КАТАЛИЗАТОР И СПОСОБ РИФОРМИНГА КИСЛОРОДСОДЕРЖАЩИХ СОЕДИНЕНИЙ

Изобретение относится к области химии. Катализатор реформинга в водной фазе включает: а) углеродный носитель, включающий углерод, модифированный титаном, ванадием, вольфрамом или рением, и каталитическую композицию, прикрепленную к углеродному носителю. Каталитическая композиция включает Re и второй металл, выбранный из группы, состоящей из Ir, Ni, Pd, Pt, Rh и Ru, и Ce или La, прикрепленный к углеродному носителю или каталитической композиции. Для реформинга кислородсодержащих углеводородов приводят в контакт сырьевой раствор, включающий воду и по меньшей мере 20 мас.% в расчете на общую массу сырьевого раствора кислородсодержащего углеводорода с катализатором реформинга при условиях температуры реакции и давлении реакции, эффективных для получения газообразного водорода и алканов, имеющих от 1 до 8 атомов углерода. Кислородсодержащий углеводород имеет по меньшей мере один атом кислорода. Катализатор реформинга включает рений и по меньшей мере один переходный металл Группы VIII на водостойком ...

ДОБАВКИ ДЛЯ УДАЛЕНИЯ МЕТАЛЛИЧЕСКИХ ЗАГРЯЗНЯЮЩИХ ПРИМЕСЕЙ

Изобретение относится к композиции и способам для уменьшения вредного действия металлических загрязняющих примесей на каталитический крекинг. Описана добавка для каталитического крекинга, включающая комбинацию: а) улавливающего металлы материала, выбранного из группы, включающей кальцийсодержащее соединение, магнийсодержащее соединение или их сочетание, гидроталькитоподобное соединение, соединение, содержащее диоксид кремния и оксид алюминия, смешанный оксид металлов или их сочетание; и b) высокоактивного катализатора, который представляет собой катализатор, имеющий процентное содержание цеолита по меньшей мере приблизительно в 1,5 раза выше и/или общую площадь поверхности по меньшей мере приблизительно в 1,5 раза больше, и/или общую кристалличность по меньшей мере приблизительно в 1,5 раза выше, чем насыпной катализатор, также используемый в реакции каталитического крекинга. Также описано циркулирующее наличное количество частиц катализатора в способе крекинга с псевдоожиженным катализатором ...

СПОСОБ УВЕЛИЧЕНИЯ МОЛЕКУЛЯРНОГО ВЕСА ОЛЕФИНОВ И УСТАНОВКА ДЛЯ ЕГО ОСУЩЕСТВЛЕНИЯ

Заявленное изобретение относится к способам (варианты) и установкам (варианты) для превращения олефинов, смешанных с парафинами, в соединения с большим молекулярным весом. Более тяжелые соединения могут быть направлены на рециркуляцию в реактор для проведения FCC-процесса или отведены в отдельную установку для проведения FCC-процесса. Способ включает транспортирование C4 олефинов и парафинов и C5-C7 олефинов и парафинов в зону конверсии для превращения C4 олефинов в соединения, производные от C4, имеющие больший молекулярный вес, посредством олигомеризации или алкилирования C4 олефинов с ароматическими соединениями, и превращения C5-C7 олефинов в соединения, производные от C5-C7, имеющие больший молекулярный вес, посредством алкилирования C5-C7 олефинов с ароматическими соединениями; отделение соединений, производных от C4, от C4 олефинов и парафинов; отделение соединений, производных от C5-C7, от C5-C7 олефинов и парафинов; и подачу соединений, производных от C4, и соединений, производных ...

КАТАЛИЗАТОРЫ И СПОСОБЫ РЕФОРМИНГА КИСЛОРОДСОДЕРЖАЩИХ СОЕДИНЕНИЙ

... 1. Способ реформинга кислородсодержащих углеводородов, включающий стадию приведения в контакт сырьевого раствора, включающего воду и по меньшей мере 20 мас.%, в расчете на общую массу сырьевого раствора, кислородсодержащего углеводорода, с катализатором реформинга при условиях температуры реакции и давления реакции, эффективных для получения газообразного водорода и алканов, имеющих от 1 до 8 атомов углерода, где кислородсодержащий углеводород имеет по меньшей мере один атом кислорода и где катализатор реформинга включает рений и по меньшей мере один переходный металл группы VIII на водостойком носителе. ! 2. Способ по п.1, где конверсия в газообразный водород больше с катализатором реформинга, чем конверсия в газообразный водород при использовании аналогичного сырьевого раствора и аналогичного катализатора с отсутствием рения. ! 3. Способ по п.1, где конверсия в алканы с катализатором реформинга больше, чем конверсия в алканы при использовании аналогичного сырьевого раствора и аналогичного ...

Generating a fuel useful for operating an internal combustion engine, e.g. an automobile, comprises supplying carbon dioxide, supplying hydrogen from water, and synthesizing methanol from supplied carbon dioxide and hydrogen

Generating a fuel comprises (a) supplying carbon dioxide (6), (b) supplying hydrogen (11) from water (9), and (c) synthesizing methanol (12) from the supplied carbon dioxide and hydrogen, where the carbon dioxide provided in the step (a) is provided by a flue gas (4), which is obtained by the combustion of a fuel.

Process of hydrocarbon conversion.

Catalyst for light olefins and LPG in fluidized catalytic units

A catalyst composition comprising at least about 10% by weight pentasil, at least about 12% by weight Y-type zeolite at a pentasil to Y zeolite ratio of at least 0.25, and wherein the pentasil and Y zeolite comprise at least about thirty-five percent of the catalyst have been shown to optimize light olefin yields and LPG from FCC processes. Embodiments having matrix surface areas greater than 25m/g, phosphorous and rare earth are preferred. The compositions of this invention are particularly useful in typical fluid catalytic cracking (FCC) processes.

PROCESS FOR FLUID CATALYTIC CRACKING OF HYDROCARBON FEEDSTOCKS WITH HIGH LEVELS OF BASIC NITROGEN

PROCESS FOR PREPARING HYDROCARBONS

MATERIAL DELIVERY SYSTEM TO ONE OR MORE UNITS AND METHODS OF SUCH DELIVERY

Material delivery systems and methods are disclosed. A material delivery system includes a delivery vessel and at least one dispense mechanism outlet. The delivery vessel is configured to deliver material to at least one unit, with the proviso that when the unit is an FCC unit, the unit includes a plurality of units. The at least one dispense mechanism outlet is configured to couple the delivery vessel to the at least one unit. A method includes providing a material to at least one unit. The method includes dispensing material from a delivery vessel, wherein a metering device provides a metric indicative of the dispensed material with respect to at least a unit, and delivering the metered material to at least one unit via at least one dispense mechanism outlet of the delivery vessel coupled to the at least one unit. Another method includes providing a material to a plurality of units.

PROCESS FOR THE PREPARATION OF HYDROCARBONS

ABSTRACT PROCESS FOR THE PREPARATION OF HYDROCARBONS A C3/C4 fraction obtained as a by-product in the preparation of aromatic gasoline from synthesis gas over a crystalline aluminium or iron silicate comprising catalyst system, is converted into aromatic gasoline by partial oxidation or partial dehydrogenation followed by conversion over a crystalline aluminium or iron silicate catalyst of the partial oxidation or dehydrogenation product.

CONVERSION OF SYNTHESIS GAS TO HYDROCARBON MIXTURES UTILIZING DUAL REACTORS

ADDITIVES FOR METAL CONTAMINANT REMOVAL

... ²²²The present invention is directed to catalytic cracking additives comprising a ²metals trapping material; and a high activity catalyst. The present invention ²is directed to processes for the catalytic cracking of feedstock comprising ²contacting said feedstock under catalytic cracking conditions with a ²composition comprising a bulk catalyst and a catalytic cracking additive, ²wherein the catalytic cracking additive comprises a metals trapping material; ²and a high activity catalyst. The invention is also directed to processes for ²increasing the performance of a bulk catalyst in the presence of at least one ²metal comprising contacting a feedstock with a catalytic cracking additive ²comprising a metals trapping material; and a high activity catalyst.² ...

APPARATUS AND PROCESS FOR PRODUCING GASOLINE, OLEFINS AND AROMATICS FROM OXYGENATES

Apparatuses and processes for converting an oxygenate feedstock, such as methanol and dimethyl ether, in a fluidized bed containing a catalyst to hydrocarbons, such as gasoline boiling components, olefins and aromatics are provided herein.

METHOD AND APPARATUS FOR PRODUCING SYNTHETIC HYDROCARBONS

The invention relates to a method for producing synthetic hydrocarbons, wherein synthesis gas is produced in that, in a step a), carbon is brought in contact with water or a mixture of carbon and hydrogen is brought in contact with water, namely at a temperature of 800 - 1700 °C. Thereafter, in a step b), the synthesis gas is converted into synthetic, functionalized, and/or non-functionalized hydrocarbons by means of a Fischer-Tropsch process, wherein the synthesis gas is brought in contact with a suitable catalyst, and wherein water arises as a by-product, in which water a part of the synthetic hydrocarbons is dissolved. Then, in a step c), at least a part of the water produced as a by-product is fed to step a). The hydrocarbons dissolved in the water decompose into particulate carbon and hydrogen at the high temperature in step a). The carbon is converted into CO in the presence of water and at high temperature in step a). In this way, expensive purification of half of the water produced ...

DESULFURIZATION SYSTEM FOR HYDROCARBON FUEL

The present invention provides a desulfurization system for desulfurizing a hydrocarbon fuel containing a light amount of methanol and a slight amount of water. The desulfurization system comprises a Y-type zeolite-based desulfurizing agent containing at least copper arranged upstream of the system and an X-type zeolite-based desulfurizing agent containing at least silver arranged downstream of the system and thus can maintain desulfurization effect for a long period of time.

CONFIGURATIONS AND METHODS FOR IMPROVED NATURAL GAS LIQUIDS RECOVERY

Contemplated plants for recovery of NGL from natural gas employ alternate reflux streams in a first column and a residue gas bypass stream, wherein expansion of various process streams provides substantially all of the refrigeration duty in the plant. Contemplated plants not only have flexible recovery of ethane between 2% and 90% while recovering at least 99% of propane, but also reduce and more typically eliminate the need for external refrigeration.

BIOGASOLINE

A process for the preparation of a biogasoline component comprising: (I) obtaining at least one biooil and, if necessary, liquefying the biooil compo nent; (II) adding the bio-oil in liquid form to a FCC unit along with at lea st one mineral oil; (III) cracking the components added to the FCC unit to f orm at least a bio-LPG fraction and a bio-naphtha fraction; (IV) alkylating or catalytically polymerising at least part of the bio-LPG fraction; and (V) combining at least a part of the product of step (IV) with at least a part of the bio-naphtha fraction to form a bio-gasoline component.

INTEGRATED CRUDE REFINING WITH REDUCED COKE FORMATION

Methods are provided for processing crude oil feeds with reduced or minimized energy usage, reduced or minimized numbers of processing steps, improved allocation of hydrogen, and reduced or minimized formation of low value products. The methods reduce or minimize the use of vacuum distillation, and in many aspects reduce or minimize the use of both atmospheric and vacuum distillation. The methods also reduce or minimize the use of coking and fluid catalytic cracking processes.

SYSTEMS AND METHODS FOR PRODUCING A CRUDE PRODUCT

A flexible once-through process for hydroprocessing heavy oil feedstock is disclosed. The process employs a plurality of contacting zones and at least a separation zone to convert at least a portion of the heavy oil feedstock to lower boiling hydrocarbons, forming upgraded products. The contacting zones operate under hydrocracking conditions, employing a slurry catalyst which comprises an active metal catalyst having an average particle size of at least 1 micron in a hydrocarbon oil diluent, at a concentration of greater than 500 wppm of active metal catalyst to heavy oil feedstock. The plurality of contacting zones and separation zones are configured in a permutable fashion allowing the once-through process to be flexible operating in various modes: a sequential mode; a parallel mode; a combination of parallel and sequential mode; all online; some online and some on stand-by; some online and some off-line; a parallel mode with the effluent stream from the contacting zone being sent to ...

Procédé pour effectuer une réaction chimique

METHOD OF PRODUCING LPG AND BTX

METHOD OF PRODUCING C2 AND C3 HYDROCARBONS

METHOD OF EXTRACTING GAS-CONDENSATE LIQUID POSTS FROM NATURAL GAS, OBTAINED IN REMOTE PLACES

CONFIGURATIONS AND METHODS FOR THE INCREASED EXTRACTION OF THE GAS-CONDENSATE LIQUIDS

SYSTEM AND METHODS FOR PREPARING CRUDE PRODUCT

ДОБАВКА ДЛЯ КАТАЛИТИЧЕСКОГО КРЕКИНГА, СПОСОБ КАТАЛИТИЧЕСКОГО КРЕКИНГА ИСХОДНОГО СЫРЬЯ С ЕЕ ИСПОЛЬЗОВАНИЕМ И ЦИРКУЛИРУЮЩАЯ МАССА ЧАСТИЦ КАТАЛИЗАТОРА

Данное изобретение касается добавок для каталитического крекинга, которые содержат материал, способный улавливать металлы, и высокоактивный катализатор. Данное изобретение касается способов каталитического крекинга исходного сырья, которое включает осуществление контакта указанного исходного сырья в условиях каталитического крекинга с составом, который включает насыпной катализатор и добавку для каталитического крекинга, в которых добавка для каталитического крекинга включает материал, способный улавливать металлы, и высокоактивный катализатор. Данное изобретение также касается способов улучшения рабочих характеристик насыпного катализатора в присутствии как минимум одного металла, которые включают осуществление контакта исходного сырья с добавкой для каталитического крекинга, которая включает материал, способный улавливать металлы, и высокоактивный катализатор.

METHOD OF PRODUCING BEFRACHTUNGS AND CIS

СПОСОБ И УСТРОЙСТВО ДЛЯ УМЕНЬШЕНИЯ СОДЕРЖАНИЯ ДОБАВОК В УГЛЕВОДОРОДНОМ ПОТОКЕ

Способ уменьшения содержания одной или более добавок в газообразном углеводородном потоке (40), включающий стадии: (a) смешение потока (10) исходного углеводородного сырья с одной или более добавками (20), в результате чего образуется многофазный углеводородный поток (30); (b) транспортирование многофазного углеводородного потока (30) от первого участка (А) ко второму участку (В2); (c) на втором участке (В2), пропускание многофазного углеводородного потока (30) через сепаратор (22), в результате чего образуется один или более жидких потоков (50), содержащих большую часть одной или более добавок, и газообразный углеводородный поток (40), содержащий остаток одной или более добавок; и (d) промывание потока газообразного углеводородного потока (40) в очистном блоке (24) промывочным потоком (60), который (промывочный поток (60)) содержит дистиллированную воду, в результате чего образуется обогащенный добавкой(ами) поток (70) и углеводородный поток (80) с пониженным содержанием добавок.

Two=stage hydrocracking of heavy feeds - for prodn. of gasoline and liquefied petroleum gas; uses oxide and noble metal-zeolite catalysts

Process of hydrocarbon reformation

PROCESS FOR THE PRODUCTION OF LIQUEFIED PETROLEUM GAS

Proceso para producir un producto diesel rico en parafinas, desde una materia prima renovable, que comprende tratar la materia prima en una primera zona de reaccion usando catalizador en presencia de hidrogeno y al menos un componente que contiene azufre en una cantidad superior a 1000 ppm/p de azufre, medido como azufre elemental.

Proceso para producir un producto diesel rico en parafinas, desde una materia prima renovable, que comprende tratar la materia prima en una primera zona de reacción usando catalizador en presencia de hidrógeno y al menos un componente que contiene azufre en una cantidad superior a 1000 ppm/p de azufre, medido como azufre elemental.

CONTROLLING COLD FLOW PROPERTIES OF TRANSPORTATION FUELS FROM RENEWABLE FEEDSTOCKS

A process for improving cold flow properties of diesel range hydrocarbons produced from renewable feedstocks such as plant oils and animal oils. A renewable feedstock is treated by hydrogenating and deoxygenating to provide an effluent comprising paraffins followed by isomerizing and selectively hydrocracking at least a portion of the paraffins to generate a diesel range hydrocarbon product. A portion of the diesel range hydrocarbon product is selectively separated and recycled to the isomerization and selective hydrocracking zone.

SYSTEMS AND METHODS FOR PRODUCING A CRUDE PRODUCT

A flexible once-through process for hydroprocessing heavy oil feedstock is disclosed. The process employs a plurality of contacting zones and at least a separation zone to convert at least a portion of the heavy oil feedstock to lower boiling hydrocarbons, forming upgraded products. The contacting zones operate under hydrocracking conditions, employing a slurry catalyst which comprises an active metal catalyst having an average particle size of at least 1 micron in a hydrocarbon oil diluent, at a concentration of greater than 500 wppm of active metal catalyst to heavy oil feedstock. The plurality of contacting zones and separation zones are configured in a permutable fashion allowing the once-through process to be flexible operating in various modes: a sequential mode; a parallel mode; a combination of parallel and sequential mode; all online; some online and some on stand-by; some online and some off-line; a parallel mode with the effluent stream from the contacting zone being sent to ...

CATALYTIC PROCESS FOR CHANGING GLYCERINE INTO IN PUTS FOR THE PETROCHEMICAL FIELD

The present invention refers to a catalytic process of hydrogenation/hydrogenolysis of glycerol or glycerine into oxygenated compounds and hydrocarbons containing 1 to 3 carbon atoms, using supported metal catalysts based on metals from group VIII-B of the periodic table of the elements, which have been supported by standard techniques on materials having a high specific area, such as powder charcoal, aluminum silicate, alumina, clays, zeolites and molecular sieves.

METHOD AND APPARATUS FOR TREATING A HYDROCARBON STREAM

A method of treating a hydrocarbon stream such as natural gas comprising at least the steps of: (a) providing a hydrocarbon feed stream (10); (b) passing the feed stream (10) through a first separation vessel (12) to provide a first gaseous stream (20) and a first liquid stream (30); (c) passing the first gaseous stream (20) from step (b) through a high pressure separation vessel (14) to provide a second gaseous stream (40) and a second liquid stream (80); (d) maintaining the pressure of the first gaseous stream (20) between step (b) and step (c) within +10 bar; (e) passing the first liquid stream (30) of step (b) through a stabilizer column (16) to provide a third gaseous stream (60) and a stabilized condensate (70); and (f) feeding the second liquid stream (80) from step (c) into the stabilizer column (16).

METHOD FOR PRODUCING A FUEL FOR INTERNAL COMBUSTION ENGINES

The method according to the invention for producing a fuel (14, 15, 16) for internal combustion engines comprises the following steps: a) providing carbon dioxide (C02) (6); b) providing hydrogen (H2) (11) from water (H20) (9); and c) synthesizing methanol (CH3OH) (12) from the provided carbon dioxide (6) and hydrogen (11). The method according to the invention is characterized in that the carbon dioxide (6) provided in step a) is provided from the flue gas (4) of the combustion of a fuel (2). A further method step d) of a process (13, 17) for converting the methanol (12) into a fuel (14, 15, 16, 18) is preferably carried out subsequent to step c); particularly preferably said process is a methanol-to-gasoline (MTG) process (13). The method according to the invention advantageously permits the reprocessing of carbon dioxide (6) from the flue gas (4) from power plants (1) and the use thereof for synthesizing fuels (14, 15, 16), in particular gasoline fuel (14), for operating internal combustion ...

PROCESS FOR FLUID CATALYTIC CRACKING OF HYDROCARBON FEEDSTOCKS WITH HIGH LEVELS OF BASIC NITROGEN

A process is described for fluid catalytic cracking of hydrocarbons with high levels of basic nitrogen, where hydrocarbon feedstocks A and B with different levels of basic nitrogen are injected in a segregated fashion, into different risers of a multiple riser FCCU that possesses at least two risers. The injection of the feedstocks is made in such a way that feedstock A, to be injected in the riser with greater volume - main riser (7) - possessing a level of basic nitrogen at least 200 ppm lower than the level of feedstock B to be injected into the riser with lower volume - secondary riser (8).

PROCESS AND APPARATUS FOR IMPROVING FLOW PROPERTIES OF CRUDE PETROLEUM

A process for improving flow properties of crude may include processing a first crude stream (5), which may in turn include cracking the first crude stream with fresh catalyst to form a cracked stream (53) and spent catalyst. The spent catalyst may be regenerated to form fresh catalyst, which may then be recycled. At least part of the cracked stream (53) may be mixed with a second crude stream (499). A ratio of part of the cracked stream to add to the second crude stream may be selected to achieve an API gravity of at least about 18. The first crude stream (5) may be heated and stripped before being cracked.

HYDROCONVERSION PROCESS FOR PRODUCTION OF LPG IN PRESENCE OF MORDENITE ALUMINOSILICATE

PROCESS FOR PRODUCING C2 AND C3 HYDROCARBONS

The invention relates to a process for producing C2 and C3 hydrocarbons, comprising a) subjecting a mixed hydrocarbon carbon stream comprising a middle distillate to first hydrocracking in the presence of a first hydrocracking catalyst to produce a first hydrocracking product stream, b) subjecting a second hydrocracking feed stream to second hydrocracking in the presence of a second hydrocracking catalyst to produce a second hydrocracking product stream, wherein the second hydrocracking is more severe than the first hydrocracking and c) subjecting a C4 hydrocracking feed stream to C4 hydrocracking optimized for converting C4 hydrocarbons into C3 hydrocarbons in the presence of a C4 hydrocracking catalyst to obtain a C4 hydrocracking product stream, wherein the C4 hydrocracking is more severe than the second hydrocracking, wherein the first hydrocracking product stream, the second hydrocracking product stream and the C4 hydrocracking product stream are fed to a separation system which provides —the second hydrocracking feed stream separated from the first hydrocracking product stream, —the C4 hydrocracking feed stream separated from the second hydrocracking product stream, —a first recycle stream to be recycled back to the first hydrocracking, —a second recycle stream to be recycled back to the second hydrocracking, —a third recycle stream to be recycled back to the C4 hydrocracking, —a hydrogen recycle stream of H2 or H2 and C1 to be recycled back to the first hydrocracking, the second hydrocracking and/or the C4 hydrocracking and —a C2 and C3 product stream of C3− hydrocarbons, wherein the second hydrocracking feed stream is a stream of C12− hydrocarbons excluding C10-C12 hydrocarbons having di-ring structures, wherein the first recycle stream is a stream of C13+ and C10-C12 hydrocarbons having di-ring structures, wherein the C4 hydrocracking feed stream is a stream of C5−, C4− or iC4−, wherein the second recycle stream is a stream of C6+, C5+ or nC4+ 30 wherein ...

