СПОСОБ ГИДРОКРЕКИНГА ИСХОДНОГО УГЛЕВОДОРОДНОГО СЫРЬЯ

Изобретение относится к способу гидрокрекинга, содержащему стадии: (a) объединения углеводородного исходного сырья и тяжелой нижней фракции отгонки потока рециркуляции с обогащенным водородом газом для получения смеси, содержащей углеводородное исходное сырье и водород; (b) каталитического гидрокрекинга смеси, содержащей углеводородное исходное сырье и водород, в зоне гидрокрекинга для получения выходящего потока гидрокрекинга; (c) разделения выходящего потока гидрокрекинга на первую паровую часть и первую жидкую часть в зоне разделения; (d) нагревания первой жидкой части для формирования испаренной первой жидкой части; (e) подачи испаренной первой жидкой части в секцию фракционирования, производя фракции отдельного продукта, включающие тяжелую нижнюю фракцию, содержащую неконвертированную нефть, в нижней зоне секции фракционирования; (f) извлечения из секции фракционирования тяжелой нижней фракции; (g) разделения тяжелой нижней фракции на поток для отгонки и поток рециркуляции нижней фракции ...

ГИДРООБРАБОТКА ПРОДУКТОВ ТЕРМИЧЕСКОГО КРЕКИНГА

Изобретение относится к принципиальным схемам технологического процесса обработки газойлей и в особенности химически активных газойлей, полученных термическим крекингом нефтяных остатков, с использованием принципа разделения потоков. Способ облагораживания газойлей до дистиллятных углеводородов включает деление первого потока газойля на первую и вторую части; смешивание второго потока газойля с первой частью первого потока газойля для формирования смешанного потока газойля; контактирование смешанного потока газойля и водорода с первым катализатором гидроконверсии в первой реакционной системе гидрокрекинга для превращения по меньшей мере части углеводородов в смешанном потоке газойля в дистиллятные углеводороды; извлечение эффлюента из первой реакционной системы гидрокрекинга, содержащего не превращенные углеводороды и дистиллятные углеводороды; фракционирование эффлюента из первой реакционной системы гидрокрекинга на одну или более углеводородные фракции, включая фракцию, содержащую не ...

PROCESS AND APPARATUS FOR PERFORMING CHEMICAL REACTIONS UNDER PRESSURE IN A MULTI-STAGE REACTION ZONE WITH EXTERNAL INTERMEDIARY THERMAL CONDITIONING

CONTROL OF POLYNUCLEAR AROMATIC BY-PRODUCTS IN A HYDROCRACKING PROCESS

Process for hydrogenation of wax and process for production of fuel base

A process for the hydrogenation of wax, which is characterized by comprising the first step of hydrocracking a raw material wax containing at least 70% by mass of n-paraffins having 16 or more carbon atoms by bringing the wax into contact with a catalyst comprising a carrier containing an amorphous solid acid and a group VIII metal of the periodic table supported on the carrier in the presence of hydrogen, the second step of changing temporarily the raw material from the wax to a light paraffin containing at least 60% by mass of paraffins having 9 to 21 carbon atoms and hydrocracking the light paraffin by bringing it into contact with the catalyst in the presence of hydrogen, and the third step of changing the raw material from the light paraffin to the same wax as used in the first step and hydrocracking the wax by bringing it into contact with the catalyst in the presence of hydrogen.

PROCESS FOR SEPARATING HYDROPROCESSED EFFLUENT STREAMS

T 5880 PROCESS FOR SEPARATING HYDROPROCESSED EFFLUENT STREAMS Process for separating a mixed-phase hydrocarbonaceous effluent originating from the conversion of a hydrocarbonaceous feedstock in the presence of hydrogen at elevated temperature and pressure in a multiple separator system, which effluent contains hydrogen, normally liquid hydrocarbonaceous components and normally gaseous hydrocarbonaceous components by i) separating in a first separation zone the effluent into a first liquid phase (L1) and a first vapour phase (V1), ii) cooling the first vapour phase obtained to a temperature in the range between 25 and 85 .degree.C and separating the cooled vapour phase in a second separation zone whilst substantially maintaining the pressure of the first separation zone into a second liquid phase (L2) and a second, hydrogenrich vapour phase (V2), iii) separating the first liquid phase in a third separation zone whilst substantially maintaining the temperature of the first separation zone ...

PROCESS FOR MAKING FUEL GAS

PROCESS FOR HYDROCRACKING A HYDROCARBON FEEDSTOCK

A hydrocracking process comprising the steps of: (a) combining a hydrocarbonaceous feedstock and a heavy bottom fraction recycle stream with a hydrogen-rich gas to obtain a mixture comprising hydrocarbonaceous feedstock and hydrogen; (b) catalytically hydrocracking the mixture comprising hydrocarbonaceous feedstock and hydrogen in a hydrocracking zone to obtain a hydrocracked effluent; (c) separating the hydrocracked effluent into a first vapour portion and a first liquid portion in a separation zone; (d) heating the first liquid portion to form a vapourised first liquid portion; (e) feeding the vapourised first liquid portion to a fractionation section producing individual product fractions including a heavy bottom fraction comprising unconverted oil at the bottom zone of the fractionation section; (f) withdrawing from the fractionation section the heavy bottom fraction; (g) splitting the heavy bottom fraction in a stream for stripping and a heavy bottom fraction recycle stream; (h) stripping ...

СПОСОБ ПЕРЕРАБОТКИ СИНТЕТИЧЕСКОГО МАСЛА ФИШЕРА-ТРОПША ДЛЯ ПОЛУЧЕНИЯ БАЗОВОГО КОМПОНЕНТА ДИЗЕЛЬНОГО ТОПЛИВА И СПОСОБ РАСЧЕТА СКОРОСТИ КРЕКИНГА ПРИ ГИДРОКРЕКИНГЕ ПАРАФИНОВОЙ ФРАКЦИИ

Целью настоящего изобретения является разработка способа переработки синтетического масла Фишера-Тропша с получением базового компонента дизельного топлива, включающего (а) фракционирование в аппарате для дробной перегонки синтетического масла Фишера-Тропша, полученного методом синтеза Фишера-Тропша, по меньшей мере на две фракции средней фракции, содержащей компонент, имеющий интервал температур кипения, соответствующий дизельному топливу, и парафиновую фракцию, содержащую парафиновый компонент более тяжелый, чем средняя фракция; (b) осуществление контакта парафиновой фракции с катализатором гидрокрекинга в реакторе гидрокрекинга с получением продукта гидрокрекинга; (с) отделение газового компонента от продукта гидрокрекинга с получением масла гидрокрекинга в газожидкостном сепараторе, расположенном вблизи реактора гидрокрекинга, использованного на стадии (b); (d) определение состава газового компонента, отделенного на стадии (с); (е) расчет скорости крекинга в реакции гидрокрекинга по ...

METHOD HYDRO CRACKING AND METHOD OF PRODUCING MINERAL OIL

СПОСОБ ГИДРОКРЕКИНГА И СПОСОБ ПОЛУЧЕНИЯ МИНЕРАЛЬНОГО МАСЛА

Способ гидрокрекинга, включающий стадию гидрокрекинга парафиновой фракции, на которой парафиновую фракцию, содержащуюся в минеральном масле Фишера-Тропша, подвергают гидрокрекингу с получением продукта гидрокрекинга; стадию разделения газ-жидкость, на которой используют многостадийный газожидкостной сепаратор для разделения продукта гидрокрекинга на газовый компонент, компонент тяжелого масла и компонент легкого масла; стадию установления содержания конкретного компонента, на которой определяют соотношение скоростей потоков между компонентом тяжелого масла и компонентом легкого масла, и данное соотношение используют для определения установленного значения содержания конкретного углеводородного компонента, содержащегося в продукте гидрокрекинга; и стадию контроля, на которой контролируют работу стадии гидрокрекинга парафиновой фракции на основе установленного значения таким образом, что содержание конкретного углеводородного компонента попадает в заранее определенный диапазон.

METHOD OF CONVERTING MIXTURE PLASTIC WASTE (MWP) IN VALUABLE PETROCHEMICAL PRODUCTS

Способ гидрокрекинга и способ получения минерального масла

Использование: нефтегазовая промышленность. Задача: обеспечение сохранения высокого качества среднего дистиллята. Сущность изобретения: способ гидрокрекинга включает гидрокрекинг парафиновой фракции жидких углеводородов, подачу полученного продукта в ректификационную колонну для получения среднего дистиллята и кубового масла, рециркулирование всего кубового масла на стадию гидрокрекинга парафиновой фракции и контроль гидрокрекинга парафиновой фракции с использованием скорости потока кубового масла. Способ получения минерального масла включает синтез жидких углеводородов из сырьевого газа, гидрокрекинг парафиновой фракции в составе жидких углеводородов, подачу продукта гидрокрекинга в ректификационную колонну для получения среднего дистиллята и кубового масла, рециркулирование всего кубового масла на стадию гидрокрекинга и контроль гидрокрекинга парафиновой фракции с использованием скорости потока кубового масла. 2 н.п.ф., 6 з.п.ф., 3 ил.

PROCESS AND APPARATUS FOR PRESSURE CHEMICAL REACTIONS IN MULTI-REACTIONARY RANGE HAVING EXTERNAL INTERMEDIARY THERMOREGULATION

Composition control of gases

METHOD SOFT HYDROCRACKING OF HEAVY HYDROCARBON CUTS OPTIMIZED THERMAL INTEGRATION FOR REDUCING EMISSIONS OF GREENHOUSE GAS

PROCESS FOR HIDROCRAQUEAR A HYDROCARBON FEEDSTOCK

HIGH THROUGHPUT DEVELOPMENT METHOD FOR CATALYTIC HYDROPROCESSING OF DIRTY FEEDSTOCKS

A method for determining a set of operating parameters for a commercial scale plug flow catalytic process and reactor system for hydroprocessing dirty feedstocks, comprises the steps of: feeding selected partial pressures of said feedstock and hydrogen to the inlet the first reactor stage of a first composite multi-stage series-connected laboratory scale plug flow reactor including at least three reactor stages, the catalyst beds of each of said reactor stages including catalyst particles capable of catalyzing the removal by hydrogen of heteroatoms from said heterocyclic molecules; sampling the effluents of each of said reactor stages; measuring the concentration of heterocyclic molecules in said dirty feedstock in the concentrations of heterocyclic molecules and intermediate and final products and by products of the catalytic reaction in the effluents of each of said reactor stages.

Hydrocarbon upgrading

Aspects of the invention provide a process for upgrading a hydrocarbon feed. The process includes providing a hydrocarbon feed and a utility fluid. Then selectively extracting from the feed at least a portion of particulates to produce a raffinate and an extract. Third hydroprocessing at least a portion of the raffinate.

Hydrocracking process for producing distillate or naptha

The invention relates to a catalytic hydrocracker with two different catalyst beds within the reactor where each is loaded with a catalyst that has different hydrocracking properties. A first catalyst bed preferably cracks heavy oil more aggressively than the catalyst in the second bed. The catalytic hydrocracker includes further two recycle lines such that one directs unconverted oil through both hydrocracker beds and a bypass inlet is positioned between the first and second catalyst beds to admit unconverted oil to pass only through the second less aggressive hydrocracker catalyst bed. When gasoline prices favor the production of gasoline, less unconverted oil is recycled through the bypass therefore making more gasoline, but when prices favor the production of jet and diesel, more recycle is directed through the bypass recycle thus making less gasoline and more diesel and jet fuel.

METHOD OF HYDROCRACKING AND PROCESS FOR PRODUCING HYDROCARBON OIL

A hydrocracking process that includes a wax fraction hydrocracking step of hydrocracking the wax fraction contained within a Fischer-Tropsch synthetic oil to obtain a hydrocracked product, a gas-liquid separation step of using a multi-stage gas-liquid separator to separate the hydrocracked product into a gas component, a heavy oil component and a light oil component, a specific component content estimation step of determining the flow rate ratio between the heavy oil component and the light oil component, and using this flow rate ratio to determine an estimated value for the content of a specific hydrocarbon component contained within the hydrocracked product, and a control step of controlling the operation of the wax fraction hydrocracking step on the basis of this estimated value, so that the content of the specific hydrocarbon component falls within a predetermined range.

DISTRIBUTOR ASSEMBLY

This invention relates to a distributor assembly for multi-bed, down-flow catalytic reactors, that is, reactors which include vertically superimposed packed beds of particulate catalytic material and where a liquid or liquid and gas mixture is processed as it flows down through the packed beds. This type of reactor is used in the petroleum and chemical processing industries for carrying out various catalytic reactions, such as hydrotreating, hydrofinishing, hydrocracking, and dewaxing.

СПОСОБ ГИДРОКОНВЕРСИИ ТЯЖЕЛЫХ ФРАКЦИЙ НЕФТИ

Настоящее изобретение относится к области нефтепереработки тяжелых нефтяных фракций. Изобретение касается способа гидроконверсии тяжелых фракций нефти - исходного сырья, состоит из нулевой стадии и последующих N стадий. Нулевая стадия включает подачу в реактор сырья, прекурсора катализатора - водного раствора соли Мо (VI) или солей Мо и Ni, и водорода при давлении 4-9 МПа при нормальных условиях, реакции сырья и водорода при 420-450°С в присутствии образующегося в реакторе из прекурсора суспендированного наноразмерного молибденового или молибдено-никелевого катализатора, атмосферную или атмосферно-вакуумную перегонку гидрогенизата, вывод низкокипящей фракции с температурой кипения не выше 500°C как продукта и возвращение высококипящей фракции ВКФ или ее части в реактор. Последующие стадии включают подачу в реактор сырья, прекурсора катализатора, возвращенной части ВКФ и водорода, их реакцию, атмосферную указанную перегонку гидрогенизата, вывод низкокипящей фракции как продукта, возвращение ...

СИСТЕМА И СПОСОБ КОНТРОЛЯ И ОПТИМИЗАЦИИ ГИДРОТЕРМАЛЬНОГО ПРОЦЕССА ОБЛАГОРАЖИВАНИЯ ТЯЖЕЛОЙ СЫРОЙ НЕФТИ И БИТУМОВ

Изобретение относится к области переработки углеводородов. Изобретение касается системы облагораживания непрерывного технологического потока, включающей тяжелую сырую нефть (ТСН), содержащую маршрут потока жидкости, выполненный с возможностью непрерывной доставки технологического потока по этому маршруту в направлении течения, при этом маршрут потока включает в себя реактор. Реактор принимает технологический поток вместе с водой при температуре на входе в пределах приблизительно 60-200°С. Реактор включает в себя одну или более расходомерных труб, имеющих совокупную длину, приблизительно в 30 раз превышающую их совокупный поперечный размер поперечного сечения, и постепенно нагревает технологический поток до температуры на выходе Т(max)1 в пределах приблизительно 260-400°С. Реактор поддерживает давление в технологическом потоке, достаточное для обеспечения однофазного течения при Т(max)1. Контроллер выборочно регулирует скорость технологического потока, проходящего через реактор, чтобы поддерживать ...

СПОСОБ ГИДРОКОНВЕРСИИ ТЯЖЕЛЫХ ФРАКЦИЙ НЕФТИ

... 1. Способ гидроконверсии тяжелых фракций нефти - исходного сырья, включающий подачу в реактор исходного сырья, прекурсора катализатора, содержащего водный раствор соли Мо (VI), и водорода, реакции сырья и водорода в присутствии образующегося в реакторе из прекурсора суспендированного наноразмерного молибденового или молибдено-никелевого катализатора, перегонку гидрогенизата, вывод низкокипящей фракции как продукта, возвращение части высококипящей фракции ВКФ на стадию подачи в реактор сырья, прекурсора катализатора - свежего и регенерированного - и водорода, термообработку остальной части ВКФ с получением золошлаковых остатков, которые используют для регенерации прекурсора катализатора и извлечения металлов, отличающийся тем, что способ состоит из нулевой стадии, включающей подачу в реактор исходного сырья, прекурсора катализатора - водного раствора соли Мо (VI) или солей Мо и Ni, и водорода при давлении 4-9 МПа при нормальных условиях, реакцию сырья и водорода при 420-450°C в присутствии ...

Способ гидроочистки тяжелых нефтяных фракций

PROCESS FOR SEPARATING HYDROPROCESSED EFFLUENT STREAMS

Petroleum hydrocracking

AUTOACCELERATION CONTROL FOR EXOTHERMIC REACTORS

PROCESS FOR CONVERSION OF RESIDUE EMPLOYING MOVING BED TECHNOLOGY AND BUBBLING BED TECHNOLOGY

L'invention décrit un procédé de conversion de fractions lourdes carbonées ayant une température initiale d'ébullition d'au moins 300 °C en produits plus légers valorisables, ledit procédé comportant un passage de ladite charge dans une zone réactionnelle d'hydroraffinage comportant au moins un réacteur à lit mobile, et le passage d'au moins une partie de l'effluent issu de l'étape a) dans une zone réactionnelle d'hydroconversion comprenant au moins un réacteur triphasique, en présence d'hydrogène, ledit réacteur contenant au moins un catalyseur d'hydroconversion et fonctionnant en lit bouillonnant, à courant ascendant de liquide et de gaz et comportant au moins un moyen de soutirage dudit catalyseur hors dudit réacteur et au moins un moyen d'appoint de catalyseur frais dans ledit réacteur, dans des conditions permettant d'obtenir une charge liquide à teneur réduite en Carbone Conradson, en métaux, en soufre et en azote.

METHOD OF HYDROCRACKING AND PROCESS FOR PRODUCING HYDROCARBON OIL

Disclosed is a method of hydrocracking which comprises: a wax-fraction hydrocracking step in which a wax fraction separated from a Fischer-Tropsch synthesis oil is hydrocracked to obtain a hydrocracking product; a gas-liquid separation step in which the hydrocracking product is separated with a multistage gas-liquid separator into gaseous matter, heavy-oil matter, and light-oil matter; a step for estimating the content of specific components in which the ratio of the flow rate of the heavy-oil matter to the flow rate of the light-oil matter is determined, and the content of specific hydrocarbon components in the hydrocracking product is estimated from the flow-rate ratio; and a control step in which the operation for the wax-fraction hydrocracking step is controlled on the basis of the estimated value so that the content of the specific hydrocarbon components is in a given range.

HYDROCRACKING PROCESS AND PROCESS FOR PRODUCING HYDROCARBON OIL

A hydrocracking process for a wax fraction that includes a wax fraction hydrocracking step of hydrocracking a wax fraction contained within liquid hydrocarbons synthesized by a Fischer-Tropsch synthesis reaction, thereby obtaining a hydrocracked product, a fractional distillation step of supplying the hydrocracked product to a fractionator in which a bottom cut temperature is set to a constant value, and obtaining at least a middle distillate and a bottom oil from the fractionator, a recycling step of resupplying all of the bottom oil to the wax fraction hydrocracking step, and a hydrocracking control step of controlling the wax fraction hydrocracking step using a flow rate of the bottom oil as an indicator.

METHODOLOGY TO DETERMINE FEED QUALITY (DI+RING AROMATIC CONTENT) OF FCC AND HYDROCRACKING FEEDS

A method of upgrading naphtha and diesel yields from fluid catalytic cracking and hydrocracking units by improving a feed quality of a petroleum feedstock, product or fraction mixture. The method of improving the feed quality of the petroleum feedstock, product or fraction mixture occurs by first determining the API Gravity of a petroleum feedstock, product or fraction mixture. A temperature at which about fifty percent of the petroleum feedstock, product or fraction boils (T50) is then determined. The feed quality for the petroleum feedstock, product or fraction mixture as determined from the API Gravity and the T50 for the feedstock, product or fraction mixture is then estimated followed by adjusting the petroleum feedstock, product or fraction mixture to achieve a higher feed quality.

METHOD OF OPERATING A CATALYTIC STREAM-HYDROCARBON REFORMER

Method of operating a catalytic steam-hydrocarbon reformer where the steam flow rate at which carbon forms on the inner wall of a catalyst-containing reformer tube is determined, and the steam flow rate to the catalytic steam-hydrocarbon reformer is controlled responsive to the determined steam flow rate at which carbon forms on the inner wall of the catalyst-containing reformer tube.

