producing carbon nanotubes

A synthesis reactor for producing carbon nanotubes. The reactor includes a main reactor, a feeder, a settler, an air inlet device, and a product outlet. The main reactor communicates with the settler in the form of a communicating vessel. The feeder communicates with the settler via a catalyst inlet. The air inlet device is disposed under the settler. The wall of the main reactor is provided with a heat exchanger. The product outlet is disposed at the lower part of the main reactor. A method for producing a carbon nanotube, includes: 1) drying red mud for 1 to 4 hour(s) at the temperature of between 101° C. and 109° C.; 2) smashing and sieving the red mud through a 200-mesh sieve to yield a catalyst; and 3) adding the catalyst to a synthesis reactor.

SYSTEM AND METHOD FOR PRODUCING CARBON NANOTUBES

In the present invention, only low-growth carbon nanotubes are selectively separated among solid particles discharged during a reaction and then re-input to a reactor, so that it is possible to improve the quality of a carbon nanotube product to be produced and the productivity of a carbon nanotube production process. 1. A system for producing carbon nanotubes , the system comprising:a fluidized bed reactor provided with an internal space in which a carbon nanotube synthesis reaction is performed and a discharge unit for discharging a mixed gas containing solid particles;a separation unit for receiving the mixed gas connected to the discharge unit and for separating the solid particles in the mixed gas according to the particle diameter thereof; anda re-input unit for re-inputting carbon nanotubes having a particle diameter of equal to or less than a predetermined particle diameter among the particles separated at the separation unit to the fluidized bed reactor.2. The system of claim 1 , wherein the discharge unit is provided on an upper portion of the fluidized bed reactor.3. The system of claim 1 , wherein the separation unit comprises a filter whose pore diameter is the predetermined particle diameter.4. The system of claim 1 , wherein the separation unit is positioned lower than the discharge unit of the fluidized bed reactor.5. The system of claim 1 , wherein the system is operated batchwise or continuously.6. A method for producing carbon nanotubes claim 1 , the method comprising:(S1) reacting a catalyst and a reaction gas containing a carbon source gas and a flowing gas in a fluidized bed reactor to obtain carbon nanotube solid particles;(S2) collecting a mixed gas discharged out of the reactor during Step S1 into a separation unit provided outside the fluidized bed reactor and separating the solid particles in the mixed gas; and{'sup': '3', '(S3) separating the separated solid particles according to the size thereof, and re-inputting particles having a ...

PROCESS AND APPARATUS FOR REGENERATING CATALYST WITH SUPPLEMENTAL FUEL

Higher temperature regenerated dehydrogenation catalyst is mixed with the lower temperature spent dehydrogenation catalyst from a dehydrogenation reaction to heat the spent catalyst. Air or other oxygen containing gas may be introduced to facilitate mixing. The mixing of hot regenerated catalyst with cooler spent catalyst increases the temperature of the spent catalyst and makes the coke on catalyst and in the supplemental fuel gas instantly ready to combust without the delay necessary to heat up the spent catalyst to combustion temperature. The regenerated dehydrogenation catalyst may be mixed with the spent dehydrogenation catalyst before the mixture of catalyst is contacted with the supplemental fuel gas. Combustion with fuel gas should be conditioned to avoid generation of a flame. 1. A catalyst regenerator for a catalytic dehydrogenation process comprising:a mixing chamber including a spent catalyst pipe inlet and a regenerated catalyst pipe inlet for mixing spent catalyst and regenerated catalyst together;an oxygen supply gas distributor for distributing an oxygen supply gas to the catalyst;a combustion chamber in which coke is combusted from said spent catalyst in the presence of oxygen; anda fuel distributor for distributing fuel gas to the regenerator for combustion in the combustion chamber.2. The catalyst regenerator of further comprising a mixing tube in said mixing chamber to facilitate mixing between said spent catalyst claim 1 , said regenerated catalyst.3. The catalyst regenerator of further comprising an opening in a lateral wall of said tube.4. The catalyst regenerator of wherein the opening in said tube is coterminous with one of the spent catalyst pipe inlet and the regenerated catalyst pipe inlet.5. The catalyst regenerator of further comprising a fuel distribution section that comprises fuel injectors penetrating through a wall of said regenerator.6. The catalyst regenerator wherein said fuel distributor is in said regenerated catalyst pipe.7. ...

FLUIDIZED BED DEVICE AND METHOD FOR PREPARING PARA-XYLENE AND CO-PRODUCING LIGHT OLEFINS FROM METHANOL AND/OR DIMETHYL ETHER AND TOLUENE

A turbulent fluidized bed reactor, device and method for preparing para-xylene and co-producing light olefins from methanol and/or dimethyl ether and toluene, resolving or improving the competition problem between an MTO reaction and an alkylation reaction during the process of producing para-xylene and co-producing light olefins from methanol and/or dimethyl ether and toluene, and achieving a synergistic effect between the MTO reaction and the alkylation reaction. By controlling the mass transfer and reaction, competition between the MTO reaction and the alkylation reaction is coordinated and optimized to facilitate a synergistic effect of the two reactions, so that the conversion rate of toluene, the yield of para-xylene, and the selectivity of light olefins are increased. The turbulent fluidized bed reactor includes a first reactor feed distributor and a number of second reactor feed distributors and are arranged sequentially along the gas flow direction. 126-. (canceled)27. A turbulent fluidized bed reactor for preparing para-xylene and co-producing light olefins from methanol and/or dimethyl ether and toluene , the turbulent fluidized bed reactor comprising: a first reactor feed distributor and a plurality of second reactor feed distributors , the first reactor feed distributor and the plurality of second reactor feed distributors are sequentially arranged along the gas flow direction in the turbulent fluidized bed reactor;the feed to the first reactor feed distributor comprises toluene and a portion of methanol and/or dimethyl ether;the feed to the second reactor feed distributor comprises methanol and/or dimethyl ether; andthe number of the second reactor feed distributors is in a range from 2 to 10.28. The turbulent fluidized bed reactor of claim 27 , the turbulent fluidized bed reactor further comprising a first reactor gas-solid separator and a second reactor gas-solid separator claim 27 , the first reactor gas-solid separator is placed in a dilute phase ...

METHOD FOR OXYGENATE CONVERSION IN A FLUID CATALYTIC CRACKER

Provided herein are dual riser fluid catalytic cracking processes for producing light olefins from an oxygenate feed, such as a methanol feed, in a conventional FCC unit. In certain aspects the processes comprise cracking a hydrocarbon feed in a first riser comprising a first catalyst under first riser conditions to form a first effluent enriched in olefins, light gasoil, gasoline, or a combination thereof; cracking a hydrocarbon oxygenate feed in a second riser comprising a second catalyst under second riser conditions to form a second effluent enriched in olefins; recovering the first and second catalyst from the first and second effluents in a common reactor; regenerating the recovered first and second catalyst in a regenerator using heat from the exothermic cracking of the hydrocarbon oxygenate feed; and recirculating the regenerated first and second catalyst to the first and second riser. 1. A dual riser fluid catalytic cracking process , comprising:cracking a hydrocarbon feed in a first riser comprising a first catalyst under first riser conditions to form a first effluent enriched in olefins, light gasoil, gasoline, or a combination thereof;cracking a hydrocarbon oxygenate feed in a second riser comprising a second catalyst under second riser conditions to form a second effluent enriched in olefins;recovering the first and second catalyst from the first and second effluents in a common reactor;regenerating the recovered first and second catalyst in a regenerator using heat from the exothermic cracking of the hydrocarbon oxygenate feed; andrecirculating the regenerated first and second catalyst to the first and second riser.2. The process of claim 1 , wherein the hydrocarbon oxygenate feed includes methanol.3. The process of claim 1 , wherein the second riser conditions include a catalyst activity claim 1 , α claim 1 , of about 5 to 130.4. The process of claim 3 , wherein the catalyst activity claim 3 , α claim 3 , is about 10.5. The process of claim 1 , ...

A Multi-Stage Fluidized Catalytic Reaction Process of Petroleum Hydrocarbons and an Apparatus Thereof

The present invention relates to the technical field of petroleum hydrocarbon catalytic conversion, referring to a multi-stage fluidized catalytic reaction process of petroleum hydrocarbon. In the present reaction process, multi-stage reaction takes place in the same reactor, including first order reaction and the second order reaction of FCC feedstock oil, cracking reaction process of light hydrocarbons and/or cycle oil. In the present process, catalyst replacement and two-stage relayed reaction takes place between the first and second order reaction of feedstock oil. Two-stage reaction of light hydrocarbons and/or cycle oil takes place too. These reactions take place in different region in the same one reactor. The first order reaction of light hydrocarbons and/or cycle oil takes place in independent region. In the present invention, catalytic cracking conversion of catalytic feedstock oil, light hydrocarbon and cycle oil takes place in respective reaction region and reaction condition. Multi-stage and stepped selectivity control of catalyst and reaction temperature is realized. Multi-stage reaction and stepped arrangement of temperature is realized in the same reactor. It could improve the yield and selectivity of olefin, and decrease the yield of by-products such as coke obviously. 1. A multi-stage fluidized catalytic reaction process of petroleum hydrocarbon , characterized in that:in the present reaction process, multi-stage reaction takes place in the same reactor, including the first order reaction, the second order reaction of feedstock oil and cracking reaction process of light hydrocarbons and/or cycle oil; in the present process, catalyst replacement and two-stage relayed reaction takes place between the first and second order reaction of catalytic cracking feedstock oil, two-stage reaction of light hydrocarbons and/or cycle oil takes place too; these reactions take place in different region in the same one reactor; the first order reaction of light ...

UPGRADING PARAFFINS AND OLEFINS

In a process for upgrading paraffins and olefins, a first feed comprising Colefins is contacted with an oligomerization catalyst in a first reaction zone under conditions effective for oligomerization of olefins to higher molecular weight hydrocarbons. Deactivated catalyst is removed from the first reaction zone at a first temperature and is contacted with an oxygen-containing gas and a hydrocarbon-containing fuel in a regeneration zone to regenerate the catalyst and raise the temperature of the catalyst to a second, higher temperature. A second feed comprising Cparaffins is contacted with the regenerated catalyst in a second reaction zone to convert at least some of the paraffins in the second feed to a reaction effluent comprising olefins, aromatic hydrocarbons and regenerated catalyst; and the reaction effluent is supplied to the first reaction zone. A system for performing such a process and a product of such a process are also provided. 1. A process for upgrading paraffins and olefins , the process comprising:{'sub': '14−', '(i) contacting a first feed comprising C olefins with an oligomerization catalyst in a first reaction zone under conditions effective for oligomerization of olefins to higher molecular weight hydrocarbons;'}(ii) removing deactivated catalyst from the first reaction zone at a first temperature;(iii) contacting the deactivated catalyst with an oxygen-containing gas and with a hydrocarbon-containing fuel in a regeneration zone to regenerate the catalyst and raise the temperature of the catalyst to a second, higher temperature;{'sub': '14−', '(iv) contacting a second feed comprising C paraffins with the regenerated catalyst in a second reaction zone to convert at least some of the paraffins in the second feed to a reaction effluent comprising olefins, aromatic hydrocarbons and regenerated catalyst; and'}(v) supplying the reaction effluent to the first reaction zone.2. The process of wherein the first reaction zone comprises a fluidized catalyst ...