METHOD AND APPARATUS FOR PRODUCING HYDROCARBONS

A method for producing hydrocarbons is proposed wherein a catalysis product stream (b) rich in n-butane, isobutane, 1-butene, 2-butene, isobutene and hydrocarbons with more than four and/or less than four carbon atoms is produced in a catalysis unit (1), using one or more catalyst feed streams containing oxygenates and/or olefins (a) and wherein additionally a steam cracking product stream (h) is produced in a steam cracking unit (2) using one or more steam cracking feed streams (g, r, s). It is provided that using the catalysis product stream (b) a skeletal isomerisation feed stream (f, q) poor in 1-butene, 2-butene and isobutene and containing at least isobutane is produced, in which the isobutane is at least predominantly reacted by skeletal isomerisation to form n-butane, and which is subsequently used at least partly as the, or one of the, steam cracking feed streams (g, r). The invention also relates to an apparatus (100, 200).

Process for the preparation of light fuels

In the process of the invention, an aliphatic C2-C14 hydrocarbon product is prepared from natural fats or derivatives thereof. The process comprises the steps of: (i) providing a natural fat or derivative thereof, (ii) deoxygenating a natural fat or derivative thereof originating from step (i) to yield an aliphatic C9-C28 hydrocarbon, (iii) hydrocracking an aliphatic C9-C28 hydrocarbon originating from step (ii) to yield a product comprising an aliphatic C2-C14 hydrocarbon, (iv) isomerising an aliphatic C2-C14 hydrocarbon originating from step (iii) into an isomerised aliphatic C2-C14 hydrocarbon, and optionally (v) recovering an isomerised C2-C14 hydrocarbon originating from step (iv) as said C2-C14 hydrocarbon product. Pure and high quality light fuel is easily obtained in sufficient amounts.

METHOD OF PROCESSING OIL REFINING WASTE

SYSTEMS AND METHODS FOR PRODUCING A CRUDE PRODUCT

УСОВЕРШЕНСТВОВАННЫЙ ПАССИВАТОР/ЛОВУШКА МЕТАЛЛА ДЛЯ ПРОЦЕССОВ КФК

FIELD: metallurgy. SUBSTANCE: present invention relates to a method of passivating and/or trapping at least one metal impurity from a liquid oil product in cracking apparatus on fluidised catalyst, comprising: contacting said liquid oil product, which contains at least one metal impurity, with a catalytic mixture containing 1) cracking catalyst on fluidised catalyst and 2) metal passivator/trap, which contain mixed metal oxide alloy of R, Sb, and optionally M, where R is Fe 2+/3+ and M is an optional activator. EFFECT: technical result is increased output of end products (selectivity with respect to transport fuel) due to reduced effect of catalyst deactivation by means of metal impurities in liquid oil products. 20 cl, 3 dwg, 6 tbl, 4 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 603 964 C2 (51) МПК C10G 11/18 (2006.01) B01J 38/00 (2006.01) B01J 29/90 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ (21)(22) Заявка: ИЗОБРЕТЕНИЯ К ПАТЕНТУ 2014125128/04, 21.11.2011 (24) Дата начала отсчета срока действия патента: 21.11.2011 (72) Автор(ы): ХОФФЕР Брам У. (US), СТОКУЭЛЛ Дейвид М. (US) (73) Патентообладатель(и): БАСФ КОРПОРЕЙШН (US) (43) Дата публикации заявки: 27.12.2015 Бюл. № 36 R U Приоритет(ы): (22) Дата подачи заявки: 21.11.2011 (45) Опубликовано: 10.12.2016 Бюл. № 34 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 23.06.2014 (86) Заявка PCT: 2 6 0 3 9 6 4 (56) Список документов, цитированных в отчете о поиске: US 4321129 A, 23.03.1982. US 4370220 А, 25.01.1983. US 6110357 A, 29.08.2000. US 4335021 A, 15.06.1982. RU 2283177 C2, 10.09.2006. EP 0461851 A2, 18.12.1991. 2 6 0 3 9 6 4 R U (87) Публикация заявки PCT: WO 2013/077836 (30.05.2013) Адрес для переписки: 105082, Москва, Спартаковский пер., д. 2, стр. 1, этаж 3, "ЕВРОМАРКПАТ" (54) УСОВЕРШЕНСТВОВАННЫЙ ПАССИВАТОР/ЛОВУШКА МЕТАЛЛА ДЛЯ ПРОЦЕССОВ КФК (57) Реферат: Настоящее изобретение относится к способу которые содержат смешанный сплав оксида пассивирования и/или ...

СПОСОБ ИЗВЛЕЧЕНИЯ СНГ

РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2018 115 230 A (51) МПК C10G 5/02 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21)(22) Заявка: 2018115230, 21.09.2016 (71) Заявитель(и): ХАЛЬДОР ТОПСЁЭ А/С (DK) Приоритет(ы): (30) Конвенционный приоритет: (72) Автор(ы): ПХУ Нгхиа Пхам (DK) 25.09.2015 DK PA 2015 00563 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 25.04.2018 R U (43) Дата публикации заявки: 25.10.2019 Бюл. № 30 (86) Заявка PCT: (87) Публикация заявки PCT: WO 2017/050795 (30.03.2017) A Адрес для переписки: 105064, Москва, а/я 88, ООО "Патентные поверенные Квашнин, Сапельников и партнеры" R U (57) Формула изобретения 1. Способ извлечения СНГ из секции фракционирования процесса нефтепереработки, включающий стадии: (a) пропускания сырьевого потока, включающего головной продукт десорбера, через губчатый абсорбер и выделения потока отходящего газа из верхней секции губчатого абсорбера и потока легких фракций нефти из нижней секции губчатого абсорбера; (b) фракционирования потока легких фракций нефти на (i) головной пар в виде потока десорбированного С3, содержащего менее 20% бутана или пропана, без конденсации и без рециркуляции сконденсированного головного пара в эту стадию фракционирования, (ii) поток продукционного СНГ и (iii) поток стабилизированной нафты. 2. Способ по п. 1, дополнительно включающий смешивание по меньшей мере части потока десорбированного С3 стадии (b) с головным продуктом десорбера для получения указанного на стадии (а) сырьевого потока. 3. Способ по п. 1, дополнительно включающий смешивание части потока стабилизированной нафты стадии (b) с потоком отходящего газа стадии (а). 4. Способ по п. 1, в котором стадия (b) включает подстадии: (b1) фракционирования потока легких фракций нефти в этаноотгонной колонне и выделения головного пара в виде указанного потока десорбированного С3 из верхней Стр.: 1 A 2 0 1 8 1 1 5 2 3 0 (54) СПОСОБ ИЗВЛЕЧЕНИЯ СНГ 2 0 1 8 1 1 5 2 3 0 EP 2016/072356 (21. ...

СПОСОБ ПЕРЕРАБОТКИ ОТХОДОВ ПЕРЕРАБОТКИ НЕФТИ

... 1. Способ переработки отходов переработки нефти, включающий подачу отхода в аппарат и нагрев отхода таким образом, чтобы выделить летучие углеводороды, где отход нагревают, используя дальнее инфракрасное излучение, и где выделенные летучие углеводороды собирают для последующего использования. ! 2. Способ по п.1, дополнительно включающий подачу в котел пластмасс. ! 3. Способ по п.1 или 2, в котором дальнее инфракрасное излучение обеспечивается множеством нагревателей дальнего инфракрасного излучения, каждый из которых по меньшей мере частично погружен в отход. ! 4. Способ по п.3, в котором нагреватели дальнего инфракрасного излучения находятся в виде керамических стержневых элементов, защищенных гильзами из нержавеющей стали, которые покрыты излучающим соединением. ! 5. Способ по п.1 или 2, где отход нагревают до температуры, лежащей в интервале от примерно 360°С до примерно 450°С. ! 6. Способ по п.1 или 2, где летучие углеводороды собирают, используя флегмируемую фракционирующую колонну ...

ДОБАВКИ ДЛЯ УДАЛЕНИЯ МЕТАЛЛИЧЕСКИХ ЗАГРЯЗНЯЮЩИХ ПРИМЕСЕЙ

... 1. Добавка для каталитического крекинга, включающая а) улавливающий металлы материал; и b) высокоактивный катализатор. 2. Добавка для каталитического крекинга по п.1, где улавливающий металлы материал составляет приблизительно от 2 до 98 мас.% добавки. 3. Добавка для каталитического крекинга по п.1, где улавливающий металлы материал составляет приблизительно от 10 до 95 мас.% добавки. 4. Добавка для каталитического крекинга по п.1, где улавливающий металлы материал составляет приблизительно от 70 до 90 мас.% добавки. 5. Добавка для каталитического крекинга по п.1, где высокоактивный катализатор составляет приблизительно от 5 до 60 мас.% добавки. 6. Добавка для каталитического крекинга по п.1, где улавливающий металлы материал и высокоактивный катализатор составляют отдельные частицы. 7. Добавка для каталитического крекинга по п.1, где улавливающий металлы материал и высокоактивный катализатор находятся внутри одной и той же частицы. 8. Добавка для каталитического крекинга по п.1, где улавливающий ...

VERFAHREN ZUR HERSTELLUNG VON ISOPARAFFINEN MIT HOHER OKTANZAHL UND DEM SIEDEBEREICH VON MOTORKRAFTSTOFFEN UND PROPAN

ISOMERIZING AND HYDROCRACKING PARAFFINS

... 1433730 Isomerization - hydrocracking CHEVRON RESEARCH CO 9 Sept 1974 [10 Sept 1973] 39344/74 Heading C5E A process for producing a gasoline boiling range isoparaffin fraction and a propane-rich fraction from a low octane C 5 -C 6 paraffin feedstock comprises (a) catalytically isomerizing the feedstock to give an effluent comprising isoparaffins and n-paraffins, (b) feeding at least part of the effluent, without separating the iso- and n-paraffins, to a hydrocracking zone containing a shape selective hydrocracking catalyst comprising a hydrogenating component and a zeolite of pore size 4-6À5 Š thereby selectively hydrocracking the n-paraffins to give an effluent which is separated into the required isoparaffin fraction and propane-rich fraction. The isomerization may be carried out at 400-900‹ F. in the presence of added H 2 using as catalyst a Group VIII metal or metal compound on an acidic inorganic oxidic support, such as a zeolite or synthetic clay. The shape selective hydrocracking ...

Process for preparing hydrocarbons

Coal is gasified to a mixture of CO and H2. The mixture is converted to a hydrocarbon mixture over a catalyst containing a crystalline iron silicate. From the hydrocarbon mixture isobutane and an aromatic gasoline fraction are separated. The isobutane is converted by alkylation into a product from which a gasoline fraction is separated. The two gasoline fractions are mixed. The catalyst employed may be a mixture of crystalline iron silicate with either (1) a Fe/Cu/K/SiO2 Fischer-Tropsch catalyst and a Cu/Zn CO shift catalyst, or (2) a ZnO-Cr2O3 composition serving to catalyse both the reduction of CO to methanol and the water gas shift reaction.

Converting biomass to gasoline

Converting biomass to gasoline

The present invention relates to a process and system for forming a bio-derived gasoline fuel from a biomass material, and the bio-derived gasoline fuel formed therefrom. The present invention also relates to a process and system for forming a bio-derived gasoline fuel from a bio-derived hydrocarbon feedstock, and the bio-derived gasoline fuel formed therefrom. The process comprises providing a biomass feedstock, ensuring the feedstock has a moisture content of 10% or less, pyrolyzing the feedstock at a temperature of at least 950 degrees C to form a mixture of biochar, hydrocarbon feedstock, non-condensable light gases, such as hydrogen, carbon monoxide, carbon dioxide and methane, and water, separating the hydrocarbon feedstock from the mixture formed above, hydrocracking the hydrocarbon feedstock, in the presence of a hydrocracking catalyst and a hydrogen containing gas to produce a bio-oil, and fractionating the resulting bio-oil to obtain a bio-derived gasoline fuel fraction.

Configurations and methods for improved natural gas liquids recovery

Contemplated plants for recovery of NGL from natural gas employ alternate reflux streams in a first column and a residue gas bypass stream, wherein expansion of various process streams provides substantially all of the refrigeration duty in the plant. Contemplated plants not only have flexible recovery of ethane between 2% and 90% while recovering at least 99% of propane, but also reduce and more typically eliminate the need for external refrigeration.

PROCESS FOR PREPARING GASOLINE FROM COAL

LIQUEFIED PETROLEUM GAS FOR LP GAS FUEL CELL, METHOD OF DESULFURIZING THE SAME AND FUEL CELL SYSTEM

A petroleum gas fuel for LP gas fuel cell to be fed to a fuel cell system according to a natural vaporization supply method, wherein the content of C2 hydrocarbon compounds is 3 vol.% or less, the content of C4 hydrocarbon compounds 3 vol.% or less, the total sulfur concentration 10 mass ppm or less, the concentration of sulfur of carbonyl sulfide 2 mass ppm or less, the concentration of sulfur of methylmercaptan 3 mass ppm or less, the concentration of sulfur of sulfur compounds whose boiling point is equal to or higher than that of dimethyl disulfide 2 mass ppm or less, the methanol concentration 50 mass ppm or less, the water concentration 50 mass ppm or less and the balance constituted of C3 hydrocarbon compounds. In the petroleum gas fuel for LP gas fuel cell, desulfurizing agents even when added in a minimum amount, efficiently function to thereby attain an enhancement of desulfurization effect and prevent damaging of a reforming catalyst lying in a reformer for hydrogen production ...

A PROCESS FOR PRODUCING HYDROCARBON FLUIDS COMBINING IN SITU HEATING, A POWER PLANT AND A GAS PLANT

An in situ method of producing hydrocarbon fluids from an organic-rich rock formation is provided. The method may include heating an organic-rich rock formation, for example an oil shale formation, in situ to pyrolyze formation hydrocarbons, for example kerogen, to form a production fluid containing hydrocarbon fluids. The method may include separating the production fluid into at least a gas stream and a liquid stream, where the gas stream is a low BTU gas stream. The low BTU gas stream is then fed to a gas turbine where it is combusted and is used to generate electricity.

SYSTEMS, APPARATUS, AND METHODS OF A DOME RETORT

A system, apparatus and method for hydrocarbon extraction from feedstock material that is or includes organic material, such as oil shale, coal, lignite, tar sands, animal waste and biomass. A retort system including at least one retort vessel may include a monolithic dome structure surrounded by a process isolation barrier, the dome structure being sealingly engaged with the process isolation barrier. The dome structure and the process isolation barrier define a retort chamber, at least a portion of which may comprise a subterranean chamber. A lower end of the dome retort structure provides an exit for collected hydrocarbons and spent feedstock material. Systems may include a plurality of such dome retort structures. A control system may be used for controlling one or more operating parameters of a retorting process performed within such a dome retort structure for extraction and collection of hydrocarbons.

METHODS FOR PRODUCING LINEAR PARAFFINS AND OLEFINS FROM NATURAL OILS

A method for producing a linear paraffin includes providing a natural oil in a feed stream, deoxygenating the natural oil to form a stream comprising paraffins, purifying the stream comprising paraffins to form a purified stream comprising paraffins, and separating a first fraction of paraffin product from the purified stream comprising paraffins. A method for producing a linear olefin includes providing a natural oil in a feed stream, deoxygenating the natural oil to form a stream comprising paraffins, dehydrogenating the stream comprising paraffins to form a stream comprising olefins, purifying the stream comprising olefins to form a purified stream comprising olefins, and separating a first fraction of olefin product from the purified stream comprising olefins.

УСТАНОВКА И СПОСОБ ДЛЯ ПОВЫШЕННОГО ИЗВЛЕЧЕНИЯ ГАЗОКОНДЕНСАТНЫХ ЖИДКОСТЕЙ

В рассматриваемых установках для извлечения ГКЖ из природного газа применяются чередующиеся потоки флегмы в первой колонне и обводной поток остаточного газа, причем расширение различных технологических потоков обеспечивает, по существу, весь режим охлаждения в установке. Рассматриваемые установки имеют не только гибкое извлечение этана в диапазоне между 2 и 90% при извлечении по меньшей мере 99% пропана, но и снижение, а в более типичном случае исключение необходимости внешнего охлаждения.

METHOD OF PRODUCING LPG AND BTX

METHOD OF REFINING HEAVY HYDROCARBONS OIL REFINING IN PETROCHEMICAL PRODUCTS

СИСТЕМЫ И СПОСОБЫ ПОЛУЧЕНИЯ СЫРОГО ПРОДУКТА

Системы и способы для гидропереработки исходного сырья на основе тяжелой нефти при уменьшенном образовании отложений в тяжелой нефти, при этом система использует множество зон введения в контакт и зон разделения в условиях проведения гидрокрекинга для превращения по меньшей мере части исходного сырья на основе тяжелой нефти в более низкокипящие углеводороды с получением облагороженных продуктов, где в первую зону введения в контакт необязательно нагнетают воду и/или водяной пар в количестве от 1 до 25 мас.% от массы исходного сырья на основе тяжелой нефти. В одном варианте осуществления первая зона введения в контакт функционирует при температуре, по меньшей мере, на 10°F (5,56°С) меньшей, чем в последующей зоне введения в контакт. Зоны введения в контакт функционируют в условиях проведения гидрокрекинга при использовании суспензионного катализатора для облагораживания исходного сырья на основе тяжелой нефти с получением облагороженных продуктов в виде более низкокипящих углеводородов.

METHOD OF PRODUCING HYDROCARBONS C2 AND C3

METHOD OF CONVERSION OF HIGH BOILING HYDROCARBON MATERIAL IN MORE EASILY KIPYaShchIE HYDROCARBON PRODUCTS ARE

СПОСОБ И УСТРОЙСТВО ДЛЯ УМЕНЬШЕНИЯ СОДЕРЖАНИЯ ДОБАВОК В УГЛЕВОДОРОДНОМ ПОТОКЕ

Способ уменьшения содержания одной или более добавок в газообразном углеводородном потоке (40), включающий стадии: (a) смешения потока (10) исходного углеводородного сырья с одной или более добавками (20), в результате чего образуется многофазный углеводородный поток (30); (b) транспортирования многофазного углеводородного потока (30) от первого участка (А) ко второму участку (В2); (c) на втором участке (В2), пропускания многофазного углеводородного потока (30) через сепаратор (22), в результате чего образуется один или более жидких потоков (50), содержащих большую часть одной или более добавок, и газообразный углеводородный поток (40), содержащий остаток одной или более добавок; и (d) промывания потока газообразного углеводородного потока (40) в очистном блоке (24) промывочным потоком (60), который (промывочный поток (60)) содержит дистиллированную воду, в результате чего образуется обогащённый добавкой(ами) поток (70) и углеводородный поток (80) с пониженным содержанием добавок.

КАТАЛИЗАТОР И СПОСОБ РИФОРМИНГА ОКИСЛЕННЫХ СОЕДИНЕНИЙ

A process for producing hydrocarbon fluids combining in situ heating, a power plant and a gas plant

PROCEEDED Of HYDROCRAQUAGE FOR the PRODUCTION OF PETROLEUM GAS LIQUIFIES

Hydrocraquage of paraffinic hydrocarbons

Process for hydrogenative cracking of naphthenic - hydrocarbon oils

ADDITIVES FOR METAL CONTAMINANT REMOVAL

The present invention is directed to catalytic cracking additives comprising a metals trapping material; and a high activity catalyst. The present invention is directed to processes for the catalytic cracking of feedstock comprising contacting said feedstock under catalytic cracking conditions with a composition comprising a bulk catalyst and a catalytic cracking additive, wherein the catalytic cracking additive comprises a metals trapping material; and a high activity catalyst. The invention is also directed to processes for increasing the performance of a bulk catalyst in the presence of at least one metal comprising contacting a feedstock with a catalytic cracking additive comprising a metals trapping material; and a high activity catalyst. © KIPO & WIPO 2007 ...

FLUID PROCESS OF CATALYTIC CRAQUEAMENTO OF MIXING LOADS OF HYDRO-CARBONS OF DIFFERENT ORIGINS

catalisador para olefinas leves e glp em unidades catalìticas fluidizadas

CATALYST FOR LIGHT OLEFINS AND LPG IN FLUIDIZED CATALYTIC UNITS

A catalyst composition comprising at least about 10% by weight pentasil, at least about 12% by weight Y-type zeolite at a pentasil to Y zeolite ratio of at least 0.25, and wherein the pentasil and Y zeolite comprise at least about thirty-five percent of the catalyst have been shown to optimize light olefin yields and LPG from FCC processes. Embodiments having matrix surface areas greater than 25m2/g, phosphorous and rare earth are preferred. The compositions of this invention are particularly useful in typical fluid catalytic cracking (FCC) processes.

