Patent RU2015110987A3

ВУ’? 2015110987” АЗ Дата публикации: 28.09.2018 Форма № 18 ИЗ,ПМ-2011 Федеральная служба по интеллектуальной собственности Федеральное государственное бюджетное учреждение ж Я «Федеральный институт промышленной собственности» (ФИПС) ОТЧЕТ О ПОИСКЕ 1. . ИДЕНТИФИКАЦИЯ ЗАЯВКИ Регистрационный номер Дата подачи 2015110987/04(017182) 26.03.2015 Приоритет установлен по дате: [ ] подачи заявки [ ] поступления дополнительных материалов от к ранее поданной заявке № [ ] приоритета по первоначальной заявке № из которой данная заявка выделена [ ] подачи первоначальной заявки № из которой данная заявка выделена [ ] подачи ранее поданной заявки № [Х] подачи первой(ых) заявки(ок) в государстве-участнике Парижской конвенции (31) Номер первой(ых) заявки(ок) (32) Дата подачи первой(ых) заявки(ок) (33) Код страны 1. 1453076 07.04.2014 ЕК Название изобретения (полезной модели): [Х] - как заявлено; [ ] - уточненное (см. Примечания) СПОСОБ ПОЛУЧЕНИЯ ЛЕГКИХ ОЛЕФИНОВ И ВТХ, В КОТОРОМ ПРИМЕНЯЕТСЯ УСТАНОВКА КАТАЛИТИЧЕСКОГО КРЕКИНГА МСС, ОБРАБАТЫВАЮЩАЯ СЫРЬЕ ТИПА НАФТЫ, УСТАНОВКА КАТАЛИТИЧЕСКОГО РИФОРМИНГА И АРОМАТИЧЕСКИЙ КОМПЛЕКС Заявитель: ИФП ЭНЕРЖИ НУВЕЛЛЬ, ЕК 2. ЕДИНСТВО ИЗОБРЕТЕНИЯ [Х] соблюдено [ ] не соблюдено. Пояснения: см. Примечания 3. ФОРМУЛА ИЗОБРЕТЕНИЯ: [Х] приняты во внимание все пункты (см. Примечания) [ ] приняты во внимание следующие пункты: [ ] принята во внимание измененная формула изобретения (см. Примечания) 4. КЛАССИФИКАЦИЯ ОБЪЕКТА ИЗОБРЕТЕНИЯ (ПОЛЕЗНОЙ МОДЕЛИ) (Указываются индексы МПК и индикатор текущей версии) С10С 11/00 (2006.01) 5. ОБЛАСТЬ ПОИСКА 5.1 Проверенный минимум документации РСТ (указывается индексами МПК) С10С 11/00, С1О0С 35/00, С07С 15/04, С10С 63/04, С07С 11/04, С07С 15/06, С1ОС 63/08, С07С 11/06, С07С 15/08 5.2 Другая проверенная документация в той мере, в какой она включена в поисковые подборки: 5.3 Электронные базы данных, использованные при поиске (название базы, и если, возможно, поисковые термины): ЕАРАТГУ, Езрасепе, ]-Р1а Рае, Разеагсв, КОРТО, ...

СПОСОБ ПОЛУЧЕНИЯ ПРОПИЛЕНА И АРОМАТИЧЕСКИХ УГЛЕВОДОРОДОВ И УСТАНОВКА ДЛЯ ИХ ПОЛУЧЕНИЯ

1. Способ получения пропилена и ароматических углеводородов, включающий: ! (1) стадию получения пропилена, в которой углеводородное сырье, содержащее 50% по массе или более по меньшей мере одного из С4-12-олефинов контактирует в реакторе для получения пропилена с формованным катализатором А, содержащим первый цеолит, в указанных ниже условиях (i)-(iv) для осуществления реакции каталитической конверсии по меньшей мере одного из С4-12-олефинов, с получением реакционной смеси, содержащей пропилен, реакционная смесь разделяют на фракцию С, содержащую преимущественно водород и C1-3-углеводороды, и фракцию D, содержащую преимущественно по меньшей мере один из С4+-углеводородов, и пропилен выделяют из фракции С: ! (i) с цеолитом, имеющим средний диаметр пор с диаметром пор от 5 до 6,5 Е; ! (ii) по существу не содержащим протонов; ! (iii) содержащим по меньшей мере один металл, выбранный из группы, состоящей из металлов Группы IB Периодической таблицы; и ! (iv) имеющим молярное соотношение SiO2/Al2O3 по меньшей мере 800, но не более 2000; и ! (2) стадию получения ароматических углеводородов, в которой сырьевой материал, содержащий полностью или частично фракцию D или ее часть, контактирует в реакторе для получения ароматических углеводородов с формованным катализатором В, содержащим второй цеолит, в указанных ниже условиях (v)-(vii), в газовой фазе при температуре 650°С или менее: ! (v) с цеолитом, имеющим средний диаметр пор с диаметром пор от 5 до 6,5 Е; ! (vi) с первоначальным диаметром частиц в диапазоне от 0,02 до 0,25 мкм; и ! (iii) содержащим по меньшей мере один металлический элемент, выбранный из группы, состоящей из металлических элементов в группе IB периодической таблиц РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2008 133 617 (13) A (51) МПК C07C 2/42 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ, ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21), (22) Заявка: 2008133617/04, 12.01.2007 (71) Заявитель(и): АСАХИ КАСЕИ КЕМИКАЛЗ КОРПОРЕЙШН (JP) (30) ...

СПОСОБ И УСТАНОВКА ДЛЯ ПЕРЕРАБОТКИ БЕНЗИНОВЫХ ФРАКЦИЙ

Изобретение касается способа переработки бензиновой фракции, включающего стадии: I) взаимодействия бензиновой фракции в узле ароматизации и разделения полученного продукта реакции с получением C4--компонента, C5-компонента, C6-C7-компонента, C8-компонента и C9+-компонента; II) взаимодействия C6-C7-компонента и C9+-компонента со стадии I) в узле крекинга и преобразования ароматических соединений и разделения полученного продукта реакции с получением C4--компонента, C5-компонента, C6-C7-компонента, C8-компонента и C9+-компонента, при этом реакция, протекающая в узле крекинга и преобразования ароматических соединений, включает реакцию крекинга неароматических соединений и реакцию трансалкилирования; III) очистки по меньшей мере одного из C8-компонентов со стадий I) и II) и разделения продукта с получением C4--компонента, C5-компонента, C6-C7-компонента, ароматического(их) C8-углеводорода(ов) и C9+-компонента; IV) проведения парового крекинга или реакции дегидрирования по меньшей мере на части ...

Hydrocarbon conversion process

A number of refinery pool gasolines are obtained from a hydrocarbon feed stock by a process involving separating from the feed stock a fraction which is reformed to obtain a gasoline product, separating from the feed stock and/or the reformed product at least one aliphatic hydrocarbon in the C5-C7 range and subjecting this to pyrolysis at 1300-1750 DEG F. to obtain ethylene which is recovered as a product and C3 and/or C4 olefines which are subjected to a combining reaction to obtain a further gasoline product. In a preferred embodiment a crude petroleum oil is distilled at 10 to obtain (1) C1-C3 gaseous hydrocarbons (2) a light gasoline fraction boiling in the range C4 to 160-200 DEG F. or to 210 DEG F. (3) a heavy gasoline reforming feed fraction boiling above (2) to an end point of 300-410 DEG F. (4) a virgin gas oil and (5) a residue. The residue is subjected to thermal viscosity breaking at 11 and fractionated to at 12 obtain C3 and lighter hydrocarbons, a light gasoline fraction which ...

Production of aromatics from noncatalytically cracked fatty acid based oils

A method for producing aromatic compounds from fatty acid oils including heating a fatty acid oil to a temperature between about 100° C to about 800° C at a pressure between about vacuum conditions and about 200 psia for a time sufficient to crack the oil and produce a cracked fatty acid oil; removing undesired materials, unreacted oil, heavy ends, and light ends from the cracked fatty acid oil; heating the resulting purified cracked fatty acid oil to a temperature between about 100° C to about 800° C at a pressure between about vacuum conditions and about 200 psia for a time sufficient to reform alkenes and alkanes in the cracked fatty acid oil into aromatic compounds and produce a reformed fatty acid oil; and extracting components from the reformed fatty acid oil to produce a mixture of chemical products containing between 5% and 90% aromatic compounds by weight.

PROCESS FOR UP-GRADING STEAM-CRACKING PRODUCTS

CATALYST SYSTEM AND PROCESS FOR CONVERSION OF A HYDROCARBON FEED UTILIZING THE CATALYST SYSTEM

The present invention relates to a catalyst system comprising: i. a first layer of a hydrocarbon conversion catalyst, the hydrocarbon conversion catalyst comprising: a first composition comprising a platinum group metal on a solid support; and a second composition comprising a transition metal on an inorganic support; ii. a second layer comprising a cracking catalyst; and to a process for conversion of a hydrocarbon feed utilizing this catalyst system.

CONVERSION OF HYDROCARBONS

METHOD OF PRODUCING LOWER OLEFIN AND MONOCYCLIC AROMATIC HYDROCARBON HAVING 6 TO 8 CARBON ATOMS AND DEVICE FOR PRODUCING LOWER OLEFIN AND MONOCYCLIC AROMATIC HYDROCARBON HAVING 6 TO 8 CARBON ATOMS

A method of producing a lower olefin and BTX from stock oils selected from at least two kinds of oils is provided. The method includes a first catalytic cracking step of bringing one stock oil A into contact with a catalytic cracking catalyst; a second catalytic cracking step of bringing one stock oil B, having an aromatic component content smaller than that of the stock oil A, into contact with the catalytic cracking catalyst; and a separation and collection step of collecting the lower olefins and BTX from a product generated in the first and second catalytic cracking steps. A contact time A during which the stock oil A is in contact with the catalytic cracking catalyst in the first catalytic cracking step is longer than a contact time B during which the stock oil B is in contact with the catalytic cracking catalyst in the second catalytic cracking step. 1. A method of producing a lower olefin and a monocyclic aromatic hydrocarbon having 6 to 8 carbon atoms from stock oils selected from at least two or more kinds of oils , the method comprising:a first catalytic cracking step of bringing one stock oil A among the stock oils into contact with a catalytic cracking catalyst;a second catalytic cracking step of bringing one stock oil B, having an aromatic component content smaller than that of the stock oil A, among the stock oils into contact with the catalytic cracking catalyst; anda separation and collection step of collecting the lower olefins and the monocyclic aromatic hydrocarbons having 6 to 8 carbon atoms from a product generated in the first and second catalytic cracking steps,wherein a contact time A during which the stock oil A is in contact with the catalytic cracking catalyst in the first catalytic cracking step is longer than a contact time B during which the stock oil B is in contact with the catalytic cracking catalyst in the second catalytic cracking step.2. The method of producing a lower olefin and a monocyclic aromatic hydrocarbon having 6 to 8 ...

Process for selectively producing high octane naphtha

This invention is related to a catalytically cracked or thermally cracked naphtha stream. The naphtha stream is contacted with a catalyst containing from about 10 to 50 wt. % of a crystalline zeolite having an average pore diameter less than about 0.7 nanometers at reaction conditions which include temperatures from about 500° C. to about 650° C. and a hydrocarbon partial pressure from about 10 to 40 psia. The resulting product is a high octane naphtha.

