УЛУЧШЕННАЯ КОНСТРУКЦИЯ РЕАКТОРА ОЛИГОМЕРИЗАЦИИ/ТРИМЕРИЗАЦИИ/ТЕТРАМЕРИЗАЦИИ ЭТИЛЕНА

FIELD: technological processes. SUBSTANCE: invention relates to a method for oligomerization of an olefin monomer, involving periodic or continuous introduction of an olefin monomer, and intermittent or continuous introduction of catalytic system or components of catalyst system into reaction mixture of reaction system; oligomerization of the olefin monomer in the reaction mixture to form an oligomer product; and a periodic or continuous outlet of the reaction system effluent containing the oligomer product from the reaction system, wherein the reaction system contains a total volume of the reaction mixture of the reaction system; and a heat exchange portion of the reaction system, comprising a volume of the heat exchange reaction mixture and a total heat exchange surface area, providing an indirect thermal contact between the reaction mixture and the heat carrier; wherein ratio of total area of heat exchange surface to total volume of reaction mixture of reaction system is in range from 1.25 inch −1 to 5 inch −1 ; and wherein the rate of output of the oligomer product from the reaction system ranges from 1.5 (lb)(hr −1 )(gallon −1 ) to 6.0 (lb)(hr −1 )(gallon −1 ). Invention also relates to a reaction system and a version of the method for oligomerization of an olefin monomer. EFFECT: technical result is improved oligomerization of olefins due to improved reaction systems. 34 cl, 10 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 738 407 C2 (51) МПК C07C 2/08 (2006.01) C07C 2/22 (2006.01) C07C 2/32 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК C07C 2/08 (2020.08); C07C 2/22 (2020.08); C07C 2/32 (2020.08) (21)(22) Заявка: 2018109132, 13.09.2016 (24) Дата начала отсчета срока действия патента: (73) Патентообладатель(и): ШЕВРОН ФИЛЛИПС КЕМИКАЛ КОМПАНИ ЭлПи (US) Дата регистрации: 11.12.2020 18.09.2015 US 14/858,526; 18.09.2015 US 14/858,588 (43) Дата публикации заявки: 18.10.2019 Бюл. № 29 (45) Опубликовано: 11 ...

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.

Process for hydrodemetallation of hydrocarbon oils

Hydrocarbon oils 11, particularly petroleum residua, containing 20-2000 ppm by weight of metals and substantial amounts of sulfur are effectively catalytically hydrodemetallated by forming a three- phase slurry of said oil with hydrogen 19 and a solid hydrodemetallation catalyst 17 of 50 to 300 mesh particle size and passing the slurry through an elongated tubular reactor 25 sized to provide a residence time of from 1.5 to 10 minutes and a liquid flow velocity of from 1 to 15 ft. per second at a temperature of 750 DEG to 900 DEG F (399-482 DEG C) and a pressure of 1000 to 2750 psig (6992-19058 KPa) and, thereafter, isolating the treated oil from the catalyst.

FLUIDIZABLE CATALYST REGENERATION PROCESS AND APPARATUS

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

Zone reactor incorporating reversible hydrogen halide capture and release

Zone reactor incorporating reversible hydrogen halide capture and release

Zone reactor incorporating reversible hydrogen halide capture and release

Device for collecting solar energy

The invention relates to a device for collecting solar energy (1), characterized in that it includes at least one solar receiver (2) including at least one suspension of solid particles fluidized by a gas, each suspension circulating between an inlet and an outlet of the receiver (2), wherein the volume of particles is between 40% and 55% of the volume of the suspension, and the average size of the particles is between 20 and 150 µm.

Temperature controlled in situ wax purification

CONVERTING OXYGENATES TO LIQUID HYDROCARBONS

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

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

PROCESS FOR HYDRODEMETALLATION OF HYDROCARBON OILS SUCH AS PETROLEUM RESIDUA

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

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

Process for catalytic treatment of a liquid feedstock and device for its use

A liquid feedstock of a catalytic process, initially contained in a storage vessel (14), is drawn off progressively from this storage vessel and conveyed into a reactor containing a stationary bed of catalyst produced, for example, by means of catalyst cartridges (16) arranged in parallel (Fig. 2). From there it is returned to the storage vessel (14). The composition of the liquid phase contained in the storage vessel therefore changes in the course of time until the reaction is finished. This technique makes it possible to carry out, using separate batches, operations such as hydrogenation, dehydrogenation, oligomerisation and polymerisation. ...

Batch hydrogenation of furfurol to furfuryl alcohol under pressure - using copper chromite catalyst and lower pressure than usual, giving high yield

Discontinuous hydrogenation of furfurol (I) to furfuryl alcohol (II) under pressure with Cu chromite catalysts (II) suspended in (I) is carried out for 30-45 min. at 184-210 deg. C and a circulating H2 pressure of 20-50 bar. Appts. has a gas introduction system inside the reactor, which consists of a tube extending from the gas space above the liq. level and rough this, ending in a rotary gas distributor near the bottom of the reactor; and also a heat exchanger inside the reactor. There pref. is also a control cycle to keep the pressure in the reactor constant by regulating the H2 supply according to the pressure in the reactor. USE/ADVANTAGE - Hydrogenation is carried out at much lower pressure than usual and gives a high (II) yield. The process is suitable for operation on the technical scale.

PROCEDURE FOR THE DRY CLEANING OF FLUE GASES.

ЗОННЫЙ РЕАКТОР С ОБРАТИМЫМ ПОГЛОЩЕНИЕМ И ВЫСВОБОЖДЕНИЕМ ГАЛОГЕНОВОДОРОДОВ

Предложены усовершенствованный способ и зонный реактор для конверсии углеводородного сырья в высшие углеводороды. Первая зона реактора содержит как материал, способный высвобождать галогеноводород (НХ), так и катализатор образования углерод-углеродной связи; вторая зона первоначально является пустой или содержит катализатор галогенирования и/или оксигалогенирования; и третья зона содержит как катализатор образования углерод-углеродной связи, так и материал, способный поглощать НХ. В первую зону вводят воздух или кислород, углеводородное сырьё вводят во вторую зону, а продукты образуются в третьей зоне. НХ, образовавшийся в течение реакции, обратимо поглощается и высвобождается в зонах 1 и 3.

THERMAL INTEGRATION

РЕАКТОР С ПСЕВДООЖИЖЕННЫМ СЛОЕМ, ЕГО ПРИМЕНЕНИЕ И СПОСОБ ЭНЕРГОНЕЗАВИСИМОГО ГИДРИРОВАНИЯ ХЛОРСИЛАНОВ

Изобретение касается устройства, его применения и способа в основном энергонезависимого непрерывного получения хлорсиланов, в частности, трихлорсилана в качестве промежуточного продукта для получения высокочистого кремния.

gazozhidko holistic and reactor and method of realization of reaction in a gas/liquid st

Газожидкостной реактор, включающий: (а) слой насыпного катализатора и устройства для подачи свежего сырья и рецикла потока, по меньшей мере, частично превращенного жидкого продукта в указанный насыпной слой катализатора; (b) устройства для отбора потока, по меньшей мере, частично превращенного жидкого продукта из указанного слоя насыпного катализатора и рецикла, по меньшей мере, его части на стадию (а); (с) вспомогательный слой катализатора, проходящий практически вертикально через слой насыпного катализатора, и устройства для подачи рецикла потока, по меньшей мере, частично превращенного жидкого продукта только в указанный вспомогательный слой катализатора; и (d) разделительную стенку между указанным слоем насыпного катализатора и вспомогательным слоем катализатора. A gas-liquid reactor, comprising: (a) a bed of bulk catalyst and a device for supplying fresh raw materials and recycling a stream of at least partially converted liquid product into said bulk bed of catalyst; (b) devices for collecting a stream of at least partially converted liquid product from said layer of bulk catalyst and recycling at least a portion of it to stage (a); (c) an auxiliary catalyst bed extending almost vertically through the bulk catalyst bed and devices for supplying a recycle stream of at least partially converted liquid product to said auxiliary catalyst bed only; and (d) a separation wall between said bulk catalyst bed and an auxiliary catalyst bed.

LIQUID/GAS REACTOR AND PROCESS FOR GAS/LIQUID REACTION

ЗОННЫЙ РЕАКТОР С ОБРАТИМЫМ ЗАХВАТЫВАНИЕМ И ВЫСВОБОЖДЕНИЕМ ГАЛОГЕНОВОДОРОДОВ

В изобретении предложен способ и зонный реактор для конверсии углеводородного сырья в высшие углеводороды. Первая зона в реакторе содержит как материал, способный высвобождать галогеноводород (HX), так и катализатор углерод-углеродного присоединения; вторая зона первоначально является пустой или содержит катализатор галогенирования и/или оксигалогенирования и третья зона содержит как катализатор углерод-углеродного присоединения, так и материал, способный захватывать HX. В первую зону вводят воздух или кислород, во вторую зону вводят сырье, а в третьей зоне образуются продукты. НХ, полученный в ходе реакции, обратимо захватывается и высвобождается в зонах 1 и 3.

Reactor with recycle liquid distributor and use thereof

OPTIMIZED METERING OF REACTANTS FOR A PROCESS FOR PREPARING AROMATIC AMINES BY HYDROGENATION OF NITROAROMATICS

A PROCESS FOR THE HYDROGENATION OF AROMATICS IN A HYDROCARBON FEEDSTOCK THAT CONTAINS A THIOPHENEIC COMPOUND

A process for the hydrogenation of aromatics contained in a hydrocarbon feedstock and for the bulk sulfiding of a nickel-based catalyst to enhance the activity and catalyst life thereof. The process includes passing at the start-of-run a dispersed hydrocarbon feedstock through a bed of the nickel-based catalyst at an elevated temperature effective in promoting the bulk sulfiding the nickel-based catalyst so as to thereby increase its activity or catalytic life, or both. © KIPO & WIPO 2009 ...

placa de leito com grade de suporte para um reator de leito fluidizado e modelagem da mesma

um modelo fluidodinâmico com ao menos 5 milhões de células da porção de um reator de fase gasosa da saída do condensador à metade do diâmetro do rea-tor acima da placa de leito é útil para determinar o design da superfície inferior ou estrutura de suporte para uma placa a fim de minimizar a aglomeração de líquido abaixo e acima da placa de leito quando operando em modo de condensação. A fluid dynamic model with at least 5 million cells from the portion of a condenser outlet gas phase reactor at half the diameter of the reactor above the bed plate is useful for determining the design of the bottom surface or support structure for a plate to minimize liquid agglomeration below and above the bed plate when operating in condensing mode.

APARELHO E PROCESSO APERFEICOADOS PARA REGENERAR UM CATILISADOR FLUIDO CONTAMINADO COM COQUE

Patent RU2018109132A3

РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2018 109 132 A (51) МПК C07C 2/08 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21)(22) Заявка: 2018109132, 13.09.2016 (71) Заявитель(и): ШЕВРОН ФИЛЛИПС КЕМИКАЛ КОМПАНИ ЭлПи (US) Приоритет(ы): (30) Конвенционный приоритет: 18.09.2015 US 14/858,526; 18.09.2015 US 14/858,588 (72) Автор(ы): КРЕЙШЕР Брюс (US) (85) Дата начала рассмотрения заявки PCT на национальной фазе: 18.04.2018 US 2016/051501 (13.09.2016) (87) Публикация заявки PCT: R U Адрес для переписки: 119019, Москва, Гоголевский б-р, 11, этаж 3, "Гоулинг ВЛГ (Интернэшнл) Инк.", Угрюмов Владислав Михайлович (54) УЛУЧШЕННАЯ КОНСТРУКЦИЯ РЕАКТОРА ОЛИГОМЕРИЗАЦИИ/ТРИМЕРИЗАЦИИ/ТЕТРАМЕРИЗАЦИИ ЭТИЛЕНА (57) Формула изобретения 1. Способ, включающий: периодическое или непрерывное введение олефинового мономера, и периодическое или непрерывное введение каталитической системы или компонентов каталитической системы в реакционную смесь реакционной системы; олигомеризацию олефинового мономера в реакционной смеси с образованием олигомерного продукта; и периодический или непрерывный вывод выходящего потока реакционной системы, содержащего олигомерный продукт, из реакционной системы, причем реакционная система содержит общий объем реакционной смеси реакционной системы; и теплообменный участок реакционной системы, содержащий объем теплообменной реакционной смеси и общую площадь поверхности теплообмена, обеспечивающую непрямой термоконтакт между реакционной смесью и теплоносителем; при этом соотношение общей площади теплообменной поверхности к общему объему реакционной смеси реакционной системы находится в диапазоне от 0,75 дюйм-1 до 5 дюйм-1; и при том, что скорость вывода олигомерного продукта из реакционной системы Стр.: 1 A 2 0 1 8 1 0 9 1 3 2 A WO 2017/048705 (23.03.2017) 2 0 1 8 1 0 9 1 3 2 (86) Заявка PCT: R U (43) Дата публикации заявки: 18.10.2019 Бюл. № 29 A 2 0 1 8 1 0 9 1 3 2 A R U 2 0 1 8 1 0 9 1 3 2 Стр.: 2 R U составляет между от 1,0 ...

