СПОСОБ ГАЗОФАЗНОЙ ПОЛИМЕРИЗАЦИИ ОЛЕФИНОВ

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

СПОСОБ И УСТРОЙСТВО ДЛЯ СНИЖЕНИЯ ЗАГРЯЗНИТЕЛЕЙ ОКРУЖАЮЩЕЙ СРЕДЫ В ТЯЖЕЛОМ СУДОВОМ ЖИДКОМ ТОПЛИВЕ

Изобретение относится к двум вариантам способа снижения загрязнителей окружающей среды в тяжелом судовом жидком топливе. Один из вариантов включает: смешивание некоторого количества сырья тяжелого судового жидкого топлива с некоторым количеством водородного газа в качестве активирующего газа с получением смеси исходного сырья; контактирование смеси сырья с катализаторами, в качестве которых используют по меньшей мере катализатор гидродеметаллирования и катализатор гидродесульфурации, с образованием технологической смеси из смеси сырья; получение указанной технологической смеси и отделение жидких компонентов продукта тяжелого судового жидкого топлива технологической смеси от газообразных компонентов и побочных углеводородных компонентов технологической смеси и выгрузку продукта тяжелого судового жидкого топлива, при этом осуществляют выборочное удаление загрязнений окружающей среды из исходного сырья тяжелого судового жидкого топлива с обеспечением контакта смеси сырья сначала со слоем катализатора ...

КОНТАКТОР С РАЗДЕЛЕННЫМ ПОТОКОМ

... 1. Контактор с разделенным потоком, содержащий: ! корпус, имеющий первую головку и вторую головку, расположенную на ней; ! два или более отдельных неподвижных слоя, расположенных по поперечному сечению корпуса; ! один или более не имеющих препятствий проходов для потока, для обхода каждого неподвижного слоя; и ! одну или более перегородок, расположенных между неподвижными слоями, причем каждый неподвижный слой содержит один или более катализаторов, одну или более ионообменных смол, один или более абсорбентов, один или более адсорбентов или любое их сочетание. ! 2. Контактор по п.1, дополнительно содержащий один или более распределителей, расположенных рядом с выпускным концом одного или более проходов для потока. ! 3. Контактор по п.1, в котором каждый неподвижный слой содержит первый инертный слой, второй инертный слой, и активный слой, содержащий один или более катализаторов, ионообменных смол, абсорбентов, адсорбентов или любое их сочетание, активный слой расположен между первым инертным ...

СПОСОБ ПОЛУЧЕНИЯ РАСПЛАВЛЕННОГО ЧУГУНА И УСТАНОВКА ДЛЯ ПОЛУЧЕНИЯ РАСПЛАВЛЕННОГО ЧУГУНА

... 1. Установка для получения расплавленного чугуна, содержащая: ! по меньшей мере один реактор восстановления с псевдоожиженным слоем, в котором восстанавливают мелкодисперсную железную руду и превращают эту мелкодисперсную железную руду в восстановленное железо; ! бункер для загрузки мелкодисперсной железной руды, из которого подают мелкодисперсную железную руду в реактор восстановления с псевдоожиженным слоем; ! линию для загрузки мелкодисперсной железной руды, которая непосредственно соединяет бункер для загрузки мелкодисперсной железной руды с каждым из реакторов восстановления с псевдоожиженным слоем, и через которую непосредственно загружают мелкодисперсную железную руду в каждый из реакторов восстановления с псевдоожиженным слоем; ! плавильную печь-газификатор, в которую загружают кусковые углеродсодержащие материалы и восстановленное железо и подают кислород, при этом в плавильной печи-газификаторе получают расплавленный чугун; и ! линию подачи восстановительного газа, по которой ...

УСТАНОВКА ДЛЯ ПОЛУЧЕНИЯ РАСПЛАВЛЕННОГО ЧУГУНА

... 1. Установка для получения расплавленного чугуна, включающая: ! по меньшей мере один реактор восстановления с псевдоожиженным слоем, в котором восстанавливают железную руду и придают ей пластичность, и превращают эту железную руду в восстановленные материалы; ! плавильную печь-газификатор, в которую загружают восстановленную руду и вводят кислород, и в плавильной печи-газификаторе изготавливают расплавленный чугун и ! линию подачи восстановительного газа, по которой подают восстановительный газ, выходящий из плавильной печи-газификатора, в реактор восстановления с псевдоожиженным слоем, ! где реактор восстановления с псевдоожиженным слоем включает циклон, который установлен в этом реакторе восстановления с псевдоожиженным слоем для того, чтобы собирать мелкодисперсную железную руду, и ! где к циклону присоединен газовый инжектор, с помощью которого предотвращают слипание мелкодисперсной руды путем введения углеродсодержащего газа. ! 2. Установка по п.1, в которой газовый инжектор присоединен ...

Precipitated silica for use, e.g., in tires, battery separators or anti-blocking agents is produced in Taylor reactor fed with aqueous silicate solution and acidifying agent

The inlet(s) of a Taylor reactor comprising an outer reactor with an inner rotor, and used for the production of precipitated silica, is(are) fed with an aqueous silicate solution and an acidifying agent. An Independent claim is included for the precipitated silica.

Reactor comprising a diffusion bonded heat exchanger that is suitable for use in the steam reforming of hydrocarbons

A reactor vessel comprises (a) a first region for performing an endothermic reaction, in particular the steam reforming of a hydrocarbon, preferably, methane; (b) a second region for performing an exothermic reaction, in particular the combustion of a hydrocarbon fuel, preferably, methane, in the presence of oxygen or air; and (c) a means to transfer the heat energy released from the second region (b) to promote the endothermic reaction in the first region (a). The heat transfer means is a diffusion bonded heat exchanger comprising two sets of channels with the first set of channels forming at least part of the first region (a) and a second set of channels forming at least part of the second region (b) and arranged so that heat transfer occurs between both sets of channels. The channels may be arranged parallel to each other; perpendicular to each other or they may be interleaved with each other. The diameter of the first set of channels may be smaller than, equivalent to or greater than ...

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.

Protein production

Compact reactor

Method of activating a catalyst, reactor, and method of obtaining hydrocarbons in the fischer-tropsch process

The invention relates to Fischer-Tropsch synthesis in its compact form. A compact reactor comprises a housing having rectangular reaction channels accommodated therein and filled with a cobalt catalyst, nozzles for injecting synthesis gas in an amount determined by the ratio of the number of channels to the number of synthesis gas injection nozzles, and a nozzle for injecting and withdrawing a heat-transfer agent, on which nozzle a pressure regulator and an assembly for the withdrawal of synthetic hydrocarbons is arranged. The cobalt catalyst is activated by passing oxygen through the same. Synthetic hydrocarbons are obtained when synthesis gas is passed through the reaction channels of the reactor, which are filled with activated cobalt catalyst. Every 300-500 hours, the flow rate of the synthesis gas is increased, and then there is a return to the initial process conditions. This allows high-molecular hydrocarbon output per unit mass of the reactor to be achieved.

Method of activating a catalyst, reactor, and method of obtaining hydrocarbons in the fischer-tropsch process

POLYOLEFIN TREATMENT FOR THE SEPARATION OF VOLATILE MATERIAL

PROCEDURE FOR CONTACTING A HYDROCARBON AND AN OXYGEN-CONTAINING GAS WITH A CATALYST BED

PROCEDURE FOR THE THERMAL TREATMENT OF POLYESTER PARTICLES AND PROCEDURE FOR THE MULTI-LEVEL FIXED PHASE POLYCONDENSATION OF POLYESTER PARTICLES

PROCEDURE FOR THE CATALYTIC POLYMERIZATION OF OLEFINEN, A REACTOR SYSTEM AND ITS USE IN THIS PROCEDURE.

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

PROCEDURE FOR THE GASEOUS PHASE POLYMERIZATION OF OLEFINEN

IMPROVED DEEP CATALYTIC CRACKING PROCEDURE

PROCEDURE FOR THE MULTI-LEVEL FIXED PHASE POLYCONDENSATION OF POLYETHYLENE TEREPHTHALATE

PROCEDURE FOR THE HYDRAULIC TRANSFORMATION OF HEAVY RAW MATERIALS IN A FLUIDIZED BED ALSO FROM ABOVE TAKING PLACE FILLING OF THE RAW MATERIAL INTO THE REACTOR

TURBULENT FLUID BED PARAFFIN CONVERSION PROCESS

PROCESS AND APPARATUS FOR THE DIRECT REDUCTION OF IRON OXIDES IN AN ELECTROTHERMAL FLUIDIZED BED AND RESULANT PRODUCT

A continuous reaction device for synthesizing polyoxymethylene dimethyl ethers

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

Process and apparatus for preparation of phosphorus oxyacids from elemental phosphorus

SUPPORTED MICROPOROUS CERAMIC MEMBRANES

METHOD AND APPARATUS FOR UPGRADING BITUMINOUS MATERIAL

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

PROCESS FOR MAKING TETRACHLOROPROPENE BY CATALYZED GAS-PHASE DEHYDROCHLORINATION OF PENTACHLOROPROPANE

The present disclosure relates to catalyzed gas-phase dehydrochlorination of a pentachloropropane to form a tetrachloropropene with high selectivity and purity.

PROCESS AND DEVICE FOR REDUCING ENVIRONMENTAL CONTAMINATES IN HEAVY MARINE FUEL OIL

A process and device for reducing the environmental contaminants in a ISO 8217 compliant Feedstock Heavy Marine Fuel Oil, the process involving: mixing a quantity of the Feedstock Heavy Marine Fuel Oil with a quantity of Activating Gas mixture to give a feedstock mixture; contacting the feedstock mixture with one or more catalysts to form a Process Mixture from the feedstock mixture; separating the Product Heavy Marine Fuel Oil liquid components of the Process Mixture from the gaseous components and by-product hydrocarbon components of the Process Mixture and, discharging the Product Heavy Marine Fuel Oil. The Product Heavy Marine Fuel Oil is compliant with ISO 821 7 for residual marine fuel oils and has a sulfur level has a maximum sulfur content (ISO 14596 or ISO 8754) between the range of 0.05 % wt. to 0.5 % wt.. The Product Heavy Marine Fuel Oil can be used as or as a blending stock for an ISO 8217 compliant, IMO MARPOL Annex VI (revised) compliant low sulfur or ultralow sulfur heavy ...

CATALYTIC OXIDATION PROCESS WITH FLOW CONTROL SYSTEM

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

PROCESS FOR HYDRODEMETALLATION OF HYDROCARBON OILS SUCH AS PETROLEUM RESIDUA

METHOD FOR MANUFACTURING MOLTEN IRONS AND APPARATUS FOR MANUFACTURING MOLTEN IRONS

The present invention relates to a method for manufacturing molten iron that improves charging and discharge of the fine iron ore, and an apparatus for manufacturing molten iron using the same. The apparatus for manufacturing molten iron according to an embodiment of the present invention includes i) at least one fluidized-bed reduction reactor that reduces fine iron ore and converts the fine iron ore into reduced iron, ii) a fine iron ore charging bin that supplies the fine iron ore to the fluidized-bed reduction reactor, iii) a fine iron ore charging line that directly connects the fine iron ore charging bin to each of the fluidized-bed reduction reactors, and directly charges the fine iron ore into each of the fluidized-bed reduction reactor, iv) a melter- gasifier into which lumped carbonaceous materials and the reduced iron are charged and oxygen is injected, the melter-gasifier manufacturing molten iron, and v) a reducing gas supply line that supplies a reducing gas discharged from ...

GAS JET INJECTOR REACTOR FOR CATALYTIC FAST PYROLYSIS

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

DISCONTINUOUS PROCESS FOR CONDUCTING A HETEROGENEOUSLY CATALYSED REACTION AND INSTALLATION FOR HETEROGENEOUSLY CATALYSED MANUFACTURE OF PRODUCTS

D 8521 A b s t r a c t A discontinuous process for conducting a heterogeneously catalyzed reaction and a plant for the heterogeneously catalyzed production of products The invention relates firstly to a discontinuous process for conducting a heterogeneously catalyzed reaction taking place at elevated temperature, in which heat-sensi-tive products are formed, a heat transfer unit (4) different from the reactor (1) being used for heating and a fixed-bed catalyst (3) being used as the catalyst and the reaction mixture being continuously circulated in succession through the catalyst (3) and then through the heat transfer unit (4). The problem to be solved in this process is to avoid losses of catalyst and product and to shorten the batch time and, optionally, the reaction time in accordance with German patent applications P 38 13 612.0 and P 38 26 320.3. The invention also relates to a plant for the discontinuous heterogeneously catalyzed production of heatsensitive products at elevated temperature ...

Verfahren zur katalytischen Oxydation von Abgasen

Procédé de copolymérisation en continu du styrène et des huiles insaturées

СПОСОБ И УСТАНОВКА ДЛЯ КАЛЬЦИНИРОВАНИЯ

Изобретение относится к способу кальцинирования пылевидного или мелкозернистого гипса, включающему две стадии флэш-кальцинирования гипса в кальцинирующей мельнице (3) и повторного кальцинирования горячего гипса в реакционной емкости (6). Согласно изобретению предусмотрено, что повторное кальцинирование осуществляют в реакционной емкости (6) при подаче влажного газа, при этом реакционная емкость (6) не подогревается. Повторное кальцинирование осуществляют с долговременной продолжительностью обработки, которая по меньшей мере в 10 раз, предпочтительно от 50 до 100 раз, превышает продолжительность обработки при флэш-кальцинировании. Изобретение позволяет добиться без дополнительных энергетических затрат полного завершения кальцинирования, причем остающийся при флэш-кальцинировании дигидрат дополнительно переходит дальше в полугидрат и снижается доля нежелательного ангидрита. Таким образом достигается гомогенизация, а также повышение качества продукта. Может быть снижена температура в подключенной ...

УСТРОЙСТВО ДЛЯ ИЗГОТОВЛЕНИЯ ЧУГУНА

Устройство для изготовления чугунов согласно типичному воплощению изобретения включает (i) по меньшей мере один восстановительный реактор с псевдосжиженным слоем, который восстанавливает и пластифицирует железную руду, превращая ее в восстановленные материалы; (іі) плавильный газогенератор, в который для изготовления чугуна загружают восстановленную руду и вдувают оксиген; и (ііі) линию подачи восстановительного газа, которая подает восстановительный газ из плавильного газогенератора в восстановительный реактор с псевдосжиженным слоем, причем восстановительный реактор с псевдосжиженным слоем включает циклон, установленный в нем для сбора тонкомеленой железной руды. К циклону присоединена газовая форсунка, которая предотвращает слипание тонкомеленой руды вдуванием карбоносоджержащего газа.

METHOD AND INSTALLATION FOR PREPARATION AND SUPPLYING TO SUSPENSION THE CATALYST BESIDE THE REACTOR OF THE POLYMERIZATION

METHOD OF THE CONTACT OF HYDROCARBON AND OXYGEN-CONTAINING GAS WITH THE CATALYST BED

СПОСОБ КОНТАКТИРОВАНИЯ УГЛЕВОДОРОДА И КИСЛОРОДСОДЕРЖАЩЕГО ГАЗА СО СЛОЕМ КАТАЛИЗАТОРА

Настоящее изобретение представляет собой способ контактирования углеводорода и кислородсодержащего газа со слоем катализатора в реакторе при объемной скорости, составляющей по крайней мере 10000 ч-1, отличающийся тем, что: а) реактор имеет многоугольное внутреннее поперечное сечение, по крайней мере, в том отделе, в котором находится слой катализатора; б) слой катализатора составлен из двух или более слоев катализатора в виде пластин многоугольной формы, которые имеют по крайней мере четыре стороны; в) каждый слой катализатора включает по крайней мере четыре пластины, которые накладываются мозаичным образом с образованием указанного слоя; г) грани двух пластин, соприкасающиеся в одном слое, не накладываются на грани пластин, соприкасающиеся в примыкающем слое.

СПОСОБ И УСТАНОВКА ДЛЯ ПРИГОТОВЛЕНИЯ И ПОДАЧИ СУСПЕНЗИИ КАТАЛИЗАТОРА В РЕАКТОР ПОЛИМЕРИЗАЦИИ

The present invention relates to an apparatus for preparing and supplying catalyst to an ethylene slurry loop polymerisation reactor and to an apparatus for controlling the injection of catalyst slurry in a polymerization reactor wherein polyethylene is prepared. The present invention also relates to a method for optimising catalyst supply to a polymerisation reactor. The diluted catalyst is transferred to the reactor (1) using a membrane pump (5) controllable in function of the concentration of a reactant in said reactor (1).