СПОСОБ ГИДРОКРЕКИНГА И СПОСОБ ПОЛУЧЕНИЯ МИНЕРАЛЬНОГО МАСЛА

Способ гидрокрекинга, включающий стадию гидрокрекинга парафиновой фракции, на которой парафиновую фракцию, содержащуюся в минеральном масле Фишера-Тропша, подвергают гидрокрекингу с получением продукта гидрокрекинга; стадию разделения газ-жидкость, на которой используют многостадийный газожидкостной сепаратор для разделения продукта гидрокрекинга на газовый компонент, компонент тяжелого масла и компонент легкого масла; стадию установления содержания конкретного компонента, на которой определяют соотношение скоростей потоков между компонентом тяжелого масла и компонентом легкого масла, и данное соотношение используют для определения установленного значения содержания конкретного углеводородного компонента, содержащегося в продукте гидрокрекинга; и стадию регулирования, на которой регулируют работу стадии гидрокрекинга парафиновой фракции на основе установленного значения таким образом, что содержание конкретного углеводородного компонента попадает в заранее определенный диапазон.

DISTRIBUTION UNIT

СПОСОБ ГИДРОКРЕКИНГА И СПОСОБ ПОЛУЧЕНИЯ МИНЕРАЛЬНОГО МАСЛА

Способ гидрокрекинга парафиновой фракции, который включает стадию гидрокрекинга парафиновой фракции, содержащейся в жидких углеводородах, синтезированных по реакции синтеза Фишера-Тропша, с получением таким образом продукта гидрокрекинга, стадию фракционной перегонки, где указанный продукт гидрокрекинга подают в ректификационную колонну, в которой температура отбора кубовой фракции установлена на постоянном значении, и получают по меньшей мере средний дистиллят и кубовое масло из указанной ректификационной колонны, стадию рециркуляции, на которой все указанное кубовое масло повторно подают на указанную стадию гидрокрекинга, и стадию контролирования гидрокрекинга, на которой контролируют стадию гидрокрекинга парафиновой фракции с использованием скорости потока указанного кубового масла в качестве индикатора.

СПОСОБ ПЕРЕРАБОТКИ СИНТЕТИЧЕСКОГО МАСЛА ФИШЕРА-ТРОПША ДЛЯ ПОЛУЧЕНИЯ БАЗОВОГО КОМПОНЕНТА ДИЗЕЛЬНОГО ТОПЛИВА И СПОСОБ РАСЧЕТА СКОРОСТИ КРЕКИНГА ПРИ ГИДРОКРЕКИНГЕ ПАРАФИНОВОЙ ФРАКЦИИ

Целью настоящего изобретения является разработка способа переработки синтетического масла Фишера-Тропша с получением базового компонента дизельного топлива, включающего: (а) фракционирование в аппарате для дробной перегонки синтетического масла Фишера-Тропша, полученного методом синтеза Фишера-Тропша, по меньшей мере на две фракции: среднюю фракцию, содержащую компонент, имеющий интервал температур кипения, соответствующий дизельному топливу, и парафиновую фракцию, содержащую парафиновый компонент более тяжелый, чем средняя фракция; (b) осуществление контакта парафиновой фракции с катализатором гидрокрекинга в реакторе гидрокрекинга с получением продукта гидрокрекинга; (с) отделение газового компонента от продукта гидрокрекинга с получением масла гидрокрекинга в газожидкостном сепараторе, расположенном после реактора гидрокрекинга, использованного на стадии (b); (d) определение состава газового компонента, отделенного на стадии (с); (е) расчет скорости крекинга в реакции гидрокрекинга по ...

СПОСОБ ПРЕВРАЩЕНИЯ СМЕСИ ПЛАСТМАССОВЫХ ОТХОДОВ (MWP) В ЦЕННЫЕ НЕФТЕХИМИЧЕСКИЕ ПРОДУКТЫ

Изобретение относится к способу превращения смеси пластмассовых отходов (MWP) в ценные нефтехимические продукты, включающему подачу смеси пластмассовых отходов в пиролизатор, превращение указанной MWP в газообразный поток и жидкий поток и дополнительную обработку указанного газообразного потока с получением ценных нефтехимических продуктов, при этом указанный способ дополнительно включает стадии i) подачи указанного жидкого потока вместе с сырьем для гидрокрекинга в установку гидрокрекинга; ii) превращения указанного жидкого потока вместе с указанным сырьем для гидрокрекинга посредством гидрокрекинга по меньшей мере в один газообразный поток и жидкий поток; iii) дополнительной обработки указанного по меньшей мере одного газообразного потока с получением ценных нефтехимических продуктов.

PROCESS FOR CONVERTING CARBONACEOUS MATERIALS

METHOD FOR THE EVALUATION OF HYDROCARBON FEEDSTOCKS FOR CATALYTIC CRACKING

Methods for assessing the potential for converting lubricating oil, for example, used lubricating oil, by catalytic cracking include subjecting a potential catalytic cracking feedstock to a plurality of tests to generate a plurality of measured properties characterized by a quantitative measured value, comparing each quantitative measured value to each pre-defined value; identifying each measured property whose quantitative measured value does not comport with the corresponding pre-defined value; and, if any measured properties are identified that do not comport with the corresponding pre-defined value, either a) processing the potential catalytic cracking feedstock to modified said measured properties to comport with the pre-defined value or b) combining a least a portion of the first potential catalytic cracking feedstock with at least a portion of a second potential catalytic cracking feedstock to generate a combined catalytic cracking feedstock.

PROCESS FOR PRODUCING A NAPHTHA STREAM

Process and apparatus for producing a naphtha stream is provided. The process comprises providing a kerosene stream to a hydrocracking reactor. The kerosene stream is hydrocracked in the presence of a hydrogen stream and a hydrocracking catalyst in the hydrocracking reactor at hydrocracking conditions comprising a hydrocracking pressure, a hydrocracking temperature, and a liquid hourly space velocity at a net conversion of at least 90%, to provide a hydrocracked effluent stream comprising liquefied petroleum gas, heavy naphtha fraction and light naphtha fraction. One or more of the hydrocracking conditions are adjusted to maintain a ratio of the light naphtha fraction to the heavy naphtha fraction of at least 2 by weight, suitably at least 2.2 and preferably at least 2.5 in the hydrocracked effluent stream while maintaining the net conversion of at least 90%.

POWER RECOVERY FROM QUENCH AND DILUTION VAPOR STREAMS

A process for reducing pressure of a vapor stream used for reducing a temperature or pressure in a reactor. A pressure of a vapor stream is reduced with a turbine to provide a lower pressure vapor stream. The vapor stream rotates a turbine wheel within the turbine. The turbine wheel is configured to transmit rotational movement to an electrical generator. Thus, electricity is generated with the turbine. The lower pressure vapor stream is injected into a reactor and reduces a temperature in the reactor or reduces a partial pressure of a hydrocarbon vapor in the reactor.

Pyrolysis Tar Pretreatment

This invention relates to thermally-treating and hydroprocessing pyrolysis tar to produce a hydroprocessed pyrolysis tar, but without excessive foulant accumulation during the hydroprocessing. The invention also relates to upgrading the hydroprocessed tar by additional hydroprocessing; to products of such processing; to blends comprising one or more of such products; and to the use of such products and blends, e.g., as lubricants, fuels, and/or constituents thereof. 1. A pyrolysis tar pretreatment process , comprising:{'sub': 'T', "(a) providing a pyrolysis tar having a reactivity (R) ≥28 BN, wherein, at least 70 wt. % of the pyrolysis tar's components have a normal boiling point of at least 290° C., based on the total weight of the pyrolysis tar;"}{'sub': 1', '2', 'HS', 'C', 'T', 'C', '1', '2', 'HS, '(b) maintaining the pyrolysis tar within a temperature range of from Tto Tfor a time (t) sufficient to produce a pyrolysis tar composition having a reactivity R Подробнее

PROZESSKONTROLLVERFAHREN FUER DIE KATALYTISCHE BEHANDLUNG VON KOHLENWASSERSTOFFOELEN

PROCEDURE FOR THE SEPARATION FROM HYDROGEN TREATMENT FROM RIVERS.

AUTOACCELERATION CONTROL FOR EXOTHERMIC REACTORS

HYDROPROCESSING REACTOR AND PROCESS WITH LIQUID QUENCH

A method and reactor system for catalytic hydrotreating and hydrocracking of liquid hydrocarbon feedstocks in order to produce a feedstock having a reduced contaminant level are disclosed. A feedstock (11) is introduced into a first reaction zone (18) of a reactor system (10) having a plurality of successive reaction zones, each having a hydroprocessing bed therein. Hydrogen gas (14) is introduced into the reactor system for flow through and over the catalyst beds in contact with the liquid in order to react with the feedstock producing an effluent. A stream having the same composition as the feedstock introduced into the first reaction zone is introduced into at least one quench stream downstream of the first reaction zone. Quench gas (42) is injected into each quench zone in an amount sufficient in combination with the effluent from the immediately upstream reaction zone to reduce the temperature of the effluent to a predetermined range. An effluent product (30) is recovered from the ...

THE K-STEP SELF-ADJUSTING MULTIVARIABLE DISCRETE CONTROLLERS

Methods to adjust the controller gain matrices of multivariable discrete controllers are suggested. The methods adjust a set of parameters called the state parameter matrices in k steps. The remaining parameter matrices of a controller are calculated from these matrices. Each step is a move in the steepest descent of the value of the variance of the disturbance caused by the dead time of the system. If the number of k steps is infinite, the self-adjusting algorithm is an adaptive algorithm. A unit value or small number of steps means that the self-adjusting algorithm is a self-tuning algorithm. The value of k determines how aggressive a control engineer wants the self-tuning algorithm to be. A zero value of k means that the controller is time invariant.

METHOD AND SYSTEM FOR CONTROLLING A HYDROCRACKER AND FRACTIONATOR

A method and system for controlling a hydrocracker and fractionator reaction loop is disclosed. The method and system utilizes a sidedraw tray within the fractionator distillation zone upon which liquid is collected. This liquid is withdrawn as a sidedraw stream. The withdrawal of the liquid from the sidedraw tray is controlled based on the level of liquid on the sidedraw tray rather than at a set or determined flow rate. The sidedraw stream is separated into a first stream and a product stream. Unlike other processes where the flow rate of the product stream is set and the internal reflux flow rate varies, the method involves fixing the flow rate of the first stream that is returned to the distillation zone of the fractionators with the flow rate of the product stream being set so as to control the liquid level on the sidedraw tray.

A METHOD OF PROCESSING HEAVY OILS AND RESIDUA

There is provided a process of treating a heavy hydrocarbon-comprising material, comprising: contacting a feed material with at least a catalyst material within a contacting zone to effect generation of a total product such that a contacting zone material is disposed within the contacting zone and consists of the catalyst material and a feed/product- comprising mixture comprising the feed material and the total product, wherein the feed/product- comprising mixture includes a Conradson carbon residue content of at least 12 weight percent, based on the total weight of the feed/product-comprising mixture, and also includes an asphaltene content of less than two (2) weight percent, based on the total weight of the feed/product- comprising mixture, and wherein the feed material includes deasphalted heavy hydrocarbon- comprising material. A heavy hydrocarbon-containing feed for a catalytic hydroprocessing or catalytic hydrocracking process is also provided, wherein the feed comprises a deasphalted ...

Process for hydrocracking a hydrocarbon feedstock

Composition control of gases

Hydro-treating or hydro converting a heavy load type atmospheric residue or vacuum residue using a fixed bed reactor with descending flow of gas phase or liquid phase during a cycle of reverse flow of reaction fluids

La présente inversion décrit un procédé d'hydrotraitement ou d'hydroconversion de charge lourde de type résidu atmosphérique ou sous vide faisant appel à au moins un réacteur en lit fixe à écoulement descendant d'au moins une phase gaz ou liquide, réacteur qui subit au cours du cycle dudit procédé une inversion de sens d'écoulement du ou des fluides réactionnels.

Process of hydrogen' ation

Procédé de conversion de matières carbonées en milieu de masse fondue.

On met en contact une charge carbonée avec un milieu de masse fondue dans la section inférieure d'une zone de réaction 1 verticale, allongée, au moins une matière gazeuse étant présente, de sorte qu'il se forme un mélange polyphasé. On transporte hydrauliquement ce mélange polyphasé vers la section supérieure de la zone de réaction 1 avec un courant parallèle des constituants de ce mélange, à une vitesse suffisante pour avoir un effet élévateur par gaz. Il se produit une réaction chimique et le mélange après réaction passe de la section supérieure de la zone de réaction 1 dans un dispositif 6 où l'on sépare en un courant gazeux et un courant liquide comprenant le milieu de masse fondue.

PROCESS OF CONVERSION OF CARBONACEOUS MATTERS INTO MEDIUM OF MOLTEN MASS

processo para hidroprocessamento de um óleo combustível

Method for producing hydrocracked lube oil products

The production of lube oil product by hydrocracking is made more selective and commercially attractive by blending charge components to achieve viscosity levels suitable for temperature selective conversion to lube oil product commensurate with the relationships established by the curves of FIGS. 1 and 2.

Hydrocracking process utilizing aqueous ammonia

A process for controlling hydrocracking reactions in a hydrocracking reactor by passing aqueous ammonia to the hydrocracking reactor. The aqueous ammonia is injected into the process at various locations at a low pressure, typically between approximately 0.17 to approximately 2.07 MPa (25 to 300 psi). A wash fluid can be used to lower the concentration of ammonia in the hydrocracking reactor, and thus, increase the catalytic activity of the hydrocracking catalyst.

VERFAHREN UND APPARAT ZUR AUSFUEHRUNG VON CHEMISCHEN REAKTIONEN UNTER HOCHDRUCK IN EINER MEHRSTUFIGEN REAKTIONSZONE MIT ZWISCHENGESCHALTETEN, AUSSEN LIEGENDEN THERMISCHEN BEHANDLUNGEN.

Device and method for the continuous reprocessing of spent oil

In a device and method for the continuous reprocessing of spent oil, the latter is pumped into single-tube reactors, in which, after passing through sections of different temperatures and pressures via separators and condensers, the individual fractions such as, for example, heavy naphtha, spindle oils and neutral oils, base oils and the like are taken off as side products and, if appropriate, hydrogenated in side streams which can likewise be designed as single-tube reactors.

Process and apparatus for carbonaceous material conversion

A process for conversion of a carbonaceous feed material (2) into gaseous products, comprising the steps of: contacting a carbonaceous feed material with a molten mass medium in the lower section of a substantially vertical, elongated reaction zone (1) to form a mixture of carbonaceous feed material and molten mass medium, whereby at least one gaseous material is present and a multi-phase mixture is formed; hydraulically transporting the multi-phase mixture substantially upwardly through the reaction zone to the upper section thereof and with a velocity sufficient to establish a gas lift effect to provide improved yields in a chemical conversion reaction producing a modified multi-phase mixture; passing the modified multi-phase mixture to a separation device (6); and separating the modified multi-phase mixture into a gaseous product(s) stream (7) and a liquid stream (9) comprising said molten mass medium; and apparatus for carrying out the process.

PROCESS FOR THE CONVERSION OF CARBONACEOUS MATERIALS

SYSTEMS AND METHODS FOR EXTERNAL PROCESSING OF FLASH ZONE GAS OIL FROM A DELAYED COKING PROCESS

Systems and methods for the external processing flash zone gas oil by recycling it through a vacuum residuum hydroprocessing unit before reentering the delayed coking process.

METHODOLOGY TO DETERMINE FEED QUALITY (DI+RING AROMATIC CONTENT) OF FCC AND HYDROCRACKING FEEDS

A method of upgrading naphtha and diesel yields from fluid catalytic cracking and hydrocracking units by improving a feed quality of a petroleum feedstock, product or fraction mixture. The method of improving the feed quality of the petroleum feedstock, product or fraction mixture occurs by first determining the API Gravity of a petroleum feedstock, product or fraction mixture. A temperature at which about fifty percent of the petroleum feedstock, product or fraction boils (T50) is then determined. The feed quality for the petroleum feedstock, product or fraction mixture as determined from the API Gravity and the T50 for the feedstock, product or fraction mixture is then estimated followed by adjusting the petroleum feedstock, product or fraction mixture to achieve a higher feed quality.

METHOD FOR CHARACTERIZING FEEDS TO CATALYTIC CRACKING PROCESS UNITS

The present invention is a method to determine the chemical concentration of one or more of a number of the constituent classes of a feed to a catalyt ic cracking process. these constituent classes which are referred to as "lumps", includi ng 14 different molecular types in 4 different boiling range fractions. A specific lump will include all individual molecular components which are expected to react in a similar way in the catalytic cracking unit.

Process for converting mixed waste plastic (mwp) into valuable petrochemicals

METHOD SOFT HYDROCRACKING OF HEAVY HYDROCARBON CUTS OPTIMIZED THERMAL INTEGRATION

PROCEDE ET APPAREIL POUR EFFECTUER SOUS PRESSION DES REACTIONS CHIMIQUES DANS UNE ZONE REACTIONNELLE MULTI-ETAGEE AVEC CONDITIONNEMENTS THERMIQUES INTERMEDIAIRES EXTERIEURS

ON DECRIT UN PROCEDE ET UN APPAREIL POUR EFFECTUER SOUS PRESSION DES REACTIONS CHIMIQUES EN PRESENCE D'UN CATALYSEUR SOLIDE DANS UNE ZONE REACTIONNELLE MULTI-ETAGEE AVEC CONDITIONNEMENTS THERMIQUES INTERMEDIAIRES EXTERIEURS. SELON LE PROCEDE, ON INTRODUIT AU MOINS UN FLUIDE REACTIONNEL DANS AU MOINS UN COMPARTIMENT 201, ON RECUPERE UN PREMIER EFFLUENT REACTIONNEL, ON ECHANGE DE LA CHALEUR A L'EXTERIEUR DE LA ZONE REACTIONNELLE ENTRE LE PREMIER EFFLUENT ET UN MILIEU D'ECHANGE 4 DE CHALEUR EXTERNE, ON INTRODUIT ENSUITE CE PREMIER EFFLUENT DANS AU MOINS UN COMPARTIMENT SUBSEQUENT 203 ET L'ON RECUPERE UN SECOND EFFLUENT REACTIONNEL DUDIT COMPARTIMENT SUBSEQUENT. ON FAIT CIRCULER, EN OUTRE, LEDIT FLUIDE REACTIONNEL OU LEDIT EFFLUENT REACTIONNEL DANS LESDITS COMPARTIMENTS 201, 203 TRANSVERSALEMENT DE FACON SENSIBLEMENT PERPENDICULAIRE A LA GENERATRICE DE LA ZONE REACTIONNELLE 2, LESDITS COMPARTIMENTS ETANT ETANCHES ET DE FORME ALLONGEE, CHACUN DES DITS COMPARTIMENTS ETANT ADJACENT A UN OU DEUX ...

수소화 분해 장치 및 분류 장치를 제어하기 위한 방법 및 시스템

... 수소화 분해 장치 및 분류 장치 반응 루프를 제어하기 위한 방법 및 시스템이 개시된다. 방법 및 시스템은 액체가 수집되는 분류 장치 증류 구역 내에 사이드 드로 트레이를 사용한다. 이러한 액체는 사이드 드로 스트림으로서 인출된다. 사이드 드로 트레이로부터의 액체의 인출은 설정된 또는 결정된 유량으로 보다 오히려 사이드 드로 트레이에서의 액체의 레벨에 기초되어 제어된다. 사이드 드로 스트림은 제 1 스트림 및 제품 스트림으로 분리된다. 제품 스트림의 유량이 설정되고 내부 환류 유량이 변하는 다른 프로세스들과 달리, 본 방법은 분류 장치들의 증류 구역으로 복귀되는 제 1 스트림의 유량을 정량하는 것을 포함하고, 제품 스트림의 유량은 사이드 드로 트레이에서 액체 레벨을 제어하도록 설정된다.

OPERATING SLIDE VALVES IN PETROCHEMICAL PLANTS OR REFINERIES

A plant or refinery may include equipment such as condensers, regenerators, distillation columns, pumps, slide valves, or the like. Different operating methods may impact deterioration in equipment condition, thereby prolonging equipment life, extending production operating time, or providing other benefits. Mechanical or digital sensors may be used for monitoring equipment to determine whether problems are developing. Specifically, sensors may be used in conjunction with one or more system components to predict and detect slide valve sticking. A shielded, tube skin thermocouple assembly may provide a temperature profile for a slide valve. Tomography may be used to image a slide valve. An operating condition of the plant or refinery may be adjusted to prolong equipment life or avoid equipment failure.

HYDROREFINING AND/HYDROCRACKING HEAVY HYDROCARBON FEEDS

PROCESS FOR HYDROGENATING A CARBONACEOUS MATERIAL, IN PARTICULAR COAL AND/OR HEAVY OIL

PRODUCTION OF HIGH OCTANE GASOLINE

PROCESSING OF FEEDSTOCKS IN SEPARATED REACTOR VOLUMES

Separated volumes can be created in a reactor using interior dividing wall or interior conduit structures. Feedstocks can be hydroprocessed in the separated volumes to allow multiple types of hydroprocessing conditions and/ or feeds to be processed in a single reactor. The feedstocks can remain separate for the entire volume of the reactor, or the dividing barrier can end at some intermediate point in the reactor.