Dual riser fluid bed process and reactor

Processes and systems for cracking feeds to produce olefins are provided. The process for cracking feeds can include converting a first feed containing at least about 50 wt % methanol in a first riser under a first set of process conditions to produce a first effluent enriched in ethylene, propylene, or a mixture thereof, wherein the first effluent contains at least about 25 wt % dry basis propylene and converting a second feed containing C 4 -C 10 light hydrocarbons in a second riser under a second set of process conditions to produce a second effluent enriched in ethylene, propylene, or a mixture thereof. The process can also include combining the first effluent with the second effluent to produce a mixed effluent, separating the mixed effluent to produce a coked-catalyst and a gaseous product, regenerating the coked-catalyst, and recycling the regenerated catalyst to the first and second risers.

PROCESS AND SYSTEM FOR THERMAL TREATMENT OF GRANULAR SOLIDS

The invention relates to a process and the respective installation for thermal treatment of granular solids, in particular for producing aluminum oxide from aluminum hydroxide, wherein the solids are heated in at least one preheating stage and then reacted in a reactor at 700 to 1400° C. In at least one preheating stage, the average temperature gradient of the solids amounts to <15K/s and the dwell time of the solids amounts to ≥15 s. 1. A process for thermal treatment of granular solids , in particular for production of aluminum oxide from aluminum hydroxide , in which the solids are heated in at least one preheating stage and then are reacted in a reactor at 700 to 1400° C. , characterized in that , the average temperature gradient of the solids amounts to <15 K/s and the dwell time of the solids amounts to ≥15 s in at least one preheating stage.2. The process according to claim 1 , characterized in that the solids are heated to 140 to 180° C. in a first preheating stage and/or heated to 200 to 400° C. in a preheating stage downstream from the first preheating stage and/or in the downstream preheating stage claim 1 , the average temperature gradient of the solids amounts to <15 K/s and the dwell time of the solids amounts to >15 s.3. The process according to or claim 1 , characterized in that the average temperature gradient of the solids in the first 10% of the dwell time is above the average temperature gradient over the entire dwell time.4. The process according to claim 3 , characterized in that claim 3 , the average temperature gradient of the solids in the first 10% of the dwell time is more than twice as great as the average temperature gradient over the total dwell time.5. The process according to any one of the preceding claims claim 3 , characterized in that the solids are heated in countercurrent with the heating medium in at least two preheating stages connected after one another.6. The process according to any one of the preceding claims claim 3 , ...

REACTOR SYSTEMS COMPRISING FLUID RECYCLING

A method for processing a chemical stream includes contacting a feed stream with a catalyst in an upstream reactor section of a reactor having the upstream reactor section and a downstream reactor section, passing an intermediate product stream to the downstream reactor section, and introducing a riser quench fluid into the downstream reactor section, upstream reactor section, or transition section and into contact with the intermediate product stream and the catalyst to slow or stop the reaction. The method includes separating at least a portion of the catalyst from the product stream, passing the product stream to a product processing section, cooling the product stream, and separating a portion of the riser quench fluid from the product stream. The riser quench fluid separated from the product stream may be recycled back to the downstream reactor section, upstream reactor section, or transition section as the riser quench fluid. 1. A method for processing a chemical stream , the method comprising:contacting a feed stream with a catalyst in an upstream reactor section of a reactor system, wherein the reactor system comprises the upstream reactor section and a downstream reactor section, and the contacting of the feed stream with the catalyst causes a reaction which forms an intermediate product stream;passing at least a portion of the intermediate product stream and the catalyst from the upstream reactor section to the downstream reactor section;introducing a riser quench fluid into the downstream reactor section, the upstream reactor section, or a transition section between the downstream reactor section and the upstream reactor section and into contact with the at least a portion of the intermediate product stream and the catalyst in the downstream reactor section, the upstream reactor section, or the transition section to slow or stop the reaction of the intermediate product stream with the catalyst to form a product stream, the riser quench fluid having a ...

Production of Aromatics from Methanol Using Selective Hydrogen Combustion

A catalyst system and processes for combined aromatization and selective hydrogen combustion of oxygenated hydrocarbons are disclosed. The catalyst system contains at least one aromatization component and at least one selective hydrogen combustion component. The process is such that the yield of hydrogen is less than the yield of hydrogen when contacting the hydrocarbons with the aromatization component alone. 1. A catalyst system comprising: (1) at least one aromatization component for converting oxygenated hydrocarbons to aromatic compounds and (2) at least one selective hydrogen combustion component for reacting hydrogen with oxygen , said selective hydrogen combustion component consisting essentially of (a) a metal combination selected from the group consisting of:i) at least one metal from group 3 and at least one metal from groups 4-15 of the Periodic Table of the Elements;ii) at least one metal from groups 5-15 of the Periodic Table of the Elements, and at least one metal from at least one of groups 1, 2, and 4 of the Periodic Table of the Elements;iii) at least one metal from groups 1-2, at least one metal from group 3, and at least one metal from groups 4-15 of the Periodic Table of the Elements; andiv) two or more metals from groups 4-15 of the Periodic Table of the Elementsand (b) at least one of oxygen and sulfur, wherein the at least one of oxygen and sulfur is chemically bound both within and between the metals.2. The catalyst system of claim 1 , wherein the selective hydrogen combustion component is a combination of metal combination (a)(i) and (b) at least one of oxygen and sulfur.3. The catalyst system of claim 2 , wherein the at least one selective hydrogen combustion component comprises one or more of YInZnMnO claim 2 , LaMnNiAlO claim 2 , LaMnAlO claim 2 , ScCuMnO claim 2 , ScZnMnO claim 2 , LaZrO claim 2 , MnScO claim 2 , and PrInZnO claim 2 , where a claim 2 , b claim 2 , c claim 2 , and d are each between 0 and 1 claim 2 , the sum of a through ...

FLUIDIZED BED REACTOR AND METHOD FOR PRODUCING PARA-XYLENE AND CO-PRODUCING LIGHT OLEFINS FROM BENZENE AND METHANOL AND/OR DIMETHYL ETHER

A fluidized bed reactor for producing para-xylene and co-producing light olefins from benzene and methanol and/or dimethyl ether, including a first distributor and a second distributor. The first distributor is located at the bottom of the fluidized bed, and the second distributor is located at the downstream of the first distributor along a gas flow direction. Also, a method for producing para-xylene and co-producing light olefins, including the following steps: a material stream A enters a reaction zone of the fluidized bed reactor from the first gas distributor; a material stream B enters the reaction zone of the fluidized bed reactor from the second gas distributor; a reactant contacts a catalyst in the reaction zone to generate a gas phase stream comprising para-xylene and light olefins. 120-. (canceled)21. A fluidized bed reactor for producing para-xylene and co-producing light olefins from benzene and methanol and/or dimethyl ether , comprising a first distributor and a second distributor , wherein the first distributor is located at the bottom of the fluidized bed , and the second distributor is located in at least one region of the gas flow downstream from the first distributor.22. The fluidized bed reactor of claim 21 , wherein the second distributor comprises an intake pipe claim 21 , a microporous pipe and an intake ring pipe;the intake pipe is connected with a gas path of the microporous pipe, the gas is introduced by the intake pipe from the outside of the fluidized bed into the microporous pipe in the fluidized bed;the intake ring pipe is connected with a gas path of the intake pipe, the intake ring pipe is disposed on a plane perpendicular to the flow direction of the gas from the first distributor;the microporous pipe is disposed on the intake ring pipe and perpendicular to a plane of the intake ring pipe.23. The fluidized bed reactor of claim 21 , wherein material stream A enters the fluidized bed through the first distributor claim 21 , material ...

Multiple Reactor and Multiple Zone Polyolefin Polymerization

Apparatuses and processes that produce multimodal polyolefins, and in particular, polyethylene resins, are disclosed herein. This is accomplished by using two reactors in series, where one of the reactors is a multi-zone circulating reactor that can circulate polyolefin particles through two polymerization zones optionally having two different flow regimes so that the final multimodal polyolefin has improved product properties and improved product homogeneity. 120.-. (canceled)21. An apparatus for producing a multimodal polyolefin , comprising:a first reactor configured to produce a first polyolefin; a riser configured to produce the second polyolefin;', 'an upper conduit having an end fluidly connected to a top portion of the riser;', 'a separator fluidly connected to an opposite end of the upper conduit;', 'a downcomer configured to produce the third polyolefin, wherein a top portion of the downcomer is fluidly connected to the separator, optionally via a liquid barrier in the top portion of the downcomer; and', 'a lower conduit having an end fluidly connected to a bottom portion of the downcomer and an opposite end fluidly connected to a bottom portion of the riser,, 'a second reactor configured to produce a second polyolefin and a third polyolefin, where the second reactor comprises the second reactor is configured to receive the first polyolefin from the first reactor, or,', 'the first reactor is configured to receive the second polyolefin and the third polyolefin from the second reactor., 'wherein22. The apparatus of claim 21 , further comprising:a heat apparatus configured to add or remove heat from the downcomer.23. The apparatus of claim 21 , wherein the second reactor further comprises:a first elbow connector connected to the bottom portion of the riser and to the opposite end of the lower conduit;a second elbow connector connected to the top portion of the riser and to the end of the upper conduit; anda third elbow connector connected to the bottom ...

Multiple Reactor and Multiple Zone Polyolefin Polymerization

Apparatuses and processes that produce multimodal polyolefins, and in particular, polyethylene resins, are disclosed herein. This is accomplished by using two reactors in series, where one of the reactors is a multi-zone circulating reactor that can circulate polyolefin particles through two polymerization zones optionally having two different flow regimes so that the final multimodal polyolefin has improved product properties and improved product homogeneity.