METHOD FOR PRODUCING A MIXTURE OF HYDROCARBONS

A blend for producing a mixture of hydrocarbons by thermal cracking, the blend comprising a renewable paraffin composition and fossil naphtha. 1. A blend for producing a mixture of hydrocarbons by thermal cracking , the blend comprising:a renewable paraffin composition and fossil naphtha,wherein the renewable paraffin composition contains more than 70 wt-% isoparaffins, the isoparaffins contain more than 20 wt-% multiple branched isoparaffins.2. The blend according to claim 1 , wherein a ratio of a wt-% amount multiple branched isoparaffins of the renewable paraffin composition to combined wt-% amounts of n-paraffins and monobranched isoparaffins of the renewable paraffin composition is at least 0.30.3. The blend according to claim 1 , wherein the blend comprises:at least 1 wt-% and at most 99 wt-% fossil naphtha.4. The blend according to claim 1 , wherein the ratio of the wt-% amount isoparaffins of the renewable paraffin composition to the wt-% amount of n-paraffins of the renewable paraffin composition is at least 4.0.5. The blend according to claim 1 , wherein the ratio of the wt-% amount isoparaffins of the renewable paraffin composition to the wt-% amount of n-paraffins of the renewable paraffin composition is at least 2.5.6. The blend according to claim 3 , wherein the isoparaffin content of the renewable paraffin composition is in a range from 73 wt-% to 95 wt-%.7. The blend according to claim 3 , wherein the total amount of isoparaffins in the renewable paraffin composition being more than 70 wt-% and the total amount of paraffins in the renewable paraffin composition being at least 90 wt-%.8. The blend according to claim 1 , wherein the renewable paraffin composition contains at least 75 wt-% isoparaffins.9. The blend according to claim 1 , wherein the renewable paraffin composition contains at least 80 wt-% isoparaffins.10. The blend according to claim 1 , wherein the renewable paraffin composition contains at least 25 wt-% multiple branched isoparaffins. ...

СПОСОБ ПОЛУЧЕНИЯ ЛЕГКИХ ОЛЕФИНОВ И ВТХ С ПРИМЕНЕНИЕМ УСТАНОВКИ КАТАЛИТИЧЕСКОГО КРЕКИНГА, ОБРАБАТЫВАЮЩЕЙ ТЯЖЕЛОЕ СЫРЬЕ ТИПА VGO ГЛУБОКОЙ ГИДРООЧИСТКИ, В КОМБИНАЦИИ С УСТАНОВКОЙ КАТАЛИТИЧЕСКОГО РИФОРМИНГА И АРОМАТИЧЕСКИМ КОМПЛЕКСОМ, ОБРАБАТЫВАЮЩИМ СЫРЬЕ ТИПА НАФТЫ

FIELD: chemistry.SUBSTANCE: invention relates to a method for producing light olefins and BTX from a first feedstock of the hydrotreated VGO or unconverted crude oil (UCO) type, exiting from hydrocracking, or any mixture of these two types of feedstock, and second naphtha-type feedstock with an initial boiling point above 30 °C and final boiling point below 220 °C, wherein said method includes a catalytic cracking unit (FCC), processing a hydrotreated fraction of VGO or non-converted oil, a catalytic reforming unit (REF), processing said naphtha fraction (30 °C–220 °C) and an aromatic complex (CA), into which the stream from catalytic reforming (REF) and the fraction denoted as LCN (PI-160 °C) flows from the FCC. Said method includes the sequence of the following operations: feeding a hydrotreated fraction of VGO or unconverted UCO oil (2) or any mixture of both to the FCC unit, which produces streams (6), fed to the fractionation unit (FRAC), from which the light fraction (8) is collected, LCN fraction (PI-160 °C), HCN fraction (160 °C–220 °C) and heavy fraction (220 °C+), feeding the light fraction (8) into a separation unit, called a cold box (SBF), allowing the separation of light olefins, ethylene and propylene, dry gases (Hand CH) and light paraffins C2, C3 and C4, feeding the gasoline fraction (PI-160 °C), denoted by LCN (9), to the aromatic complex (CA) mixed with streams (5) leaving catalytic reforming (RF) to form raw material (10) for the aromatic complex (CA), HCN fraction (160°C–220 °C) used as is, the heavy fraction (220 °C+) with an initial boiling point above 220 °C is returned to the FCC unit, feeding hydrotreated naphtha (4) as raw materials to the catalytic reforming unit (REF), collecting from the aromatic complex (CA) BTX, raffinate (12), defined as the non-aromatic part of the effluent, which is fed, at least in part, in a mixture with raw materials (2) of FCC and a fraction, called heavy aromatics (11), which is also fed in a mixture with raw ...

СПОСОБ КОНВЕРСИИ ТЯЖЕЛОГО СЫРЬЯ В БЕНЗИН И ПРОПИЛЕН С РЕГУЛИРУЕМЫМ ВЫХОДОМ

FIELD: chemistry. SUBSTANCE: invention relates to a method for combined production of petrol and propylene from heavy hydrocarbon material with initial boiling point of 340°C on a catalytic cracking apparatus (FCC), downstream of which there is an oligomerisation apparatus, capable of operating in two modes designated as "maximum propylene" and "maximum petrol", wherein for the "maximum propylene" mode, material fed into the oligomerisation apparatus consists of a C4 or C4/C5 olefin fraction, for the "maximum petrol" mode, material fed into the oligomerisation apparatus consists of a C3/C4 olefin fraction; catalytic cracking is carried out in a single reactor or in two different reactors, each reactor capable of operating in an ascending stream. The invention also relates to a method where catalytic cracking is carried out in a single reactor or in two different reactors, each reactor capable of operating in a descending stream. EFFECT: improved flexibility of the method with respect to production of propylene and petrol. 6 cl, 2 dwg, 3 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2 501 778 (13) C2 (51) МПК C07C C07C C07C C10G 2/04 (2006.01) 4/06 (2006.01) 11/06 (2006.01) 63/04 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (21)(22) Заявка: 2011111688/04, 29.07.2009 (24) Дата начала отсчета срока действия патента: 29.07.2009 (73) Патентообладатель(и): ИФП ЭНЕРЖИ НУВЕЛЛЬ (FR) (43) Дата публикации заявки: 10.10.2012 Бюл. № 28 2 5 0 1 7 7 8 (45) Опубликовано: 20.12.2013 Бюл. № 35 (56) Список документов, цитированных в отчете о поиске: RU 2294916 C2, 10.03.2003. RU 2299191 C2, 20.05.2007. US 4822477 A, 18.04.1989. WO 9302025 A, 22.07.1991. EP 0426400 A1, 26.10.1990. 2 5 0 1 7 7 8 R U (86) Заявка PCT: FR 2009/000945 (29.07.2009) C 2 C 2 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 29.03.2011 (87) Публикация заявки РСТ: WO 2010/023369 (04.03.2010) Адрес для переписки: 129090, ...

УСОВЕРШЕНСТВОВАННЫЙ СПОСОБ ПОЛУЧЕНИЯ ОЛЕФИНОВ И БТК С ИСПОЛЬЗОВАНИЕМ РЕАКТОРА КРЕКИНГА АЛИФАТИЧЕСКИХ СОЕДИНЕНИЙ

FIELD: manufacturing technology.SUBSTANCE: invention relates to a method of producing aromatic compounds, involving: reforming a stream of naphtha in a reforming zone under reforming conditions to form a reformer effluent containing aromatic compounds and non-aromatic compounds, wherein at least part of aromatic compounds contains alkyl groups; heating the effluent reformer stream and directing the reformer effluent directly to the acid cracking reaction zone; selective cracking of non-aromatic compounds and selective dealkylation of at least a portion of alkyl groups in aromatic compounds in the presence of an acid cracking catalyst in an acidic cracking reaction zone in acid cracking conditions to form a cracked reformer effluent stream containing aromatic compounds and cracked olefins cracked, wherein said acid cracking catalyst has an MFI type structure and does not contain a hydrogenating metal. Invention also relates to the device.EFFECT: use of disclosed invention eliminates distillation columns.10 cl, 3 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 698 722 C1 (51) МПК C10G 63/04 (2006.01) C10G 57/00 (2006.01) C07C 15/00 (2006.01) C07C 15/067 (2006.01) C07C 11/02 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК C10G 63/04 (2019.02); C10G 57/00 (2019.02) (21)(22) Заявка: 2018127189, 21.11.2016 (24) Дата начала отсчета срока действия патента: Дата регистрации: (73) Патентообладатель(и): ЮОП ЛЛК (US) 29.08.2019 (56) Список документов, цитированных в отчете о поиске: WO 2015/128317 A1, 03.09.2015. US 2015/0284646 A1, 08.10.2015. US 2015/0284646 A1, 08.10.2015. RU 2013146967 A, 27.04.2015. 30.12.2015 US 62/273,073 (45) Опубликовано: 29.08.2019 Бюл. № 25 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 30.07.2018 (86) Заявка PCT: 2 6 9 8 7 2 2 R U (87) Публикация заявки PCT: WO 2017/116584 (06.07.2017) C 1 C 1 US 2016/063126 (21.11.2016) 2 6 9 8 7 2 2 Приоритет(ы): (30) Конвенционный приоритет: ...

СПОСОБ ПОЛУЧЕНИЯ ЛЕГКИХ ОЛЕФИНОВ И ВТХ С ПРИМЕНЕНИЕМ УСТАНОВКИ КАТАЛИТИЧЕСКОГО КРЕКИНГА, ОБРАБАТЫВАЮЩЕЙ ТЯЖЕЛОЕ СЫРЬЕ ТИПА VGO ГЛУБОКОЙ ГИДРООЧИСТКИ, В КОМБИНАЦИИ С УСТАНОВКОЙ КАТАЛИТИЧЕСКОГО РИФОРМИНГА И АРОМАТИЧЕСКИМ КОМПЛЕКСОМ, ОБРАБАТЫВАЮЩИМ СЫРЬЕ ТИПА НАФТЫ

... 1. Способ получения легких олефинов и BTX из первого сырья типа гидроочищенного VGO или неконвертированной нефти (UCO), выходящей с гидрокрекинга, или любой смеси эти двух видов сырья, и второго сырья типа нафты с начальной точкой кипения выше 30˚C и конечной точкой кипения ниже 220˚C, причем указанный способ включает установку каталитического крекинга (FCC), обрабатывающую гидроочищенную фракцию VGO или неконвертированную нефть, установку каталитического риформинга (REF), обрабатывающую указанную фракцию нафты (30˚C-220˚C), и ароматический комплекс (CA), в который подаются поток с каталитического риформинга (REF) и фракция, обозначаемая как LCN (PI-160˚C) потоков из FCC, причем указанный способ включает последовательность следующих операций:проведение гидроочищенной фракции VGO или неконвертированной нефти UCO (2) или любой смеси обеих на установку FCC, которая производит потоки (6), направляемые на установку фракционирования (FRAC), из которой отбирают легкую фракцию (8), фракцию LCN ...

CONVERSION OF HYDROCARBONS

METHOD OF PRODUCING BENZENE, TOLUENE, XYLENE (BEFRACHTUNGS) FROM MIXTURE OF HYDROCARBONS WITH - WITH

PROCESS FOR PRODUCING LIGHT OLEFINS AND BTX DEVICE USING THE FCC BY TREATING A LIKE HEAVY CATALYTICALLY CONVERT VGO VERY HYDROTRAITE, COUPLED WITH A CATALYTIC REFORMING UNIT AND A COMPLEX AROMATIC BY TREATING A NAPHTHA-RANGE.

HIGH OCTANE GASOLINE PRODUCTION

OLEFIN AND SINGLE-RING AROMATIC HYDROCARBON PRODUCTION METHOD, AND ETHYLENE PRODUCTION DEVICE

Integrated hydrothermal process for heavy oil upgrading

INTEGRATED PROCESS FOR MAXIMIZING RECOVERY OF HYDROGEN

An integrated process for maximizing recovery of hydrogen is provided. The process comprises: providing a hydrocarbonaceous feed comprising naphtha, and a hydrogen stream to a reforming zone, wherein the hydrogen stream is obtained from at least one of a hydrocracking zone, a transalkylation zone, and an isomerization zone. The hydrocarbonaceous feed is reformed in the reforming zone in the presence of the hydrogen stream and a reforming catalyst to provide a reformate effluent stream. At least a portion of the reformate effluent stream is passed to a debutanizer column of the reforming zone to provide a net hydrogen stream and a fraction comprising liquid petroleum gas (LPG). At least a portion of the net hydrogen stream is recycled to the reforming zone as the hydrogen stream.