Modeling method for hydrogenation reaction effluent system failure control parameter

The invention discloses a modeling method for invalidation control parameter of hydrogenation reaction effluent system; wherein, the invalidation control parameter modeling comprises a KP value, the concentration of NH4HS, the theoretical quantity of water injection, the deposition temperature of NH4HS, the deposition temperature of NH4Cl and the mean velocity of air cooler. The modeling method is characterized in that the operation parameters of hydrogenation reaction effluent system are loaded by the DCS control system data base, the material chemical examination analysis data and the principle flow chart of hydrogenation reaction are combined, the modeling is processed according to the concrete invalidation control parameter in the running of hydrogenation reaction effluent system variable condition, and that the KP value, the concentration of NH4HS, the theoretical quantity of water injection, the deposition temperature of NH4HS, the deposition temperature of NH4Cl and the mean velocity ...

Method for improving cracking and stable performance of jet fuel

The invention discloses a method for improving the cracking and stable performance of jet fuel, which comprises the following steps of: coating a catalyst on the inner wall surface of a heat exchanging pipeline and adding a proper amount of hydrogen donor into the jet fuel. The method can reduce the generation of deposited carbon and prolong the service life of the catalyst while ensuring the catalytic cracking and heat absorption of the jet fuel in a heat exchanging system. The selected hydrogen donor is cyclane or cycloalkyl aromatic hydrocarbon containing 1-2 naphthenic rings, or the cycloalkyl aromatic hydrocarbon in which substitutions of oxygen, nitrogen, sulfur and the like occur on a cycloalkyl; the catalyst is one or more from a ZSM-5, or a Y-shaped or beta-shaped molecular sieve, or one or more from the ZSM-5, or the Y-shaped or beta-shaped molecular sieve loading one or more noble metals of Pd, Pt, Ag or Ni. The method can improve the high heat stability of the fuel and prolong ...

HYDROPROCESSING METHOD FOR HEAVY HYDROCARBON THERMAL INTEGRATED OPTIMIZED TO REDUCE THE GREENHOUSE GAS EMISSIONS

La présente invention décrit un procédé d'hydrocraquage doux de coupes hydrocarbures lourdes de type distillat sous vide ou huile désasphaltée à intégration thermique optimisée en vue de réduire les émissions de gaz à effet de serre.

METHOD AND APPARATUS FOR PERFORMING CHEMICAL REACTIONS UNDER PRESSURE IN A REACTION ZONE WITH MULTISTAGE HEAT PACKAGES EXTERNAL INTERMEDIATES

ADDITIVE CONTAINING AROMATICS AND RESINS AND HYDROCONVERSION METHOD USING SAME

The present invention relates to an additive for suppressing deposits or cokes which is introduced to suppress deposits or cokes generated by aggregation of asphaltene during the hydrocracking reaction of raw oil or refined oil. The additive of the present invention contains aromatics and resins, and the dipole momentum ranges from 2.0 to 4.2D. The present invention also relates to a method for reducing deposits and cokes generated during the hydrocracking reaction of the raw oil or refined oil. According to the present invention, the method includes the steps of: inserting the raw oil or the refined oil into a reactor; making the raw oil or the refined oil in the reactor hydroconversion-react; and introducing an additive containing the aromatics and resins when the conversion rate of the raw oil or the refined oil reaches 80 to 95%. COPYRIGHT KIPO 2018 ...

PROCESS FOR HYDROCRACKING HEAVY OIL AND OIL RESIDUE WITH AN ADDITIVE

A process for the hydroprocessing of heavy oils and/or oil residues, the process comprising the step of contacting the heavy oils and/or oil residues with a non-metallised carbonaceous additive in the presence of a hydrogen-containing gas at a temperature of from 250° C. to 600° C., wherein at least 80% of the cumulative pore volume of the non-metallised carbonaceous additive arises from pores having a pore size of at least 2 nm, wherein at least 50% of the cumulative pore volume of the non-metallised carbonaceous additive arises from pores having a pore size of at least 5 nm, and/or wherein at least 30% of the cumulative pore volume of the non-metallised carbonaceous additive arises from pores having a pore size of at least 10 nm. 2. A process according to claim 1 , wherein the non-metallised carbonaceous additive has an average pore size of at least 2 nm claim 1 , preferably from 2 nm to 10 nm claim 1 , more preferably from 2.25 nm to 8 nm claim 1 , even more preferably from 2.5 nm to 6 nm and even more preferably still from 3 nm to 5 nm.3. A process according to claim 1 , wherein the non-metallised carbonaceous additive is selected from the list consisting of: anthracite cokes claim 1 , lignite cokes claim 1 , carbon blacks claim 1 , activated cokes claim 1 , petroleum cokes claim 1 , furnace dusts claim 1 , dusts from Winkler gasification of coal claim 1 , red mud claim 1 , electrostatic filter dusts and cyclone dusts claim 1 , preferably wherein the non-metallised carbonaceous additive is a lignite coke.4. A process according to claim 1 , wherein the non-metallised carbonaceous additive comprises one or more metals in a combined amount of at least 6000 ppm claim 1 , preferably from 6000 ppm to 100000 ppm claim 1 , more preferably from 7000 ppm to 30000 ppm claim 1 , even more preferably from 8000 ppm to 20000 ppm claim 1 , even more preferably still from 9000 ppm to 15000 ppm and yet more preferably still from 10000 ppm to 13000 ppm claim 1 , by weight of the ...

POWER RECOVERY FROM QUENCH AND DILUTION VAPOR STREAMS

A process for reducing pressure of a vapor stream used for reducing a temperature or pressure in a reactor. A pressure of a vapor stream is reduced with a turbine to provide a lower pressure vapor stream. The vapor stream rotates a turbine wheel within the turbine. The turbine wheel is configured to transmit rotational movement to an electrical generator. Thus, electricity is generated with the turbine. The lower pressure vapor stream is injected into a reactor and reduces a temperature in the reactor or reduces a partial pressure of a hydrocarbon vapor in the reactor. 1. A process comprising: reducing a pressure of the vapor stream with a turbine to provide a lower pressure vapor stream, wherein the vapor stream comprises hydrogen;', 'rotating a turbine wheel within the turbine; and,', 'injecting the lower pressure vapor stream into the reactor and reducing the temperature in the reactor, wherein the reactor comprises an FCC reactor, and wherein the vapor stream comprises a steam stream,, 'reducing an amount of a vapor stream used for reducing a temperature, or heat load, in a reactor relative to a control valve bywherein the reactor comprises an FCC reactor, and wherein the vapor stream comprises a steam stream.2. A process comprising: providing a vapor stream comprising steam;', 'passing the vapor stream through a turbine, the turbine comprising a turbine wheel within the turbine; and,', 'reducing a partial pressure of a hydrocarbon vapor by mixing the reduced pressure vapor stream with the hydrocarbon vapor., 'reducing pressure of a vapor stream used for adjusting a partial pressure of a hydrocarbon vapor by3. The process of claim 1 , wherein the reduced pressure vapor stream is injected into an FCC reactor to reduce the partial pressure of the hydrocarbon vapor in the FCC reactor.4. The process of further comprising:recovering electricity generated with the turbine.5. The process of further comprising:adjusting one or more process conditions for the FCC reactor ...

Controlling temperature within a catalyst bed in a reactor vessel

A quenching medium is delivered directly to selected regions or locations within a catalyst bed in a hydroprocessing reactor vessel in order to control the reactivity of a hydroprocess occurring in the selected regions or locations separately from other regions or locations. Temperature sensors for providing temperature indications and conduits for delivering the quench medium are distributed throughout the catalyst bed. One or more conduits can be selected for delivery of the quenching medium to selected regions or locations so that separate control of the level of reactivity in each of various regions or locations throughout the bed can be achieved.

A method of characterizing hydrocarbon feeds and products using infra-red spectra

Process for separating hydroprocessed effluent streams

Process for separating a mixed-phase hydrocarbonaceous effluent originating from the conversion of a hydrocarbonaceous feedstock in the presence of hydrogen at elevated temperature and pressure in a multiple separator system, which effluent contains hydrogen, normally liquid hydrocarbonaceous components and normally gaseous hydrocarbonaceous components by i) separating in a first separation zone the effluent into a first liquid phase (L1) and a first vapour phase (V1), ii) cooling the first vapour phase obtained to a temperature in the range between 25 and 85 °C and separating the cooled vapour phase in a second separation zone whilst substantially maintaining the pressure of the first separation zone into a second liquid phase (L2) and a second, hydrogen-rich vapour phase (V2), iii) separating the first liquid phase in a third separation zone whilst substantially maintaining the temperature of the first separation zone and at a pressure below 60 bar into a third liquid phase (L3) and a ...

Hydrocracking process

СПОСОБ И СИСТЕМА РЕГУЛИРОВАНИЯ УСТАНОВКИ ГИДРОКРЕКИНГА И ФРАКЦИОНИРУЮЩЕЙ КОЛОННЫ

Настоящее изобретение относится к способу регулирования работы реакционного контура фракционирующей колонны и установки гидрокрекинга. Способ включает следующие стадии: обеспечение фракционирующей колонны для приема выходящего потока из реактора гидрокрекинга в качестве подаваемого сырья для фракционирующей колонны, при этом указанная фракционирующая колонна ограничивает зону дистилляции, которая включает в себя нижнюю зону, верхнюю зону и промежуточную зону между указанной нижней зоной и указанной верхней зоной, причем указанная промежуточная зона имеет тарелку отбора боковой фракции; введение указанного подаваемого сырья для фракционирующей колонны в указанную нижнюю зону указанной фракционирующей колонны; накопление на указанной тарелке отбора боковой фракции жидких углеводородов, имеющих желаемый температурный интервал кипения; отведение потока боковой фракции указанных углеводородов с указанной тарелки отбора боковой фракции; разделение указанного потока боковой фракции на первый поток ...

Hydrocrackverfahren

VERFAHREN ZUR TRENNUNG VON WASSERSTOFFBEHANDLUNGS-AUSFLUESSEN.

PROCESS FOR CONVERSION OF RESIDUE EMPLOYING MOVING BED TECHNOLOGY AND BUBBLING BED TECHNOLOGY

L'invention décrit un procédé de conversion de fractions lourdes carbonées ayant une température initiale d'ébullition d'au moins 300 °C en produits plus légers valorisables, ledit procédé comportant un passage de ladite charge dans une zone réactionnelle d'hydroraffinage comportant au moins un réacteur à lit mobile, et le passage d'au moins une partie de l'effluent issu de l'étape a) dans une zone réactionnelle d'hydroconversion comprenant au moins un réacteur triphasique, en présence d'hydrogène, ledit réacteur contenant au moins un catalyseur d'hydroconversion et fonctionnant en lit bouillonnant, à courant ascendant de liquide et de gaz et comportant au moins un moyen de soutirage dudit catalyseur hors dudit réacteur et au moins un moyen d'appoint de catalyseur frais dans ledit réacteur, dans des conditions permettant d'obtenir une charge liquide à teneur réduite en Carbone Conradson, en métaux, en soufre et en azote.

HYDROCRACKING PROCESS

T 2286 HYDROCRACKING PROCESS Process for hydrocracking a hydrocarbonaceous feedstock wherein use is made of a reactor comprising at least two separate beds of catalyst stacked on top of each other, which catalyst comprises one or more hydrogenation components of a Group VIB metal and/or Group VIII metal and a carrier having hydrocracking activity, whereby the metals content of at least one of the hydrogenation components of the catalyst used in one or more of the top beds comprising up to fifty percent by volume of the total catalyst used in the reactor is at least 1.5 times the metals content of the corresponding hydrogenation component of the catalyst used in the remaining beds and the average effective particle diameter of the catalyst used in one or more of the top beds is at most 0.75 times the average effective particle diameter of the catalyst used in the remaining beds. C14/T2286FF ...

PROCESS FOR HYDROCRACKING A HYDROCARBON FEEDSTOCK

USE OF LOW BOILING POINT AROMATIC SOLVENT IN HYDROPROCESSING HEAVY HYDROCARBONS

This invention is directed to a process for producing a hydroprocessed product. The invention is particularly advantageous in that substantially less hydrogen is absorbed during the process relative to conventional hydroprocessing methods. This benefit is achieved by using a particular solvent as a co-feed component. In particular, the solvent component contains at least one single ring aromatic compound and has a relatively low boiling point range compared to the heavy hydrocarbon oil component used as another co-feed component. 1. A process for producing a hydroprocessed product , comprising:sending to a hydroprocessing zone a combined feed comprised of a heavy hydrocarbon oil component, wherein the heavy hydrocarbon oil component has a ASTM D86 10% distillation point of at least 650° F. (343° C.), and a solvent component containing at least one single ring aromatic compound in which the solvent has an ASTM D86 10% distillation point of at least 120° C. (248° F.) and a 90% distillation point of not greater than 300° C. (572° F.); andcontacting the combined feed with a hydroprocessing catalyst in the presence of hydrogen in the hydroprocessing zone to form a hydroprocessed product.2. The process of claim 1 , wherein the heavy hydrocarbon oil component has an initial ASTM D86 boiling point of at least 650° F. (343° C.).3. The process of claim 1 , wherein the heavy hydrocarbon oil component has an ASTM D86 10% distillation point of at least 750° F. (399° C.).4. The process of claim 1 , wherein the heavy hydrocarbon oil component contains at least 0.0001 grams of Ni/V/Fe claim 1 , on a total elemental basis of nickel claim 1 , vanadium and iron.5. The process of claim 1 , wherein the heavy hydrocarbon oil component contains at least 50 wppm elemental nitrogen claim 1 , based on total weight of the heavy hydrocarbon oil component.6. The process of claim 5 , wherein the heavy hydrocarbon oil component contains at least 500 wppm elemental sulfur claim 5 , based on total ...

INTEGRATED THERMAL PROCESS FOR HEAVY OIL AND GAS TO LIQUIDS CONVERSION

The present disclosure generally relates to upgrading difficult to process heavy-oil. In particular, the disclosure relates to upgrading heavy oil and other high carbon content materials by using an integrated thermal-process (ITP) that utilizes anti-coking management and toluene insoluble organic residues (TIOR) management to directly incorporate lighter hydrocarbons into high molecular weight, low hydrogen content hydrocarbons such as thermally processed heavy oil products. This process can be integrated with other thermal processing schemes, such as cokers and visbreakers, to improve the conversion and yields from these integrated processes. 1331-. (canceled)332. A reactor unit for upgrading a hydrocarbon-feedstock , the reactor unit comprising:i) a first end;ii) a second end;iii) a sidewall that defines a plenum between the first end and the second end;iv) an anti-coking additive inlet that is configured to introduce an anti-coking additive into the plenum;v) a feedstock inlet that is configured to introduce a low hydrogen-content hydrocarbon feedstock into the plenum proximal the first end;vi) a first gas-inlet that is configured to introduce a high hydrogen-content light hydrocarbon gas mixture having an average molecular weight of at least 5 into the plenum at an inlet temperature of at least about 800° F.; andvii) a first outlet that is configured to remove a mixed effluent from the plenum proximal the second end.333. The reactor unit of claim 332 , wherein the high hydrogen-content light hydrocarbon gas mixture has an average molecular weight of at least 8.334. The reactor unit of claim 332 , wherein the high hydrogen-content light hydrocarbon gas mixture has an average molecular weight of at least 15.335. The reactor unit of claim 332 , wherein the first gas-inlet has a nozzle exit velocity of at least 200 ft/second.336. The reactor unit of claim 335 , wherein the first gas-inlet has a nozzle exit velocity of between 300 and 500 ft/second.337. The reactor ...

SYSTEMS AND METHODS FOR HOLISTIC LOW CARBON INTENSITY FUEL PRODUCTION

Systems and methods to provide low carbon intensity (CI) transportation fuels through one or more targeted reductions of carbon emissions based upon an analysis of carbon emissions associated with a combination of various options for feedstock procurement, feedstock refining, processing, or transformation, and fuel product distribution pathways to end users. Such options are selected to maintain the total CI (carbon emissions per unit energy) of the transportation fuel below a pre-selected threshold that defines an upper limit of CI for the transportation fuel. 1. A process to provide a low carbon intensity (CI) transportation fuel obtained through one or more targeted reductions of carbon emissions associated with a combination of various feedstock procurement , feedstock transportation , feedstock refining and fuel product distribution pathways , the process comprising:selecting a carbon intensity threshold to define an upper limit for carbon intensity of a transportation fuel to be provided to an end user location that qualifies the transportation fuel as a low carbon intensity transportation fuel;selecting a refinery feedstock that is procured at a source for transport, the refinery feedstock being selected to reduce carbon emissions associated therewith and thereby maintain the carbon intensity of the transportation fuel below the carbon intensity threshold;selecting a transportation mode to transport the refinery feedstock from the source to a refinery, the transportation mode being selected to reduce carbon emissions associated therewith and thereby maintain the carbon intensity of the transportation fuel below the carbon intensity threshold;selecting refinery processes to reduce carbon emissions associated with refining the refinery feedstock to a plurality of refined products and thereby maintain the carbon intensity of the transportation fuel below the carbon intensity threshold;refining the refinery feedstock into one or more of the plurality of refined ...

Method for On-line Imaging of Mesophase Particles

On-line detection of mesophase particles employs a laser diode light source to illuminate a target area with a pulsed laser linearly or circularly polarized probe beam. Analysis of images determines extent of presence the birefringent mesophase particles, which are precursors to coking in catalytic hydrocracking processes. The inherently polarized low-coherence, unfocused but sufficiently collimated, pulsed laser beam yield sharp imaging with high depth of field of very small mesophase particles that are present in a moving, dark reactor liquid environment. 1. An on-line method for detection of mesophase particles formed in a hydrocarbon conversion reactor that comprises the steps of:(a) establishing a continuous reactor fluid stream containing mesophase particles;(b) employing a laser diode light source to illuminate a target area of the reactor fluid stream with a pulsed laser probe beam along a first beam path that comprises linearly polarized light or circularly polarized light such that an output beam emerges from the target area along a second beam path;(c) obtaining an image of the mesophase particles in the continuous reactor fluid stream; and(d) analyzing the image to determine at least one of (i) volume fraction or (ii) size distribution of mesophase particles in the continuous reactor fluid stream.2. The method of wherein the laser diode light source generates a pulsed laser probe beam without employing a polarizer filter.3. The method of wherein the probe beam is reflected from the target area to form the output beam.4. The method of wherein the probe beam is transmitted through the target area to form the output beam.5. The method of wherein the laser diode light source comprises a plurality of laser bars wherein each laser bar comprises one or more laser diodes and wherein the laser bars each emit a laser beam that is multiplexed to form the pulsed laser probe beam.6. The method of wherein each laser bar emits light of a different wavelength.7. The ...

CRYSTALLINE TRANSITION METAL TUNGSTATE PROCESS DATA SYSTEM

A hydroprocessing catalyst has been developed. The catalyst is a crystalline transition metal tungstate material or metal sulfides derived therefrom, or both. The hydroprocessing using the crystalline transition metal tungstate material may include hydrodenitrification, hydrodesulfurization, hydrodemetallation, hydrodesilication, hydrodearomatization, hydroisomerization, hydrotreating, hydrofining, and hydrocracking. A data system comprising at least one processor; at least one memory storing computer-executable instructions; and at least one receiver configured to receive data of at least one unit or stream in fluid communication with and downstream from or upstream to a conversion process comprising at least one reaction catalyzed by the catalyst or a metal sulfide decomposition product of the catalyst has been developed. 2. The system of further comprising an Input/Output device to collect the data claim 1 , or evaluate the date claim 1 , or correlate the data claim 1 , or any combination thereof.3. The system of further comprising a transmitter to transmit a signal to the conversion process.4. The system of wherein the signal comprises instructions.5. The system of wherein the signal comprises instructions regarding an adjustment to a parameter.6. The system of further comprising collecting data from multiple systems wherein one system is the parameter data system.7. The system of wherein the processor is configured to generate predictive information or quantitative information.8. The system of wherein the at least one unit or stream is not in direct fluid communication with the conversion process10. The method of further comprising at least one of displaying or transmitting or analyzing the received data.11. The method of further comprising analyzing the received data to generate at least one instruction and transmitting the at least one instruction.12. The method of further comprising analyzing the received data and generating predictive information or ...