MULTIPLE REACTOR AND MULTIPLE ZONE POLYOLEFIN POLYMERIZATION

Apparatuses and processes that produce multimodal polyolefins, and in particular, polyethylene resins, are disclosed herein. This is accomplished by using two reactors in series, where one of the reactors is a multi-zone circulating reactor that can circulate polyolefin particles through two polymerization zones optionally having two different flow regimes so that the final multimodal polyolefin has improved product properties and improved product homogeneity. 15-. (canceled)6. A trimodal polyethlene resin having a low molecular weight (LMW) component , an intermediate molecular weight (IMW) component , and a high molecular weight (HMW) component; wherein the LMW component is present in an amount of from about 20 wt. % to about 75 wt. %; wherein the IMW component is present in an amount of from about 5 wt. % to about 40 wt. %; wherein the LMW component has a weight average molecular weight of from about 20 kg/mol to about 150 kg/mol; wherein the IMW component has a weight average molecular weight of from about 85 kg/mol to about 350 kg/mol; wherein the weight average molecular weight of the IMW component is greater than the weight average molecular weight of the LMW component; wherein the weight average molecular weight of the HMW component is greater than the weight average e molecular weight of the IMW component; and wherein the trimodal polyethylene resin has a strain hardening modulus of from about 50 MPa to about 90 MPa , when tested in accordance with ISO 18488-2015(E) ,wherein (A1) the HMW component is present in an amount of from about 10 wt. % to about 60 wt. %; (A2) the HMW component has weight average molecular weight of great than about 350 kg/mol; or (A3) both the HMW component is present in an amount of from about 10 wt. % to about 60 wt. %, and the HMW component has weight average molecular weight of greater than about 350 kg/mol;wherein the trimodal polyethylene resin is characterized by (B1) a short chain branching content in the LMW component of ...

MULTIPLE REACTOR AND MULTIPLE ZONE POLYOLEFIN POLYMERIZATION

Apparatuses and processes that produce multimodal polyolefins, and in particular, polyethylene resins, are disclosed herein. This is accomplished by using two reactors in series, where one of the reactors is a multi-zone circulating reactor that can circulate polyolefin particles through two polymerization zones optionally having two different flow regimes so that the final multimodal polyolefin has improved product properties and improved product homogeneity. 18-. (canceled)9. A trimodal polyethylene resin having a low molecular weight (LMW) component , an intermediate molecular weight (IMW) component , and a high molecular weight (HMW) component; wherein the LMW component is present in an amount of from about 20 wt. % to about 75 wt. %; wherein the LMW component is present in an amount of from about 5 wt. % to about 40 wt. %; wherein the LMW component has a weight average molecular weight of from about 20 kg/mol to about 150 kg/mol; wherein the IMW component has a weight average molecular weight of from about 85 kg/mmol to about 350 kg/mol; wherein the weight average molecular weight of the IMW component is greater than the weight average molecular weight of the LMW component; wherein the weight average molecular weight of the HMW component is greater than the weight average molecular weight of the IMW component; and wherein the trimodal polyethylene resin has a tensile strength in the machine direction (MD) of greater than about 13 ,000 psi (89.6 MPa) , when tested in accordance with ASTM D638 at 90 MPa;wherein (A1) the HMW component is present in an amount of from about 10 wt. % to about 60 wt. %; (A2) the HMW component has weight average molecular weight of greater than about 350 kg/mol; or (A3) both the HMW component is present in an amount of from about 10 wt. % to about 60 wt. %, and the HMW component has weight average molecular weight of greater than about 350 kg/mol;wherein the trimodal polyethylene resin is characterized by (B1) a short chain branching ...

FLUID CATALYTIC CRACKING PROCESS AND APPARATUS FOR MAXIMIZING LIGHT OLEFIN YIELD AND OTHER APPLICATIONS

Apparatus and processes herein provide for converting hydrocarbon feeds to light olefins and other hydrocarbons. The processes and apparatus include, in some embodiments, feeding a hydrocarbon, a first catalyst and a second catalyst to a reactor, wherein the first catalyst has a smaller average particle size and is less dense than the second catalyst. A first portion of the second catalyst may be recovered as a bottoms product from the reactor, and a cracked hydrocarbon effluent, a second portion of the second catalyst, and the first catalyst may be recovered as an overhead product from the reactor. The second portion of the second catalyst may be separated from the overhead product, providing a first stream comprising the first catalyst and the hydrocarbon effluent and a second stream comprising the separated second catalyst, allowing return of the separated second catalyst in the second stream to the reactor. 143.-. (canceled)44. (canceled)45. (canceled)46. (canceled)47. (canceled)48. (canceled)49. (canceled)50. (canceled)51. (canceled)52. (canceled)53. A process for the conversion of hydrocarbons , comprising:regenerating a catalyst mixture comprising a first catalyst and a second particle in a regenerator, wherein the first catalyst has a smaller average particle size and/or is less dense than the second particle, and wherein the second particle may be catalytic or non-catalytic;feeding the catalyst mixture and hydrocarbons to a riser reactor to convert at least a portion of the hydrocarbons and recover a first effluent comprising the catalyst mixture and converted hydrocarbons;feeding the catalyst mixture to a second reactor;feeding a hydrocarbon feedstock to the second reactor and fluidizing the catalyst mixture;recovering an overhead product from the second reactor comprising the second particle, the first catalyst, and a reacted hydrocarbon product;separating the second particle from the overhead product to provide a first stream comprising the first ...

Process for the polymerization of olefins

The present invention relates to a process for the continuous preparation of polypropylene in a reactor from propylene and optionally ethylene and/or at least one other oolefin monomer, wherein the reactor comprises a fluidized bed, an expanded section located at or near the top of the reactor, a distribution plate located at the lower part of the reactor and an inlet for a recycle stream located under the distribution plate, wherein the process comprises—feeding a polymerization catalyst to the fluidized bed in the area above the distribution plate—feeding the propylene and the optional at least one other oolefin monomer to the reactor—withdrawing the polypropylene from the reactor—circulating fluids from the top of the reactor to the bottom of the reactor, wherein the circulating fluids are compressed using a compressor and cooled using a heat exchanger, resulting in a cooled recycle stream comprising liquid, and wherein the cooled recycle stream is introduced into the reactor using the inlet for the recycle stream wherein an alkane chosen from the group of iso-butane, n-butane, cyclopropane and mixtures thereof is added to the reactor and wherein the molar composition of the components in the recycle stream is chosen such that the dew temperature of the recycle stream at the reactor pressure is at least 0.10° C. below the temperature of the reactor

INTEGRATED C3-C4 HYDROCARBON DEHYDROGENATION PROCESS

An integrated process for producing C3-C4 olefins or di-olefins including: contacting a hydrocarbon feed and a catalyst feed in a fluidized dehydrogenation reactor under conditions such that a product mixture is formed and the catalyst is at least partially deactivated; transferring the product mixture and the catalyst from the reactor to a cyclonic separation system under conditions such that the product mixture is converted to form a new product mixture and is separated from the catalyst; transferring at least a portion of the catalyst to a regenerator vessel and heating it in order to combust the coke deposited thereon; subjecting the catalyst to a conditioning step to form an oxygen-containing, at least partially reactivated catalyst; and transferring the partially reactivated catalyst back to the fluidized dehydrogenation reactor. 1. An integrated process for producing C3-C4 olefins or C3-C4 di-olefins comprising the steps of:{'b': '1', 'claim-text': (i) a C3-C4 hydrocarbon feed and', '(ii) a catalyst feed comprising a catalyst;', 'under conditions such that a step (1)(a) product mixture, comprising a C3-C4 target olefin or di-olefin, hydrogen and unreacted C3-C4 hydrocarbon feed, is formed;, '() (a) contacting, in a fluidized dehydrogenation reactor,'} 'the catalyst has coke deposited thereon and is at least partially deactivated such that it forms an at least partially deactivated catalyst; and', 'and'}(b) transferring the step (1)(a) product mixture and the at least partially deactivated catalyst from the fluidized dehydrogenation reactor to a cyclonic separation system, andunder conditions such that the step (1)(a) product mixture is converted to form a step (1)(b) product mixture; andthereafter substantially separating the step (1)(b) product mixture and the at least partially deactivated catalyst from each other;(c) transferring at least a portion of the at least partially deactivated catalyst to a regenerator vessel and heating the at least partially ...

PROCESS FOR THE POLYMERIZATION OF OLEFINS

The present invention relates to a process for the continuous preparation of a polyolefin in a reactor from one or more α-olefin monomers of which at least one is ethylene or propylene, wherein the reactor comprises a fluidized bed, an expanded section located at or near the top of the reactor, a distribution plate located at the lower part of the reactor and an inlet for a recycle stream located under the distribution plate wherein the process comprises—feeding a polymerization catalyst to the fluidized bed in the area above the distribution plate—feeding the one or more α-olefin monomers to the reactor—withdrawing the polyolefin from the reactor—circulating fluids from the top of the reactor to the bottom of the reactor, wherein the circulating fluids are compressed using a compressor and subsequently cooled using a heat exchanger to form a cooled recycle stream comprising liquid, and wherein the cooled recycle stream is introduced into the reactor using the inlet for the recycle stream wherein a part of the cooled recycle stream is drawn to form a liquid comprising stream, wherein the liquid comprising stream is introduced into the expanded section during at least part of the polymerization process, and wherein the liquid comprising stream is brought into contact with at least part of the interior surface of the expanded section. 1. A process for the continuous preparation of a polyolefin in a reactor from one or more α-olefin monomers of which at least one is ethylene or propylene ,wherein the reactor comprises a fluidized bed, an expanded section located at or near the top of the reactor, a distribution plate located at the lower part of the reactor and an inlet for a recycle stream located under the distribution plate; feeding a polymerization catalyst to the fluidized bed in the area above the distribution plate', 'feeding the one or more α-olefin monomers to the reactor', 'withdrawing the polyolefin from the reactor', 'circulating fluids from the top of the ...

Systems for promoting endothermic conversions with oxygen transfer agents

A system for promoting endothermic conversions includes a first and second portion, a first and second supply, a first outlet, and a heat exchanger. The first portion defines a first inner volume containing an oxygen transfer agent. The first supply contains a reducing agent and is fluidly connected to the first inner volume. The first outlet conveys one or more of carbon dioxide, water, and an unsaturated hydrocarbon from the first inner volume. The second portion and the heat exchanger positioned within the second portion define a second inner volume containing reduced oxygen transfer agent. The second supply contains an oxidizing agent fluidly connected to the second inner volume. The heat exchanger also defines a third inner volume segregated from the second inner volume, and the heat exchanger is configured to transfer heat resulting from the oxidation of the reduced oxygen transfer agent to the third inner volume.