OLEFIN AND BTX PRODUCTION USING ALIPHATIC CRACKING REACTOR

A process and apparatus for making aromatics are described. The process includes reforming a naphtha stream in a reforming zone to form a reformer effluent comprising aromatic compounds and non-aromatic compounds, wherein at least a portion of the aromatic compounds contain alkyl groups. The reformer effluent is heated and passed directly to an acid cracking reaction zone. The non-aromatic compounds are selectively cracked and at least a portion of the alkyl groups on the aromatic compounds are selectively dealkylated in the presence of an acid cracking catalyst to form a cracked reformer effluent comprising the aromatic compounds and cracked olefins. 1. A process for making aromatics comprising:reforming a naphtha stream in a reforming zone under reforming conditions to form a reformer effluent comprising aromatic compounds and non-aromatic compounds, wherein at least a portion of the aromatic compounds contain alkyl groups;heating the reformer effluent and passing the reformer effluent directly to an acid cracking reaction zone;selectively cracking the non-aromatic compounds and selectively dealkylating at least a portion of the alkyl groups on the aromatic compounds in the presence of an acid cracking catalyst in the acid cracking reaction zone under acid cracking conditions to form a cracked reformer effluent comprising the aromatic compounds and cracked olefins.2. The process of wherein the cracked olefins comprise at least one of ethylene claim 1 , propylene claim 1 , and butylene claim 1 , and further comprising:recovering the cracked olefins, wherein the recovered cracked olefins are greater than about 95 wt % pure.3. The process of wherein the acid cracking catalyst comprises ZSM-5.4. The process of wherein the acid cracking catalyst comprises a silicalite catalyst having a zeolite silica to alumina molar ratio of greater than about 250.5. The process of further comprising:separating the cracked reformer effluent into an aromatic lean fraction comprising ...

Mixture containing 1, 3-Butadiene and process for producing the same

To provide a C4 fraction that contains significantly reduced amounts of butynes and methylallene and to provide a process for low-cost and effective production of ethers in which the C4 fraction is used as the starting material for a telomerization process. A mixture containing 25 to 80 mass% 1,3-butadiene, 13 to 68 mass% butenes and 2 to 15 mass% butanes with butynes and methylallene being contained in amounts of 50 ppm or less and 5 to 800 ppm, respectively ...

СПОСОБ ПОЛУЧЕНИЯ ЛЕГКИХ ОЛЕФИНОВ И BTX, В КОТОРОМ ПРИМЕНЯЕТСЯ УСТАНОВКА КАТАЛИТИЧЕСКОГО КРЕКИНГА NCC, ОБРАБАТЫВАЮЩАЯ СЫРЬЕ ТИПА НАФТЫ, УСТАНОВКА КАТАЛИТИЧЕСКОГО РИФОРМИНГА И АРОМАТИЧЕСКИЙ КОМПЛЕКС

... 1. Способ получения легких олефинов и BTX из фракции нафты с начальной точкой кипения выше 30°C и конечной точкой кипения ниже 220°C, причем с применением установки каталитического крекинга (NCC) для обработки сырья типа легкой нафты (30-T°C), установки каталитического риформинга (REF) для обработки сырья, называемого тяжелой нафтой (T°C-220°C), и ароматического комплекса (CA), на который подаются потоки с каталитического риформинга (REF) и фракции 60+ потоков из NCC, причем указанный способ включает последовательность следующих операций:- подачу сырьевой нафты (1) с начальной точкой кипения больше или равной 30°C и конечной точкой кипения больше или равной 220°C в установку гидроочистки (HDT), для удаления присутствующих в сырье соединений серы и азота,- подачу гидроочищенной сырьевой нафты (2) на установку разделения (SPLIT 1), которая позволяет отделить легкую фракцию, называемую легкой нафтой, с интервалом кипения 40-T°C, и тяжелую фракцию, называемую тяжелой нафтой, с интервалом кипения ...

CONVERSION OF HYDROCARBONS

PROCEEDED OF CATALYTIC CRACKING IMPROVES

processo de conversão de uma carga pesada em gasolina e em propileno, que apresenta uma estrutura de rendimento modulável

PROCEDURE FOR THE PRODUCTION OF LIGHT OLEFINS AND BTX USING A CATALYTIC CRACKING UNIT, , THAT TREATS AN LOADER NAPHTHA, A CATALYTIC REFORMING UNIT AND A COMPLEX AROMATIC

Un procedimiento de producción de olefinas ligeras y de BTX que utiliza una unidad de craqueo catalítico, NCC, que trata una carga de tipo nafta y un complejo aromático. Puede utilizarse para beneficiarse de las sinergias entre estas dos unidades. El balance térmico de la NCC, que es básicamente deficiente en coque, se resuelve por el uso óptimo de calor de los hornos de reformado con el objeto del calentamiento previo de la carga del NCC, y por introducción del refinado, al menos en parte, resultante del complejo aromático en mezcla con la nafta.

SYSTEM AND PROCESS FOR STEAM CRACKING AND PFO TREATMENT INTEGRATING HYDRODEALKYLATION AND NAPHTHA REFORMING

A process for treatment of PFO from a steam cracking zone includes hydrodealkylating PFO or a portion thereof for conversion of polyaromatics compounds contained in the PFO into hydrodealkylated aromatic compounds with one benzene ring, a hydrodealkylated BTX+ stream. In addition, a naphtha reformer is integrated, so that the hydrodealkylated BTX+ stream and a reformate stream are separated into BTX compounds.

PROCESS FOR PRODUCTION OF PROPYLENE AND AROMATIC HYDROCARBON, AND APPARATUS FOR THE PROCESS

It is an object of the present invention to provide an improved process whereby the yield structure of the components can be varied by a simple method, and the products can be produced stably and efficiently in a process for producing propylene and aromatic hydrocarbons from a hydrocarbon feedstock containing C4-12 olefins using a medium pore diameter zeolite-containing catalyst. A process for producing is disclosed which comprises a propylene production step wherein a specific zeolite catalyst is used to remove a C4+ hydrocarbon component from a reaction mixture, and part of the hydrocarbon component is recycled as necessary without modification, and an aromatic hydrocarbon production step wherein all or a part of the C4+ hydrocarbon component is used as the raw material.

СПОСОБ ПОЛУЧЕНИЯ ПРОПИЛЕНА И АРОМАТИЧЕСКИХ УГЛЕВОДОРОДОВ И УСТАНОВКА ДЛЯ ИХ ПОЛУЧЕНИЯ

FIELD: chemistry. SUBSTANCE: invention relates to a method of producing propylene and aromatic hydrocarbons (two versions), one of which involves: (1) a step for producing propylene, where hydrocarbon material which contains 50 wt % or more of at least one of C 4 - 12 -olefins in a reactor for producing propylene are brought into contact with a moulded catalyst A, which contains a first zeolite, in the conditions (i)-(iv) given below in order to carry out catalytic conversion of at least one of the C 4-12 -olefins to obtain a reaction mixture which contains propylene; the reaction mixture is divided into a fraction C mainly containing hydrogen and C 1-3 -hydrocarbons and a fraction D mainly containing at least one of the C 4+ -hydrocarbons, and propylene is extracted from the fraction C: (i) with a zeolite having average pore diametre of 5-6.5 Å; (ii) having 0.02 mmol or less protons per gram of zeolite, measured through liquid-phase ion exchange/titration of the filtrate; (iii) containing at least one metal selected from a group consisting of Group IB metals; and (iv) having molar ratio SiO 2 /Al 2 O 3 at least equal to 800 but not greater than 2000; and (2) a step for obtaining aromatic hydrocarbons in which the raw material, which completely or partially contains a fraction D or a portion of it, is brought into contact in a reactor for producing aromatic hydrocarbons with a moulded catalyst B which contains a second zeolite, under the conditions (v)-(vii) given below, in a gas phase at temperature of 650°C or below: (v) with zeolite having average pore diametre of 5-6.5 Å; (vi) with initial particle diametre in between 0.02 and 0.25 mcm; and (vii) containing at least one metal element selected from a group consisting of Group IB metal elements. EFFECT: use of the method enables to obtain propylene and aromatic hydrocarbons from hydrocarbon material which contains C 4-12 -olefins, in which the structure of two output components can be varied using a simple ...

СПОСОБ КОНВЕРСИИ ТЯЖЕЛОГО СЫРЬЯ В БЕНЗИН И ПРОПИЛЕН С РЕГУЛИРУЕМЫМ ВЫХОДОМ

... 1. Способ совместного получения бензина и пропилена из тяжелого углеводородного сырья с начальной точкой кипения больше или равной 340°С на установке каталитического крекинга, за которой следует установка олигомеризации, которые могут работать в двух режимах, называемых "максимум пропилена" и "максимум бензина", причем ! - для режима "максимум пропилена" сырье, подаваемое на установку олигомеризации, состоит из олефиновой фракции С4 или С4/С5, полученной в результате каталитического крекинга, и потоки, выходящие с установки олигомеризации, разделяют на фракцию олигомеров С8+, которую по меньшей мере частично возвращают на вход установки каталитического крекинга, причем бензиновая фракция состоит из фракции бензина, произведенной на установке каталитического крекинга, и фракции олигомеров, выходящей с установки олигомеризации, которая не была возвращена на каталитический крекинг, ! - для режима "максимум бензина" сырье, подаваемое на установку олигомеризации, состоит из олефиновой фракции ...

СПОСОБ ПОВЫШЕНИЯ ПРОИЗВОДСТВА АРОМАТИЧЕСКИХ СОЕДИНЕНИЙ

1. Способ получения ароматических соединений из лигроина в качестве сырья, включающий:подачу потока сырья в установку фракционирования и получение вследствие этого первого потока, содержащего легкие углеводороды, и второго потока, содержащего тяжелые углеводороды;подачу первого потока в первую установку риформинга, работающую при первом наборе условий реакции, и получение вследствие этого первого потока продукта, при этом первая установка риформинга имеет вход для катализатора и выход для катализатора;подачу второго потока во вторую установку риформинга, работающую при втором наборе условий реакции, и получение вследствие этого второго потока продукта, при этом вторая установка риформинга имеет вход для катализатора и выход для катализатора, в котором первый набор условий реакции включает первую температуру реакции, а второй набор условий реакции включает вторую температуру реакции, и при этом первая температура реакции больше, чем вторая температура реакции, и в котором второе давление меньше чем 580 кПа;подачу второго потока продукта в первую установку риформинга и получение при этом первого потока продукта;подачу катализатора из регенератора во вторую установку риформинга;подачу катализатора из второй установки риформинга в первую установку риформинга; иподачу первого потока продукта в установку разделения ароматических соединений,при этом указанный катализатор содержит благородный металл VIII группы на носителе.2. Способ по п. 1, в котором вторая установка риформинга содержит множество реакторов, где катализатор и второй поток последовательно проходят через множество реакторов, и дополнительн РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2013 146 967 A (51) МПК C10G 63/04 (2006.01) C10G 61/02 (2006.01) C10G 59/02 (2006.01) C10G 35/04 (2006.01) C07C 4/00 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21)(22) Заявка: 2013146967/04, 23.04.2012 (71) Заявитель(и): ЮОП ЛЛК (US) Приоритет(ы): (30) Конвенционный приоритет: 29.04.2011 ...