A fuel processing system for generating hydrogen

A fuel processing system (10) comprises a combined reformer and hydrogen separator (32) which is supplied with methanol from a supply tank (12), water from a tank (14) and oxygen from a supply (16). The combined reformer and hydrogen separator (32) has two chambers (40, 42) separated by a hydrogen permeable membrane (38). The reactants are supplied into one chamber (40) and react on a catalyst (44) to produce hydrogen and byproduct gases. The hydrogen passes through the membrane (38) into the other chamber (42) and is supplied to a fuel cell. The byproduct gases are recycled via pipes (52,68) to enter the first chamber (40) of the reformer with the reactants. Additionally a device (54) removes soluble byproduct gases from the gases being recycled to the reformer. <IMAGE>

PROCEDURE FOR THE CATALYTIC EXECUTION OF ALDOLKONENSATIONEN OF MEANS MULTI-PHASE REACTION

PROCEDURE FOR STARTING AND FOR THE CONTROLLING OF THE REGENERATION CRACKING CATALYSTS POLLUTED BY WITH COKE

METHOD OF HEAT TREATING A MATERIAL

HEAT INTEGRATION

A PROCESS FOR THE HYDROGENATION OF AROMATICS IN A HYDROCARBON FEEDSTOCK THAT CONTAINS A THIOPHENEIC COMPOUND

A process for the hydrogenation of aromatics contained in a hydrocarbon feedstock and for the bulk sulfiding of a nickel-based catalyst to enhance the activity and catalyst life thereof. The process includes passing at the start-of-run a dispersed hydrocarbon feedstock through a bed of the nickel-based catalyst at an elevated temperature effective in promoting the bulk sulfiding the nickel-based catalyst so as to thereby increase its activity or catalytic life, or both.

PROCESS FOR FEEDING CATALYST TO FLUIDIZED BED FOR VAPOR PHASE POLYMERISATION

A process for feeding a powdery catalyst with a gas intermittently to a high-pressure fluidized bed reactor for the vapor phase polymerisation of olefin, wherein the cross section of a catalyst feed pipe is reduced midway through the pipe to thereby make continuous catalyst feed possible and prevent the formation of a lump polymer.

AUTOTHERMAL REACTOR FOR CONDUCTING GAS-PHASE DEHYDROGENATION

СИСТЕМА УТИЛИЗАЦИИ ТЕПЛА

Предложена система утилизации тепла для отведения реакционного тепла из реактора ЕС-1 и получения охлажденной жидкости для использования одной или более потребляющими установками в каталитическом способе получения ЕС из ЕО для конверсии в MEG, при этом система содержит устройство охлаждения реактора ЕС-1, выполненное с возможность отведения тепла из реактора ЕС-1, промежуточный контур, сообщающийся с устройством охлаждения реактора ЕС-1 и с абсорбционной холодильной установкой и выполненный с возможностью пропускания промежуточной жидкости между ними, причем абсорбционная холодильная установка выполнена с возможностью обеспечения получения охлажденной жидкости, и контур охлажденной жидкости, выполненный с возможностью пропускания охлажденной жидкости, полученной в абсорбционной холодильной установке для использования одной или более потребляющими установками, при этом система выполнена так, что абсорбционная холодильная установка использует тепло, полученное в реакторе ЕС-1, для получения ...

Optimized metering of reactants for a process for preparing aromatic amines by hydrogenation of nitroaromatics

The invention relates to a process for preparing aromatic amines by hydrogenating corresponding nitroaromatics with hydrogen, and also to apparatus suitable for this purpose. The invention relates more particularly to a process for preparing tolylenediamine (TDA) by hydrogenation of dinitrotoluene (DNT).

Process of adjustment of catalytic reforming

processo para preparar aminas aromáticas, e, aparelho para a execução do processo.

DEVICE FOR COLLECTING SOLAR ENERGY

The invention relates to a device for collecting solar energy (1), characterized in that it includes at least one solar receiver (2) including at least one suspension of solid particles fluidized by a gas, each suspension circulating between an inlet and an outlet of the receiver (2), wherein the volume of particles is between 40% and 55% of the volume of the suspension, and the average size of the particles is between 20 and 150 µm.

TEMPERATURE CONTROLLED IN SITU WAX PURIFICATION

A hydrocarbon wax product from a HCS slurry comprising liquid synthesis product and catalyst particles is purified by circulating the slurry from a synthesis zone with a first temperature through a treatment zone with a second temperature in which a hydrogen-containing treatment gas contacts the slurry. The gas treatment removes impurities from the hydrocarbon wax product and also removes catalyst de-activating species which may be present in the slurry. Purified wax product is separated and removed from the treated slurry via wax withdrawal means. This avoids or minimizes the need for further treating the wax product. Remaining treated slurry may be returned to the synthesis zone.

Ethylene separation with pressure swing adsorption

A process for component separation in a polymer production system comprising: (a) separating a polymerization product into a gas stream and a polymer stream; (b) processing the gas stream in distillation columns to yield a light hydrocarbon stream (LHS) comprising ethylene and ethane; (c) contacting LHS with a purged hydrocarbon adsorber to yield a loaded hydrocarbon adsorber and a non-adsorbed gas stream, wherein ethane is adsorbed by the purged hydrocarbon adsorber at a first pressure to yield adsorbed ethane, and wherein the non-adsorbed gas stream comprises recovered ethylene; (d) contacting the loaded hydrocarbon adsorber with a sweeping gas stream at a second pressure to yield an unloaded hydrocarbon adsorber and a recovered adsorbed gas stream comprising the sweeping gas stream and desorbed ethane; and (e) contacting the unloaded hydrocarbon adsorber with the sweeping gas stream at the first pressure to yield the purged hydrocarbon adsorber and a spent sweeping gas.

GAS-GAS HEAT EXCHANGER

Gas-gas type heat exchanger using the principle of interconnected fluidized beds. It comprises a cylindrical or polygonal vertical tubular container which is vertically and radially divided into at least four adjacent compartments communicating between each other (1, 2, 3, 4) of which at least two adjacent compartments form a cold part (1, 2) and comprising at least one cold gas discharge (7) and at least two adjacent compartments form a so called hot part and comprising at least one hot gas discharge (8). Each compartment contains a fluidized bed which consists of solid material in suspension in one of the hot or cold gases involved in the heat exchange. In the circulation direction of the fluidized solids, a high speed fluidized bed (1, 3) is followed by a low speed fluidized bed (2, 4) and the latter is followed by a high speed fluidized bed, a high speed fluidized bed (1, 3) which may overflow by the top into the next low speed fluidized bed (2, 4) and a low speed fluidized bed (2, ...

An improved method of temperature control in chemical reactions employing powdered catalytic material

The temperature of a fluidized catalytic exothermic reaction is controlled by continuously adding a powdered inert material cooled to a temperature not exceeding 350 DEG F. below the reaction temperature and in sufficient quantity to maintain the reaction temperature at a desired level, the said inert material being added at least in part to a lower portion of the catalyst bed, continuously removing by elutriation the inert material substantially free from the catalyst from an upper portion of the catalyst bed, cooling the so removed inert material to the above extent and returning it to the catalyst bed. The inert material is of smaller size and lower specific gravity than the catalyst, and is cooled by contact with a vaporizable liquid, preferably water. In an example, the process is applied to a Fischer-Tropsch synthesis catalyst of iron having a particle size of 5 to 300 microns. Inert materials specified include alumina, fuller's earth, clay and silica gel of 1 to 50 microns particle ...

PROCEDURE FOR THE DRY CLEANING OF FLUE GASES.

PROCEDURE FOR STARTING AND FOR THE CONTROLLING OF THE REGENERATION CRACKING CATALYSTS POLLUTED BY WITH COKE

HEAT INTEGRATION

AUTOTHERMAL STEAM REFORMING PROCESS

FLUID CATALYST REGENERATION PROCESS AND APPARATUS

PROCESS FOR CONVERTING OXYGENATES INTO LIQUID HYDROCARBONS

PROCESS FOR CONVERTING OXYGENATES INTO LIQUID HYDROCARBONS In a process for converting oxygenated feedstock, such as methanol and dimethyl ether into liquid hydrocarbons, in which the feedstock is first contacted with a zeolite catalyst to produce C2-C4 olefins and C5+ hydrocarbons, and in which C3+ olefins are then contacted with oligomerization catalyst comprising medium-pore, shape-selective acidic zeolite at increased pressure to produce gasoline and/or distillate liquids, lower alkenes in the form of ethene and/or olefinic gasoline are recycled to the first catalyst stage.

TEMPERATURE CONTROLLED IN SITU WAX PURIFICATION

A hydrocarbon wax product from a HCS slurry comprising liquid synthesis product and catalyst particles is purified by circulating the slurry from a synthesis zone with a first temperature through a treatment zone with a second temperature in which a hydrogen-containing treatment gas contacts the slurry. The gas treatment removes impurities from the hydrocarbon wax product and also removes catalyst de-activating species which may be present in the slurry. Purified wax product is separated and removed from the treated slurry via wax withdrawal means. This avoids or minimizes the need for further treating the wax product. Remaining treated slurry may be returned to the synthesis zone. © KIPO & WIPO 2007 ...

DEVICE AND PROCESS PERFECTED TO REGENERATE A CONTAMINATED FLUID CATILISADOR WITH COKE

ТЕПЛООБМЕННИК, ВКЛЮЧАЮЩАЯ ТЕПЛООБМЕННИК РЕАКТОРНАЯ СИСТЕМА И СПОСОБ ТЕРМОСТАТИРОВАНИЯ РЕАКТОРА

В заявке описан теплообменник (1), включающий пучок по меньшей мере из двух трубок (3) теплообменника, причем пучок (3) трубок теплообменника размещен вертикально и снизу закрыт трубной решеткой (31) теплообменника, кожух (5) теплообменника, окружающий пучок трубок (3) теплообменника, причем пучок трубок (3) теплообменника омывается в кожухе (5) теплообменника жидким теплоносителем (7), крышку (9) теплообменника, закрывающую кожух (5) теплообменника сверху, днище (11) теплообменника, закрывающее кожух (5) теплообменника снизу, питающий трубопровод (13), предназначенный для подачи теплоносителя (7) в кожух (5) теплообменника (1), предусмотренный на кожухе (5) теплообменника питающий трубопровод (13), предназначенный для подачи теплоносителя (7) в теплообменник (1), и расположенный вблизи крышки (9) теплообменника патрубок снятия аварийной нагрузки (17). Теплообменник (1) отличается тем, что он снабжен расположенным вблизи днища (11) теплообменника устройством безопасности (19). Кроме того ...

Установка дегидрирования этилбензола для получения стирола и соответствующий способ

VERFAHREN ZUR ANREICHERUNG VON PROPEN-ÄTHER-MISCHUNGEN IN EINEM KATALYSATOR-WIRBELBETTREAKTOR.

VERFAHREN ZUR ANREICHERUNG VON PROPEN-ÄTHER-MISCHUNGEN IN EINEM KATALYSATOR-WIRBELBETTREAKTOR.

Wärmetauscher, Reaktoranordnung umfassend diesen Wärmetauscher und Verfahren zum Temperieren eines Reaktors

Die vorliegende Erfindung bezieht sich auf einen Wärmetauscher (1), der ein Bündel von zumindest zwei Wärmetauscherrohren (3), wobei das Bündel von Wärmetauscherrohren (3) vertikal ausgerichtet ist und nach unten von einem Wärmetauscherrohrboden (31) abgeschlossen wird, ein das Bündel von Wärmetauscherrohren (3) umgebendes Wärmetauschergehäuse (5), wobei das Bündel von Wärmetauscherrohren (3) in dem Wärmetauschergehäuse (5) von einem flüssigen Wärmeträger (7) umspült wird, eine das Wärmetauschergehäuse (5) nach oben abschließende Wärmetauscherhaube (9), einen das Wärmetauschergehäuse (5) nach unten abschließenden Wärmetauscherboden (11), einen am Wärmetauschergehäuse (5) vorgesehenen Zulauf (13) für den Wärmeträger (7) in den Wärmetauscher (1), einen am Wärmetauschergehäuse (5) vorgesehenen Ablauf (15) für den Wärmeträger (7) aus dem Wärmetauscher (1) und ein Notentlastungsstutzen (17), der in der Nähe der Wärmetauscherhaube (9) angeordnet ist, umfasst. Der Wärmetauscher (1) ist dadurch ...