PROCESS FOR INCREASING PRODUCTION OF LIGHT OLEFIN HYDROCARBON FROM HYDROCARBON FEEDSTOCK

Disclosed herein is a process for increasing the production of light olefin hydrocarbons from a hydrocarbon feedstock. A process for producing an aromatic hydrocarbon mixture and LPG from a hydrocarbon mixture, and a process for producing a hydrocarbon feedstock which is capable of being used as a feedstock in the former process, that is to say, a fluidized catalytic cracking (FCC) process, a catalytic reforming process, and/or a pyrolysis process, are integrated, thereby it is possible to increase the production of C2-C4 light olefin hydrocarbons.

METHOD FOR PRODUCING AROMATIC HYDROCARBONS, AND AROMATIC HYDROCARBON PRODUCTION PLANT

Provided is a method for producing aromatic hydrocarbons, comprising: a step (a) in which oil feedstock such as LCO is brought into contact with a catalyst for aromatic production to obtain a reaction product containing aromatic hydrocarbons; a step (b) in which the reaction product is separated into column top fraction and column bottom fraction by means of a distillation column; a step (c) in which the column top fraction is separated into a crude aromatic fraction containing an LPG fraction and off gas containing hydrogen; a step (d) of separating the crude aromatic fraction containing an LPG fraction into the LPG fraction and a crude aromatic fraction; a step (e) of separating off gas containing hydrogen into hydrogen and off-gas; and a step (f) in which the hydrogen obtained in step (e) is used to hydrocrack the crude aromatic fraction to obtain an aromatic fraction.

CATALYST FOR PRODUCING LIQUEFIED PETROLEUM GAS, PROCESS FOR PRODUCING THE SAME, AND PROCESS FOR PRODUCING LIQUEFIED PETROLEUM GAS WITH THE CATALYST

A catalyst for the production of a liquefied petroleum gas which comprises a methanol synthesis catalyst ingredient and a zeolite catalyst ingredient. Carbon monoxide is reacted with hydrogen in the presence of the catalyst to produce a liquefied petroleum gas comprising propane as the main component.

Process for conversion of hydrocarbons to saturated LPG and high octane gasoline

The present invention relates to a process for the conversion of hydrocarbon streams with 95% true boiling point less than 400° C. to very high yield of liquefied petroleum gas in the range of 45-65 wt % of feed and high octane gasoline, the said process comprises catalytic cracking of the hydrocarbons using a solid fluidizable catalyst comprising a medium pore crystalline alumino-silicates with or without Y-zeolite, non crystalline acidic materials or combinations thereof in a fluidized dense bed reactor operating at a temperature range of 400 to 550° C., pressure range of 2 to 20 kg/cm²(g) and weight hourly space velocity in range of 0.1 to 20 hour^-1, wherein the said dense bed reactor is in flow communication to a catalyst stripper and a regenerator for continuous regeneration of the coked catalyst in presence of air and or oxygen containing gases, the catalyst being continuously circulated between the reactor-regenerator system.

BIOGASOLINE

A process for the preparation of a biogasoline component comprising: (I) obtaining at least one biooil and, if necessary, liquefying the biooil component; (II) adding the bio-oil in liquid form to a FCC unit along with at least one mineral oil; (III) cracking the components added to the FCC unit to form at least a bio-LPG fraction and a bio-naphtha fraction; (IV) alkylating or catalytically polymerising at least part of the bio-LPG fraction; and (V) combining at least a part of the product of step (IV) with at least a part of the bio-naphtha fraction to form a bio-gasoline component.

METHOD AND APPARATUS FOR TREATING A HYDROCARBON STREAM

A method of treating a hydrocarbon stream such as natural gas comprising at least the steps of: (a) providing a hydrocarbon feed stream (10); (b) passing the feed stream (10) through a first separation vessel (12) to provide a first gaseous stream (20) and a first liquid stream (30); (c) passing the first gaseous stream (20) from step (b) through a high pressure separation vessel (14) to provide a second gaseous stream (40) and a second liquid stream (80); (d) maintaining the pressure of the first gaseous stream (20) between step (b) and step (c) within +10 bar; (e) passing the first liquid stream (30) of step (b) through a stabilizer column (16) to provide a third gaseous stream (60) and a stabilized condensate (70); and (f) feeding the second liquid stream (80) from step (c) into the stabilizer column (16).

Circular chemicals or polymers from pyrolyzed plastic waste and the use of mass balance accounting to allow for crediting the resultant products as circular

This disclosure relates to the production of chemicals and plastics using pyrolysis oil from the pyrolysis of plastic waste as a co-feedstock along with a petroleum-based or fossil fuel co-feed, or as a feedstock in the absence of a petroleum-based or fossil fuel co-feed. A mass balance accounting approach is employed to attribute the pounds of pyrolyzed plastic products derived from pyrolysis oil to any output stream of a given unit, which permits assigning circular product credit to product streams. In an aspect, the polymers and chemicals produced according to this disclosure can be certified under International Sustainability and Carbon Certification (ISCC) provisions as circular polymers and chemicals at any point along complex chemical reaction pathways.

СПОСОБ И УСТАНОВКА ДЛЯ УЛУЧШЕНИЯ ХАРАКТЕРИСТИК ТЕКУЧЕСТИ СЫРОЙ НЕФТИ

Изобретение относится к нефтепереработке. Изобретение касается способа улучшения характеристик текучести углеводородного сырья, включающего разделение углеводородного сырья на первый и второй сырьевые потоки, переработку первого сырьевого потока, обладающего по меньшей мере одним свойством из числа плотности в градусах API ниже 18, вязкости выше 10000 сСт (38°С) и температуры застывания выше 20°С, включающую крекинг первого сырьевого потока со свежим катализатором, в результате чего образуются: крекированный поток и отработанный катализатор; регенерация отработанного катализатора с образованием свежего катализатора: рециркуляция указанного свежего катализатора; и смешение по крайней мере части крекированного потока со вторым сырьевым потоком. Также изобретение относится к установке для осуществления способа улучшения характеристик текучести углеводородного сырья. Технический результат - нефтепродукт с хорошими характеристиками текучести, такими как низкая температура застывания, высокая плотность в градусах API и низкая вязкость. 2 н. и 7 з.п. ф-лы, 9 табл., 3 ил. РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2 418 841 (13) C2 (51) МПК C10G 11/00 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ, ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (21)(22) Заявка: 2008108823/04, 21.07.2006 (24) Дата начала отсчета срока действия патента: 21.07.2006 (73) Патентообладатель(и): ЮОП ЛЛК (US) R U Приоритет(ы): (30) Конвенционный приоритет: 09.08.2005 US 11/200,285 (72) Автор(ы): ХЕДРИК Брайан Уэсли (US), МакГИ Джеймс Фрэнсис (US), ЭРИСКЕН Селман Зия (US), КАФИШЕХ Джибрил Абдул (US) (43) Дата публикации заявки: 20.09.2009 Бюл. № 26 2 4 1 8 8 4 1 (45) Опубликовано: 20.05.2011 Бюл. № 14 2 4 1 8 8 4 1 R U (85) Дата начала рассмотрения заявки PCT на национальной фазе: 11.03.2008 C 2 C 2 (56) Список документов, цитированных в отчете о поиске: RU 2214441 C2, 20.10.2003. SU 408960 A, 18.06.1979. RU 96119940 A, 10.12.1998. US 4940529 A, 10.07.1990. US 4359379 A, 16.11 ...

КАТАЛИЗАТОР ДЛЯ ЛЕГКИХ ОЛЕФИНОВ И LPG В ПСЕВДООЖИЖЕННЫХ КАТАЛИТИЧЕСКИХ УСТАНОВКАХ И СПОСОБ КАТАЛИТИЧЕСКОГО КРЕКИНГА

FIELD: chemistry. ^ SUBSTANCE: invention relates to a catalytic cracking composition. The composition contains: a) from approximately 12 to approximately 60 wt % zeolite Y; b) from 0.5 to 6 wt % rare-earth element, measured in form of an oxide of a rare-earth element; c) at least approximately 10 wt % pentasil, where the weight ratio of pentasil to zeolite Y is equal to at least 0.25 but not more than 3.0; and d) zeolite Y and pentasil make up at least approximately 35 wt % of the weight of the entire catalyst composition. The invention also discloses catalytic cracking methods. ^ EFFECT: invention increases output of light olefins. ^ 81 cl, 8 ex, 8 tbl РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2 412 760 (13) C2 (51) МПК B01J 29/80 (2006.01) C10G 11/05 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ, ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (21)(22) Заявка: 2007120764/04, 03.11.2005 (24) Дата начала отсчета срока действия патента: 03.11.2005 (56) Список документов, цитированных в отчете о поиске: US 4289606 A, 15.09.1981. DE 4114874 A1, 14.11.1991. RU 2144525 C1, 20.01.2000. RU 2283177 C2, 10.09.2006. 2 4 1 2 7 6 0 R U (86) Заявка PCT: US 2005/039916 (03.11.2005) C 2 C 2 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 05.06.2007 (87) Публикация заявки РСТ: WO 2006/050487 (11.05.2006) Адрес для переписки: 103735, Москва, ул. Ильинка, 5/2, ООО "Союзпатент", Н.Н.Высоцкой (54) КАТАЛИЗАТОР ДЛЯ ЛЕГКИХ ОЛЕФИНОВ И LPG В ПСЕВДООЖИЖЕННЫХ КАТАЛИТИЧЕСКИХ УСТАНОВКАХ И СПОСОБ КАТАЛИТИЧЕСКОГО КРЕКИНГА (57) Реферат: Изобретение относится к композиции для каталитического крекинга. Композиция включает: a) от примерно 12 до примерно 60 мас.% цеолита Y-типа; b) от 0.5 до 6 мас.% редкоземельного элемента, измеренного в виде оксида редкоземельного элемента; c) по меньшей мере, примерно 10 мас.% пентасила, причем весовое соотношение пентасил: цеолит Y-типа составляет, по крайней мере, 0,25, но не более чем 3,0; и d) цеолит Y-типа и пентасил ...

СПОСОБ И УСТАНОВКА ДЛЯ ПОВЫШЕНИЯ ЭФФЕКТИВНОСТИ АБСОРБЦИОННОГО МАСЛА

Изобретение может быть использовано в нефтегазовой и химической промышленности. Способ повышения эффективности абсорбции абсорбционным маслом включает подачу жидкости (11) холодного испарительного барабана (12А) ко входу холодной отпарной колонны (12) для получения потока результирующего пара головного погона холодной отпарной колонны (12), обогащенного сжиженным нефтяным газом, и отдельную подачу жидкости (21) горячего испарительного барабана ко входу (22А) горячей отпарной колонны (22) для получения потока результирующего пара головного погона горячей отпарной колонны (22), обогащенного водородом. Поток результирующего пара головного погона холодной отпарной колонны (12) и поток результирующего пара головного погона горячей отпарной колонны (22) по отдельности направляются в абсорбер (34) с абсорбционным маслом в тарелки, расположенные в разных местах, для извлечения выходящего потока сжиженного нефтяного газа при использовании абсорбционного масла. Изобретение позволяет повысить эффективность ...

СПОСОБ ПЕРЕРАБОТКИ ОТХОДОВ ПЕРЕРАБОТКИ НЕФТИ

FIELD: oil and gas industry. SUBSTANCE: invention is related to processing of oil refining wastes. The oil refining waste treatment method includes delivery of oil refining and plastic processing wastes and heating of the combined wastes using far-infrared radiation in order to split off volatile hydrocarbons, wherein the split off volatile hydrocarbons a collected for further usage. EFFECT: sound management of wastes, which includes uniform heating, minimisation of hot stains formation, minimisation of heat losses, reduction of coke deposits in the process of the method implementation. 8 cl, 1 tbl, 1 dwg, 3 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (51) МПК C10G 15/00 B09B 3/00 C10G 32/00 C08J 11/00 C10G 1/00 (13) 2 532 907 C2 (2006.01) (2006.01) (2006.01) (2006.01) (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ (21)(22) Заявка: ИЗОБРЕТЕНИЯ К ПАТЕНТУ 2011105024/04, 07.07.2009 (24) Дата начала отсчета срока действия патента: 07.07.2009 (72) Автор(ы): СКЕЙРС Джон (AU) (73) Патентообладатель(и): П-ФЬЮЭЛ ЛТД (AU) Приоритет(ы): (30) Конвенционный приоритет: (43) Дата публикации заявки: 20.08.2012 Бюл. № 23 R U 11.07.2008 AU 2008903565 (45) Опубликовано: 20.11.2014 Бюл. № 32 1923957 A, 07.03.2007. CN 1492024 A, 28.04.2004. RU 2005138138 A, 20.06.2007. US 20040235970 A1, 25.11.2004 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 11.02.2011 2 5 3 2 9 0 7 (56) Список документов, цитированных в отчете о поиске: KR 20020016566 A, 04.03.2002. CN 2 5 3 2 9 0 7 R U UA 2009/000878 (07.07.2009) C 2 C 2 (86) Заявка PCT: (87) Публикация заявки PCT: WO 2010/003180 (14.01.2010) Адрес для переписки: 129090, Москва, ул. Большая Спасская, 25, стр. 3, ООО "Юридическая фирма "Городисский и Партнеры" (54) СПОСОБ ПЕРЕРАБОТКИ ОТХОДОВ ПЕРЕРАБОТКИ НЕФТИ (57) Реферат: Изобретение относится к способу переработки углеводороды собирают для последующего отходов. Способ переработки отходов использования. Технический результат переработки нефти включает подачу ...

СПОСОБ И ОБОРУДОВАНИЕ ДЛЯ МНОГОСТАДИЙНОГО ОЖИЖЕНИЯ УГЛЕРОДОСОДЕРЖАЩЕГО ТВЕРДОГО ТОПЛИВА

FIELD: oil and gas industry. SUBSTANCE: method includes the following stages: 1) one or several types of carbon-containing solid fuel are mixed with residual oil till formation of fuel-residual oil suspension, after that this fuel-residual oil suspension is dewatered via heating and then partially liquefied by way of hydrogenation at low-average pressure, as a result there obtained are light oil components and residual slurry; 2) light oil components obtained at stage 1) are hydro-refined for obtaining refined oil; 3) residual slurry obtained at stage 1) are gasified for obtaining synthetic gas; 4) synthetic gas obtained at stage 3) is transferred into oil of synthesis F-T with the help of simple process of synthesis F-T; 5) oil of synthesis F-T obtained at stage 4) is then hydro-refined and undergoes hydro cracking for obtaining refined oil that is further fractionated for obtaining high-quality oil products, including liquefied petroleum gas (LPG), gasoline, aviation kerosene, diesel oil and other related chemical products. Invention also refers to reactor with three-phase pseudoliquid layer. EFFECT: effective conversion of carbon-containing solid fuel to oil products. 18 cl, 3 dwg, 2 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2 460 757 (13) C1 (51) МПК C10G 1/00 (2006.01) C10G 1/06 (2006.01) C10J 3/00 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (21)(22) Заявка: 2011110305/04, 01.07.2009 (24) Дата начала отсчета срока действия патента: 01.07.2009 (73) Патентообладатель(и): СИНФЬЮЭЛС ЧАЙНА ТЕКНОЛОДЖИ КО., ЛТД. (CN) (45) Опубликовано: 10.09.2012 Бюл. № 25 2 4 6 0 7 5 7 (56) Список документов, цитированных в отчете о поиске: SU 812186 А, 07.03.1981. US 4152244 А, 01.05.1979. CN 101270294 А, 24.09.2008. DE 3835494 С2, 16.02.1995. SU 1099847 А, 23.06.1984. RU 2317315 С1, 20.02.2008. (85) Дата начала рассмотрения заявки PCT на национальной фазе: 10.05.2011 2 4 6 0 7 5 7 R U (87) Публикация заявки РСТ: WO 2010/040291 (15. ...

СПОСОБ И УСТРОЙСТВО ОБРАБОТКИ ПОТОКА УГЛЕВОДОРОДОВ

1. Способ обработки потока углеводородов, такого как природный газ, отличающийся тем, что включает в себя, по меньшей мере, следующие стадии: ! (а) подача сырьевого потока (10) углеводородов; ! (б) пропускание сырьевого потока (10) через первый сепаратор (12) с получением первого газообразного потока (20) и первого потока (30) жидкости; !(в) пропускание первого газообразного потока (20) со стадии (б) через сепаратор (14) высокого давления с получением второго газообразного потока (40) и второго потока (80) жидкости; ! (г) поддерживание давления первого газообразного потока (20) между стадией (б) и (в) в пределах ±1 МПа; ! (д) пропускание первого потока (30) жидкости со стадии (б) через стабилизационную колонну (16) с получением третьего газообразного потока (60) и стабилизированного конденсата (70); и ! (е) подача второго потока (80) жидкости со стадии (в) в стабилизационную колонну (16). ! 2. Способ по п.1, отличающийся тем, что третий газообразный поток (60) с этапа (г) сжимают и соединяют с первым газообразным потоком (20). ! 3. Способ по п.1, отличающийся тем, что первый газообразный поток (20) со стадии (б) охлаждают до стадии (в). ! 4. Способ по п.2, отличающийся тем, что первый газообразный поток (20) со стадии (б) охлаждают до стадии (в). ! 5. Способ по п.1, отличающийся тем, что перед стадией (в) первый газообразный поток (20) обрабатывают с целью уменьшения одного или нескольких веществ, выбранных из группы, содержащей серу, соединения серы, углекислый газ, влажности или воду. ! 6. Способ по любому из пп.1-4, отличающийся тем, что стабилизированный конденсат (70) со стадии (д) содержит более 85 мол.%, предпочтительно более 90 мол.% углеводородов С5+. ! 7. Способ по любому из пп.1-4, отлича� РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2008 152 127 (13) A (51) МПК F25J 3/02 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ, ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (71) Заявитель(и): ШЕЛЛ ИНТЕРНЭШНЛ РИСЕРЧ МААТСХАППИЙ Б.В. (NL) (21), (22) ...

Способ и установка для получения углеводородов

КАТАЛИЗАТОР ДЛЯ ЛЕГКИХ ОЛЕФИНОВ И LPG В ПСЕВДООЖИЖЕННЫХ КАТАЛИТИЧЕСКИХ УСТАНОВКАХ И СПОСОБ КАТАЛИТИЧЕСКОГО КРЕКИНГА

... 1. Каталитическая композиция, включающаяа) от примерно 12 до примерно 60 мас.% цеолита Y-типа;b) по крайней мере примерно 10 мас.% пентасила, причем массовое соотношение пентасил: цеолит Y-типа составляет, по крайней мере, 0,25, но не более чем 0,3; ис) цеолит Y-типа и пентасил составляют, по крайней мере, примерно 35 мас.% от массы всей каталитической композиции.2. Каталитическая композиция по п.1, которая содержит фосфор.3. Каталитическая композиция по п.2, которая включает до примерно 12 мас.% фосфора от всей массы РO.4. Каталитическая композиция по п.1, которая включает матрикс, имеющий площадь поверхности по крайней мере 25 м/г.5. Каталитическая композиция по п.2, в которой пентасил и цеолит Y-типа содержатся в виде отдельных частиц, причем частицы пентасила содержат частицы фосфора.6. Каталитическая композиция по п.5, в которой частицы пентасила содержат фосфор в количестве от примерно 6 до примерно 24 мас.% от всей массы РO.7. Каталитическая композиция по п.2, в которой частицы, ...

Verfahren zur Herstellung von LPG und Leichtolefinen mit hohen Ausbeuten

VERFAHREN UND VORRICHTUNG ZUR FLIESSKATALYTISCHEN UMWANDLUNG VON ALKOHOLEN UND VERWANDTEN SAUERSTOFFVERBINDUNGEN IN KOHLENWASSERSTOFFE

Procedure for the production of hydrocarbons gaseous under standard conditions or from mixtures under standard conditions gaseous hydrocarbons and condensable, inbesondere aromatic hydrocarbons

Pretreatment of fcc naphthas and selective hydrotreating

This invention provides methods for multi-stage hydroprocessing treatment of FCC naphthas for improving the overall production quantity of naphtha boiling-range materials during naphtha production for low sulfur gasolines. Of particular benefit of the present processes is the selective treating of cat naphthas to remove gums instead of undercutting the overall naphtha pool by lowering the end cutpoints of the cat naphtha fraction. This maximizes the amount of refinery cat naphtha that can be directed to the gasoline blending pool while eliminating existing processing problems in hydrodesulfurization units. The processes disclosed herein have the additional benefit of minimizing octane losses in the increased naphtha pool volume.

System and process for converting plastics to petroleum products

A system and process for converting plastics and other heavy hydrocarbon solids into retail petroleum products are provided. The plastics are processed by melting, pyrolysis, vapourization, and selective condensation, whereby final in-spec petroleum products are produced. The system provides a reactor for subjecting the plastics to pyrolysis and cracking hydrocarbons in the plastics to produce a plastics vapour comprising hydrocarbon substituents; one or more separation vessels for separating the plastics vapour into hydrocarbon substituents based on boiling points of the hydrocarbon substituents; one or more condensers for condensing the hydrocarbon substituents into one or more petroleum products; and means for collecting the one or more petroleum products. Fuels generated during the process can be recycled for use upstream in the process.