GAS-PHASE PROCESS FOR PREPARING ETHYLENE POLYMERS

A process for preparation of an ethylene polymer in a gas-phase polymerization unit comprising a gas-phase polymerization reactor by homopolymerizing ethylene or copolymerizing ethylene and one or more C-C-1-alkenes in a reaction gas made from or containing propane as polymerization diluent in the presence of a pre-activated polymerization catalyst, wherein a purified propane feed stream made from or containing at least 99 mol % propane and from 0.1 to 100 ppm mol propylene is fed to the gas-phase polymerization unit. 1. A process for the preparation of an ethylene polymer , comprising the step of{'sub': 4', '12, 'forming an ethylene polymer in particle form in a gas-phase polymerization unit comprising a gas-phase polymerization reactor by homopolymerizing ethylene or copolymerizing ethylene and one or more C-C-1-alkenes at temperatures from 20 to 200° C. and pressures of from 0.5 to 10 MPa in a reaction gas comprising propane as polymerization diluent in the presence of a pre-activated polymerization catalyst,'}wherein a purified propane feed stream comprising at least 99% mol propane and not more than 100 ppm-mol propylene is fed to the gas-phase polymerization unit and the purification has been carried out by passing a hydrocarbon stream through hydrocarbon purification units which reduce at least the concentration of propylene, acetylene, carbon monoxide, carbon dioxide, oxygen and water contained in the hydrocarbon stream.2. The process of claim 1 , wherein the purified propane feed stream fed to the gas-phase polymerization unit comprises not more than 0.03 ppm-mol carbon monoxide claim 1 , not more than 0.4 ppm-mol carbon dioxide claim 1 , not more than 2.0 ppm-mol oxygen claim 1 , not more than 3.0 ppm-mol acetylene claim 1 , and not more than 2.0 ppm-mol water.3. The process of claim 1 , wherein the pre-activation of the polymerization catalyst is carried out by contacting claim 1 , in liquid propane as diluent claim 1 , a solid catalyst component with an ...

Multiple Reactor and Multiple Zone Polyolefin Polymerization

Apparatuses and processes that produce multimodal polyolefins, and in particular, polyethylene resins, are disclosed herein. This is accomplished by using two reactors in series, where one of the reactors is a multi-zone circulating reactor that can circulate polyolefin particles through two polymerization zones optionally having two different flow regimes so that the final multimodal polyolefin has improved product properties and improved product homogeneity. 1. A trimodal polyethylene resin having a low molecular weight (LMW) component , an intermediate molecular weight (IMW) component , and a high molecular weight (HMW) component; wherein the LMW component is present in an amount of from about 20 wt. % to about 75 wt. %; wherein the IMW component is present in an amount of from about 5 wt. % to about 40 wt. %; wherein the LMW component has a weight average molecular weight of from about 20 kg/mol to about 150 kg/mol; wherein the IMW component has a weight average molecular weight of from about 85 kg/mol to about 350 kg/mol; wherein the weight average molecular weight of the IMW component is greater than the weight average molecular weight of the LMW component; wherein the weight average molecular weight of the HMW component is greater than the weight average molecular weight of the IMW component; wherein the trimodal polyethylene resin has an η(eta_0) of equal to or greater than about 0.7×10Pa-s; and wherein the trimodal polyethylene resin has a strain hardening modulus of from about 50 MPa to about 90 MPa , when tested in accordance with ISO 18488-2015(E).2. The trimodal polyethylene resin of claim 1 , wherein (A1) the HMW component is present in an amount of from about 10 wt. % to about 60 wt. %; (A2) the HMW component has weight average molecular weight of greater than about 350 kg/mol; or (A3) both the HMW component is present in an amount of from about 10 wt. % to about 60 wt. % claim 1 , and the HMW component has weight average molecular weight of greater ...

Multiple Reactor and Multiple Zone Polyolefin Polymerization

Apparatuses and processes that produce multimodal polyolefins, and in particular, polyethylene resins, are disclosed herein. This is accomplished by using two reactors in series, where one of the reactors is a multi-zone circulating reactor that can circulate polyolefin particles through two polymerization zones optionally having two different flow regimes so that the final multimodal polyolefin has improved product properties and improved product homogeneity. 1. A trimodal polyethylene resin having a low molecular weight (LMW) component , an intermediate molecular weight (IMW) component , and a high molecular weight (HMW) component; wherein the LMW component is present in an amount of from about 20 wt. % to about 75 wt. %; wherein the IMW component is present in an amount of from about 5 wt. % to about 40 wt. %; wherein the LMW component has a weight average molecular weight of from about 20 kg/mol to about 150 kg/mol; wherein the IMW component has a weight average molecular weight of from about 85 kg/mol to about 350 kg/mol; wherein the weight average molecular weight of the IMW component is greater than the weight average molecular weight of the LMW component; wherein the weight average molecular weight of the HMW component is greater than the weight average molecular weight of the IMW component; wherein the trimodal polyethylene resin has an η(eta_0) of equal to or greater than about 0.7×10Pa-s; and wherein the trimodal polyethylene resin has a tensile strength in the machine direction (MD) of greater than about 13 ,000 psi (89.6 MPa) , when tested in accordance with ASTM D638 at 90 MPa.2. The trimodal polyethylene resin of claim 1 , wherein (A1) the HMW component is present in an amount of from about 10 wt. % to about 60 wt. %; (A2) the HMW component has weight average molecular weight of greater than about 350 kg/mol; or (A3) both the HMW component is present in an amount of from about 10 wt. % to about 60 wt. % claim 1 , and the HMW component has weight ...

FLUID CATALYTIC CRACKING PROCESS AND APPARATUS FOR MAXIMIZING LIGHT OLEFIN YIELD AND OTHER APPLICATIONS

Apparatus and processes herein provide for converting hydrocarbon feeds to light olefins and other hydrocarbons. The processes and apparatus include, in some embodiments, feeding a hydrocarbon, a first catalyst and a second catalyst to a reactor, wherein the first catalyst has a smaller average particle size and is less dense than the second catalyst. A first portion of the second catalyst may be recovered as a bottoms product from the reactor, and a cracked hydrocarbon effluent, a second portion of the second catalyst, and the first catalyst may be recovered as an overhead product from the reactor. The second portion of the second catalyst may be separated from the overhead product, providing a first stream comprising the first catalyst and the hydrocarbon effluent and a second stream comprising the separated second catalyst, allowing return of the separated second catalyst in the second stream to the reactor.

FLUIDIZED BED SYSTEM

A fluidized bed system is a single unitary modular system that packages a circulation fan, a fluidized bed, and a dust collection system within a same structure. The structure is formed to include internal ducts to provide fluid communication between the circulation fan, the fluidized bed, and the dust collection system. The fan provides a flow of air via a pressure duct to the fluidized bed. Particulate is separated from particles included on the fluidized bed by the flow of air being uniformly distributed to the fluidized bed. Particulate separated in a disengagement area and suspended in the flow of air is conducted through a particulate clearance space surrounding the dust collection system. The particulate is captured by the dust collection system and conveyed to a location external to the system. 1. A fluidized bed system comprising:an enclosure having an inner chamber positioned below a dust hopper;a fluidized bed positioned in the inner chamber below the dust hopper and configured to process particles and remove particulate;a fan included in a plenum, the fan configured to provide a flow of air through the fluidized bed toward the dust hopper; anda wall defining the inner chamber, the dust hopper moveably positioned vertically within the inner chamber at a predetermined height above the fluidized bed to separate a predetermined size of particulate from the particles within the flow of air toward the dust hopper, the dust hopper at least partially surrounded by the wall to provide a particulate clearance space between the wall and the dust hopper, an entrance to the particulate clearance space configured to receive only the predetermined size of the particulate separated from the particles within the flow of air due to the predetermined height.2. The fluidized bed system of claim 1 , further comprising a pressure duct at an outlet of the fan and a suction duct at an inlet of the fan claim 1 , the suction duct having heated air that is in thermal communication ...

SYSTEM COMPONENTS OF FLUID CATALYTIC REACTOR SYSTEMS

According to one or more embodiments disclosed herein, a system component of a fluid catalytic reactor system may include a catalyst separation section, a riser, and a reactor vessel. The catalyst separation section may include separation section walls defining an interior region of the catalyst separation section, a gas outlet port, a riser port, a separation device, and a catalyst outlet port. The riser may extend through the riser port of the catalyst separation section and include an external riser section and an internal riser section. The reactor vessel may include a reactor vessel inlet port, and a reactor vessel outlet port in fluid communication with the external riser section of the riser. 1. A system component of a fluid catalytic reactor system , the system component comprising:a catalyst separation section comprising separation section walls defining an interior region of the catalyst separation section, a gas outlet port, a riser port, a separation device, and a catalyst outlet port;a riser extending through the riser port of the catalyst separation section, the riser comprising a main interior riser wall segment, a main exterior riser wall segment, and a riser transition wall segment, the main interior riser wall segment positioned at least partially in the interior region of the catalyst separation section and connected with at least the main interior riser wall segment, and the exterior riser wall segment positioned at least partially outside of the catalyst separation section; anda reactor vessel comprising a reactor vessel inlet port, and a reactor vessel outlet port in fluid communication with the main exterior riser wall segment.2. The system component of claim 1 , wherein the main interior riser wall segment and the main exterior riser wall segment are substantially parallel claim 1 , and the maximum diameter of the main interior riser wall segment is less than the maximum diameter of the main exterior riser wall segment.3. The system component ...

Staged fluid catalytic cracking processes incorporating a solids separation device for upgrading naphtha range material

Processes and systems for the conversion of hydrocarbons herein may include separating an effluent from a moving bed reactor, the effluent including reaction product, first particulate catalyst, and second particulate catalyst. The separating may recover a first stream including the reaction product and first particulate catalyst and a second stream including second particulate catalyst. The second stream may be admixed with a regenerated catalyst stream including both first and second particulate catalyst at an elevated temperature. The admixing may produce a mixed catalyst at a relatively uniform temperature less than the elevated regenerated catalyst temperature, where the temperature is more advantageous for contacting light naphtha and heavy naphtha within the moving bed reactor to produce the effluent including the reaction product, the first particulate catalyst, and the second particulate catalyst.

OLEFIN POLYMERIZATION PROCESS IN A GAS-PHASE REACTOR COMPRISING A RISER UNIT AND A DOWNCOMER

A process for preparing an ethylene polymer including the step of homopolymerizing ethylene or copolymerizing ethylene with one or more comonomers in a gas-phase polymerization reactor including a riser unit wherein growing polymer particles flow upwards under fluidization, fast fluidization or transport conditions and a downcomer wherein growing polymer particles flow downward in a densified form, wherein the hold-up of polymer particles in the downcomer is from 55 wt. % to 80 wt. % of the total hold-up of polymer particles in the gas-phase polymerization reactor. 1. A process for preparing an ethylene polymer comprising the step of: a riser unit wherein growing polymer particles flow upwards under fluidization, fast fluidization or transport conditions, and', 'a downcomer wherein growing polymer particles flow downward in a densified form,, 'homopolymerizing ethylene or copolymerizing ethylene with a comonomer in the presence of a polymerization catalyst in a gas-phase polymerization reactor to yield growing polymer particles, the gas-phase polymerization reactor comprising'}wherein the hold-up of polymer particles in the downcomer is from 55 wt. % to 80 wt. % of the total hold-up of polymer particles in the gas-phase polymerization reactor.2. The process of claim 1 , wherein the gas-phase polymerization reactor is a multizone circulating reactor wherein the riser unit is a riser wherein growing polymer particles flow upwards under fast fluidization or transport conditions claim 1 , the riser and the downcomer are interconnected claim 1 , the polymer particles leaving the riser enter the downcomer claim 1 , and the polymer particles leaving the downcomer enter the riser claim 1 , thereby establishing a circulation of polymer particles through the riser and the downcomer.3. The process of claim 1 , wherein the riser unit wherein the growing polymer particles flow upwards; comprisesa fluidized bed of growing polymer particles.4. The process of claim 1 , wherein the ...