VERFAHREN ZUM ANFAHREN UND ZUR STEUERUNG DER REGENERATION VON MIT KOKS VERUNREINIGTEN KRACKKATALYSATOREN

METHOD FOR MAKING FUNCTION AN INCINERATOR BED HAS FLUIDIZES, AND MEANS FOR THE IMPLEMENTATION OF THIS PROCESS

PROCESS FOR THE ESTERIFICATION OF TEREPHTHALIC ACID

CATALYTIC PROCESS OF TREATMENT Of a WATER LOAD AND DEVICE FOR SA IMPLEMENTED

PROCEEDED OF REGENERATION Of a CATALYST USES CONTAINING COKE

PROCESS FOR THE ESTERIFICATION OF TEREPTHALIC ACID

INSTALLATION AND PROCESS FOR the REGENERATION Of a CATALYST

Le générateur représenté comprend une zone de combustion 1 disposée verticalement, en combinaison avec une zone 2 d'extraction de chaleur. Le catalyseur contaminé par du coke pénètre dans le régénérateur par une conduite 4 après avoir franchi une vannè de commande 5. Du gaz de régénération pénètre dans le système par une conduite 3 et se combine avec du catalyseur contaminé par du coke se trouvant dans la conduite 4 et avec du catalyseur régénéré se trouvant dans une conduite 20 avant de sortir par un dispositif distributeur 6 situé à la partie inférieure de la zone de combustion 1. Un mélange de gaz de régénération, de catalyseur régénéré et de catalyseur contaminé sort du dispositif de distribution 6 et monte dans la zone de combustion 1. The generator shown comprises a combustion zone 1 arranged vertically, in combination with a heat extraction zone 2. Catalyst contaminated with coke enters the regenerator through line 4 after passing through a control valve 5. Regeneration gas enters the system through line 3 and combines with coke contaminated catalyst in line. 4 and with regenerated catalyst being in a pipe 20 before leaving through a distributor device 6 located at the lower part of the combustion zone 1. A mixture of regeneration gas, regenerated catalyst and contaminated catalyst comes out of the combustion device. distribution 6 and rises in combustion zone 1.

에틸렌 올리고머화/삼량체화/사량체화 반응기의 개선된 설계

... 방법은 반응 시스템 내의 반응 혼합물 중에 올레핀 단량체를 주기적으로 또는 연속적으로 도입하고, 촉매 시스템 또는 촉매 시스템 성분을 주기적으로 또는 연속적으로 도입하는 단계, 상기 반응 혼합물 내에서 상기 올레핀 단량체를 올리고머화시켜 올리고머 생성물을 형성하는 단계, 및 상기 올리고머 생성물을 포함하는 반응 시스템 유출물을 반응 시스템으로부터 주기적으로 또는 연속적으로 방출시키는 단계를 포함한다. 상기 반응 시스템은 전체 반응 혼합물 체적, 및 교환 반응 혼합물 체적 및 상기 반응 혼합물과 열 교환 매질 사이의 간접적인 열 접촉을 제공하는 전체 열 교환 표면적을 포함하는 상기 반응 시스템의 열 교환 부분을 포함한다. 상기 반응 시스템 내에서 상기 전체 반응 혼합물 체적에 대한 상기 전체 열 교환 표면적의 비는 0.75in-1 내지 5in-1 범위이고, 상기 반응 시스템으로부터의 올리고머 생성물 방출률은 1.0(lb)(hr-1)(gal-1) 내지 6.0(lb)(hr-1)(gal-1)이다.

FORFARANDE VID DRIFT AV EN VIRVELBEDDSUGN SAMT ANORDNING FOR UTFORANDE AV FORFARANDET

REMOVAL OF CATALYST FINES FROM A REACTION SYSTEM

This invention provides a process for limiting the loss of catalyst particles through olefin product streams and regenerator flue gas streams exiting the reaction system. In particular, this invention provides for removing catalyst particles from the reactor using a water stream and from the regenerator using a two step separation process. The two step process involves the use of a catalyst fine separation unit.

TEMPERATURE CONTROLLED IN SITU WAX PURIFICATION

A hydrocarbon wax product from a HCS slurry comprising liquid synthesis product and catalyst particles is purified by circulating the slurry from a synthesis zone with a first temperature through a treatment zone with a second temperature in which a hydrogen-containing treatment gas contacts the slurry. The gas treatment removes impurities from the hydrocarbon wax product and also removes catalyst de-activating species which may be present in the slurry. Purified wax product is separated and removed from the treated slurry via wax withdrawal means. This avoids or minimizes the need for further treating the wax product. Remaining treated slurry may be returned to the synthesis zone.

REACTOR FOR CARRYING OUT RAPID HIGHLY EXOTHERMIC REACTIONS AND USE THEREOF

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.

OPTIMIZED METERING OF REACTANTS FOR A PROCESS FOR PREPARING AROMATIC AMINES BY HYDROGENATION OF NITROAROMATICS

The invention relates to a process for preparing aromatic amines by hydrogenating corresponding nitroaromatics with hydrogen, and also to apparatus suitable for this purpose. The invention relates more particularly to a process for preparing tolylenediamine (TDA) by hydrogenation of dinitrotoluene (DNT).

Exothermic process with porous means to control reacton rate and exothermic heat

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

Process for upgrading light olefins in a turbulent fluidized catalyst bed reactor

Установка дегидрирования этилбензола для получения стирола и соответствующий способ

FIELD: chemistry. SUBSTANCE: invention relates to ethylbenzene dehydrogenation plant and process for producing styrene. Plant includes a reaction section including one or more adiabatic reactors arranged in series, a steam circuit including a first steam heat exchanger disposed downstream of the first adiabatic reactor, and a heating device comprising one or more ultra-heaters arranged in the heating circuit and in fluid communication with each other, one or more combustion chambers comprising a steam diffuser, a burner and a mixer, and one or more ventilation devices where the smoke gases generated in the combustion chamber are recirculated through the ventilation device through the heating circuit, wherein the ultra-heater of the heating circuit is located between one adiabatic reactor and the subsequent adiabatic reactor or on the feed line to the first reactor or the steam circuit. EFFECT: invention makes it possible to use flue gases as a coolant with the possibility of their circulation in the heating circuit and provides an increase in the energy efficiency of the production of styrene. 13 cl, 6 dwg, 6 tbl РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 659 255 C1 (51) МПК B01J 8/00 (2006.01) B01J 19/24 (2006.01) C07C 5/333 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК B01J 8/00 (2018.05); B01J 19/24 (2018.05); C07C 5/333 (2018.05) (21)(22) Заявка: 2016119936, 10.11.2014 (24) Дата начала отсчета срока действия патента: (73) Патентообладатель(и): Версалис С.П.А. (IT) Дата регистрации: 29.06.2018 5053572 A, 01.10.1991. US 3417156 A, 17.12.1968. CN 102040466 A, 04.05.2011. 11.11.2013 IT MI2013A001870 (45) Опубликовано: 29.06.2018 Бюл. № 19 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 14.06.2016 (86) Заявка PCT: (87) Публикация заявки PCT: WO 2015/068138 (14.05.2015) R U 2 6 5 9 2 5 5 Адрес для переписки: 191036, Санкт-Петербург, а/я 24, "НЕВИНПАТ" (54) Установка дегидрирования этилбензола ...

УЛУЧШЕННАЯ КОНСТРУКЦИЯ РЕАКТОРА ОЛИГОМЕРИЗАЦИИ/ТРИМЕРИЗАЦИИ/ТЕТРАМЕРИЗАЦИИ ЭТИЛЕНА

ОТДЕЛЕНИЕ ЭТИЛЕНА ПОСРЕДСТВОМ КОРОТКОЦИКЛОВОЙ АДСОРБЦИИ

РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2017 117 511 A (51) МПК C07C 7/00 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21)(22) Заявка: 2017117511, 19.11.2015 (71) Заявитель(и): ШЕВРОН ФИЛЛИПС КЕМИКАЛ КОМПАНИ ЭлПи (US) Приоритет(ы): (30) Конвенционный приоритет: 21.11.2014 US 14/550,638 36 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 21.06.2017 US 2015/061610 (19.11.2015) (87) Публикация заявки PCT: A WO 2016/081738 (26.05.2016) Адрес для переписки: 119019, Москва, Гоголевский б-р, 11, этаж 3, "Гоулинг ВЛГ (Интернэшнл) Инк.", Угрюмов Владислав Михайлович R U (57) Формула изобретения 1. Способ разделения компонентов в системе для получения полимеров, включающий: (a) разделение потока продуктов полимеризации на газовый поток и поток полимеров; (b) обработку газового потока в одной или более ректификационных колоннах с получением потока легких углеводородов, при этом указанный поток легких углеводородов содержит этилен и этан; (c) приведение по меньшей мере части потока легких углеводородов в контакт с продутым углеводородным адсорбентом с получением загруженного углеводородного адсорбента и потока неадсорбированного газа, при этом по меньшей мере часть этана адсорбируется продутым углеводородным адсорбентом при первом давлении с получением адсорбированного этана, при этом указанный поток неадсорбированного газа содержит извлеченный этилен, при этом извлеченный этилен содержит по меньшей мере часть этилена из указанного потока легких углеводородов; (d) приведение по меньшей мере части загруженного углеводородного адсорбента в контакт с потоком продувочного газа при втором давлении с получением разгруженного углеводородного адсорбента и потока извлеченного адсорбированного газа, при этом указанный поток извлеченного адсорбированного газа содержит по меньшей мере часть потока продувочного газа и по меньшей мере часть десорбированного этана, при этом указанный десорбированный этан содержит по Стр.: 1 A 2 0 1 7 ...

ТЕПЛООБМЕННИК, ВКЛЮЧАЮЩАЯ ТЕПЛООБМЕННИК РЕАКТОРНАЯ СИСТЕМА И СПОСОБ ТЕРМОСТАТИРОВАНИЯ РЕАКТОРА

Verfahren zur autothermen Dampf-Reformierung.

Verfahren und Vorrichtung zur Steuerung eines katalytischen Kohlenwasserstoff-Umwandlungssystems

PROCESS FOR HYDRODEMETALLATION OF HYDROCARBON OILS

Method of and apparatus for effecting catalytic gaseous reactions

In catalytic gaseous reactions, e.g. cracking hydrocarbons, a plurality of catalyst containers are moved successively through a reacting zone and a regeneration zone, whereby the process is rendered continuous. As shown (Figs. 5, 6) a four-stage converter comprises a pressure vessel 21 in which a drum 24, divided by partitions 44 into a plurality of catalyst-containing compartments 43, is rotatably mounted, the vapours and regenerating medium being fed to and discharged from the vessel through a pair of stationary manifolds 22, 23 and sealing means indicated generally at 70 being provided to co-operate with the partitions and divide the drum and the manifolds into four gas-tight chambers, three for a three-stage reaction and one for regeneration of the catalyst. Reactant vapours are passed through line 7 (Fig. 2), heater 2 and line 8 to the first reaction chamber, then through line 9, heater 3 and line 10 to the second reaction ...

FLUIDISED BED INCINERATOR

COKE AND CATALYZED OXIDATION OF CO TO CO2 IN A FCCINITIATING AND CONTROLLING DENSE-BED OXIDATION OF REGENERATION ZONE

SINGLE ZONE OLIGOMERIZATION OF LOWER OLEFINS TO DISTILLATE UNDER LOW SEVERITY IN A FLUID BED WITH TAILORED ACTIVITY

SINGLE ZONE OLIGOMERIZATION OF LOWER OLEFINS TO DISTILLATE UNDER LOW SEVERITY IN A FLUID BED WITH TAILORED ACTIVITY

PROCESS FOR UPGRADING PROPENE-ETHENE MIXTURES IN A TURBULENT FLUIDIZED CATALYST BED REACTOR

FLUID CATALYST REGENERATION PROCESS AND APPARATUS

A catalyst regeneration process and apparatus for the oxidative removal of coke from a coke-contaminated fluid catalyst. Simultaneous production of hot regenerated catalyst and a relatively-cooler flue gas is provided. The process comprises a high temperature coke combustion zone, and a lower temperature heat removal zone. Coke contaminated catalyst, oxygen containing gas and regenerated catalyst from the heat removal zone are contacted in the high temperature combustion zone, the temperature of which is controlled by adjusting the rate at which catalyst is recycled from the heat removal zone. Catalyst may be withdrawn from the top of the combustion zone and sent to the reaction zone at the controlled combustion zone temperature, the remainder of the catalyst and the hot flue gas pass to the upper heat removal zone, where both gas and catalyst are cooled, preferably by utilizing the catalyst as a heat transfer medium in a dense-phase heat exchange system. the optimum temperature may be ...