PROCESSING THERMAL-CRACKED OIL DISTILLATES

HYDROCARBON CONVERSION CATALYST SYSTEM

The present invention relates to a hydrocarbon conversion catalyst system comprising: a first composition comprising a dehydrogenation active metal on a solid support; and a second composition comprising a transition metal on an inorganic support and a hydrocarbon conversion process utilizing the hydrocarbon conversion catalyst system.

Method for producing aromatic hydrocarbons

Coal tar to provide aromatic compounds

Process of reforming of fuels for engines

Systems and Methods Related to The Syngas to Olefin Process

The current onvention relates to method comprising the steps of: a) providing a producing a first product steam via a Fischer-Tropsch process, wherein the first product stream comprisingcomprises a C2-C3 hydrocarbon stream, a C4 hydrocarbon stream comprising butane and butene, and a C5+ hydrocarbon stream; separating at least a portion of the C2-C3 hydrocarbon stream from the first product stream; separating at least a portion of the C4 hydrocarbon stream comprising butane and butene from the first product stream; separating at least a portion of the C5+ hydrocarbon stream from the first product stream; converting at least a portion of the butane in the C4 hydrocarbon stream to butene; and converting at least a portion of the butene in the C4 hydrocarbon stream to butadiene; and converting at least a portion of the C5+ hydrocarbon stream to BTX.

NAPHTHA HYDROPROCESSING WITH MERCAPTAN REMOVAL

Cette invention traite du craquage de la naphtabitumine avec extraction de mercaptan du produit.L'alimentation en naphtabitumine est hydrotraitée et hydrocraquée.Les contaminants à teneur de soufre, notamment les C5+ mercaptans recombinants, sont alors extraits sélectivement de la naphtabitumine hydrocraquée par extraction sélective ou adsorption.

Synthetic hydrocarbon products

The invention includes a process for producing synthetic middle distillates and synthetic middle distillates produced therefrom. In one embodiment, the process comprises fractionating a hydrocarbon synthesis product to at least generate a light middle distillate, a heavy middle distillate, and a waxy fraction; thermally cracking the waxy fraction; and isomerizing the heavy middle distillate. A synthetic diesel or blending component is formed by the combination of at least a portion of the light middle distillate; at least a portion or fraction of the thermally cracked product; and at least a portion or fraction of the isomerized product. In some embodiments, the hydrocarbon synthesis product and/or the thermally cracked product may be hydrotreated. In other embodiments, a synthetic middle distillate comprises at least two fractions: a light fraction with not more than 10% branched hydrocarbons, and a heavy fraction with at least 30% branched hydrocarbons.

АЛИФАТИЧЕСКИЙ КОМПОНЕНТ БЕНЗИНА И СПОСОБ ЕГО ПОЛУЧЕНИЯ

... 1. Алифатический бензиновой компонент, содержащий более 90 мас.% смеси триметилзамещенных соединений и монометилзамещенных соединений в массовом соотношении между триметил и монометилпроизводными, по меньшей мере, 0,03, причем указанные соединения могут представлять собой парафины и олефины.2. Бензиновый компонент по п.1 с массовым соотношением между триметил и монометилпроизводными, составляющим не более 0,3.3. Бензиновый компонент по любому из пп.1 и 2, в котором содержание 2,2,4-триметилпентана составляет 2-20 мас.%.4. Бензиновая топливная композиция, содержащая алифатический бензиновый компонент по любому из пп.1-3, одну или несколько присадок, ароматические соединения в количестве 1-22 об.% (определенные согласно ASTM D5580-95), имеющая моторное октановое число выше 90 и содержащая серу в количестве менее 15 мас.ч./млн (определенную согласно ASTM D5453-93).5. Способ получения алифатического бензинового компонента, включающий(a) контактирование продукта синтеза Фишера-Тропша с каталитической ...

Processing thermally cracked oil distillates

A hydrocarbon feed comprising a thermal-cracked oil distillate obtained from a process for thermal cracking of a petrolic heavy residual oil at a temperature of 400 DEG C to 700 DEG C, said distillate consisting mainly of hydrocarbons boiling in the range of 120 DEG to 290 DEG C and said distillate containing aliphatic olefins, is treated at a reaction temperature of 30 DEG to 300 DEG C in liquid phase in the presence of an acid catalyst, to obtain a reaction product having a boiling range which is higher than that of the hydrocarbons as the main component of the distillate and which is not lower than 260 DEG C.

PROCESSES FOR AN IMPROVEMENT TO GASOLINE OCTANE FOR LONG-CHAIN PARAFFIN FEED STREAMS

Method for making higher-octane fuel components from a feed stream of C8+ paraffins, including catalytically cracking the C8+ paraffins using a Zeolite catalyst to produce a reaction product of mid-chain paraffins and olefins and short-chain paraffins and olefins. The reaction product comprises liquid phase paraffins having an increased Octane Value over the feed stream paraffins. The reaction product further comprises a gas phase of short-chain paraffins which are separated from the liquid phase. In embodiments, the short chain olefins are hydrogenated to form mid-chain paraffins and a gas phase containing short chain paraffins.

PRODUCTION OF AROMATICS FROM NONCATALYTICALLY CRACKED FATTY ACID BASED OILS

A method for producing aromatic compounds from fatty acid oils including heating a fatty acid oil to a temperature between about 100° C to about 800° C at a pressure between about vacuum conditions and about 200 psia for a time sufficient to crack the oil and produce a cracked fatty acid oil; removing undesired materials, unreacted oil, heavy ends, and light ends from the cracked fatty acid oil; heating the resulting purified cracked fatty acid oil to a temperature between about 100° C to about 800° C at a pressure between about vacuum conditions and about 200 psia for a time sufficient to reform alkenes and alkanes in the cracked fatty acid oil into aromatic compounds and produce a reformed fatty acid oil; and extracting components from the reformed fatty acid oil to produce a mixture of chemical products containing between 5% and 90% aromatic compounds by weight.

PROCESS FOR THE PRODUCTION OF OLEFINS AND LIGHTWEIGHT [...] USING A CATALYTIC CRACKING UNIT [...] TREATING A FILLER TYPE NAPHTHA, CATALYTIC REFORMING UNIT A AND HAS A COMPLEX AROMATIC

CATALYTIC REFORMING OF NAPHTHA

PROCESS FOR PRODUCING LIGHT OLEFINS AND BTX USING A CATALYTIC CRACKING UNIT NCC TREATING A FILLER TYPE NAPHTHA, CATALYTIC REFORMING UNIT AND HAS A COMPLEX AROMATIC

AROMATIC HYDROCARBON PRODUCTION PROCESS

PRODUCTION OF AROMATICS FROM NONCATALYTICALLY CRACKED FATTY ACID BASED OILS

A method for producing aromatic compounds from fatty acid oils including heating a fatty acid oil to a temperature between about 100° C to about 800° C at a pressure between about vacuum conditions and about 200 psia for a time sufficient to crack the oil and produce a cracked fatty acid oil; removing undesired materials, unreacted oil, heavy ends, and light ends from the cracked fatty acid oil; heating the resulting purified cracked fatty acid oil to a temperature between about 100° C to about 800° C at a pressure between about vacuum conditions and about 200 psia for a time sufficient to reform alkenes and alkanes in the cracked fatty acid oil into aromatic compounds and produce a reformed fatty acid oil; and extracting components from the reformed fatty acid oil to produce a mixture of chemical products containing between 5% and 90% aromatic compounds by weight.

Thermo-catalytic cracking for conversion of higher hydrocarbons into lower hydrocarbons

Described herein are processes and related devices and systems for the conversion of higher hydrocarbons, such as in the form of waste plastics, petroleum sludge, slope oil, vegetable oil, and so forth, into lower hydrocarbons, which can be used as fuels or raw materials for a variety of industrial and domestic uses.

Aliphatic gasoline component and process to prepare said gasoline component

A process to prepare an aliphatic gasoline component comprising more than 90 wt % of trimethyl substituted compounds and monomethyl substituted compounds in a weight ratio of trimethyl to monomethyl compounds of at least 0.03 by (a) contacting a Fischer-Tropsch synthesis product with a catalyst comprising an acidic matrix and a large pore molecular sieve in a riser reactor at a temperature of between 450 and 650° C. at a contact time of between 1 and 10 seconds and at a catalyst to oil ratio of between 2 and 20 kg/kg; (b) isolating from the product of step (a) a gasoline fraction and a fraction comprising iso-butane and iso-butylene; (c) subjecting the iso-butane and the iso-butylene obtained in step (b) to an alkylation step to prepare a trimethyl substituted pentane; and (d) combining the gasoline fraction with the product rich in trimethyl substituted pentane.

PROCESSES AND SYSTEMS FOR PETROCHEMICAL PRODUCTION INTEGRATING FLUID CATALYTIC CRACKING AND DEEP HYDROGENATION OF FLUID CATALYTIC CRACKING REACTION PRODUCTS

A feedstock is processed in an FCC unit to produce at least light olefins, FCC naphtha, light cycle oil and heavy cycle oil. Light cycle oil, and in certain embodiments hydrotreated light cycle oil, is subjected to deep hydrogenation to produce a deeply hydrogenated middle distillate fraction. All or a portion of the deeply hydrogenated middle distillate fraction is used as feed to the stream cracking zone to produce light olefins. 1. A process for petrochemical production comprising:providing a feedstock selected from the group consisting of naphtha, diesel or heavy oils;subjecting the feedstock to fluid catalytic cracking to produce at least light cycle oil;subjecting all or a portion of the light cycle oil to hydrogenation to hydrogenate aromatics contained in the light cycle oil and produce hydrogenated middle distillates, wherein hydrogenation occurs in the presence of an effective quantity of a hydrogenation catalyst containing one or more active metal components selected from Pt, Pd, Re and a combination comprising at least two of Pt, Pd or Re, and the hydrogenation catalyst including a catalyst support comprising non-acidic amorphous alumina and about 0.1-15 wt % of a modified USY zeolite having one or more of Ti, Zr and/or Hf substituting aluminum atoms constituting the zeolite framework thereof; andsubjecting all or a portion of the hydrogenated middle distillates to thermal cracking in a steam cracking complex to obtain light olefins.2. The process as in claim 1 , whereinthe feedstock is a heavy oil selected from the group consisting of atmospheric gas oil, heavy atmospheric gas oil, vacuum gas oil, atmospheric residue, deasphalted oil, demetallized oil, coker gas oil, gas oil obtained from a visbreaking process, and combinations comprising at least one of the foregoing heavy oils.38-. (canceled)9. The process as in claim 1 , further comprisinghydrotreating all or a portion of the light cycle oil to produce hydrotreated light cycle oil, and subjecting all ...

Synthetic hydrocarbon products

The invention includes a process for producing synthetic middle distillates and synthetic middle distillates produced therefrom. In one embodiment, the process comprises fractionating a hydrocarbon synthesis product to at least generate a light middle distillate, a heavy middle distillate, and a waxy fraction; thermally cracking the waxy fraction; and isomerizing the heavy middle distillate. A synthetic diesel or blending component is formed by the combination of at least a portion of the light middle distillate; at least a portion or fraction of the thermally cracked product; and at least a portion or fraction of the isomerized product. In some embodiments, the hydrocarbon synthesis product and/or the thermally cracked product may be hydrotreated. In other embodiments, a synthetic middle distillate comprises at least two fractions: a light fraction with not more than 10% branched hydrocarbons, and a heavy fraction with at least 30% branched hydrocarbons.