SYSTEM AND METHODS FOR PREPARING CERAMIC POWDERS

Method for directionally synthesizing gasoline or diesel oil through Fischer-Tropsch process

Proceeded for the styrenation continues unsaturated oils

Process for the catalytic oxidation of gases of reject

Conditioning solids returning from a gas-solid separator, comprises introducing solids in an inlet placed at a first end of a reactor, injecting a conditioning gas in a chamber, and counter-currently circulating the gas in the reactor

Selon ce procédé : - on introduit les solides à conditionner (10) dans un réacteur (202) comprenant une vis sans fin (204), - on admet, à un. débit compris entre 1 et 60 kg/hr, un gaz de conditionnement (7) au sein du réacteur, et on fait circuler ce gaz de conditionnement dans le réacteur à contre-courant des solides, - on règle le débit de solides et les dimensions de la vis sans fin, afin que le temps de passage des solides, au contact du gaz de conditionnement, soit compris entre 30 secondes et 8 minutes, de préférence entre 1 et 5 minutes, et - on extrait les solides ainsi conditionnés (8), de façon à les renvoyer vers le séparateur.

PRODUCTION METHOD OF OLEFIN USING CIRCULATING FLUIDIZED BED PROCESS

The present invention relates to a circulating fluidized bed process for producing olefin from a hydrocarbon raw material using a fast fluidized bed, and suggests a preferred process form to increase the production of olefin more efficiently. According to the present invention, by using a catalyst capable of dehydrogenation reaction and a high-speed fluidization region during a circulating fluidized bed process, more sufficient catalyst volume fraction and distribution in which the dehydrogenation reaction can occur are provided, so that the production amount of olefin can be effectively increased, and in particular, the excellent selectivity for propylene can be maintained. COPYRIGHT KIPO 2019 (AA) Height of an ascending pipe [m] (BB) Catalyst volume ratio ε_s[-] ...

MULTIPLE BURN ZONES WITH INDEPENDENT CIRCULATION LOOPS

APPARATUS FOR HEAT TREATMENT OF POLYESTER PARTICLES, AND, SOLID PHASE POLYCONDENSATION METHODS IN MULTI-STAGES FOR POLYESTER PARTICLES, AND OF PRODUCING A POLYESTER, AND A POLYETHYLENE TEREPHTHALATE

reator com injetor de jato de gás para pirólise rápida catalítica

Supported rhodium-spinel catalysts and process for producing synthesis gas

Rhodium-spinel catalysts with activity for efficiently catalyzing the net partial oxidation of methane at high selectivities for CO and H2products are disclosed, along with their method of making. A syngas production process employing such catalysts for the net catalytic partial oxidation of a C1-C5hydrocarbon (e.g., natural gas or methane) to a product gas mixture comprising CO and H2is also disclosed. Preferred reaction conditions include maintaining the catalyst at a temperature of about 400-1,200° C., superatmospheric pressure, and flow rate sufficient to pass the reactant gas mixture over the catalyst at space velocities of at least about 100,000-25,000,000 hr−1.

BIOMASS CONVERSION SYSTEMS AND METHODS FOR USE THEREOF

Digestion of cellulosic biomass solids to form a hydrolysate may be accompanied by decomposition if the soluble carbohydrates produced from the biomass under hydrothermal digestion conditions are not transformed into a more stable reaction product. Biomass conversion systems may be configured to address this issue and others. Biomass conversion systems can comprise: a hydrothermal digestion unit; a first catalytic reduction reactor unit fluidly coupled to the hydrothermal digestion unit along its height by two or more fluid inlet lines and two or more fluid return lines, the first catalytic reduction reactor unit containing a catalyst capable of activating molecular hydrogen; and a fluid circulation loop comprising the hydrothermal digestion unit and a second catalytic reduction reactor unit that contains a catalyst capable of activating molecular hydrogen.

Multi-Stage Device for Reducing Environmental Contaminates in Heavy Marine Fuel Oil

A multi-stage device for reducing the environmental contaminants in an ISO8217 compliant Feedstock Heavy Marine Fuel Oil involving a core desulfurizing process and an ionic liquid extraction desulfurizing process as either a pre-treating step or post-treating step to the core process. The Product Heavy Marine Fuel Oil is compliant with ISO 8217 for residual marine fuel oils and has a sulfur level has a maximum sulfur content (ISO 14596 or ISO 8754) between the range of 0.05% wt. to 0.5% wt. 1. A device for reducing the environmental contaminants in a Feedstock Heavy Marine Fuel Oil , the device comprising: means for contacting a Feedstock Heavy Marine Fuel Oil with an ionic liquid under extractive desulfurizing conditions to give a pre-treated Feedstock Heavy Marine Fuel Oil; means for mixing a quantity of the pre-treated Feedstock Heavy Marine Fuel Oil with a quantity of Activating Gas mixture to give a Feedstock Mixture; means for contacting the Feedstock Mixture with one or more catalysts under desulfurizing conditions to form a Process Mixture from said Feedstock Mixture; means for receiving said Process Mixture and separating liquid components of the Process Mixture from any gaseous components and any by-product hydrocarbon components of the Process Mixture to form a Product Heavy Marine Fuel Oil and , means for discharging the Product Heavy Marine Fuel Oil.2. The device of claim 1 , wherein the means for contacting a Feedstock Heavy Marine Fuel Oil with a ionic liquid under extractive desulfurizing conditions to give a pre-treated Feedstock Heavy Marine Fuel Oil comprises of a contacting vessel having a first feed inlet pipe through which the Feedstock Heavy Marine Fuel Oil is introduced into the contacting vessel and a second feed inlet pipe through which a sulfur lean ionic liquid is introduced into the contacting vessel; one or more contacting devices or mixing devices in the contacting vessel for forming an emulsion like mixture of the Feedstock Heavy ...

Module for continuous transformation of at least one fluid product, associated unit and method.

Ce module comporte une enceinte (22), au moins un premier tube (26A) de transformation du produit. Le premier tube (26A) comprend une entrée (52A) d'injection de produit, une région intermédiaire (44A) en forme d'hélice disposée dans l'enceinte, et une sortie (54A) de récupération de produit transformé. Le premier tube (26A) délimite une lumière interne (51) continue de circulation du produit entre l'entrée d'injection (52A) et la sortie de récupération (54A), l'entrée d'injection (52A) et la sortie de récupération (54A) faisant saillie hors de l'enceinte (22). Dans la région intermédiaire (44A), le rapport du rayon de l'hélice à l'étendue transversale maximale de la lumière interne (51) est compris entre 20 et 100, avantageusement inférieur entre 20 et 70.

METHOD FOR PRODUCING CHLORINE BY MULTI STEP ADIABATIC GAS PHASE OXIDATION

REACTION DISTILLATION APPARATUS AND REACTION DISTILLATION METHOD

A reaction distillation apparatus which can be applied to a relatively complicated reaction comprising the combination of two or more stages of equilibrium reactions, and a reaction distillation method which can efficiently conduct this reaction. Raw material feed pipes (5, 6 and 7) are connected to a reaction distillation column (1). These raw material feed pipes (5, 6 and 7) are sequentially disposed at mutually different stages from the column top. More preferably, the reaction distillation column (1) is equipped with stages not having a raw material feed pipe connected thereto, between the first stage at which the raw material feed pipe (5) is connected and the second stage at which the raw material feed pipe (6) is connected, and between the second stage and the third stage at which the raw material feed pipe (7) is connected. The raw material (A) is supplied from the raw material feed pipe (5), the raw material (B) is supplied from the raw material feed pipe (6) and the raw material ...

КОНТАКТОР С РАЗДЕЛЕННЫМ ПОТОКОМ

Группа изобретений относится к устройствам и способам приведения в контакт жидкости, газа и/или многофазной смеси с твердыми продуктами в виде частиц. Контактор с разделенным потоком содержит корпус, имеющий первую головку и вторую головку, расположенную на ней, два или более отдельных неподвижных слоя, расположенных по поперечному сечению корпуса, один или более не имеющих препятствий проходов для потока для обхода каждого неподвижного слоя и одну или более перегородок, расположенных между неподвижными слоями. Каждый неподвижный слой содержит один или более катализаторов, одну или более ионообменных смол, один или более абсорбентов, один или более адсорбентов или любое их сочетание. Согласно способу модернизации резервуара внутри резервуара размещают два или более поддерживающих сит, причем каждое сито располагается отдельно, формируют один или более не имеющих препятствий проходов для потока через каждое из поддерживающих сит и размещают одну или более перегородок между соседними поддерживающими ...

СПОСОБЫ ИЗМЕНЕНИЯ СКОРОСТИ ПРОИЗВОДСТВА ПОЛИОЛЕФИНОВ С ПРИМЕНЕНИЕМ КОМПОЗИЦИИ ИНДУЦИРОВАННЫХ КОНДЕНСИРУЮЩИХ АГЕНТОВ

FIELD: chemistry. SUBSTANCE: polymerisation of polyolefin, which is carried out by bringing into contact in the reactor an olefin monomer and optionally a comonomer with a catalyst system in the presence of induced condensing agents (ICA) and optionally hydrogen. ICA can contain two or more ICA components. Change in relative concentration of two or more components of ICA is carried out in accordance with equivalence factors of ICA, which enable to increase rate of production of polyolefin while maintaining temperature of adhesion, increase rate of production of polyolefin with increase in temperature drop of dew point ICA. EFFECT: ICA composition influences rate of polyolefin production. 10 cl, 4 dwg, 1 tbl, 1 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 696 875 C2 (51) МПК C08F 2/34 (2006.01) C08F 10/00 (2006.01) C08F 10/02 (2006.01) B01J 8/18 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК C08F 2/34 (2019.05); C08F 110/02 (2019.05); B01J 8/003 (2019.05); B01J 8/0055 (2019.05); B01J 8/006 (2019.05); B01J 8/1809 (2019.05); B01J 8/1827 (2019.05); B01J 8/1836 (2019.05); B01J 8/24 (2019.05) (21)(22) Заявка: 2017120186, 24.11.2015 24.11.2015 Дата регистрации: 07.08.2019 25.11.2014 US 62/084,271 (43) Дата публикации заявки: 10.12.2018 Бюл. № 34 (45) Опубликовано: 07.08.2019 Бюл. № 22 (86) Заявка PCT: US 2015/062465 (24.11.2015) C 2 C 2 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 08.06.2017 (56) Список документов, цитированных в отчете о поиске: WO 2014/039519 А1, 13.03.2014. WO 2014/039522 А1, 13.03.2014. US 6391986 В1, 21.05.2002. ЕР 1040129 А1, 04.10.2000. US 2007/ 265400 А1, 15.11.2007. WO 2011/147539 А1, 01.12.2011. RU 2448981 C2, 27.04.2012. (87) Публикация заявки PCT: 2 6 9 6 8 7 5 WO 2016/086006 (02.06.2016) R U 2 6 9 6 8 7 5 (73) Патентообладатель(и): ЮНИВЕЙШН ТЕКНОЛОДЖИЗ, ЭлЭлСи (US) Приоритет(ы): (30) Конвенционный приоритет: R U (24) Дата начала отсчета срока действия патента: (72) ...

УСТРОЙСТВО И СПОСОБ ГЛУБОКОГО КАТАЛИТИЧЕСКОГО КРЕКИНГА УГЛЕВОДОРОДНОГО СЫРЬЯ

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

УСТАНОВКА ДЛЯ ПОЛУЧЕНИЯ РАСПЛАВЛЕННОГО ЧУГУНА

Изобретение относится к установке для получения расплавленного чугуна. Установка включает, по меньшей мере, один реактор восстановления с псевдоожиженным слоем, в котором восстанавливают железную руду и придают ей пластичность, плавильную печь-газификатор, в которую загружают восстановленную руду и вводят кислород с изготовлением расплавленного чугуна, и линию подачи восстановительного газа, выходящего из плавильной печи-газификатора, в реактор восстановления с псевдоожиженным слоем. В реакторе восстановления с псевдоожиженным слоем установлен циклон для сбора мелкодисперсной железной руды. К циклону присоединен газовый инжектор, с помощью которого предотвращают слипание мелкодисперсной руды путем введения в циклон углеродсодержащего газа. Газовый инжектор включает линию ввода газа, которая при соединении с циклоном проходит вдоль вертикальной оси через верхнюю часть реактора восстановления с псевдоожиженным слоем. Линия ввода газа охватывает циклон и может иметь форму спирали или ее часть ...

СПОСОБ УМЕНЬШЕНИЯ ЗАГРЯЗНЕНИЯ ОКРУЖАЮЩЕЙ СРЕДЫ ИСХОДНЫМ СЫРЬЕМ ТЯЖЕЛОГО СУДОВОГО ЖИДКОГО ТОПЛИВА И УСТРОЙСТВО ДЛЯ ЕГО ОСУЩЕСТВЛЕНИЯ

БЫСТРАЯ ПЕРЕРАБОТКА МЕТАЛЛОСОДЕРЖАЩИХ ХИМИЧЕСКИХ СОЕДИНЕНИЙ ДЛЯ ОБРАЗОВАНИЯ МЕТАЛЛОВ ИЛИ ОКИСЛОВ МЕТАЛЛОВ

... 1. Способ переработки металлосодержащего химического соединения для образования металла или окисла металла металлосодержащего химического соединения, предусматривающий нагрев металлосодержащего химического соединения со скоростью от приблизительно 100 до примерно 100000000°С/с до повышенной температуры, которая делает конверсию металлосодержащего химического соединения термодинамически благоприятной, и выдержку металлосодержащего химического соединения при повышенной температуре в течение времени обработки, которого достаточно для преобразования металлосодержащего химического соединения, по меньшей мере, в один продукт, выбранный из группы, состоящей из (1) металла и (2) окислов металла. 2. Способ по п.1, в котором время обработки имеет продолжительность от приблизительно 0,1 до примерно 60 с. 3. Способ по п.1, в котором конверсию осуществляют посредством разложения. 4. Способ по п.1, в котором конверсию осуществляют посредством окисления. 5. Способ по п.1, в котором конверсию осуществляют ...

ЦИКЛОННОЕ РАЗДЕЛИТЕЛЬНОЕ УСТРОЙСТВО, ИМЕЮЩЕЕ КЕССОН С КОРОТКОЙ ПРОДОЛЖИТЕЛЬНОСТЬЮ ПРЕБЫВАНИЯ, УСТАНОВЛЕННЫЙ В РЕАКЦИОННОМ РЕЗЕРВУАРЕ С ПСЕВДООЖИЖЕННЫМ СЛОЕМ

УСТРОЙСТВО И СПОСОБ ГЛУБОКОГО КАТАЛИТИЧЕСКОГО КРЕКИНГА УГЛЕВОДОРОДНОГО СЫРЬЯ

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

Production of chlorine by catalytic gas-phase oxidation of hydrogen chloride with oxygen, involves using a multi-zone reactor with special heat exchangers between successive zones to cool the process gas

A method for the production of chlorine by the adiabatic gas-phase oxidation of hydrogen chloride with oxygen on a catalyst bed in a reactor with at least two separate zones from at least one of which the process gas is then passed through a heat exchanger, involves using a heat exchanger with a stack of connected plates, each with at least two separate flow channels in a predetermined pattern, arranged so that the process gas flows in one direction and the heat exchange medium in another. An independent claim is included for a reactor system for this process as described above.

A method and apparatus for fabricating a carbon nanotube

CONVERSION OF COMBUSTIBLE GAS MIXTURES

Fluidized bed reactor with residence time control

Method for manufacturing molten irons and apparatus for manufacturing molten irons

METHOD AND DEVICE FOR THE HEAT TREATMENT OF GRANULAR SOLIDS

The present invention concerns a method for the heat treatment of granular solids. In this regard, the solids are initially introduced into a first reactor configured as a flash reactor or fluidized bed reactor where they are brought into contact with hot gases at temperatures in the range 500°C to 1500°C. Next, the solids are passed through a residence time reactor in which they are fluidized. The residence time reactor is configured in a manner such that it has various regions which are separated from one another, from which the solid can be withdrawn in a manner such that it is provided with a variety of residence times in the residence time reactor.

IMPROVED DEEP CATALYTIC CRACKING PROCESS

The present invention provides a catalytic cracking reactor system and process in which a riser reactor is configured to have two sections (2, 4) of different radii in order to produce improved selectivity to propene and butenes as products.