TWO-STAGE HYDROCRACKING PROCESS COMPRISING A HYDROGENATION STAGE DOWNSTREAM OF THE SECOND HYDROCRACKING STAGE, FOR THE PRODUCTION OF MIDDLE DISTILLATES

The invention relates to the implementation of a multi-stage hydrocracking process comprising a hydrogenation stage located downstream of the second hydrocracking stage, said hydrogenation stage treating the effluent produced in the second hydrocracking stage, in the presence of a specific hydrogenation catalyst. In addition, the hydrogenation and second hydrocracking stages are implemented under specific operating conditions and particularly under very specific temperature conditions. 1. Process for producing middle distillates from hydrocarbon feedstocks containing at least 20% by volume of compounds boiling above 340° C. , said process comprising the following steps:{'sup': '−1', 'a) a step of hydrotreating said feedstocks in the presence of hydrogen and at least one hydrotreating catalyst, at a temperature of between 200° C. and 450° C., under a pressure of between 2 and 25 MPa, at a space velocity of between 0.1 and 6 hand with an amount of hydrogen introduced such that the litre of hydrogen/litre of hydrocarbon volume ratio is between 100 and 2000 Nl/l,'}{'sup': '−1', 'b) a step of hydrocracking at least one portion of the effluent resulting from step a), the hydrocracking step b) taking place, in the presence of hydrogen and at least one hydrocracking catalyst, at a temperature of between 250° C. and 480° C., under a pressure of between 2 and 25 MPa, at a space velocity of between 0.1 and 6 hand with an amount of hydrogen introduced such that the litre of hydrogen/litre of hydrocarbon volume ratio is between 80 and 2000 Nl/l,'}c) a step of high-pressure separation of the effluent resulting from the hydrocracking step b) to produce at least a gaseous effluent and a liquid hydrocarbon effluent, a gaseous fraction,', 'at least one petroleum fraction having at least 80% by volume of products boiling at a temperature below 150° C.,', 'at least one middle distillates fraction having at least 80% by volume of products having a boiling point between 150° C. and 380° ...

HYDROCRACKING CATALYST COMPRISING A BETA ZEOLITE (*BEA) FRAMEWORK SUBSTITUTED WITH Ti AND Zr AND METHODS FOR ITS PREPARATION AND USE

The invention relates to methods for hydrocracking or hydrotreating hydrocarbon containing feedstocks. This is accomplished via the use of a catalyst which comprises a β zeolite of *BEA framework, where a portion of aluminum atoms in the *BEA framework have been substituted by from 0.1-5.0 wt % of each of Ti and Zr, calculated on an oxide basis. 1. A method for hydrocracking or hydrotreating a hydrocarbon containing feedstock , comprising contacting said feedstock with (i) a catalyst , said catalyst comprising an active phase metal and a β zeolite of *BEA framework , wherein a portion of aluminum atoms in said *BEA framework have been substituted by from 0.1 to 5.0 wt % of Ti atoms and from 0.1 to 5.0 wt % Zr atoms , said wt % being calculated on an oxide basis , and (ii) hydrogen , to hydrocrack or hydrotreat said feedstock.2. The method of claim 1 , wherein said catalyst further comprises from 0.1 to 5.0 wt % of Hf atoms calculated in an oxide basis.3. The method of claim 1 , wherein said catalyst wherein said β zeolite has the following characteristics:(a) a crystal lattice constant of a=1,260 to 1.270 nm, b=1.260 to 1,270 nm, and c=2.6200 to 2.6500 nm.{'sup': '2', '(b) a specific surface area of 400 to 800 m/g, and'}{'sub': 2', '3, '(c) a molar ratio of SiOto Al2Oof 10 to 200.'}4. The method of claim 1 , wherein said zeolite containing catalyst support has a specific surface area of 15 to 500 m/g; a volume of pores having a diameter of 600 A or in the range of 0.40 to 0.75 ml/g; and an amount of an active phase metal component ranging from 0.01 to 40 mass %.5. The method of claim 1 , further comprising:filling a reactor vessel which is a flow reactor with the hydrocracking catalyst; and{'sup': −1', '3', '3, 'treating a feedstock having a boiling point of 300° C., to 833° C. in the presence of hydrogen at a reactor temperature of 300° C. to 450° C., a hydrogen pressure of 4 to 30 MPa, a liquid hourly space velocity (LHSV) of 0.1 to 10 h, and a hydrogen/oil ratio ...

ENERGY-RECOVERY TURBINES FOR GAS STREAMS

Processes for controlling the flowrate of and recovering energy from a gas stream in a processing unit are described. One process comprises directing a portion of the gas stream through one or more variable-resistance power-recovery turbines to control the flowrate of the gas stream and generate electric power therefrom; and controlling the pressure and temperature of the gas stream so that the gas exiting the power-recovery turbine remains in the gas phase. 1. A process for controlling a flowrate of and recovering energy from a gas stream in a processing unit comprising:directing at least a portion of the gas stream through one or more variable-resistance power-recovery turbine to control the flowrate of the gas stream and generate electric power therefrom;controlling a pressure and temperature of the gas stream through the one or more power-recovery turbines so that the gas exiting the one or more power-recovery turbine remains in a gas phase; andmeasuring the flowrate using turbine revolutions per minute of the one or more power-recovery turbine and a load on a circuit.2. The process of further comprising controlling the flowrate by varying one or more of the speed or shaft torque of the one or more power-recovery turbine.3. The process of further comprising replacing a control valve with the one or more power-recovery turbine before directing the at least the portion of the gas stream through the one or more power-recovery turbine.4. The process of wherein the one or more power-recovery turbine is used in conjunction with a control valve claim 1 , and further comprising directing a second portion of the gas stream through the control valve.5. The process of wherein the portion of the gas stream directed through the one or more power-recovery turbine is greater than the second portion of the gas stream directed though the control valve.6. The process of wherein the power recovered is displayed on at least one display screen.7. The process of further comprising: ...

PROCESS FOR PRODUCING A NAPHTHA STREAM

Process and apparatus for producing a naphtha stream is provided. The process comprises providing a kerosene stream to a hydrocracking reactor. The kerosene stream is hydrocracked in the presence of a hydrogen stream and a hydrocracking catalyst in the hydrocracking reactor at hydrocracking conditions comprising a hydrocracking pressure, a hydrocracking temperature, and a liquid hourly space velocity at a net conversion of at least about 90%, to provide a hydrocracked effluent stream comprising liquefied petroleum gas, heavy naphtha fraction and light naphtha fraction. One or more of the hydrocracking conditions are adjusted to maintain a ratio of the light naphtha fraction to the heavy naphtha fraction of at least about 2 by weight, suitably at least about 2.2 and preferably at least about 2.5 in the hydrocracked effluent stream while maintaining the net conversion of at least about 90%. 1. A process for producing a naphtha stream comprising:a) providing a kerosene stream to a hydrocracking reactor;b) hydrocracking the kerosene stream in the presence of a hydrogen stream and a hydrocracking catalyst in the hydrocracking reactor at hydrocracking conditions comprising a hydrocracking pressure, a hydrocracking temperature, and a liquid hourly space velocity (LHSV) at a net conversion of at least about 90%, to provide a hydrocracked effluent stream comprising liquefied petroleum gas (LPG), heavy naphtha fraction and light naphtha fraction;c) adjusting one or more of the hydrocracking conditions to maintain a ratio of the light naphtha fraction to the heavy naphtha fraction of at least about 2 by weight in the hydrocracked effluent stream while maintaining the net conversion of at least about 90%; andd) obtaining a naphtha stream comprising the ratio of the light naphtha fraction to the heavy naphtha fraction of at least about 2 by weight from the hydrocracking effluent stream.2. The process of further comprising:a) splitting at least a portion of the naphtha stream in ...

HEAVY AROMATIC SOLVENTS FOR CATALYST REACTIVATION

Compositions and methods for restoring catalytic activity by dissolving soft coke with a solvent, one method including detecting soft coke deposition on a catalyst composition; preparing an aromatic bottoms composition with a Hildebrand solubility parameter of at least about 20 SI to remove the soft coke from the catalyst composition; and washing the catalyst composition with the aromatic bottoms composition until at least a portion of the soft coke deposition is removed. 1. A method for restoring catalytic activity by dissolving soft coke with a solvent , the method comprising the steps of:detecting soft coke deposition on a catalyst composition;preparing an aromatic bottoms composition with a Hildebrand solubility parameter of at least about 20 (SI) to remove the soft coke from the catalyst composition; andwashing the catalyst composition with the aromatic bottoms composition until at least a portion of the soft coke deposition is removed.2. The method according to claim 1 , where the step of detecting soft coke deposition on the catalyst composition comprises detecting a pressure drop increase over a catalyst bed comprising the catalyst composition of at least about 1 bar.3. The method according to claim 1 , where the step of detecting soft coke deposition on the catalyst composition comprises detecting a radial temperature profile change in a reactor of at least about 1° C.4. The method according to claim 1 , where the aromatic bottoms composition comprises aromatic bottoms from an aromatic recovery complex.5. The method according to claim 1 , where the aromatic bottoms composition comprises aromatic bottoms from a xylene rerun column of an aromatic recovery complex.6. The method according to claim 1 , where the aromatic bottoms composition consists essentially of aromatic bottoms from a xylene rerun column of an aromatic recovery complex.7. The method according to claim 1 , where the aromatic bottoms composition consists of aromatic bottoms from a xylene rerun ...

Method for On-line Imaging of Mesophase Particles

On-line detection of mesophase particles employs a laser diode light source to illuminate a target area with a pulsed laser linearly or circularly polarized probe beam. Analysis of images determines extent of presence the birefringent mesophase particles, which are precursors to coking in catalytic hydrocracking processes. The inherently polarized low-coherence, unfocused but sufficiently collimated, pulsed laser beam yield sharp imaging with high depth of field of very small mesophase particles that are present in a moving, dark reactor liquid environment. 1. A method of converting a heavy hydrocarbon feed into light hydrocarbon products comprising the steps of:(a) mixing a heavy hydrocarbons liquid feed with catalyst particles to form a slurry;(b) hydrocracking heavy hydrocarbons in the slurry in the presence of hydrogen in a reactor to produce a hydrocracked slurry product comprising lighter hydrocarbon products wherein the slurry product is withdrawn from the reactor;(c) monitoring mesophase particles in the reactor by (i) directing a pulsed laser probe beam from a laser diode light source along a first beam path into a continuous reactor fluid stream wherein the probe beam comprises linearly polarized light such that an output beam emerges from the continuous reactor fluid stream along a second beam path, (ii) obtaining an image of the mesophase particles in the continuous reactor fluid stream, and (iii) analyzing the image to determine at least one of volume fraction or size distribution of mesophase particles in the continuous reactor fluid stream; and(d) adjusting reactor conditions to reduce levels of mesophase particles formed during hydrocracking.2. The method of wherein the laser diode light source generates a pulsed laser probe beam without employing a polarizer filter.3. (canceled)4. A method of converting a heavy hydrocarbon feed into light hydrocarbon products comprising the steps of:(a) mixing a heavy hydrocarbons liquid feed with catalyst particles ...

Abnormal temperature detection for fixed bed reactors

Systems and methods are provided for detecting abnormal temperature conditions within a fixed bed reactor. In a fixed bed reactor, a hydrocarbon (or hydrocarbon-like) feedstock can be exposed to one or more types of catalyst particles at elevated temperatures and/or pressures. In addition to the one or more types of catalyst particles, a plurality of temperature-sensor structures can be included in a catalyst bed and/or a coating including one or more temperature-sensor structures can be provided on an interior wall or other interior surface in the reactor. The temperature-sensor structures can have a threshold temperature at which the temperature-sensor structure changes to allow introduction and/or release of a detectable substance.

System and Method for Controlling and Optimizing the Hydrothermal Upgrading of Heavy Crude Oil and Bitumen

A system and method is provided for upgrading a continuously flowing process stream including heavy crude oil (HCO). A reactor receives the process stream in combination with water, at an inlet temperature within a range of about 60° C. to about 200° C. The reactor includes one or more process flow tubes having a combined length of about 30 times their aggregated transverse cross-sectional dimension, and progressively heats the process stream to an outlet temperature T(max) within a range of between about 260° C. to about 400° C. The reactor maintains the process stream at a pressure sufficient to ensure that it remains a single phase at T(max) A controller selectively adjusts the rate of flow of the process stream through the reactor to maintain a total residence time of greater than about 1 minute and less than about 25 minutes. 1. A system for upgrading a continuously flowing process stream including heavy crude oil (HCO) , comprising:a fluid flow path configured to convey the process stream continuously therethrough in a downstream direction, the flow path including a reactor;the reactor configured to receive the process stream in combination with water, at an inlet temperature within a range of about 60° C. to about 200° C.;the reactor including one or more process flow tubes defining an aggregated interior cross-sectional dimension in a plane extending transversely to the downstream direction therethrough, the one or more flow tubes having a combined length of at least about 30 times the aggregated interior cross-sectional dimension;the reactor configured to apply heat to the process stream flowing therethrough, to progressively heat the process stream from the inlet temperature at an upstream portion of the reactor, to an outlet temperature T(max)1 within a range of between about 260° C. to about 400° C. at a downstream portion of the reactor;{'b': '1', 'the reactor configured to maintain the process stream at a pressure sufficient to ensure that the process ...

CATALYST AND PROCESS OF UPGRADING HEAVY OIL IN THE PRESENCE OF STEAM

Embodiments of the disclosure provide an aqueous reforming system and a method for upgrading heavy hydrocarbons. A hydrocarbon feed and a surfactant stream are combined to produce a first precursor stream. The first precursor stream and an alkali feed are combined to produce a second precursor stream. The second precursor stream and a transition metal feed are combined to produce a catalytic emulsion stream. The catalytic emulsion stream is heated to produce a catalytic suspension and a decomposition gas, where the decomposition gas is separated by a first separator. The catalytic suspension is combined with a preheated water stream to produce an aqueous reformer feed. The aqueous reformer feed is introduced to an aqueous reformer such that the heavy hydrocarbons undergo conversion reactions to produce an effluent stream. The effluent stream is introduced to a second separator to produce a heavy stream and a light stream. The light stream is introduced to a third separator to produce a gas stream, a distillate stream, and a spent water stream. Optionally, a portion of the distillate stream and the hydrocarbon feed can be combined to produce the first precursor stream such that the first precursor stream is in the absence of a surfactant. 1. A method for upgrading heavy hydrocarbons , the method comprising the steps of:combining a hydrocarbon feed and a surfactant stream to produce a first precursor stream, wherein the hydrocarbon feed comprises the heavy hydrocarbons, wherein the surfactant stream comprises a surfactant;combining the first precursor stream and an alkali feed to produce a second precursor stream, wherein the alkali feed comprises an alkali metal and water;combining the second precursor stream and a transition metal feed to produce a catalytic emulsion stream, wherein the transition metal feed comprises a transition metal and water, wherein the catalytic emulsion stream includes an emulsion comprising the heavy hydrocarbons, the alkali metal, the ...

HYDROCRACKING PROCESSES

A process for controlling hydrocracking reactions in a hydrocracking reactor by passing aqueous ammonia to the hydrocracking reactor. The aqueous ammonia is injected into the process at various locations at a low pressure, typically between approximately 0.17 to approximately 2.07 MPa (25 to 300 psi). A wash fluid can be used to lower the concentration of ammonia in the hydrocracking reactor, and thus, increase the catalytic activity of the hydrocracking catalyst. 1. A process for controlling an activity of a hydrocracking catalyst in a hydrocracking reaction zone , the process comprising:passing an aqueous ammonia stream into a hydrocracking reaction zone having an acidic hydrocracking catalyst, wherein a pressure of the aqueous ammonia stream when injected is between approximately 0.17 to approximately 2.07 MPa (25 to 300 psi).2. The process of claim 1 , wherein the aqueous ammonia stream is mixed with a feed stream to form a combined stream claim 1 , wherein the combined stream is passed into the hydrocracking reaction zone.3. The process of wherein a pressure of the aqueous ammonia stream is between approximately 0.34 to approximately 1.7 MPa (50 to 250 psi).4. The process of wherein the aqueous ammonia stream comprises between 15 to 25 wt % of ammonia.5. The process of further comprising:passing a feed stream into the hydrocracking reaction zone; and,operating the hydrocracking reaction zone under hydrocracking conditions.6. The process of further comprising:reducing an ammonia concentration in the hydrocracking reaction zone with a wash fluid.7. The process of further comprising:monitoring for ammonia in an effleunt from the hydrocracking reaction zone; and,reducing an amount of the ammonia passed to the hydrocracking reaction zone upon a detection of ammonia in the effluent.8. The process of further comprising:increasing a temperature in the hydrocracking reaction zone after the amount of ammonia passed to the hydrocracking reaction zone is reduced.9. The ...

Pyrolysis Tar Conversion

A process is provided for determining the suitability of pyrolysis tar, such as steam cracker tar, for upgrading using hydroprocessing without long term fouling of the hydroprocessing reactor. The process includes heating a sample of the tar, quenching the sample, and measuring the total free radical content of the quenched sample. A pyrolysis tar can be blended with one having a lesser total free radical content to produce a blend that can be hydroprocessed with decreased fouling. 1. A hydrocarbon process , comprising:{'sub': '1', '(a) providing a first pyrolysis tar having a temperature T≤350° C., the pyrolysis tar being a hydrocarbon-containing mixture which includes free radicals and is derived from hydrocarbon pyrolysis, wherein at least 70 wt. % of the mixture has a normal boiling point of at least 290° C.;'}{'sub': 2', 'h', '2', '1, '(b) isolating a sample from the first pyrolysis tar and producing additional free radicals in the sample by exposing the sample to a predetermined second temperature Tfor a predetermined time t, wherein T≥T+10° C.;'}{'sub': 3', '3', '1', 'T, '(c) cooling the sample to a temperature T, Tbeing ≤T, the cooled sample having a total free radical content R;'}{'sub': 'T', 'claim-text': {'sub': T', 'ref, 'claim-text': [{'sub': '1', '(A) providing a second pyrolysis tar at a temperature ≤T, the second pyrolysis tar being a hydrocarbon-containing mixture derived from hydrocarbon pyrolysis, wherein at least 70 wt. % of the mixture has a normal boiling point of at least 290° C., and combining the first pyrolysis tar with a predetermined amount of the second pyrolysis tar to produce a pyrolysis tar composition,'}, {'sub': 2', 'h', '3', 'T, '(B) (I) isolating a sample from the pyrolysis tar composition, (II) producing additional free radicals in the pyrolysis tar composition sample by exposing the pyrolysis tar composition sample to a temperature of at least Tfor time of at least t, and (III) cooling the pyrolysis tar composition sample to a ...

AMMONIATED QUENCHING OF A HYDROPROCESSING REACTION

The disclosure provided herein describes processes for rapidly quenching an over-temperature hydroprocessing reaction utilizing a pressurized quenching agent that is rapidly released into the hydroprocessing reactor. Optimally, the quenching agent blocks acidic catalytic sites of the hydroprocessing catalyst to competitively inhibit exothermic reaction rate. Exemplary quench agents include ammonia or a chemical that is converted to ammonia under hydroprocessing conditions. 1. A process for quenching a catalytic hydroprocessing reaction , comprising:a) contacting a feedstock derived from at least one of petroleum or biomass with a hydroprocessing catalyst comprising at least on acidic catalytic active site in a reaction zone at a temperature and pressure that facilitates hydroprocessing reactions, wherein the contacting converts the feedstock to a reactor effluent comprising a liquid hydrocarbon fuel or a blending component thereof;b) detecting a temperature condition in the reaction zone;c) dispensing a quenching agent from a pressurized vessel to the reaction zone when the temperature condition exceeds a first predetermined threshold temperature, wherein the quenching agent binds to and blocks at least one active site of the hydroprocessing catalyst.2. The process of claim 1 , wherein the first predetermined threshold temperature is at least 473° C. (820° F.)3. The process of claim 1 , wherein the first predetermined threshold temperature is at least 476° C. (825° F.).4. The process of claim 1 , wherein the first predetermined threshold temperature is at least 479° C. (830° F.).5. The process of claim 1 , wherein the first predetermined threshold temperature is at least 482° C. (835° F.).6. The process of claim 1 , wherein the first predetermined threshold temperature is at least 484° C. (840° F.).7. The process of claim 1 , wherein the first predetermined threshold temperature is at least 487° C. (845° F.).8. The process of claim 1 , wherein the first ...