PRODUCTION OF AROMATICS FROM NONCATALYTICALLY CRACKED FATTY ACID BASED OILS

СПОСОБ ПОЛУЧЕНИЯ ЛЕГКИХ ОЛЕФИНОВ И BTX, В КОТОРОМ ПРИМЕНЯЕТСЯ УСТАНОВКА КАТАЛИТИЧЕСКОГО КРЕКИНГА NCC, ОБРАБАТЫВАЮЩАЯ СЫРЬЕ ТИПА НАФТЫ, УСТАНОВКА КАТАЛИТИЧЕСКОГО РИФОРМИНГА И АРОМАТИЧЕСКИЙ КОМПЛЕКС

FIELD: oil and gas industry. SUBSTANCE: invention relates to a method for producing light olefins and BTX from a naphtha fraction with an initial boiling point above 30 °C and final boiling point below 220 °C, wherein using a catalytic cracking unit (NCC) to process light naphtha-type feedstock (30–T M  °C), catalytic reformer (REF) for processing feedstock referred to as heavy naphtha (T M  °C–220 °C), and an aromatic complex (CA), to which are fed streams from catalytic reforming (REF) and fractions of 60+ streams from the NCC. Said method includes the sequence of the following operations: feeding naphtha feedstock with initial boiling point higher than or equal to 30 °C, and a final boiling point higher than or equal to 220 °C, into a hydrotreating unit (HDT), to remove sulphur and nitrogen compounds present in the feedstock, feeding the hydrotreated naphtha feedstock to a separation unit (SPLIT 1), which enables to separate a light fraction, called light naphtha, with a boiling range of 40–T M  °C, and a heavy fraction, called heavy naphtha, with a boiling range T M –220 °C, where T M  °C ranges from 80 °C to 160 °C, preferably from 100 °C to 150 °C and very preferably from 110 °C to 140 °C, feeding light naphtha as feedstock into the NCC, feeding heavy naphtha as a feedstock to the catalytic reforming unit (REF), separation of the streams leaving the NCC in a fractionation unit (FRAC), which allows separating the light fraction fed for separation, called the cold box (SBF), which allows separation of H 2 , CH 4 and light paraffins C2, C3 and C4, on one hand, and ethylene and propylene, on the other hand, feeding the heavy fraction leaving the separator (FRAC) mixed with catalytic reforming (REF) streams as feedstock to the aromatic complex (CA), collecting from the aromatic complex (CA) BTX, raffinate, defined as the non-aromatic part of the stream, at least part of which is fed in a mixture with light naphtha as feedstock for NCC, and a fraction, called heavy ...

ИНТЕГРИРОВАННЫЙ ПРОЦЕСС ДЛЯ МАКСИМАЛЬНОГО ИЗВЛЕЧЕНИЯ ВОДОРОДА

Изобретение касается интегрированного процесса для максимального извлечения водорода. Процесс включает в себя: подачу углеводородсодержащего сырья, содержащего лигроин, и потока водорода в зону риформинга, причем поток водорода получают из по меньшей мере одной из зоны гидрокрекинга, зоны трансалкилирования и зоны изомеризации. Углеводородсодержащее сырье проходит риформинг в зоне риформинга в присутствии потока водорода и катализатора риформинга для создания потока продукта риформинга. По меньшей мере часть потока продукта риформинга поступает в колонну дебутанизации зоны риформинга для создания конечного потока водорода и фракции, содержащей сжиженный нефтяной газ (СНГ). По меньшей мере часть конечного потока водорода возвращают в зону риформинга в виде потока водорода. Изобретение также касается варианта интегрированного процесса для максимального извлечения водорода. Технический результат - комплексная интеграция зоны гидрокрекинга, зоны трансалкилирования, зоны изомеризации с зоной ...

Patent RU2015112094A3

`7ВУ’” 2015112094`” АЗ Дата публикации: 12.10.2018 Форма № 18 ИЗ,ПМ-2011 Федеральная служба по интеллектуальной собственности Федеральное государственное бюджетное учреждение ж Я «Федеральный институт промышленной собственности» (ФИПС) ОТЧЕТ О ПОИСКЕ 1. . ИДЕНТИФИКАЦИЯ ЗАЯВКИ Регистрационный номер Дата подачи 2015112094/04(018896) 02.04.2015 Приоритет установлен по дате: [ ] подачи заявки [ ] поступления дополнительных материалов от к ранее поданной заявке № [ ] приоритета по первоначальной заявке № из которой данная заявка выделена [ ] подачи первоначальной заявки № из которой данная заявка выделена [ ] подачи ранее поданной заявки № [Х] подачи первой(ых) заявки(ок) в государстве-участнике Парижской конвенции (31) Номер первой(ых) заявки(ок) (32) Дата подачи первой(ых) заявки(ок) (33) Код страны 1. 1453075 07.04.2014 ЕК Название изобретения (полезной модели): [Х] - как заявлено; [ ] - уточненное (см. Примечания) СПОСОБ ПОЛУЧЕНИЯ ЛЕГКИХ ОЛЕФИНОВ И ВТХ С ПРИМЕНЕНИЕМ УСТАНОВКИ КАТАЛИТИЧЕСКОГО КРЕКИНГА, ОБРАБАТЫВАЮЩЕЙ ТЯЖЕЛОЕ СЫРЬЕ ТИПА УСО ГЛУБОКОЙ ГИДРООЧИСТКИ, В КОМБИНАЦИИ С УСТАНОВКОЙ КАТАЛИТИЧЕСКОГО РИФОРМИНГА И АРОМАТИЧЕСКИМ КОМПЛЕКСОМ, ОБРАБАТЫВАЮЩИМ СЫРЬЕ ТИПА НАФТЫ Заявитель: ИФП ЭНЕРЖИ НУВЕЛЛЬ, ЕК 2. ЕДИНСТВО ИЗОБРЕТЕНИЯ [Х] соблюдено [ ] не соблюдено. Пояснения: см. Примечания 3. ФОРМУЛА ИЗОБРЕТЕНИЯ: [Х] приняты во внимание все пункты (см. Примечания) [ ] приняты во внимание следующие пункты: [ ] принята во внимание измененная формула изобретения (см. Примечания) 4. КЛАССИФИКАЦИЯ ОБЪЕКТА ИЗОБРЕТЕНИЯ (ПОЛЕЗНОЙ МОДЕЛИ) (Указываются индексы МПК и индикатор текущей версии) С10С 11/18 (2006.01) С10С 35/00 (2006.01) С07С 15/04 (2006.01) С10С 69/04 (2006.01) С07С 11/4 (2006.01) С07С 15/08 (2006.01) С10С 69/08 (2006.01) С07С 11/06 (2006.01) С1ОС 63/04 (2006.01) С07С 15/06 (2006.01) 5. ОБЛАСТЬ ПОИСКА 5.1 Проверенный минимум документации РСТ (указывается индексами МПК) С10С 11/18, С10С 35/00, С07С 15/04, С1ОС 69/04, С07С 11/04, С07С 15/08, С10С 69/08, С07С 11/06, ...

СПОСОБ ПОВЫШЕНИЯ ПРОИЗВОДСТВА АРОМАТИЧЕСКИХ СОЕДИНЕНИЙ

Изобретение относится к способу получения ароматических соединений из лигроина в качестве сырья. Способ включает: подачу потока сырья в установку фракционирования и получение вследствие этого первого потока, содержащего легкие углеводороды, и второго потока, содержащего тяжелые углеводороды; подачу первого потока в первую установку риформинга, работающую при первом наборе условий реакции, и получение вследствие этого первого потока продукта, при этом первая установка риформинга имеет вход для катализатора и выход для катализатора; подачу второго потока во вторую установку риформинга, работающую при втором наборе условий реакции, и получение вследствие этого второго потока продукта, при этом вторая установка риформинга имеет вход для катализатора и выход для катализатора, в котором первый набор условий реакции включает первую температуру реакции, а второй набор условий реакции включает вторую температуру реакции, и при этом первая температура реакции больше, чем вторая температура реакции ...

ПРЕВРАЩЕНИЕ МАЗУТА В ХИМИЧЕСКИЕ ПРОДУКТЫ

Изобретение касается способа превращения высокосернистого мазута в нефтехимические продукты, который включает гидрокрекинг высокосернистого мазута на установке гидрокрекинга мазута, содержащей кипящий слой или суспендированный слой катализатора, с образованием потока крекированного мазута. Также способ включает стадии разделения потока крекированного мазута на легкую фракцию и тяжелую фракцию, гидрокрекинг легкой фракции на установке гидрокрекинга дистиллята с образованием крекинг-потока, разделения крекинг-потока на фракцию водорода, легкую углеводородную фракцию, легкую фракцию нафты и тяжелую фракцию нафты; риформинг тяжелой фракции нафты с получением потока риформинга, содержащего водород и по меньшей мере одно из бензола, толуола и ксилолов, а также паровой крекинг легкой углеводородной фракции и/или легкой фракции нафты с получением потока, выходящего из установки парового крекинга, содержащего по меньшей мере одно из этилена, пропилена, бензола, толуола и ксилолов. Гидрокрекинг высокосернистого ...

Process for making an improved gasoline

... 551.663. Cracking hydrocarbons. INTERNATIONAL CATALYTIC OIL PROCESSES CORPORATION. Aug. 28, 1941, No. 9949. Convention date, Aug. 2. 1940. [Class 32] [Also in Group IV] Gasoline of improved octane number and stability is obtained by cracking a gas oil in presence of a catalyst which has already been used in the catalytic treatment of hydrocarbons, fractionating the cracked products to separate hydrogen, gaseous hydrocarbons and gasoline, and reforming the gasoline with or without the gases by passage over fresh or regenerated catalyst. The reforming operation effects the polymerization and alkylization of olefines, the isomerization of paraffins and the stabilization of unsaturates in the cracked product. Preferably the catalyst which has been used in the reforming is used without regeneration in the cracking stage. East Texas reduced crude vaporized in coil 3, heated to 825-850‹F. and separated from heavy fractions in flash evaporator 8, is formed into a suspension in an injector 12 with ...

Thermo-catalytic cracking for conversion of higher hydrocarbons into lower hydrocarbons

Described herein are processes and related devices and systems for the conversion of higher hydrocarbons, such as in the form of waste plastics, petroleum sludge, slope oil, vegetable oil, and so forth, into lower hydrocarbons, which can be used as fuels or raw materials for a variety of industrial and domestic uses.

METHOD OF PROCESSING THERMAL-CRACKED OIL DISTILLATES

PROCESS FOR UP-GRADING STEAM-CRACKING PRODUCTS

There is provided with the present invention a new process for up-grading products resulting from the steam-cracking of hydrocarbons which comprises bringing the steam-cracking reaction products in contact with a catalyst comprising a mixture of from 2.5 to 7.5% wt of Cr2O3, 5 to 17.5% wt of A12O3 and 75 to 85% wt of a Zn-ZSM-5 zeolite or a Zn-ZSM-5 zeolite/asbestos and recovering the desired products.

나프타 분해

... 탄화수소 스트림으로부터 경질 올레핀의 수율과 방향족 화합물의 수율을 증가시키는 방법을 제공한다. 이 방법은, 개질이 불가능한 경질 성분을 분해 유닛으로 이송하고 나머지는 제2 분리 유닛으로 이송하기 위한 제1 분리를 포함한다. 제2 분리 유닛은 분해 유닛으로 이송하기 위해 탄화수소 스트림으로부터 노말(normal) 성분을 추출한다. 이렇게 얻은, 경질 유분 및 노말 성분이 감소된 탄화수소 스트림은 개질 유닛으로 이송된다.

componente de gasolina alifática, composição de combustìvel de gasolina, e, processo para preparar um componente de gasolina alifática

Systems and processes for separating and upgrading hydrocarbons integrating a refinery system with steam cracking of an aromatic bottoms stream

A process for separating and upgrading a hydrocarbon feed includes passing the hydrocarbon feed to a distillation unit to separate it into at least a naphtha stream and a residue, passing the naphtha stream to a NHT that hydrotreats the naphtha stream to produce a hydrotreated naphtha, passing the hydrotreated naphtha to an NREF that reforms the hydrotreated naphtha to produce a reformate, passing the reformate to an ARC that processes the reformate to produce at least one aromatic product effluent and an aromatic bottoms stream, and passing at least a portion of the aromatic bottoms stream comprising C9+ aromatic compounds to a steam cracking unit. The steam cracking unit may further upgrade the aromatic bottoms stream, which may increase the yields of greater value chemical intermediates and fuel blending components from the process. Systems for conducting the process are also described.