CATALYTIC FIXED BED REACTOR FOR PRODUCING ETHYLENE OXIDE BY PARTIAL OXIDATION OF ETHYLENE

A method and a reaction vessel for producing gaseous ethylene oxide from partial oxidation of hydrocarbon using a heterogeneous catalyst fixed bed comprising: - introducing gaseous ethylene, oxygen, ballast gas, and catalyst promoter into a reaction vessel having a catalyst bed with a length such that an outflow area and an inflow area over said catalyst bed length in between the reactor outflow and inflow has an absolute ratio difference less than or equal to 1.3 m; said catalyst having a selectivity greater than 80%; - circulating a heat transfer fluid through at least one coolant heat exchanger in said shell interior; said heat exchanger having a coolant flow cross sectional area ratio to cooling surface area less than 1; - flowing said gaseous ethylene, oxygen, ballast gas and catalyst promoter over said catalyst and through an outlet zone in said reactor vessel, said zone configured with an average residence time of less than or equal to 4 seconds from the catalyst bed to the heat ...

MULTIPLE BURN ZONES WITH INDEPENDENT CIRCULATION LOOPS

A process for a continuous regeneration of a catalyst wherein the regeneration section includes at least two separate zones. The regeneration includes a combustion zone, and an oxygen boost zone, where the process utilizes at least two independent regeneration gas loops for control of the amount of oxygen to regenerate the catalyst.

HEAT INTEGRATED REFORMER WITH CATALYTIC COMBUSTION FOR HYDROGEN PRODUCTION

A heat integrated steam reformer, which incorporates a catalytic combustor, which can be used in a fuel processor for hydrogen production from a fuel source, is described. The reformer assembly comprises a reforming section and a combustion section, separated by a wall. Catalyst (21) able to induce the reforming reactions is placed in the reforming section, either in the form of pellets or in the form of coating on a suitable structured catalyst substrate such as fecralloy sheets. Catalyst (22) able to induce the combustion reactions is placed in the combustion section in the form of coating on suitable structured catalyst substrate such as fecralloy sheet. A steam and fuel mixture (30) is supplied to the reforming section (14) where it is reformed to produce hydrogen. A fuel and an oxygen (32) containing gas mixture is supplied to the combustion section where it is catalytically combusted to supply the heat for the reformer. The close placement of the combustion and reforming catalysts ...

MODIFIED SULFUR, METHOD FOR PREPARING SAME, APPARATUS FOR PREPARING SAME, AND USE THEREOF

The present application relates to modified sulfur, to a method for preparing same, and to an apparatus for preparing same. The modified sulfur is radioactive or includes a fine structure such as a fibrous structure, a tabular structure, or a network structure. The modified sulfur may be prepared by a process of inducing polymerization or aging using ultrasonic waves. The modified sulfur may have various excellent characteristics such as anticorrosion, water resistance, strength, and high-speed drying, and such characteristics may be adjusted based on the viscosity or the degree of polymerization. Further, as the modified sulfur has the above-described characteristics, the modified sulfur can be applied to an anticorrosive material or water-resistant material, and the modified sulfur can be used in the production of an anticorrosive material and water-resistant material having superior workability and hardening properties, resistance to salt spray, weldability, and the like at an optimum ...

ЭКСТРАКЦИЯ ПОД ВЫСОКИМ ДАВЛЕНИЕМ

... 1. Технологическое устройство для обработки одного или более материалов, состоящее из одной или более емкостей, расположенных ниже поверхности земли, из которых одна или более емкостей предназначены для приема одного или более материалов или их части, причем одна или более емкостей включают зону реакции, впускное средство для подачи по меньшей мере одного из материалов в зону реакции и выпускное средство для вывода обработанного материала из зоны реакции, в котором по меньшей мере одна из емкостей простирается на глубину под поверхностью земли, достаточную для создания давления гидростатического напора во впускном и/или выпускном средстве, причем впускное средство содержит по меньшей мере две трубы. 2. Технологическое устройство по п.1, содержащее также две или более емкостей, расположенных ниже поверхности земли, из которых каждая емкость предназначена для приема по меньшей мере одного материала, каждая из емкостей включает зону реакции, впускное средство для подачи по меньшей мере одного ...

СПОСОБ КАТАЛИТИЧЕСКОЙ ПОЛИМЕРИЗАЦИИ ОЛЕФИНОВ, РЕАКТОРНАЯ СИСТЕМА И ЕЕ ПРИМЕНЕНИЕ

Изобретение относится к способу каталитической полимеризации олефинов, в котором олефины контактируют с сыпучим катализатором в псевдоожиженном слое и движущемся слое таким образом, что время пребывания в псевдоожиженном слое и время пребывания в движущемся слое регулируются независимо к реакторной системе, включающей реактор с псевдоожиженным слоем, оборудованный вводом для реагирующего материала, выводом для продукта и устройством для поддержания псевдоожиженного слоя в реакторе с псевдоожиженным слоем, и реактор с движущимся слоем, оборудованный вводом, непосредственно соединенным с реактором с псевдоожиженным слоем, и выводом, соединенным с реактором с псевдоожиженным слоем, благодаря чему время пребывания в реакторе с псевдоожиженным слоем и время пребывания в реакторе с движущимся слоем регулируются независимо, и к ее применению для каталитической полимеризации олефинов.

УСТРОЙСТВО ДЛЯ ИЗГОТОВЛЕНИЯ ЖИДКОГО ЧУГУНА

Устройство для изготовления чугуна в соответствии с типичным воплощением изобретения включает и) как минимум один восстановительный реактор с псевдоожиженным слоем, который превращает железную руду в восстановленные материалы восстановлением и пластификацией железной руды, ii) плавильный газогенератор, в который для изготовления чугуна загружают восстановленные материалы и вдувают кислород, и iii) линию подачи восстановительного газа, которым подают восстановительный газ, образованный в плавильном газогенераторе, в восстановительный реактор с псевдоожиженным слоем. Восстановительный реактор с псевдоожиженным слоем имеет газовую форсунку, которая вдувает газ в восстановительный реактор с псевдоожиженным слоем для удаления застойных слоев.

СПОСОБ И УСТРОЙСТВО (ВАРИАНТЫ) ДЛЯ ИЗГОТОВЛЕНИЯ ЧУГУНА

Изобретение касается способа изготовления чугуна, который усовершенствует загрузку и выгрузку тонкоизмельченной железной руды, и устройства для изготовления чугуна, в котором используется этот способ. Устройство для изготовления чугуна в соответствии с осуществлением изобретения включает ) как минимум один восстановительный реактор с псевдоожиженным слоем для восстановления тонкоизмельченной железной руды и превращение тонкоизмельченной железной руды в восстановленное железо, ) загрузочный бункер тонкоизмельченной железной руды для подачи этой руды в восстановительный реактор с псевдоожиженным слоем, ) линию загрузки тонкоизмельченной железной руды, которая непосредственно соединяет загрузочный бункер тонкоизмельченной железной руды с каждым восстановительным реактором с псевдоожиженным слоем и непосредственно загружает тонкоизмельченную железную руду в каждый восстановительный реактор с псевдоожиженным слоем, iv) плавильный газогенератор, в котором изготовляется чугун и в который загружают ...

СПОСОБ КАТАЛИТИЧЕСКОЙ ПОЛИМЕРИЗАЦИИ ОЛЕФИНОВ И РЕАКТОРНАЯ СИСТЕМА

Настоящее изобретение относится к способу каталитической полимеризации олефинов, включающему следующие стадии: i) первую полимеризацию в первом реакторе, в котором олефины полимеризуют в присутствии мелкодисперсного катализатора, водорода и необязательного сомономера в среде инертного низкокипящего углеводорода с образованием реакционной смеси, содержащей полимеризованные олефины; и ii) вторую полимеризацию во втором реакторе, в котором полимеризованные олефины подвергают дополнительной полимеризации в псевдоожиженном слое и в подвижном слое при таких условиях, которые позволяют независимо регулировать время пребывания в псевдоожиженном слое и время пребывания в подвижном слое; изобретение также относится к реакторной системе для осуществления указанного способа, ее применению, полиолефинам, получаемым с помощью рассматриваемого способа и к применению таких полиолефинов.

УСТРОЙСТВО И СПОСОБ НЕПРЕРЫВНОЙ ТЕРМООБРАБОТКИ СЫПУЧИХ МАТЕРИАЛОВ

Изобретение относится к устройству (1) для непрерывной термообработки гранулированного материала, в частности для кристаллизации полимерного гранулята, такого как, например, полиэтилентерефталат. Устройство содержит несколько смежных камер (2, 3, 4, 5, 6) с кипящим слоем, снабженных дырчатым днищем (11), через которое в соответствующую камеру может вдуваться снизу через отверстие (9) газ для псевдоожижения гранулята и отводиться через отверстие (10) в потолочной части устройства. На долю первой камеры (2) приходится большая часть общего объема всех камер (2, 3, 4, 5, 6), смежные камеры сообщены с помощью отверстий (18, 19, 20, 21; 28, 29, 30, 31) для прохода материала, выполненных в перегородках (14, 15, 16, 17) между этими камерами. Согласно способу, использующему устройство (1) согласно изобретению, гранулированный материал направляют через несколько смежных камер (2, 3, 4, 5, 6) с кипящим слоем, при этом абсолютный уровень заполнения первой камеры (2) псевдоожижаемым гранулятом соответствует ...

METHOD OF CATALYTIC POLYMERIZATION OF OLEFINS, REACTOR SYSTEM, ITS APPLICATION, POLYOLEFINS AND THEIR APPLICATION

EXTRACTION UNDER HIGH PRESSURE

Apparatus and method for catalytically converting chemical species at residence time 0.1-10 seconds

CATALYTIC REACTOR

Liquid phase xylene isomerization in the absence of hydrogen

The field of this claimed subject matter generally relates to liquid phase isomerization technology. More specification, the field relates to liquid phase isomerization in complete absence of hydrogen which eliminates the need for gas-liquid separation at the reactor outlet. Even in the absence of the hydrogen, the catalyst demonstrates a stable isomerization performance with a paraxylene to xylene ratio of 23 wt% in the product stream.

METHOD FOR THE PRODUCTION OF NANOPARTICLES

The present invention relates to methods for the production of nanoparticles which may be optionally coated. In particular, the present invention relates to methods for the production of nanoparticles characterized in that precursors are subjected to substantially the same amount of activation energy or combination of activation energies in the activation zone at a predetermined concentration of precursors and at a predetermined time of exposure to the activation energy/energies. Furthermore, the present invention relates to nanoparticles produced by the methods according to the present invention. Finally, the present invention concerns a device for producing nanoparticles according to the method of the present invention. The invention provides for a tighter particle size distribution of the generated nanoparticles. The activation energy is selected from the group of RF, MW, IR, plasma, heat and photon absorption.

MULTIFUNCTIONAL CHEMICAL REACTOR

A chamber (1 ) for a chemical reactor (100), comprising: - a lower base (2) provided with a through hole (2c), - an upper opening (8), - a perimeter wall (5), - an internal volume (V), - a hydraulic guard (4) equipped with an internal cylinder (6) and an outer cylinder (7) fitted onto said inner cylinder (6), - a plurality of blades (10) placed on the outer cylinder (7) to cause a stirring state in a fluid contained in said chamber (1). - a rotating shaft (9) connected to the outer cylinder (7), - a weir (3, 30) passing through the lower base (2) and slidingly coupled with a through hole (12, 32) of the lower base (2).

FLUIDIZED BED REACTOR WITH RESIDENCE TIME CONTROL

Disclosed is an apparatus and process for controlling residence time in a reaction zone by adjusting the effect of reactor volume by varying the elevation of feed introduction or the space velocity in a fluidized catalytic conversion reactor. Changing effective volume results in controllable residence time and/or space velocity. The effect of reactor volume may be changed by altering the space velocity the feed distributor elevation, diluent flow rate or the number of reaction subsections to which feed is distributed.

Hydrodesulfurization process utilizing a distillation column realtor

A process for the hydrodesulfurization of petroleum streams is disclosed wherein the sulfur containing petroleum stream is contacted along with hydrogen at a partial pressure of less than 70 psig in a distillation column reactor containing a hydrodesulfurization catalyst in the form of a catalytic distillation structure.

CONTINUOUS REACTION DEVICE FOR SYNTHESIZING POLYOXYMETHYLENE DIMETHYL ETHERS

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

СПОСОБ КАТАЛИТИЧЕСКОГО КРЕКИНГА ДЛЯ ОБРАБОТКИ ФРАКЦИИ, ИМЕЮЩЕЙ НИЗКИЙ УГЛЕРОДНЫЙ ОСТАТОК КОНРАДСОНА

Изобретение относится к способу каталитического крекинга в псевдоожиженном слое слабо коксующегося исходного сырья, имеющего углеродный остаток Конрадсона, равный или менее 0,1% мас., и содержание водорода, равное или более 12,7% мас., содержащий, по меньшей мере, стадию крекинга исходного сырья в присутствии катализатора, стадию разделения/отпаривания выходящих потоков из коксованных частиц катализатора, стадию регенерирования указанных частиц при частичном или полном сгорании кокса, и рециркуляцию к гомогенно распределенному и слабо коксованному катализатору перед регенерацией по меньшей мере одного коксующегося углеродного и/или углеводородного выходящего потока. При этом способ характеризуется тем, что количество коксующегося выходящего потока в коксованный катализатор регулируется так, чтобы подавать дополнительное количество кокса Qв катализатор и удовлетворять следующему уравнению (I):в котором Qпредставляет собой начальное содержание кокса коксованного катализатора после того, как ...

РЕАКТОР С ПСЕВДООЖИЖЕННЫМ СЛОЕМ НЕПРЕРЫВНОГО ДЕЙСТВИЯ

Изобретение относится к способу и устройству для непрерывного псевдоожижения, которое содержит две ячейки, соединенные отверстием, предоставляющим возможность введения твердого материала в следующую ячейку, расположенную ниже по потоку, посредством псевдоожиженного горизонтального потока, изолированное «свободное» пространство внутри каждой ячейки, две фильтровальные трубки, размещенные внутри изолированного «свободного» пространства каждой ячейки, один клапан обратной продувки, размещенный внутри каждой фильтровальной трубки. Устройство обеспечивает возможность обработки материалов, которые обычно трудно псевдоожижаются, посредством поддержания постоянной разности давлений между каждым изолированным «свободным» пространством. 3 н. и 14 з.п. ф-лы, 3 ил., 1 пр.

Hydrogen production by an autothermal heat exchanger packed-bed membrane gas reformer

A process for producing hydrogen from natural gas, said process comprises the steps of: (i) providing an autothermal heat exchanger packed-bed membrane reformer (APBMR) comprising: (a) an elongated external gas oxidation compartment comprising an inlet, an outlet and packed oxidation catalyst particles, said inlet and outlet being located each at one extremity of said external gas oxidation compartment; (b) an elongated internal gas steam-reforming compartment comprising an inlet, an outlet and packed steam-reforming catalyst particles, said inlet and outlet being located each at one extremity of said internal gas steam-reforming compartment; (c) one or more hydrogen-separating membrane(s) positioned in said steam-reforming compartment substantially parallel to the longitudinal axis of said steam-reforming compartment; (d) one insulation layer surrounding said external compartment; and, optionally, (e) one or more elongated internal gas oxidation compartment(s) positioned in said steamreforming compartment substantially parallel to the longitudinal axis of said gas steam-reforming internal compartment, and comprising an inlet, an outlet and packed oxidation catalyst particles, said inlet and outlet being located each at an extremity of said internal gas oxidation compartment(s); (ii) supplying a mixture comprising said natural gas and air to said gas oxidation compartment(s) of said reformer; and (iii) supplying a mixture comprising said natural gas and water to said gas steam-reforming compartment, wherein the water-to-gas molar ratio

Split Flow Contactor

Systems and methods for contacting a liquid, gas, and/or a multi-phase mixture with particulate solids. The system can include a body having a first head and a second head disposed thereon. Two or more discrete fixed beds can be disposed across a cross-section of the body. One or more unobstructed fluid flow paths can bypass each fixed bed, and one or more baffles can be disposed between the fixed beds.

Multiple burn zones with independent circulation loops

A process for a continuous regeneration of a catalyst wherein the regeneration section includes at least two separate zones. The regeneration includes a combustion zone, and an oxygen boost zone, where the process utilizes at least two independent regeneration gas loops for control of the amount of oxygen to regenerate the catalyst.