SYSTEMS FOR AMMONIATED QUENCHING OF A HYDROPROCESSING REACTION

The disclosure provided herein describes systems for rapidly quenching an over-temperature hydroprocessing reaction utilizing a pressurized quenching agent that is rapidly released into the hydroprocessing reactor. Optimally, the quenching agent blocks acidic catalytic sites of the hydroprocessing catalyst to competitively inhibit exothermic reaction rate. Exemplary quench agents include ammonia or a chemical that is converted to ammonia under hydroprocessing conditions. 1. A system for quenching a catalytic hydroprocessing reaction , comprising:a) a hydroprocessing reactor comprising a reaction zone and containing a hydroprocessing catalyst comprising at least one acidic catalytic active site, wherein the hydroprocessing reactor is operable to be maintained at a temperature and pressure that facilitates hydroprocessing reactions, wherein the hydroprocessing reactor is further operable to facilitate contact between the acidic catalytic sites of the hydroprocessing catalyst and a feedstock derived from at least one of petroleum or biomass to produce a reactor effluent;b) a vessel operably connected to the hydroprocessing reactor via a conduit comprising a valve, wherein the vessel is operable to contain a quenching agent that is operable to bind the at least one acidic catalytic active site, wherein the valve is operable to release the quenching agent into the conduit and the conduit is operable to convey the quenching agent to the hydroprocessing reactor reaction zone.c) at least one temperature sensor operably connected to the hydroprocessing reactor that is operable to send an electrical signal indicating the temperature condition within the reaction zone;d) a control panel that is operable to receive and interpret the electrical signal from the at least one temperature sensor, and further operable to signal the first valve to operate to release the quenching agent when the electrical signal from the temperature sensor indicates a temperature condition that ...

Hydrocracking process for producing distillate or naptha

The invention relates to a catalytic hydrocracker with two different catalyst beds within the reactor where each is loaded with a catalyst that has different hydrocracking properties. A first catalyst bed preferably cracks heavy oil more aggressively than the catalyst in the second bed. The catalytic hydrocracker includes further two recycle lines such that one directs unconverted oil through both hydrocracker beds and a bypass inlet is positioned between the first and second catalyst beds to admit unconverted oil to pass only through the second less aggressive hydrocracker catalyst bed. When gasoline prices favor the production of gasoline, less unconverted oil is recycled through the bypass therefore making more gasoline, but when prices favor the production of jet and diesel, more recycle is directed through the bypass recycle thus making less gasoline and more diesel and jet fuel.

Hydrocracking system for producing distillate or naptha

The invention relates to a catalytic hydrocracker with two different catalyst beds within the reactor where each is loaded with a catalyst that has different hydrocracking properties. A first catalyst bed preferably cracks heavy oil more aggressively than the catalyst in the second bed. The catalytic hydrocracker includes further two recycle lines such that one directs unconverted oil through both hydrocracker beds and a bypass inlet is positioned between the first and second catalyst beds to admit unconverted oil to pass only through the second less aggressive hydrocracker catalyst bed. When gasoline prices favor the production of gasoline, less unconverted oil is recycled through the bypass therefore making more gasoline, but when prices favor the production of j et and diesel, more recycle is directed through the bypass recycle thus making less gasoline and more diesel and jet fuel.

PROCESS FOR UPGRADATION OF HEAVY CRUDE OIL/RESIDUE USING WASTE PLASTIC AS HYDROGEN DONATING AGENT

Waste plastics are mixed with heavy crude and vacuum residues at temperature within the range from 180-220° C. and the resulting mixture are hydroprocessed to produce lighter products. The hydrodemetallization, asphaltene conversion and hydrocracking activities of the resulting mixture have been tested in an autoclave batch reactor. This process provides a very cheap material and method to upgrade problematic feeds to produce transportation fuels. 1. A for upgradation of heavy crude oil and residues comprising the steps of:a) mixing of heavy crude/residue with waste plastic in the range of 1:1 to 4:1 ratio and taken into a reactor vessel,b) preheating the mixture obtained in step (a) at a temperature in the range of 130-220° C. for a period in the range of 20-30 minutes,{'sup': '2', 'c) further heating the mixture obtained in step (b) for hydrocracking reactions at a temperature in the range of 350-450° C. and pressure in the range of 40-100 kg/cmfor a period of 30-90 minutes with stirring in the presence of hydrogen in a reactor and separated the desired products.'}2. The process as claimed in claim 1 , comprising high conversion of hydrodemetallization (97 wt %) and high conversions of hydrocracking (84 wt %) with vacuum residue (VR-I).3. The process as claimed in claim 1 , wherein the heavy contaminant crude employed as feedstock comprising high metals content >100 wppm; high microcarbon residue content >3 wt %; and containing 550° C. plus material not less than 20 wt %.4. The process as claimed in claim 1 , wherein the vacuum residue employed as feedstock comprising high metals content >150 wppm; high microcarbon residue content in the range 5-25 wt %; and containing 550° C. plus material not less than 60 wt %.5. The process as claimed in claim 1 , wherein the ratio of crude oil/residue and plastic ranges from 1:1 to 4:1.6. The process as claimed in claim 1 , wherein the plastic used in the process is selected from plastic used for packaging purposes.7. The ...

ABNORMAL TEMPERATURE DETECTION FOR FIXED BED REACTORS

Systems and methods are provided for detecting abnormal temperature conditions within a fixed bed reactor. In a fixed bed reactor, a hydrocarbon (or hydrocarbon-like) feedstock can be exposed to one or more types of catalyst particles at elevated temperatures and/or pressures. In addition to the one or more types of catalyst particles, a plurality of temperature-sensor structures can be included in a catalyst bed and/or a coating including one or more temperature-sensor structures can be provided on an interior wall or other interior surface in the reactor. The temperature-sensor structures can have a threshold temperature at which the temperature-sensor structure changes to allow introduction and/or release of a detectable substance. 1. A fixed bed processing system , comprising:a reactor vessel having a reactor inlet and a reactor outlet;at least one fixed bed of catalyst particles within the reactor vessel;one or more temperature-sensor structures within the reactor vessel;a detector in fluid communication with the reactor outlet,wherein the one or more temperature-sensor structures are composed of a material that undergoes a structural change at a threshold temperature, andwherein the one or more temperature-sensor structures have a first rate of introducing a detectable substance into the reactor at a temperature below the threshold temperature and a second rate of introducing the detectable substance at a temperature above the threshold temperature, the second introduction rate being at least about 5 times the first introduction rate.2. The system of claim 1 , wherein the one or more temperature-sensor structures comprise temperature-sensor particles.3. The system of claim 1 , wherein the one or more temperature-sensor structures are distributed randomly within the catalyst bed.4. The system of claim 3 , wherein the temperature-sensor particles further comprise a catalyst.5. The system of claim 1 , wherein the one or more temperature-sensor structures are ...

UPGRADED EBULLATED BED REACTOR WITH LESS FOULING SEDIMENT

An ebullated bed hydroprocessing system is upgraded using a dual catalyst system that includes a heterogeneous catalyst and dispersed metal sulfide particles to produce less fouling sediment. The dual catalyst system more effectively converts sediment-forming precursors to produce sediment that is less fouling than sediment produced using only the heterogeneous catalyst and not the dispersed metal sulfide particles. The dual catalyst system provides for a lower rate of equipment fouling for a given sediment production rate and/or concentration. In some cases, sediment production rate and/or concentration can be maintained or increased while equipment fouling is reduced. In some cases, sediment production rate and/or concentration can be increased without increasing equipment fouling. 1. A method of upgrading an ebullated bed hydroprocessing system that includes one or more ebullated bed reactors to produce less fouling sediment , comprising:operating an ebullated bed reactor using a heterogeneous catalyst to hydroprocess heavy oil at initial conditions, including an initial sediment production rate and/or initial sediment concentration in a process stream and an initial rate of equipment fouling;thereafter upgrading the ebullated bed reactor to operate using a dual catalyst system comprised of dispersed metal sulfide catalyst particles and heterogeneous catalyst; andoperating the upgraded ebullated bed reactor using the dual catalyst system to produce less fouling sediment, resulting in less equipment fouling at a given sediment production rate and/or concentration compared to when operating the ebullated bed reactor at the initial conditions.2. The method of claim 1 , wherein operating the upgraded ebullated bed reactor using the dual catalyst system to produce less fouling sediment comprises:producing converted products at a same or similar rate as an initial production rate of converted products when operating at the initial conditions;producing sediment at a ...

A temperature-controlling measure for the hydrogenation slurry bed reactor and its design method and use

A temperature-controlling measure for a hydrogenation slurry bed reactor has three control points that are set from low to high: cold hydrogen is injected automatically when the system reaches control point 1; cold oil is injected automatically when the system reaches control point 2; each pressure relief is opened automatically when the system reaches control point 3. The pressure relief point is set before and/or after the circulation pump of the reactor if internal circulation is set in the reactor; the pressure relief point is set at the reactor bottom if the internal circulation is not set; at least one pressure relief valve is set at each pressure relief point. 1. A temperature-controlling measure of a hydrogenation slurry bed reactor , characterized in that:three control points are set in turn from low to high: cold hydrogen is injected automatically when the reaction system reaches control point 1; cold oil is injected automatically when the system reaches control point 2; each pressure relief point is opened automatically when the system reaches control point 3;the control point 1 is: 425° C.≤T<440° C. and/or P≥19 MPa; the control point 2 is: 440° C.≤T<455° C. and/or P≥19 MPa; the control point 3 is: T≥455° C. and/or P≥20 MPa;the pressure relief point is set before and/or after the circulation pump of the reactor if internal circulation is set in the reactor; the pressure relief point is set at the bottom of the reactor if the internal circulation is not set in the reactor; at least one pressure relief valve is set at each pressure relief point.2. The temperature-controlling measure according to claim 1 , wherein the hydrogenation reactors are used in series claim 1 , the number of series is 2-4 claim 1 , and the number of reactors with pressure relief points is more than 1.3. An temperature-controlling measure according to claim 1 , wherein the pressure relief valve is controlled by the temperature or pressure in the reactor claim 1 , the number of ...

CATALYST AND PROCESS OF UPGRADING HEAVY OIL IN THE PRESENCE OF STEAM

Embodiments of the disclosure provide an aqueous reforming system and a method for upgrading heavy hydrocarbons. A hydrocarbon feed and a surfactant stream are combined to produce a first precursor stream. The first precursor stream and an alkali feed are combined to produce a second precursor stream. The second precursor stream and a transition metal feed are combined to produce a catalytic emulsion stream. The catalytic emulsion stream is heated to produce a catalytic suspension and a decomposition gas, where the decomposition gas is separated by a first separator. The catalytic suspension is combined with a preheated water stream to produce an aqueous reformer feed. The aqueous reformer feed is introduced to an aqueous reformer such that the heavy hydrocarbons undergo conversion reactions to produce an effluent stream. The effluent stream is introduced to a second separator to produce a heavy stream and a light stream. The light stream is introduced to a third separator to produce a gas stream, a distillate stream, and a spent water stream. Optionally, a portion of the distillate stream and the hydrocarbon feed can be combined to produce the first precursor stream such that the first precursor stream is in the absence of a surfactant. 1. An aqueous reforming system for upgrading heavy hydrocarbons , the aqueous reforming system comprising:a first mixer, the first mixer configured to combine a hydrocarbon feed and a surfactant stream to produce a first precursor stream, wherein the hydrocarbon feed comprises the heavy hydrocarbons, wherein the surfactant stream comprises a surfactant;a second mixer, the second mixer fluidly connected downstream of the first mixer, the second mixer configured to combine the first precursor stream and an alkali feed to produce a second precursor stream, wherein the alkali feed comprises an alkali metal and water;a third mixer, the third mixer fluidly connected downstream of the second mixer, the third mixer configured to combine the ...

Strain gauges and detecting pre-leakage in heat exchangers in a petrochemical plant or refinery

A plant or refinery may include equipment such as reactors, heaters, heat exchangers, regenerators, separators, or the like. Types of heat exchangers include shell and tube, plate, plate and shell, plate fin, air cooled, wetted-surface air cooled, or the like. Operating methods may impact deterioration in equipment condition, prolong equipment life, extend production operating time, or provide other benefits. Mechanical or digital sensors may be used for monitoring equipment, and sensor data may be programmatically analyzed to identify developing problems. For example, sensors may be used in conjunction with one or more system components to detect and correct maldistribution, cross-leakage, strain, pre-leakage, thermal stresses, fouling, vibration, problems in liquid lifting, conditions that can affect air-cooled exchangers, conditions that can affect a wetted-surface air-cooled heat exchanger, or the like. An operating condition or mode may be adjusted to prolong equipment life or avoid equipment failure.

POWER RECOVERY FROM QUENCH AND DILUTION VAPOR STREAMS

A process for reducing pressure of a vapor stream used for reducing a temperature or pressure in a reactor. A pressure of a vapor stream is reduced with a turbine to provide a lower pressure vapor stream. The vapor stream rotates a turbine wheel within the turbine. The turbine wheel is configured to transmit rotational movement to an electrical generator. Thus, electricity is generated with the turbine. The lower pressure vapor stream is injected into a reactor and reduces a temperature in the reactor or reduces a partial pressure of a hydrocarbon vapor in the reactor. 1. A process for reducing pressure of a vapor stream used for reducing a temperature , heat load , or hydrocarbon partial pressure in a reactor , the process comprising:reducing a pressure of a vapor stream with a turbine to provide a lower pressure vapor stream;rotating a turbine wheel within the turbine,injecting the lower pressure vapor stream into a reactor and reducing a temperature in the reactor or reducing a partial pressure of a hydrocarbon vapor in the reactor.2. The process of further comprising increasing the feed rate to the reactor by relaxing a high temperature bottleneck by extracting energy from the vapor stream.3. The process of wherein the turbine wheel is configured to transmit rotational movement to an electrical generator claim 1 , and the process further comprising:generating electricity with the turbine.4. The process of further comprising:receiving information from the turbine relative to an amount of electricity generated by the turbine; and,displaying the amount of electricity generated by the turbine on at least one display screen.5. The process of further comprising:maintaining a throughput of the reactor while adjusting at least one process parameter of the reactor.6. The process of claim 4 , wherein the reactor comprises a plurality of turbines each configured to generate electricity claim 4 , and wherein the process comprises:determining a total power generated based ...

Hydrocarbon Upgrading

Aspects of the invention provide a process for upgrading a hydrocarbon feed. The process includes providing a hydrocarbon feed and a utility fluid. Then selectively extracting from the feed at least a portion of particulates to produce a raffinate and an extract. Third hydroprocessing at least a portion of the raffinate. 119-. (canceled)21. The upgrading system of claim 20 , wherein the separation system comprises a backwashing filtration system for providing the extract and the raffinate.22. The upgrading system of claim 20 , wherein the separation system comprises a sedimentation unit for providing the extract and the raffinate.23. The upgrading system of claim 20 , further comprising a solids separation unit configured to receive the extract and to separate a liquid portion therefrom.24. The upgrading system of claim 20 , further comprising (A) means for withdrawing a hydroprocessed effluent from the hydroprocessor and (B) a first separation unit configured to (i) receive the withdrawn hydroprocessed effluent and (ii) separate from the hydroprocessed effluent a first fluid-enriched stream and a hydroprocessed product stream.25. The upgrading system of claim 24 , further comprising a second separation unit claim 24 , preferably a stabilizer claim 24 , to provide an overhead stream claim 24 , configured to receive the hydroprocessed product stream and to separate from the hydroprocessed product stream a second fluid-enriched stream and a product stream. This application claims priority to and the benefit of U.S. Provisional Application Ser. No. 62/011,965, filed Jun. 13, 2014 and EP 14181262.8 filed Aug. 18, 2014, the entireties are incorporated herein by reference. The present application relates to U.S. Provisional Application No. 62/011,959 filed Jun. 13, 2014 which is incorporated by reference in its entirety.The invention relates to upgrading hydrocarbons for improved blending characteristics, to processes for producing such upgraded hydrocarbons, to ...

SERVER, METHOD, AND PROGRAM FOR SUPPLYING DESULFURIZATION CATALYST-RELATED INFORMATION, AND COMPUTER-READABLE RECORDING MEDIUM RECORDING SAME

A server is configured to be connected to a user terminal via a network, and to supply a desulfurization catalyst lifetime of a user plant to a user based on desulfurization catalyst pilot plant data and a desulfurization catalyst lifetime function. The server includes a processor and a memory storing computer-readable instructions. When the computer-readable instructions are executed by the processor, the server receives user plant-related data and a user desulfurization catalyst performance prediction condition from the user terminal to the user plant based on a comparison between the desulfurization catalyst pilot plant data and the obtained user plant-related data, calculates a catalyst lifetime for the user's desulfurization catalyst based on the obtained user desulfurization catalyst performance prediction condition and the user desulfurization catalyst lifetime function, and transmits the calculated catalyst lifetime to the user terminal. 1. A server to be connected to a user terminal via a network to supply a desulfurization catalyst lifetime of a user plant to a user based on desulfurization catalyst pilot plant data and a desulfurization catalyst lifetime function , the server comprising:a processor and a memory storing computer-readable instructions,wherein, when the computer-readable instructions are executed by the processor, the serverreceives user plant-related data and a user desulfurization catalyst performance prediction condition from the user terminal,generates from the desulfurization catalyst lifetime function a user desulfurization catalyst lifetime function tailored to the user plant based on a comparison between the desulfurization catalyst pilot plant data and the received user plant-related data,calculates a catalyst lifetime for a user desulfurization catalyst based on the received user desulfurization catalyst performance prediction condition and the user desulfurization catalyst lifetime function, andtransmits the calculated catalyst ...

Catalyst Cycle Length Prediction Using Eigen Analysis

Systems and methods are disclosed for managing the operation of a plant, such as a chemical plant or a petrochemical plant or a refinery, and more particularly for enhancing system performance of a catalyzed reaction system by, among other features, detecting catalyst deactivation and cycle length. Plants may include those that provide hydrocarbon cracking or other process units. A plant may include a reactor, a heater, a catalyst bed, a separator, and other equipment. The equipment may use catalyst to treat feed products to remove compounds and produce different products. Catalysts used in the various reactors in these processes become deactivated over time. Systems and methods are disclosed for extending catalyst life and thereby improving efficiency of the plant. 1. A system comprising: a reactor;', 'a compressor;', 'a separator; and', 'a catalyst bed;, 'a plant comprisingone or more sensors configured to measure operating information for the plant; one or more processors of the data collection platform;', 'a communication interface of the data collection platform and in communication with the one or more sensors; and', receive sensor data comprising the operating information for the plant;', 'correlate the sensor data with time data; and', 'transmit the sensor data;, 'non-transitory computer-readable memory storing executable instructions that, when executed, cause the data collection platform to], 'a data collection platform comprising one or more processors of the data analysis platform;', receive the sensor data from the data collection platform;', 'analyze the sensor data to determine an amount of reactant conversion taking place in the reactor of the plant;', 'based on the amount of reactant conversion taking place in the reactor, determine an estimated catalyst life for catalyst being used in the reactor;', 'determine an adjustment to an operating parameter of the plant based on the estimated catalyst life for the catalyst being used in the reactor; and', ...

PROCESS FOR CONTINUOUSLY CONVERTING MIXED WASTE PLASTIC INTO WAXES AND LIQUID FUELS BY CRACKING

The present invention relates to a process for continuously converting mixed waste plastic into waxes and liquid fuels by cracking. The process comprises the steps of feeding a mixed waste plastic stream to a cracking reactor where the mixed waste plastic is catalytically cracked in the presence of a catalyst and circulating the catalyst between the cracking reactor and a regenerator where the catalyst received from the cracking reactor is regenerated and heated by burning coke and/or other combustible material deposited on or mixed with the catalyst. 2. The process according to wherein the catalyst is a mixture of at least two different catalysts having different catalytic activity and the heat balance between the cracking reactor and the regenerator is adjusted by adjusting the ratio of the at least two different catalysts in the mixture of catalysts.3. The process according to wherein the heat balance between the cracking reactor and the regenerator is adjusted by diluting the mixed waste plastic with a diluent.4. The process according to wherein the mixed waste plastic in the feed stream is diluted with waxes and/or liquid fuels.5. The process according to wherein the waxes and liquid fuels are obtained from the cracking process.6. The process according to wherein the heat balance between the cracking reactor and the regenerator is adjusted by introducing a combustible stream into the regenerator.7. The process according to wherein the heat balance between the cracking reactor and the regenerator is adjusted such that the cracking reactor and the regenerator are maintained in a steady state heat balance.8. The process according to wherein the heat balance between the cracking reactor and the regenerator is adjusted such that a predetermined ratio of waxes to liquid fuels is obtained from the cracking reactor.9. The process according to wherein temperature and flow of the circulating catalyst are adjusted to maintain a pre-selected temperature in the cracking ...