Process For Co-Conversion Of Waste Plastics And Hydrocarbon Feedstock

The present invention relates to a process for converting the waste plastics along with the petroleum feedstock in a Catalytic Cracking Unit, in particular a Fluid Catalytic Cracking Unit employed in petroleum refineries. The invention also provides a method and hardware system to enable waste plastic to fuel conversion along with hydrocarbon catalytic cracking. The invented process aims to convert any type of waste plastic including polystyrene, polypropylene, polyethylene, metal containing Polyethylene-Polypropylene multilayer plastics & other metal containing plastics along with the petroleum derived feedstock such as vacuum gas oil, reduced crude oil, vacuum residue etc. in catalytic cracking unit. 1. A method for co-conversion of plastics and hydrocarbons into lighter distillate products , the method comprising of:a) spray feeding hydrocarbon feed in the bottom section of the riser reactor through the injection nozzles;b) feeding hot regenerated catalyst from the regenerator vessel into the bottom section of the riser reactor to allow contacting with hydrocarbon feed;c) feeding a lift fluidization media into the bottom section of the riser reactor;d) conveying the waste plastic from the supply vessel to the bottom section of riser, to allow thermal decomposition of plastic material into lighter molecules and catalytic cracking of the same by contacting with the catalyst particles during the upward motion through riser reactor;e) separation of catalyst and product vapors by means of riser termination devices;f) separation of hydrocarbon molecules from the catalyst by steam stripping in the stripper vessel; andg) separation of product vapors into different product fractions like Naphtha, Light cycle oil, Heavy cycle oil, clarified oil etc by fractionator column.2. The method as claimed in claim 1 , wherein the waste plastic is optionally pre-processed by steps comprising of washing claim 1 , drying claim 1 , extrusion claim 1 , pelletization etc.3. The method as ...

Plasmonic Nanoparticle Catalysts and Methods for Producing Long-Chain Hydrocarbon Molecules

A plasmonic nanoparticle catalyst for producing hydrocarbon molecules by light irradiation, which comprises at least one plasmonic provider and at least one catalytic property provider, wherein the plasmonic provider and the catalytic property provider are in contact with each other or have distance less than 200 nm, and molecular composition of the hydrocarbon molecules produced by light irradiation is temperature-dependent. And a method for producing hydrocarbon molecules by light irradiation utilizing the plasmonic nanoparticle catalyst.

PROCESS FOR CONVERTING MIXED HYDROCARBON STREAMS TO LPG AND BTX

The present invention relates to a process for converting a feed comprising C5-C12 hydrocarbons to higher BTX, LPG and methane in the presence of hydrogen in n reaction zones operated in series, wherein m reaction zones are not participating in the conversion process and only (n−m) reaction zones are operated under reaction conditions sufficient to convert at least a portion of said a feed comprising C5-C12 hydrocarbons to an effluent having said BTX. An object of the present invention is to provide a process for converting C5-C12 hydrocarbons to LPG, optionally BTX, and methane in the presence of hydrogen wherein coke formation on the catalyst is controlled and the physical movement of particulate catalyst is avoided. 1. A process for converting a mixed C5-C12 hydrocarbons stream to BTX , LPG and methane in the presence of hydrogen in n reaction zones operated in series , wherein m reaction zones are not participating in the conversion process and only (n−m) reaction zones are operated under reaction conditions sufficient to convert at least a portion of said C5-C12 hydrocarbon stream to an effluent having said BTX , wherein each reaction zone is initially numbered serially with a designator from 1 to n , the process comprising:(a) providing a quantity of catalytic material within each reaction zone;(b) providing to the reaction zone designated as 1 a hydrocarbon feedstock containing C5-C12 hydrocarbons and hydrogen;(c) cooling at least a portion of the effluent of the said reaction zone designated as 1 to the inlet temperature of the reaction zone designated as 2, and more generally, cooling at least a portion of the effluent of each reaction zone with a designator equal or smaller than (n−m−1) to the inlet temperature of the reaction zone with a designator larger by one than that of the reaction zone from which said effluent originates;(d) transferring said at least portion of said effluent of the said reaction zone designated as 1 to said reaction zone ...

Methods and systems for processing lignin during hydrothermal digestion of cellulosic biomass solids

Digestion of cellulosic biomass solids may be complicated by release of lignin therefrom. Methods for digesting cellulosic biomass solids may comprise: providing cellulosic biomass solids in a digestion solvent; at least partially converting the cellulosic biomass solids into a phenolics liquid phase comprising lignin, an aqueous phase comprising an alcoholic component derived from the cellulosic biomass solids, and an optional light organics phase; and separating the phenolics liquid phase from the aqueous phase, at least partially depolymerizing the lignin in the phenolics liquid phase, wherein at least partially depolymerizing the lignin generates hydrocarbons.

Processes for producing a fuel from a renewable feedstock

Processes for the production of transportation fuel from a renewable feedstock. A gaseous mixture of carbon monoxide and hydrogen is used to deoxygenate and hydrogenate the glycerides to produce long chain hydrocarbons. Water is also introduced into the reaction zone to increase the amount of hydrogen and to increase the utilization of carbon monoxide within the reaction zone. Synthesis gas may also be used to supply at least a portion of the gaseous mixture of carbon monoxide and hydrogen. The amount of hydrogen equivalents in the reaction zone is at least 100% of a stoichiometric hydrogen demand within the reaction zone.

Plasmonic Nanoparticle Catalysts and Methods for Producing Long-Chain Hydrocarbon Molecules

A plasmonic nanoparticle catalyst for producing hydrocarbon molecules by light irradiation, which comprises at least one plasmonic provider and at least one catalytic property provider, wherein the plasmonic provider and the catalytic property provider are in contact with each other or have distance less than 200 nm, and molecular composition of the hydrocarbon molecules produced by light irradiation is temperature-dependent. And a method for producing hydrocarbon molecules by light irradiation utilizing the plasmonic nanoparticle catalyst. 1. A plasmonic nanoparticle catalyst for producing hydrocarbon molecules by light irradiation , comprising:at least one plasmonic provider; andat least one catalytic property provider, whereinthe plasmonic provider and the catalytic property provider are in contact with each other or have distance less than 200 nm, andmolecular composition of the hydrocarbon molecules produced by light irradiation is temperature-dependent.2. The plasmonic nanoparticle catalyst of claim 1 , whereinsaid at least one plasmonic provider and said at least one catalytic property provider are provided in one nanoparticle, andsaid nanoparticle comprises one chemical element as both the plasmonic provider and the catalytic property provider, or alloy of two or more chemical elements each as the plasmonic provider or the catalytic property provider.3. The plasmonic nanoparticle catalyst of or claim 1 , whereinthe plasmonic provider is selected from the group consisting of Co, Fe, Al, Ag, Au, Pt, Cu, Ni, Zn, Ti, C and alloys of two or more chemical elements thereof.4. The plasmonic nanoparticle catalyst of or claim 1 , whereinthe catalytic property provider is selected from the group consisting of Co, Fe, Ru, Rh, Pd, Os, Ir, La, Ce, Cu, Ni, Ti, C and oxide, chloride, carbonate and bicarbonate thereof.5. The plasmonic nanoparticle catalyst of any one of to claim 1 , whereinthe dimension of the plasmonic nanoparticle catalyst is about 1 nm to about 1000 nm in ...

CHEMICAL COMPOSITIONS AND METHODS FOR REMEDIATING HYDROGEN SULFIDE AND OTHER CONTAMINANTS IN HYDROCARBON BASED LIQUIDS AND AQUEOUS SOLUTIONS WITHOUT THE FORMATION OF PRECIPITATES OR SCALE

A treatment process for remediating a contaminated liquid containing more than 5 ppm hydrogen sulfide (HS) and substantially without formation of precipitate, includes steps of steps of adding an aqueous solution containing at least one hydroxide compound at a collective concentration of 35-55 wt % to the contaminated liquid to achieve a concentration of 125-5000 ppm of the hydroxide compounds in the contaminated liquid, adding at least one organic acid and to the liquid to achieve a concentration of 0.01-10 ppm in the contaminated liquid, and dispersing the aqueous solution and the at least one organic acid in the contaminated liquid and allowing the aqueous solution and the at least one organic acid to react with the contaminated liquid for a period of time until a concentration of hydrogen sulfide in the contaminated liquid is reduced to ≤5 ppm. 1. An aqueous based treatment solution for remediating hydrogen sulfide (HS) and other contaminants in liquids and substantially without formation of precipitate , the treatment solution comprising:at least one hydroxide compound;at least one organic acid selected from a group consisting of a fulvic acid and a humic acid; andwater, whereina collective concentration of the at least one hydroxide compound in the treatment solution is in a range of 35-55 weight %,a content of water in the treatment solution is at least 30 weight %, anda collective concentration of the at least one organic acid in the treatment solution is at least 0.01 weight %.2. The treatment solution according to claim 1 , wherein the collective concentration of the at least one hydroxide in the solution is 45-55 weight %.3. The treatment solution according to claim 1 , wherein the treatment solution contains at least two different hydroxide compounds.4. The treatment solution according to claim 1 , wherein the treatment solution contains sodium hydroxide (NaOH) and potassium hydroxide (KOH).5. The treatment solution according to claim 1 , wherein the ...

METHOD AND APPARATUS FOR PRODUCING BIOFUEL

The present invention relates to the field of renewable energy. More specifically, the present invention relates to the production of biofuel from biomass including, for example, polymeric materials. 1. A method for producing a bio-oil , the method comprising:extruding polymeric material in an extruder to thereby form a melt stream comprising the polymeric material,providing a stream of aqueous solvent that is separate to the melt stream,contacting the melt stream with the stream of aqueous solvent to form a reaction mixture,treating the reaction mixture in a reactor vessel at a reaction temperature and a reaction pressure for a time period suitable for conversion of all or a portion of the polymeric material present in the reaction mixture into a product comprising the bio-oil, anddepressurising and cooling the product.2. The method according to claim 1 , wherein the extruder is a single screw extruder claim 1 , a multiscrew extruder claim 1 , a counter-rotating multiscrew extruder claim 1 , a co-rotating multiscrew extruder claim 1 , a twin screw extruder claim 1 , a counter-rotating twin screw extruder claim 1 , a co-rotating twin screw extruder claim 1 , an intermeshing screw extruder claim 1 , a radial extruder claim 1 , or a roll-type extrusion press.3. The method according to or claim 1 , wherein the method further comprises venting gases and/or vapours from one or a series of ports present in a barrel of the extruder.4. The method according to claim 3 , wherein the gases and/or vapours comprise any one or more of: hydrogen chloride claim 3 , hydrogen bromide claim 3 , hydrogen fluoride claim 3 , chlorine claim 3 , ammonia claim 3 , carbon monoxide claim 3 , carbon dioxide.5. The method according to any one of to claim 3 , further comprising adding a base to any one or more of: the polymeric material prior to extrusion claim 3 , the melt stream claim 3 , the stream of aqueous solvent claim 3 , and/or the reaction mixture claim 3 , wherein:the base is an ...

AN FCC CATALYST ADDITIVE AND A PROCESS FOR PREPARATION THEREOF

The present disclosure relates to an FCC catalyst additive for cracking of petroleum feedstock and a process for its preparation. The FCC catalyst additive of the present disclosure comprises at least one zeolite, at least one clay, at least one binder, phosphorous in the form of PO, and at least one Group IVB metal compound. The FCC catalyst additive of the present disclosure is hydrothermally stable and has improved matrix surface area even after various hydrothermal treatments. The FCC catalyst additive of the present disclosure can be used in combination with the conventional FCC catalyst for catalytic cracking to selectively enhance the propylene and LPG yields. 1. An FCC catalyst additive comprisingi. at least one zeolite in an amount in the range of 30 to 50 wt %;ii. at least one clay in an amount in the range of 5 to 40 wt %;iii. at least one binder in an amount in the range of 5 to 20 wt %;{'sub': 2', '5, 'iv. POin an amount in the range of 5 to 10 wt %; and'}v. at least one Group IVB metal compound in an amount in the range of 0.1 to 10 wt %.2. The FCC catalyst additive as claimed in claim 1 , wherein said zeolite is at least one selected from the group consisting of ZSM-5 claim 1 , ZSM-11 claim 1 , and ZSM-22 zeolite.3. The FCC catalyst additive as claimed in claim 1 , wherein said zeolite is ZSM-5 in an amount in the range of 40 to 50 wt %.4. The FCC catalyst additive as claimed in claim 1 , wherein said clay is at least one selected from the group consisting of kaolin clay claim 1 , halloysite claim 1 , bentonite and mixtures thereof.5. The FCC catalyst additive as claimed in claim 1 , wherein said binder is at least one selected from the group consisting of colloidal silica claim 1 , colloidal alumina claim 1 , pseduoboehmite alumina claim 1 , bayrite alumina claim 1 , gamma alumina and mixtures thereof.6. The FCC catalyst additive as claimed in claim 1 , whereinsaid clay is kaolin clay in an amount in the range of 10 to 20 wt %; andsaid binder is ...

CIRCULAR CHEMICALS OR POLYMERS FROM PYROLYZED PLASTIC WASTE AND THE USE OF MASS BALANCE ACCOUNTING TO ALLOW FOR CREDITING THE RESULTANT PRODUCTS AS CIRCULAR

This disclosure relates to the production of chemicals and plastics using pyrolysis oil from the pyrolysis of plastic waste as a co-feedstock along with a petroleum-based, fossil fuel-based, or bio-based feedstock. In an aspect, the polymers and chemicals produced according to this disclosure can be certified under International Sustainability and Carbon Certification (ISCC) provisions as circular polymers and chemicals at any point along complex chemical reaction pathways. The use of a mass balance approach which attributes the pounds of pyrolyzed plastic products derived from pyrolysis oil to any output stream of a given unit has been developed, which permits ISCC certification agency approval. 1. A process for producing chemicals or polymers from plastic waste , the process comprising:(a) providing a pyrolysis oil from plastic waste;(b) providing a petroleum-based, fossil fuel-based, or bio-based feed;(c) introducing the pyrolysis oil and the petroleum-based, fossil fuel-based, or bio-based feed, each at a known feed rate, into one or more primary processing units, thereby providing one or more primary processing unit feeds, each comprising the pyrolysis oil in a known concentration; and(d) converting the one or more primary processing unit feeds into one or more primary processing unit output streams, a portion of each output stream comprising at least one circular product, wherein the weight or the fraction of each circular product attributable to the pyrolysis oil or plastic waste is determined by mass balance.2. A process for producing chemicals or polymers from plastic waste according to claim 1 , wherein the process further comprises:(e) transferring at least a portion of one, or at least a portion of more than one, of the primary processing unit output streams, each at a known feed rate, into one or more secondary or subsequent processing units, thereby providing one or more secondary or subsequent processing unit feeds, each comprising a circular product ...

CIRCULAR CHEMICALS OR POLYMERS FROM PYROLYZED PLASTIC WASTE AND THE USE OF MASS BALANCE ACCOUNTING TO ALLOW FOR CREDITING THE RESULTANT PRODUCTS AS CIRCULAR

This disclosure relates to the production of chemicals and plastics using pyrolysis oil from the pyrolysis of plastic waste as a co-feedstock along with a petroleum-based or fossil fuel co-feed, or as a feedstock in the absence of a petroleum-based or fossil fuel co-feed. A mass balance accounting approach is employed to attribute the pounds of pyrolyzed plastic products derived from pyrolysis oil to any output stream of a given unit, which permits assigning circular product credit to product streams. In an aspect, the polymers and chemicals produced according to this disclosure can be certified under International Sustainability and Carbon Certification (ISCC) provisions as circular polymers and chemicals at any point along complex chemical reaction pathways. 1. A process for producing chemicals or polymers from plastic waste , the process comprising:(a) providing a pyrolysis oil from plastic waste;(b) introducing the pyrolysis oil at a known feed rate into one or more primary processing units thereby providing one or more primary processing unit feeds comprising the pyrolysis oil; and(c) converting the one or more primary processing unit feeds into one or more primary processing unit output streams, each output stream comprising at least one circular product, wherein the weight or the fraction of each circular product attributable to the pyrolysis oil or plastic waste is determined by mass balance.2. The process for producing chemicals or polymers from plastic waste according to claim 1 , wherein a petroleum-based or a fossil fuel-based feed is not co-fed with the pyrolysis oil into the primary processing unit.3. The process for producing chemicals or polymers from plastic waste according to claim 1 , wherein the process further comprises:(d) transferring at least a portion of one, or at least a portion of more than one, of the primary processing unit output streams, each at a known feed rate, into one or more secondary or subsequent processing units, thereby ...

METHOD FOR CONVERTING A HIGH-BOILING HYDROCARBON FEEDSTOCK INTO LIGHTER BOILING HYDROCARBON PRODUCTS

A process for converting hydrocarbons originating from refinery operations such as atmospheric distillation unit or a fluid catalytic cracking unit (FCC), into lighter boiling hydrocracked hydrocarbons having a boiling point lower than naphthalene and lower. 1. A process for converting a high-boiling hydrocarbon feedstock into lighter boiling hydrocarbon products , said lighter boiling hydrocarbon products being suitable as a feedstock for petrochemicals processes , said converting process comprising the following steps of:feeding a heavy hydrocarbon feedstock to a cascade of hydrocracking unit(s):cracking said feedstock in a hydrocrackingseparating said cracked feedstock into a top stream comprising a light boiling hydrocarbon fraction and a bottom stream comprising a heavy hydrocarbon fraction:feeding said bottom stream of such a hydrocracking unit as a feedstock for a subsequent hydrocracking unit in said cascade of hydrocracking unit(s), wherein the process conditions in each hydrocracking unit(s) are different from each other, in which the hydrocracking conditions from the first to the subsequent hydrocracking unit(s) increase from least severe to most severe; andprocessing the lighter boiling hydrocarbon fractions from each hydrocracking unit(s) as a feedstock for a BTX and LPG producing unit, said BTX and LPG producing unit being a hydrocracking unit wherein the process conditions prevailing in said hydrocracking unit are different from the process conditions prevailing in any one of the hydrocracking unit(s) in the cascade of hydrocracking unit(s).2. The process according to claim 1 , wherein the lighter boiling hydrocarbon fractions from all hydrocracking units in said cascade of hydrocracking unit(s) are hydrocarbons having a boiling point lower than naphthalene.3. The process according claim 1 , wherein each hydrocracking unit in said cascade of hydrocracking unit(s) is operated under liquid phase hydrocracking conditions claim 1 , and wherein said ...

APPARATUSES AND METHODS FOR ENERGY EFFICIENT SEPARATIONS INCLUDING REFINING OF FUEL PRODUCTS

In various aspects, methods and apparatuses for liquid-liquid extraction are provided. In certain aspects, an emulsion can be formed by combining a feed stream, an extractant, and a surfactant. The feed stream comprises a plurality of distinct components including a first component to be removed therefrom. The feed stream may be selected from a group consisting of: a hydrocarbon feed stream and an azeotrope. Then, a portion of the first component is extracted from the feed stream (or emulsion) by contact with a superoleophobic and hygroscopic membrane filter that facilitates passage of the first component and extractant through the superoleophobic and hygroscopic membrane filter. A purified product is collected having the portion of the first component removed. Such methods are particularly useful for refining fuels and oils and separating azeotropes and other miscible component systems. Energy-efficient, continuous single unit operation apparatuses for conducting such separation techniques are also provided. 1. A method of liquid-liquid extraction comprising:creating an emulsion by combining a feed stream, an extractant, and a surfactant, wherein the feed stream comprises a first component that is a contaminant or impurity present at an initial amount and the feed stream is selected from a group consisting of: a non-polar feed stream and an azeotrope comprising the non-polar feed stream;removing a portion of the first component from the emulsion by contacting the emulsion with a first side of a superoleophobic and hygroscopic membrane filter to facilitate passage of the first component and the extractant through the superoleophobic and hygroscopic membrane filter to a second side of the superoleophobic and hygroscopic membrane filter; andcollecting a purified product having the portion of the first component removed.2. The method of claim 1 , wherein the removing the portion of the first component by contacting includes gravity-feeding the emulsion to the first ...

APPARATUS FOR SEPARATION AND RECOVERY OF HYDROCARBONS FROM LNG

Provided are an apparatus and a method for separation and recovery of propane and heavier hydrocarbons from LNG. The apparatus has, from the upstream side toward the downstream side of LNG supply, first column () equipped with first column overhead condenser (), first column bottom reboiler () and side reboiler (), and second column () equipped with second column overhead condenser () and second column bottom reboiler (). The first column () separates methane and a part of ethane as an overhead vapor and separates remaining ethane and C3 or higher hydrocarbons as a bottom liquid. The second column () separates ethane as an overhead vapor and separates C3 or higher hydrocarbons as a bottom liquid. 31114. The apparatus according to claim 1 , wherein the second column overhead condenser () which produces the condensed second overhead vapor of the second column () is configured to totally condense the second overhead vapor by heat exchange with an internal liquid of the first column.411. The apparatus according to claim 3 , wherein the second column overhead condenser () which produces the condensed second overhead vapor of the second column is configured to totally condense the second overhead vapor by recovering cold heat within the first column by heat exchange with an intermediate heating medium claim 3 , which is an anti-freezing liquid claim 3 , in the side reboiler claim 3 , and by cooling the second overhead vapor in the second column overhead condenser by the cooled intermediate heating medium.5. The apparatus according to claim 4 , wherein the intermediate heating medium is selected from methanol claim 4 , ethanol and monoethylene glycol.611. The apparatus according to claim 1 , wherein the second column overhead condenser () which produces the condensed second overhead vapor of the second column is configured to totally condense the second overhead vapor by using an external refrigerant selected from ethane claim 1 , ethylene claim 1 , propane and propylene.7 ...

Chemical compositions and methods for remediating hydrogen sulfide and other contaminants in hydrocarbon based liquids and aqueous solutions without the formation of precipitates or scale

A treatment process for preparing a remediated liquid from a contaminated liquid originally containing more than 5 ppm hydrogen sulfide (H 2 S) and substantially without formation of precipitate, includes steps of steps of adding an aqueous solution containing at least one hydroxide compound at a collective concentration of 35-55 wt % to the contaminated liquid to achieve a concentration of 125-5000 ppm of the hydroxide compounds in the contaminated liquid, adding a fulvic acid and/or a humic acid to the contaminated liquid to achieve a concentration of 0.01-10 ppm of the acid(s) in the contaminated liquid, and dispersing the aqueous solution and the at least one organic acid in the contaminated liquid and allowing the aqueous solution and the at least one organic acid to react with the contaminated liquid for a period of time until a concentration of hydrogen sulfide in the contaminated liquid is reduced to ≤5 ppm.