PROCESS FOR UPGRADING LIGHT OLEFINS IN A TURBULENT FLUIDIZED CATALYST BED REACTOR

PROCESS FOR UPGRADING LIGHT OLEFINS IN A TURBULENT FLUIDIZED CATALYST BED REACTOR A fluidized bed catalytic process for conversion of light olefinic gas feedstock containing ethene to produce hydrocarbons rich in C5+ liquids, comprising the steps of maintaining a fluidized bed of zeolite catalyst particles in a turbulent reactor bed at a temperature of about 315 to 510.degree.C, said catalyst having an apparent particle density of about 0.9 to 1.6 g/cm3 and a size range of about 1 to 150 microns, and average catalyst particle size of about 20 to 100 microns containing about 10 to 25 weight percent of fine particles having a particle size less than 32 microns; passing hot feedstock vapor upwardly through the fluidized catalyst bed under turbulent flow conditions; maintaining turbulent fluidized bed conditions through the reactor bed between transition velocity and transport velocity at a superficial fluid velocity of about 0.3 to 2 meters per second; and recovering hydrocarbon product containing ...

PROCESS FOR CONVERTING OXYGENATES INTO LIQUID HYDROCARBONS

ZONE REACTOR INCORPORATING REVERSIBLE HYDROGEN HALIDE CAPTURE AND RELEASE

An improved process and a zone reactor for converting a hydrocarbon feeds tock into higher hydrocarbons is provided. A first zone in the reactor conta ins both a material capable of releasing hydrogen halide (HX) and a carbon-c arbon coupling catalyst; a second zone is initially empty or contains a halo genation and/or oxyhalogenation catalyst; and a third zone contains both a c arbon-carbon coupling catalyst and a material capable of capturing HX. Air o r oxygen is introduced into the first zone, a feedstock is introduced into t he second zone, and products are produced in the third zone. HX produced dur ing the reaction is reversibly captured and released in zones 1 and 3.

Ethylene separation with pressure swing adsorption

一种用于在聚合物生产系统中进行组分分离的方法，其包括：(a)将聚合产物分离成气体流和聚合物流；(b)在蒸馏塔中处理所述气体流，得到包含乙烯和乙烷的轻质烃流(LHS)；(c)使LHS与清洗烃吸附剂接触，得到负载烃吸附剂和非吸附气体流，其中乙烷在第一压力下被所述清洗烃吸附剂吸附，得到吸附乙烷，并且其中所述非吸附气体流包含回收乙烯；(d)使所述负载烃吸附剂与吹扫气体流在第二压力下接触，得到无载烃吸附剂和包含所述吹扫气体流和解吸乙烷的回收吸附气体流；和(e)使所述无载烃吸附剂与所述吹扫气体流在所述第一压力下接触，得到所述清洗烃吸附剂和废吹扫气体。

Reaction device for preparing alkanolamine and preparing method using the device

REFORMING EXCHANGER SYSTEM WITH INTERMEDIATE SHIFT CONVERSION

A reforming exchanger system for syngas production is provided. The reforming exchanger system can have a first and a second reforming exchanger, each with a shell-and-tube configuration, and a shift reactor located intermediate to the first and second reforming exchangers to reduce carbon monoxide concentration in the outlet gas. Processes for forming syngas using the reforming exchanger systems described herein are also provided.

РЕАКТОР С ПСЕВДООЖИЖЕННЫМ СЛОЕМ, ЕГО ПРИМЕНЕНИЕ И СПОСОБ ЭНЕРГОНЕЗАВИСИМОГО ГИДРИРОВАНИЯ ХЛОРСИЛАНОВ

1. Реактор с псевдоожиженным слоем для непрерывного гидрирования высших хлорсиланов формулы HnSiCl4-n, где n=0, 1, 2 или 3, в присутствии кремния, в частности, для получения хлорсиланов путем взаимодействия в основном между кремнием (А), тетрахлоридом кремния (В), водородом (С), а также необязательно хлороводородом или хлором в газообразной форме (D) и необязательно в присутствии катализатора, под давлением 25-55 бар и при температуре от 450 до 650°С, включающий в ! - корпус реактора (1.1) с оболочкой (1.2) для охлаждения или нагрева реактора, а также расположенным параллельно продольной оси реактора во внутреннем пространстве реактора теплообменником (1.3), причем по блокам (1.2) и (1.3) может протекать газообразная среда (F), а среду (F) можно нагревать с помощью отапливаемого газом теплообменника (1.11), ! - по меньшей мере один нижний подводящий трубопровод (1.4) для содержащего хлорсилан или ТХС потока исходных компонентов (В*), ! - по меньшей мере один подводящий трубопровод (1.5) для одного или нескольких газообразных компонентов из ряда (С) и (D), ! - по меньшей мере один подводящий трубопровод (1.6) для кремния в форме частиц (А), к которому при необходимости добавлен катализатор, и ! - средство отведения и разделения продукта (G, Н) через верхнюю часть реактора, пылевой фильтр (1.7) и конденсатор (1.8). ! 2. Реактор с псевдоожиженным слоем по п.1, отличающийся тем, что он дополнительно включает в себя теплообменник (1.10) для использования имеющегося отводимого тепла для предварительного подогрева газовых потоков (F). ! 3. Реактор с псевдоожиженным слоем по п.1, отличающийся тем, что он дополнительно включает в себя теплообменник (1.5.5) для использования имеющегося � РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2011 113 636 (13) A (51) МПК B01J 8/18 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (71) Заявитель(и): ЭВОНИК ДЕГУССА ГМБХ (DE) (21)(22) Заявка: 2011113636/05, 10.07.2009 Приоритет(ы): (30) Конвенционный приоритет: ...

Способ получения диметилтерефталата

Design of an Ethylene Oligomerization/Trimerization/Tetramerization Reactor

A process includes periodically or continuously introducing an olefin monomer and periodically or continuously introducing a catalyst system or catalyst system components into a reaction mixture within a reaction system, oligomerizing the olefin monomer within the reaction mixture to form an oligomer product, and periodically or continuously discharging a reaction system effluent comprising the oligomer product from the reaction system. The reaction system includes a total reaction mixture volume and a heat exchanged portion of the reaction system comprising a heat exchanged reaction mixture volume and a total heat exchanged surface area providing indirect contact between the reaction mixture and a heat exchange medium. A ratio of the total heat exchanged surface area to the total reaction mixture volume within the reaction system is in a range from 0.75 into 5 in, and an oligomer product discharge rate from the reaction system is between 1.0 (lb)(hr)(gal) to 6.0 (lb)(hr)(gal). 1. A process comprising:periodically or continuously introducing an olefin monomer and periodically or continuously introducing a catalyst system or catalyst system components into a reaction mixture within a reaction system;oligomerizing the olefin monomer within the reaction mixture to form an oligomer product; andperiodically or continuously discharging a reaction system effluent comprising the oligomer product from the reaction system;wherein the reaction system comprises: a total reaction mixture volume within the reaction system; and a heat exchanged portion of the reaction system comprising a heat exchanged reaction mixture volume and a total heat exchanged surface area providing indirect thermal contact between the reaction mixture and a heat exchange medium;{'sup': −1', '−1', '−1', '−1, 'wherein an oligomer product discharge rate from the reaction system is between 1.5 (lb)(hr)(gal) to 6.0 (lb)(hr)(gal); and'}{'sup': −1', '−1, 'wherein a ratio of the total heat exchanged surface area ...

PROCESS AND REACTOR ASSEMBLY FOR THE ENHANCEMENT OF HYDRODYNAMICS IN A GAS-SOLIDS FLUIDIZED BED REACTOR

A process for polymerizing olefin monomer(s) in a gas-solids olefin polymerization reactor comprising a top zone; a middle zone, which comprises a top end in direct contact with said top zone and which is located below said top zone, the middle zone having a generally cylindrical shape; and a bottom zone, which is in direct contact with a bottom end of the middle zone and which is located below the middle zone; comprising the following steps: introducing a fluidization gas stream into the bottom zone; polymerizing olefin monomer(s) in the presence of a polymerization catalyst in a dense phase formed by particles of a polymer of the olefin monomer(s) suspended in an upwards flowing stream of the fluidization gas in the middle zone; introducing a jet gas stream through one or more jet gas feeding ports in a jet gas feeding area of the middle zone at the dense phase in the middle zone of the gas-solids olefin polymerization reactor; wherein the kinetic energy (E) input in the reactor by the jet stream is between 1.5 and 50 times higher than the kinetic energy (E) input in the reactor by the fluidization gas stream (FG). 2186. The process according to claim 1 , wherein the fluidization gas is removed from the top zone () of the reactor and at least a part of the fluidization gas is introduced into the jet gas stream () and into the fluidization stream ().35. The process according to claim 1 , wherein the jet gas stream (JG) fed through at least one of the one or more jet gas feeding ports () is provided by a flash pipe (FP) from a preceding reactor claim 1 , preferably a reactor for polymerizing polypropylene claim 1 , more preferably a loop reactor for polymerizing polypropylene.4. The process according to claim 1 , wherein the jet gas stream (JG) is cooled to yield a partially condensed jet gas stream and wherein the fluidization gas stream (FG) is not condensed.568. The process according to claim 1 , wherein the fluidization gas stream (FG) in the first line () and ...

Design of an Ethylene Oligomerization/Trimerization/Tetramerization Reactor

A process includes periodically or continuously introducing an olefin monomer and periodically or continuously introducing a catalyst system or catalyst system components into a reaction mixture within a reaction system, oligomerizing the olefin monomer within the reaction mixture to form an oligomer product, and periodically or continuously discharging a reaction system effluent comprising the oligomer product from the reaction system. The reaction system includes a total reaction mixture volume and a heat exchanged portion of the reaction system comprising a heat exchanged reaction mixture volume and a total heat exchanged surface area providing indirect contact between the reaction mixture and a heat exchange medium. A ratio of the total heat exchanged surface area to the total reaction mixture volume within the reaction system is in a range from 0.75 into 5 in, and an oligomer product discharge rate from the reaction system is between 1.0 (lb)(hr)(gal) to 6.0 (lb)(hr)(gal). 1. A reaction system for oligomerizing an olefin monomer , the reaction system comprising:one or more reaction system inlets configured to periodically or continuously introduce an olefin monomer, a catalyst system or catalyst system components, or any combination thereof to a reaction mixture within the reaction system;one or more reaction system reaction mixture outlets configured to periodically or continuously discharge a reaction system effluent comprising an oligomer product from the reaction system;a total reaction mixture volume within the reaction system; anda heat exchanged portion of the reaction system comprising a heat exchanged reaction mixture volume and a total heat exchanged surface area providing indirect thermal contact between the reaction mixture and a heat exchange medium;wherein an oligomer product discharge rate from the reaction system is between 1.5 lb/hr/gal to 6.0 lb/hr/gal; and{'sup': −1', '−1, 'wherein a ratio of the total heat exchanged surface area to the total ...

Process for the Conversion of Free Fatty Acids to Glycerol Esters and Production of Novel Catalyst systems

Animal and seed based triglycerides are oils used in cosmetics, pharmaceuticals, animal feed, energy generation, etc. These triglycerides or glycerol esters are a mixture of triglycerides and free fatty esters (FFA) along with unsaponifiables and gums (MIU). FFA may range from very low, 1% or less, to more than 40% in some rendered animal oils. Corn oil from the wet or dry process of ethanol production may have from 7 to 15% FFA. The varying amount of FFA presents numerous process issues for downstream users of these oils especially in the production of biodiesel, fatty acid methyl ester (FAME). FFA about 1 or 2% requires esterification as well as transesterification for the production of FAME. What is needed is a method to perform Glycerolysis. This disclosure describes an improved catalyst system as well as process equipment and operating conditions to allow economical commercialization of Glycerolysis.

CONTINUOUS MANUFACTURING APPARATUS AND METHOD FOR CARBON NANOTUBES HAVING GAS SEPARATION UNITS

The present invention relates to a continuous manufacturing apparatus for a carbon nanotube having gas separation units and a continuous manufacturing method for a carbon nanotube using the same. According to the present invention, the present invention has an effect to provide the continuous manufacturing apparatus of the carbon nanotube and continuous manufacturing method using the same, in which it makes possible to perform a rapid processing; has excellent productivity and excellent conversion rate of carbon source; can significantly reduce the cost of production; can reduce energy consumption because a reactor size can be decreased as compared with capacity; and a gas separation unit that not generate a waste gas. 119-. (canceled)20. A continuous manufacturing apparatus of a carbon nanotube , comprisingi) a reactor for synthesizing the carbon nanotube;ii) a separator for separating a mixed gas and the carbon nanotube transferred from the reactor;iii) a gas separation unit for removing in part or in whole of more than one component gas from the mixed gas separated; andiv) a re-circulation pipe for recirculating the mixed gas without in part or in whole of the component gas to the carbon nanotube reactor,wherein a heat exchanger is installed between the reactor i) and the separator ii).21. The continuous manufacturing apparatus of the carbon nanotube according to claim 20 , wherein the polymer membrane is produced with more than one polymer selected from the group consisting of polysulfone claim 20 , polycarbonate claim 20 , polyimide claim 20 , and polystyrene claim 20 , and is for low temperature to operate at below 50° C.22. The continuous manufacturing apparatus of the carbon nanotube according to claim 20 , wherein the component gas claim 20 , of iii) claim 20 , is hydrogen.23. The continuous manufacturing apparatus of the carbon nanotube according to claim 20 , wherein the component gas of iii) is a byproduct gas produced in the reactor of i).24. The ...