PROCESS FOR TRANSALKYLATING BENZENE

Benzene is transalkylated with existing aromatic alkyl groups in a hydrocracking reactor by feeding a benzene stream and alkylated aromatic compounds to a hydrocracking unit. Alkyl groups migrate from heavier alkylated aromatic compounds to the benzene compounds during transalkylation in the hydrocracking unit. The hydrocracking conditions do not prevent the alkyl groups from transferring from one benzene ring to another benzene ring. 1. A process for converting benzene to alkylbenzene comprising:reacting a hydrocarbon feed stream comprising a naphtha fraction including at least 5 wt % benzene, alkylated aromatic compounds and a distillate fraction boiling in the range of at least about 193° C. (380° F.) and having a T95 between about 315° C. (600° F.) and about 650° C. (1200° F.) in a hydrocracking reactor over a hydrocracking catalyst under hydrocracking conditions in the presence of hydrogen to hydrocrack said distillate fraction and transalkylate said benzene to alkylbenzene to produce a hydrocracked stream comprising a higher concentration of alkyl benzene and a lower concentration of distillate boiling in the range of at least about 193° C. (380° F.) than said hydrocarbon feed stream.2. The process of wherein the hydrocracking conditions comprise a hydrocracking pressure of about 4.83 MPag (700 psig) to about 10.34 MPag (1500 psig).3. The process of wherein at least about 30 wt % of the hydrocarbon feed stream boils in the range of at least about 193° C. (380° F.).4. The process of further comprising converting at least about 5 wt % of the distillate fraction boiling in the range of at least about 193° C. (380° F.) to material boiling below about 193° C. (380° F.).5. The process of wherein said hydrocarbon feed stream comprises at least 30 wppm nitrogen.6. The process of further comprising separating benzene from said hydrocracked stream and recycling said separated benzene back to said hydrocracking reactor.7. The process of further comprising separating a ...

Method and apparatus for managing for hydrogen content through the conversion of hydrocarbons into olefins

An apparatus and method are provided for processing hydrocarbon feeds. The method enhances the conversion of hydrocarbon feeds into conversion products, such as ethylene and propylene. In particular, the present techniques combine a first hydrocarbon feed with a second hydrocarbon feed and a hydrogen (¾) containing stream to manage the hydrogen content of the feed provided to a pyrolysis reactor. The mixture is then exposed to high-severity operating conditions in a pyrolysis reactor and further processing into desired olefins.

Air-cooled heat exchangers

A plant or refinery may include equipment such as reactors, heaters, heat exchangers, regenerators, separators, or the like. Types of heat exchangers include shell and tube, plate, plate and shell, plate fin, air cooled, wetted-surface air cooled, or the like. Operating methods may impact deterioration in equipment condition, prolong equipment life, extend production operating time, or provide other benefits. Mechanical or digital sensors may be used for monitoring equipment, and sensor data may be programmatically analyzed to identify developing problems. For example, sensors may be used in conjunction with one or more system components to detect and correct maldistribution, cross-leakage, strain, pre-leakage, thermal stresses, fouling, vibration, problems in liquid lifting, conditions that can affect air-cooled exchangers, conditions that can affect a wetted-surface air-cooled heat exchanger, or the like. An operating condition or mode may be adjusted to prolong equipment life or avoid equipment failure.

Catalyst cycle length prediction using eigen analysis

Systems and methods are disclosed for managing the operation of a plant, such as a chemical plant or a petrochemical plant or a refinery, and more particularly for enhancing system performance of a catalyzed reaction system by, among other features, detecting catalyst deactivation and cycle length. Plants may include those that provide hydrocarbon cracking or other process units. A plant may include a reactor, a heater, a catalyst bed, a separator, and other equipment. The equipment may use catalyst to treat feed products to remove compounds and produce different products. Catalysts used in the various reactors in these processes become deactivated over time. Systems and methods are disclosed for extending catalyst life and thereby improving efficiency of the plant.

Incipient temperature excursion mitigation and control

Systems and methods are disclosed for detecting temperature excursion in a chemical plant or petrochemical plant or refinery. Aspects of the disclosure provide an enhanced control system for a reactor, such as in hydroprocessing. The enhanced control system may provide early warnings of impending undesirable events, directly or indirectly manipulate certain process variables to reduce undesirable outcomes, and/or directly or indirectly manipulate of certain process variables so as to place a reactor unit in a “safe park” state. This may avoid a high temperature trip, depressuration, associated operating risks, allow for faster recovery from temperature excursions, and/or avoid unplanned emergency shutdowns of the reactor, chemical process, plant, or refinery.

System and method to optimize crude oil distillation or other processing by inline analysis of crude oil properties

An apparatus includes at least one processor configured to obtain inline measurements of one or more properties of crude oil, translate the measurements into a set of process and control parameters, and apply the process and control parameters to process equipment. The process and control parameters configure the process equipment to process the crude oil having the one or more properties. The one or more properties of the crude oil may include at least one of: density, specific gravity, viscosity, carbon residue, and sulfur content of the crude oil. The process and control parameters could be applied to one or more controllers associated with a blending unit in a refinery or to one or more controllers associated with a crude oil distillation column in the refinery.

System and method controlling and optimizing the hydrothermal upgrading of heavy crude oil and bitumen

A system and method is provided for upgrading a continuously flowing process stream including heavy crude oil (HCO). A reactor receives the process stream in combination with water, at an inlet temperature within a range of about 60 °C to about 200 °C. The reactor includes one or more process flow tubes having a combined length of about 30 times their aggregated transverse cross-sectional dimension, and progressively heats the process stream to an outlet temperature T(max)1 within a range of between about 260 °C to about 400 °C. The reactor maintains the process stream at a pressure sufficient to ensure that it remains a single phase at T(max)1. A controller selectively adjusts the rate of flow of the process stream through the reactor to maintain a total residence time of greater than about 1 minute and less than about 25 minutes.

Process for separating pitch from slurry hydrocracked vacuum gas oil

A process is disclosed for converting heavy hydrocarbon feed into lighter hydrocarbon products. The heavy hydrocarbon feed is slurried with a particulate solid material to form a heavy hydrocarbon slurry and hydrocracked in a slurry hydrocracking unit to produce vacuum gas oil (VGO) and pitch. A first vacuum column separates VGO from pitch, and a second vacuum column further separates VGO from pitch. As much as 15 wt-% of VGO can be recovered by the second vacuum column and recycled to the slurry hydrocracking unit. A pitch composition is obtained which can be made into particles and transported without sticking together.

Apparatus for separating pitch from slurry hydrocracked vacuum gas oil

An apparatus is disclosed for converting heavy hydrocarbon feed into lighter hydrocarbon products. The heavy hydrocarbon feed is slurried with a particulate solid material to form a heavy hydrocarbon slurry and hydrocracked in a slurry hydrocracking unit to produce vacuum gas oil (VGO) and pitch. A first vacuum column separates VGO from pitch, and a second vacuum column further separates VGO from pitch. As much as 15 wt-% of VGO can be recovered by the second vacuum column and recycled to the slurry hydrocracking unit. A pitch composition is obtained which can be made into particles and transported without sticking together.

固定床反应器的异常温度检测

提供用于检测固定床反应器内的异常温度状况的系统和方法。在固定床反应器中，烃(或烃类)原料可在升高的温度和/或压力下暴露于一类或多类催化剂颗粒。除所述一类或多类催化剂颗粒外，多个温度传感器结构可包括在催化剂床内和/或可在反应器的内壁或其它内表面上提供包括一个或多个温度传感器结构的涂层。温度传感器结构可具有阈值温度，在阈值温度下，温度传感器结构改变以容许引入和/或释放可检测物质。

由可再生原料控制生产运输燃料

用于控制由可再生原料如植物油和动物油同时生产柴油范围烃和航空范围烃二者的方法。该方法包括确定期望产物的所需规格以及仍满足所述规格的产物期望的相对产率。为了形成满足所需产物规格和产率的链烷烃混合物，确定必要的异构化和选择性加氢裂化区条件。确定必要的分馏区条件以分离期望的产物。将可再生原料(2)通过氢化和脱氧(4)进行处理以提供包含链烷烃的流出物(6)，在预定条件下将至少一部分链烷烃异构化和选择性氢化(22)，并在预定分馏条件下通过分馏(42)进行分离，由此产生柴油范围烃产物(46)和航空范围烃产物(45)。

Method for producing regenerated hydrotreating catalyst and method for producing petroleum product

【課題】 使用済みの水素化処理用触媒から、安定して高い活性を有する再生水素化処理用触媒を製造可能な、再生水素化処理用触媒の製造方法を提供すること、及び再生水素化処理用触媒を用いた、経済的な石油製品の製造方法を提供すること。 【解決手段】 使用済み水素化処理用触媒を、所定の温度範囲で再生処理する再生水素化処理用触媒の製造方法であって、前記所定の温度範囲は、前記使用済み水素化処理用触媒を示差熱分析し、１００℃以上６００℃以下の測定温度領域における示差熱量を起電力の差に換算した値を温度で２回微分した場合の最小の極値及び２番目に小さい極値のうち、低温側の極値に対応する温度をＴ１、高温側の極値に対応する温度をＴ２としたときに、Ｔ１−３０℃以上Ｔ２＋３０℃以下の温度範囲であることを特徴とする再生水素化処理用触媒の製造方法。 【選択図】なし 【Task】 To provide a method for producing a regenerated hydrotreating catalyst capable of producing a regenerated hydrotreating catalyst having high activity stably from a spent hydrotreating catalyst, and to provide a regenerated hydrotreating catalyst. To provide an economical method for producing petroleum products. [Solution] A method for producing a regenerated hydrotreating catalyst for regenerating a used hydrotreating catalyst within a predetermined temperature range, wherein the predetermined temperature range is obtained by performing differential thermal analysis on the used hydrotreating catalyst. Of the minimum extreme value and the second smallest extreme value when the value obtained by converting the differential calorific value in the measurement temperature range of 100 ° C. to 600 ° C. into the difference in electromotive force is differentiated by temperature twice, the extreme value on the low temperature side Production of regenerative hydrotreating catalyst characterized in that the temperature range is from T1-30 ° C. to T2 + 30 ° C., where T1 is the temperature corresponding to the value and T2 is the temperature corresponding to the extreme value on the high temperature side. Method. [Selection figure] None

再生氢化处理用催化剂的制造方法及石油制品的制造方法

一种再生氢化处理用催化剂的制造方法，其特征在于，其为将使用后的氢化处理用催化剂在规定的温度范围内进行再生处理的再生氢化处理用催化剂的制造方法，所述规定的温度范围为T 1 -30℃以上且T 2 +30℃以下的温度范围，所述T 1 、T 2 如下定义：对前述使用后的氢化处理用催化剂进行差热分析，将在100℃以上600℃以下的测定温度范围内的差示热量换算成电动势的差，在将该换算后的值用温度进行2次微分时的最小极值及第2小极值之中，将对应低温侧的极值的温度设为T 1 、对应高温侧的极值的温度设为T 2 。

反応器の洗浄方法

Способ изготовления регенерированного катализатора гидроочистки и способ получения нефтехимического продукта

Предложен способ приготовления регенерированного катализатора гидроочистки путем регенерации отработанного катализатора гидроочистки в заданном интервале температур, где заданным интервалом температур является интервал температур от Т 1 - 30°С или более до Т 2 + 30°С или менее, которые определены путем проведения дифференциального термического анализа отработанного катализатора гидроочистки, преобразования дифференциальной теплоты в интервале измерения температуры от 100°С или более до 600°С или менее в разность электродвижущей силы, двукратного дифференцирования преобразованного значения по температуре для того, чтобы получить наименьшее экстремальное значение и второе наименьшее экстремальное значение, и представления температуры, соответствующей экстремальному значению на стороне более низких температур, как Т 1 , и температуры, соответствующей экстремальному значению на стороне более высоких температур, как Т 2 . Также предложены способ получения нефтяного продукта с использованием указанного катализатора и сам регенерированный катализатор. Способ позволяет получить из отработанного катализатора гидроочистки регенерированный катализатор гидроочистки, имеющий неизменно высокую активность. 3 н. и 4 з.п. ф-лы, 5 ил., 1 табл., 4 пр. РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 528 375 C2 (51) МПК B01J 38/02 (2006.01) B01J 38/12 (2006.01) C10G 45/08 (2006.01) C07C 5/02 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ (21)(22) Заявка: ИЗОБРЕТЕНИЯ К ПАТЕНТУ 2012104538/04, 18.06.2010 (24) Дата начала отсчета срока действия патента: 18.06.2010 Приоритет(ы): (30) Конвенционный приоритет: (43) Дата публикации заявки: 20.08.2013 Бюл. № 23 (73) Патентообладатель(и): ДжейЭкс НИППОН ОЙЛ ЭНД ЭНЕРДЖИ КОРПОРЕЙШН (JP) R U 09.07.2009 JP 2009-162949 (72) Автор(ы): КОННО Соуитироу (JP), ИВАНАМИ Йосиму (JP), САХАРА Ватару (JP), КИМУРА Нобухару (JP) (45) Опубликовано: 20.09.2014 Бюл. № 26 068453 A, 25.03.1991 . RU 2358805 C1, 20.06.2009 . WO 2001/002091 A1, 11. ...

A kind of combined technical method and system handling low grade oils

本发明公开了一种处理劣质油品的组合工艺方法和系统，涉及劣质油品处理领域。所述处理劣质油品的组合工艺方法包括：重油原料、固定床加氢处理反应区生成油与氢气混合后进入沸腾床加氢裂化反应区进行反应，反应流出物分离后得到干气、液化气、汽油、柴油和重馏分；得到的重馏分依次经过串联设置的固定床加氢预处理反应区和固定床加氢处理反应区，固定床加氢处理反应区得到的生成油进入沸腾床加氢裂化反应区。根据本发明方法可以大幅延长处理装置的运转周期。

process for hydrocracking a hydrocarbon feedstock

A kind of combined technical method and system for handling low grade oils

本发明公开了一种处理劣质油品的组合工艺方法和系统，涉及劣质油品处理领域。所述处理劣质油品的组合工艺方法包括：重油原料、固定床加氢处理反应区生成油与氢气混合后进入沸腾床加氢裂化反应区进行反应，反应流出物分离后得到干气、液化气、汽油、柴油和重馏分；得到的重馏分依次经过串联设置的固定床加氢预处理反应区和固定床加氢处理反应区，固定床加氢处理反应区得到的生成油进入沸腾床加氢裂化反应区。根据本发明方法可以大幅延长处理装置的运转周期。

Hydrocracking product quality automatic control method, device and storage

本发明公开了加氢裂化的产品质量自控方法、装置和存储器，其中所述方法包括步骤：获取加氢裂化系统的监测数据；根据监控数据的预设数据标准，统一各种监控数据的采集周期和采集时间点；在工况数据中确定出与产品质量具有关联性且可调节的参数项作为自动控制参数项；构建建模数据；根据预设目标变量和预设自变量对建模数据进行模型训练，生成产品质量预测模型；以从实时监控数据中确定出的重点参数项为输入，通过产品质量预测模型获取加氢裂化系统预设产品的预测结果；当预测结果超出预设范围值时，根据预测模型生成自动控制参数项的调节方案。本发明可以使加氢裂化装置的工况保持在合理的运行状态，进而也就能够有效地减少产品质量不合格的情况。

Process for hydrocracking a hydrocarbon feedstock

수소화분해 방법으로서 (a) 탄화수소 공급원료 및 중질 바닥 부분 재순환 스트림을 수소-풍부 가스와 조합하여 탄화수소 공급원료 및 수소를 포함하는 혼합물을 얻는 단계; (b) 탄화수소 공급원료 및 수소를 포함하는 혼합물을 수소화분해 구역에서 촉매학적으로 수소화분해하여 수소화분해 유출물을 얻는 단계; (c) 분리 구역에서 수소화분해 유출물을 제 1증기부분 및 제 1액체부분으로 분리하는 단계; (d) 제 1액체부분을 가열하여 기화된 제 1액체부분을 형성하는 단계; (e) 기화된 제 1액체부분을 분별 섹션의 바닥 구역에서 미전환유를 포함하는 중질 바닥 부분을 포함하는 개별 생성물 부분들을 생성하는 분별 섹션으로 이송하는 단계; (f) 분별 섹션으로부터 중질 바닥 부분을 회수하는 단계; (g) 중질 바닥 부분을 스트리핑을 위한 스트림 및 중질 바닥 부분 재순환 스트림으로 분할하는 단계; (h) 대향류 스트리핑 컬럼에서 스트리핑을 위한 스트림을 스트리핑 매질로 스트리핑하여 오버헤드 증기 및 스트리핑된 액체를 형성하는 단계; (i) 오버헤드 증기를 분별 섹션으로, 재순환 스트림으로, 또는 분별 섹션 위의 위치로 이송하는 단계; 및 (j) 미전환유의 순퍼지로서 대향류 스트리핑 컬럼으로부터 스트리핑된 액체의 적어도 일부를 제거하는 단계를 포함하는 수소화분해 방법. A process for hydrocracking comprising: (a) combining a hydrocarbon feedstock and a heavy bottom fraction recycle stream with a hydrogen-rich gas to obtain a mixture comprising a hydrocarbon feedstock and hydrogen; (b) catalytically hydrogenating a mixture comprising a hydrocarbon feedstock and hydrogen in a hydrocracking zone to obtain a hydrocracked effluent; (c) separating the hydrocracking effluent in the separation zone into a first vapor portion and a first liquid portion; (d) heating the first liquid portion to form a vaporized first liquid portion; (e) transferring the vaporized first liquid portion to a fractionation section to produce individual product fractions comprising a heavy bottom fraction comprising untransformed oil in a bottom section of the fractionation section; (f) recovering the heavy bottom portion from the fractionation section; (g) dividing the heavy bottom portion into a stream for stripping and a heavy bottom portion recycle stream; (h) stripping the stream for stripping in a countercurrent stripping column with a stripping medium to form an overhead vapor and a stripped liquid; (i) transferring the overhead vapor to a fractionation section, into a recycle stream, or to a location above the fractionation section; And (j) removing at least a portion of the stripped liquid from the countercurrent ...

Controlling production of transportation fuels from renewable feedstocks

A process for controlling the concurrent production of both diesel range hydrocarbons and aviation range hydrocarbons from renewable feedstocks such as plant oils and animal oils. The process involves determining the required specification of the desired products and the desired relative yields of the product that still meet the required specifications. The necessary isomerization and selective hydrocracking zone conditions are determined in order to create a mixture of paraffins which meet the required product specifications and yields. The necessary fractionation zone conditions are determined to separate the desired products. A renewable feedstock is treated by hydrogenating and deoxygenating to provide an effluent comprising paraffins, isomerizing and selectively hydrogenating at least a portion of the paraffins at the predetermined conditions, and separating by fractionation at the predetermined fractionation conditions to generate a diesel range hydrocarbon product and an aviation range hydrocarbon product.

Conversion of a light sweet refinery to a heavy sour refinery

This is a unique way of upgrading an existing refinery to process heavy sour crude. The system does not significantly modify an existing sweet refinery. Rather, a hydrocracker is used at the existing light sweet refinery location to create light sweet crudes from heavy sour crudes prior to processing in an existing sweet refinery.

Process for the fractionation of diluted bitumen for use in light sweet refinery

This is a unique way of upgrading an existing refinery to process heavy bitumen. The upgrade utilizes a diluent recovery unit (DRU) in front of a Resid Hydrocracker. The diluent is light enough that the DRU does not require significant metallurgy upgrades. The corrosive, heavier material is neutralized in the Resid Hydrocracker eliminating need for metallurgical upgrades in downstream units.

Process for the conversion of hydrocarbonaceous black oil

A process for the conversion of a hydrocarbonaceous black oil, wherein a heated portion of the charge stock is recycled to the inlet of the charge heater, is disclosed.

Hydrocarbon upgrading

Aspects of the invention provide a process and system for upgrading a hydrocarbon feed. The process includes providing a hydrocarbon feed and a utility fluid. Then selectively extracting from the feed at least a portion of particulates to produce a raffinate and an extract. Third, hydroprocessing at least a portion of the raffinate.