Method of producing lower olefin and monocyclic aromatic hydrocarbon having 6 to 8 carbon atoms and device for producing lower olefin and monocyclic aromatic hydrocarbon having 6 to 8 carbon atoms

A method of producing a lower olefin and BTX from stock oils selected from at least two kinds of oils is provided. The method includes a first catalytic cracking step of bringing one stock oil A into contact with a catalytic cracking catalyst; a second catalytic cracking step of bringing one stock oil B, having an aromatic component content smaller than that of the stock oil A, into contact with the catalytic cracking catalyst; and a separation and collection step of collecting the lower olefins and BTX from a product generated in the first and second catalytic cracking steps. A contact time A during which the stock oil A is in contact with the catalytic cracking catalyst in the first catalytic cracking step is longer than a contact time B during which the stock oil B is in contact with the catalytic cracking catalyst in the second catalytic cracking step.

PROCESSES AND SYSTEMS FOR PETROCHEMICAL PRODUCTION INTEGRATING DEEP HYDROGENATION OF MIDDLE DISTILLATES

Process scheme configurations are disclosed that enable deep hydrogenation of middle distillates. The hydrogenated middle distillates are processed in a steam cracker for conversion into light olefins. Feeds to the deep hydrogenation zone include diesel range streams from a diesel hydrotreating zone, a gas oil hydroprocessing zone, and/or a vacuum residue hydrocracking zone. The deep hydrogenation zone operates under conditions effective to reduce aromatic content in a diesel range feedstream from a range of about 10-40 wt % or greater, to a hydrogenated distillate range intermediate product having an aromatic content of less than about 5-0.5 wt %.

Process for making high octane gasoline

A process for converting the naphtha fractions distilled from crude oil into greater volumes than heretofore of a gasoline product having higher octane number and a distillate stream of improved cetane number and smoke point by sending the lower boiling naphtha fraction directly to the gasoline pool and subjecting the higher boiling naphtha fraction to a mild reforming treatment, extracting the reformate to separate two streams, aromatics which are directed to the pool and paraffins which are sent to a splitter to separate the paraffin stream into fractions greater than C8 and a C8 or less fraction. The C8 or less fraction is cracked, thermally or catalytically and alkylated and/or polymerized before being directed to the gasoline pool. The fraction from the splitter containing hydrocarbons greater than C8 can be used in the distillate pool.

PROCESS FOR IMPROVING THE OCTANE NUMBER OF CRACKED GASOLINES

A METHOD FOR PRODUCING A MIXTURE OF HYDROCARBONS

A method for producing a mixture hydrocarbons; a blend for producing a mixture of hydrocarbons; a mixture of hydrocarbons; and use of the mixture of hydrocarbons for producing chemicals and/or polymers.

THERMO-CATALYTIC CRACKING FOR CONVERSION OF HIGHER HYDROCARBONS INTO LOWER HYDROCARBONS

Described herein are processes and related devices and systems for the conversion of higher hydrocarbons, such as in the form of waste plastics, petroleum sludge, slope oil, vegetable oil, and so forth, into lower hydrocarbons, which can be used as fuels or raw materials for a variety of industrial and domestic uses.

THERMO-CATALYTIC CRACKING FOR CONVERSION OF HIGHER HYDROCARBONS INTO LOWER HYDROCARBONS

Described herein are processes and related devices and systems for the conversion of higher hydrocarbons, such as in the form of waste plastics, petroleum sludge, slope oil, vegetable oil, and so forth, into lower hydrocarbons. The process comprises providing a feedstock in the form of at least one solid raw material and at least one liquid raw material; converting the feedstock into a liquid and/or liquid slurry; cracking the feedstock at 275° C to 500° C with creation of a thin film of the feedstock to produce cracked feedstock in a gaseous phase; and condensing the resulting restricted gaseous product to produce a product including lower hydrocarbons.

HIGH OCTANE GASOLINE PRODUCTION

Catalytically reforming naphtha, comprises contacting naphtha with reforming catalyst, in presence of hydrogen gas for performing surface catalytic reforming reaction to obtain naphthenes, and hydrocarbon arenes and paraffins

Catalytically reforming naphtha, comprises contacting naphtha with reforming catalyst, in the presence of hydrogen gas, under conditions of pressure of 0.15-3 MPa at 300-450[deg] C and a volume space velocity of 2.1-50 h -> 1>for performing a surface catalytic reforming reaction to obtain a conversion ratio of naphthenes of greater than 85 wt.%, and a conversion ratio of 4C-hydrocarbon arenes and paraffins of less than 30 wt.%.

PROCESS FOR PRODUCING LIGHT OLEFINS AND BTX UNIT FCC TREATING A FILLER LIKE HEAVY VGO HYDROTRAITE HIGH, COUPLED WITH A CATALYTIC REFORMER UNIT AND A COMPLEX AROMATIC NAPHTHA-TREATING A FILLER.

La présente invention concerne les unités de FCC traitant des charges lourdes enrichies en hydrogène, telle par exemple qu'un VGO très hydrotraité, ou la partie non convertie à l'issue d'un hydrocraquage de ce même type de charge VGO, charges qui présentent la caractéristique de craquer en oléfines légères telles que l'éthylène et le propylène. L'intégration d'un FCC avec un complexe aromatique permet la récupération par le complexe aromatique des BTX formés dans le FCC, et la récupération par le FCC du flux de fond de la colonne aromatiques lourds du complexe aromatique. The present invention relates to FCC units treating hydrogen-enriched heavy charges, such as for example a highly hydrotreated VGO, or the unconverted part resulting from a hydrocracking of the same type of VGO charge, charges which present the characteristic of cracking light olefins such as ethylene and propylene. The integration of an FCC with an aromatic complex allows the recovery by the aromatic complex of the BTX formed in the FCC, and the recovery by the FCC of the bottom flow of the aromatic heavy column of the aromatic complex.

Processes for an improvement to gasoline octane for long chain paraffin feed streams

Methods for making higher-octane fuel components from a feed stream of C8+ paraffins, including catalytically cracking the C8+ paraffins using a Zeolite catalyst to produce a reaction product of mid-chain paraffins and olefins and short-chain paraffins and olefins. The reaction product comprises liquid phase paraffins having an increased Octane Value over the feed stream paraffins. The reaction product further comprises a gas phase of short-chain paraffins which are separated from the liquid phase. In embodiments, the short chain olefins are hydrogenated to form mid-chain paraffins and a gas phase containing short-chain paraffins.

Improvements in and relating to cracking of heavy hydrocarbon oils

Heavy hydrocarbon oils are cracked in the presence of liquid hydrogen fluoride as catalyst, the effluent from the cracking zone is allowed to settle into two liquid phases, viz. a hydrocarbon phase and a hydrogen fluoride phase, gasoline is separated from the hydrocarbon phase, at least a portion of the gasoline is subjected to catalytic reforming under conditions conducive to the formation of free hydrogen, and the hydrogen fluoride phase is treated with this free hydrogen, preferably in the presence of boron trifluoride, in order to hydrogenate the hydrocarbon and other contaminants dissolved therein so that purified hydrogen fluoride may be readily recovered. Gasoline rich in isoparaffins and aromatic hydrocarbons is the primary product of the process. The reforming step, which involves dehydrogenation of naphthenes, is ordinarily carried out in the presence of hydrogen. Alumina composited with an oxide of molybdenum, chromium or vanadium may be used as reforming catalyst; but a preferred ...

HIGH OCTANE GASOLINE PRODUCTION

METHOD FOR PRODUCING LOWER OLEFIN AND C6-8 MONOCYCLIC AROMATIC HYDROCARBON AND APPARATUS FOR PRODUCING LOWER OLEFIN AND C6-8 MONOCYCLIC AROMATIC HYDROCARBON

REFORMING PROCESS WITH INTEGRATED FLUID CATALYTIC CRACKER GASOLINE AND HYDROPROCESSED CYCLE OIL

INTEGRATED HYDROTHERMAL PROCESS TO UPGRADE HEAVY OIL

SupercriticalWater Reactor Flash Drum Aqueous Reforming Unit FIG. (12) INTERNATIONAL APPLICATION PUBLISHED UNDER THE PATENT COOPERATION TREATY (PCT) (19) World Intellectual Property Organization International Bureau (43) International Publication Date 13 September 2018 (13.09.2018) WIPO I PCT IiiimmoimiolollmonolomommoiloolmommovoimIE (10) International Publication Number WO 2018/165394 Al (51) International Patent Classification: ClOG 31/08 (2006.01) ClOG 53/02 (2006.01) C01B 3/38 (2006.01) ClOG 65/12 (2006.01) ClOG 45/26 (2006.01) ClOG 47/32 (2006.01) (21) International Application Number: PCT/US2018/021491 (22) International Filing Date: 08 March 2018 (08.03.2018) (25) Filing Language: English (26) Publication Language: English (30) Priority Data: 62/468,721 08 March 2017 (08.03.2017) US (71) Applicant: SAUDI ARABIAN OIL COMPANY [SA/SA]; 1 Eastern Avenue, Dhahran, 31311 (SA). (71) Applicant (for AG only): ARAMCO SERVICES COM- PANY [US/US]; 9009 West Loop South, Houston, TX 77096 (US) ...

METHOD FOR PRODUCING AROMATIC HYDROCARBONS

A method for producing aromatic hydrocarbons by bringing a feedstock derived from a fraction containing a light cycle oil produced in a fluid catalytic cracking into contact with a catalyst containing a crystalline aluminosilicate, wherein the proportion of the naphthene content within the feedstock is adjusted so as to be greater than the proportion of the naphthene content in the fraction containing the light cycle oil, and the contact between the feedstock and the catalyst is performed under a pressure within a range from 0.1 MPaG to 1.0 MPaG.

Method and System for Processing Gasoline Fractions

A method for processing a gasoline fraction includes the steps of: a) reacting the gasoline fraction in an aromatization unit, and separating the resulting reaction product to obtain a C4− component, a C5component, a C6-C7component, a C8component and a C9+ component; b) reacting the resulting C6-C7component and the C9+ component in a cracking and aromatics conversion unit, and separating the resulting reaction product to obtain a C4− component, a C5component, a C6-C7component, a C8component and a C9+ component; and c) recycling at least a part of at least one of the C6-C7component and the C9+ component from step b) to the cracking and aromatics conversion unit of step b) for further reaction. The method can convert the gasoline fraction into C8aromatic hydrocarbon(s) and produce light olefins and a high-quality light gasoline as byproducts.

METHOD OF PROCESSING THERMAL-CRACKED OIL DISTILLATES

A hydrocarbon feed comprising a thermal-cracked oil distillate obtained from a process for thermal cracking of a petrolic heavy residual oil at a temperature not lower than 400.degree.C and not exceeding 700.degree.C, said distillate consisting mainly of hydrocarbons boiling in the range of 120.degree. to 290.degree.C and said distillate containing aliphatic olefins, is treated at a reaction temperature of 30.degree. to 300.degree.C in liquid phase in the presence of an acid catalyst, to obtain a reaction product having a boiling range which is higher than that of the hydrocarbons as the main component of the distillate and which is not lower than 260.degree.C.