Catalyst supply method for gas-phase polymerization fluidized bed

Catalyst feed control during catalyst transition periods

Techniques are provided for operating a reactor during a catalyst transition period. The instantaneous reaction rate during a catalyst transition period can be determined using real-time measured process variables, and material balance calculations to provide an instantaneous reaction rate in approximately real time. According to certain embodiments, a material balance can be performed on the reactor system using a continuous ideal stirred tank reactor to determine the fractions of each type of catalyst that are present in the reactor, as well as the overall weight percent of catalyst in the reactor. A controller can then calculate the overall instantaneous reaction rate based on the respective catalyst fractions and the overall weight percent of catalyst in the reactor. The catalyst feed rate can then be adjusted based on the determined instantaneous reaction rate to maintain the instantaneous reaction rate within desired limits during a catalyst transition period.

Catalyst feed control during catalyst transition periods

Techniques are provided for operating a reactor during a catalyst transition period. The instantaneous reaction rate during a catalyst transition period can be determined using real-time measured process variables, and material balance calculations to provide an instantaneous reaction rate in approximately real time. According to certain embodiments, a material balance can be performed on the reactor system using a continuous ideal stirred tank reactor to determine the fractions of each type of catalyst that are present in the reactor, as well as the overall weight percent of catalyst in the reactor. A controller can then calculate the overall instantaneous reaction rate based on the respective catalyst fractions and the overall weight percent of catalyst in the reactor. The catalyst feed rate can then be adjusted based on the determined instantaneous reaction rate to maintain the instantaneous reaction rate within desired limits during a catalyst transition period.

Process for feeding catalyst to fluidized bed for vapor phase polymerisation

A process for feeding a powdery catalyst with a gas intermittently to a high-pressure fluidized bed reactor for the vapor phase polymerisation of olefin, wherein the cross section of a catalyst feed pipe is reduced midway through the pipe to thereby make continuous catalyst feed possible and prevent the formation of a lump polymer.

Process for feeding catalyst to fluidized bed for vapor phase polymerization

A process for feeding a powder catalyst with a gas intermittently to a high-pressure fluidized bed reactor for the vapor phase polymerization of olefin, wherein the cross section of a catalyst feed pipe is reduced midway through the pipe to thereby make continual catalyst feeding possible and prevent the formation of a lump polymer.

Process for feeding catalyst to fluidized bed for vapor phase polymerisation

A process for feeding a powdery catalyst with a gas intermittently to a high-pressure fluidized bed reactor for the vapor phase polymerisation of olefin, wherein the cross section of a catalyst feed pipe is reduced midway through the pipe to thereby make continuous catalyst feed possible and prevent the formation of a lump polymer.

Method for preventing or reducing clogging of a fines ejector

A method for preventing or reducing clogging of a fines ejector in a gas-phase olefin polymerization process is disclosed. The process involves injecting a liquid into the motive gas stream entering the fines ejector.

Process for feeding catalyst to fluidized bed for vapor phase polymerization

A process for feeding a powder catalyst with a gas intermittently to a high-pressure fluidized bed reactor for the vapor phase polymerization of olefin, wherein the cross section of a catalyst feed pipe is reduced midway through the pipe to thereby make continual catalyst feeding possible and prevent the formation of a lump polymer.

Hydrocarbon recovery with pressure swing adsorption

A process for component separation in a polymer production system comprising: (a) separating a polymerization product into a gas stream and a polymer stream; (b) processing the gas stream in distillation columns to yield a light hydrocarbon stream (LHS) comprising ethylene and ethane; (c) contacting LHS with a purged hydrocarbon adsorber to yield a loaded hydrocarbon adsorber and a non-adsorbed gas stream, wherein ethane is adsorbed by the purged hydrocarbon adsorber at a first pressure to yield adsorbed ethane, and wherein the non-adsorbed gas stream comprises recovered ethylene; (d) contacting the loaded hydrocarbon adsorber with a sweeping gas stream at a second pressure to yield an unloaded hydrocarbon adsorber and a recovered adsorbed gas stream comprising the sweeping gas stream and desorbed ethane; and (e) contacting the unloaded hydrocarbon adsorber with the sweeping gas stream at the first pressure to yield the purged hydrocarbon adsorber and a spent sweeping gas.

Hydrocarbon recovery with pressure swing adsorption

A process for component separation in a polymer production system comprising: (a) separating a polymerization product into a gas stream and a polymer stream; (b) processing the gas stream in distillation columns to yield a light hydrocarbon stream (LHS) comprising ethylene and ethane; (c) contacting LHS with a purged hydrocarbon adsorber to yield a loaded hydrocarbon adsorber and a non-adsorbed gas stream, wherein ethane is adsorbed by the purged hydrocarbon adsorber at a first pressure to yield adsorbed ethane, and wherein the non-adsorbed gas stream comprises recovered ethylene; (d) contacting the loaded hydrocarbon adsorber with a sweeping gas stream at a second pressure to yield an unloaded hydrocarbon adsorber and a recovered adsorbed gas stream comprising the sweeping gas stream and desorbed ethane; and (e) contacting the unloaded hydrocarbon adsorber with the sweeping gas stream at the first pressure to yield the purged hydrocarbon adsorber and a spent sweeping gas.

Ethylene separation with pressure swing adsorption

A process for component separation in a polymer production system comprising: (a) separating a polymerization product into a gas stream and a polymer stream; (b) processing the gas stream in distillation columns to yield a light hydrocarbon stream (LHS) comprising ethylene and ethane; (c) contacting LHS with a purged hydrocarbon adsorber to yield a loaded hydrocarbon adsorber and a non-adsorbed gas stream, wherein ethane is adsorbed by the purged hydrocarbon adsorber at a first pressure to yield adsorbed ethane, and wherein the non-adsorbed gas stream comprises recovered ethylene; (d) contacting the loaded hydrocarbon adsorber with a sweeping gas stream at a second pressure to yield an unloaded hydrocarbon adsorber and a recovered adsorbed gas stream comprising the sweeping gas stream and desorbed ethane; and (e) contacting the unloaded hydrocarbon adsorber with the sweeping gas stream at the first pressure to yield the purged hydrocarbon adsorber and a spent sweeping gas.

A bed plate with supporting grid for a fluidized bed reactor and its modeling

A fluid dynamic model having at least 5,000,000 cells of the portion of a gas phase reactor from the exit of the condenser to a half a reactor diameter above the bed plate is useful in determining the design of the bottom surface or support structure for a bed plate to minimize liquid pooling below and above the bed plate when operating in condensing mode.

Molding a bed plate and its use

A fluid dynamic model having at least 5,000,000 cells of the portion of a gas phase reactor from the exit of the condenser to a half a reactor diameter above the bed plate is useful in determining the design of the bottom surface or support structure for a bed plate to minimize liquid pooling below and above the bed plate when operating in condensing mode.

Process and apparatus for olefin polymerization in a fluidized bed reactor

A process and apparatus for gas phase polymerization of olefins in a fluidized bed reactor are disclosed. The process and apparatus employ a vertically oriented fines ejector in order to reduce fouling and reactor downtime.

Process and apparatus for olefin polymerization in a fluidized bed reactor

A process and apparatus for gas phase polymerization of olefins in a fluidized bed reactor are disclosed. The process and apparatus employ a vertically oriented fines ejector in order to reduce fouling and reactor downtime.

Process and apparatus for olefin polymerization in a fluidized bed reactor

A process and apparatus for gas phase polymerization of olefins in a fluidized bed reactor are disclosed. The process and apparatus employ a vertically oriented fines ejector in order to reduce fouling and reactor downtime.

Method for preventing or reducing clogging of a fines ejector

A method for preventing or reducing clogging of a fines ejector in a gas-phase olefin polymerization process is disclosed. The process involves injecting a liquid into the motive gas stream entering the fines ejector.

Process for feeding catalyst to fluidized bed for vapor phase polymerisation

A process for feeding a powdery catalyst with a gas intermittently to a high-pressure fluidized bed reactor for the vapor phase polymerisation of olefin, wherein the cross section of a catalyst feed pipe is reduced midway through the pipe to thereby make continuous catalyst feed possible and prevent the formation of a lump polymer.

METHOD FOR SUPPLYING CATALYST TO A FLUID BED FOR STEAM PHASE POLYMERIZATION

METHOD FOR SUPPLYING CATALYST TO A FLUID BED FOR STEAM PHASE POLYMERIZATION

Process for feeding catalyst to fluidized bed for vapor phase polymerisation

A process for feeding a powdery catalyst with a gas intermittently to a high-pressure fluidized bed reactor for the vapor phase polymerisation of olefin, wherein the cross section of a catalyst feed pipe is reduced midway through the pipe to thereby make continuous catalyst feed possible and prevent the formation of a lump polymer.

Process for feeding catalyst to fluidized bed for vapor phase polymerisation.

A process for feeding a powdery catalyst with a gas intermittently to a high-pressure fluidized bed reactor for the vapor phase polymerisation of olefin, wherein the cross section of a catalyst feed pipe is reduced midway through the pipe to thereby make continuous catalyst feed possible and prevent the formation of a lump polymer.

床板之模型化及其用途

本發明提供一種流體動力學模型，其具有自冷凝器之出口至床板上方之反應器直徑之一半的氣相反應器之部分的至少5,000,000個單元，該流體動力學模型可用於確定用於床板之底表面或支撐結構之設計以在以冷凝模式操作時使該床板下方及上方之液體彙集降至最低。

method to prevent or reduce the clogging of a fines ejector, and, process to polymerize olefins

MÉTODO PARA PREVENIR OU REDUZIR O ENTUPIMENTO DE UM EJETOR DE FINOS, E, PROCESSO PARA POLIMERIZAR OLEFINAS. Um método para prevenir ou reduzir entupimento de um ejetor de finos em um processo de polimerização de olefina de fase gasosa é divulgado. O processo envolve injetar um líquido na corrente de gás propulsor que entra no ejetor de finos. METHOD TO PREVENT OR REDUCE THE CLOUDING OF A FINES EJECTOR, AND PROCESS TO POLYMERIZE OLEFINS. A method for preventing or reducing clogging of a fines ejector in a gas phase olefin polymerization process is disclosed. The process involves injecting a liquid into the stream of propellant gas that enters the fines ejector.

Modeling a bed plate and its use

A fluid dynamic model having at least 5,000,000 cells of the portion of a gas phase reactor from the exit of the condenser to a half a reactor diameter above the bed plate is useful in determining the design of the bottom surface or support structure for a bed plate to minimize liquid pooling below and above the bed plate when operating in condensing mode.

Zone reactor incorporating reversible hydrogen halide capture and release

An improved process and a zone reactor for converting a hydrocarbon feedstock into higher hydrocarbons is provided. A first zone in the reactor contains both a material capable of releasing hydrogen halide (HX) and a carbon-carbon coupling catalyst; a second zone is initially empty or contains a halogenation and/or oxyhalogenation catalyst; and a third zone contains both a carbon-carbon coupling catalyst and a material capable of capturing HX. Air or oxygen is introduced into the first zone, a feedstock is introduced into the second zone, and products are produced in the third zone. HX produced during the reaction is reversibly captured and released in zones 1 and 3.

Fluidized bed reactor, the use thereof, and a method for the energy-independent hydration of chlorosilanes

The present invention relates to a device, to the use thereof, and to a method for the substantially energy-independent continuous production of chlorosilanes, particularly for the production of trichlorosilane as an intermediate product for yielding high-purity silicon.