Method and device for the heat treatment of granular solids

A method for the heat treatment of granular solids includes initially introducing solids into a first reactor configured as a flash reactor or fluidized bed reactor where they are brought into contact with hot gases at temperatures in the range 500° C. to 1500° C. Next, the solids are passed through a residence time reactor in which they are fluidized. The residence time reactor is configured in a manner such that it has various regions which are separated from one another, from which the solid can be withdrawn in a manner such that it is provided with a variety of residence times in the residence time reactor. 1. A method for the heat treatment of granular solids , wherein the solids are initially introduced into a first reactor configured as a flash reactor or fluidized bed reactor where they are brought into contact with hot gases at temperatures in the range 500° C. to 1500° C. , and wherein the solids are then guided through a residence time reactor in which they are fluidized , wherein the residence time reactor is configured in a manner such that it is provided with various mutually separated regions from which the solid is separately removed in a manner such that it has a residence time in the residence time reactor which is of a variable duration , wherein removal from the various regions of the residence time reactor is carried out in a manner such that not all of the regions are fluidized , wherein the fluidized regions are fluidically connected in succession , whereby specific downstream regions are no longer fluidized and therefore actively removed.2. The method as claimed in claim 1 , wherein solid is actively removed from at least one region.3. The method as claimed in claim 1 , wherein the fluidized bed reactor is provided with a circulating fluidized bed.4. The method as claimed claim 1 , wherein the air is used as the fluidizing gas in the residence time reactor.5. The method as claimed in claim 1 , wherein the residence time in the first reactor ...

FCC YIELD SELECTIVITY IMPROVEMENTS IN HIGH CONTAINMENT RISER TERMINATION SYSTEMS

The invention provides an improved system for separation technology intended to reduce unwanted catalyst/thermal reactions by minimizing contact of the hydrocarbons and the catalyst within the reactor. 1. The process for increasing hydrocarbon yield and decreasing coke production in an FCC reactor having a separation unit and at least one chamber window , wherein the bottom of the separation unit is spaced apart from a bed of fluidized catalyst , comprising the step of locating the bed of fluidized catalyst level in the FCC reactor such that the bed of fluidized catalyst is directly above the at least one chamber windows of the separation unit.2. The process of wherein the catalyst bed level falls within the range of 125 IWC to 170 IWC.3. The process of wherein the catalyst bed density is 32.8 lbs/ftat an operating level of 125 IWC at an elevation of 164 ft.4. The process of wherein the catalyst bed density is 36.9 lbs/ftat an operating level of 140 IWC at an elevation of 164 ft.5. The process of wherein the catalyst bed density is 41 lbs/ftat an operating level of 150 IWC at an elevation of 164 ft.6. The process of wherein the catalyst bed density is 45.1 lbs/ftat an operating level of 170 IWC at an elevation of 164 ft.7. The process of wherein the distance between the bottom of the separation unit and the top of the catalyst bed is maximized to prevent fluidized catalyst from entering the bottom of the separator unit.8. The process of wherein fluidized catalyst is prevented from entering the separation unit by means of a baffle member positioned between the bottom of the separation unit and the top of the fluidized bed.9. The process of wherein hydrocarbon gases evacuate from the fluidized bed after residence in the catalyst through at least one vent tube which carry the clean hydrocarbon gases directly to the top region of the separator unit.10. A process for increasing hydrocarbon yield and decreasing coke production in an FCC reactor having a separation unit ...

Multi-Stage Process and Device for Distributive Production of a Low Sulfur Heavy Marine Fuel Oil

A multi-stage process for the distributive production of an ISO8217 compliant Product Heavy Marine Fuel Oil from ISO 8217 compliant Feedstock Heavy Marine Fuel Oil involving a core desulfurizing process that is distributed in a Reaction System composed of multiple reaction vessels. The Product Heavy Marine Fuel Oil has a sulfur level has a maximum sulfur content (ISO 14596 or ISO 8754) between the range of 0.05 mass % to 1.0 mass. A process plant for conducting the process for conducting the distributive process is disclosed that can utilize a modular reactor vessel contained within a frame work based on ISO 40 foot or ISO 20 foot container dimensions. 1. A process for the distributive production of a Heavy Marine Fuel Oil , the process comprising: mixing a quantity of Feedstock Heavy Marine Fuel Oil with a quantity of Activating Gas mixture to give a Feedstock Mixture; contacting the Feedstock Mixture with one or more catalysts under reactive conditions in a Reaction System to form a Process Mixture from said Feedstock Mixture; receiving said Process Mixture and separating the liquid components of the Process Mixture from the bulk gaseous components of the Process Mixture; subsequently separating any residual gaseous components and by-product hydrocarbon components from the Product Heavy Marine Fuel Oil; and , discharging the Product Heavy Marine Fuel Oil; wherein the Reaction System comprises two or more reactor vessels wherein said reactor vessels are configured in a matrix of at least 2 reactors by 2 reactors.2. The process of wherein the Feedstock Heavy Marine Fuel Oil complies with ISO 8217 (2017) and has a sulfur content (ISO 14596 or ISO 8754) between the range of 5.0 mass % to 1.0 mass % and wherein the Product Heavy Marine Fuel Oil complies with ISO 8217 (2017) and has a sulfur content (ISO 14596 or ISO 8754) between the range of 0.50 mass % to 0.05 mass %.3. The process of claim 2 , wherein said Feedstock Heavy Marine Fuel Oil has: a maximum of kinematic ...

METHODS AND APPARATUSES FOR PROCESSING HYDROCARBONS TO PRODUCE LIGHT OLEFINS

Light olefins may be produced from hydrocarbons by a method including passing a hydrocarbon feed stream into a feed inlet of a reactor. The reactor may include an upper reactor portion defining an upper reaction zone and a lower reactor portion defining a lower reaction zone. The catalyst may move in a generally downward direction through the upper reactor portion and the lower reactor portion, and the hydrocarbon feed stream may move in a generally upward direction through the upper reactor portion and lower reactor portion such that the hydrocarbon feed stream and the catalyst move with a counter-current orientation. Contacting the catalyst with the hydrocarbon feed stream may crack one or more components of the hydrocarbon feed stream and form a hydrocarbon product stream. The method may further include passing the hydrocarbon product stream out of the upper reaction zone through the hydrocarbon product outlet. 1. A method for processing hydrocarbons to produce light olefins , the method comprising: an upper reactor portion defining an upper reaction zone, the upper reactor portion comprising a catalyst inlet and a hydrocarbon product outlet, wherein the catalyst inlet and the hydrocarbon product outlet are positioned at or near the top of the upper reactor portion; and', 'a lower reactor portion defining a lower reaction zone, the lower reactor portion comprising a feed inlet and a catalyst outlet, wherein feed inlet and the catalyst outlet are positioned at or near the bottom of the lower reactor portion, and wherein the lower reaction zone is in fluid communication with and adjacent to the upper reaction zone; and', the catalyst moves in a generally downward direction through the upper reactor portion and the lower reactor portion and the hydrocarbon feed stream moves in a generally upward direction through the upper reactor portion and lower reactor portion such that the hydrocarbon feed stream and the catalyst move with a counter-current orientation;', 'the ...

METHOD FOR ACTIVATING A CATALYST, REACTOR, AND METHOD OF OBTAINING HYDROCARBONS IN FISCHER-TROPSCH PROCESS

The invention relates to Fischer-Tropsch synthesis in a compact version. A compact reactor comprises a housing, rectangular reaction channels inside the housing, which are filled with a cobalt catalyst, synthesis gas injection nozzles in the number determined by the ratio of the number of channels to the number of synthesis gas injection nozzles, an input and output nozzle for heat transfer medium on which a pressure controller installed, and an assembly for withdrawing synthetic hydrocarbons. The cobalt catalyst is activated by passing hydrogen through it. Synthetic hydrocarbons are produced by passing synthesis gas through the reaction channels filled with the activated cobalt catalyst. The space velocity of synthesis gas is increased every 300-500 h, followed by returning to the initial process conditions. This provides a high-molecular-weight hydrocarbon output per unit mass of the reactor. 1. A compact reactor for the production of synthetic hydrocarbons in a Fischer-Tropsch process , comprising a housing with reaction channels filled with a cobalt catalyst , wherein the channels have a thickness of 1 to 5 mm and a rectangular cross section; synthesis gas injection nozzles; input and output nozzles for heat transfer medium; and an assembly for withdrawing synthetic hydrocarbons , wherein the reactor is characterized in that a pressure controller is installed on the output nozzle for heat transfer medium , the outer surface of the wall of the reaction channels with the catalyst has a roughness of 1.6 to 25 μm , a distance between the nearest reaction channels is 1 to 5 mm , a thickness of the wall of the reaction channel is 1 to 3 mm , a width-to-thickness ratio of the reaction channel is 2 to 100 , and a height-to-thickness ratio of the reaction channel is from 20 to 2000 , wherein a ratio of the number of reaction channels to the number of synthesis gas injection nozzles is from 1 to 50.2. The reactor according to claim 1 , characterized in that a ratio of the ...

METHANATION REACTOR AND METHOD

The present relates to a chemical reactor comprising a catalyst bed enclosed in a reactor vessel and at least one cooling tube placed in the reactor vessel and passing through the catalyst bed, characterized in that the cooling tubes are disposed within the reactor so as to generate thermal gradients of at least 20° C./cm thereby generating hot spots throughout the reactor upon carrying out a reaction. The invention further relates to a methanation process. 121-. (canceled)22. A chemical reactor comprising a catalyst bed enclosed in a reactor vessel and at least one cooling tube placed in the reactor vessel and passing through the catalyst bed , characterized in that the cooling tubes are disposed within the reactor so as to generate thermal gradients of at least 20° C./cm thereby generating hot spots throughout the reactor upon carrying out a reaction.23. The chemical reactor according to claim 22 , characterized in that the catalysts comprises at least one of nickel claim 22 , cobalt and ruthenium based catalysts.24. The chemical reactor according to claim 22 , characterized in that the catalysts comprises 20% wt. Ni/AlOor 3% wt. Ru/AlO.25. The chemical reactor according to claim 22 , characterized in that it comprises at least two cooling tubes.26. The chemical reactor according to claim 22 , characterized in that the minimal distance between the tubes is not less than 1.5 times the tube diameter.27. The chemical reactor according to claim 22 , characterized in that the minimal distance between the tubes is not less than 2 times the tube diameter.28. The chemical reactor according to claim 22 , characterized in that the temperature of the cooling medium is different in the different tubes.29. The chemical reactor according to claim 22 , characterized in that the tubes are fed with a cooling medium.30. The chemical reactor according to claim 22 , characterized in that the thermal gradients are at least 100° C./cm.31. The chemical reactor according to claim 22 , ...

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

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

METHOD FOR CO-PRODUCTION OF 1-CHLORO-3,3,3-TRIFLUOROPROPENE, 2,3,3,3-TETRAFLUOROPROPENE AND 1,3,3,3-TETRAFLUOROPROPENE

This invention discloses a method for co-production of 1-chloro-3,3,3-trifluoropropene, 2,3,3,3-tetrafluoropropene and 1,3,3,3-tetrafluoropropene. This method includes inputting the mixed gases of hydrogen fluoride and 1,1,1,3,3-pentachloropropane together with 1,1,2,3-tetrachloropropene into a first reactor for a reaction to obtain a reaction product; directly inputting the reaction product into a second reactor to perform a reaction in the presence of a catalyst; separating hydrogen chloride from the obtained product; obtaining 1-chloro-3,3,3-trifluoropropene, 2,3,3,3-tetrafluoropropene and 1,3,3,3-tetrafluoropropene respectively after water washing, alkaline washing, drying and rectifying. This invention has the advantages of flexible production, simple process, small investment, low energy consumption and high conversion rate. 17-. (canceled)8. A method for co-production of 1-chloro-3 ,3 ,3-trifluoropropene , 2 ,3 ,3 ,3-tetrafluoropropene and 1 ,3 ,3 ,3-tetrafluoropropene , the method comprising:{'sup': '−1', '(a) preheating and then directing hydrogen fluoride and 1,1,1,3,3-pentachloropropane into a first reactor in a molar ratio of 9:1-15:1, wherein the first reactor comprises an upper section filled with an aluminum oxide supported chromium metal catalyst and a lower section filled with a chromic oxide supported indium metal catalyst, wherein the hydrogen fluoride and the 1,1,1,3,3-pentachloropropane are reacted in the upper section of the first reactor at a temperature of 200-400° C. and at an air flow rate of 300-1,000 h, and a product from the upper section enters the lower section of the first reactor to continuously react with the 1,1,2,3-tetrachloropropane to obtain a first reaction product of the first reactor, wherein a molar ratio of the 1,1,2,3-tetrachloropropane to the hydrogen fluoride in the lower section of the first reactor is 3:9-5:9;'}{'sup': '−1', '(b) directly directing the first reaction product of the first reactor into a second reactor ...

Catalytic Alkane Conversion and Olefin Separation

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

Fluidized Bed Dehydrogenation Process For Light Olefin Production

The present invention discloses process and apparatus for the production of light olefins from their respective alkanes by catalytic dehydrogenation, where in the dehydrogenation reaction is carried out in multiple semi-continuously operated fluidized bed isothermal reactors, connected to a common regenerator and wherein the process is carried out in a sequence of steps in each cycle i.e., entry of hot regenerated catalyst, pre-treatment with reducing gas, dehydrogenation reaction, stripping, transfer of catalyst to regenerator and catalyst regeneration. Process cycle in each reactor starts at different times such that the catalyst inventory in the regenerator is invariable with time. 2. The process as claimed in claim 1 , wherein the fluidized bed reactors are maintained under isothermal conditions by an additional heating element (F).3. The process as claimed in claim 1 , wherein the temperature of hot regenerated catalyst entering the reactor is 600-800° C. claim 1 , and wherein diluent stream comprises of nitrogen or steam or helium or any other gas claim 1 , and wherein pre-heated alkane feed is sent to reactor with or without diluents.4. The process as claimed in claim 1 , wherein the reducing gas is selected from the group consisting of hydrogen or methane or hydrogen containing gas or dry gas from FCCU or Pressure Swing Adsorption (PSA) off-gas from Hydrogen Generation Unit (HGU) or any combination thereof.5. The process as claimed in claim 1 , wherein the dehydrogenation reaction is carried out at a temperature in the range of 500-850° C. claim 1 , preferably 550-700° C.; pressure in the range of 0.1-3.0 bar; gas hourly space velocity (GHSV) of the feed stream in the range of 500-10000 h claim 1 , and molar ratio of diluent to hydrocarbon in the feed stream is in the range of 0.1 to 5.6. The process as claimed in claim 1 , wherein the alkane feed stream comprises of ethane or propane or iso-butane or n-butane or any combination.7. The process as claimed in ...

SALT-FREE PRODUCTION OF METHIONINE FROM METHIONINE NITRILE

The invention refers to the use of a particulate catalyst containing 60.0 to 99.5 wt. % ZrOstabilised with an oxide of the element Hf and at least one oxide of the element M, wherein M=Ce, Si, Ti, or Y, for the hydrolysis reaction of methionine amide to methionine, wherein the median particle size xof the particulate catalyst is in the range of from 0.8 to 9.0 mm, preferably of from 1.0 to 7.0 mm. The invention also refers to a process for preparing methionine comprising a step of contacting a solution or suspension comprising methionine amide and water with said particulate catalyst to provide a reaction mixture comprising methionine and/or its ammonium salt from which methionine can be isolated. 1. A method of catalyzing the hydrolysis reaction of methionine amide to methionine , the method comprising contacting a solution or suspension comprising methionine amide and water with a particulate catalyst to produce a reaction mixture comprising methionine ,wherein the particulate catalyst comprises:{'sub': '2', '#text': '60.0 to 99.5 wt. % ZrO;'}an oxide of the element Hf; andat least one oxide of the element M, wherein M=Ce, Si, Ti, or Y,{'sub': '2', '#text': 'wherein the ZrOis stabilized by the oxide of the element Hf and the at least one oxide of the element M, and'}{'sub': '50', '#text': 'wherein the median particle size xof the particulate catalyst is in the range of from 0.8 to 9.0 mm.'}2. The method of claim 1 , wherein the element M=Si claim 1 , Ti claim 1 , or Y.3. The method of claim 1 , wherein the particle size xof the particulate catalyst is in the range of from 0.5 to 8.0 mm.4. The method of claim 1 , wherein the particulate catalyst comprises 0.1 to 40 wt. % of oxides of the elements Hf claim 1 , Ce claim 1 , Si claim 1 , Ti claim 1 , and Y.5. The method of claim 1 , wherein the particulate catalyst comprises:{'sub': ['2', '2', '2', '2', '3', '2'], '#text': '0.5 to 3.0 wt. % HfOand at least one selected from the group consisting of 0.1 to 40 wt. % TiO, ...

Modified Supported Chromium Catalysts and Ethylene-Based Polymers Produced Therefrom

Supported chromium catalysts with an average valence less than +6 and having a hydrocarbon-containing or halogenated hydrocarbon-containing ligand attached to at least one bonding site on the chromium are disclosed, as well as ethylene-based polymers with terminal alkane, aromatic, or halogenated hydrocarbon chain ends. Another ethylene polymer characterized by at least 2 wt. % of the polymer having a molecular weight greater than 1,000,000 g/mol and at least 1.5 wt. % of the polymer having a molecular weight less than 1000 g/mol is provided, as well as an ethylene homopolymer with at least 3.5 methyl short chain branches and less than 0.6 butyl short chain branches per 1000 total carbon atoms.