TWO-STAGE HYDROCRACKING UNIT WITH INTERMEDIATE HPNA HYDROGENATION STEP

A method and a system for hydrocracking an oil feedstock to produce a light oil stream without build-up of heavy polynuclear aromatic (HPNA) hydrocarbons in the recycle stream. The method may include hydrocracking an oil feedstock, separating the produced effluent into a first, second, and third product stream, and hydrogenating the third product stream in a third reactor over a noble metal hydrogenation catalyst at an operational pressure equal to or less than the second reactor. 1. A method of hydrocracking an oil feedstock to produce a light oil stream without build-up of heavy polynuclear aromatic (HPNA) hydrocarbons in the recycle stream , the method comprising the steps of:hydrocracking the oil feedstock with a first stage hydrocracking catalyst possessing hydrotreating and hydrocracking functionality in a first reactor to produce an effluent stream;{'sub': 1', '4, 'fractionating the effluent stream into first, second and third product streams, wherein the first product stream comprises C-C, naphtha, and diesel boiling in the range of 36-370° C., the second product stream comprises hydrocarbon components having an initial nominal boiling point of 370° C. and a final boiling point ranging from 420-750° C., and the third product stream comprises HPNA hydrocarbons and other hydrocarbons boiling above 420° C. to 750° C., depending upon the final boiling point of the second product stream;'}cracking the second product stream in a second reactor; andhydrogenating the third product stream in a third reactor over a noble metal hydrogenation catalyst at an operational pressure equal to or less than the second reactor.2. The method of claim 1 , wherein the feedstock oil comprises at least one of a vacuum gas oil claim 1 , deasphalted or demetalized oil from a solvent deasphalting process claim 1 , light and heavy coker gas oils from a coker process claim 1 , cycle oils from a fluid catalytic cracking (FCC) process derived from crude oils claim 1 , synthetic crude oils ...

USE OF RENEWABLE OIL IN HYDROTREATMENT PROCESS

The use of bio oil from at least one renewable source in a hydrotreatment process, in which process hydrocarbons are formed from said glyceride oil in a catalytic reaction, and the iron content of said bio oil is less than 1 w-ppm calculated as elemental iron. A bio oil intermediate including bio oil from at least one renewable source and the iron content of said bio oil is less than 1 w-ppm calculated as elemental iron. 1. A bio oil intermediate for a hydrotreatment process to form hydrocarbons , the bio oil intermediate comprising:a bio oil from at least one renewable source, wherein an iron content of said bio oil contains:an iron concentration of less than 1 to 0.2 w-ppm calculated as elemental iron;a phosphorous concentration of less than 5 w-ppm; anda cumulative alkali metals concentration and alkali earth metals concentration calculated as elemental metal of less than 1 w-ppm.2. A bio oil intermediate according to claim 1 , wherein said bio oil intermediate is a group of bio oils characterized by a result-effective range of iron concentrations to address plugging in a hydrodeoxygenation reactor claim 1 , the range having a lower bound of 0.2 w-ppm and an upper bound of 1 w-ppm.3. A bio oil intermediate according to claim 1 , in combination with a catalyst bed of a hydrodeoxygenation reactor claim 1 , wherein the catalyst bed comprises:a NiMo catalyst.4. A bio oil intermediate according to claim 1 , in combination with a catalyst bed of a hydrodeoxygenation reactor claim 1 , wherein the catalyst bed comprises:a CoMo catalyst.5. A bio oil intermediate according to claim 1 , in combination with a catalyst bed of a hydrodeoxygenation reactor claim 1 , wherein the catalyst bed comprises:{'sub': 2', '3, 'a NiMo/A1Ocatalyst.'}6. A bio oil intermediate according to claim 1 , in combination with a catalyst bed of a hydrodeoxygenation reactor claim 1 , wherein the catalyst bed comprises:a catalyst containing at least one or more of Pd, Pt, Ni, NiMo and CoMo.7. A bio ...

PROCESS FOR PRODUCING BTX AND LPG

The invention is directed to a process for producing BTX and LPG, comprising: a) contacting a feed stream comprising C5-C12 hydrocarbons in the presence of hydrogen with a hydrocracking catalyst in a hydrocracking reactor to produce a hydrocracking product stream comprising hydrogen, methane, LPG and BTX, b) separating the hydrocracking product stream into a first gas stream and a first liquid stream, c) separating the first gas stream to obtain a second gas stream comprising hydrogen and methane and a second liquid stream comprising LPG and BTX, wherein the separation is performed such that the second liquid stream is substantially free of hydrogen and methane, d) separating the second liquid stream into a third gas stream comprising LPG and a third liquid stream comprising BTX, wherein step (c) involves adding a part of the third liquid stream to the first gas stream to absorb the LPG in the first gas stream to obtain the second liquid stream or adding a part of the third liquid stream to a gas stream sep crated from the first gas stream to absorb the LPG in said gas stream separated from the first gas stream to obtain the second liquid stream. 1. A process for producing BTX and LPG , comprising:(a) contacting a feed stream comprising C5-C12 hydrocarbons in the presence of hydrogen with a hydrocracking catalyst in a hydrocracking reactor to produce a hydrocracking product stream comprising hydrogen, methane, LPG and BTX,(b) separating the hydrocracking product stream into a first gas stream and a first liquid stream,(c) separating the first gas stream to obtain a second gas stream comprising hydrogen and methane and a second liquid stream comprising LPG and BTX, wherein the separation is performed such that the second liquid stream is substantially free of hydrogen and methane,(d) separating the second liquid stream into a third gas stream comprising LPG and a third liquid stream comprising BTX,wherein step (c) involves adding a part of the third liquid stream to ...

CIRCULAR ECONOMY FOR PLASTIC WASTE TO POLYETHYLENE VIA REFINERY CRUDE UNIT

Provided is a continuous process for converting waste plastic into a feedstock for polyethylene polymerization. The process comprises selecting waste plastics containing polyethylene and/or polypropylene, and then passing the waste plastics through a pyrolysis reactor to thermally crack at least a portion of the polyolefin waste and produce a pyrolyzed effluent. The pyrolyzed effluent is then separated into offgas, a pyrolysis oil comprising a naphtha/diesel/heavy fraction, and char. The pyrolysis oil is passed to a crude unit in a refinery from which a naphtha fraction (C-C), or a propane and butane (C-C) fraction, is recovered. The naphtha fraction, or propane and butane (C-C) fraction, is then passed to a steam cracker for ethylene production. 1. A continuous process for converting waste plastic into naphtha for polyethylene polymerization comprising:(a) selecting waste plastics containing polyethylene and/or polypropylene;(b) passing the waste plastics from (a) through a pyrolysis reactor to thermally crack at least a portion of the polyolefin waste and produce a pyrolyzed effluent;(c) separating the pyrolyzed effluent into offgas, a pyrolysis oil and optionally pyrolysis wax comprising a naphtha/diesel fraction and a heavy fraction, and char;(d) passing the pyrolysis oil and wax to a crude unit in a refinery;{'sub': 5', '8, '(e) recovering a naphtha fraction (C-C) from the crude unit;'}(f) passing the naphtha fraction to a steam cracker for ethylene production.2. The process of claim 1 , wherein the pyrolysis oil and wax of (c) is passed directly to a refinery crude unit and the contaminants are removed in a crude unit desalter.3. The process of claim 1 , wherein contaminants are removed at the pyrolysis site.4. The process of claim 1 , wherein the ethylene produced in (f) is subsequently polymerized.5. The process of claim 4 , wherein polyethylene products are prepared from the polymerized ethylene.6. The process of claim 1 , wherein heavy naphtha/diesel/ ...

CIRCULAR ECONOMY FOR PLASTIC WASTE TO POLYPROPYLENE VIA REFINERY FCC AND ALKYLATION UNITS

Provided is a continuous process for converting waste plastic into recycle for polypropylene polymerization. The process comprises selecting waste plastics containing polyethylene and/or polypropylene and passing the waste plastics through a pyrolysis reactor to thermally crack at least a portion of the polyolefin waste and produce a pyrolyzed effluent. The pyrolyzed effluent is separated into offgas, a naphtha/diesel fraction, a heavy fraction, and char. Pyrolysis oil and wax, comprising the naphtha/diesel fraction and heavy fraction, is sent to a refinery FCC unit. A liquid petroleum gas C-Colefin/paraffin mixture is recovered from the FCC unit and passed to a refinery alkylation unit. A propane fraction is recovered from the alkylation unit and passed to a dehydrogenation unit to produce propylene. The propylene is passed to a propylene polymerization reactor. 1. A continuous process for converting waste plastic into recycle for polypropylene polymerization comprising:(a) selecting waste plastics containing polyethylene and/or polypropylene;(b) passing the waste plastics from (a) through a pyrolysis reactor to thermally crack at least a portion of the polyolefin waste and produce a pyrolyzed effluent;(c) separating the pyrolyzed effluent into offgas, a naphtha/diesel fraction, a heavy fraction, and char;(d) passing a pyrolysis oil and optionally wax comprising the naphtha/diesel fraction and the heavy fraction to a refinery FCC unit;{'sub': 3', '5, '(e) recovering a liquid petroleum gas comprising a C-Colefin/paraffin mixture from the FCC unit;'}passing the liquid petroleum gas fraction to a refinery alkylation unit;(g) recovering a propane fraction from the alkylation unit; and(h) passing the propane fraction to a dehydrogenation unit to produce propylene.2. The process of claim 1 , wherein the pyrolysis oil and wax of (d) is passed directly to a refinery FCC unit distillation section.3. The process of claim 1 , wherein a gasoline and heavy fraction is recovered ...

Circular economy for plastic waste to polypropylene via refinery fcc unit

Provided is a continuous process for converting waste plastic into recycle for polypropylene polymerization. The process comprises selecting waste plastics containing polyethylene and/or polypropylene, and passing the waste plastics through a pyrolysis reactor to thermally crack at least a portion of the polyolefin waste and produce a pyrolyzed effluent. The pyrolyzed effluent is separated into offgas, a naphtha/diesel fraction, a heavy fraction, and char. Pyrolysis oil and wax, comprising naphtha/diesel and heavy fractions, is passed to a refinery FCC unit. A liquid petroleum gas C 3 olefin/paraffin mixture is recovered from the FCC unit. The C 3 paraffins and C 3 olefins are separated into different fractions with the C 3 olefin fraction passed to a propylene polymerization reactor, and the C 3 paraffin fraction passed optionally to a dehydrogenation unit to produce additional propylene.

Use of renewable oil in hydrotreatment process

The use of bio oil from at least one renewable source in a hydrotreatment process, in which process hydrocarbons are formed from said glyceride oil in a catalytic reaction, and the iron content of said bio oil is less than 1 w-ppm calculated as elemental iron. A bio oil intermediate including bio oil from at least one renewable source and the iron content of said bio oil is less than 1 w-ppm calculated as elemental iron.

Hydrodynamic Cavitation Process to Protect Catalytic Processes Used to Deoxygenate Complex Mixtures of Natural Occurring Fats & Oils Into Oxygen-Free Hydrocarbons

The present invention relates to the production of high value bio-chemicals, in particular bio-paraffins, bio-LPG, bio-naphtha, bio-jet and bio-distillates in an integrated bio-refinery from complex mixtures of natural occurring fats & oils. 112.-. (canceled)13. A process for the production of high value bio-chemicals comprising paraffins , LPG , jet fuel , diesel and naphtha , from natural occurring oil(s) containing acyl-containing compounds having 10 to 24 carbons including fatty acid esters and free fatty acids , and other components including impurities , comprising the steps of:(a) refining the natural occurring oil(s) to remove at least a part of the impurities and to obtain a refined oil,(b) optionally pre-treating the refined oil to further remove impurities and to obtain a pre-treated oil, a hydrodynamic cavitation processing of the natural occurring oil(s) in presence of water under conditions efficient to generate cavitation features and to transfer at least a part of impurities contained in the natural occurring oil(s) into an aqueous phase, and', 'separating the aqueous phase from an oil phase and recovering the oil phase as a refined oil., '(c) hydroprocessing the refined oil or the pre-treated oil in presence of dihydrogen and of at least one catalyst to transform fatty acid esters and free fatty acids contained in said refined oil or pre-treated oil into linear or substantially linear paraffins, where the hydroprocessing is chosen among hydrodeoxygenation, decarboxylation and decarbonylation, characterized in that the refining step (a) includes'}14. The process according to wherein the natural occurring oil(s) contain(s) one or several oils chosen among vegetable oil claim 13 , animal fat claim 13 , waste oils claim 13 , by-products of the refining of vegetable oil(s) or of animal oil(s) containing free fatty acids claim 13 , tall oils claim 13 , and oil produced by bacteria claim 13 , yeast claim 13 , algae claim 13 , prokaryotes or eukaryotes.15. ...

UPGRADING POLYNUCLEARAROMATIC HYDROCARBON-RICH FEEDS

A method of upgrading refining streams with high polynucleararomatic hydrocarbon (PNA) concentrations can include: hydrocracking a PNA feed in the presence of a catalyst and hydrogen at 380° C. to 430° C., 2500 psig or greater, and 0.1 hrto hrliquid hourly space velocity (LSHV), wherein the weight ratio of PNA feed to hydrogen is 30:1 to 10:1, wherein the PNA feed comprises 25 wt % or less of hydrocarbons having a boiling point of 700° F. (371° C.) or less and having an aromatic content of 50 wt % or greater to form a product comprising 50 wt % or greater of the hydrocarbons having a boiling point of 700° F. (371° C.) or less and having an aromatic content of 20 wt % or less. 1. A method comprising:{'sup': −1', '−1, 'hydrocracking a polynucleararomatic hydrocarbon (PNA) feed in the presence of a catalyst and hydrogen at 380° C. to 430° C., 2500 psig or greater, and 0.1 hrto 5 hrliquid hourly space velocity (LSHV), wherein the weight ratio of PNA feed to hydrogen is 30:1 to 10:1, wherein the PNA feed comprises 25 wt % or less of hydrocarbons having a boiling point of 700° F. (371° C.) or less and having an aromatic content of 50 wt % or greater to form a product comprising 50 wt % or greater of the hydrocarbons having a boiling point of 700° F. (371° C.) or less and having an aromatic content of 20 wt % or less.'}2. The method of claim 1 , wherein the PNA feed comprises 2 wt % or greater sulfur.3. The method of further comprising distilling the product to produce one or more fractions selected from the group consisting of: a C paraffin stream comprising less than 15 ppm sulfur claim 1 , a naphtha fraction having less than 15 ppm sulfur claim 1 , a distillate fraction having less than 15 ppm sulfur claim 1 , and a 700+° F. (371+° C.) boiling point stream having less than 15 ppm sulfur.4. The method of claim 1 , wherein the aromatic content of the PNA feed is 70 wt % or greater and the aromatic content of product is 10 wt % or less.5. The method of claim 1 , wherein ...

PROCESS FOR LPG RECOVERY

Process and plant for recovering LPG in a refinery process combining the use of sponge absorber, deethanizer and debutanizer. The process and plant enable high LPG recovery and removal of hydrogen sulphide in the LPG product to low levels. 1. A process for recovering LPG from the fractionation section of a refinery process comprising the steps of:(a) passing a feed stream comprising a stripper overhead product through a sponge absorber, and separating an off-gas stream from the top section of the sponge absorber and a light oil stream from the bottom section of the sponge absorber; and{'sub': '3', '(b) fractionating the light oil stream into (i) an overhead vapour in the form of a Cstripped stream comprising less than 20% butane or propane, without condensing and without recycling of condensed overhead vapour into this fractionating step, (ii) a LPG product stream, and (iii) a stabilized naphtha stream.'}2. The process according to further comprising mixing at least a portion of the Cstripped stream of step (b) with stripper overhead product to form said feed stream of step (a).3. The process according to comprising mixing a portion of the stabilized naphtha stream of step (b) with the off-gas stream of step (a).4. The process according to in which step(b) comprises the sub-steps:{'sub': '3', '(b1) fractionating the light oil stream in a deethanizer column, and separating the overhead vapour in the form of said Cstripped stream from the top section of the deethanizer column;'}(b2) fractionating a stream from the bottom section of the deethanizer column in a debutanizer column, separating said LPG product stream from the top section of the debutanizer column, and said stabilized naphtha stream from the bottom section of the debutanizer column.5. The process according to further comprising using a portion of vapour from the debutanizer column as stripping vapour for the deethanizer column.6. The process according to further comprising feeding the vapour from the ...

Raffinate-2 Refining Method

Provided is a method of separating and refining 1-butene with a high purity and a high yield from a raffinate-2 stream, and recovering the refined 1-butene while maximizing an energy saving rate by using a high efficiency distillation column installed with a separation wall.

Process and system for hydrogenation, hydrocracking and catalytic conversion of aromatic complex bottoms

Processes and systems are disclosed for improving the yield from reforming processes. Aromatic complex bottoms, or a heavy fraction thereof, are subjected to hydrogenation/hydrocracking, followed by catalytic conversion, to produce additional gasoline and higher-quality aromatic compounds.

USE OF REFINERY FUEL GAS TO IMPROVE STEAM REFORMER PRESSURE SWING ADSORPTION PROCESSES

A process is disclosed for producing hydrogen for a hydrogen consuming process comprising obtaining a gas stream containing hydrogen from a steam reforming hydrogen plant, sending the gas stream to a pressure swing adsorption unit to be separated into a hydrogen stream and a fuel gas stream; purging the pressure swing adsorption unit with an external purge gas stream from a hydroprocessing unit off gas; treating the off gas with a thermal swing adsorption unit to remove water and other impurities prior to purging the pressure swing adsorption unit; and using a protective adsorbent layer in the pressure swing adsorption unit at the product-hydrogen end of the bed to adsorb impurities from the external purge gas. 1. A process for producing hydrogen for a hydrogen consuming process comprising:obtaining a gas stream containing hydrogen from a steam reforming hydrogen plant;sending the gas stream to a pressure swing adsorption unit to be separated into a hydrogen stream and a fuel gas stream;purging said pressure swing adsorption unit with an external purge gas stream from a hydroprocessing unit off gas;treating said off gas with a thermal swing adsorption unit to remove water and other impurities prior to purging said pressure swing adsorption unit; andusing a protective adsorbent layer in said pressure swing adsorption unit at the product-hydrogen end of the bed to adsorb impurities from said external purge gas.2. The process of wherein said external purge gas stream is a flash gas stream from a hydrocracking reactor.3. The process of wherein said external purge gas stream is a flash gas stream from a hydrotreating reactor.4. The process of wherein said external purge gas stream is at a pressure of about 35 to 276 kPa (5 to 40 psig) when entering said pressure swing adsorption unit.5. The process of wherein said external purge gas stream is mixed with an internal purge gas stream obtained from de-pressurizing a bed in the pressure swing adsorption unit.6. The process ...

Apparatus and Process for the Hydroconversion of Heavy Oil Products

The present invention relates to an apparatus for the hydroconversion of heavy oil products (the fresh load). Said apparatus comprises: a slurry bubble column hydroconversion reactor, which comprises a feed line in which the fresh load and the recirculated slurry phase are conveyed, an inlet line for a hydrogenating stream and an outlet for a reaction effluent through an outlet nozzle; a stripping column at high pressure and high temperature placed downstream of the reactor and directly connected to the reactor head through a pipeline in which the reaction effluent flows; said column having an inlet line for a stripping gas, an inlet for the reactor effluent, a head outlet for steam and an outlet for the slurry phase; lines and means for recirculating the slurry leaving the stripping column; lines and means for taking a drain stream, which has the function of preventing the accumulation of solids in the reactor. The stripping column is characterized in that it contains one or more contact devices that allow physical contact to be created between different phases. 1. Apparatus for the hydroconversion of heavy oil products which constitute the fresh load , said apparatus comprising:a slurry bubble column hydroconversion reactor, which comprises a feed line in which the fresh load and the recirculated slurry phase are conveyed, an inlet line for a hydrogenating stream and an outlet for a reaction effluent through an outlet nozzle;a high pressure and high temperature stripping column placed downstream of the reactor and directly connected to the reactor head through a pipeline in which the reaction effluent flows; said column having an inlet line for a stripping gas, an inlet for the reactor effluent, a head outlet for steam and an outlet for the slurry phase;lines and means for recirculating the slurry leaving the stripping column;lines and means for taking a drain stream, which has the function of preventing the accumulation of solids in the reactor;said stripping ...

CHEMICAL COMPOSITIONS AND METHODS OF USING SAME FOR REMEDIATING SULFUR-CONTAINING COMPOSITIONS AND OTHER CONTAMINANTS IN LIQUIDS AND GASES

A treatment process for remediating HS and other contaminants in liquids includes: partially filling a closed vessel with a contaminated liquid containing ≥5 ppm HS with a head space above the liquid within the vessel where gasses released from the liquid from the liquid collect; separately providing a treatment composition in the head space so that the gasses from the liquid may contact the treatment composition; and permitting the contact between the vapors from the liquid and the treatment composition to continue until a collective concentration of HS in the liquid and in the head space is <5 ppm. The treatment composition includes an aqueous solution containing at least one hydroxide compound, a collective concentration of the at least one hydroxide compound in the aqueous solution is in a range of 35-55 weight %, and the aqueous solution constitutes at least 80 weight % of the treatment composition. 1. A treatment process for remediating HS and other contaminants in contaminated liquids comprising steps of: disposing an amount of a contaminated liquid containing ≥5 ppm HS in a closed vessel such that the liquid partially fills the vessel and a head space is defined within the vessel above the liquid where vapors from the liquid collect; providing a treatment composition in the head space such that the vapors from the liquid may contact the treatment composition; and permitting the contact between the vapors from the liquid and the treatment composition to continue until a collective concentration of HS in the liquid and in the head space is <5 ppm , wherein the treatment composition includes an aqueous hydroxide solution containing at least one hydroxide compound , a collective concentration of the at least one hydroxide compound in the aqueous hydroxide solution is in a range of 35-55 weight % , and the aqueous hydroxide solution constitutes at least 80 weight % of the treatment composition.2. The treatment process according to claim 1 , wherein the reaction ...