APPARATUS AND PROCESS FOR SEPARATING GASES FROM CATALYST

In an FCC apparatus in which swirl arms are used to discharge gas and catalyst from a riser, the swirling movement of the catalyst particles is inhibited while impeding the catalyst particles and gaseous products from exiting the disengaging chamber and entering a reactor annulus. The catalyst particles and gaseous products pass through a tunnel comprising a vertical wall to enter the reactor annulus. The vertical wall presents a face that is opposed to the angular direction in which the catalyst particles and gaseous products swirl. 1. A process for separating catalyst particles from a gaseous product stream comprising: contacting a hydrocarbon feed stream with catalyst particles in an elongated riser to produce gaseous products; inducing the catalyst particles and gaseous products to swirl in an angular direction upon exiting said riser and entering a disengaging chamber to disengage catalyst particles from said gaseous product; inhibiting said catalyst particles and gaseous products from exiting said disengaging chamber and entering a reactor annulus.2. The process of further comprising requiring passage of said catalyst particles and said gaseous products through a tunnel with a vertical wall to exit said disengaging chamber and enter said reactor annulus.3. The process of wherein said vertical wall of said tunnel presents a face opposed to the angular direction in which the catalyst particles and gaseous products swirl.4. The process of further comprising: stripping descending catalyst particles with a stripping gas over elongated strips in a stripping section; and separating catalyst particles entrained with ascending gaseous products from said gaseous products.5. The process of further comprising deflecting downward movement of said catalyst particles laterally upon entering into said disengaging chamber from said tunnel.6. The process of further comprising fluidizing said catalyst particles being deflected with fluidizing gas through openings in a deflecting ...

FLUID CATALYTIC CRACKING PROCESS AND APPARATUS FOR MAXIMIZING LIGHT OLEFIN YIELD AND OTHER APPLICATIONS

Apparatus and processes herein provide for converting hydrocarbon feeds to light olefins and other hydrocarbons. The processes and apparatus include, in some embodiments, feeding a hydrocarbon, a first catalyst and a second catalyst to a reactor, wherein the first catalyst has a smaller average particle size and is less dense than the second catalyst. A first portion of the second catalyst may be recovered as a bottoms product from the reactor, and a cracked hydrocarbon effluent, a second portion of the second catalyst, and the first catalyst may be recovered as an overhead product from the reactor. The second portion of the second catalyst may be separated from the overhead product, providing a first stream comprising the first catalyst and the hydrocarbon effluent and a second stream comprising the separated second catalyst, allowing return of the separated second catalyst in the second stream to the reactor. 143.-. (canceled)44. A process for the conversion of hydrocarbons , comprising:feeding first particles and second particles to a reactor, wherein the first particles have a smaller average particle size and/or are less dense than the second particles, and wherein the first particles and second particles may independently be catalytic or non-catalytic particles;feeding a hydrocarbon feedstock to the reactor;recovering an overhead product from the reactor comprising a converted hydrocarbon effluent, the second particles, and the first particles;separating the second particles from the overhead product to provide a first stream comprising the first particles and the converted hydrocarbon effluent and a second stream comprising the separated second particles;returning the separated second particles in the second stream to the reactor.45. The process of claim 44 , further comprising recovering a bottoms product from the reactor comprising the second particle.46. The process of claim 44 , further comprising:feeding a second hydrocarbon feedstock and a mixture of ...

FLUID CATALYTIC CRACKING PROCESS AND APPARATUS FOR MAXIMIZING LIGHT OLEFIN YIELD AND OTHER APPLICATIONS

Apparatus and processes herein provide for converting hydrocarbon feeds to light olefins and other hydrocarbons. The processes and apparatus include, in some embodiments, feeding a hydrocarbon, a first catalyst and a second catalyst to a reactor, wherein the first catalyst has a smaller average particle size and is less dense than the second catalyst. A first portion of the second catalyst may be recovered as a bottoms product from the reactor, and a cracked hydrocarbon effluent, a second portion of the second catalyst, and the first catalyst may be recovered as an overhead product from the reactor. The second portion of the second catalyst may be separated from the overhead product, providing a first stream comprising the first catalyst and the hydrocarbon effluent and a second stream comprising the separated second catalyst, allowing return of the separated second catalyst in the second stream to the reactor. 1. A particle separator for separating catalysts or other particles based on size and/or density , comprising:an inlet for providing a mixture comprising a carrier gas, a first particle type, and a second particle type, each particle type having a particle size distribution, an average particle size and an average density, the second particle type having an average particle size and/or average density greater than the first particle type;a chamber for receiving the mixture, wherein the chamber is configured to separate at least a portion of the second particle type from the carrier gas and the first particle type;a first outlet to recover the second particle type;a second outlet to recover the carrier gas and the first particle type; anda distributor disposed within or proximate the first outlet for introducing a fluidizing gas, facilitating additional separation of the first particle type from the second particle type.2. The separator of claim 1 , wherein a cross-sectional area of the chamber or a portion thereof is adjustable.3. The separator of claim 1 , ...

A method for returning polymer to a fluidised bed reactor

The present invention deals with a process of polymerising at least one olefin in a fluidised bed in a fluidised bed polymerisation reactor comprising a top zone, a middle zone in direct contact and below, a bottom zone in direct contact with and below the middle zone and wherein the reactor does not comprise a fluidisation grid. The process comprises passing a stream comprising the fluidisation gas and polymer particles into a separation step and withdrawing a stream comprising the polymer particles from the separation step and returning it to the polymerisation reactor. The process comprises adding a support gas stream to the stream comprising the polymer particles downstream of the separation step.

Multiple Reactor and Multiple Zone Polyolefin Polymerization

Apparatuses and processes that produce multimodal polyolefins, and in particular, polyethylene resins, are disclosed herein. This is accomplished by using two reactors in series, where one of the reactors is a multi-zone circulating reactor that can circulate polyolefin particles through two polymerization zones optionally having two different flow regimes so that the final multimodal polyolefin has improved product properties and improved product homogeneity. 1. A process for producing a multimodal polyolefin , comprising:(a) polymerizing ethylene in a first reactor to produce a first polyolefin;(b) polymerizing ethylene in a first reaction mixture in a riser of a second reactor to produce a second polyolefin;(c) passing the first reaction mixture through an upper conduit from the riser to a separator;(d) recovering, in the separator, the second polyolefin from the first reaction mixture;(e) passing the second polyolefin from the separator into a downcomer of the second reactor, optionally via a liquid barrier;(f) polymerizing ethylene in a second reaction mixture in the downcomer to produce a third polyolefin in a downcomer product mixture;(g) passing the downcomer product mixture through a lower conduit from the downcomer to the riser; and (1) after step (a) and before steps (b)-(g), receiving the first polyolefin into the second reactor; or', '(2) before step (a) and after steps (b)-(g), receiving the second polyolefin and the third polyolefin into the first reactor., '(h) one of2. The process of claim 1 , wherein an elbow connector is connected i) to a bottom portion of the riser and to an end of the lower conduit claim 1 , ii) to a top portion of the riser and to an end of the upper conduit claim 1 , or iii) to a bottom portion of the downcomer and to an opposite end of the lower conduit claim 1 , wherein the elbow connector comprises:a first tap on an outside radius of the elbow connector;a second tap on an inside radius of the elbow connector;a first sensing ...

THERMOLYTIC FRAGMENTATION OF SUGARS

A process for large scale and energy efficient production of oxygenates from sugar is disclosed in which a sugar feedstock is introduced into a thermolytic fragmentation reactor including a fluidized stream of heat carrying particles. The heat carrying particles may be separated from the fluidized stream prior to cooling the fragmentation product and may be directed to a reheater to reheat the particles and recirculate the heated particles to the fragmentation reactor. 1. A process for thermolytic fragmentation of a sugar into C-Coxygenates , said process comprising the steps of:a. providing particles carrying heat and suitable for fluidization;b. providing a fluidized bed fragmentation reactor comprising a riser and suitable for conducting thermolytic fragmentation and suitable for fluidizing a stream of particles;c. providing a feedstock solution comprising a sugar;d. introducing the particles into the reactor at a rate sufficient to maintain a temperature of at least 250° C., such as at least 300 350, 400 or 450° C., after the thermolytic fragmentation has taken place, and sufficient to obtain a fluidized stream of particles;e. introducing the feedstock into the fluidized stream of particles to obtain thermolytic fragmentation of the sugar to produce a particle dense fragmentation product; thenf. separating a fraction of the particles from the particle dense fragmentation product to produce a particle lean fragmentation product;g. quenching the particle lean fragmentation product at least 50° C. such that from introducing the feedstock into the particle containing fluidization stream to the quench is performed, the mean residence time of the gas is maximum 5, such as maximum 3 seconds, such as maximum 2, 1, 0.8 or 0.6 seconds;h. recovering the crude fragmentation product,i. transferring the particles separated in step f) to a reheater for heating; andj. recirculating the heated particles to the fragmentation reactor. The present application is a continuation of U ...

Reactor systems and processes for using the same

circulating fluidized bed reactor

Process for polymerizing olefin in a gas phase reactor with improved thermal homogeneity

The present invention relates to a process for polymerizing at least one olefin in gas phase in a fluidized bed in a polymerization reactor having a top zone of a generally conical shape as such that the equivalent cross-sectional diameter is monotonically decreasing with respect to the flow direction of the fluidization gas, a middle zone in direct contact with and below said top zone of a generally cylindrical shape and a bottom zone in direct contact and below said middle zone and of a generally conical shape as such that the equivalent cross-sectional diameter is monotonically increasing with respect to the flow direction of the fluidization gas, comprising the steps of: a) introducing a first stream of fluidization gas into the bottom zone; b) polymerizing at least one olefin in the presence of a polymerization catalyst in the fluidized bed formed by particles of a polymer of the at least one olefin suspended in an upwards flowing stream of the fluidization gas in the middle zone; c) withdrawing a second stream comprising the fluidization gas and optionally particles of a polymer of the at least one olefin from the top zone; characterized in that the temperature of the particles of the polymer of the at least one olefin in the fluidized bed (T PP ) does not exceed 120% of the operating temperature set point (T S ) of the polymerization reactor, wherein T PP and T S are both given in °C, and the use of said process for polymerizing an olefin homo- or copolymer having a narrow particle size distribution.