Process And Device For Treating High Sulfur Heavy Marine Fuel Oil For Use As Feedstock In A Subsequent Refinery Unit

A multi-stage process for transforming a high sulfur ISO 8217 compliant Feedstock Heavy Marine Fuel Oil involving a core desulfurizing process that produces a Product Heavy Marine Fuel Oil that can be used as a feedstock for subsequent refinery process such as anode grade coking, needle coking and fluid catalytic cracking. The Product Heavy Marine Fuel Oil exhibits multiple properties desirable as a feedstock for those processes including a sulfur level has a maximum sulfur content (ISO 14596 or ISO 8754) between the range of 0.05 mass % to 1.0 mass. A process plant for conducting the process is also disclosed. 1. A process for treating high sulfur Heavy Marine Fuel Oil for use as feedstock in a subsequent refinery unit , the process comprising: mixing a quantity of Feedstock Heavy Marine Fuel Oil with a quantity of Activating Gas mixture to give a Feedstock Mixture; contacting the Feedstock Mixture with one or more catalysts under reactive conditions to form a Process Mixture from said Feedstock Mixture; receiving said Process Mixture and separating the liquid components of the Process Mixture from the bulk gaseous components of the Process Mixture; subsequently separating any residual gaseous components and by-product hydrocarbon components from the Process Mixture to form a Product Heavy Marine Fuel Oil; and , discharging the Product Heavy Marine Fuel Oil.2. The process of wherein the Feedstock Heavy Marine Fuel Oil complies with ISO 8217 (2017) and has a sulfur content (ISO 14596 or ISO 8754) between the range of 5.0 mass % to 1.0 mass % and wherein the Product Heavy Marine Fuel Oil has a sulfur content (ISO 14596 or ISO 8754) between the range of 0.50 mass % to 0.05 mass %.3. The process of claim 2 , further comprising fractionating the Product Heavy Marine Fuel Oil to remove a light to middle distillate fraction claim 2 , said light to middle distillate fraction have a maximum boiling point less than 650° F.4. The process of wherein the one or more catalysts ...

CHEMICAL LOOPING SYSTEMS FOR CONVERSION OF LOW- AND NO-CARBON FUELS TO HYDROGEN

Disclosed herein are systems and methods for producing H2 from low carbon fuels (LCFs) using metal oxides in a chemical looping process. 1. A system for converting a carbon-neutral or low-carbon fuel , the system comprising:a first reactor comprising a plurality of particles in which a primary metal oxide is disposed on a support, and an inlet for providing a carbon-neutral or low-carbon fuel, wherein the first reactor is configured to reduce the primary metal oxide to produce a reduced metal or a reduced metal oxide; and a second reactor configured to oxidize at least a portion of the reduced metal or reduced metal oxide from the first reactor, to regenerate the primary metal oxide.2. The system of claim 1 , wherein the fuel is selected from the group consisting of ammonia claim 1 , hydrazine claim 1 , carbohydrazide claim 1 , and hydrogen sulfide.3. The system of claim 2 , wherein the fuel is ammonia.4. The system of claim 1 , wherein the system is configured to operate at a temperature of between 50° C. and 2000° C.5. The system of claim 1 , wherein the system is configured to operate at a pressure of between 1 atm and 30 atm.6. The system of claim 1 , wherein the system is configured to operate at a GHSV of between 50 hrand 5000 hr.7. The system of claim 1 , wherein the first reactor comprises a co-current moving bed reactor claim 1 , a counter-current moving bed reactor claim 1 , a fluidized bed reactor claim 1 , or a fixed bed reactor.8. The system of claim 1 , wherein the second reactor comprises a co-current moving bed reactor claim 1 , a counter-current moving bed reactor claim 1 , a fluidized bed reactor claim 1 , or a fixed bed reactor.9. The system of claim 1 , wherein the inlet for the fuel is situated at the top claim 1 , in the middle claim 1 , or at the bottom of the first reactor.10. The system of claim 1 , wherein the primary metal oxide is FeO.11. The system of claim 1 , wherein the support is selected from the group consisting of oxides of Ti ...

SYSTEMS AND METHODS FOR MAKING CERAMIC POWDERS

Systems and methods for making ceramic powders configured with consistent, tailored characteristics and/or properties are provided herein. In some embodiments a system for making ceramic powders, includes: a reactor body having a reaction chamber and configured with a heat source to provide a hot zone along the reaction chamber; a sweep gas inlet configured to direct a sweep gas into the reaction chamber and a sweep gas outlet configured to direct an exhaust gas from the reaction chamber; a plurality of containers, within the reactor body, configured to retain at least one preform, wherein each container is configured to permit the sweep gas to flow therethrough, wherein the preform is configured to permit the sweep gas to flow there through, such that the precursor mixture is reacted in the hot zone to form a ceramic powder product having uniform properties. 136-. (canceled)37. A method for carbothermically producing a ceramic powder , the method comprising:a) preheating at least one container in a staging zone, wherein the at least one container comprises at least one preform, wherein the preform comprises carbon;b) moving the at least one container into a reactor body, wherein the reactor body comprises a reaction zone;c) carbothermically reacting the at least one preform in the reaction zone thereby producing a ceramic powder, wherein the carbothermically reacting comprises reducing, via the carbon of the preform, a metal compound of the preform to a metal carbide, a metal boride, or a metal nitride; andd) moving the at least one container from the reactor body to a receiving zone.38. The method of claim 37 , comprising flowing claim 37 , during at least the carbothermically reacting step claim 37 , a sweep gas into the at least one container.39. The method of claim 38 , wherein the at least one preform comprises a porosity claim 38 , wherein the flowing comprises flowing the sweep gas through at least one pore of the at least one preform.40. The method of claim ...

OXIDATIVE COUPLING OF METHANE SYSTEMS AND METHODS

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

Multi-Stage Process and Device for Treatment Heavy Marine Fuel Oil and Resultant Composition Including Ultrasound Promoted Desulfurization

A multi-stage process for reducing the environmental contaminants in an ISO8217 compliant Feedstock Heavy Marine Fuel Oil involving a core desulfurizing process and a ultrasound treatment process as either a pre-treating step or post-treating step to the core process. The Product Heavy Marine Fuel Oil complies with ISO 8217 for residual marine fuel oils and has a sulfur level has a maximum sulfur content (ISO 14596 or ISO 8754) between the range of 0.05 mass % to 1.0 mass. A process plant for conducting the process is also disclosed. 1. A process for reducing the environmental contaminants in a Feedstock Heavy Marine Fuel Oil , the process comprising: contacting a Feedstock Heavy Marine Fuel Oil , wherein the Feedstock Heavy Marine Fuel Oil complies with ISO 8217 except for the environmental contaminates including a sulfur content (ISO 14596 or ISO 8754) greater than 0.50 wt % , with ultrasound having a frequency in the range of about 10 kHz and about 100 megahertz and a sonic energy in the range of about 30 watts/cmto about 300 watts/cm , and a temperature ranging between 30° C. and 260° C. to give an ultrasonic pre-treated Feedstock Heavy Marine Fuel Oil; mixing a quantity of the ultrasonic pre-treated Feedstock Heavy Marine Fuel Oil with a quantity of Activating Gas mixture to give a Feedstock Mixture; contacting the Feedstock Mixture with one or more supported transition metal catalysts under reactive conditions to form a Process Mixture from said Feedstock Mixture; receiving said Process Mixture and separating the Product Heavy Marine Fuel Oil liquid components of the Process Mixture from the gaseous components and by-product hydrocarbon components of the Process Mixture and , discharging the Product Heavy Marine Fuel Oil.2. The process of claim 1 , wherein the step of contacting a Feedstock Heavy Marine Fuel Oil with ultrasound takes place in the presence of water or supercritical water in which the volume ratio of the Feedstock Heavy Marine Fuel Oil to the ...

DEVICE AND METHOD FOR CATALYTICALLY CONVERTING CHEMICAL SUBSTANCES AT DWELL TIMES IN THE RANGE OF 0.1-10 SECONDS

Disclosed herein is an apparatus and a method for catalytic conversion of chemical substances in the presence of pulverulent catalysts in a trickle bed reactor with residence times in the range of 0.1-10 seconds, wherein the apparatus includes a trickle bed reactor (), the inlet side of which is functionally connected to a catalyst reservoir vessel () and a reactant feed, and the outlet side of which is functionally connected to a separator (). The separator () has an exit conduit for leading off product stream, wherein the apparatus has the characteristic feature that the exit conduit disposed on the separator () for leading off product stream has a continuously acting valve connected via a controller to a pressure measurement sensor, wherein the continuously acting valve and the pressure measurement sensor form a pressure control circuit with a controller. 1: An apparatus for catalytic conversion of chemical substances in the presence of pulverulent catalysts in a trickle bed reactor with residence times in the range of 0.1-10 seconds , wherein:the apparatus comprises at least a trickle bed reactor, a catalyst reservoir vessel and a separator;the reactor is a tubular reactor having a length in the range of 0.3-3 m and a diameter in the range of 0.3-10 cm;an inlet side of the reactor is functionally connected to at least one catalyst reservoir vessel and at least one reactant feed, and an outlet side of the reactor is functionally connected to the at least one separator; the at least one separator having at least one exit conduit for leading off product stream; andthe apparatus has the characteristic feature that an exit conduit disposed on the separator for leading off product stream has a continuously acting valve connected via a controller to a pressure measurement sensor, in which the continuously acting valve and the pressure measurement sensor form a pressure control circuit with a controller.2: The apparatus according to claim 1 , wherein:the catalyst ...

Multi-Stage Process and Device Utilizing Structured Catalyst Beds and Reactive Distillation for the Production of a Low Sulfur Heavy Marine Fuel Oil

A multi-stage process for the production of an ISO8217 compliant Product Heavy Marine Fuel Oil from ISO 8217 compliant Feedstock Heavy Marine Fuel Oil involving a core process under reactive conditions in a Reaction System composed of one or more reaction vessels, wherein one or more of the reaction vessels contains one or more catalysts in the form of a structured catalyst bed and is operated under reactive distillation conditions. The Product Heavy Marine Fuel Oil has a sulfur level has a maximum sulfur content (ISO 14596 or ISO 8754) between the range of 0.05 mass % to 1.0 mass. A process plant for conducting the process for conducting the process is disclosed. 1. A process for the production of a Product Heavy Marine Fuel Oil , the process comprising: mixing a quantity of Feedstock Heavy Marine Fuel Oil , wherein Feedstock Heavy Marine Fuel Oil complies with ISO 8217 (2017) but has a sulfur content (ISO 14596 or ISO 8754) greater than 0.5% wt. with a quantity of Activating Gas mixture to give a Feedstock Mixture; contacting the Feedstock Mixture with one or more catalysts under reactive distillation conditions to promote the formation of a Process Mixture from said Feedstock Mixture , wherein said one or more catalysts are in the form of a structured catalyst bed; receiving said Process Mixture and separating the liquid components of the Process Mixture from the bulk gaseous components of the Process Mixture; and separating any residual gaseous components and by-product hydrocarbon components from the Product Heavy Marine Fuel Oil.2. The process of claim 1 , wherein the structured catalyst bed comprises a plurality of catalyst retention structures claim 1 , each catalyst retention structure composed of a pair of fluid permeable corrugated metal sheets claim 1 , wherein the pair of the fluid permeable corrugated metal sheets are aligned such that the corrugations are out of phase and thereby defining a catalyst rich space and a catalyst lean space within the ...

Process for producing lithiated transition metal oxides

Provided are processes for the formation of electrochemically active materials such as lithiated transition metal oxides that solve prior issues with throughput and calcination. The processes include forming the materials in the presence of a processing additive that includes potassium prior to calcination that produces active materials with increased primary particle grain sizes.

PROCESSES AND APPARATUSES FOR TOLUENE METHYLATION IN AN AROMATICS COMPLEX

This present disclosure relates to processes and apparatuses for toluene methylation in an aromatics complex for producing paraxylene. More specifically, the present disclosure relates to processes and apparatuses for toluene methylation within an aromatics complex for producing paraxylene wherein an embodiment uses a riser reactor, another embodiment uses a pre-reactor producing dimethyl ether, and another embodiment uses partial regeneration of the catalyst. 1. A process for alkylating an aromatic hydrocarbon reactant with an alkylating reagent comprising methanol to produce an alkylated aromatic product , comprising:introducing the aromatic hydrocarbon reactant into a mixing chamber comprising water;introducing the aromatic hydrocarbon into a riser reactor system, having a residence time of about 0.5 seconds to about 6 seconds, for producing the alkylated aromatic product;{'sup': 3', '3, 'wherein the riser reactor system comprises an operating bed density of about 0.05 kg/mto 0.29 kg/m; and'}recovering the alkylate aromatic product, produced by reaction of the aromatic reactant and the alkylating reagent, from the reactor system.2. The process of claim 1 , wherein the aromatic hydrocarbon reactant includes toluene claim 1 , the alkylating reagent includes methanol claim 1 , and the alkylated aromatic product includes xylene.3. The process of claim 1 , wherein the residence time in the riser reactor is 4 seconds.4. The process of claim 1 , wherein a fraction of the coked catalyst is recirculated from the top of the riser to the mixing chamber.5. The process of claim 1 , wherein a fraction of coked catalyst is cooled to remove heat of reaction and returned to the mixing chamber.6. The process of claim 1 , wherein a fraction of regenerated catalyst is returned to the mixing chamber.7. The process of claim 1 , wherein the riser reactor system comprises a temperature of about 500° C. to about 700° C.8. The process of claim 1 , wherein the weight hourly space velocity ...

MODIFIED SULFUR, METHOD FOR PREPARING SAME, APPARATUS FOR PREPARING SAME, AND USE THEREOF

Disclosure relates to modified sulfur, preparation method thereof, preparation equipment thereof. The modified sulfur has spinnability or includes micro-structures such as fiber-, film- and network-like structure. The modified sulfur can be prepared by inducing polymerization with ultrasonic or ageing. The modified sulfur has various excellent features such as anticorrosiveness, waterproofing, strength, and fast drying and can control the features depending on its viscosity or polymerization degree. In addition due to the above features, the modified sulfur can be applied to anticorrosive or waterproofing material and can prepare anticorrosive or waterproofing material which has good workability, hardening, salt spray resistance, and weldability exceeding a certain level, and specially improved adhesiveness. Furthermore, when applying the modified sulfur to asphalt composition, gelation and depression are reduced, properties such as bending strength and tensile strength are improved, and it is possible to obtain asphalt composition with good working stability at RT. 1. A method for preparing modified sulfur comprising:mixing 100 parts by weight of sulfur with 1˜300 parts by weight of dicyclopentadiene-based modifier and melting them at 120 or higher to prepare the first mixture;polymerizing the first mixture at 120 or higher to prepare the first reactant; andterminating the polymerization of the first reactant at the end point of the reaction to prepare modified sulfur,wherein the end point of the reaction is between the time when the first reactant obtains spinnability and the time when rubberization of the first reactant occurs, andwherein the modified sulfur prepared after the terminating has 3,000˜2,000,000 cP of viscosity at 135 and comprises micro-structures such as fiber, film, or network structure, or has spinnability.2. The method of claim 1 , wherein the first mixture claim 1 , the first reactant claim 1 , and their combinations may further comprise an ...

Modified sulfur, method for preparing same, apparatus for preparing same, and use thereof

Disclosure relates to modified sulfur, preparation method thereof, preparation equipment thereof. The modified sulfur has spinnability or includes micro-structures such as fiber-, film- and network-like structure. The modified sulfur can be prepared by inducing polymerization with ultrasonic or ageing. The modified sulfur has various excellent features such as anticorrosiveness, waterproofing, strength, and fast drying and can control the features depending on its viscosity or polymerization degree. In addition due to the above features, the modified sulfur can be applied to anticorrosive or waterproofing material and can prepare anticorrosive or waterproofing material which has good workability, hardening, salt spray resistance, and weldability exceeding a certain level, and specially improved adhesiveness. Furthermore, when applying the modified sulfur to asphalt composition, gelation and depression are reduced, properties such as bending strength and tensile strength are improved, and it is possible to obtain asphalt composition with good working stability at RT.

Fcc yield selectivity improvements in high containment riser termination systems

The invention provides an improved system for separation technology intended to reduce unwanted catalyst/thermal reactions by minimizing contact of the hydrocarbons and the catalyst within the reactor.