Patent RU2016140701A3

`7ВУ’” 2016140701`” АЗ Дата публикации: 09.10.2018 Форма № 18 ИЗ,ПМ-2011 Федеральная служба по интеллектуальной собственности Федеральное государственное бюджетное учреждение ж 5 «Федеральный институт промышленной собственности» (ФИПС) ОТЧЕТ О ПОИСКЕ 1. . ИДЕНТИФИКАЦИЯ ЗАЯВКИ Регистрационный номер Дата подачи 2016140701/04(06494Т) 18.03.2015 РСТЛ52015/021258 18.03.2015 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. 14/218,619 18.03.2014 05 Название изобретения (полезной модели): [Х] - как заявлено; [ ] - уточненное (см. Примечания) СИСТЕМА И СПОСОБ КОНТРОЛЯ И ОПТИМИЗАЦИИ ГИДРОТЕРМАЛЬНОГО ПРОЦЕССА ОБЛАГОРАЖИВАНИЯ ТЯЖЕЛОИ СЫРОИ НЕФТИ И БИТУМОВ Заявитель: АДУРО ЭНЕРДЖИ, ИНК., СА, ТРИГСТАД, Дабл-Ю., Маркус, 05 2. ЕДИНСТВО ИЗОБРЕТЕНИЯ [Х] соблюдено [ ] не соблюдено. Пояснения: см. Примечания 3. ФОРМУЛА ИЗОБРЕТЕНИЯ: [Х] приняты во внимание все пункты (см. Примечания) [ ] приняты во внимание следующие пункты: [ ] принята во внимание измененная формула изобретения (см. Примечания) 4. КЛАССИФИКАЦИЯ ОБЪЕКТА ИЗОБРЕТЕНИЯ (ПОЛЕЗНОЙ МОДЕЛИ) (Указываются индексы МПК и индикатор текущей версии) С10С 9/14 (2006.01) С10С 31/08 (2006.01) С10С 47/36 (2006.01) 5. ОБЛАСТЬ ПОИСКА 5.1 Проверенный минимум документации РСТ (указывается индексами МПК) С10С 9/14, С10С 31/08, С10С 47/36 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): ЕАРАТГУ, Езрасепе, Соозе, Рабеагсв 6 ДОКУМЕНТЫ, ОТНОСЯЩИЕСЯ К ПРЕДМЕТУ ПОИСКА Кате- Наименование ...

Method and apparatus for separating coal tar from suspended-phase hydrocracked vacuum gas oil and composition thereof

Изобретение относится к гидроконверсии тяжелых углеводородов. Изобретение касается способа превращения тяжелого углеводородного сырья в более легкие углеводородные продукты и отделения пека, включающего гидрокрекинг тяжелого углеводородного сырья, суспендированного с зернистым твердым материалом в присутствии водорода в реакторе гидрокрекинга, в результате чего образуется подвергнутый гидрокрекингу поток, включающий вакуумный газойль (ВГ) и пек. В первой вакуумной колонне производят отделение ВГ от пека, а во второй вакуумной колонне производят дополнительное отделение ВГ от пека. Изобретение также касается устройства для превращения тяжелого углеводородного сырья в более легкие углеводородные продукты и отделения пека. Технический результат - получение пека, из которого могут быть приготовлены частицы, способные транспортироваться без слипания. 2 н.з. и 8 з.п. ф-лы, 2 ил., 1 табл., 1 пр. РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2 504 575 (13) C2 (51) МПК C10G 47/00 (2006.01) C10G 7/06 (2006.01) C10C 3/00 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (21)(22) Заявка: 2012102378/04, 16.06.2010 (24) Дата начала отсчета срока действия патента: 16.06.2010 (73) Патентообладатель(и): ЮОП ЛЛК (US) R U Приоритет(ы): (30) Конвенционный приоритет: 25.06.2009 US 12/491,444 25.06.2009 US 12/491,439 (72) Автор(ы): ВАН ВИС Марк (US), КЛЯЙНВОРТ Рут Бускус (US), МакГИХИ Джеймс Ф. (US), МАЙЕРС Дэвид Н. (US), ЦИММЕРМАН Пол Р. (US) (43) Дата публикации заявки: 27.07.2013 Бюл. № 21 2 5 0 4 5 7 5 (45) Опубликовано: 20.01.2014 Бюл. № 2 (56) Список документов, цитированных в отчете о поиске: US 4525267 A, 25.06.1985. US 5755955 A, 26.05.1998. US 20080156693 A1, 03.07.2008. US 20050006279 A1, 13.01.2005. RU 2145971 C1, 27.02.2000. 2 5 0 4 5 7 5 R U (86) Заявка PCT: US 2010/038759 (16.06.2010) C 2 C 2 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 25.01.2012 (87) Публикация заявки РСТ: WO 2010/151463 (29.12.2010) Адрес для ...

Method and device for reducing heavy polycyclic aromatic compounds in hydrocracking units

본 발명은 분별 칼럼을 포함하는 수소화 분해 유닛들의 재순환 루프에서 중질 다환 방향족 화합물들 (HPNA) 의 농도를 감소시킬 수 있는 방법 및 장치에 관한 것이다. 상기 방법에 따르면, 수소화 분해된 유출액 공급 트레이와 가장 중질의 증류액 분획물을 위한 인출 트레이 사이에 위치한 적어도 하나의 트레이의 영역에 존재하는 스트림의 일 부분은 분별 칼럼으로부터 인출되고, 인출된 상기 스트림의 적어도 일 부분은 직접 또는 액체의 선택적 분리 후 칼럼에서 재순환되고, 선택적으로 인출된 상기 스트림의 일 부분은 직접 또는 가스의 선택적 분리 후 수소화 분해 단계에서 재순환된다. The present invention relates to a method and apparatus capable of reducing the concentration of heavy polycyclic aromatic compounds (HPNA) in the recycle loop of hydrocracking units comprising a fractionation column. According to the process, a portion of the stream present in the region of the at least one tray located between the hydrocracked effluent feed tray and the draw tray for the heaviest distillate fraction is withdrawn from the fractionation column, and At least a portion is recycled to the column, either directly or after selective separation of the liquid, and optionally a portion of said stream withdrawn is recycled in the hydrocracking stage either directly or after selective separation of gases.

SYSTEM AND METHOD FOR CONTROL AND OPTIMIZATION OF THE HYDROTHERMAL PROCESS OF HANDLING HEAVY RAW OIL AND BITUMEN

РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2016 140 701 A (51) МПК C10G 9/08 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21)(22) Заявка: 2016140701, 18.03.2015 (71) Заявитель(и): АДУРО ЭНЕРДЖИ, ИНК. (CA), ТРИГСТАД, Дабл-Ю., Маркус (US) Приоритет(ы): (30) Конвенционный приоритет: 18.03.2014 US 14/218,619 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 18.10.2016 R U (43) Дата публикации заявки: 20.04.2018 Бюл. № 11 (72) Автор(ы): ТРИГСТАД Дабл-Ю. Маркус (US) (86) Заявка PCT: (87) Публикация заявки PCT: WO 2015/143039 (24.09.2015) R U (54) СИСТЕМА И СПОСОБ КОНТРОЛЯ И ОПТИМИЗАЦИИ ГИДРОТЕРМАЛЬНОГО ПРОЦЕССА ОБЛАГОРАЖИВАНИЯ ТЯЖЕЛОЙ СЫРОЙ НЕФТИ И БИТУМОВ (57) Формула изобретения 1. Система облагораживания непрерывного технологического потока, включающего тяжелую сырую нефть (ТСН), содержащая: маршрут потока жидкости, выполненный с возможностью непрерывной доставки технологического потока по этому маршруту в направлении течения, при этом маршрут потока включает в себя реактор; реактор, выполненный с возможностью принимать технологический поток вместе с водой при температуре на входе в пределах приблизительно 60-200°С; реактор, включающий в себя одну или более расходомерных труб, определяющих совокупный поперечный размер потока внутри труб поперек течения, при этом общая длина одной или более расходомерных труб по меньшей мере в 30 раз превышает совокупный внутренний поперечный размер; реактор, выполненный с возможностью подвода тепла на проходящий через него технологический поток, чтобы постепенно нагревать технологический поток от температуры на входе на входной части реактора до температуры на выходе Т(max)1 в пределах приблизительно 260-400°С на выходной части реактора, реактор выполнен с возможностью поддерживать давление в технологическом потоке, достаточное для обеспечения того, чтобы технологический поток находился в одной фазе при Т(max)1; контроллер, выполненный с возможностью выборочно регулировать ...

Method of hydrogenating synthetic oil and method of producing base fuel

FIELD: chemistry. SUBSTANCE: invention relates to a method of hydrofining synthetic oil, realised by bringing synthetic oil, obtained via Fischer-Tropsch synthesis and having content of C-9-21 hydrocarbons greater than or equal to 90 wt %, into contact with a hydrofining catalyst which has a support which contains one or more solid acids selected from ultra-stable Y-(USY) zeolite, aluminosilicate, zirconia-silicate and aluminium-bromine oxide catalyst and at least one metal selected from a group comprising group VIII metals, deposited on the support, in the presence of hydrogen with regulation of the reaction temperature when the hydrofining catalyst is in contact with the synthetic oil, in order to hydrofine the synthetic oil such that content (wt %) of C8 or lower hydrocarbons in the synthetic oil after contact is 3-9 wt % higher than before contact. The invention also relates to a method of producing base fuel material. EFFECT: obtaining base oil with excellent low-temperature rheological properties with good output of the middle fraction of the synthetic oil. 6 cl, 8 ex, 2 tbl, 1 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2 419 649 (13) C2 (51) МПК C10G 45/10 C10G 45/12 (2006.01) (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ, ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (21)(22) Заявка: 2008136837/04, 06.02.2007 (24) Дата начала отсчета срока действия патента: 06.02.2007 (73) Патентообладатель(и): НИППОН ОЙЛ КОРПОРЕЙШН (JP) R U Приоритет(ы): (30) Конвенционный приоритет: 13.02.2006 JP 2006-035638 (72) Автор(ы): ТАНАКА Юити (JP), ТАКАХАСИ Синя (JP), ТИБА Йосифуми (JP) (43) Дата публикации заявки: 20.03.2010 Бюл. № 8 2 4 1 9 6 4 9 (45) Опубликовано: 27.05.2011 Бюл. № 15 (56) Список документов, цитированных в отчете о поиске: JP 10-053776 А, 24.02.1998. JP 58-210029 A, 07.12.1983. US 3709817 A, 09.01.1973. RU 2228947 C2, 20.05.2004. RU 2160764 C2, 20.12.2000. 2 4 1 9 6 4 9 R U (86) Заявка PCT: JP 2007/051990 (06.02.2007) C 2 C 2 (85) ...

Treatment method for producing diesel fuel base and method of calculating degree of cracking of wax fraction

本发明的目的是提供一种用于从费-托合成油制造柴油燃料基材的处理方法，其是对费-托合成油进行处理的方法，其包含以下步骤：(a)使用精馏塔将用费-托合成法得到的合成油分馏成至少两个馏分即含有相当于柴油燃料油的沸点范围的成分的中间馏分、和含有比该中间馏分重质的蜡组分的蜡馏分的步骤；(b)在加氢裂化反应器中，通过使蜡馏分与加氢裂化催化剂接触以进行加氢裂化，从而得到裂化产物的步骤；(c)在所述(b)步骤中，在加氢裂化反应器之后配置气液分离器，从裂化产物中分离除去气体组分，同时得到裂化生成油的步骤；(d)对在所述(c)步骤中被分离除去的气体组分的组成进行测定的步骤；(e)从通过所述(d)步骤测定的气体组分的组成算出加氢裂化反应的裂化率的步骤；(f)控制所述加氢裂化反应器的运转条件使得在所述(e)步骤算出的裂化率成为目标裂化率的步骤。另外，本发明的目的是提供一种算出加氢裂化蜡馏分时的裂化率的方法，所述蜡馏分是使用精馏塔对费-托合成油进行分馏而得到的。

Controlling temperature within a catalyst bed in a reactor vessel

A quenching medium is delivered directly to selected regions or locations within a catalyst bed in a hydroprocessing reactor vessel in order to control the reactivity of a hydroprocess occurring in the selected regions or locations separately from other regions or locations. Temperature sensors for providing temperature indications and conduits for delivering the quench medium are distributed throughout the catalyst bed. One or more conduits can be selected for delivery of the quenching medium to selected regions or locations so that separate control of the level of reactivity in each of various regions or locations throughout the bed can be achieved.

Initial temperature excursion mitigation and control

本发明公开了用于检测化工厂或石化厂或精炼厂中的温度剧增的系统和方法。本公开的各方面提供了用于反应器的增强的控制系统，诸如在加氢处理时使用。所述增强的控制系统可提供对即将发生的非期望事件的早期警示，直接或间接地操纵某些过程变量以减少非期望结果，并且/或者直接或间接地操纵某些过程变量以便将反应器单元置于“安全停放”状态。这可避免高温跳闸、降压、相关联的操作风险，允许更快地从温度剧增状态恢复正常，并且/或者避免所述反应器、化学过程、工厂或精炼厂的非计划紧急关闭。

Hydrocracking product quality automatic control method, device and storage

本发明公开了加氢裂化的产品质量自控方法、装置和存储器，其中所述方法包括步骤：获取加氢裂化系统的监测数据；根据监测数据的预设数据标准，统一各种监测数据的采集周期和采集时间点；在工况数据中确定出与产品质量具有关联性且可调节的参数项作为自动控制参数项；构建建模数据；根据预设目标变量和预设自变量对建模数据进行模型训练，生成产品质量预测模型；以从实时监测数据中确定出的重点参数项为输入，通过产品质量预测模型获取加氢裂化系统预设产品的预测结果；当预测结果超出预设范围值时，根据预测模型生成自动控制参数项的调节方案。本发明可以使加氢裂化装置的工况保持在合理的运行状态，进而也就能够有效地减少产品质量不合格的情况。

METHOD AND INSTALLATION FOR SEPARATING A PITCH FROM AN EXTENDED HYDROCRACKING IN THE SUSPENSION PHASE OF VACUUM GAS OIL AND ITS COMPOSITION

1. Способ превращения тяжелого углеводородного сырья в более легкие углеводородные продукты, включающий:гидрокрекинг указанного тяжелого углеводородного сырья, суспендированного с зернистым твердым материалом в присутствии водорода в реакторе гидрокрекинга, в результате чего образуется подвергнутый гидрокрекингу поток, включающий вакуумный газойль (ВГ) и пек;отделение по крайней мере части указанного подвергнутого гидрокрекингу потока в первой вакуумной колонне, в результате чего образуется первый поток пека и первый поток ВГ; иотделение по крайней мере части указанного первого потока пека во второй вакуумной колонне, в результате чего образуется второй поток пека и второй поток ВГ.2. Способ по п.1, в котором давление на входе в первую вакуумную колонну выше, чем давление на входе во вторую вакуумную колонну.3. Способ по п.1, дополнительно включающий в себя формование пека в указанном втором потоке пека в нелипкие твердые частицы при температурах до 66°С (150°F).4. Способ по п.1, в котором поток парафинового гача, отбираемый ниже погона тяжелого ВГ, возвращают в виде рециркулята в реактор гидрокрекинга.5. Способ по п.1, в котором пек из второй вакуумной колонны имеет температуру начала размягчения по меньшей мере 66°С (150°F).6. Способ по п.1, дополнительно включающий в себя рециркуляцию указанного первого потока пека на стадию гидрокрекинга.7. Способ по п.1, дополнительно включающий в себя рециркуляцию второго потока ВГ на стадию гидрокрекинга.8. Устройство для превращения тяжелого углеводородного сырья в более легкие углеводородные продукты, включающее:реактор гидрокрекинга в суспензионной фазе для осуществления кон РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2012 102 378 A (51) МПК C10G 47/00 (2006.01) C10G 7/06 (2006.01) C10C 3/00 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21)(22) Заявка: 2012102378/04, 16.06.2010 (71) Заявитель(и): ЮОП ЛЛК (US) Приоритет(ы): (30) Конвенционный приоритет: 25.06.2009 US 12/491,444; 25.06 ...

Catalyst reaction layer with separate raw material feeding in the hydraulic cleaning plant

FIELD: oil and gas industry. SUBSTANCE: invention relates to the plant with hydrotreating reactor and to the naphtha mixture stream hydrotreating method. Plant comprises the reaction chamber, in which the first layer and the second layer are arranged, and which comprises first input arranged so, that to provide the hydrocarbons stream supply to the first layer, and the second input arranged so, that to bypass the first layer and direct the hydrocarbons flow to the second layer, regulator for the temperature differences measuring across the first layer height, installed near the second inlet and connected to the regulator control valve, configured to control the supplied through the second inlet hydrocarbon stream flow rate, based on the measured by the regulator temperature difference, raw material heater, from which a hydrocarbon stream exits through the output line, which contains branching, at that, the output line first branch is connected to the first input and in fluid communication with the first layer, and the output line second branch is connected to the second input and in fluid communication with the second layer, and throttle device installed downstream of the output line branching point between the raw material heater and the first input and serving to monitor the differential pressure at the first input. EFFECT: invention enables temperature control over the first layer height without disturbing the other layers functioning. 10 cl, 1 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 659 263 C2 (51) МПК B01J 8/24 (2006.01) B01J 19/24 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК B01J 8/24 (2018.02); B01J 19/24 (2018.02) (21)(22) Заявка: 2016112530, 03.09.2014 (24) Дата начала отсчета срока действия патента: Дата регистрации: 29.06.2018 10.09.2013 US 14/022,543 (43) Дата публикации заявки: 05.10.2017 Бюл. № 28 (56) Список документов, цитированных в отчете о поиске: US 2012/0273394 A1, 01.11.2012. ...

Energy-recovery turbines for gas streams

Processes for controlling the flowrate of and recovering energy from a gas stream in a processing unit are described. One process comprises directing a portion of the gas stream through one or more variable-resistance power-recovery turbines to control the flowrate of the gas stream and generate electric power therefrom; and controlling the pressure and temperature of the gas stream so that the gas exiting the power-recovery turbine remains in the gas phase.

Controlling production of transportation fuels from renewable feedstocks

A process for controlling the concurrent production of both diesel range hydrocarbons and aviation range hydrocarbons from renewable feedstocks such as plant oils and animal oils. The process involves determining the required specification of the desired products and the desired relative yields of the product that still meet the required specifications. The necessary isomerization and selective hydrocracking zone conditions are determined in order to create a mixture of paraffins which meet the required product specifications and yields. The necessary fractionation zone conditions are determined to separate the desired products. A renewable feedstock (2) is treated by hydrogenating and deoxygenating (4) to provide an effluent (6) comprising paraffins, isomerizing and selectively hydrogenating (22) at least a portion of the paraffins at the predetermined conditions, and separating by fractionation (42) at the predetermined fractionation conditions to generate a diesel range hydrocarbon product (46) and an aviation range hydrocarbon product (45).

Controlling production of transportation fuels from renewable feedstocks

用于控制由可再生原料如植物油和动物油同时生产柴油范围烃和航空范围烃二者的方法。该方法包括确定期望产物的所需规格以及仍满足所述规格的产物期望的相对产率。为了形成满足所需产物规格和产率的链烷烃混合物，确定必要的异构化和选择性加氢裂化区条件。确定必要的分馏区条件以分离期望的产物。将可再生原料(2)通过氢化和脱氧(4)进行处理以提供包含链烷烃的流出物(6)，在预定条件下将至少一部分链烷烃异构化和选择性氢化(22)，并在预定分馏条件下通过分馏(42)进行分离，由此产生柴油范围烃产物(46)和航空范围烃产物(45)。

Controlling production of transportation fuels from renewable feedstocks

A process for controlling the concurrent production of both diesel range hydrocarbons and aviation range hydrocarbons from renewable feedstocks such as plant oils and animal oils. The process involves determining the required specification of the desired products and the desired relative yields of the product that still meet the required specifications. The necessary isomerization and selective hydrocracking zone conditions are determined in order to create a mixture of paraffins which meet the required product specifications and yields. The necessary fractionation zone conditions are determined to separate the desired products. A renewable feedstock (2) is treated by hydrogenating and deoxygenating (4) to provide an effluent (6) comprising paraffins, isomerizing and selectively hydrogenating (22) at least a portion of the paraffins at the predetermined conditions, and separating by fractionation (42) at the predetermined fractionation conditions to generate a diesel range hydrocarbon product (46) and an aviation range hydrocarbon product (45).

Controlling production of transportation fuels from renewable feedstocks

A process for controlling the concurrent production of both diesel range hydrocarbons and aviation range hydrocarbons from renewable feedstocks such as plant oils and animal oils. The process involves determining the required specification of the desired products and the desired relative yields of the product that still meet the required specifications. The necessary isomerization and selective hydrocracking zone conditions are determined in order to create a mixture of paraffins which meet the required product specifications and yields. The necessary fractionation zone conditions are determined to separate the desired products. A renewable feedstock (2) is treated by hydrogenating and deoxygenating (4) to provide an effluent (6) comprising paraffins, isomerizing and selectively hydrogenating (22) at least a portion of the paraffins at the predetermined conditions, and separating by fractionation (42) at the predetermined fractionation conditions to generate a diesel range hydrocarbon product (46) and an aviation range hydrocarbon product (45).