用于增强气固流化床反应器中流体动力学的方法和反应器组件

一种在气固烯烃聚合反应器中聚合烯烃单体的方法，所述气固烯烃聚合反应器包括：顶部区；中间区，所述中间区包括与所述顶部区直接接触的顶端并位于所述顶部区的下方，所述中间区具有大致圆柱形的形状；以及底部区，其与所述中间区的底端直接接触，并位于所述中间区的下方；所述方法包括以下步骤：将流化气流引入底部区；在聚合催化剂的存在下在密相中聚合烯烃单体，所述密相由悬浮在中间区的向上流动的流化气体流中的烯烃单体的聚合物颗粒形成；在气固烯烃聚合反应器的中间区中的密相处，通过在中间区的喷射气体进料区中的一个或多个喷射气体进料口引入喷射气流；其中喷射流输入反应器的动能(E JG )比流化气流(FG)输入反应器的动能(E FG )高1.5至50倍。

Zone reactor incorporating reversible hydrogen halide capture and release

A reactor for converting a hydrocarbon feedstock into one or more products is disclosed, which comprises: one or more hollow vessels that define multiple zones in the reactor, wherein a first zone contains a material capable of releasing hydrogen halide and a carbon-carbon coupling catalyst, a second zone is coupled to the first zone, and a third zone is coupled to the second zone and contains a carbon-carbon coupling catalyst and a material capable of capturing hydrogen halide. Preferably, the material capable of releasing hydrogen halide comprises partially halogenated olefins selected from partially halogenated 1dodecene, 1,12-dodecadiene, and/or 1-eicosane; and partially halogenated organic polymers selected from the group consisting of partially halogenated polyacetylene, polyethylene that has been partially dehydrogenated and partially halogenated, polypropylene that has been partially dehydrogenated and partially halogenated, and mixtures thereof. Similarly, the preferred material capable of capturing hydrogen halide comprises unsaturated organic polymers which are selected from the group consisting of polyacetylene, polyethylene that has been partially dehydrogenated, polypropylene that has been partially dehydrogenated, and mixtures thereof.

Ethylene oligomerization/trimerization/tetramerization reactor

A process includes periodically or continuously introducing an olefin monomer and periodically or continuously introducing a catalyst system or catalyst system components into a reaction mixture within a reaction system, oligomerizing the olefin monomer within the reaction mixture to form an oligomer product, and periodically or continuously discharging a reaction system effluent comprising the oligomer product from the reaction system. The reaction system includes a total reaction mixture volume and a heat exchanged portion of the reaction system comprising a heat exchanged reaction mixture volume and a total heat exchanged surface area providing indirect contact between the reaction mixture and a heat exchange medium. A ratio of the total heat exchanged surface area to the total reaction mixture volume within the reaction system is in a range from 0.75 in−1 to 5 in−1, and an oligomer product discharge rate from the reaction system is between 1.0 (lb)(hr−1)(gal−1) to 6.0 (lb)(hr−1)(gal−1).

Reaction apparatus for production of alkanolamine

SELECTIVE PRODUCTION OF A DIALKANOLAMINE IS ATTAINED BY CONTROLLING THE VOLUME PRECEDING THE ENTRANCE TO A CATALYST BED AND THE TEMPERATURE PREVAILING UNDER RESPECTIVELY FIXED LEVELS SUBSEQUENT TO THE MIXTURE OF AN ALKYLENE OXIDE THEREBY REPRESSING A REACTION OCCURING IN THE ABSENCE OF A CATALYST AND CURBING THE FORMATION OF TRIALKANOLAMINE. @ THE REACTANT FLUID IS PREVENTED FROM GENERATING A CHANNELING BY DISPOSING AN EXPORTABLE STRUCTURE IN A REACTOR THEREBY CREATING THE STATE OF A FALSE SHELL-AND-TUBE TYPE REACTOR. @ THE REACTION INITIATED WITH THE INLET TEMPERATURE SET AT A HIGHER LEVEL THAN THE PRESCRIBED LEVEL AND THE ALKYLENE OXIDE CONCENTRATION SET AT A LOWER LEVEL THAN THE PRESCRIBED LEVEL AND THEREAFTER THE INLET TEMPERATURE AND THE ALKYLENE OXIDE CONCENTRATION ARE GRADUALLY CHANGED TOWARD THE RESPECTIVELY PRESCRIBED LEVELS.

用於在氣固流體化床反應器中增強流體動力學的方法及反應器組件

一種用於在氣固烯烴聚合反應器中聚合烯烴單體的方法，該反應器包括：頂部區域；中間區域，位於頂部區域下方，包括與頂部區域直接接觸的頂端，且具有大致圓柱形的形狀；以及底部區域，位於中間區域下方，且與中間區域的底端直接接觸；該方法包括以下步驟：將流體化氣體流引入底部區域；在稠密相中在聚合反應催化劑的存在下聚合烯烴單體，稠密相由烯烴單體的聚合物的顆粒形成，該些顆粒懸浮在中間區域中的流體化氣體的向上流動流中；經由在中間區域的噴射氣體進料區中的一個或多個噴射氣體進料口將噴射氣體流引入在氣固烯烴聚合反應器的中間區域中的稠密相，其中，由噴射氣體流輸入到反應器中的動能（ E JG ）為由流體化氣體流（FG）輸入到反應器中的動能（ E FG ）的1.5至50倍。

Process and reactor assembly for the enhancement of hydrodynamics in a gas-solids fluidized bed reactor

A process for polymerizing olefin monomer(s) in a gas-solids olefin polymerization reactor comprising a top zone; a middle zone, which comprises a top end in direct contact with said top zone and which is located below said top zone, the middle zone having a generally cylindrical shape; and a bottom zone, which is in direct contact with a bottom end of the middle zone and which is located below the middle zone; comprising the following steps: introducing a fluidization gas stream into the bottom zone; polymerizing olefin monomer(s) in the presence of a polymerization catalyst in a dense phase formed by particles of a polymer of the olefin monomer(s) suspended in an upwards flowing stream of the fluidization gas in the middle zone; introducing a jet gas stream through one or more jet gas feeding ports in a jet gas feeding area of the middle zone at the dense phase in the middle zone of the gas-solids olefin polymerization reactor; wherein the kinetic energy (E JG ) input in the reactor by the jet stream is between 1.5 and 50 times higher than the kinetic energy (E FG ) input in the reactor by the fluidization gas stream (FG).

Ethylene oligomerization/trimerization/tetramerization reactor

A process includes periodically or continuously introducing an olefin monomer and periodically or continuously introducing a catalyst system or catalyst system components into a reaction mixture within a reaction system, oligomerizing the olefin monomer within the reaction mixture to form an oligomer product, and periodically or continuously discharging a reaction system effluent comprising the oligomer product from the reaction system. The reaction system includes a total reaction mixture volume and a heat exchanged portion of the reaction system comprising a heat exchanged reaction mixture volume and a total heat exchanged surface area providing indirect contact between the reaction mixture and a heat exchange medium. A ratio of the total heat exchanged surface area to the total reaction mixture volume within the reaction system is in a range from 0.75 in −1 to 5 in −1 , and an oligomer product discharge rate from the reaction system is between 1.0 (lb)(hr −1 )(gal −1 ) to 6.0 (lb)(hr −1 )(gal −1 ).

用于避免或减少细末喷射器阻塞的方法

本发明公开了一种用于在气相烯烃聚合工艺中避免或减少细末喷射器阻塞的方法。所述工艺涉及向进入细末喷射器的动力气流中注入液体。

Method for preventing or reducing clogging of a fines ejector

Ethylene separation with pressure swing adsorption

method for preventing or reducing clogging of a fin ejector, and process for polymerizing olefins

método para prevenir our eduzir o entupimento de um ejetor de finos, e, processo para polimerizar olefinas. um método para prevenir ou reduzir entupimento de um ejetor de finos em um processo de polimerização de olefina de fase gasosa é divulgado. o processo envolve injetar um líquido na corrente de gás propulsor que entra no ejetor de finos. A method for preventing or reducing clogging of a fin ejector, and a process for polymerizing olefins. A method for preventing or reducing clogging of a fines ejector in a gas phase olefin polymerization process is disclosed. The process involves injecting a liquid into the propellant gas stream that enters the fines ejector.

Process and apparatus for olefin polymerization in a fluidized bed reactor

A process and apparatus for gas phase polymerization of olefins in a fluidized bed reactor are disclosed. The process and apparatus employ a vertically oriented fines ejector in order to reduce fouling and reactor downtime.

Process and Apparatus for Olefin Polymerization in a Fluidized Bed Reactor

A process and apparatus for gas phase polymerization of olefins in a fluidized bed reactor are disclosed. The process and apparatus employ a vertically oriented fines ejector in order to reduce fouling and reactor downtime.

用于避免或减少细末喷射器阻塞的方法

公开了一种用于在气相烯烃聚合工艺中避免或减少细末喷射器阻塞的方法。所述工艺涉及向进入细末喷射器的动力气流中注入液体。

METHOD FOR CATALYTIC TREATMENT OF A LIQUID BATCH AND DEVICE FOR CARRYING OUT THE METHOD

Upgrading light olefins in a turbulent fluidized catalyst bed reactor

A fluidized bed catalytic process for conversion of light olefinic gas feedstock containing ethene to produce hydrocarbons rich in C 5 + liquids, comprising the steps of maintaining a fluidized bed of zeolite catalyst particles in a turbulent reactor bed at a temperature of about 315° to 510° C., said catalyst having an apparent particle density of about 0.9 to 1.6 g/cm 3 and a size range of about 1 to 150 microns, and average catalyst particles size of about 20 to 100 microns containing about 10 to 25 weight percent of fine particles having a particle size less than 32 microns; passing hot feedstock vapor upwardly through the fluidized catalyst bed under turbulent flow conditions; maintaining turbulent fluidized bed conditions through the reactor bed between transition velocity and transport velocity at a superficial fluid velocity of about 0.3 to 2 meters per second; and recovering hydrocarbon product containing a major amount of C 5 + hydrocarbons and containing C 3 -C 5 alkanes and alkenes in the ratio of about 0.2:1 to 5:1.

Upgrading light olefin fuel gas and catalytic reformate in a turbulent fluidized bed catalyst reactor

A fluidized bed catalytic process for conversion of light olefinic gas feedstock containing ethene and propene to produce C 5 + hydrocarbons and for the conversion of catalytic reformate feedstock to produce C 7 -C 11 aromatic hydrocarbons, comprising a maintaining a fluidized bed of zeolite catalyst particles in a turbulent reactor bed at a temperature of about 600° to 750° F. (316° to 399° C.) and pressure of about 100 to 250 psig (790 to 825 kPa. The catalyst has an apparent particle density of about 0.9 to 1.6 g/cm 3 and a size range of about 1 to 150 microns, and average catalyst particle size of about 20 to 100 microns containing about 10 to 25 weight percent of fine particles having a particle size less than 32 microns. The feed vapor is passed upwardly through the fluidized catalyst bed under turbulent flow conditions; turbulent fluidized bed conditions are maintained through the reactor bed between transition velocity and transport velocity at a superficial fluid velocity of about 0.3 to 2 meters per second; and hydrocarbon product is recovered containing C 5 + hydrocarbons and C 7 to C 11 aromatic hydrocarbons.

一种集成催化剂颗粒后处理装置与应用

本发明公开了一种集成催化剂颗粒后处理装置与应用，属于多相催化剂制备领域。所述集成催化剂颗粒后处理装置由气态/液态共混预热系统，预热系统，鼓泡传质系统，烘干脱水系统，换热回收系统等模块构成，通过本套装置与处理方法，将繁杂的催化剂颗粒后处理工序高度集成，可以实现一次装料，连续完成化学试剂浸渍、洗涤、脱水等工序，集成程度高，采用气液共混鼓泡模式，达到高效快捷完成相关处理工序，设计合理，化学试剂可回收再利用，三废量较少，环境友好，自动连续化高，大大减少了人工操作成本，为大规模的工业化生产提供了一种新方法。

Verfahren zur katalytischen Durchführung von Aldolkondensationen mittels Mehrphasenreaktion

Die Erfindung betrifft ein Verfahren zur katalytischen Aldolkondensation von Aldehyden durch Mehrphasenreaktion in einem Rohrreaktor, wobei der Katalysator in der kontinuierlichen Phase und mindestens ein Aldehyd in einer dispergierten Phase enthalten ist und der Belastungsfaktor B des Rohrreaktors gleich oder größer 0,8 ist. DOLLAR A Die so erhaltenen Aldolkondensationsprodukte können zur Herstellung von Alkoholen oder Carbonsäuren verwendet werden.