Heavy Marine Fuel Compositions

A process for reducing the environmental contaminants in a ISO8217 compliant Feedstock Heavy Marine Fuel Oil, the process involving: mixing a quantity of the Feedstock Heavy Marine Fuel Oil with a quantity of Activating Gas mixture to give a feedstock mixture; contacting the feedstock mixture with one or more catalysts to form a Process Mixture from the feedstock mixture; separating the Product Heavy Marine Fuel Oil liquid components of the Process Mixture from the gaseous components and by-product hydrocarbon components of the Process Mixture and, discharging the Product Heavy Marine Fuel Oil. The Product Heavy Marine Fuel Oil is compliant with ISO 8217 for residual marine fuel oils and the Environmental Contaminants, which are selected from the group consisting of: a sulfur; vanadium, nickel, iron, aluminum and silicon and combinations thereof, have concentration less than 0.5 wt %. The Product Heavy Marine Fuel Oil can be used as or as a blending stock for an ISO 8217 compliant, IMO MARPOL Annex VI (revised) compliant low sulfur or ultralow sulfur heavy marine fuel oil. 1. A low sulfur heavy marine fuel oil , consisting essentially of a 100% hydroprocessed high sulfur heavy marine fuel oil , wherein prior to hydroprocessing the high sulfur heavy marine fuel oil is compliant with ISO 8217: 2017 and is of merchantable quality as a residual marine fuel oil , but Environmental Contaminants have a concentration greater than 0.5% wt. , wherein Environmental Contaminates are selected from the group consisting of: a sulfur; vanadium , nickel , iron , aluminum and silicon and combinations thereof and wherein the low sulfur heavy marine fuel oil is compliant with ISO 8217: 2017 and is of merchantable quality as a residual marine fuel oil and the Environmental Contaminants have concentration less than 0.5 wt %.2. The low sulfur heavy marine fuel oil of claim 1 , wherein sulfur is determined by ISO 14596 or ISO 8754; vanadium is determined by IP 501 or IP 470 or ISO 14597 ...

Heavy Marine Fuel Oil Composition

A process for reducing the environmental contaminants in a ISO 8217 compliant Feedstock Heavy Marine Fuel Oil, the process involving: mixing a quantity of the Feedstock Heavy Marine Fuel Oil with a quantity of Activating Gas mixture to give a feedstock mixture; contacting the feedstock mixture with one or more catalysts to form a Process Mixture from the feedstock mixture; separating the Product Heavy Marine Fuel Oil liquid components of the Process Mixture from the gaseous components and by-product hydrocarbon components of the Process Mixture and, discharging the Product Heavy Marine Fuel Oil. The Product Heavy Marine Fuel Oil is compliant with ISO 8217 for residual marine fuel oils and the sulfur and Specific Contaminants have concentration less than 0.5 wt %., wherein the Specific Contaminates are selected from the group consisting of: vanadium, sodium, aluminum, silicon, calcium, zinc, phosphorus, nickel, iron and combinations thereof. The Product Heavy Marine Fuel Oil can be used as or as a blending stock for an ISO 8217 compliant, IMO MARPOL Annex VI (revised) compliant low sulfur or ultralow sulfur heavy marine fuel oil.

Multi-Stage Device and Process for Production of a Low Sulfur Heavy Marine Fuel Oil

A multi-stage process for the production of an ISO 8217 compliant Product Heavy Marine Fuel Oil from ISO 8217 compliant Feedstock Heavy Marine Fuel Oil involving a Reaction System composed of one or more reactor vessels selected from a group reactor wherein said one or more reactor vessels contains one or more reaction sections configured to promote the transformation of the Feedstock Heavy Marine Fuel Oil to the Product Heavy Marine Fuel Oil. The Product Heavy Marine Fuel Oil has a Environmental Contaminate level has a maximum sulfur content (ISO 14596 or ISO 8754) between the range of 0.05 mass % to 1.0 mass. A process plant for conducting the process for conducting the process is disclosed that can utilize a modular reactor vessel. 1. A process for the production of a Product Heavy Marine Fuel Oil , the process comprising: mixing a quantity of a Heavy Marine Fuel Oil feed with a quantity of an Activating Gas to give a Feedstock Mixture , wherein said Heavy Marine Fuel Oil feed complies with ISO 8217 (2017) as a residual marine fuel , except said Heavy Marine Fuel Oil feed has one or more Environmental Contaminants selected from the group consisting of: sulfur; vanadium , nickel , iron , aluminum and silicon and combinations thereof , and wherein said one or more Environmental Contaminants have a combined concentration greater than 0.5% wt.; distributing said Feedstock Mixture to a Reaction System , wherein the Reaction System is comprised of five or more reactor vessels , and wherein each of the five or more reactor vessels is independently selected from the group of operational configurations consisting of: dense packed fixed bed trickle reactor; dense packed fixed bed up-flow reactor; ebulliated bed three phase up-flow reactor; fixed bed divided wall reactor; fixed bed three phase bubble reactor; fixed bed liquid full reactor , fixed bed high flux reactor; fixed bed structured catalyst bed reactor; fixed bed reactive distillation reactor and combinations ...

Multi-Stage Process and Device for Reducing Environmental Contaminates in Heavy Marine Fuel Oil

A multi-stage process for reducing the environmental contaminants in a ISO 8217 compliant Feedstock Heavy Marine Fuel Oil involving a core desulfurizing process and an ionic liquid extraction desulfurizing process as either a pre-treating step or post-treating step to the core process. The Product Heavy Marine Fuel Oil is compliant with ISO 8217A for residual marine fuel oils and has a sulfur level has a maximum sulfur content (ISO 14596 or ISO 8754) between the range of 0.05% wt. to 0.5% wt. A process plant for conducting the process is also disclosed.

METHODS FOR REACTING CHEMICAL STREAMS WITH CATALYSTS COMPRISING SILICA, ALUMINA, AND TUNGSTEN

One or more embodiments presently disclosed is directed to a method for reacting a chemical stream which may include contacting the chemical stream with a catalyst to produce a product stream. The catalyst may include alumina, silica, and a catalytically active compound such as tungsten. 1. A method for reacting a chemical stream , the method comprising:contacting the chemical stream with a catalyst to produce a product stream, wherein the chemical stream comprises at least a first alkene and the product stream comprises at least a second alkene which is a result of isomerization, metathesis, or both, of the first alkene;wherein the contacting of the chemical stream with the catalyst is at a temperature of less than or equal to 500° C.; and a plurality of catalyst support particles comprising from 0.1 weight percent to 5 weight percent alumina and from 95 weight percent to 99.9 weight percent silica based on the total weight of the catalyst support particles; and', 'a catalytically active compound deposited onto surfaces of the plurality of catalyst support particles, the surfaces of the plurality of catalyst support particles being accessible to gases and vapors, wherein the catalytically active compound comprises tungsten and the catalytically active compound is deposited on from 1% to 50% of the surfaces of the catalyst support particles that are accessible to gases and vapors., 'the catalyst comprises2. The method of claim 1 , wherein the first alkene is 2-butene claim 1 , and the chemical stream comprises at least 5 mol. % 2-butene.3. The method of claim 2 , wherein the second alkene is propylene claim 2 , and the product stream comprises at least 10 mol. % propylene.4. The method of claim 1 , wherein the chemical stream has a space velocity of at least 1000/hour.5. The method of claim 1 , wherein the catalyst comprises from 2 weight percent to 11 weight percent of the catalytically active compound based on the total weight of the catalyst.6. The method of ...

Multi-Stage Device and Process for Production of a Low Sulfur Heavy Marine Fuel Oil

A multi-stage process for the production of an ISO 8217 compliant Product Heavy Marine Fuel Oil from ISO 8217 compliant Feedstock Heavy Marine Fuel Oil involving a Reaction System composed of one or more reactor vessels selected from a group reactor wherein said one or more reactor vessels contains one or more reaction sections configured to promote the transformation of the Feedstock Heavy Marine Fuel Oil to the Product Heavy Marine Fuel Oil. The Product Heavy Marine Fuel Oil has a sulfur level has a maximum sulfur content (ISO 14596 or ISO 8754) between the range of 0.05 mass % to 1.0 mass. A process plant for conducting the process for conducting the process is disclosed that can utilize a modular reactor vessel contained within a frame work based on ISO 40 foot or ISO 20 foot container dimensions. 1. A device for the production of a Product Heavy Marine Fuel Oil , the device comprising: means for mixing a quantity of a Feedstock Heavy Marine Fuel Oil with a quantity of Activating Gas mixture to give a Feedstock Mixture; means for heating the Feedstock Mixture , wherein the means for mixing and means for heating are in fluid communication with each other; a Reaction System in fluid communication with the means for heating , wherein the Reaction System comprises one or more reactor vessels selected from the group consisting of: dense packed fixed bed trickle reactor; dense packed fixed bed up-flow reactor; ebulliated bed three phase up-flow reactor; fixed bed divided wall reactor; fixed bed three phase bubble reactor; fixed bed liquid full reactor , fixed bed high flux reactor; fixed bed structured catalyst bed reactor; fixed bed reactive distillation reactor and combinations thereof , and wherein said one or more reactor vessels contains one or more reaction sections configured to promote the transformation of said Feedstock Mixture to a Process Mixture; means for receiving said Process Mixture and separating any liquid components of said Process Mixture from any ...

CATALYST TUBE FOR REFORMING

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

Methods for reacting chemical streams with catalysts comprising silica, alumina, and tungsten

One or more embodiments presently disclosed is directed to a method for reacting a chemical stream which may include contacting the chemical stream with a catalyst to produce a product stream. The catalyst may include alumina, silica, and a catalytically active compound such as tungsten.

HEAVY MARINE FUEL OIL COMPOSITION

A process for reducing the environmental contaminants in a ISO8217 compliant Feedstock Heavy Marine Fuel Oil, the process involving: mixing a quantity of the Feedstock Heavy Marine Fuel Oil with a quantity of Activating Gas mixture to give a feedstock mixture; contacting the feedstock mixture with one or more catalysts to form a Process Mixture from the feedstock mixture; separating the Product Heavy Marine Fuel Oil liquid components of the Process Mixture from the gaseous components and by-product hydrocarbon components of the Process Mixture and, discharging the Product Heavy Marine Fuel Oil. The Product Heavy Marine Fuel Oil is compliant with ISO 8217A for residual marine fuel oils and has a sulfur level has a maximum sulfur content (ISO 14596 or ISO 8754) between the range of 0.05% wt. to 1.0 mass. The Product Heavy Marine Fuel Oil can be used as or as a blending stock for an ISO 8217 compliant, IMO MARPOL Annex VI (revised) compliant low sulfur or ultralow sulfur heavy marine fuel oil. A device for conducting the process is also disclosed. 1. A heavy marine fuel oil product that is ISO 8217: 2017 compliant , is of merchantable quality , and has a sulfur content (ISO 14596 or ISO 8754) less than 0.5 wt % , said product being produced by a process comprising:a) combining a predetermined quantity of a Feedstock Heavy Marine Fuel Oil that is compliant with ISO 8217: 2017 and has a sulfur content (ISO 14596 or ISO 8754) greater than 0.5% wt. with a predetermined amount of an Activating Gas to form a Feedstock Mixture;b) bringing the Feedstock Mixture up to predetermined process conditions of temperature and pressure to form a heated and pressurized Feedstock Mixture;c) contacting said heated and pressurized Feedstock Mixture in at least one reactor vessel with one or more catalyst systems selected from the group consisting of: an ebulliated bed supported transition metal heterogeneous catalyst, a fixed bed supported transition metal heterogeneous catalyst, and a ...

SYSTEMS AND METHODS FOR MAKING CERAMIC POWDERS

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

OXIDATIVE COUPLING OF METHANE SYSTEMS AND METHODS

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

PROCESS FOR OPERATING A HIGHLY PRODUCTIVE TUBULAR REACTOR

The present technology is directed to processes for conversion of synthesis gas in a tubular reactor to produce a synthetic product that utilizes high activity carbon monoxide hydrogenation catalysts and a heat transfer structure that surprisingly provides for higher per pass conversion with high selectivity for the desired synthetic product without thermal runaway. 1. A process for the conversion of synthesis gas , the process comprising contacting in a tubular reactor a gaseous stream comprising synthesis gas with a carbon monoxide hydrogenation catalyst to produce a synthetic product; a reactor inlet in fluid communication with one or more reactor tubes wherein each reactor tube comprises a tube inlet, a tube outlet located downstream of the tube inlet, an inner tube wall comprising a surface area, an outer tube wall, a heat transfer structure within the reactor tube, and a volume of the carbon monoxide hydrogenation catalyst within the reactor tube;', 'a reactor outlet located downstream of the reactor inlet in fluid communication with the one or more reactor tubes; and', 'a cooling medium in contact with the one or more reactor tubes;, 'wherein the tubular reactor comprises'} the diameter of the inner tube wall is from 20 mm to 80 mm;', {'sub': '2', 'sup': '−1', 'the carbon monoxide hydrogenation catalyst exhibits a conversion rate of at least 30 millimoles CO per mL of catalyst per hour when tested by reacting a stream comprising 30 vol. % inert gas and a ratio of H/CO of 1.84 at a temperature of 205° C. and a pressure of 348 psig with a catalyst gas hourly space velocity of 20,000 hrusing a particulate form of the carbon monoxide hydrogenation catalyst with a weight average diameter of less than 65 μm;'}, 'the heat transfer structure comprises a network of heat conducting surfaces in conductive thermal contact with a portion of the carbon monoxide hydrogenation catalyst and wherein the heat transfer structure is in at least partial conductive thermal contact ...

Efficient fixed bed platform for production of ethylene oxide by partial oxidation of ethylene using catalyst of wide selectivity

At least one method to efficiently produce alkylene oxide from partial oxidation of hydrocarbons using a high efficiency heterogeneous catalyst in a fixed bed enclosed within a reaction vessel, and a reaction vessel constructed to facilitate the same.

Olefin production method using circulating fluidized bed process

Disclosed is an olefin production method which includes: (a) providing the regenerated catalyst and the hydrocarbon including not less than 90 wt % of LPG into Riser of Fast Fluidization Regime, and dehydrogenating in the presence of an alumina type catalyst; (b) separating an effluent from the dehydrogenation reaction into the catalyst and propylene mixture; (c) stripping to remove the hydrocarbon compound included in the catalyst separated at stage (b); (d) mixing the catalyst stripped at stage (c) with the gas including oxygen, and continuously regenerating it; (e) recycling the catalyst regenerated at stage (d) to stage (a), and providing it again into Riser; and (f) producing propylene product by cooling, compressing and separating propylene mixture of the reaction product separated at stage (b).

Activated carbon method and material

A method and system for making enhanced activated carbon are disclosed. A first heated gas including oxygen flows through a fluidized bed including particles comprising activated carbon to form oxidized activated carbon particles. A second heated gas including nitrogen, ammonia or a combination thereof, flows through a fluidized bed including the oxidized activated carbon particles to form nitrogenated activated carbon particles. A third heated gas including hydrogen flows through a fluidized bed including the nitrogenated activated carbon particles to form the enhanced activated carbon particles.

HEAT INTEGRATED REFORMER WITH CATALYTIC COMBUSTION FOR HYDROGEN PRODUCTION

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

Methods of changing polyolefin production rate with the composition of the induced condensing agents

Polyolefin polymerization performed by contacting in a reactor an olefin monomer and optionally a comonomer with a catalyst system in the presence of induced condensing agents (ICA) and optionally hydrogen. The ICA may include two or more ICA components where the composition of the ICA (i.e ., the concentration of each ICA component) may affect the polyolefin production rate. Changes to the relative concentration of the two or more ICA components may be according to ICA equivalency factors that allow for increasing the polyolefin production rate while maintain a sticking temperature, increasing polyolefin production rate while increasing the dew point approach temperature of the ICA, or a combination thereof.

Method and apparatus for preparing and supplying catalyst slurry to a polymerisation reactor.

The present invention relates to an apparatus for preparing and supplying catalyst to an ethylene slurry loop polymerisation reactor and to an apparatus for controlling the injection of catalyst slurry in a polymerization reactor wherein polyethylene is prepared. The present invention a Iso relates to a method for optimising catalyst supply to a polymerisation reactor. The diluted catalyst is transferred to the reactor (1) using a membrane pump (5) controllable in function of the concentration of a reactant in said reactor (1).

Método e aparelho para preparar e fornecer suspensão catalítica a um reactor de polimerização.

Methods of changing polyolefin production rate with the composition of the induced condensing agents

Polyolefin polymerization performed by contacting in a reactor an olefin monomer and optionally a comonomer with a catalyst system in the presence of induced condensing agents (ICA) and optionally hydrogen. The ICA may include two or more ICA components where the composition of the ICA (i.e., the concentration of each ICA component) may affect the polyolefin production rate. Changes to the relative concentration of the two or more ICA components may be according to ICA equivalency factors that allow for increasing the polyolefin production rate while maintain a sticking temperature, increasing polyolefin production rate while increasing the dew point approach temperature of the ICA, or a combination thereof.