SYSTEM FOR CONVERSION OF CRUDE OIL TO PETROCHEMICALS AND FUEL PRODUCTS INTEGRATING STEAM CRACKING AND FLUID CATALYTIC CRACKING

Process scheme configurations are disclosed that enable conversion of crude oil feeds with several processing units in an integrated manner into petrochemicals. The designs utilize minimum capital expenditures to prepare suitable feedstocks for the steam cracker complex. The integrated process for converting crude oil to petrochemical products including olefins and aromatics, and fuel products, includes mixed feed steam cracking and fluid catalytic cracking. Feeds to the mixed feed steam cracker include light products and naphtha from hydroprocessing zones within the battery limits, recycle streams from the C3 and C4 olefins recovery steps, and raffinate from a pyrolysis gasoline and FCC naphtha aromatics extraction zone within the battery limits. 118.-. (canceled)19. An integrated system for producing petrochemicals and fuel products comprising:an atmospheric distillation unit (ADU) operable to receive and separate a feed, and discharge a first ADU fraction comprising naphtha, a second ADU fraction comprising at least a portion of middle distillates from the feed, and a third ADU fraction comprising atmospheric residue;a vacuum distillation unit (VDU) operable to receive and separate the third ADU fraction, and discharge a first VDU fraction comprising vacuum gas oil;a distillate hydroprocessing (DHP) zone operable to receive and convert middle distillates from the second ADU fraction into a first DHP fraction and a second DHP fraction, wherein the first DHP fraction comprises naphtha and the second DHP fraction is used for diesel fuel production;a fluid catalytic cracking (FCC) zone operable to receive and convert the first VDU fraction into a first FCC fraction containing light olefins, a second FCC fraction containing FCC naphtha and a third FCC fraction containing cycle oil;a steam cracking zone comprising a mixed feed steam cracking (MFSC) zone operable to receive and thermally crack a C6-C9 non-aromatics raffinate stream derived from an aromatics extraction ...

CATALYTIC CRACKING PROCESS FOR PRODUCING ISOBUTANE AND/OR LIGHT AROMATICS IN HIGH YIELD

Disclosed is a catalytic cracking process for producing isobutane and/or light aromatics in high yield, comprising the steps of: a) providing a catalytic cracking feedstock oil having a polycyclic naphthene content of greater than about 25 wt %; b) subjecting the catalytic cracking feedstock oil to a first catalytic cracking reaction and a second catalytic cracking reaction sequentially under different reaction conditions to obtain a catalytic cracking product; c) separating the resulting catalytic cracking product to obtain a liquefied gas fraction comprising isobutane and a gasoline fraction comprising light aromatics; and d) optionally, recovering isobutane from the liquefied gas fraction and/or recovering light aromatics from the gasoline fraction. The process can enable the production of isobutane and/or light aromatics in high yield. 1. A catalytic cracking process , comprising the steps of:a) providing a catalytic cracking feedstock oil having a polycyclic naphthene content of greater than about 25 wt %, preferably greater than about 40 wt %, based on the weight of the catalytic cracking feedstock oil;b) contacting the catalytic cracking feedstock oil with a catalytic cracking catalyst in a catalytic cracking reactor, and subjecting the mixture to a first catalytic cracking reaction and a second catalytic cracking reaction sequentially under different reaction conditions to obtain a catalytic cracking product;c) separating the resulting catalytic cracking product to obtain a liquefied gas fraction comprising isobutane and a gasoline fraction comprising light aromatics; andd) optionally, recovering isobutane from the liquefied gas fraction and/or recovering light aromatics from the gasoline fraction.2. The process according to claim 1 , wherein the separation in the step c) also produces a light cycle oil fraction claim 1 , a heavy cycle oil fraction claim 1 , and optionally a slurry oil claim 1 , and the process further comprises the steps of:e) subjecting at ...

PROCESS AND SYSTEM FOR CRACKING A HYDROCARBON FEED

A process for hydrocracking a hydrocarbon feed is provided. The process comprises hydrocracking the hydrocarbon feed to produce a first hydrocracking product stream, separating the first hydrocracking product stream to form a gas stream and a liquid stream, hydrocracking the liquid stream to produce a second hydrocracking product stream, separating the second hydrocracking product stream to form a first light stream and a first heavy stream comprising benzene, toluene, xylene, C hydrocarbon, or a combination comprising at least one of the foregoing, purifying the gas stream to form a purified gas stream, and separating the purified gas stream to form at least two of a hydrogen stream, Cstream, Cstream, Cstream, Cstream, C stream, or a combination comprising at least one of the foregoing. 1. A process for hydrocracking a hydrocarbon feed , comprising:hydrocracking the hydrocarbon feed to produce a first hydrocracking product stream;separating the first hydrocracking product stream to form a gas stream and a liquid stream;hydrocracking the liquid stream to produce a second hydrocracking product stream;{'sub': '9+', 'separating the second hydrocracking product stream to form a first light stream and a first heavy stream comprising benzene, toluene, xylene, C hydrocarbon, or a combination comprising at least one of the foregoing;'}purifying the gas stream to form a purified gas stream; and{'sub': 1', '2', '3', '4', '5+, 'separating the purified gas stream to form at least two of a hydrogen stream, Cstream, Cstream, Cstream, Cstream, C stream, or a combination comprising at least one of the foregoing.'}2. The process of claim 1 , wherein the gas stream comprises hydrogen and C-Chydrocarbons and the liquid stream comprises C hydrocarbons.3. The process of claim 1 , wherein the second hydrocracking product stream comprises a C hydrocarbon claim 1 , benzene claim 1 , toluene claim 1 , xylene claim 1 , C hydrocarbon claim 1 , or a combination comprising at least one of the ...

Method for quenching pyrolysis product

A method for quenching a pyrolysis product, including: supplying a discharge stream from a liquid decomposition furnace to a first quench tower; supplying an upper discharge stream from the first quench tower to a second quench tower; supplying a discharge stream from a first gas decomposition furnace to the second quench tower; and supplying a discharge stream from a second gas decomposition furnace to the second quench tower.

LIGHT OIL REFLUX HEAVIES REMOVAL PROCESS

The invention relates to various nonlimiting embodiments that include methods, apparatuses or systems for processing natural gas comprising a heavies removal column processing natural gas and light oil reflux. The overhead stream goes to heavies treated natural gas storage. The heavies removal column reboiler bottoms stream product is input to a debutanizer column. The debutanizer column overhead lights are input to a flash drum where the bottoms is pumped through a heat exchanger as a light oil reflux input to the heavies removal column, while the debutanizer reboiler bottoms product is stored as stabilized condensate. Alternatively, debutanizer column overhead lights are sent to heavies treated gas storage and the bottoms stream product goes to a depentanizer column, the overhead lights are pumped through a heat exchanger as a light oil reflux input to the heavies removal column, while the depentanizer reboiler bottoms product is stabilized condensate. 1. A method for natural gas processing comprising:a) introducing a natural gas feed to a heavies removal column;b) introducing a light oil reflux gas feed to the heavies removal column;c) processing the natural gas feed and the light oil reflux gas feed in the heavies removal column to produce a first bottoms stream and a first overhead stream, wherein the first bottoms stream and the first overhead stream are separate streams upon expulsion from the heavies removal column, wherein the first bottoms stream is routed to a first reboiler to separate a first reboiler bottom stream product and then route the first reboiler bottom stream product to a debutanizer column and the first overhead stream is routed to heavies treated natural gas storage;d) processing the first reboiler bottoms stream product in the debutanizer column to produce a second bottoms stream and a second overhead stream, wherein the second bottoms stream and the second overhead stream are separate streams upon expulsion from the debutanizer column, ...

Process for producing aromatics from a heavy hydrocarbon feed

The present invention relates to a process for producing monoaromatic hydrocarbons from a hydrocarbon feed comprising polyaromatics, the process comprising contacting said feed in the presence of hydrogen with a M/A/zeolite catalyst under hydrocracking process conditions.

USE OF RENEWABLE OIL IN HYDROTREATMENT PROCESS

The use of bio oil from at least one renewable source in a hydrotreatment process, in which process hydrocarbons are formed from said glyceride oil in a catalytic reaction, and the iron content of said bio oil is less than 1 w-ppm calculated as elemental iron. A bio oil intermediate including bio oil from at least one renewable source and the iron content of said bio oil is less than 1 w-ppm calculated as elemental iron. 121-. (canceled)22. A method for avoiding catalyst plugging that causes an increase in the pressure drop of the hydrotreatment reactor during hydrotreatment comprising: purifying a biological feedstock from at least one renewable source to lower the content of impurities having a correlation between the rate of increase in the pressure drop measured as bar/kg of biological feedstock and the concentration of impurity measured in ppm that is greater than 0.14 , to a value between 0.25 to 1 w-ppm; hydrotreating the purified biological feedstock from at least one renewable source with a catalyst to form hydrocarbons during a catalytic reaction in a trickle bed reactor; and avoiding plugging of the catalyst used in hydrotreating that causes an increase in the pressure drop of the hydrotreatment reactor.23. The method according to claim 22 , wherein the correlation is 0.75 or greater.24. The method according to claim 22 , wherein the impurities that are lowered each have a concentration above 1 ppm before purification.25. The method according to claim 22 , claim 22 , or wherein the impurities that are lowered to a value between 0.25 to 1 w-ppm include iron.26. The biological feedstock intermediate according to claim 22 , wherein the impurities are lowered to a value between 0.25 to 0.5 w-ppm.27. The method according to claim 22 , wherein the biological feedstock is selected from the group consisting of rapeseed oil claim 22 , colza oil claim 22 , canola oil claim 22 , tall oil claim 22 , sunflower oil claim 22 , soybean oil claim 22 , hempseed oil claim ...

Method for Separating Normal Paraffin and Isoparaffin from Hydrocarbon Oil

Provided is a method for separating normal paraffin and isoparaffin from raffinates of a benzene, toluene, and xylene (BTX) reforming process including C5 to C8 light naphtha, the method including: a liquid hydrogenation process for removing olefin by feeding raffinates in which hydrogen is dissolved into a reactor filled with a hydrogenation catalyst. 1. A method for separating normal paraffin and isoparaffin from raffinates of a benzene , toluene , and xylene (BTX) reforming process including C5 to C8 light naphtha , the method comprising:a liquid hydrogenation process for removing olefin by feeding raffinates in which hydrogen is dissolved into a reactor filled with a hydrogenation catalyst, [{'br': None, 'i': A', '/A, 'sub': 1', '2, '16≤≤35\u2003\u2003[Equation 1]'}, {'br': None, 'i': A', '/A, 'sub': 3', '2, 'sup': '4', '1.5≤≤2.5\u2003\u2003[Equation 2]'}], 'wherein the liquid hydrogenation process is performed under conditions satisfying Equations 1 and 2 belowin Equations 1 and 2,{'sub': '1', 'sup': '−1', 'Ais a space velocity (Hr) of reactants in the reactor,'}{'sub': '2', 'Ais a ratio of a molar amount of dissolved hydrogen gas with respect to a molar amount of olefin in the raffinates in which hydrogen is dissolved, and'}{'sub': '3', 'sup': '−1', 'Ais a space velocity (Hr) of the raffinates in which hydrogen is dissolved in the reactor.'}2. The method of claim 1 , wherein in the liquid hydrogenation process claim 1 , a ratio of a molar amount of dissolved hydrogen gas with respect to a molar amount of olefin in the raffinates in which hydrogen is dissolved is 1.0 to 1.5.3. The method of claim 1 , wherein the liquid hydrogenation process is performed at a temperature outside the reactor of 45 to 55° C. and a pressure in the reactor of 15 to 30 kg/cmg.4. The method of claim 1 , wherein the liquid hydrogenation process has a recycle ratio of 2.5 to 5.0.5. The method of claim 1 , wherein the space velocity in the reactor of the raffinates in which hydrogen is ...

C3+ RECOVERY WITH MEMBRANES

A method of separating hydrocarbons containing three or more carbon atoms from an off-gas stream is provided. This method includes separating a light ends stream from a fractionator, thereby producing a stream rich in hydrocarbons containing three or more carbon atoms, and a stream lean in hydrocarbons containing three or more carbon atoms, separating the stream lean in hydrocarbons containing three or more carbon atoms in a membrane unit, thereby producing a permeate stream enriched in hydrocarbons containing three or more carbon atoms and a retentate stream, and separating the stream rich in hydrocarbons containing three or more carbon atoms in one or more separation columns, thereby producing one or more streams selected from the group consisting of a propylene stream, a propane stream, a butane stream, a light cat naptha stream, and a heavy cat naptha stream. 1. A method of separating hydrocarbons containing three or more carbon atoms from an off-gas stream , comprising:{'b': 204', '203', '210', '211', '212, 'a) separating a light ends stream () from a fractionator () comprising hydrocarbons containing three or more carbon atoms in main absorption unit (), thereby producing a stream rich in hydrocarbons containing three or more carbon atoms (), and a stream lean in hydrocarbons containing three or more carbon atoms (),'}{'b': 212', '501', '503', '502, 'b) separating the stream lean in hydrocarbons containing three or more carbon atoms () in a membrane unit (), thereby producing a permeate stream enriched in hydrocarbons containing three or more carbon atoms () and a retentate stream (), and'}{'b': 211', '217, 'c) separating the stream rich in hydrocarbons containing three or more carbon atoms () in one or more separation columns (), thereby producing one or more streams selected from the group consisting of a propylene stream, a propane stream, a butane stream, a light cat naptha stream, and a heavy cat naptha stream.'}2503203. The method of claim 1 , wherein ...

PROCESS FOR LPG RECOVERY

Process and plant for recovering LPG in a refinery process combining the use of sponge absorber, deethanizer and debutanizer. The process and plant enable high LPG recovery and removal of hydrogen sulphide in the LPG product to low levels. 1. A system for recovering LPG from a fractionation section of a refinery process , the system comprising: an inlet for receiving a stream comprising a stripper overhead product;', 'a top section for producing an off-gas stream, the top section comprising an outlet for withdrawing the off-gas stream; and', 'a bottom section for producing a light oil stream, the bottom section comprising an outlet for withdrawing the light oil stream;, 'a sponge absorber comprising an inlet for receiving the light oil stream from the sponge absorber;', {'sub': '3', 'a top section for producing an overhead vapour in the form of a Cstripped stream, the top section being provided with no overhead condenser and comprising an outlet for withdrawing the overhead vapour; and'}, 'a bottom section for producing a bottoms stream, the bottom section comprising an outlet for withdrawing the bottoms stream; and, 'a deethanizer column comprising an inlet for receiving the bottoms stream from the deethanizer column;', 'a top section for producing a LPG product stream, the top section comprising an outlet for withdrawing the LPG product stream; and', 'a bottom section for producing a stabilized naphtha stream, the bottom section comprising an outlet for withdrawing the stabilized naphtha stream., 'a debutanizer column comprising2. The system of claim 1 , wherein the deethanizer column and debutanizer column are provided as a single column in the form of a dividing wall column.3. The system of claim 2 , wherein the dividing wall column comprises a dividing wall disposed at the upper section of the dividing wall column.4. The system of comprising an overhead condenser and overhead drum to receive the off-gas stream from the top section of the sponge absorber.5. The ...

PROCESS FOR RECOVERING NATURAL GAS LIQUIDS FROM NATURAL GAS PRODUCED IN REMOTE LOCATIONS

Disclosed is a method to reduce the environmental impact of flaring a natural gas feedstream by removing and recovering some or all natural gas liquids (NGLs) () from the natural gas feedstream () prior to flaring (). One embodiment of the present method provides for the use of a regenerable adsorbent media to remove the NGLs from the natural gas which can be regenerated by a microwave heating system. Said regeneration step may be operated as a batch process, a semi-continuous process, or a continuous process. 1. A method for separating and recovering some or all natural gas liquids (NGLs): ethane , propane , butane , pentane , or heavier hydrocarbons from a natural gas feedstream forming a methane-rich natural gas supply and then flaring said methane-rich natural gas supply , wherein the NGLs are separated from the natural gas feedstream by means of a NGLs separation unit , wherein the NGLs separation unit comprises:(i) an adsorption unit comprising an adsorption bed comprising an adsorbent media which adsorbs NGLs to form a loaded adsorbent mediaand(ii) a regeneration unit comprising a means to regenerate loaded adsorbent media by causing the release of adsorbed NGLs from the loaded adsorbing media and forming regenerated adsorbent media (a) passing the natural gas feedstream through the adsorption unit generating the adsorbent loaded with NGLs and a methane-rich natural gas supply,', '(b) transporting the adsorbent loaded with NGLs from the adsorption unit to the regeneration unit,', '(c) regenerating the adsorbent loaded with NGLs by releasing the adsorbed NGLs from the loaded adsorbing media and forming regenerated adsorbent media', '(d) transporting the regenerated adsorbent media back to the adsorption unit for reuse,', '(e) recovering the released NGLs,', 'and', '(f) flaring the methane-rich natural gas supply., 'wherein the method comprises the steps of2. The method of wherein the natural gas feedstream is from an oil well claim 1 , a gas well claim 1 , or ...

Fcc feed additive for propylene/butylene maximization

An injection of a small amount of sweet vacuum residue into an FCC feed consisting of sweet gas oil combined with shape selective technology improves propylene and butylene yields significantly.

USE OF RENEWABLE OIL IN HYDROTREATMENT PROCESS

The use of bio oil from at least one renewable source in a hydrotreatment process, in which process hydrocarbons are formed from said glyceride oil in a catalytic reaction, and the iron content of said bio oil is less than 1 w-ppm calculated as elemental iron. A bio oil intermediate including bio oil from at least one renewable source and the iron content of said bio oil is less than 1 w-ppm calculated as elemental iron. 1. A method for preparing a hydrocarbon , the method comprising:subjecting a bio oil from at least one renewable source to a hydrotreatment process, wherein in the hydrotreatment process, hydrocarbons are formed from said bio oil in a catalytic reaction employing a catalyst,wherein an iron content of said bio oil is less than 1 w-ppm calculated as elemental iron.221-. (canceled) This application claims the benefit of priority of U.S. patent application Ser. No. 14/932,566, filed Nov. 4, 2015, in turn, to U.S. patent application Ser. No. 14/273,024, filed May 8, 2014, now U.S. Pat. No. 9,206,092 issued Dec. 8, 2015, in turn, to U.S. patent application Ser. No. 13/397,236, filed Feb. 15, 2012, now. U.S. Pat. No. 8,742,185 issued Jun. 3, 2014, in turn, to U.S. Provisional Application No. 61/443,161 filed Feb. 15, 2011, the entire contents of which are herein incorporated by reference. U.S. patent application Ser. No. 13/397,236 also claims the benefit of priority under 35 U.S.C. § 119 to European Patent Application No. 11154437.5 filed in Europe on Feb. 15, 2011, the entire contents of which are herein incorporated by reference.Disclosed is the use of renewable oil in a hydrotreatment process, for example, for the production of hydrocarbons. Also disclosed is the use of renewable oil comprising less than 1 ppm of iron, for the production of liquid fuel components or components which can be converted to liquid fuels.Liquid fuel components are mainly based on crude oil. There is an ever growing demand for liquid fuels with lower COemissions compared to ...

CHEMICAL COMPOSITIONS AND METHODS FOR REMEDIATING HYDROGEN SULFIDE AND OTHER CONTAMINANTS IN HYDROCARBON BASED LIQUIDS AND AQUEOUS SOLUTIONS WITHOUT THE FORMATION OF PRECIPITATES OR SCALE

A treatment process for remediating a contaminated liquid containing more than 5 ppm hydrogen sulfide (HS) and substantially without formation of precipitate, includes steps of steps of adding an aqueous solution containing at least one hydroxide compound at a collective concentration of 35-55 wt % to the contaminated liquid to achieve a concentration of 125-5000 ppm of the hydroxide compounds in the contaminated liquid, adding at least one organic acid and to the liquid to achieve a concentration of 0.01-10 ppm in the contaminated liquid, and dispersing the aqueous solution and the at least one organic acid in the contaminated liquid and allowing the aqueous solution and the at least one organic acid to react with the contaminated liquid for a period of time until a concentration of hydrogen sulfide in the contaminated liquid is reduced to ≤5 ppm. 1. An aqueous based treatment solution for remediating hydrogen sulfide (HS) and other contaminants in liquids and substantially without formation of precipitate , the treatment solution comprising:at least one hydroxide compound;at least one organic acid selected from a group consisting of a fulvic acid and a humic acid; andwater, whereina collective concentration of the at least one hydroxide compound in the treatment solution is in a range of 35-55 weight %,a content of water in the treatment solution is at least 30 weight %, anda collective concentration of the at least one organic acid in the treatment solution is at least 0.01 weight %.2. The treatment solution according to claim 1 , wherein the collective concentration of the at least one hydroxide in the solution is 45-55 weight %.3. The treatment solution according to claim 1 , wherein the treatment solution contains at least two different hydroxide compounds.4. The treatment solution according to claim 1 , wherein the treatment solution contains sodium hydroxide (NaOH) and potassium hydroxide (KOH).5. The treatment solution according to claim 1 , wherein the ...