Use of infrared spectroscopy to produce high lubricity, high stability, Fischer-Tropsch diesel fuels and blend fuel

本发明涉及一种对生产重于汽油的馏出燃料工艺进行控制的方法。本方法包括若干不同的馏分、料流,包括醇、烯烃和酸。至少一种料流用IR光照射,使得能够确定醇、烯烃和酸的至少一个浓度。然后调节分离器的温度,将浓度改变到预定值。

REACTIVE LAYER OF THE CATALYST WITH SEPARATE FEEDING OF RAW MATERIALS IN A HYDROCLEANING PLANT

А 2016112530 ко РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) р я „7 З © ЗАО п $5 <“ < 5% <& Хх 5х хх х& 13 КО ’ 2016 112 5307 А (51) МПК ВО! 8/24 (2006.01) А 28 777 ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21)(22) Заявка: 2016112530, 03.09.2014 (71) Заявитель(и): ЮОП ЛЛК (05) Приоритет(ы): (30) Конвенционный приоритет: (72) Автор(ы): 10.09.2013 95 14/022,543 БАНЕРЖИ Соумендра М. (0$), ХОЭН Ричард К. (05), ВАРАДАРАДЖАН Сриниваса Гопалан (85) Дата начала рассмотрения заявки РСТ на Раджан (05), национальной фазе: 01.04.2016 КОТАНДАРАМАН Партасарати (05) (43) Дата публикации заявки: 05.10.2017 Бюл. № 28 (86) Заявка РСТ: 0$ 2014/053848 (03.09.2014) (87) Публикация заявки РСТ: УГО 2015/038379 (19.03.2015) Адрес для переписки: 109012, Москва, ул. Ильинка, 5/2, ООО "Союзпатент" (54) РЕАКЦИОННЫЙ СЛОЙ КАТАЛИЗАТОРА С РАЗДЕЛЬНОЙ ПОДАЧЕЙ СЫРЬЯ В УСТАНОВКЕ ДЛЯ ГИДРООЧИСТКИ (57) Формула изобретения 1. Установка (10) с реактором гидроочистки, содержащая реакционную камеру (28), в которой размещены по меньшей мере первый слой (30) и второй слой (32), и, кроме того, реакционная камера содержит первый вход (28а), расположенный так, чтобы обеспечить подвод потока углеводородов к первому слою, и второй вход (285), расположенный так, чтобы байпасировать первый слой и направлять поток углеводородов к указанному второму слою; регулятор (34) для измерения перепада температур по высоте указанного первого слоя (30); регулирующий клапан (38), установленный вблизи второго входа (28) и соединенный с указанным регулятором (34) перепада температур; при этом регулирующий клапан выполнен с возможностью регулирования расхода потока углеводородов, подаваемого через второй вход, исходя из перепада температур, измеренного с помощью регулятора перепада температур; нагреватель сырья (16), из которого выходит поток углеводородов через выходную линию (20), которая содержит разветвление, при этом первая ветвь (24) указанной выходной линии соединена с указанным первым входом (28а) и ...

Method of producing hydrocarbon product with sulfur level below 50 ppm

FIELD: petroleum processing. SUBSTANCE: two or more types of hydrocarbon stock with sulfur level above 50 ppm are combined to form blended stock. The latter is subjected to hydrodesulfurization step to reduced sulfur resulting in production of reduced-sulfur hydrocarbon fraction. Process is adjusted so that a situation is achieved wherein level of sulfur in hydrocarbon product is close or equal to desired sulfur level, production of hydrocarbon product with desired sulfur level being optimized through integrated control of hydrocarbon stock blending step and installation operation in hydrodesulfurization step taking into account level of sulfur in blended hydrocarbon product subjected to hydrodesulfurization. EFFECT: maximized production of lower sulfur-level gas oil. 24 cl, 4 cl ÐÎÑÑÈÉÑÊÀß ÔÅÄÅÐÀÖÈß (19) RU (11) 2 292 379 (13) C2 (51) ÌÏÊ C10G 45/02 C10G 45/72 (2006.01) (2006.01) ÔÅÄÅÐÀËÜÍÀß ÑËÓÆÁÀ ÏÎ ÈÍÒÅËËÅÊÒÓÀËÜÍÎÉ ÑÎÁÑÒÂÅÍÍÎÑÒÈ, ÏÀÒÅÍÒÀÌ È ÒÎÂÀÐÍÛÌ ÇÍÀÊÀÌ (12) ÎÏÈÑÀÍÈÅ ÈÇÎÁÐÅÒÅÍÈß Ê ÏÀÒÅÍÒÓ (21), (22) Çà âêà: 2004106603/04, 06.08.2002 (72) Àâòîð(û): ÌÀÐÒÝÍ Áåðíàð (FR), ÐÓÁÈ Æàí-Ëþê Êðèñòü í (NL), ÒÈÌÌÅÐÌÀÍÑ Âàóòåð Ôðåäåðèê (NL), ÂÈÅËÜ Ôðåäåðèê (NL) (24) Äàòà íà÷àëà îòñ÷åòà ñðîêà äåéñòâè ïàòåíòà: 06.08.2002 (73) Ïàòåíòîîáëàäàòåëü(è): ØÅËË ÈÍÒÅÐÍÝØÍË ÐÈÑÅÐ× ÌÀÀÒÑÕÀÏÏÈÉ Á.Â. (NL) (43) Äàòà ïóáëèêàöèè çà âêè: 27.07.2005 R U (30) Êîíâåíöèîííûé ïðèîðèòåò: 08.08.2001 EP 01402144.8 (45) Îïóáëèêîâàíî: 27.01.2007 Áþë. ¹ 3 2 2 9 2 3 7 9 (56) Ñïèñîê äîêóìåíòîâ, öèòèðîâàííûõ â îò÷åòå î ïîèñêå: ÅÐ 01316656 À1, 24.05.1989. GB 2157854 À, 30.10.1985. SU 1468913 À1, 30.03.1989. US 4990242 À, 05.02.1991. JP 4046993 A, 17.02.1992. (85) Äàòà ïåðåâîäà çà âêè PCT íà íàöèîíàëüíóþ ôàçó: 09.03.2004 2 2 9 2 3 7 9 R U (87) Ïóáëèêàöè PCT: WO 03/014264 (20.02.2003) C 2 C 2 (86) Çà âêà PCT: EP 02/08807 (06.08.2002) Àäðåñ äë ïåðåïèñêè: 103735, Ìîñêâà, óë. Èëüèíêà, 5/2, ÎÎÎ "Ñîþçïàòåíò", Í.Í.Âûñîöêîé (54) ÑÏÎÑÎÁ ÏÎËÓ×ÅÍÈß ÓÃËÅÂÎÄÎÐÎÄÍÎÃÎ ÏÐÎÄÓÊÒÀ Ñ ÑÎÄÅÐÆÀÍÈÅÌ ÑÅÐÛ ÍÈÆÅ 0,05 ÌÀÑ.% (57) ...

Process for hydrocracking a hydrocarbon feedstock

氢化裂解方法，其包括以下步骤：(a)将含烃进料和重质底部馏分再循环料流与富氢气体合并，以获得包含含烃进料和氢气的混合物；(b)在氢化裂解区催化氢化裂解所述包含含烃进料和氢气的混合物以获得氢化裂解流出物；(c)在分离区将所述氢化裂解流出物分离成第一蒸气部分和第一液体部分；(d)加热所述第一液体部分至形成蒸发的第一液体部分；(e)将所述蒸发的第一液体部分进料至分馏区域，在该分馏区域产生了单独产品馏分，其包含在该分馏区域底部区含有未转化油的重质底部馏分；(f)从所述分馏区域移出所述重质底部馏分；(g)将所述重质底部馏分分割成用于汽提的料流和重质底部馏分再循环料流；(h)在逆流汽提塔中采用汽提介质将用于汽提的料流汽提，以形成顶部蒸气和汽提的液体；(i)将所述顶部蒸气进料至分馏区域成为再循环料流或进料至该分馏区域上游的位置；和(j)从作为未转化油的净清除的逆流汽提塔中除去汽提的液体的至少一部分。

Hydrodealkylation reactor system

Method of processing fischer-tropsch synthetic oil to manufacture diesel fuel base stock and method of calculating cracking rate upon hydrocracking wax fraction

An object of the present invention is to provide a method of processing Fischer-Tropsch synthetic oil to manufacture a diesel fuel base stock, the method including: (a) fractionating, in a fractionator, Fischer-Tropsch synthetic oil obtained by a Fischer-Tropsch synthesis method into at least two fractions of a middle fraction containing a component having a boiling point range corresponding to diesel fuel oil and a wax fraction containing a wax component heavier than the middle fraction; (b) bringing the wax fraction into contact with a hydrocracking catalyst in a hydrocracking reactor to obtain a hydrocracked product; (c) separating a gas component from the hydrocracked product to produce hydrocracked oil in a gas-liquid separator disposed in the rear of the hydrocracking reactor used in the step (b); (d) measuring the composition of the gas component separated in the step (c); (e) calculating a cracking rate in the hydrocracking reaction based on the composition of the gas component measured in the step (d); and (f) controlling an operation condition of the hydrocracking reactor so that the cracking rate calculated in the step (e) agrees with an objective cracking rate. Furthermore, another object of the present invention is to provide a method of calculating the cracking rate in hydrocracking the wax fraction obtained by fractionating the Fischer-Tropsch synthetic oil in the fractionator.

Process for the catalytic degradation of cyclic compounds

Hydro cracking of feeds contg. nitrogen - with prior hydro denitrification and high ppressure prefactionation of effluent

THREE-PHASE REACTOR WITH VERTICAL COMPARTMENTS IN SERIES AND PROCESS FOR HYDROCONVERSION OF HEAVY OIL LOADS

La présente invention concerne un réacteur d’hydroconversion d'une charge liquide d'hydrocarbures comprenant une enveloppe de réacteur (3) et une pluralité de compartiments (S1, S2) configurés pour fonctionner en série, délimités par des parois internes verticales (16), chaque compartiment comprenant :- une chambre d’injection de fluides (7), lesdits fluides comprenant la charge liquide d'hydrocarbures et un gaz contenant de l’hydrogène, - une zone catalytique d’hydroconversion surmontant et séparée de ladite chambre (7) par un plateau de distribution des fluides (8), ladite zone catalytique d’hydroconversion comportant un lit bouillonnant de catalyseur (9), lesdites parois internes verticales (16) étant étanches dans la partie du réacteur située au-dessus du plateau de distribution (8) de manière à empêcher le transfert de catalyseur et des fluides entre les compartiments dans ladite partie du réacteur. L’invention a également concerne également un procédé d’hydroconversion catalytique d'une charge liquide d'hydrocarbures mettant en œuvre un tel réacteur. Figure 1 à publier The present invention relates to a reactor for the hydroconversion of a liquid hydrocarbon feed comprising a reactor envelope (3) and a plurality of compartments (S1, S2) configured to operate in series, delimited by vertical internal walls (16) , each compartment comprising:- a fluid injection chamber (7), said fluids comprising the liquid hydrocarbon charge and a gas containing hydrogen, - a catalytic hydroconversion zone surmounting and separated from said chamber (7 ) by a fluid distribution plate (8), said catalytic hydroconversion zone comprising a bubbling bed of catalyst (9), said vertical internal walls (16) being sealed in the part of the reactor located above the distribution plate (8) so as to prevent the transfer of catalyst and fluids between the compartments in said part of the reactor. The invention also relates to a process for the catalytic hydroconversion ...

Hydro cracking of feeds contg. nitrogen - with prior hydro denitrification and high ppressure prefactionation of effluent

Petroleum hydrocarbon feeds contaminated with N cpds. are hydrocracked by (a) contacting the feed with H2 in the presence of a hydrodesulphurisation, hydrodenitrification or hydrocracking catalyst in a first reactor at 300-550 degrees C (pref. 300-470 degrees C) and 15-250) atm; (b) passing the effluent to a 1st separator at the same pressure and a temp. of 200-300 degrees C (pref. 250-290 degrees C) to obtain an NH3-redn. rich vapour fraction and a liq. effluent contg. 50 ppm NH3; (c) mixing the liq. effluent with at least part of the bottom product from a subsequent prefractionator; (d) passing the mixt. to a 2nd reactor, where it is treated at 300-550 degrees C (pref. 300-440 degrees C) and 15-250 (pref. 50-250) atm; (e) mixing the effluent from the 2nd reactor with the vapour fraction from the 1st reactor; (f) passing the mixt. to a prefractionator at the same press. as in the 2nd reactor, and stripping it with a gas (pref. H2) to obtain a vapour overhead (H2 + products) and a heavy bottom product (heavy products + unconverted feed); (g) recycling at least part of the bottoms to step (c); and (h) cooling the vapour overhead, separating an H2-rich gas, and fractionating the liq. phase to isolate the required products. Since the NH3 formed in the 1st reactor by-passes the 2nd reactor, the latter can be operated with a conventional NH3-sensitive hydrocracking catalyst. The heavy bottom product from the prefractionator is recycled at the same pressure as that in the 2nd reactor, thus reducing energy consumption.

Hydro cracking of feeds contg. nitrogen - with prior hydro denitrification and high ppressure prefactionation of effluent

Petroleum hydrocarbon feeds contaminated with N cpds. are hydrocracked by (a) contacting the feed with H2 in the presence of a hydrodesulphurisation, hydrodenitrification or hydrocracking catalyst in a first reactor at 300-550 degrees C (pref. 300-470 degrees C) and 15-250) atm; (b) passing the effluent to a 1st separator at the same pressure and a temp. of 200-300 degrees C (pref. 250-290 degrees C) to obtain an NH3-redn. rich vapour fraction and a liq. effluent contg. 50 ppm NH3; (c) mixing the liq. effluent with at least part of the bottom product from a subsequent prefractionator; (d) passing the mixt. to a 2nd reactor, where it is treated at 300-550 degrees C (pref. 300-440 degrees C) and 15-250 (pref. 50-250) atm; (e) mixing the effluent from the 2nd reactor with the vapour fraction from the 1st reactor; (f) passing the mixt. to a prefractionator at the same press. as in the 2nd reactor, and stripping it with a gas (pref. H2) to obtain a vapour overhead (H2 + products) and a heavy bottom product (heavy products + unconverted feed); (g) recycling at least part of the bottoms to step (c); and (h) cooling the vapour overhead, separating an H2-rich gas, and fractionating the liq. phase to isolate the required products. Since the NH3 formed in the 1st reactor by-passes the 2nd reactor, the latter can be operated with a conventional NH3-sensitive hydrocracking catalyst. The heavy bottom product from the prefractionator is recycled at the same pressure as that in the 2nd reactor, thus reducing energy consumption.

Process for the production of fuel for internal combustion engines

Patent FR2308397B1

Patent FR2294225B1

PROCEDURE FOR THE HYDROCONVERSION OF OIL WASTE

La presente invención se refiere a procedimiento para la hidroconversión de residuos de petróleo, conteniendo cuando menos aproximadamente 25 por ciento por volúmen de material de ebullición arriba de 538 grados C aproximadamente para producir productos líquidos de hidrocarburo de ebullición inferior, caracterizado porque comprende: (a) cargar un material de residuos de petróleo junto con hidrógeno dentro de una zona de reacción que contiene un lecho de catalizador en ebullición, conservar a la zona de reacción a una temperatura de 399-482ºC, una presión manométrica parcial de hidrógeno de 70.3-35l.5 kilogramos por centímetro cuadrado, y una velocidad espacial de 0.1 - 2.5 Vf/hr/Vr para reacción de fase líquida para producir un material hidroconvertido que contiene una mezcla de fracciones de gas y de líquido; (b) separar la fracción de gas de las fracciones de líquido en una primera zona de separación para proporcionar una primera fracción de gas y una primera fracción de líquido y enfriar la primera fracción de gas a 260 -343ºC para condensar el gas y formar una mezcla de gas y líquido; (c) separar la fracción de gas enfriada de la mezcla en una segunda zona de separación de fase para provocar una segunda fracción de gas y una segunda fracción de líquido y enfriar a la segunda fracción de líquido a menos de 343ºC aproximadamente; (d) reducir la presión de la primera fracción de líquido a una presión manometrica inferior a 70.3 kg/cm2 aproximadamente y escurrir vapor desde la fracción de liquído mientras se mezcla el líquido resultante con cuando menos una porción de la segunda fracción de líquido enfriada para apagar el líquido hasta una temperatura de 393-413ºC, en donde la segunda fracción de líquido enfriada tiene una gravedad API de no más de 22º API aproximadamente más alta que la gravedad API de la primera fracción de líquido; y (e) destilar las fracciones de líquido mezcladas para producir productos líquidos de destilado de hidrocarburo teniendo temperatura ...

Patent FR2311836B1

HYDROCARBON CONVERSION PROCESS FOR THE PRODUCTION IN PARTICULAR OF A PRODUCT CONTAINING HYDROCARBONS WITH TWO CARBON ATOMS

Process to prepare a hydrocarbon product having a sulphur content of below 0.05 wt %

Process to continuously prepare a hydrocarbon product having a specified desired sulphur content lower than 0.05 wt %, starting from at least two or more high-sulphur hydrocarbon feedstocks having a sulphur content of above 0.05 wt %, by (a) blending the two or more of the high-sulphur hydrocarbon feedstocks, to form a blended feed mixture, (b) reducing the sulphur content of the blended feed mixture in a hydrodesulphurisation (HDS) step, (c) obtaining a hydrocarbon fraction, having a reduced sulphur content, comprising the effluent of step (b) and determining the sulphur content of the hydrocarbon fraction, and (d) obtaining the final hydrocarbon product from the direct product of step (c) and adjusting the process to achieve that the sulphur content of the hydrocarbon product is close or equal to the desired sulphur content of the hydrocarbon product, wherein the production of the hydrocarbon product having the desired sulphur content is optimised by integrated control of the blending in step (a) and of the HDS unit operation in step (b), and wherein the sulphur content of the hydrocarbon fraction as determined in step (c) is taken into account.

A process for producing naphthalene from a material containing alkylnaphthalenes

Process for obtaining aromatic products from polycyclic compounds

Abnormal temperature detection for fixed bed reactors

Systems and methods are provided for detecting abnormal temperature conditions within a fixed bed reactor. In a fixed bed reactor, a hydrocarbon (or hydrocarbon-like) feedstock can be exposed to one or more types of catalyst particles at elevated temperatures and/or pressures. In addition to the one or more types of catalyst particles, a plurality of temperature-sensor structures can be included in a catalyst bed and/or a coating including one or more temperature-sensor structures can be provided on an interior wall or other interior surface in the reactor. The temperature-sensor structures can have a threshold temperature at which the temperature-sensor structure changes to allow introduction and/or release of a detectable substance.

A process for the production of low boiling point hydrocarbons using higher boiling point hydrocarbons by the action of hydrogen at elevated temperatures

METHOD AND DEVICE FOR REDUCING HEAVY POLYCYCLIC AROMATIC COMPOUNDS IN HYDROCRACKING UNITS

Gasification of hydrocarbon feedstocks

GASIFICATION OF HYDROCARBON FEED STOCKS Abstract of the Disclosure Hydrocarbon feedstock is first vaporized in the presence of hydrogen and then the vaporized hydrocarbon feedstock together with excess hydrogen, is gasified to form an effluent gas consist-ing essentially of methane and aromatic hydrocarbons together with hydrogen and minor amounts of hydrogen sulfide. The process is suitable for the production of a pipeline gas having a heating value of approximately 1,000 BTU/SCF by further processing the effluent, after separation of the aromatic fraction and hydrogen sulfide from the gasifier effluent; the effluent is subject to cryogenic separation of the hydrogen with the hydrogen being re-cycled to the gasification step and the methane being discharged into a product pipeline. The overall process contemplates re-vaporization of the aromatic fraction separated from the effluent and regasification to extinction of this fraction. Preferred feedstock are crude oil, bitumen produced from tar sands, shale oil,liquid volatiles resulting from coking of coal, liquiefied coal resulting from solvating coal with a solvent and hydrogen, aromatic hydrocarbons, naphtha, gas oils, crude oil distillates, and crude oil residues. It is contemplated that the gasifier effluent could be used as a feedstream for the production of a hydrogen-carbon monoxide synthesis gas, hydrogen, carbon monoxide or as a source of fuel to be burned in place of oil or other liquid hydrocarbons.