Process for the catalytic polymerization of olefins, a reactor system and its use in the same process

Light treatment of chromium catalysts and related catalyst preparation systems and polymerization processes

Catalyst preparation systems and methods for preparing reduced chromium catalysts are disclosed, and can comprise irradiating a supported chromium catalyst containing hexavalent chromium with a light beam having a wavelength within the UV-visible light spectrum. Such reduced chromium catalysts have improved catalytic activity compared to chromium catalysts reduced by other means. The use of the reduced chromium catalyst in polymerization reactor systems and olefin polymerization processes also is disclosed, resulting in polymers with a higher melt index.

Modified supported chromium catalysts and ethylene-based polymers produced therefrom

Supported chromium catalysts with an average valence less than +6 and having a hydrocarbon-containing or halogenated hydrocarbon-containing ligand attached to at least one bonding site on the chromium are disclosed, as well as ethylene-based polymers with terminal alkane, aromatic, or halogenated hydrocarbon chain ends. Another ethylene polymer characterized by at least 2 wt. % of the polymer having a molecular weight greater than 1,000,000 g/mol and at least 1.5 wt. % of the polymer having a molecular weight less than 1000 g/mol is provided, as well as an ethylene homopolymer with at least 3.5 methyl short chain branches and less than 0.6 butyl short chain branches per 1000 total carbon atoms.

Light treatment of chromium catalysts and related catalyst preparation systems and polymerization processes

Catalyst preparation systems and methods for preparing reduced chromium catalysts are disclosed, and can comprise irradiating a supported chromium catalyst containing hexavalent chromium with a light beam having a wavelength within the UV-visible light spectrum. Such reduced chromium catalysts have improved catalytic activity compared to chromium catalysts reduced by other means. The use of the reduced chromium catalyst in polymerization reactor systems and olefin polymerization processes also is disclosed, resulting in polymers with a higher melt index.

Light treatment of chromium catalysts and related catalyst preparation systems and polymerization processes

Catalyst preparation systems and methods for preparing reduced chromium catalysts are disclosed, and can comprise irradiating a supported chromium catalyst containing hexavalent chromium with a light beam having a wavelength within the UV-visible light spectrum. Such reduced chromium catalysts have improved catalytic activity compared to chromium catalysts reduced by other means. The use of the reduced chromium catalyst in polymerization reactor systems and olefin polymerization processes also is disclosed, resulting in polymers with a higher melt index.

Process for the gas-phase polymerization of olefins

Process for the catalytic polymerization of olefins, a reactor system, its use in the process, the polyolefins obtained and their use

The present invention relates to a process for the catalytic polymerization of olefins comprising the steps of; i) a first polymerization in a first reactor, wherein olefins are polymerized with a particulate catalyst, hydrogen and optional a comonomer in a fluidum of an inert low boiling hydrocarbon medium into an reaction mixture comprising polymerized olefins; and ii) a second polymerization in a second reactor, wherein the polymerized olefins are further polymerized in a fluidized bed and in a moving bed under such conditions that the residence time in the fluidized bed and the residence time in the moving bed are independently controlled to a reactor system for carrying out said process, to the use of the reactor system, the polyolefins obtainable with said method and to the use of these polyolefins.

用于烯烃气相聚合的方法和设备

具有相互连接的聚合区域的气相聚合反应器，包括：-上升管，聚合物颗粒在快速流化条件或传输条件下向上流动通过该上升管；-下降管，聚合物颗粒在重力作用下以致密的形式向下流动通过该下降管，所述下降管的底部通过传输段与所述上升管的下部区域相连，所述传输段被设计为从下降管到上升管下降的弯曲。

Process and apparatus for the gas-phase polymerization of olefins

A gas-phase polymerization reactor having interconnected polymerization zones comprising: - a riser through which the polymer particles flow upwards under fast fluidization conditions or transport conditions; -a dowcomer through which the polymer particles flow downward in a densified form under the action of gravity, the bottom of said downcomer being connected to the lower region of said riser by means of a transport section, said transport section being designed as a bend descending from the downcomer to the riser.

Process and apparatus for the gas-phase polymerization of olefins

A gas-phase polymerization reactor having interconnected polymerization zones comprising: - a riser through which the polymer particles flow upwards under fast fluidization conditions or transport conditions; -a dowcomer through which the polymer particles flow downward in a densified form under the action of gravity, the bottom of said downcomer being connected to the lower region of said riser by means of a transport section, said transport section being designed as a bend descending from the downcomer to the riser.

Methods of changing polyolefin production conditions to mitigate small gels in a polyolefin article

The number of small gels that form in polyolefin thin films may be reduced by altering certain production parameters of the polyolefin. In some instances, the number of small gels may be influenced by the melt index of the polyolefin. However, in many instances, melt index is a critical part of the polyolefin product specification and, therefore, is not manipulated. Two parameters that may be manipulated to mitigate small gel count while maintaining the melt index are polyolefin residence time in the reactor and ICA concentration in the reactor.

METHOD AND DEVICE FOR CONTROLLING THE SUPPLY OF CATALYST SLUDGE INTO A POLYMERIZATION REACTOR

Method and apparatus for adjusting and supplying catalyst slurry to polymerization reactor

Reactor system for the catalytic polymerization of olefins comprising shielding means and a process and use thereof

The invention relates to a reactor system for the catalytic polymerization of olefin monomer and optionally comonomer(s), comprising one or more inlets for olefin monomer, catalyst, optionally for comonomer, chain growth controllers or chain transfer agents, and/or inert gas, an outlet for gas and an outlet for polymerization particles, which reactor system comprises at least one fluidized bed unit and at least one a moving bed unit, wherein the fluidized bed unit comprises means for maintaining a fluidized bed in the fluidized bed unit and wherein the moving bed unit is provided with an inlet and an outlet which are connected to the fluidized bed unit, wherein in the fluidized bed unit is positioned shielding means such that via the outlet of the moving bed unit inflow of fluidization gas is inhibited and outflow of polymerization particles allowed and to a process and use thereof.

Reactor system and process for the catalytic polymerization of olefins, and the use of such reactor system in catalytic polymerization of olefins

The invention relates to a reactor system and process for the catalytic polymerization of olefin monomer and optionally comonomer(s), comprising one or more inlets for olefin monomer, catalyst, optionally for comonomer, chain growth controllers or chain transfer agents, and/or inert gas, an outlet for gas and an outlet for polymerized particles, which reactor system comprises at least one fluidized bed unit and at least one moving bed unit, wherein the fluidized bed unit comprises means for maintaining a fluidized bed in the fluidized bed unit and wherein the moving bed unit is provided with an inlet and an outlet which are connected to the fluidized bed unit, wherein the outlet of the moving bed unit is provided with means for displacing metered quantities of polymerized particles from the moving bed unit into the fluidized bed unit, and to the use of such reactor system.

Reactor systems and process for the catalytic polymerization of olefins, and the use of such reactor system in catalytic polymeration of olefins

The invention relates to a reactor system for the catalytic polymerization of olefin monomer and optionally comonomer(s), comprising one or more inlets for olefin monomer, catalyst, optionally for comonomer, chain growth controllers or chain transfer agents, and/or inert gas, an outlet for gas and an outlet for polymerized particles, which reactor system comprises at least one fluidized bed unit and at least one moving bed unit, wherein the fluidized bed unit comprises means for maintaining a fluidized bed in the fluidized bed unit and wherein the moving bed unit is provided with an inlet and an outlet which are directly connected to the fluidized bed unit, wherein the outlet of the moving bed unit is provided with means for pneumatically displacing polymer particles from the moving bed unit into the fluidized bed unit.

Reactor system and process for the catalytic polymerization of olefins, and the use of such reactor system in catalytic polymerization of olefins

The invention relates to a reactor system and process for the catalytic polymerization of olefin monomer and optionally comonomer(s), having one or more inlets for olefin monomer, catalyst, optionally for comonomer, chain growth controllers or chain transfer agents, and/or inert gas, an outlet for gas and an outlet for polymerized particles. The reactor system has at least one fluidized bed unit and at least one moving bed unit, wherein the fluidized bed unit has means for maintaining a fluidized bed in the fluidized bed unit and wherein the moving bed unit is provided with an inlet and an outlet which are connected to the fluidized bed unit, wherein the outlet of the moving bed unit is provided with means for displacing metered quantities of polymerized particles from the moving bed unit into the fluidized bed unit, and to the use of such reactor system.

Reactor System and Process for the Catalytic Polymerization of Olefins, and the Use of Such Reactor System in Catalytic Polymerization of Olefins

The invention relates to a reactor system for the catalytic polymerization of olefin monomer and optionally comonomer(s), having one or more inlets for olefin monomer, catalyst, optionally for comonomer, chain growth controllers or chain transfer agents, and/or inert gas, an outlet for gas and an outlet for polymerized particles. The reactor system has at least one fluidized bed unit and at least one moving bed unit, wherein the fluidized bed unit has means for maintaining a fluidized bed in the fluidized bed unit and wherein the moving bed unit is provided with an inlet and an outlet which are directly connected to the fluidized bed unit, wherein the outlet of the moving bed unit is provided with means for pneumatically displacing polymer particles from the moving bed unit into the fluidized bed unit.

Reactor System and Process for the Catalytic Polymerization of Olefins, and the Use of Such Reactor System in Catalytic Polymerization of Olefins

The invention relates to a reactor system and process for the catalytic polymerization of olefin monomer and optionally comonomer(s), having one or more inlets for olefin monomer, catalyst, optionally for comonomer, chain growth controllers or chain transfer agents, and/or inert gas, an outlet for gas and an outlet for polymerized particles. The reactor system has at least one fluidized bed unit and at least one moving bed unit, wherein the fluidized bed unit has means for maintaining a fluidized bed in the fluidized bed unit and wherein the moving bed unit is provided with an inlet and an outlet which are connected to the fluidized bed unit, wherein the outlet of the moving bed unit is provided with means for displacing metered quantities of polymerized particles from the moving bed unit into the fluidized bed unit, and to the use of such reactor system.

Reactor system and process for the catalytic polymerization of olefins, and the use of such reactor system in catalytic polymerization of olefins

The invention relates to a reactor system for the catalytic polymerization of olefin monomer and optionally comonomer(s), having one or more inlets for olefin monomer, catalyst, optionally for comonomer, chain growth controllers or chain transfer agents, and/or inert gas, an outlet for gas and an outlet for polymerized particles. The reactor system has at least one fluidized bed unit and at least one moving bed unit, wherein the fluidized bed unit has means for maintaining a fluidized bed in the fluidized bed unit and wherein the moving bed unit is provided with an inlet and an outlet which are directly connected to the fluidized bed unit, wherein the outlet of the moving bed unit is provided with means for pneumatically displacing polymer particles from the moving bed unit into the fluidized bed unit.

Calcination method and system

The invention relates to a method for the calcination of powdery or fine-particled plaster, comprising two steps: the plaster is subjected to a flash-calcination in a calcinator (3) and the hot plaster is post-calcinated in a reaction vessel (6). According to the invention, post-calcination is carried out in the reaction vessel (6) by adding humid gas, said reaction vessel (6) not being heated. Said post-calcination takes place over a long period of time, that is at least 10 times, preferably 50 - 100 times longer than the amount of time taken for flash calcination. Said invention enables complete calcination to take place without expending additional energy, and the remaining dihydrate produced during the flash calcination is also transformed into semi-hydrate and undesired anhydrite fractions are reduced. Said method ensures consistency in the product quality and also increases product quality. The temperature in the upstream calcinator (3) can be lowered thus saving more energy. Said invention can also be used to accelerate the ageing of calcinated plaster.

Reactor system and process for the catalytic polymerization of olefins, and the use of such reactor system in catalytic polymerization of olefins

올레핀의 촉매 방식 중합 방법, 상기 중합용 반응기 시스템및 용도

본 발명은, 유동상에서의 체류 시간과 이동상에서의 체류 시간이 독립적으로 제어되도록 올레핀을 유동상 및 이동상에서 입자상 촉매와 접촉시키는 올레핀의 촉매 방식 중합 방법, 반응물 입구, 제품 출구 및 유동상 반응기에서의 유동화를 유지하기 위한 수단을 구비한 유동상 반응기, 및 상기 유동상 반응기에 직접 연결된 입구 및 상기 유동상 반응기에서의 체류 시간과 이동상 반응기에서의 체류 시간이 독립적으로 제어되도록 상기 유동상 반응기에 연결된 출구를 구비한 이동상 반응기를 포함하는 반응기 시스템 및 올레핀의 촉매 방식 중합반응에 이용하는 상기 반응기 시스템의 용도에 관한 것이다. 촉매 방식 중합반응, 올레핀, 유동상, 이동상, 체류 시간, 바이모달, 다분산성

Process for the catalytic polymerization of olefins, a reactor system and its use in the process.

The invention relates to a process for the catalytic polymerization of olefins, wherein olefins are contacted with a particulate catalyst in a fluidized bed and in a moving bed such that the residence time in the fluidized bed and the residence time in the moving bed are independently controlled, to a reactor system comprising a fluidized bed reactor provided with a reactant inlet, a product outlet and means for maintaining a fluidized bed in the fluidized bed reactor and with a moving bed reactor provided with an inlet directly connected to the fluidized bed reactor and an outlet connected to the fluidized bed reactor such that the residence time in the fluidized bed reactor and the residence in the moving bed reactor are independently controlled, and to its use for the catalytic polymerization of olefins. <IMAGE>

Process for the catalytic polymerization of olefins, a reactor system, its use in the process, the polyolefins obtained and their use

The present invention relates to a process for the catalytic polymerization of olefins comprising the steps of; i) a first polymerization in a first reactor, wherein olefins are polymerized with a particulate catalyst, hydrogen and optional a comonomer in a fluidum of an inert low boiling hydrocarbon medium into an reaction mixture comprising polymerized olefins; and ii) a second polymerization in a second reactor, wherein the polymerized olefins are further polymerized in a fluidized bed and in a moving bed under such conditions that the residence time in the fluidized bed and the residence time in the moving bed are independently controlled to a reactor system for carrying out said process, to the use of the reactor system, the polyolefins obtainable with said method and to the use of these polyolefins.

Methods of controlling polyolefin melt index while increasing catalyst productivity

The catalyst productivity of a polyolefin catalyst in the methods disclosed herein may be increased by increasing the concentration of an induced condensing agent (ICA) in the reactor system. The effect the increased ICA concentration may have on a melt index may be counteracted, if necessary, in various ways.

Process for the catalytic polymerization of olefins, a reactor system and its use in the same process

The invention relates to a process for the catalytic polymerization of olefins, wherein olefins are contacted with a particulate catalyst in a fluidized bed and in a moving bed such that the residence time in the fluidized bed and the residence time in the moving bed are independently controlled, to a reactor system comprising a fluidized bed reactor provided with a reactant inlet, a product outlet and means for maintaining a fluidized bed in the fluidized bed reactor and with a moving bed reactor provided with an inlet directly connected to the fluidized bed reactor and an outlet connected to the fluidized bed reactor such that the residence time in the fluidized bed reactor and the residence in the moving bed reactor are independently controlled, and to its use for the catalytic polymerization of olefins.

PROCESS AND APPARATUS FOR OLEFINE GAS PHASE POLYMERIZATION

processo e aparelho para a polimerização de fase gás de olefinas. a presente invenção refere-se a um reator de polimerização de fase gás tendo zonas de polimerização integradas compreendendo: um tubo ascensor através no qual as partículas de polímero fluem para cima sob condições de fluidização rápida ou condições de transporte; um tubo de descenso através do qual as partículas de polímero fluem para baixo em uma forma densificada sob a ação da gravidade, o fundo referido tubo de descenso estando ligado á região inferior de referido tubo ascensor por meio de uma seção de tranpsorte, referida seção de transporte sendo projetada como um descenso de encurvamento a partir do tubo de descenso par ao tubo ascensor. process and apparatus for olefin gas phase polymerization. The present invention relates to a gas phase polymerization reactor having integrated polymerization zones comprising: a riser tube through which polymer particles flow upward under rapid fluidization conditions or transport conditions; a descent tube through which the polymer particles flow down in a densified form under the action of gravity, the bottom of said descent tube being connected to the lower region of said elevator tube by means of a transverse section, said section of transport being designed as a curving descent from the descent tube to the lift tube.

Continuous polymerization reactor

A process for the continuous polymerization of monomer, the process comprising (a) adding monomer and catalyst to an annulus within an annular reactor to form a polymerization medium within the annulus, where the annulus includes the space between an outer casing wall and an inner tubular wall, (b) allowing the polymerization medium a sufficient residence time within the annulus to provide a living polymer product, and (c) removing the polymer product from the annulus.