Process for catalytic aldol condensations by means of a multiphase reaction

본 발명은, 촉매가 연속 상에 존재하고 하나 이상의 알데히드가 분산 상에 존재하며 관형 반응기의 부하율 B가 0.8 이상임을 특징으로 하는, 관형 반응기 속에서 다중상 반응에 의한 알데히드의 촉매적 알돌 축합방법에 관한 것이다. The present invention relates to a method for the catalytic aldol condensation of aldehydes by a multi-phase reaction in a tubular reactor, characterized in that the catalyst is present in the continuous phase and at least one aldehyde is present in the dispersion phase and the load factor B of the tubular reactor is at least 0.8. It is about. 이런 식으로 수득된 알돌 축합 생성물은 알콜 또는 카복실산을 제조하는 데 사용될 수 있다. The aldol condensation products obtained in this way can be used to prepare alcohols or carboxylic acids. 촉매적 알돌 축합방법, 다중상 반응, 관형 반응기, 부하율, 가소제 Catalytic aldol condensation method, multiphase reaction, tubular reactor, loading rate, plasticizer

Improved design of ethylene oligomerization/trimerization/tetramerization reactor

방법은 반응 시스템 내의 반응 혼합물 중에 올레핀 단량체를 주기적으로 또는 연속적으로 도입하고, 촉매 시스템 또는 촉매 시스템 성분을 주기적으로 또는 연속적으로 도입하는 단계, 상기 반응 혼합물 내에서 상기 올레핀 단량체를 올리고머화시켜 올리고머 생성물을 형성하는 단계, 및 상기 올리고머 생성물을 포함하는 반응 시스템 유출물을 반응 시스템으로부터 주기적으로 또는 연속적으로 방출시키는 단계를 포함한다. 상기 반응 시스템은 전체 반응 혼합물 체적, 및 교환 반응 혼합물 체적 및 상기 반응 혼합물과 열 교환 매질 사이의 간접적인 열 접촉을 제공하는 전체 열 교환 표면적을 포함하는 상기 반응 시스템의 열 교환 부분을 포함한다. 상기 반응 시스템 내에서 상기 전체 반응 혼합물 체적에 대한 상기 전체 열 교환 표면적의 비는 0.75in -1 내지 5in- 1 범위이고, 상기 반응 시스템으로부터의 올리고머 생성물 방출률은 1.0(lb)(hr -1 )(gal -1 ) 내지 6.0(lb)(hr -1 )(gal -1 )이다. The process includes periodically or continuously introducing an olefin monomer into a reaction mixture in a reaction system, periodically or continuously introducing a catalyst system or catalyst system component, oligomerizing the olefin monomer in the reaction mixture to obtain an oligomeric product forming, and periodically or continuously discharging the reaction system effluent comprising the oligomeric product from the reaction system. The reaction system comprises a heat exchange portion of the reaction system comprising a total reaction mixture volume and an exchange reaction mixture volume and a total heat exchange surface area that provides indirect thermal contact between the reaction mixture and a heat exchange medium. The reaction in the system and the ratio of 0.75in the range of -1 to 1 5in- the total heat exchange surface area with respect to the total reaction mixture volume, release rate of the oligomer product from the reaction system is 1.0 (lb) (hr -1) ( gal -1 ) to 6.0 (lb) (hr -1 ) (gal -1 ).

Process and reactor assembly for the enhancement of hydrodynamics in a gas-solids fluidized bed reactor

A process for polymerizing olefin monomer(s) in a gas-solids olefin polymerization reactor comprising a top zone; a middle zone, which comprises a top end in direct contact with said top zone and which is located below said top zone, the middle zone having a generally cylindrical shape; and a bottom zone, which is in direct contact with a bottom end of the middle zone and which is located below the middle zone; comprising the following steps: introducing a fluidization gas stream into the bottom zone; polymerizing olefin monomer(s) in the presence of a polymerization catalyst in a dense phase formed by particles of a polymer of the olefin monomer(s) suspended in an upwards flowing stream of the fluidization gas in the middle zone; introducing a jet gas stream through one or more jet gas feeding ports in a jet gas feeding area of the middle zone at the dense phase in the middle zone of the gas-solids olefin polymerization reactor; wherein the kinetic energy (E JG ) input in the reactor by the jet stream is between 1.5 and 50 times higher than the kinetic energy (E FG ) input in the reactor by the fluidization gas stream (FG).

Method to prevent or reduce clogging of fine powder discharger

미립 분사기의 막힘을 방지하거나 감소시키는 방법

기상 올레핀 중합 공정에서 미분 분사기의 막힘을 방지하거나 감소시키는 방법이 개시되어 있다. 이 방법은 미분 분사기에 들어가는 이동 기체 스트림 중으로 액체를 도입함을 포함한다.

Method for preventing or reducing clogging of a fines ejector

A method for preventing or reducing clogging of a fines ejector in a gas-phase olefin polymerization process is disclosed. The process involves injecting a liquid into the motive gas stream entering the fines ejector.

Process and apparatus for olefin polymerization in a fluidized bed reactor

A process and apparatus for gas phase polymerization of olefins in a fluidized bed reactor are disclosed. The process and apparatus employ a vertically oriented fines ejector in order to reduce fouling and reactor downtime.

用于烯烃在流化床反应器中聚合的方法和装置

公开了用于烯烃在流化床反应器中气相聚合的方法和装置。该方法和装置使用垂直定向的微粒喷射器用于降低结垢和反应器停工时间。

Autothermal steam reforming process

증기, 산화제 및 새로운 탄화수소 공급의 대부분을 발열 촉매 개질 영역에서 반응시키는 것에 의해 매우 낮은 메탄 성분을 갖는 제 1 개질된 가스를 회수한다. 새로운 공급의 균형은 흡열 촉매 개질 영역에서 증기와 반응하여 낮은 메탄 성분을 갖는 제 2 개질된 가스로 된다. 상기 제 1 및 제 2 개질된 가스는 합쳐지고 흡열 개질 영역에서 반응물질과 간접 열 교환하에 통과되어 그 안에 필요한 모든 열을 제공하며 제품 합성 가스로서 회수된다. The first reformed gas having a very low methane component is recovered by reacting most of the steam, oxidant and fresh hydrocarbon feed in the exothermic catalyst reforming zone. The new feed balance is reacted with steam in the endothermic catalyst reforming zone to a second reformed gas having a low methane component. The first and second modified gases are combined and passed under indirect heat exchange with the reactants in the endothermic reforming zone to provide all the heat required therein and recovered as product synthesis gas.

Ethylene separation with pressure swing adsorption

Continuous manufacturing apparatus and method for carbon nanotube having gas seperation units

The present invention relates to a continuous production apparatus for a carbon nanotube having a gas separation unit and a continuous production method using the same, and more specifically iii) a reactor in which carbon nanotubes are synthesized; Ii) a separator for separating the carbon nanotubes and the mixed gas transferred from the reactor; Iii) a gas separation unit for removing some or all of one or more component gases from the separated mixed gas; And iii) a recycle pipe for recycling the filtered mixed gas to the carbon nanotube reactor of iii). It relates to a continuous production apparatus for a carbon nanotube having a gas separation unit comprising a and a continuous manufacturing method using the same. According to the present invention, the present invention is capable of a high-speed process, excellent productivity and conversion of carbon sources, significantly reduced production costs, reduced reactor size compared to capacity, energy consumption is reduced, waste gas There is an effect of providing a continuous production apparatus for a carbon nanotube having a gas separation unit that hardly occurs and a continuous production method using the same.

Fluidized bed reactor, the use thereof, and a method for the energy-independent hydration of chlorosilanes

本发明涉及以能量基本上自给自足地连续制备氯硅烷，特别是用于制备获取高纯硅的中间产品即三氯硅烷的装置、其应用及方法。

Improved design of an ethylene oligomerization/trimerization/tetramerization reactor

방법은 반응 시스템 내의 반응 혼합물 중에 올레핀 단량체를 주기적으로 또는 연속적으로 도입하고, 촉매 시스템 또는 촉매 시스템 성분을 주기적으로 또는 연속적으로 도입하는 단계, 상기 반응 혼합물 내에서 상기 올레핀 단량체를 올리고머화시켜 올리고머 생성물을 형성하는 단계, 및 상기 올리고머 생성물을 포함하는 반응 시스템 유출물을 반응 시스템으로부터 주기적으로 또는 연속적으로 방출시키는 단계를 포함한다. 상기 반응 시스템은 전체 반응 혼합물 체적, 및 교환 반응 혼합물 체적 및 상기 반응 혼합물과 열 교환 매질 사이의 간접적인 열 접촉을 제공하는 전체 열 교환 표면적을 포함하는 상기 반응 시스템의 열 교환 부분을 포함한다. 상기 반응 시스템 내에서 상기 전체 반응 혼합물 체적에 대한 상기 전체 열 교환 표면적의 비는 0.75in -1 내지 5in- 1 범위이고, 상기 반응 시스템으로부터의 올리고머 생성물 방출률은 1.0(lb)(hr -1 )(gal -1 ) 내지 6.0(lb)(hr -1 )(gal -1 )이다.

Ethylene separation with pressure swing adsorption

A process for component separation in a polymer production system comprising: (a) separating a polymerization product into a gas stream and a polymer stream; (b) processing the gas stream in distillation columns to yield a light hydrocarbon stream (LHS) comprising ethylene and ethane; (c) contacting LHS with a purged hydrocarbon adsorber to yield a loaded hydrocarbon adsorber and a non-adsorbed gas stream, wherein ethane is adsorbed by the purged hydrocarbon adsorber at a first pressure to yield adsorbed ethane, and wherein the non-adsorbed gas stream comprises recovered ethylene; (d) contacting the loaded hydrocarbon adsorber with a sweeping gas stream at a second pressure to yield an unloaded hydrocarbon adsorber and a recovered adsorbed gas stream comprising the sweeping gas stream and desorbed ethane; and (e) contacting the unloaded hydrocarbon adsorber with the sweeping gas stream at the first pressure to yield the purged hydrocarbon adsorber and a spent sweeping gas.

Ethylene separation with pressure swing adsorption.

La presente invención se refiere a un proceso para la separación de componente en un sistema de producción de polímero que comprende: (a) separar un producto de polimerización en una corriente de gas y una corriente de polímero; (b) procesar la corriente de gas en columnas de destilación para proporcionar una corriente de hidrocarburo ligero (LHS) que comprende etileno y etano; (c) poner en contacto la LHS con un adsorbedor de hidrocarburo purgado para proporcionar un adsorbedor de hidrocarburo cargado y una corriente de gas no adsorbido, en donde el etano es adsorbido por el adsorbedor de hidrocarburo purgado en una primera presión para proporcionar etano adsorbido, comprende etileno recuperado; (d) poner en contacto el adsorbedor de hidrocarburo cargado con una corriente de gas de barrido y etanol desorbido; y (e) poner en contacto el adsorbente de hidrocarburo cargado con la corriente de gas de barrido a una segunda presión para proporcionar un adsorbedor de hidrocarburo descargado y una corriente de gas adsorbido recuperado que comprende la corriente de gas de barrido y etano adesorbido; y (e) poner en contacto el adsorbedor de hidrocarburo descargado con la corriente de gas de barrido a la primera presión para proporcionar el adsorbedor de hidrocarburo descargado con la corriente de gas de barrido a la primera presión para proporcionar el adsorbedor de hidrocarburo purgado y un gas de barrido agotado.

ethylene separation with pressure swing adsorption

Ethylene separation with pressure swing adsorption

A process for component separation in a polymer production system comprising: (a) separating a polymerization product into a gas stream and a polymer stream; (b) processing the gas stream in distillation columns to yield a light hydrocarbon stream (LHS) comprising ethylene and ethane; (c) contacting LHS with a purged hydrocarbon adsorber to yield a loaded hydrocarbon adsorber and a non-adsorbed gas stream, wherein ethane is adsorbed by the purged hydrocarbon adsorber at a first pressure to yield adsorbed ethane, and wherein the non-adsorbed gas stream comprises recovered ethylene; (d) contacting the loaded hydrocarbon adsorber with a sweeping gas stream at a second pressure to yield an unloaded hydrocarbon adsorber and a recovered adsorbed gas stream comprising the sweeping gas stream and desorbed ethane; and (e) contacting the unloaded hydrocarbon adsorber with the sweeping gas stream at the first pressure to yield the purged hydrocarbon adsorber and a spent sweeping gas.

Ethylbenzene dehydrogenation plant for producing styrene and relative process

하나 이상의 단열 반응 장비가 직렬로 위치하는 반응 섹션, 및 최소 하나의 제1 수증기 열교환 장비가 있는 수증기 회로를 포함하는 스타이렌 제조를 위한 에틸벤젠 탈수소 플랜트에 있어서; 상기 플랜트는 스타이렌을 제공하는 에틸벤젠의 탈수소 공정 동안 형성된 연무의 재순환에 의한 가열 회로가 있는 가열 설비를 포함함을 특징으로 하고, 여기서 상기 가열 설비는 상기 가열 회로에 의하여 서로 유체 소통하는 하기 장비를 포함하는 탈수소 플랜트: 하나 이상의 초고온-가열 장비, 최소 하나의 수증기 확산기, 하나의 버너 및 최소 하나의 혼합 장비가 삽입되는 하나 이상의 연소 장치, 하나 이상의 통풍 장치(들). An ethylbenzene dehydrogenation plant for styrene production comprising a reaction section in which one or more adiabatic reaction equipment is located in series, and a steam circuit with at least one first steam heat exchange equipment; The plant is characterized in that it comprises a heating facility with a heating circuit by recirculation of the fumes formed during the dehydrogenation process of ethylbenzene to provide styrene, wherein the heating facility is in fluid communication with each other by the heating circuit: Dehydrogenation plant comprising: One or more ultra-hot-heating equipment, One or more combustion devices in which at least one steam diffuser, one burner and at least one mixing equipment are inserted, One or more ventilation device(s).