PROCESS FOR PRODUCING LPG AND BTX

The invention relates to a process for producing LPG and BTX, comprising a) subjecting a mixed hydrocarbon stream to first hydrocracking in the presence of a first hydrocracking catalyst to produce a first hydrocracking product stream; b) separating the first hydrocracking product stream to provide at least a light hydrocarbon stream comprising at least C2 and C3 hydrocarbons, a middle hydrocarbon stream consisting of C4 and/or C5 hydrocarbons and a heavy hydrocarbon stream comprising at least C6+ hydrocarbons and c) subjecting the heavy hydrocarbon stream to second hydrocracking in the presence of a second hydrocracking catalyst to produce a second hydrocracking product stream comprising BTX, wherein the second hydrocracking is more severe than the first hydrocracking, d) wherein at least part of the middle hydrocarbon stream is subjected to C4 hydrocracking optimized for converting C4 hydrocarbons into C3 hydrocarbons in the presence of a C4 hydrocracking catalyst to produce a C4 hydrocracking product stream. 1. A process for producing LPG and BTX , comprisinga) subjecting a mixed hydrocarbon stream to first hydrocracking in the presence of a first hydrocracking catalyst to produce a first hydrocracking product stream;b) separating the first hydrocracking product stream to provide at leasta light hydrocarbon stream comprising at least C2 and C3 hydrocarbons,a middle hydrocarbon stream consisting of C4 and/or C5 hydrocarbons anda heavy hydrocarbon stream comprising at least C6+ hydrocarbons andc) subjecting the heavy hydrocarbon stream to second hydrocracking in the presence of a second hydrocracking catalyst to produce a second hydrocracking product stream comprising BTX, wherein the second hydrocracking is more severe than the first hydrocracking,wherein at least part of the middle hydrocarbon stream is subjected to C4 hydrocracking optimized for converting C4 hydrocarbons into C3 hydrocarbons in the presence of a C4 hydrocracking catalyst to produce a C4 ...

Process for producing lpg and btx

The invention relates to a process for producing LPG and BTX, comprising a) subjecting a mixed hydrocarbon feedstream to first hydrocracking in the presence of a first hydrocracking catalyst to produce a first hydrocracking product stream; b) separating the first hydrocracking product stream to provide at least a light hydrocarbon stream comprising at least C2 and C3 hydrocarbons, a middle hydrocarbon stream comprising C4 and/or C5 hydrocarbons and a heavy hydrocarbon stream comprising at least C6+ hydrocarbons and c) subjecting the heavy hydrocarbon stream to second hydrocracking to produce a second hydrocracking product stream comprising BTX, wherein the second hydrocracking is more severe than the first hydrocracking, wherein at least part of the middle hydrocarbon stream is recycled back to the first hydrocracking in step a).

PROCESS FOR PRODUCING C2 AND C3 HYDROCARBONS

The invention relates to a process for producing C2 and C3 hydrocarbons, comprising a) subjecting a mixed hydrocarbon feedstream to first hydrocracking in the presence of a first hydrocracking catalyst to produce a first hydrocracking product stream; b) separating the first hydrocracking product stream to provide a light hydrocarbon stream comprising C4− hydrocarbons and c) subjecting the light hydrocarbon stream to C4 hydrocracking in the presence of a C4 hydrocracking catalyst to obtain a C4 hydrocracking product stream comprising C2 and C3 hydrocarbons. 1. A process for producing C2 and C3 hydrocarbons , comprisinga) subjecting a mixed hydrocarbon feedstream to first hydrocracking in the presence of a first hydrocracking catalyst to produce a first hydrocracking product stream;b) separating the first hydrocracking product stream to provide a light hydrocarbon stream comprising C4− hydrocarbons andc) subjecting the light hydrocarbon stream to C4 hydrocracking optimized for converting C4 hydrocarbons into C3 hydrocarbons in the presence of a C4 hydrocracking catalyst to obtain a C4 hydrocracking product stream comprising C2 and C3 hydrocarbons.2. The process according to claim 1 , wherein the first hydrocracking is a hydrocracking process suitable for converting a hydrocarbon feed that is relatively rich in naphthenic and paraffinic hydrocarbon compounds to a stream rich in LPG and aromatic hydrocarbons.3. The process according to claim 1 , wherein the first hydrocracking catalyst is a catalyst containing one metal or two or more metals of group VIII claim 1 , VI B or VII B of the periodic classification of elements deposited on a carrier.4. The process according to claim 1 , wherein the C4 hydrocracking catalyst comprises a mordenite or an erionite.5. The process according to claim 1 , wherein the C4 hydrocracking catalyst consists of a mordenite and an optional binder or comprises sulfided-nickel/H-Erionitel and the C4 hydrocracking is performed under conditions ...

SYSTEM AND METHOD FOR PRODUCTION OF CHEMICAL FEEDSTOCK FROM CRUDE OIL

The present disclosure provides a system and method for converting crude oil to light hydrocarbon products useful as a chemical feedstock. The system may also include a conversion system, such as a steam cracking unit, that converts the chemical feedstock from the feed preparation system to useful hydrocarbon chemicals. Exemplary hydrocarbon chemicals produced by the conversion system include light olefins, such as ethylene, propylene, and/or butadiene. 1. A system for converting a crude oil feedstock to a chemical feedstock for a steam cracker unit , the system comprising: a hydrocarbon gas fraction;', 'a naphtha fraction;', 'a middle distillate fraction; and', 'a residue fraction;, 'a distillation unit that separates the crude oil feedstock into at leasta first isomerization unit having a first input that receives the hydrocarbon gas fraction from the distillation unit and a first output, the first isomerization unit establishing equilibrium by converting a branched butane in the first input to a normal butane in the first output;a naphtha hydrotreating unit that receives the naphtha fraction from the distillation unit, the naphtha hydrotreating unit saturating the naphtha fraction;a middle distillate hydrotreating unit that receives the middle distillate fraction from the distillation unit, the middle distillate hydrotreating unit saturating the middle distillate fraction;a residue hydrotreating unit that receives the residue fraction from the distillation unit, the residue hydrotreating unit saturating the residue fraction; an unsaturated gas fraction;', 'a light hydrocarbon fraction rich in olefins and aromatics;', 'a light cycle oil fraction rich in rich in multi-ring aromatics; and', 'a heavy waste fraction;, 'a cracking unit that receives the saturated residue fraction from the residue hydrotreating unit, the cracking unit converting the saturated residue fraction into at leasta butene processing unit that receives the unsaturated gas fraction from the ...

Process for upgrading refinery heavy hydrocarbons to petrochemicals

The present invention relates to a process for upgrading refinery heavy hydrocarbons to petrochemicals, comprising the following steps of: (a) feeding a hydrocarbon feedstock to a ring opening reaction area; (b) feeding the effluent from (a) to a separation unit for producing gaseous stream comprising light boiling hydrocarbons, a liquid stream comprising naphtha boiling range hydrocarbons and a liquid stream comprising diesel boiling range hydrocarbons; (c) feeding said liquid stream comprising naphtha boiling range hydrocarbons to a hydrocracking unit.

PROCESS FOR PRODUCING C2 AND C3 HYDROCARBONS

The invention relates to a process for producing C2 and C3 hydrocarbons, comprising a) subjecting a mixed hydrocarbon stream to first hydrocracking in the presence of a first hydrocracking catalyst to produce a first hydrocracking product stream; and b) subjecting the first hydrocarbon product stream to C4 hydrocracking optimized for converting C4 hydrocarbons into C3 hydrocarbons in the presence of a C4 hydrocracking catalyst to obtain a C4 hydrocracking product stream comprising C2 and C3 hydrocarbons. 1. A process for producing C2 and C3 hydrocarbons , comprisinga) subjecting a mixed hydrocarbon stream to first hydrocracking in the presence of a first hydrocracking catalyst to produce a first hydrocracking product stream; andb) subjecting the first hydrocarbon product stream to C4 hydrocracking optimized for converting C4 hydrocarbons into C3 hydrocarbons in the presence of a C4 hydrocracking catalyst to obtain a C4 hydrocracking product stream comprising C2 and C3 hydrocarbons.2. The process according to claim 1 , wherein the first hydrocracking is a hydrocracking process suitable for converting a hydrocarbon feed that is relatively rich in naphthenic and paraffinic hydrocarbon compounds to a stream rich in LPG and aromatic hydrocarbons.3. The process according to claim 1 , wherein the first hydrocracking catalyst is a catalyst containing one metal or two or more metals of group VIII claim 1 , VI B or VII B of the periodic classification of elements deposited on a carrier.4. The process according to claim 1 , wherein the C4 hydrocracking catalyst comprises a mordenite or an erionite.5. The process according to claim 1 , wherein the C4 hydrocracking catalyst consists of a mordenite and an optional binder or comprises sulfided-nickel/H-Erionite1 and the C4 hydrocracking is performed under conditions comprising a temperature between 325 and 450° C. claim 1 , a partial hydrogen pressure between 2 and 4 MPa claim 1 , a molar ratio hydrogen to hydrocarbon feed of 2:1 ...

Selective Conversion of Paraffinic Naphtha to Propane in the Presence of Hydrogen

The invention relates to Process of catalytic conversion by hydrocracking of paraffinic and naphthenic hydrocarbons from a naphtha feedstock to propane, the process comprising the steps of providing a naphtha feedstock containing one or more paraffin comprising 4 to 10 carbon atoms and no olefins; and contacting said naphtha feedstock with a catalyst composition in the presence of hydrogen in a reaction zone under hydrocracking conditions; wherein the catalyst composition consists of one or more zeolite catalysts comprising acid 10-membered ring channels containing no added metals. 115.-. (canceled)16. A process of catalytic conversion by hydrocracking of paraffinic and naphthenic hydrocarbons from a naphtha feedstock to propane , the process comprising the following steps:a. providing a naphtha feedstock containing one or more paraffins comprising 4 to 10 carbon atoms, wherein the one or more paraffins have an olefin content of less than 1 wt % relating to the total weight of said naphtha feedstock; andb. submitting said naphtha feedstock to a hydrocracking step by contacting said naphtha feedstock with a catalyst composition in the presence of hydrogen in a reaction zone under hydrocracking conditions;characterized in that the catalyst composition comprises one or more zeolite catalysts comprising an acid 10-membered ring channels and in that said catalyst composition contains no added noble metal and no added transition metals.17. The process according to claim 16 , characterized in that the naphtha feedstock comprises at least 10 wt % of naphthenes as based on the total weight of the naphtha feedstock.18. The process according to claim 16 , characterized in that the one or more zeolite catalysts have a Si/Al molar ratio ranging from 10 to 100.19. The process according to claim 16 , characterized in that the hydrocracking conditions of the hydrocracking step comprise:a. the naphtha feedstock being contacted with the catalyst composition at a temperature ranging ...

Selective Conversion of Paraffinic Naphtha to Propylene in the Presence of Hydrogen

The invention relates to a process of catalytic conversion by hydrocracking of paraffinic and naphthenic hydrocarbons from a naphtha feedstock () to propylene, the process comprising the steps of providing a naphtha feedstock () containing one or more paraffins comprising 4 to 10 carbon atoms; and contacting said naphtha feedstock () with a catalyst composition in the presence of hydrogen in a reaction zone under hydrocracking conditions; wherein the catalyst composition consists of one or more zeolite catalysts comprising acid 10-membered ring channels. 115.-. (canceled)16. A process of catalytic conversion by hydrocracking of paraffinic and naphthenic hydrocarbons from a naphtha feedstock to propylene , the process being characterized in that it comprises the following steps:a) providing a naphtha feedstock containing one or more paraffins comprising 4 to 10 carbon atoms; andb) submitting said naphtha feedstock to a hydrocracking step by contacting said naphtha feedstock with a catalyst composition in the presence of hydrogen in a reaction zone under hydrocracking conditions to produce an effluent;c) submitting the effluent to a separation step to recover propane; andd) submitting said propane to a step of dehydrogenation into propylene in a propane dehydrogenation reactor;e) collecting hydrogen produced in the step of dehydrogenation into propylene, and recycling said hydrogen back to the hydrocracking reaction zone in order to perform the hydrocracking step;and in that the catalyst composition of the hydrocracking step comprises one or more zeolite catalysts comprising one or more acid 10-membered ring channels.17. The process according to claim 16 , characterized in that the naphtha feedstock comprises at least 10 wt % of naphthenes as based on the total weight of the naphtha feedstock.18. The process according to claim 16 , characterized in that the one or more zeolite catalysts have a Si/Al molar ratio ranging from 10 to 100.19. The process according to claim ...

Catalysts and methods for reforming oxygenated compounds

Disclosed are catalysts and methods that can reform aqueous solutions of oxygenated compounds such as ethylene glycol, glycerol, sugar alcohols, and sugars to generate products such as hydrogen and alkanes. In some embodiments, aqueous solutions containing at least 20 wt% of the oxygenated compounds can be reformed over a catalyst comprising a Group VIII transition metal and a Group VIIB transition metal, preferably supported on an activated carbon-supported catalyst. In other embodiments, catalysts are provided for the production of hydrogen or alkanes at reaction temperatures less than 300°C.

Catalyst for light olefins and lpg in fluidized catalytic cracking units

Method for upgrading bio-based material and upgraded material

Provided is a method for upgrading a bio-based material, the method comprising the steps of pre-treating bio-renewable oil(s) and/or fat(s) to provide a biobased fresh feed material, hydrotreating the bio-based fresh feed material, followed by separation, to provide a bio-propane composition.

Method and apparatus for treating a hydrocarbon stream

A method of treating a hydrocarbon stream such as natural gas comprising at least the steps of: (a) providing a hydrocarbon feed stream ( 10 ); (b) passing the feed stream ( 10 ) through a first separation vessel ( 12 ) to provide a first gaseous stream ( 20 ) and a first liquid stream ( 30 ); (c) passing the first gaseous stream ( 20 ) from step (b) through a high pressure separation vessel ( 14 ) to provide a second gaseous stream ( 40 ) and a second liquid stream ( 80 ); (d) maintaining the pressure of the first gaseous stream ( 20 ) between step (b) and step (c) within +10 bar; (e) passing the first liquid stream ( 30 ) of step (b) through a stabilizer column ( 16 ) to provide a third gaseous stream ( 60 ) and a stabilized condensate ( 70 ); and (f) feeding the second liquid stream ( 80 ) from step (c) into the stabilizer column ( 16 ).

Method and apparatus for treating a hydrocarbon stream

A method of treating a hydrocarbon stream such as natural gas comprising at least the steps of: (a) providing a hydrocarbon feed stream ( 10 ); (b) passing the feed stream ( 10 ) through a first separation vessel ( 12 ) to provide a first gaseous stream ( 20 ) and a first liquid stream ( 30 ); (c) passing the first gaseous stream ( 20 ) from step (b) through a high pressure separation vessel ( 14 ) to provide a second gaseous stream ( 40 ) and a second liquid stream ( 80 ); (d) maintaining the pressure of the first gaseous stream ( 20 ) between step (b) and step (c) within +10 bar; (e) passing the first liquid stream ( 30 ) of step (b) through a stabilizer column ( 16 ) to provide a third gaseous stream ( 60 ) and a stabilized condensate ( 70 ); and (f) feeding the second liquid stream ( 80 ) from step (c) into the stabilizer column ( 16 ).

Method for improving propylene recovery from fluid catalytic cracker unit

The present invention relates to a method for treating a cracked stream stemming from a fluid catalytic cracker unit (FCCU) in order to improve propylene recovery. The present invention also relates to the corresponding installation to implement the method.

Configurations And Methods For Improved Natural Gas Liquids Recovery

Contemplated plants for recovery of NGL from natural gas employ alternate reflux streams in a first column and a residue gas bypass stream, wherein expansion of various process streams provides substantially all of the refrigeration duty in the plant. Contemplated plants not only have flexible recovery of ethane between 2% and 90% while recovering at least 99% of propane, but also reduce and more typically eliminate the need for external refrigeration.

Configurations and methods for improved natural gas liquids recovery

Contemplated plants for recovery of NGL from natural gas employ alternate reflux streams in a first column and a residue gas bypass stream, wherein expansion of various process streams provides substantially all of the refrigeration duty in the plant. Contemplated plants not only have flexible recovery of ethane between 2% and 90% while recovering at least 99% of propane, but also reduce and more typically eliminate the need for external refrigeration.

A process for simultaneous cracking of lighter and heavier hydrocarbon feed and system for the same

The invention provides for a process and apparatus for simultaneous conversion of lighter and heavier hydrocarbon feedstocks into improved yields of light olefins in the range of C2 to C4, liquid aromatics in the range C6 to C8 mainly benzene, toluene, xylene and ethyl benzene and other useful products employing at least two different reactors operated in series with respect to catalyst flow and parallel with respect to feed flow under different regimes and process conditions with same catalyst system.

Conversion of light naphtha to enhanced value products in an integrated two-zone reactor process

An integrated process for conversion of a hydrocarbon stream comprising light naphtha to enhanced value products. The process includes passing the hydrocarbon stream through a first reactor, the first reactor being a catalytic bed reactor with a dual-function catalyst to simultaneously reform light naphtha to BTEX and crack light naphtha to ethane, propane, and butanes. Further, the process includes passing an effluent of the first reactor to a gas-liquid separating unit to generate a liquid stream and a gas stream, and passing the gas stream to a gas separator unit to remove hydrogen gas and methane and generate an enhanced gas stream. The process further includes passing the enhanced gas stream through a second reactor, the second reactor being a pyrolysis unit operated at steam cracking conditions to convert ethane, propane, and butanes in the enhanced gas stream to light. An associated system for performing the process is also provided wherein the integrated process does not include passage of a process stream to a separate and independent hydrocracking unit to crack light alkanes in the hydrocarbon stream to smaller alkanes.

Process for simultaneous cracking of lighter and heavier hydrocarbon feed and system for the same

The invention provides for a process and apparatus for simultaneous conversion of lighter and heavier hydrocarbon feedstocks into improved yields of light olefins in the range of C2 to C4, liquid aromatics in the range C6 to C8 mainly benzene, toluene, xylene and ethyl benzene and other useful products employing at least two different reactors operated in series with respect to catalyst flow and parallel with respect to feed flow under different regimes and process conditions with same catalyst system.

Method for improving propylene recovery from fluid catalytic cracker unit

The present invention relates to a method for treating a cracked stream stemming from a fluid catalytic cracker unit (FCCU) in order to improve propylene recovery. The present invention also relates to the corresponding installation to implement the method.

An improved process for recovery of propylene and lpg from fcc fuel gas using stripped main column overhead distillate as absorber oil

用于生产粗产品的系统和方法

公开了一种用于将重油给料进行加氢处理的灵活性一次通过式方法。该方法使用多个接触区和至少一个分离区以将至少部分所述重油给料转化为低沸点烃，从而形成提质产物。接触区在加氢裂化条件下操作，以活性金属催化剂与重油给料比大于500wppm的浓度，使用包含烃油稀释剂中平均粒径为至少1微米的活性金属催化剂的浆料催化剂。以可互换方式对所述多个接触区和分离区进行设计以使一次通过式方法以如下模式灵活性操作：顺序模式；平行模式；平行模式和顺序模式的组合；全部在线；一些在线和一些备用；一些在线和一些离线；来自接触区的流出物料流被送至与该接触区串联的至少一个分离区的平行模式；来自接触区的流出物料流与来自至少另一个接触区的流出物料流合并并且送至分离区的平行模式；以及它们的组合。在一个实施方案中，将来自接触区的流出物送至串联的下一接触区用于进一步提质，其中下一接触区具有至多100psi的压降，压降不是由如现有技术中的减压装置引起。在一个实施方案中，将选自抑制剂添加物、消泡剂、稳定剂、金属清除剂、金属污染物去除剂、金属钝化剂和牺牲材料的至少一种添加剂物质以小于重油给料的1wt％的量加入到至少一个接触区。

用于产生长链烃分子的等离激元纳米颗粒催化剂和方法

一种通过光辐射产生烃分子的等离激元纳米颗粒催化剂，其包含至少一种等离激元供体和至少一种催化特性供体，其中等离激元供体和催化特性供体可相互接触或距离小于200nm，并且由光辐射产生的烃分子的分子组成是温度依赖性的。以及一种利用等离激元纳米颗粒催化剂通过光辐射产生烃分子的方法。

Btx和lpg的生产方法

本发明涉及一种生产BTX和LPG的方法，所述方法包括：(a)在氢存在下使含C5‑C12烃的原料物流在加氢裂化反应器中与加氢裂化催化剂接触，以产生包含氢、甲烷、LPG和BTX的加氢裂化产品物流，(b)将加氢裂化产品物流分离为第一气体物流和第一液体物流，(c)将第一气体物流分离以获得含氢和甲烷的第二气体物流和含LPG和BTX的第二液体物流，其中实施所述分离使得第二液体物流基本不含氢和甲烷，(d)将第二液体物流分离为包含LPG的第三气体物流和包含BTX的第三液体物流，其中步骤(c)包括：将部分第三液体物流加入第一气体物流以吸收第一气体物流中的LPG，从而获得第二液体物流，或者将部分第三液体物流加入由第一气体物流分离的气体物流中以吸收由第一气体物流分离的气体物流中的LPG，从而获得第二液体物流。

The method of production increase of benzene from hydrocarbon feedstock

A method for production increase of benzene from hydrocarbon mixture is provided to combine the process of manufacturing aromatic hydrocarbon mixture and LPG from hydrocarbon mixture and the solvent extracting process for separating polar hydrocarbon from hydrocarbon mixture. The method for production increase of benzene from hydrocarbon mixture including the steps of: (a) separating hydrocarbon mixture into hydrocarbon flow of less than C6 and hydrocarbon flow of more than C7; (b) separating non-aromatic hydrocarbon flow and aromatic carbon flow from hydrocarbon of less than C6 through solvent extracting process; (c) collecting benzene from aromatic hydrocarbon flow; (d) flowing hydrocarbon of more than C7 and hydrogen into on reaction area; (e) converting hydrocarbon of more than C7 to aromatic hydrocarbon by dealkylation or transalkylation and then converting it to non-aromatic hydrocarbon by hydrocracking; (f) separating the reaction product of step(e) into upper flow and a bottom flow; and (g) collecting benzene, toluene, xylene and aromatic compound of more than C9 from the bottom flow.