用于在具有改善的热均质性的气相反应器中聚合烯烃的方法

本发明涉及一种用于在聚合反应器中在流化床中在气相中聚合至少一种烯烃的方法以及所述方法用于聚合具有窄粒度分布的烯烃均聚物或共聚物的用途，所述聚合反应器具有顶部区域、与所述顶部区域直接接触并在其下方的中部区域和与所述中部区域直接接触并在其下方的底部区域，所述顶部区域为大致锥形，使得等效横截面直径相对于流化气体的流动方向单调递减，所述中部区域为大致柱形，所述底部区域为大致锥形，使得等效横截面直径相对于所述流化气体的流动方向单调递增，所述方法包括以下步骤：a)将第一流化气体物流引入底部区域；b)在由悬浮在中部区域中向上流动的流化气体物流中的至少一种烯烃的聚合物颗粒形成的流化床中在聚合催化剂的存在下聚合至少一种烯烃；c)从顶部区域中抽出包含流化气体和任选的至少一种烯烃的聚合物颗粒的第二物流；其特征在于流化床中的至少一种烯烃的聚合物颗粒的温度(T PP )不超过聚合反应器的工作温度设定点(T S )的120％，其中T PP 和T S 均以℃给出。

Polyolefin reactor system having a gas phase reactor

A system and method for polymerizing olefin in a gas phase reactor into a polyolefin in presence of catalyst, measuring static charge in the reactor system; determining an indication of polyolefin fines in the reactor system, and adjusting operation of the reactor system in response to the indication.

Process for the polymerization of olefins

Process for the polymerization of olefins

Multi-zone reactor for continuous polymerization of alpha olefin monomers

The invention relates to a multi-zone reactor suitable for the continuous fluidized bed polymerization of one or more α-olefin monomers of which at least one is ethylene or propylene, which multi-zone reactor is operable in condensed mode, which multi-zone reactor comprises a first zone, a second zone, a third zone, a fourth zone and a distribution plate, wherein the first zone is separated from the second zone by the distribution plate, wherein the multi-zone reactor is extended in the vertical direction wherein the second zone of the multi-zone reactor is located above the first zone and wherein the third zone of the multi-zone reactor is located above the second zone, and wherein the fourth zone of the multi-zone reactor is located above the third zone wherein the second zone contains an inner wall, wherein at least part of the inner wall of the second zone is either in the form of a gradually increasing inner diameter or a continuously opening cone, wherein the diameter or the opening increases in the vertical direction towards the top of the multi-zone reactor wherein the third zone contains an inner wall, wherein at least part of the inner wall of the third zone is either in the form of a gradually increasing inner diameter or a continuously opening cone, wherein the diameter or the opening increases in the vertical direction towards the top of the multi-zone reactor wherein the largest diameter of the inner wall of the third zone is larger than the largest diameter of the inner wall of the second zone.

Process for polymerizing olefin in a gas phase reactor with improved thermal homogeneity

The present invention relates to a process for polymerizing at least one olefin in gas phase in a fluidized bed in a polymerization reactor having a top zone of a generally conical shape as such that the equivalent cross-sectional diameter is monotonically decreasing with respect to the flow direction of the fluidization gas, a middle zone in direct contact with and below said top zone of a generally cylindrical shape and a bottom zone in direct contact and below said middle zone and of a generally conical shape as such that the equivalent cross-sectional diameter is monotonically increasing with respect to the flow direction of the fluidization gas, comprising the steps of: a) introducing a first stream of fluidization gas into the bottom zone; b) polymerizing at least one olefin in the presence of a polymerization catalyst in the fluidized bed formed by particles of a polymer of the at least one olefin suspended in an upwards flowing stream of the fluidization gas in the middle zone; c) withdrawing a second stream comprising the fluidization gas and optionally particles of a polymer of the at least one olefin from the top zone; characterized in that the temperature of the particles of the polymer of the at least one olefin in the fluidized bed (T PP ) does not exceed 120% of the operating temperature set point (T S ) of the polymerization reactor, wherein T PP and T S are both given in ° C., and the use of said process for polymerizing an olefin homo- or copolymer having a narrow particle size distribution.

Process and apparatus for the gas-phase polymerization of α-olefins

Process for gas-phase polymerization carried out in two interconnected polymerization zones, to which one or more α-olefins CH 2 ═CHR are fed in the presence of catalyst under reaction conditions and from which the polymer product is discharged. The process is characterized in that the growing polymer flows through a first polymerization zone under fast fluidization conditions, leaves said first zone and enters a second polymerization zone through which it flows in a densified form under the action of gravity, leaves said second zone and is reintroduced into the first polymerization zone, thus establishing a circulation of polymer around the two polymerization zones. The novel process allows olefins to be polymerized in the gas phase with high productivity per unit volume of the reactor without incurring the problems of the fluidized-bed technologies of the known state of the art.

Process for the gas-phase polymerization of olefins

Processo ed apparecchiatura per la pomimerizzazione in fase gas delle alfa-olefine

Process and apparatus for the gas-phase polymerization of alpha-olefins

Process for gas-phase polymerization carried out in two interconnected polymerization zones, to which one or more .alpha.--olefins CH2=CHR are fed in the presence of catalyst under reaction conditions and from which the polymer product is discharged. The process is characterized in that the growing polymer flows through a first polymerization zone under fast fluidization conditions, leaves said first zone and enters a second polymerization zone through which it flows in a densified form under the action of gravity, leaves said second zone and is reintroduced into the first polymerization zone, thus establishing a circulation of polymer around the two polymerization zones. The novel process allows olefins to be polymerized in the gas phase with high productivity per unit volume of the reactor without incurring the problems of the fluidized-bed technologies of the known state of the art.

Process and apparatus for the gas-phase polymerization of alpha-olefins

Process for gas-phase polymerization carried out in two interconnected polymerization zones, to which one or more α-olefins CH2=CHR are fed in the presence of catalyst under reaction conditions and from which the polymer product is discharged. The process is characterized in that the growing polymer flows through a first polymerization zone under fast fluidization conditions, leaves said first zone and enters a second polymerization zone through which it flows in a densified form under the action of gravity, leaves said second zone and is reintroduced into the first polymerization zone, thus establishing a circulation of polymer around the two polymerization zones. The novel process allows olefins to be polymerized in the gas phase with high productivity per unit volume of the reactor without incurring the problems of the fluidized-bed technologies of the known state of the art.

Elimination of polymer fouling in fluidized bed gas-phase fines recovery eductors

An eductor, a process and apparatus for gas phase polymerization of olefins in a polymerization reactor are disclosed. The process and apparatus employ an eductor which has an inlet which makes a bend of less than about 90° toward the outlet after entering the mixing chamber of the eductor.

Process and apparatus for the gas-phase polymerisation

A process for the gas-phase catalytic polymerisation carried out in two interconnected polymerisation zones, to which one or more monomers are fed in the presence of a catalyst under polymerisation conditions and from which the produced polymer is discharged. The growing polymer particles flow through a first polymerisation zone under fast fluidisation conditions, leave said first zone and enter a second polymerisation zone through which they flow in a densified form under the action of gravity, leave said second zone and are reintroduced into the first polymerisation zone, thus establishing a circulation of polymer between the two polymerisation zones. The present invention is characterised in that a gas of composition different from that present in the first polymerisation zone is introduced into the second polymerisation zone and it is avoided that the gases present in the first polymerisation zone are introduced into the second polymerisation zone. The process is particularly suited for obtaining in-reactor made blends of olefin polymers having different compositions.

用于丙烯聚合的方法和装置

一种制备异相丙烯共聚物的方法，其通过在存在作为分子量调节剂的聚合催化剂和氢的情况下聚合丙烯制备，所述方法包括下述步骤：a)聚合气相或液相丙烯，制备结晶聚合物级分；b)在具有相互连接聚合区域的气相反应器中，共聚合乙烯和丙烯和/或1-丁烯和任选的一种或多种α-烯烃共聚单体C 5 -C 12 ，其中在快速流化或递送条件下，生长聚合物颗粒向上流过第一聚合区域(上升管)，离开所述上升管并进入第二聚合区域(降液管)，所述聚合物颗粒在重力作用下向下流动通过所述第二聚合区域(降液管)。

Reactor systems and processes for using the same

A process for the polymerization of olefin's, including: introducing an olefin and a polymerization catalyst into a polymerization reactor to form a polyolefin, the polymerization reactor including: a fluidized bed region having a top and a bottom; and a motive bed region; wherein a first end of the motive bed region is fluidly connected to the top of the fluidized bed region; and wherein a second end of the motive bed region is fluidly connected to the bottom of the fluidized bed region; and wherein a diameter of the fluidized bed region is greater than a diameter of the motive bed region; circulating at least a portion of the olefin, the catalyst, and the polyolefin through the fluidized bed region and the motive bed region; maintaining a dense-phase fluidized bed within the fluidized bed region; recovering polyolefin from the fluidized bed region, is provided. A reactor system directed to the process is also provided.

Circulating fluidized bed reactor

A continuous gas phase circulating bed reactor, including: a riser for contacting a catalyst and a first gas composition comprising an olefin to form a polyolefin under fast-fluidization regime or a dilute-phase pneumatic conveying regime conditions; a downer for contacting the catalyst and a second gas composition comprising an olefin to form additional polyolefin under fast fluidization regime or a dilute-phase pneumatic conveying regime conditions; and a transport section for conveying at least a portion of the catalyst, polyolefin, and additional polyolefin from the downer to the riser. Also disclosed is a polymerization process using such a circulating bed reactor.

Fluidized bed polymerization reactor and process for preparing polymer

The present invention provides a fluidized bed polymerization reactor, comprising: a tower body, provided therein with a liquid phase distributor and a gas phase distributor above the liquid phase distributor, so as to divide a reaction area into a first area and a second area by means of the gas phase distributor; and a recycling unit, for recycling the gaseous substances originating from the top area of the tower to the bottom area in the form of a gas liquid mixture. In this situation, the gas liquid mixture is subjected to a gas liquid separation in the bottom area, wherein the gas phase obtained is output into the gas phase distributor and thence into the second area, and the liquid phase obtained enters the first area via the liquid phase distributor, such that the temperature in the first area is lower than the temperature in the second area. A polymer with a relatively wide molecular weight distribution can thus be produced. The present invention also provides a process for preparing polymers.

Method for gas-phase polymerization of alpha-olefin

PURPOSE: A gas-phase polymerization method of alpha-olefins is provided to prepare polyolefin with high productivity and to efficiently remove reaction heat by increasing contact time. CONSTITUTION: A gas-phase polymerization method of alpha-olefins comprises the steps of: producing a polyolefin prepolymer by prepolymerizing a catalyst, liquid isobutene, and at least one alpha-olefin; supplying the mixture of the catalyst and polyolefin prepolymer, and a cycling gas including at least one alpha-olefin and inert gas to a second reactor(200); polymerizing prepolymer and alpha-olefin with polyolefin; and discharging a polyolefin polymer from a reactor.