CONVERSION OF HYDROCARBONS

HIGH OCTANE GASOLINE PRODUCTION

Improvements with the treatments of hydrocarbons

A PROCESS FOR CONVERTING A FEEDSTOCK FOR THE PRODUCTION OF HYDROCARBONS BY THE FISCHER-TROPSCH SYNTHESIS PATHWAY

La présente invention concerne un procédé de production d'hydrocarbures de synthèse à partir d'une charge, ledit procédé comprenant au moins une étape de gazéification, une étape de conversion du CO à la vapeur, une étape de recombinaison des effluents, une étape d'élimination des gaz acides, une étape de purification finale, une étape de synthèse Fischer-Tropsch, une étape d'hydrotraitement, une étape d'hydroisomérisation/d'hydrocraquage, une étape de séparation, une étape de reformage/aromatisation permettant de produire de l'hydrogène qui est recyclé dans une des étapes en aval de l'étape de conversion du CO et en amont de l'étape de synthèse Fischer-Tropsch. L'apport de cet hydrogène permet de réduire la quantité de CO à convertir au niveau de l'étape de conversion du CO et de limiter la perte de matière carbonée par la formation de CO2.

Aromatics production process

Embodiments of the present disclosure include methods for producing aromatic products, the methods including separating a crude oil and condensate feed into at least a light naphtha stream, a heavy naphtha stream, and a bottoms stream, reforming at least a portion of the heavy naphtha stream to produce a reformate stream, feeding a cracker feed stream, comprising the light naphtha stream, the bottoms stream, and a reformate extraction raffinate, to an olefins cracker to produce cracker products comprising pyrolysis gasoline, and introducing an extractor feed stream comprising the pyrolysis gasoline and the reformate to an aromatic extraction unit to produce an aromatic product and the reformate extraction raffinate.

AROMATIC GASOLINE PRODUCTION

... 1338612 Cracking and reforming naphtha UNIVERSAL OIL PRODUCTS CO 16 Dec 1970 [17 Dec 1969] 59689/70 Heading C5E An aromatic gasoline and saturated and unsaturated hydrocarbons having three or four carbon atoms in the molecule are made from a feedstock comprising both alkanes and naphthenes boiling in the range 82‹ to 204‹ C. by first reforming the feed under conditions to convert more than 80% of the naphthenes but less than 40% of the alkanes to aromatics, then separating the product into an aromatic gasoline stream and a saturated hydrocarbon stream by solvent extraction and finally cracking the saturated stream in a fluidized bed of catalyst without added hydrogen. The hydrocarbons of three or four carbon atoms may be used to make alkylate gasoline, or hydrolysed to alcohols or converted to amines, esters, ethers or ketones, all of which can be used as gasoline components. Suitable feedstocks are straight-run gasoline, natural gasolines, and thermally or catalytically cracked gasolines ...

MIXTURE CONTAINING 1,3-BUTADIENE AND PROCESS FOR PRODUCING THE SAME

To provide a C4 fraction that contains significantly reduced amounts of butynes and methylallene and to provide a process for low-cost and effective production of ethers in which the C4 fraction is used as the starting material for a telomerization process. A mixture containing 25 to 80 mass% 1,3-butadiene, 13 to 68 mass% butenes and 2 to 15 mass% butanes with butynes and methylallene being contained in amounts of 50 ppm or less and to 800 ppm, respectively

Process for providing aromatics from coal tar

MIXTURE CONTAINING 1,3-BUTADIENE, AND PROCESS FOR PREPARING THE SAME, WHICH COMPRISES STEP OF CARRYING OUT TELOMERIZATION OF C4 CUTS

PURPOSE: Provided is a mixture containing 1,3-butadiene, which contains a very low amount of butynes and methyl allene, is obtained through a simple and cost-efficient process, and shows high industrial applicability. CONSTITUTION: The mixture comprises: 25-80 wt% of 1,3-butadiene; 13-68 wt% of butenes; 2-15 wt% of butynes; 50 ppm or less of butynes; and 5-800 ppm of methyl allene. The mixture is obtained by subjecting cuts obtained from naptha cracking and based on compound having 4 carbon atoms to selective hydrogenation of butynes and methyl allene in the presence of a Cu-based catalyst containing an alkaline earth metal. © KIPO 2007 ...

Aliphatic gasoline component and process to prepare said gasoline component

An aliphatic gasoline component comprising more than 90 wt % of a mixture of trimethyl substituted compounds and monomethyl substituted compounds in a weight ratio of trimethyl to monomethyl compounds of at least 0.03 and wherein the compounds may be paraffins and olefins. The invention is also directed to a process to prepare an aliphatic gasoline component by (a) contacting a Fischer-Tropsch synthesis product with a catalyst system comprising a catalyst, which catalyst comprises an acidic matrix and a large pore molecular sieve in a riser reactor at a temperature of between 450 and 650° C. at a contact time of between 1 and 10 seconds and at a catalyst to oil ratio of between 2 and 20 k.g/kg, (b) isolating from the product of step (a) a gasoline fraction and a fraction comprising iso-butane and isobutylene; (c) subjecting the iso-butane and the iso-butylene obtained in step (b) to an alkylation step to prepare a trimethyl substituted pentane, and (d) combining the gasoline fraction obtained ...

PROCESS FOR IMPROVING THE OCTANE NUMBER OF CRACKED GASOLINES

process for producing propylene and aromatic hydrocarbons

Petrochemical processes

Petrochemical processes, including reforming processes are described herein. The reforming processes generally include introducing an input stream to a reforming unit having a reforming catalyst disposed therein, wherein the input stream includes a naphtha having an N+2A value of from about 65 to about 85 and contacting the input stream with the reforming catalyst and hydrogen to form an output stream.

Reforming process with integrated fluid catalytic cracker gasoline and hydroprocessed cycle oil

A reforming process includes integrating catalytic cracking product naphtha dehydrogenation and naphtha from a hydrocracking zone and feeding them to a dehydrogenation zone. The dehydrogenation zone includes a first portion of reforming catalyst from a catalyst regenerator that moves downward through the dehydrogenation zone. A product stream from the dehydrogenation zone flows to an aromatics unit and is separated into an aromatic-rich extract and a raffinate. Straight run naphtha and the raffinate are introduced to a first reforming zone that includes a second portion of reforming catalyst. The reforming catalyst moves through the first reforming zone then is removed from the bottom of each of the first reforming zone and the dehydrogenation zone and is fed to a second reforming zone. An effluent from the first reforming zone is fed to a plurality of reforming zones. The reforming catalyst moves downward through the multiple refoiniing zones then to a regenerator.

Enhanced aromatics production by low pressure end point reduction and selective hydrogenation and hydrodealkylation

A reforming process includes an endpoint reduction zone for converting C 11+ components via selective hydrogenation and hydrodealkylation to lower boiling point aromatics, such as benzene, toluene, and xylene, or their single ring aromatic C 9 -C 10 precursors.

Method for producing monocyclic aromatic hydrocarbons

A method of producing monocyclic aromatic hydrocarbons includes bringing a light feedstock oil having a 10 vol % distillation temperature of 140° C. to 205° C. and a 90 vol % distillation temperature of 300° C. or lower, which has been prepared from a feedstock oil having a 10 vol % distillation temperature of 140° C. or higher and a 90 vol % distillation temperature of 380° C. or lower, into contact with a catalyst for monocyclic aromatic hydrocarbon production containing a crystalline aluminosilicate, in which a content ratio of monocyclic naphthenobenzenes in the light feedstock oil is adjusted by distillation of the feedstock oil such that the content ratio of monocyclic naphthenobenzenes in the light feedstock oil is higher than a content ratio of monocyclic naphthenobenzenes in the feedstock oil.

Aromatic recovery complex with a hydrodearylation step to process clay tower effluents

The disclosure provides a process to hydrodearylate the non-condensed alkyl-bridged multi-aromatics at the outlet of the clay tower where such multi-aromatics form rather than performing hydrodearylation on the reject stream of the aromatics complex. Hydrodearylation may feature combining a C8+ hydrocarbon stream from a clay treater with a hydrogen stream over a catalyst bed comprising a support and an acidic component optionally containing Group 8 and/or Group 6 metals.

THERMO-CATALYTIC CRACKING FOR CONVERSION OF HIGHER HYDROCARBONS INTO LOWER HYDROCARBONS

Described herein are processes and related devices and systems for the conversion of higher hydrocarbons, such as in the form of waste plastics, petroleum sludge, slope oil, vegetable oil, and so forth, into lower hydrocarbons, which can be used as fuels or raw materials for a variety of industrial and domestic uses. 120-. (canceled)21. A cracking device for converting higher hydrocarbons into lower hydrocarbons , comprising:a jacketed vessel including a top, a bottom, and an internal surface;a blade assembly housed in the jacketed vessel and including wiping blades adjacent to the internal surface of the jacketed vessel;and a motor connected to the blade assembly and configured to rotate the blade assembly, wherein the jacketed vessel is configured to receive a feedstock adjacent to the top of the jacketed vessel, and, upon rotation of the blade assembly, the wiping blades are configured to spread the feedstock to create a film of the feedstock adjacent to the internal surface of the jacketed vessel.22. The cracking device of claim 21 , wherein claim 21 , upon rotation of the blade assembly claim 21 , the wiping blades are configured to slide in a radial direction towards the internal surface of the jacketed vessel.23. The cracking device of claim 21 , wherein claim 21 , upon rotation of the blade assembly claim 21 , the wiping blades are configured to spread the feedstock in a generally upward direction.24. The cracking device of claim 23 , wherein at least one of the wiping blades includes a groove having a positive angular orientation relative to a horizontal plane.25. The cracking device of claim 21 , wherein the jacketed vessel further includes a coating adjacent to the internal surface of the jacketed vessel claim 21 , and the coating includes a set of catalysts to promote cracking of the feedstock.26. The cracking device of claim 21 , wherein the jacketed vessel is configured such that cracked feedstock is removed adjacent to the top of the jacketed vessel ...

Light alkanes to liquid fuels

The present disclosure relates generally processes and systems for converting a C2-C7 light alkanes feed to liquid transportation fuels or value-added chemicals. The feed is contacted with an aromatization catalyst at a temperature and pressure that selectively converts C4 and larger alkanes to an intermediate product comprising monocyclic aromatics and olefins. Following separation of the aromatics and C5+ hydrocarbons from the intermediate product, unconverted C2-C3 alkanes are thermally-cracked to produce olefins that are subsequently oligomerized to produce a liquid transportation fuel blend stock or value-added chemicals.

ISOMERIZATION AND CATALYTIC ACTIVATION OF PENTANE-ENRICHED HYDROCARBON MIXTURES

The present disclosure relates to processes that catalytically convert a hydrocarbon feed stream predominantly comprising both isopentane and n-pentane to yield upgraded hydrocarbon products that are suitable for use either as a blend component of liquid transportation fuels or as an intermediate in the production of other value-added chemicals. The hydrocarbon feed stream is isomerized in a first reaction zone to convert at least a portion of the n-pentane to isopentane, followed by catalytic-activation of the isomerization effluent in a second reaction zone with an activation catalyst to produce an activation effluent. The process increases the conversion of the hydrocarbon feed stream to olefins and aromatics, while minimizing the production of C1-C4 light paraffins. Certain embodiments provide for further upgrading of at least a portion of the activation effluent by either oligomerization or alkylation. 1. A method for converting a feed stream comprising pentanes to produce a liquid transportation fuel , comprising:a. providing a hydrocarbon feed stream comprising at least 50 wt. % pentanes, including both n-pentane and isopentane;b. contacting the hydrocarbon feed stream with one or more isomerization catalysts in a first reaction zone that is maintained at a temperature and a pressure that facilitates the isomerization of at least a portion of the n-pentane in the hydrocarbon feed stream to isopentane, thereby producing an isomerization effluent characterized by an increased ratio of isopentane to n-pentane relative to the hydrocarbon feed stream;c. contacting the isomerization effluent with an activation catalyst in a second reaction zone that is maintained at a temperature and pressure that facilitates at least one reaction selected from dehydrogenation, cracking and aromatization, thereby converting at least a portion of hydrocarbons present in the isomerization effluent to produce an activation effluent comprising olefins containing from two to five carbon ...