Process for The Preparation of Aromatic Hydrocarbons and Liquefied Petroleum Gas from Hydrocarbon Mixture

본 발명은 탄화수소 혼합물로부터 방향족 탄화수소 및 액화석유가스를 제조하는 공정에 관한 것으로, 제올라이트와 무기질 바인더로 이루어진 혼합담체에 백금/비스무트를 담지시켜 된 촉매의 존재 하에서 탄화수소 원료 혼합물 중 비방향족 화합물은 수소첨가분해 반응을 통하여 액화석유가스(LPG)가 풍부한 기상물질로 전환되고, 방향족 화합물은 탈알킬화 및 트랜스알킬화 반응을 통하여 벤젠, 톨루엔, 자일렌 등이 풍부한 유분으로 전환된다. 상기 기상생성물은 증류과정을 통해서 비점 차이를 이용하여 LPG 및 메탄과 에탄의 혼합물로 분리되며, 액상생성물은 증류과정을 통해서 비점 차이에 의하여 벤젠, 톨루엔, 자일렌, C9+ 방향족 화합물 등으로 분리되어 각각 수득된다. 탄화수소, 액화석유가스, 제올라이트, 백금, 비스무트, 수소첨가 분해, 탈알킬화, 트랜스알킬화 The present invention relates to a process for producing an aromatic hydrocarbon and liquefied petroleum gas from a hydrocarbon mixture, wherein the non-aromatic compound in the hydrocarbon raw material mixture is hydrogenated in the presence of a catalyst having platinum / bismuth supported on a mixed carrier composed of zeolite and an inorganic binder. The decomposition reaction converts LPG into a gaseous substance rich in liquefied petroleum gas (LPG), and the aromatic compound is converted into an oil rich in benzene, toluene and xylene through dealkylation and transalkylation. The gaseous product is separated into a mixture of LPG and methane and ethane using a boiling point difference through a distillation process, and the liquid product is separated into a benzene, toluene, xylene, C9 + aromatic compound and the like by a boiling point difference through a distillation process, respectively. Obtained. Hydrocarbon, liquefied petroleum gas, zeolite, platinum, bismuth, hydrocracking, dealkylation, transalkylation

用于针对低聚轻质烯烃的工艺的分馏方法

本发明涉及用于低聚轻质烯烃的方法，其中将来自低聚区段的流出物传送至预分馏塔，所述预分馏塔产生至少一种含有液化石油气和轻质汽油的混合物的头馏分以及含有重质汽油和中间馏出物的混合物的底馏分，将所述头馏分传送至脱丁烷塔，所述脱丁烷塔产生至少一种液化石油气切取馏分和轻质汽油切取馏分，将所述底馏分和至少部分所述轻质石油切取馏分传送至分离器，所述分离器使得能够获得至少气态馏分、汽油馏分和瓦斯油馏分。

Method for converting a high-boiling hydrocarbon feedstock into lighter boiling hydrocarbon products

본 발명은, 고비점 탄화수소 공급원료를 보다 저비점의 탄화수소 생성물로 전환하는 공정에 관한 것으로, 상기 보다 저비점의 탄화수소 생성물은 석유 화학 공정을 위한 공급원료로서 적합하고, 상기 전환하는 공정은 다음의 단계를 포함한다: 중질의 탄화수소 공급원료를 수소화분해 유닛(들)의 캐스케이드로 공급하는 단계; 수소화분해 유닛에서 상기 공급원료를 분해하는 단계; 상기 분해된 공급원료를 저비점 탄화수소 분획을 포함하는 탑정 스트림 및 중질 탄화수소 분획을 포함하는 탑저 스트림으로 분리하는 단계; 상기 수소화분해 유닛의 상기 탑저 스트림을 상기 수소화분해 유닛(들) 내 이어지는 수소화분해 유닛을 위한 공급원료로서 공급하는 단계, - 각각의 수소화분해 유닛(들) 내에서 공정 조건은 서로 상이하고, 제 1 수소화분해 유닛부터 이어지는 수소화분해 유닛(들)까지의 수소화분해 조건은 가장 덜 가혹한 것에서부터 가장 가혹한 것까지 증가함 -, 및 각각의 수소화분해 유닛(들)로부터의 보다 저비점의 탄화수소 분획을 BTX 및 LPG 생성 유닛을 위한 공급원료로서 처리하는 단계. The present invention relates to a process for converting a high-boiling hydrocarbon feedstock into a lower-boiling hydrocarbon product, said lower-boiling hydrocarbon product being suitable as a feedstock for a petrochemical process, said converting process comprising the steps of: comprising: feeding a heavy hydrocarbon feedstock to a cascade of hydrocracking unit(s); cracking the feedstock in a hydrocracking unit; separating the cracked feedstock into an overhead stream comprising a low-boiling hydrocarbon fraction and a bottoms stream comprising a heavy hydrocarbon fraction; feeding said bottoms stream of said hydrocracking unit as a feedstock for a subsequent hydrocracking unit in said hydrocracking unit(s), wherein the process conditions in each hydrocracking unit(s) are different from each other, the first The hydrocracking conditions from the hydrocracking unit to the subsequent hydrocracking unit(s) increase from the least severe to the most severe - and lower boiling hydrocarbon fractions from the respective hydrocracking unit(s) to BTX and LPG processing as feedstock for the production unit.

저급 원료유로부터 경질 연료를 제조하는 방법

저급 원료유를 촉매식 변환용 반응기의 제1 반응 구역 및 제2 반응 구역에 차례로 공급하는 단계, 저급 원료유를 상기 촉매식 변환용 반응기의 상기 제1 반응 구역 및 상기 제2 반응 구역에서 촉매식 변환용 촉매와 접촉시켜 반응을 수행하는 단계를 포함하는 저급 원료유로부터 경질 연료를 얻는 방법. 폐촉매는 기체-고체 분리 공정에 의해 반응 생성물로부터 분리된다. 폐촉매는 스팀 스트리핑되고, 코크스 연소되어 재생된 다음, 재사용을 위해 반응기로 반송된다. 반응 생성물은 분리되어 프로필렌, 경질 연료, 촉매식 왁스 오일 및 기타 생성물이 얻어지고, 촉매식 왁스 오일은 수소화 처리기 및/또는 방향족 추출 장치로 이송되고, 반응 배출물은 분리되어 수소첨가 촉매식 왁스 오일 및/또는 추출 잔사유가 얻어지고, 수소첨가 촉매식 왁스 오일 및/또는 추출 잔사유는 촉매식 변환용 반응기의 제1 반응 구역 및/또는 다른 촉매식 변환 장치로 반송되어 목표 생성물인 경질 연료 및 부산물인 프로필렌이 얻어진다. 상기 방법에서, 저급 원료유는 온화한 촉매식 변환 반응을 거치고, 얻어지는 촉매식 왁스 오일은 방향족 추출 공정을 거치므로, 추출 오일은 2환형 방향족이 농후하여 유용한 화학적 물질이며; 추출 잔사유는 알칸 및 나프텐이 농후하여 촉매식 변환 반응용으로 적합하다. 상기 방법에 의해 석유 자원의 고효율적인 활용이 가능하다.

Method for separating normal-paraffin and iso-paraffin from hydrocarboneous oil

The present invention relates to a method for separating normal paraffin and isoparaffin from raffinate of a BTX reforming process comprising light naphtha of C5 to C8. The present invention can provide a method for separating normal paraffin and isoparaffin, which comprises a liquid hydrogenation step for removing olefin by introducing the raffinate in which hydrogen is dissolved into a reactor filled with a hydrogenation catalyst.

C2 및 c3 탄화수소 제조 방법

본 발명은 C2 및 C3 탄화수소를 제조하는 제조 방법에 관한 것으로서, a) 중간 증류물을 포함하는 혼합된 탄화수소 스트림에 대해 제1 수소첨가분해 촉매의 존재하에 제1 수소첨가분해를 수행하여, 제1 수소첨가분해 생성물 스트림을 생성하는 단계; b) 제2 수소첨가분해 공급물 스트림에 대해 제2 수소첨가분해 촉매의 존재하에 제2 수소첨가분해를 수행하여, 제2 수소첨가분해 생성물 스트림을 생성하는 단계로서, 상기 제2 수소첨가분해는 상기 제1 수소첨가분해보다 더 가혹한(severe), 단계; 및 c) C4 수소첨가분해 공급물 스트림에 대해, C4 수소첨가분해 촉매의 존재하에서, C4 탄화수소를 C3 탄화수소로 전환하는데 최적화된 C4 수소첨가분해를 수행하여, C4 수소첨가분해 생성물 스트림을 얻는 단계로서, 상기 C4 수소첨가분해는 상기 제2 수소첨가분해보다 더 가혹한, 단계;를 포함하며, 상기 제1 수소첨가분해 생성물 스트림, 상기 제2 수소첨가분해 생성물 스트림 및 상기 C4 수소첨가분해 생성물 스트림은 분리 시스템에 공급되며, 상기 분리 시스템은, 상기 제1 수소첨가분해 생성물 스트림으로부터 분리된 상기 제2 수소첨가분해 공급물 스트림; 상기 제2 수소첨가분해 생성물 스트림으로부터 분리된 상기 C4 수소첨가분해 공급물 스트림; 상기 제1 수소첨가분해로 재순환되는 제1 재순환 스트림; 상기 제2 수소첨가분해로 재순환되는 제2 재순환 스트림; 상기 C4 수소첨가분해로 재순환되는 제3 재순환 스트림; 상기 제1 수소첨가분해, 상기 제2 수소첨가분해 및/또는 상기 C4 수소첨가분해로 재순환되는 H 2 또는 H 2 및 C1의 수소 재순환 스트림; 및 C3- 탄화수소의 C2 및 C3 생성물 스트림;을 제공하며, 상기 제2 수소첨가분해 공급물 스트림은 2고리 구조를 갖는 C10-C12 탄화수소를 제외한 C12- 탄화수소 스트림이며, 상기 제1 재순환 스트림은 2고리 구조를 갖는 C10-C12 및 C13+ 탄화수소 스트림이며, 상기 C4 수소첨가분해 공급물 스트림은 C5-, C4- 또는 iC4- 탄화수소 스트림이며, 상기 제2 재순환 스트림은 C6+, C5+ 또는 nC4+ 탄화수소 스트림이며, 상기 제3 재순환 스트림은 nC4+ 또는 C4+ 탄화수소 스트림이다.

Method for conversion of low-grade raw feedstock to high-quality oil fuel

FIELD: oil and gas industry.SUBSTANCE: invention is related to process of hydrocarbon oil catalytic conversion. Invention is referred to conversion of law-grade raw feedstock which is input to the first reaction zone in catalytic conversion reactor and subjected to catalytic reactions of cracking by means of raw feedstock contacting with catalyst of catalytic conversion. Vapours and used catalyst are mixed at random basis with light raw feedstock and/or cooling medium and are introduced into the second reaction zone in catalytic conversion reactor for the purpose of further cracking, hydrogen transfer and isomerisation reactor. Products of the reaction are separated from used catalyst by separation into gaseous and solid phases and introduced into separation system in order to obtain dry gas, LPG, petrol and diesel fuel and catalytic gas oil with c suspended catalyst (FGO). Used catalyst is desorbed, regenerated and then hot regenerated catalyst is returned to the reactor. FGO is introduced into hydrofining plant and/or plant for aromatic hydrocarbons separation in order to receive hydrofined FGO and/or FGO raffinate. Hydrofined FGO and/or FGO raffinate is transferred to the first reaction zone of catalytic conversion reactor and/or to other FCC plants for further reactions in order to receive the target oil fuel as a high-quality product.EFFECT: conversion of low-grade feedstock to high-quality oil fuel and propylene and effective use of oil resources by significant reducing output of dry gas and coke.21 cl, 4 dwg, 10 tbl, 16 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2 497 933 (13) C2 (51) МПК C10G 69/04 C10G 11/08 (2006.01) (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (21)(22) Заявка: 2010133616/04, 13.03.2009 (24) Дата начала отсчета срока действия патента: 13.03.2009 (43) Дата публикации заявки: 20.02.2012 Бюл. № 5 (56) Список документов, цитированных в отчете о поиске: ЕР 1734098 А1, 20.12.2006. CN 1896192 А, 17. ...

Method and device for treatment of hydrocarbons flow

FIELD: power engineering. SUBSTANCE: method for treatment of a flow of hydrocarbons, such as natural gas, which includes at least the following stages: supply of a feed stream (10) of hydrocarbons, sending the feed stream (10) via the first separator (12) to produce the first gaseous flow (20) and the first liquid flow (30), sending the first gaseous flow (20) from the stage (b) via a high-pressure separator (14) to produce the second gaseous flow (40) and the second flow (80) of liquid, maintenance of pressure of the first gaseous flow (20) between the stages (b) and (c) within the range of ±1 MPa, sending the first flow (30) of liquid from the stage (b) via a rectifier (16) to produce the third gaseous flow (60) and a stabilised condensate (70), supply of the second flow (80) of liquid from the stage (c) into the rectifier (16), liquefaction of the second gaseous flow (40) in the system (26) of liquefaction with production of the liquefied hydrocarbon flow (50) and supply of the liquid recirculation flow (90) from the system (26) of liquefaction back into the high pressure separator (14). EFFECT: using the invention will make it possible to increase efficiency of natural gas separation, to reduce capital costs, to improve quality of compressed gas. 10 cl, 1 dwg, 3 tbl РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2 439 453 (13) C2 (51) МПК F25J 3/02 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (21)(22) Заявка: 2008152127/06, 04.06.2007 (24) Дата начала отсчета срока действия патента: 04.06.2007 (72) Автор(ы): КЛЕЙН НАГЕЛВОРТ Роберт (NL), МЕИРИНГ Ваутер Ян (MY) (43) Дата публикации заявки: 20.07.2010 Бюл. № 20 2 4 3 9 4 5 3 (45) Опубликовано: 10.01.2012 Бюл. № 1 (56) Список документов, цитированных в отчете о поиске: WO 2006049515 А1, 11.05.2006. RU 2096701 С1, 20.11.1997. US 2004238412 А1, 02.12.2004. US 5502266 А, 26.03.1996. RU 2133931 C1, 27.07.1999. 2 4 3 9 4 5 3 R U (86) Заявка PCT: EP 2007/055436 (04.06.2007) C 2 C 2 ...

Method of producing liquefied petroleum gas

提供了从天然气等含碳原料经由合成气、甲醇和/或二甲醚制造主要成分为丙烷或丁烷的烃，即可经济制造液化石油气(LPG)的方法。由含碳原料制造合成气，再由合成气制造含一氧化碳和/或二氧化碳的粗甲醇或粗二甲醚，从得到的粗甲醇或粗二甲醚制造所含烃的主要成分为丙烷或丁烷的液化石油气。

Process for Purification of Raffinate-2 streams

본 발명은 라피네이트-2 스트림으로부터 1-부텐을 고순도 고수율로 분리 정제하는 방법에 관한 것으로서, 분리벽을 설치한 고효율 증류 컬럼을 이용하여 에너지 절감율을 극대화 하면서 1-부텐을 고순도 고수율로 회수할 수 있는 방법을 제공한다. The present invention relates to a method for separating and purifying 1-butene from a raffinate-2 stream in high purity and high yield, and recovers 1-butene with high purity and high yield while maximizing energy saving by using a high-efficiency distillation column equipped with a dividing wall. provide a way to do it.

Method for indudstrialized refining liquefied petrolium gas (LPG)

本发明涉及一种工业化精制液化石油气的新方法。在完全无碱条件下，经过醇胺处理后的液化石油气通过设置在固定床反应器中的脱硫剂和催化剂依次进行精脱硫和转化硫醇，精脱硫时液化石油气中的硫化氢与铁钙氧化物或水合铁钙氧化物反应的生成物附着在脱硫剂上，转化硫醇时液化石油气中的硫醇与液化石油气中残留的微量空气在催化剂的催化作用下反应生成二硫化物，所生成的二硫化物随液化石油气流出固定床反应器；转化硫醇后的液化石油气通过精馏处理得到液化石油气精制品；进一步精馏则可得到高价值的二硫化物产品。本发明的精制方法，效率高、无碱液排放，大大简化了以前对液化石油气精制所采用的有碱处理方法，而且无环境污染。

Method of treating biomass, fuel for fuel cell, gasoline, diesel fuel, liquefied petroleum gas, and synthetic resin

在使用具有反应带、分离带、汽提带和再生带的流化催化裂化装置，通过催化裂化处理生物质时，在反应带中，用含有10～50质量％超稳定Y型沸石的催化剂，在反应带出口温度为580～680℃、催化剂/油比率为10～40wt/wt、反应压力为1～3kg/cm 2 G和反应带中的原料油与催化剂的接触时间为0.1～1.0秒的条件下处理含有生物质的原料油，然后，在再生带中，在再生带温度为640～720℃、再生带压力为1～3kg/cm 2 G和再生带出口处的废气中的氧气浓度为0～3mol％的条件下处理催化剂。

Production of diesel fuel from biorenewable feedstocks with selective separation of converted oxygen

A process has been developed for producing diesel boiling range fuel from renewable feedstocks such as plant and animal fats and oils, the process providing for sulfur management. The process involves catalytically treating a renewable feedstock by hydrogenating and deoxygenating to provide a hydrocarbon fraction useful as a diesel boiling range fuel. The hydrocarbon fraction is isomerized to improve cold flow properties. A selective separation such as a hot high pressure hydrogen stripper is used to remove at least the carbon oxides from the first zone effluent before entering the isomerization zone, and to provide liquid recycle to the treating zone at pressure and temperature. A vapor stream is separated from the isomerization effluent and at least carbon dioxide is removed using at least one selective or flexible amine solution absorber. The resulting hydrogen-rich stream is recycled to the deoxygenation reaction zone.

Production of diesel fuel from biorenewable feedstocks with heat integration

A process has been developed for producing diesel boiling range fuel or fuel blending component from renewable feedstocks such as plant oils and greases. The process involves treating a renewable feedstock by hydrogenating and deoxygenating i.e. decarboxylating and/or hydrodeoxygenating to provide a hydrocarbon fraction useful as a diesel fuel. The hydrocarbon fraction is isomerized to improve cold flow properties. At least one interstage stream of the hydrogenating and deoxygenating reaction zone is heat exchanged with the feed to the isomerization reaction zone, and/or the effluent of the hydrogenating and deoxygenating reaction zone is heat exchanged with the feed to the isomerization reaction zone.

Production of diesel fuel from renewable feedstocks with reduced hydrogen consumption

A process has been developed for producing diesel boiling range fuel from renewable feedstocks such as plant and animal fats and oils. The process involves treating a renewable feedstock by hydrogenating and deoxygenating to provide a hydrocarbon fraction useful as a diesel boiling range fuel. Water is added to the deoxygenation reaction to drive carbon monoxide and water to react to form hydrogen and carbon dioxide. The hydrogen is then consumed by the reactions. If desired, the hydrocarbon fraction can be isomerized to improve cold flow properties.

Production of diesel fuel from biorenewable feedstocks

A process has been developed for producing diesel boiling range fuel from renewable feedstocks such as plant oils and animal oils, fats, and greases. The process involves treating a renewable feedstock by hydrogenating and deoxygenating i.e. decarboxylating, decarbonylating, and/or hydrodeoxygenating to provide a hydrocarbon fraction useful as a diesel boiling range fuel or diesel boiling range fuel blending component. If desired, the hydrocarbon fraction can be isomerized to improve cold flow properties. A portion of the hydrogenated and deoxygenated feedstock is selectively separated and then recycled to the treatment zone to increase the hydrogen solubility of the reaction mixture.

Integrated process for oil extraction and production of diesel fuel from biorenewable feedstocks

An integrated process has been developed for producing diesel boiling range fuel from renewable feedstocks such as animal and plant oils and using a byproduct naphtha as an extraction solvent in the generation of the renewable feedstock. The process involves treating a renewable feedstock by hydrogenating and deoxygenating to provide a hydrocarbon fraction useful as a diesel fuel or diesel boiling range fuel blending component. A byproduct naphtha stream is used as an extraction solvent in a process for the generation of the renewable feedstock. If desired, the hydrocarbon fraction can be isomerized to improve cold flow properties.

Production of diesel fuel from biorenewable feedstocks with lower hydrogen consumption

A process has been developed for producing diesel boiling range fuel from renewable feedstocks such as plant and animal fats and oils. The process involves treating a renewable feedstock by hydrogenating and deoxygenating i.e. decarboxylating, decarbonylating, and hydrodeoxygenating to provide a hydrocarbon fraction useful as a diesel boiling range fuel. A sulfur containing component is added to drive the conversion preferentially through carbonylation and carbonylation with reduced hydrodeoxygenation. If desired, the hydrocarbon fraction can be isomerized to improve cold flow properties.

Production of transportation fuel from renewable feedstocks

A process has been developed for producing a diesel boiling point range product and an aviation boiling point range product from renewable feedstocks such as plant and animal oils. The process involves treating a renewable feedstock by hydrogenating and deoxygenating to provide a hydrocarbon fraction which is then isomerized and selectively cracked to form the diesel boiling point range product and the aviation boiling point range product. A portion of the diesel boiling point range product, aviation boiling point range product, naphtha product, LPG, or any combination thereof can be optionally used as a rectification agent in the selective hot high pressure hydrogen stripper to decrease the amount of product carried in the stripper overhead.