烯烃催化聚合的方法、反应器体系、它在该方法中的用途、所制备的聚烯烃和它们的用途

本发明涉及烯烃催化聚合的方法，其包括步骤：i)在第一反应器中的第一聚合，其中烯烃在惰性低沸点烃介质的流体中与颗粒状催化剂、氢气和任选的共聚单体聚合进入到包括聚合烯烃的反应混合物之内；和ii)在第二反应器中的第二聚合，其中聚合烯烃在流化床中和在移动床中在下述条件下进一步聚合，该条件为独立地控制在流化床中的停留时间和在移动床中的停留时间；还涉及实施所述方法的反应器体系、该反应器体系的用途、用所述方法制备的聚烯烃以及这些聚烯烃的用途。

利用超重力反应器进行费托合成的方法

Method and Apparatus for Preparing and Supplying Catalyst Slurry to a Polymerization Reactor

The present invention relates to an apparatus for preparing and supplying catalyst to an ethylene slurry loop polymerisation reactor and to an apparatus for controlling the injection of catalyst slurry in a polymerization reactor wherein polyethylene is prepared. The present invention a Iso relates to a method for optimising catalyst supply to a polymerisation reactor. The diluted catalyst is transferred to the reactor ( 1 ) using a membrane pump ( 5 ) controllable in function of the concentration of a reactant in said reactor ( 1 ).

Method and apparatus for preparing and supplying catalyst slurry to a polymerization reactor

The present invention relates to an apparatus for preparing and supplying catalyst to an ethylene slurry loop polymerisation reactor and to an apparatus for controlling the injection of catalyst slurry in a polymerization reactor wherein polyethylene is prepared. The present invention a Iso relates to a method for optimising catalyst supply to a polymerisation reactor. The diluted catalyst is transferred to the reactor ( 1 ) using a membrane pump ( 5 ) controllable in function of the concentration of a reactant in said reactor ( 1 ).

Method and apparatus for preparing and supplying catalyst slurry to polymerisation reactor

본 발명은 촉매를 생성하고, 이를 에틸렌 슬러리 루프 중합 반응기에 공급하기 위한 장치, 폴리에틸렌이 생성되는 중합 반응기로의 촉매 슬러리의 주입을 조절하기 위한 장치에 관한 것이다. 또한, 본 발명은 중합 반응기로의 촉매 공급의 최적화를 위한 방법에 관한 것이다. 희석된 촉매는 상기 반응기(1)내의 반응물의 농도에 따라서 조절 가능한 막 펌프(5)를 사용하여 반응기(1)로 전달된다. The present invention relates to an apparatus for producing a catalyst and feeding it to an ethylene slurry loop polymerization reactor, an apparatus for controlling the injection of catalyst slurry into a polymerization reactor in which polyethylene is produced. The invention also relates to a method for optimizing the catalyst feed to the polymerization reactor. The diluted catalyst is delivered to reactor 1 using a membrane pump 5 which is adjustable according to the concentration of reactants in the reactor 1. 접촉 반응, 촉매 슬러리, 중합 반응기 Catalytic reaction, catalyst slurry, polymerization reactor

Methods of changing polyolefin production conditions to mitigate small gels in a polyolefin article

The number of small gels that form in polyolefin thin films may be reduced by altering certain production parameters of the polyolefin. In some instances, the number of small gels may be influenced by the melt index of the polyolefin. However, in many instances, melt index is a critical part of the polyolefin product specification and, therefore, is not manipulated. Two parameters that may be manipulated to mitigate small gel count while maintaining the melt index are polyolefin residence time in the reactor and ICA concentration in the reactor.

Olefin gas phase polymerization process

Polymerization process for olefins

The present invention relates to a process for the polymerization of olefin monomers in the presence of a catalyst system, using a tubular pre-polymerization reactor, wherein the tubular pre-polymerization reactor has a length L and the flow of a catalyst system is introduced in the tubular pre-polymerization reactor in the middle (30-70% of L) or the end (70-95% of L) of the tubular pre-polymerization reactor.

Process and apparatus for the gas-phase polymerization of olefins

A gas-phase polymerization reactor having interconnected polymerization zones comprising:—a riser through which the polymer particles flow upwards under fast fluidization conditions or transport conditions;—a downcomer through which the polymer particles flow downward in a densified form under the action of gravity, the bottom of said downcomer being connected to the lower region of said riser by means of a transport section, said transport section being designed as a bend descending from the downcomer to the riser.

Method and apparatus for preparing and supplying catalyst slurry to a polymerisation reactor

Methods of changing polyolefin production conditions to mitigate small gels in a polyolefin article

The number of small gels that form in polyolefin thin films may be reduced by altering certain production parameters of the polyolefin. In some instances, the number of small gels may be influenced by the melt index of the polyolefin. However, in many instances, melt index is a critical part of the polyolefin product specification and, therefore, is not manipulated. Two parameters that may be manipulated to mitigate small gel count while maintaining the melt index are polyolefin residence time in the reactor and ICA concentration in the reactor.

Methods for Controlling Polyolefin Melt Index While Increasing Catalyst Productivity

La productividad del catalizador de un catalizador de poliolefina en los métodos descritos en el presente documento puede incrementarse aumentando la concentración de un agente de condensación inducida (ICA) en el sistema del reactor. El efecto que puede tener la mayor concentración de ICA sobre el índice de fusión puede contrarrestarse, si es necesario, de varias formas. (Traducción automática con Google Translate, sin valor legal) The catalyst productivity of a polyolefin catalyst in the methods described herein can be increased by increasing the concentration of an induced condensation agent (ICA) in the reactor system. The effect that the higher concentration of ICA may have on the melt index can be counteracted, if necessary, in various ways. (Automatic translation with Google Translate, without legal value)

Methods of changing polyolefin production rate with the composition of the induced condensing agents

Polyolefin polymerization performed by contacting in a reactor an olefin monomer and optionally a comonomer with a catalyst system in the presence of induced condensing agents (ICA) and optionally hydrogen. The ICA may include two or more ICA components where the composition of the ICA (i.e ., the concentration of each ICA component) may affect the polyolefin production rate. Changes to the relative concentration of the two or more ICA components may be according to ICA equivalency factors that allow for increasing the polyolefin production rate while maintain a sticking temperature, increasing polyolefin production rate while increasing the dew point approach temperature of the ICA, or a combination thereof.

Method to change polyolefin production rate with the composition of induced condensing agents

Polimerização de poliolefina realizada fazendo contatar, em um reator um monômero de olefina e, opcionalmente, um comonômero, com um sistema de catalisador na presença de agentes de condensação induzida (ICA) e opcionalmente hidrogênio. O ICA pode incluir dois ou mais componentes ICA, onde a composição do ICA (isto é, a concentração de cada componente ICA) pode afetar a taxa de produção de poliolefinas. Mudanças na concentração relativa dos dois ou mais componentes ICA podem ser de acordo com fatores de equivalência de ICA que permitem o aumento da taxa de produção de poliolefinas, enquanto mantendo uma temperatura de pegajosidade, aumentando a taxa de produção de poliolefinas, enquanto aumentando a temperatura de aproximação do ponto de condensação do ICA, ou uma combinação dos mesmos. Polyolefin polymerization carried out by contacting, in a reactor, an olefin monomer and, optionally, a comonomer, with a catalyst system in the presence of induced condensing agents (ICA) and optionally hydrogen. The ICA may include two or more ICA components, where the composition of the ICA (ie the concentration of each ICA component) can affect the rate of production of polyolefins. Changes in the relative concentration of the two or more ICA components can be in accordance with ICA equivalence factors that allow increasing the rate of production of polyolefins, while maintaining a sticky temperature, increasing the rate of production of polyolefins, while increasing the temperature. ICA dew point approach, or a combination thereof.

Methods of changing polyolefin production rate with the composition of the induced condensing agents

Polyolefin polymerization performed by contacting in a reactor an olefin monomer and optionally a comonomer with a catalyst system in the presence of induced condensing agents (ICA) and optionally hydrogen. The ICA may include two or more ICA components where the composition of the ICA (i.e., the concentration of each ICA component) may affect the polyolefin production rate. Changes to the relative concentration of the two or more ICA components may be according to ICA equivalency factors that allow for increasing the polyolefin production rate while maintain a sticking temperature, increasing polyolefin production rate while increasing the dew point approach temperature of the ICA, or a combination thereof.

用诱导冷凝剂的组成改变聚烯烃生产速率的方法

聚烯烃聚合通过以下进行：在反应器中，在诱导冷凝剂(ICA)和任选氢气存在下，使烯烃单体和任选共聚单体与催化剂系统接触。所述ICA可以包括两种或更多种ICA组分，其中所述ICA的组成(即，每一ICA组分的浓度)可以影响聚烯烃生产速率。可以根据ICA等效系数改变所述两种或更多种ICA组分的相对浓度，所述改变使所述聚烯烃生产速率提高同时保持粘着温度，使聚烯烃生产速率提高同时提高所述ICA的露点趋近温度，或其组合。

Способы изменения скорости производства полиолефинов с применением композиции индуцированных конденсирующих агентов

РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2017 120 186 A (51) МПК C08F 2/34 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21)(22) Заявка: 2017120186, 24.11.2015 (71) Заявитель(и): ЮНИВЕЙШН ТЕКНОЛОДЖИЗ, ЭлЭлСи (US) Приоритет(ы): (30) Конвенционный приоритет: 25.11.2014 US 62/084,271 34 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 08.06.2017 US 2015/062465 (24.11.2015) (87) Публикация заявки PCT: WO 2016/086006 (02.06.2016) A Адрес для переписки: 105082, Москва, Спартаковский пер., 2, стр. 1, секция 1, этаж 3, ЕВРОМАРКПАТ R U (57) Формула изобретения 1. Способ, включающий: приведение в контакт олефинового мономера с каталитической системой в газофазном реакторе с псевдоожиженным слоем в присутствии индуцированного конденсирующего агента (ICA) и необязательно водорода с получением полиолефина, имеющего температуру слипания, при этом ICA содержит первый компонент ICA и второй компонент ICA; эксплуатацию газофазного реактора с псевдоожиженным слоем при рабочей температуре, которая ниже температуры слипания полиолефина; выгрузку газофазной композиции, содержащей по меньшей мере часть полиолефина, по меньшей мере часть ICA и необязательно по меньшей мере часть водорода; конденсацию части ICA из газофазной композиции с получением конденсированного ICA; возврат в цикл по меньшей мере части конденсированного ICA и по меньшей мере части газофазной композиции в газофазный реактор с псевдоожиженным слоем; и изменение молярного процента каждого из первого и второго компонентов ICA относительно общего количества газа в реакторе в соответствии с фактором эквивалентности первого ICA ко второму ICA, при котором изменяют один моль второго компонента ICA на заранее определенное количество моль первого компонента Стр.: 1 A 2 0 1 7 1 2 0 1 8 6 (54) СПОСОБЫ ИЗМЕНЕНИЯ СКОРОСТИ ПРОИЗВОДСТВА ПОЛИОЛЕФИНОВ С ПРИМЕНЕНИЕМ КОМПОЗИЦИИ ИНДУЦИРОВАННЫХ КОНДЕНСИРУЮЩИХ АГЕНТОВ 2 0 1 7 1 2 0 1 8 6 (86) Заявка PCT: R U (43) Дата публикации ...

Patent RU2017120186A3

ВИ“? 2017120186” АЗ Дата публикации: 11.06.2019 Форма № 18 ИЗИМ-2011 Федеральная служба по интеллектуальной собственности Федеральное государственное бюджетное учреждение 5 «Федеральный институт промышленной собственности» (ФИПС) ОТЧЕТ О ПОИСКЕ 1. . ИДЕНТИФИКАЦИЯ ЗАЯВКИ Регистрационный номер Дата подачи 2017120186/04(034970) 24.11.2015 РСТЛО52015/062465 24.11.2015 Приоритет установлен по дате: [ ] подачи заявки [ ] поступления дополнительных материалов от к ранее поданной заявке № [ ] приоритета по первоначальной заявке № из которой данная заявка выделена [ ] подачи первоначальной заявки № из которой данная заявка выделена [ ] подачи ранее поданной заявки № [Х] подачи первой(ых) заявки(ок) в государстве-участнике Парижской конвенции (31) Номер первой(ых) заявки(ок) (32) Дата подачи первой(ых) заявки(ок) (33) Код страны 1. 62/084,271 25.11.2014 05 Название изобретения (полезной модели): [Х] - как заявлено; [ ] - уточненное (см. Примечания) СПОСОБЫ ИЗМЕНЕНИЯ СКОРОСТИ ПРОИЗВОДСТВА ПОЛИОЛЕФИНОВ С ПРИМЕНЕНИЕМ КОМПОЗИЦИИ ИНДУЦИРОВАННЫХ КОНДЕНСИРУЮЩИХ АГЕНТОВ Заявитель: ЮНИВЕЙШН ТЕКНОЛОДЖИЗ, ЭлЭлСи, 0$ 2. ЕДИНСТВО ИЗОБРЕТЕНИЯ [Х] соблюдено [ ] не соблюдено. Пояснения: см. Примечания 3. ФОРМУЛА ИЗОБРЕТЕНИЯ: [Х] приняты во внимание все пункты (см. П см. Примечания [ ] приняты во внимание следующие пункты: р [ ] принята во внимание измененная формула изобретения (см. Примечания) 4. КЛАССИФИКАЦИЯ ОБЪЕКТА ИЗОБРЕТЕНИЯ (ПОЛЕЗНОЙ МОДЕЛИ) (Указываются индексы МПК и индикатор текущей версии) СОЗЕ 2/34 (2006.01) С08Е 10/00 (2006.01) С08Е 10/02 (2006.01) ВО1.] 5/18 (2006.01) 5. ОБЛАСТЬ ПОИСКА 5.1 Проверенный минимум документации РСТ (указывается индексами МПК) СОВ8Е 2/34 СО8Е 10/00 СОЗЕ 10/02 ВО1] 8/18 5.2 Другая проверенная документация в той мере, в какой она включена в поисковые подборки: 5.3 Электронные базы данных, использованные при поиске (название базы, и если, возможно, поисковые термины): Езрасепе Соозе, Рабеагсв, КОРТО 6. _ ДОКУМЕНТЫ, ОТНОСЯЩИЕСЯ К ПРЕДМЕТУ ПОИСКА (см. на ...

methods of changing polyolefin production rate with the composition of induced condensing agents

polimerização de poliolefina realizada fazendo contatar, em um reator um monômero de olefina e, opcionalmente, um comonômero, com um sistema de catalisador na presença de agentes de condensação induzida (ica) e opcionalmente hidrogênio. o ica pode incluir dois ou mais componentes ica, onde a composição do ica (isto é, a concentração de cada componente ica) pode afetar a taxa de produção de poliolefinas. mudanças na concentração relativa dos dois ou mais componentes ica podem ser de acordo com fatores de equivalência de ica que permitem o aumento da taxa de produção de poliolefinas, enquanto mantendo uma temperatura de pegajosidade, aumentando a taxa de produção de poliolefinas, enquanto aumentando a temperatura de aproximação do ponto de condensação do ica, ou uma combinação dos mesmos. polyolefin polymerization carried out by contacting in one reactor an olefin monomer and optionally a comonomer with a catalyst system in the presence of induced (ica) condensing agents and optionally hydrogen. The ica may include two or more single components, where the composition of the ica (i.e. the concentration of each single component) may affect the rate of polyolefin production. Changes in the relative concentration of the two or more ica components may be in accordance with ica equivalence factors that allow for increased polyolefin production rate while maintaining a tackiness temperature, increasing polyolefin production rate, while increasing temperature. dew point approximation point or a combination thereof.

改变聚烯烃生产条件以减轻聚烯烃物品中的小凝胶的方法

可通过更改聚烯烃的某些生产参数来减少形成在聚烯烃薄膜中的小凝胶的数目。在一些情况下，小凝胶的数目可受到所述聚烯烃的熔融指数影响。然而，在许多情况下，熔融指数是聚烯烃产物规格的关键部分且因此不被操控。可被操控以减轻小凝胶计数同时维持所述熔融指数的两个参数是反应器中的聚烯烃滞留时间和所述反应器中的ICA浓度。

控制聚烯烃熔融指数，同时增加催化剂产率的方法

本文所公开的方法中的聚烯烃催化剂的催化剂产率可通过增加反应器系统中的诱导冷凝剂(ICA)的浓度而增加。必要时，可以不同方式抵消增加的ICA浓度可能对于熔融指数具有的影响。