Method for gas-phase polymerization of alpha-olefin

PURPOSE: A gas-phase polymerization method is provided to efficiently remove polymerization reaction heat, and to increase the productivity of a polymer and a catalyst. CONSTITUTION: A gas-phase polymerization method comprises the steps of: supplying cycling gas including at least one kind of alpha-olefin and inert gas to a reactor(100); polymerizing the alpha-olefin with polyolefin in a two polymerization regions divided in a reactor; and discharging the polyolefin polymer from the reactor.

Process and the apparatus for the catalytic polymerisation in the gas phase

A process for the catalytic polymerisation in the gas-phase carried out in at least interconnected polymerisation zones, the process comprising feeding one or more monomers to said polymerisation zones in the presence of catalyst under reaction conditions and collecting the polymer product from said polymerisation zones (riser), in which process the growing polymer particles flow upward through one said polymerisation zones under fast fluidisation or transport conditions, leave said riser and enter another polymerisation zone (downcomer) through which they flow downward under the action of gravity, leave said downcomer and are reintroduced into the riser, thus establishing a circulation of polymer between the riser and the downcomer. An apparatus for the gas-phase catalytic polymerisation comprising a first vertical reactor (1), a second vertical reactor (2), the upper region of said reactor (1) being connected by a connecting part (3) to a solid gas separator (4) which is in turn connected to the upper region of said second reactor (2) the lower region of said second reactor (2) being connected to the lower region of said first reactor (1) by a connecting part (5) said solid gas separator (4) being connected through a recycle line (6) to one more points of reintroduction into said connecting part (5) or into said reactor (1).

Reactor Systems and Processes for Using the Same

A process for the polymerization of olefin's, including: introducing an olefin and a polymerization catalyst into a polymerization reactor to form a polyolefin, the polymerization reactor including: a fluidized bed region having a top and a bottom; and a motive bed region; wherein a first end of the motive bed region is fluidly connected to the top of the fluidized bed region; and wherein a second end of the motive bed region is fluidly connected to the bottom of the fluidized bed region; and wherein a diameter of the fluidized bed region is greater than a diameter of the motive bed region; circulating at least a portion of the olefin, the catalyst, and the polyolefin through the fluidized bed region and the motive bed region; maintaining a dense-phase fluidized bed within the fluidized bed region; recovering polyolefin from the fluidized bed region, is provided. A reactor system directed to the process is also provided.

Circulating Fluidized Bed Reactor

A continuous gas phase circulating bed reactor, including: a riser for contacting a catalyst and a first gas composition comprising an olefin to form a polyolefin under fast-fluidization regime or a dilute-phase pneumatic conveying regime conditions; a downer for contacting the catalyst and a second gas composition comprising an olefin to form additional polyolefin under fast fluidization regime or a dilute-phase pneumatic conveying regime conditions; and a transport section for conveying at least a portion of the catalyst, polyolefin, and additional polyolefin from the downer to the riser. Also disclosed is a polymerization process using such a circulating bed reactor.

Gas phase polymerization and reactor assembly comprising a fluidized bed reactor and an external moving bed reactor

The present invention relates to a reactor assembly for the catalytic polymerization of olefin monomer and optionally comonomer(s) comprising at least one fluidized bed reactor (1) and at least one moving bed reactor (2) adjacent to the fluidized bed reactor (1), wherein the moving bed reactor (2)comprises an inlet at the upper section of the moving bed reactor (2) which is directly connected to an outlet of the fluidized bed reactor (1), and an outlet at the lower section of the moving bed reactor (2) which is directly connected to an inlet of the fluidized bed reactor (1) by means of a conveying pipe (5), and said conveying pipe is provided with means (7) for pneumatically displacing polymer particles from said outlet of moving bed reactor (2) to said inlet of the fluidized bed reactor (1), which pneumatic displacing means (7) comprises an inlet for pneumatic gas to said conveying pipe (5), wherein the reactor assembly is characterized in that said conveying pipe (5) follows a horizontal or declining direction from said outlet of the moving bed reactor (2) to said inlet of the fluidized bed reactor (1), said conveying pipe (5) has a length of not longer than three times the diameter of the moving bed reactor (2). It also relates to a process for producing olefin polymers by catalytically polymerizing olefin monomer and optionally comonomer(s) in at least one interconnected fluidized bed reactor and the use of the reactor assembly for the production of an olefin polymer.

Process for the polymerization of olefins

The present invention relates to a process for the continuous preparation of polypropylene in a reactor from propylene and optionally ethylene and/or at least one other oolefin monomer, wherein the reactor comprises a fluidized bed, an expanded section located at or near the top of the reactor, a distribution plate located at the lower part of the reactor and an inlet for a recycle stream located under the distribution plate, wherein the process comprises - feeding a polymerization catalyst to the fluidized bed in the area above the distribution plate - feeding the propylene and the optional at least one other oolefin monomer to the reactor - withdrawing the polypropylene from the reactor - circulating fluids from the top of the reactor to the bottom of the reactor, wherein the circulating fluids are compressed using a compressor and cooled using a heat exchanger, resulting in a cooled recycle stream comprising liquid, and wherein the cooled recycle stream is introduced into the reactor using the inlet for the recycle stream wherein an alkane chosen from the group of iso-butane, n-butane, cyclopropane and mixtures thereof is added to the reactor and wherein the molar composition of the components in the recycle stream is chosen such that the dew temperature of the recycle stream at the reactor pressure is at least 0.10°C below the temperature of the reactor

Process for the polymerization of olefins

The present invention relates to a process for the continuous preparation of a polyolefin in a reactor from one or more α-olefin monomers of which at least one is ethylene or propylene, wherein the reactor comprises a fluidized bed, an expanded section located at or near the top of the reactor, a distribution plate located at the lower part of the reactor and an inlet for a recycle stream located under the distribution plate wherein the process comprises - feeding a polymerization catalyst to the fluidized bed in the area above the distribution plate - feeding the one or more α-olefin monomers to the reactor - withdrawing the polyolefin from the reactor - circulating fluids from the top of the reactor to the bottom of the reactor, wherein the circulating fluids are compressed using a compressor and subsequently cooled using a heat exchanger to form a cooled recycle stream comprising liquid, and wherein the cooled recycle stream is introduced into the reactor using the inlet for the recycle stream wherein a part of the cooled recycle stream is drawn to form a liquid comprising stream, wherein the liquid comprising stream is introduced into the expanded section during at least part of the polymerization process, and wherein the liquid comprising stream is brought into contact with at least part of the interior surface of the expanded section.

用于烯烃聚合的方法

本发明涉及一种用于在反应器中由一种或多种α‑烯烃单体连续制备聚烯烃的方法，所述α‑烯烃单体中的至少一种是乙烯或丙烯，其中所述反应器包括流化床、位于所述反应器的顶部处或附近的膨胀区段、位于所述反应器的下部部分的分配板和位于所述分配板下方的再循环流的入口，其中所述方法包括‑将聚合催化剂进料到所述分配板上方的区域中的流化床中‑将所述一种或多种α‑烯烃单体进料到所述反应器中‑从所述反应器中抽取出所述聚烯烃‑将流体从所述反应器的顶部循环至所述反应器的底部，其中所述循环流体使用压缩机压缩并且随后使用热交换器冷却以形成包含液体的冷却的再循环流，并且其中将所述冷却的再循环流使用所述再循环流的入口引入到所述反应器中，其中将所述冷却的再循环流的一部分抽取出以形成含液体流，其中在所述聚合方法的至少一部分期间将所述含液体流引入到所述膨胀区段中，并且其中使所述含液体流与所述膨胀区段的内表面的至少一部分接触。

Process for the polymerization of olefins

The present invention relates to a process for the continuous preparation of polypropylene in a reactor from propylene and optionally ethylene and/or at least one other oolefin monomer, wherein the reactor comprises a fluidized bed, an expanded section located at or near the top of the reactor, a distribution plate located at the lower part of the reactor and an inlet for a recycle stream located under the distribution plate, wherein the process comprises—feeding a polymerization catalyst to the fluidized bed in the area above the distribution plate—feeding the propylene and the optional at least one other oolefin monomer to the reactor—withdrawing the polypropylene from the reactor—circulating fluids from the top of the reactor to the bottom of the reactor, wherein the circulating fluids are compressed using a compressor and cooled using a heat exchanger, resulting in a cooled recycle stream comprising liquid, and wherein the cooled recycle stream is introduced into the reactor using the inlet for the recycle stream wherein an alkane chosen from the group of iso-butane, n-butane, cyclopropane and mixtures thereof is added to the reactor and wherein the molar composition of the components in the recycle stream is chosen such that the dew temperature of the recycle stream at the reactor pressure is at least 0.10° C. below the temperature of the reactor.

Process for the polymerization of olefins

The present invention relates to a process for the continuous preparation of a polyolefin in a reactor from one or more α-olefin monomers of which at least one is ethylene or propylene, wherein the reactor comprises a fluidized bed, an expanded section located at or near the top of the reactor, a distribution plate located at the lower part of the reactor and an inlet for a recycle stream located under the distribution plate wherein the process comprises—feeding a polymerization catalyst to the fluidized bed in the area above the distribution plate—feeding the one or more α-olefin monomers to the reactor—withdrawing the polyolefin from the reactor—circulating fluids from the top of the reactor to the bottom of the reactor, wherein the circulating fluids are compressed using a compressor and subsequently cooled using a heat exchanger to form a cooled recycle stream comprising liquid, and wherein the cooled recycle stream is introduced into the reactor using the inlet for the recycle stream wherein a part of the cooled recycle stream is drawn to form a liquid comprising stream, wherein the liquid comprising stream is introduced into the expanded section during at least part of the polymerization process, and wherein the liquid comprising stream is brought into contact with at least part of the interior surface of the expanded section.