A bed plate with supporting grid for a fluidized bed reactor and its modeling.

Un modelo dinámico de fluido que tiene al menos 5,000,000 celdas de la porción de un reactor de fase gaseosa desde la salida del condensador hasta un medio del diámetro del reactor por encima de la placa de lecho es útil para determinar el diseño de la superficie del fondo o la estructura de soporte para una placa de lecho para minimizar la acumulación de líquidos por debajo y por encima de la placa de lecho cuando se opera en un modo de condensación.

Modeling a bed plate and its use

A fluid dynamic model having at least 5,000,000 cells of the portion of a gas phase reactor from the exit of the condenser to a half a reactor diameter above the bed plate is useful in determining the design of the bottom surface or support structure for a bed plate to minimize liquid pooling below and above the bed plate when operating in condensing mode.

Process for the production of gasoline from fuel gas and catalytic reformate

Heat exchanger, reactor arrangement comprising said heat exchanger, and method for temperature control of a reactor

본 발명은 열교환기(1)에 관한 것이며, 그 열교환기는, - 수직으로 지향되고 열교환기 튜브 판(31)에 의해 바닥에서 종결되는 일군의 적어도 두 개의 열교환기 튜브(3), - 일군의 열교환기 튜브(3)를 둘러싸는 열교환기 하우징(5)으로서, 액체 열전달 매체(7)가 열교환기 하우징(5) 내에서 일군의 열교환기 튜브(3) 주위로 통과하는, 상기 열교환기 하우징, - 열교환기 하우징(5)의 상부를 밀봉하는 열교환기 캡(9), - 열교환기 하우징(5)의 바닥을 밀봉하는 열교환기 바닥(11), - 열교환기 하우징(5) 상에 제공되며 열교환기(1) 내측으로 이어지는, 열전달 매체(7)용 공급 지점(13), - 열교환기 하우징(5) 상에 제공되며 열교환기(1) 외측으로 이어지는, 열전달 매체(7)용 출구(15), 및 - 열교환기 캡(9)에 근접하여 배치된 비상 릴리프 포트(17)를 포함한다. 열교환기(1)는 열교환기 바닥(11)에 근접하여 배치된 안전 장치(19)를 포함한다. 본 발명은 또한, 반응로 설비(101)에 관한 것이며, 그 반응로 설비는, - 반응로(27), - 반응로(27)에 연결되는, 본 발명에 따른 열교환기(1), 및 - 반응로(27) 및/또는 열교환기(1)에 연결되며, 액체 열전달 매체(7)의 적어도 일부를 순환시키기 위한 펌프(29)를 포함한다. 마지막으로, 반응로(27)의 온도를 제어하기 위한 방법, 및 본 발명에 따른 열교환기(1)의 용도가 설명된다. The present invention relates to a heat exchanger (1), the heat exchanger comprising: - a group of at least two heat exchanger tubes (3) oriented vertically and terminated at the bottom by a heat exchanger tube plate (31); - a heat exchanger housing (5) surrounding a group of heat exchanger tubes (3), wherein a liquid heat transfer medium (7) passes in the heat exchanger housing (5) around the group of heat exchanger tubes (3) group housing, - a heat exchanger cap (9) sealing the upper part of the heat exchanger housing (5), - a heat exchanger bottom (11) sealing the bottom of the heat exchanger housing (5), - a feed point 13 for the heat transfer medium 7 provided on the heat exchanger housing 5 and running inside the heat exchanger 1 , - an outlet 15 for the heat transfer medium 7 provided on the heat exchanger housing 5 and running outside the heat exchanger 1 , and - an emergency relief port (17) arranged close to the heat exchanger cap (9); The heat exchanger 1 comprises a safety device 19 arranged close to the bottom of the heat exchanger 11 . The present invention also relates to a reactor facility (101), the reactor facility comprising: - reactor (27), - a heat exchanger (1) according to the invention, connected to the reactor (27), and - a pump (29) ...

Enhancement of quality of soft olefins in disturbance fluidized catalyst bed reactor

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

Method for synthetic methane using fluidized bed

본원 발명은 전환율을 높일 수 있는 메탄 유동층 반응기 및 이를 이용한 메탄의 생산 방법에 관한 것으로서, 제올라이트 등의 흡착제를 사용하여 반응이 진행되는 중에도 물을 계속 흡착함으로써, 반응이 평형상태에 이르지 않고 계속적으로 정반응이 진행될 수 있다. The present invention relates to a methane fluidized bed reactor capable of increasing the conversion rate and a method for producing methane using the same.By continuously adsorbing water while the reaction is in progress using an adsorbent such as zeolite, the reaction does not reach an equilibrium state and continues to react positively. Can proceed.

Temperature controlled in situ wax purification

수소 함유 처리 기체가 슬러리와 접촉하는 제 2 온도를 갖는 처리 대역을 통해 제 1 온도를 갖는 합성 대역으로부터의 슬러리를 순환시킴으로써, 액체 합성 생성물 및 촉매 입자를 포함하는 HCS 슬러리로부터 탄화수소 왁스 생성물을 정제한다. 상기 기체 처리는 탄화수소 왁스 생성물로부터 불순물을 제거하고 또한 슬러리에 존재할 수 있는 촉매 탈활성화 종도 제거한다. 정제된 왁스 생성물을 처리된 슬러리로부터 왁스 회수 수단을 통해 분리 및 제거한다. 이는 왁스 생성물을 추가로 처리할 필요를 없애거나 최소화시킨다. 잔류하는 처리된 슬러리는 합성 대역으로 회송시킬 수도 있다.

Dual-bed catalytic distillation tower and method for preparing dimethyl ether using the same

A dual-bed catalytic distillation tower has a catalytic column having an upper catalytic bed filled with low temperature dehydration catalysts and a lower catalytic bed filled with high temperature dehydration catalysts. When using the dual-bed catalytic distillation tower, the feed may be fed to the tower at the top of the upper catalytic bed, between the upper and lower catalytic beds, or at the bottom of the lower catalytic bed for dehydration to obtain DME. The dual-bed catalytic distillation tower has the advantage of flexible set up depending on various feeds, such as anhydrous or crude methanol and on different grades of DME to be obtained.

Dual-bed catalytic distillation tower and method for preparing dimethyl ether using the same

A dual-bed catalytic distillation tower has a catalytic column having an upper catalytic bed filled with low temperature dehydration catalysts and a lower catalytic bed filled with high temperature dehydration catalysts. When using the dual-bed catalytic distillation tower, the feeding may be fed to the tower at the top of the upper catalytic bed, between the upper and lower catalytic beds, or at the bottom of the lower catalytic bed for dehydration to obtain DME. The dual-bed catalytic distillation tower has the advantage of flexible set-up depending on various feedings such as anhydrous or crude methanol and on different grades of DME to be obtained.

Method and installation for producing methanol from under-stoichiometric synthesis gas

Es wird ein Verfahren zum Herstellen von Methanol aus Synthesegas mittels mehrstufiger, beispielsweise zweistufiger, heterogen-katalytischer Methanolsynthese vorgeschlagen, wobei das in jeder Synthesestufe gebildete Methanol-Produkt durch Kondensation abgetrennt wird und das verbliebene Restgas der stromabwärts angeordneten Synthesestufe aufgegeben oder nach Abtrennen eines Spülstroms als Recyclestrom zu der ersten Synthesestufe zurückgeführt wird. Erfindungsgemäß wird aus den Restgasströmen nach jeder Synthesestufe jeweils ein Spülstrom abgetrennt, aus denen mittels einer oder mehrerer Wasserstoffrückgewinnungsvorrichtungen Wasserstoff abgetrennt und zu der ersten Synthesestufe zurückgeführt. Gegebenenfalls kann das Verhältnis der einzelnen Spülströme sowie ihr Gesamtmengenstrom variiert werden, um das Reaktionsgeschehen in den einzelnen Synthesestufen besser kontrollieren zu können und auf das Fortschreiten der Desaktivierung der in ihnen enthaltenen Katalysatoren reagieren zu können. A process is proposed for producing methanol from synthesis gas by means of multi-stage, for example two-stage, heterogeneous-catalytic methanol synthesis, in which the methanol product formed in each synthesis stage is separated off by condensation and the remaining residual gas is fed to the synthesis stage arranged downstream or, after separating off a flushing stream, as Recycle stream is returned to the first synthesis stage. According to the invention, a purge stream is separated from the residual gas streams after each synthesis stage, from which hydrogen is separated by means of one or more hydrogen recovery devices and returned to the first synthesis stage. If necessary, the ratio of the individual flushing streams and their total flow rate can be varied in order to be able to better control the reaction in the individual synthesis stages and to be able to react to the progress of the deactivation of the catalysts contained in them.

METHOD FOR OPERATING A FLUIDIZED BED INCINERATOR, AND MEANS FOR CARRYING OUT SAID METHOD

L'invention concerne un dispositif d'incinérateur à lit fluidisé. Selon l'invention, l'incinérateur à lit fluidisé comporte une chambre de combustion contenant un milieu formant lit fluidisé et est caractérisé en ce qu'il comporte des moyens 7 pour dériver le milieu formant lit fluidisé à partir de la chambre de combustion 1, un échangeur de chaleur 8 destiné à être alimenté avec le milieu formant lit fluidisé durant la dérivation à partir de la chambre de combustion, et des moyens 12 pour transférer ledit milieu de l'échangeur de chaleur 8 vers la chambre de combustion 1. Le dispositif de l'invention permet d'obtenir un incinérateur solide qui fournit des gaz d'échappement à une température suffisamment basse pour qu'ils puissent être utilisés par exemple par des chaudières d'importance moyenne.

Patent FR2443878B1

Dimethyl terephthalate prepared by the esterification of terephthalic acid

Dimethyl terephthalate is prepared by the continuous esterification of terephthalic acid in the gas phase by evaporating solid terephthalic acid in a pre-reactor by means of a hot methanol vapor stream, conducting the gas mixture through a solid bed catalyst in a follow-up reactor, and recirculating a portion of the reaction product to the pre-reactor.

Ethylbenzene dehydrogenation plant for producing styrene and relative process

An ethylbenzene dehydrogenation plant for producing styrene which comprises a reaction section in which one or more adiabatic reaction apparatuses are positioned in series, and a steam circuit in which there is at least one first steam heat exchange apparatus; said plant being characterized in that it comprises heating equipment in which there is a heating circuit by means of recirculation of the fumes formed during dehydrogenation processes of ethylbenzene to give styrene, wherein said heating equipment comprises the following apparatuses in fluid communication with each other by means of said heating circuit: one or more ultra-heating apparatuses, one or more combustion devices in which at least one steam diffuser, one burner and at least one mixing apparatus are inserted, one or more ventilation device(s).

Zone reactor incorporating reversible hydrogen halide capture and release

An improved process and a zone reactor for converting a hydrocarbon feedstock into higher hydrocarbons is provided. A first zone in the reactor contains both a material capable of releasing hydrogen halide (HX) and a carbon-carbon coupling catalyst; a second zone is initially empty or contains a halogenation and/or oxyhalogenation catalyst; and a third zone contains both a carbon-carbon coupling catalyst and a material capable of capturing HX. Air or oxygen is introduced into the first zone, a feedstock is introduced into the second zone, and products are produced in the third zone. HX produced during the reaction is reversibly captured and released in zones 1 and 3.

Ethylbenzene dehydrogenation plant for producing styrene and relative process.

Una planta de deshidrogenación de etilbenceno para producir estireno la cual comprende una sección de reacción en donde están colocados en serie uno o más aparatos de reacción adiabática y un circuito de vapor en el cual hay por lo menos un primer aparato intercambiador de calor de vapor; dicha planta que se caracteriza porque comprende equipo de calentamiento en el cual hay un circuito de calentamiento por medio de recirculación de los vapores formados durante los procesos de deshidrogenación del etilbenceno para dar estireno, en donde dicho equipo de calentamiento comprende los siguientes aparatos en comunicación de fluido entre ellos por medio de dicho circuito de calentamiento: uno o más aparatos de ultracalentamiento, uno o más dispositivos de combustión en los cuales hay insertados por lo menos un difusor de vapor, un quemador y por lo menos un aparato de mezclado, uno o más dispositivos de ventilación.

Removal of catalyst fines from a reaction system

本发明提供了限制催化剂颗粒通过离开反应系统的烯烃产物物流和再生器烟道气物流损失的方法。特别地，本发明提供了使用水流从反应器中和使用两步分离法从再生器中脱除催化剂颗粒的方法。该两步法包括使用催化剂细粉分离装置。