用于烯烃聚合的方法

本发明涉及一种用于在反应器中由一种或多种α‑烯烃单体连续制备聚烯烃的方法，所述α‑烯烃单体中的至少一种是乙烯或丙烯，其中所述反应器包括流化床、位于所述反应器的顶部处或附近的膨胀区段、位于所述反应器的下部部分的分配板和位于所述分配板下方的再循环流的入口，其中所述方法包括‑将聚合催化剂进料到所述分配板上方的区域中的流化床中‑将所述一种或多种α‑烯烃单体进料到所述反应器中‑从所述反应器中抽取出所述聚烯烃‑将流体从所述反应器的顶部循环至所述反应器的底部，其中所述循环流体使用压缩机压缩并且随后使用热交换器冷却以形成包含液体的冷却的再循环流，并且其中将所述冷却的再循环流使用所述再循环流的入口引入到所述反应器中，其中将所述冷却的再循环流的一部分抽取出以形成含液体流，其中在所述聚合方法的至少一部分期间将所述含液体流引入到所述膨胀区段中，并且其中使所述含液体流与所述膨胀区段的内表面的至少一部分接触。

Reaktor zur durchführung rascher stark exothermer reaktionen und dessen verwendung

Es wird ein Rohrbündelreaktor (1) für rasche stark exotherme Reaktionen beschrieben. Dieser besteht aus einem Reaktorgehäuse (2) mit einem Bündel (3) von Rohren (6), die ggf. radial zu ihrer Längenausdehnung miteinander verbunden sind, als Reaktionszone, Eduktzuleitungen (4, 11), einem Produktauslaß (12) und einem Wärmetauscher (5) und ist dadurch gekennzeichnet, daß die Eduktzuleitungen (4) als in den Rohren (6) der Bündel (3) verlaufende und mit einer Vielzahl von Öffnungen (7) versehene Rohrleitungen (4a, 4b, 4c, 4d) ausgeführt sind, wobei die Öffnungen (7) in den Rohrleitungen (4a, 4b, 4c, 4d) über die ganze Länge oder einen Längenabschnitt der Reaktionszone verteilt sind.

Process and apparatus for the gas-phase polymerization of α-olefins

Process for gas-phase polymerization carried out in two interconnected polymerization zones, to which one or more α-olefins CH 2 ═CHR are fed in the presence of catalyst under reaction conditions and from which the polymer product is discharged. The process is characterized in that the growing polymer flows through a first polymerization zone under fast fluidization conditions, leaves said first zone and enters a second polymerization zone through which it flows in a densified form under the action of gravity, leaves said second zone and is reintroduced into the first polymerization zone, thus establishing a circulation of polymer around the two polymerization zones. The novel process allows olefins to be polymerized in the gas phase with high productivity per unit volume of the reactor without incurring the problems of the fluidized-bed technologies of the known state of the art.

Systems and methods for removing entrained particulates from gas streams, and reactor systems implementing the same

Various methods and systems for removing particulates from a cycle gas stream, e.g., in a reactor system, are provided. In certain embodiments, the methods are performed in conjunction with a polymerization reactor system such as a gas-phase reactor system.

Reactor systems and processes for using the same

A process for the polymerization of olefin's, including: introducing an olefin and a polymerization catalyst into a polymerization reactor to form a polyolefin, the polymerization reactor including: a fluidized bed region having a top and a bottom; and a motive bed region; wherein a first end of the motive bed region is fluidly connected to the top of the fluidized bed region; and wherein a second end of the motive bed region is fluidly connected to the bottom of the fluidized bed region; and wherein a diameter of the fluidized bed region is greater than a diameter of the motive bed region; circulating at least a portion of the olefin, the catalyst, and the polyolefin through the fluidized bed region and the motive bed region; maintaining a dense-phase fluidized bed within the fluidized bed region; recovering polyolefin from the fluidized bed region, is provided. A reactor system directed to the process is also provided.

Process and apparatus for the gas-phase polymerization of alpha-olefins

Process for gas-phase polymerization carried out in two interconnected polymerization zones, to which one or more α-olefins CH 2 =CHR are fed in the presence of catalyst under reaction conditions and from which the polymer product is discharged. The process is characterized in that the growing polymer flows through a first polymerization zone under fast fluidization conditions, leaves said first zone and enters a second polymerization zone through which it flows in a densified form under the action of gravity, leaves said second zone and is reintroduced into the first polymerization zone, thus establishing a circulation of polymer around the two polymerization zones. The novel process allows olefins to be polymerized in the gas phase with high productivity per unit volume of the reactor without incurring the problems of the fluidized-bed technologies of the known state of the art.

Systems and methods for removing entrained particulates from gas streams, and reactor systems implementing the same

Various methods and systems for removing- particulates from a cycle gas stream, e.g., in a reactor system, are provided. In certain embodiments, the methods are performed in conjunction with a polymerization reactor system such as a gas-phase reactor system for production of polyolef in polymers. The methods comprise the step of compressing a gas stream having particulates entrained therein.

用于从气流中移除夹带的颗粒的系统和方法以及实现其的反应器系统

本发明提供了用于从如反应器系统中的循环气流中移除微粒的各种方法和系统。在特定的实施例中，与聚合反应器系统结合来执行该方法，例如用于产生聚合物中的聚烯烃的气相反应器系统。该方法包括对气流进行压缩的步骤，该气流具有进入其中的微粒。

Systems and Methods for Removing Entrained Particulates from Gas Streams, and Reactor Systems

Various methods and systems for removing particulates from a cycle gas stream, e.g., in a reactor system, are provided. In certain embodiments, the methods are performed in conjunction with a polymerization reactor system such as a gas-phase reactor system for production of polyolefin polymers. The methods comprise the step of compressing a gas stream having particulates entrained therein.

Systems and methods for removing entrained particulates from gas streams, and reactor systems

Various methods and systems for removing particulates from a cycle gas stream, e.g., in a reactor system, are provided. In certain embodiments, the methods are performed in conjunction with a polymerization reactor system such as a gas-phase reactor system.

Gas-phase polymerization of alpha-olefin

A method for preparing polyolefin from alpha-olefin with high productivity using an internal circulating fluidized bed polymerization reactor is disclosed. The method for gas-phase polymerization of alpha-olefin comprising the steps of: supplying circulation gas including one or more alpha-olefins and inert gas into a polymerization reactor; polymerizing the alpha-olefin to polyolefin in two separated polymerization areas in the polymerization reactor; and discharging produced polyolefin from the polymerization reactor. The polymerization reactor is divided into the two polymerization areas by a draft tube, and an inside of the draft tube forms a riser where growing polyolefin polymers move up in fast fluidization, and an outside of the draft tube forms an annulus where the polyolefin polymers passing the riser move down by gravity, and the polyolefin polymers passing the annulus are introduced to a lower part of the riser again, so that the polyolefin polymers are polymerized during circulating between the riser and the annulus.

Fluidized bed system and method for powder fluidization using the same

본 발명의 일 구현예는 유동층 반응기; 상기 유동층 반응기와 연결라인을 통해 연결되어 가동 상태의 상기 유동층 반응기로부터 분체를 채취한 후, 분체의 온도 및 압력을 측정하여 최소유동화속도를 산출하고, 측정이 종료된 분체를 유동층 반응기로 재주입하는 최소유동화속도 측정장치; 및 상기 유동층 반응기 및 상기 최소유동화속도 측정장치에 각각 전기적으로 연결되며, 상기 최소유동화속도 측정 장치로부터 산출된 최소 유동화속도에 따라 유동층 반응기 시스템의 유량을 조절하는 시스템 유량 제어장치; 를 포함하는 유동층 반응기 시스템에 관한 것이다. One embodiment of the present invention is a fluidized bed reactor; After collecting powder from the fluidized bed reactor in operation connected to the fluidized bed reactor through a connection line, measuring the temperature and pressure of the powder to calculate the minimum fluidization rate, and re-injecting the finished powder into the fluidized bed reactor Minimum fluidization rate measuring device; and a system flow control device electrically connected to the fluidized bed reactor and the minimum fluidization rate measuring device, respectively, and adjusting the flow rate of the fluidized bed reactor system according to the minimum fluidization rate calculated from the minimum fluidization rate measuring device. It relates to a fluidized bed reactor system comprising a.

Gas-phase polymerisation of alpha-olefin

FIELD: chemistry.SUBSTANCE: invention relates to a method for gas-phase polymerisation of alpha-olefin and an internal circulation fluidised-bed polymerisation reactor for realising said method. The method for gas-phase polymerisation of alpha-olefin involves cycled gas containing one or more alpha-olefins and an inert gas into a polymerisation reactor; polymerising the alpha-olefin to polyolefin in the presence of a catalyst in two separate polymerisation zones in the polymerisation reactor; and removing the obtained polyolefin from the polymerisation reactor. The internal circulation fluidised-bed polymerisation reactor has one outlet pipe which is mounted in the reactor, in which at least one through-hole is formed, said through-hole connecting the inner and outer parts of the outlet pipe, and a gas-distributing plate which is mounted with inclination from the outer part of the outlet pipe to the side wall of the polymerisation reactor. The polymerisation reactor is divided into two polymerisation zones by the outlet pipe and the inner part of the outlet pipe forms a riser in which polyolefins rise during fast fluidisation. The outer part of the outlet pipe forms an annular gap in which polyolefins passing through the riser descent under gravity. Polyolefins passing through the annular gap are again fed into the bottom part of the riser and are polymerised during circulation between the riser and the annular gap. The alpha-olefin is a compound of formula CH=CHR, where R is a hydrogen atom or a hydrocarbon radical with 1-12 carbon atoms.EFFECT: highly efficient method and reactor for gas-phase polymerisation of alpha-olefin.19 cl, 5 tbl, 5 dwg, 17 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2 490 281 (13) C2 (51) МПК C08F 2/34 (2006.01) C08F 10/00 (2006.01) C08F 210/16 (2006.01) B01J 19/24 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (21)(22) Заявка: 2011133354/04, 19.04.2011 (24) Дата начала отсчета срока действия ...

Reactor for a gas-phase olefin polymerization

A reactor for carrying out a gas-phase olefin polymerization in the presence of a polymerization catalyst, the reactor comprising at least a first polymerization zone adapted and arranged for growing polymer particles to flow upward under fast fluidization or transport conditions and at least a second polymerization zone adapted and arranged for the growing polymer particles to flow downward; and at least one set of bars for introducing feedstock and/or a barrier stream into the reactor, wherein each bar comprises a hollow space along the length of the bar and has a particle deviating top and each bar has openings arranged along the bottom half of the periphery of the bar.

Multi-zone reactor for continuous polymerization of alpha olefin monomers

The invention relates to a multi-zone reactor for the continuous fluidized bed polymerization of one or more α-olefin monomers of which at least one is ethylene or propylene, which multi-zone reactor is operable in condensed mode, which multi-zone reactor comprises a first zone, a second zone, a third zone, a fourth zone and a distribution plate, wherein the second zone contains an inner wall, wherein the third zone contains an inner wall, wherein at least part of the inner wall of the third zone is either in the form of a gradually increasing inner diameter or a continuously opening cone, wherein the diameter or the opening increases in the vertical direction towards the top of the multi-zone reactor, wherein the largest diameter of the inner wall of the third zone is larger than the largest diameter of the inner wall of the second zone.

Elimination of polymer fouling in fluidized bed gas-phase fines recovery eductors

An eductor, a process and apparatus for gas phase polymerization of olefins in a polymerization reactor are disclosed. The process and apparatus employ an eductor which has an inlet which makes a bend of less than about 90° toward the outlet after entering the mixing chamber of the eductor.