Process for providing aromatics from coal tar

A process for providing aromatics from a coal tar stream. A coal tar stream is provided, and the coal tar stream is fractionated into at least a naphtha range stream. The naphtha range stream is hydrotreated, and the hydrotreated naphtha range stream is separated to provide at least a naphthene rich stream. The naphthene rich stream is reformed or dehydrogenated to convert the naphthene. The dehydrogenated naphthene rich stream may be combined with a portion of a reformed crude oil hydrocarbon stream.

METHOD FOR PRODUCING A MIXTURE OF HYDROCARBONS

A method for producing a mixture hydrocarbons; a blend for producing a mixture of hydrocarbons; a mixture of hydrocarbons; and use of the mixture of hydrocarbons for producing chemicals and/or polymers. 1. A method for producing a mixture of hydrocarbons , the method comprising:(a) providing a renewable paraffin composition containing at least 75 wt-% isoparaffins;(b) combining fossil naphtha with the renewable paraffin composition to form a blend; and(c) thermally cracking the blend to produce a mixture of hydrocarbons.2. The method according to claim 1 , wherein the renewable paraffin composition contains at least 80 wt % isoparaffins.3. The method according to claim 1 , wherein the renewable paraffin composition contains at least 25 wt-% multiple branched isoparaffins.4. The method according to claim 1 , wherein the renewable paraffin composition contains at least 90 wt-% paraffins.5. The method according to claim 1 , wherein fossil naphtha is combined with the renewable paraffin composition such that the blend contains at least 1 wt % fossil naphtha claim 1 , a sum of wt-% amounts of the renewable paraffin composition and of the fossil naphtha in the blend being selected to contain at least 90 wt-% claim 1 , of a total weight of the blend.6. The method according to claim 1 , wherein fossil naphtha is combined with the renewable paraffin composition such that the blend contains at most 99 wt-% claim 1 , fossil naphtha.7. The method according to claim 1 , wherein the renewable paraffin composition and the fossil naphtha form one liquid phase above a pour point of the blend.8. The method according to claim 1 , wherein the thermally cracking is steam cracking.9. The method according to claim 1 , wherein providing a renewable paraffin composition comprises:(i) preparing a hydrocarbon raw material from a renewable feedstock; and(ii) subjecting at least straight chain hydrocarbons in the hydrocarbon raw material to an isomerization treatment to prepare the renewable ...

OLEFIN AND BTX PRODUCTION USING ALIPHATIC CRACKING AND DEALKYLATION REACTOR

A process and apparatus for making olefins and aromatics are described. The process includes reforming a naphtha stream in a reforming unit to produce a reformer effluent stream comprising aromatic compounds and aliphatic compounds, wherein at least a portion of the aromatic compounds contain alkyl groups. A cracking feed stream is taken from the reformer effluent stream, heated and passed to a cracking reactor. The aliphatic compounds are selectively cracked and at least a portion of the alkyl groups on the aromatic compounds are selectively dealkylated in the presence of a cracking catalyst to produce a cracked reformer effluent stream comprising aromatic compounds and cracked olefins. 1. A process for making aromatics and olefins comprising:reforming a naphtha stream in a reforming unit under reforming conditions to produce a reformer effluent stream comprising aromatic compounds and aliphatic compounds, wherein at least a portion of the aromatic compounds contain alkyl groups;taking a cracking feed stream from the reformer effluent stream;passing the cracking feed stream at a temperature of at least 500° C. to a cracking reactor comprising a cracking catalyst particles, more than 90 wt % of the cracking catalyst particles in the cracking reactor include a zeolite having a maximum pore diameter of greater than 5 Angstroms;selectively cracking the aliphatic compounds and selectively dealkylating the alkyl groups on the aromatic compounds in the presence of the cracking catalyst in the cracking reactor under cracking conditions to cracked olefins and aromatic compounds in a cracked reformer effluent stream.2. The process of wherein the cracked reformer effluent stream comprises a molar ratio of olefins to paraffins of at least 0.1.3. The process of wherein the zeolite comprises MFI zeolite.4. The process of wherein the zeolite comprises a silicalite catalyst having a zeolite silica to alumina molar ratio of greater than about 250.5. The process of further ...

Petrochemical Processes

Petrochemical processes, including reforming processes are described herein. The reforming processes generally include introducing an input stream to a reforming unit having a reforming catalyst disposed therein, wherein the input stream includes a naphtha having an N+2A value of from about 65 to about 85 and contacting the input stream with the reforming catalyst and hydrogen to form an output stream. 120-. (canceled)21. A petrochemical process comprising:introducing a first input stream to a cracking unit, wherein the first input stream comprises a naphtha feedstock;{'sub': '5', 'cracking the naphtha feedstock within the cracking unit to form a first output stream comprising light olefins and pygas, wherein the pygas comprises Chydrocarbons;'}{'sub': '5', 'passing the pygas comprising Chydrocarbons from the cracking unit to an extraction unit;'}{'sub': '5', 'separating benzene and toluene from the pygas comprising Chydrocarbons within the extraction unit;'}recovering a raffinate from the extraction unit;passing the raffinate from the extraction unit to a reforming unit having a reforming catalyst disposed therein;contacting the raffinate with the reforming catalyst to form a second output stream; andrecovering the second output stream from the reforming unit.22. The process of claim 21 , wherein the naphtha feedstock comprises a N+2A value of from about 40 to about 55.23. The process of claim 21 , wherein the cracking unit comprises a steam cracker.24. The process of claim 21 , further comprising hydrogenating the pygas comprising Chydrocarbons prior to extraction.25. The process of claim 21 , wherein the raffinate has a higher N+2A than the naphtha feedstock.26. The process of claim 21 , wherein the raffinate comprises a N+2A value of from about 75 to about 85.27. The process of claim 21 , wherein the reforming catalyst comprises a Group VIII noble metal.28. The process of claim 21 , wherein the reforming catalyst comprises a promoter selected from gallium claim ...

SIMPLIFIED FUELS REFINING

Systems and methods are provided for refining crude oils and/or other broad boiling range feedstocks to form fuels. A flash separation can be used to separate the feed into a lower boiling fraction and a higher boiling fraction. After the flash separation, the higher boiling portion is passed into a pyrolysis reactor for conversion of higher boiling compounds and formation of light olefins. The lower boiling fraction can be combined with the resulting pyrolysis effluent as a quench stream. The combined, partially pyrolyzed stream can then be passed into an olefin oligomerization process to convert the olefins formed during pyrolysis into naphtha and/or diesel boiling range compounds. After the olefin oligomerization process, one or more separations can be performed to generate various fractions, including but not limited to a naphtha fraction, a distillate fuel fraction, a fuel oil fraction, a light hydrocarbon recycle stream, and a CO-containing stream. Optionally, the naphtha fraction, the distillate fraction, and/or the fuel oil fraction can be hydrotreated. 1. A method for converting a feed into fuels fractions , comprising:performing a flash separation on a feedstock comprising hydrocarbons to form a lower boiling fraction and a higher boiling fraction, the lower boiling fraction comprising 10 wt % or more of the feedstock and a 343° C.− portion, the higher boiling fraction comprising 10 wt % or more of the feedstock and a 538° C.+ portion;{'sub': 2', '3, 'exposing the higher boiling fraction to fluidized bed pyrolysis conditions in a pyrolysis reactor to form a pyrolysis effluent comprising 20 wt % or more of C-Colefins;'}combining at least a portion of the pyrolysis effluent with the lower boiling fraction to form a combined effluent, a temperature of the combined effluent being lower than the pyrolysis effluent by 100° C. or more;exposing at least a portion of the combined effluent to a catalyst in an oligomerization zone under fluidized bed olefin ...

PROCESSES FOR AN IMPROVEMENT TO GASOLINE OCTANE FOR LONG-CHAIN PARAFFIN FEED STREAMS

Methods for making higher-octane fuel components from a feed stream of C8+ paraffins, including catalytically cracking the C8+ paraffins using a Zeolite catalyst to produce a reaction product of mid-chain paraffins and olefins and short-chain paraffins and olefins. The reaction product comprises liquid phase paraffins having an increased Octane Value over the feed stream paraffins. The reaction product further comprises a gas phase of short-chain paraffins which are separated from the liquid phase. In embodiments, the short chain olefins are hydrogenated to form mid-chain paraffins and a gas phase containing short-chain paraffins. 1catalytically cracking C8+ paraffins in the feed stream using a Zeolite catalyst under operating conditions suitable to substantially convert the C8+ paraffins to a reaction product comprising mid-chain paraffins and olefins and short-chain paraffins and olefins converted from the C8+ paraffins, the reaction product comprising a liquid phase containing product mid-chain paraffins and a gas phase containing product short-chain paraffins;the liquid phase paraffins having an Octane Value that is at least 1 Octane Value higher than the Octane Value of the paraffins in the feed stream; andseparating the liquid phase from the gas phase.. A method for making a higher-octane fuel component from a feed stream containing C8+ paraffins, comprising: Disclosed is a low-severity, catalytic reaction process applied selectively to long-chain paraffinic compounds, particularly n-paraffins, such as those present in traditional, catalytic reforming processes. The low-severity process, operated with or without hydrogen, converts targeted long-chain paraffins to higher-octane compounds ideal for gasoline blending, along with a byproduct of mixed light gases.Global demand for high-octane gasoline blendstocks continues to grow to support new higher-compression internal combustion engines. The presence of long-chain paraffin compounds (“LCPs”), particularly n- ...

Processes and systems for petrochemical production integrating deep hydrogenation of middle distillates obtained from gas oil hydroprocessing

Process scheme configurations are disclosed that enable deep hydrogenation of middle distillates. The hydrogenated middle distillates are processed in a steam cracker for conversion into light olefins. Feeds to the deep hydrogenation zone include diesel range streams from a diesel hydrotreating zone, a gas oil hydroprocessing zone, and/or a vacuum residue hydrocracking zone. The deep hydrogenation zone operates under conditions effective to reduce aromatic content in a diesel range feedstream from a range of about 10-40 wt % or greater, to a hydrogenated distillate range intermediate product having an aromatic content of less than about 5-0.5 wt %.

PROCESSES AND APPARATUSES FOR PRODUCTION OF OLEFINS

Processes and apparatuses for the production of olefins are provided. In an embodiment, a process for production of a process is provided for increasing light olefin yield comprising passing a hydrocarbon feedstream comprising paraffins, naphthenes and aromatic hydrocarbons to a catalytic reforming unit. The hydrocarbon feedstream is contacted with a reforming catalyst under mild reforming conditions suitable for converting naphthenes into aromatics while minimizing conversion of the paraffins, to provide a reforming effluent stream. The reforming effluent stream is passed to a solvent extraction unit to provide an overhead stream comprising predominantly paraffins and a bottoms stream comprising predominantly aromatics. Finally, the overhead stream is passed to a cracking unit to provide a product stream comprising the light olefins. 1. A process for increasing light olefin yield comprising:a) passing a hydrocarbon feedstream comprising paraffins, naphthenes and aromatic hydrocarbons to a catalytic reforming unit, the hydrocarbon feedstream being contacted with a reforming catalyst under mild reforming conditions suitable for converting naphthenes into aromatics while minimizing conversion of the paraffins, to provide a reforming effluent stream;b) passing the reforming effluent stream to a solvent extraction unit to provide an overhead stream comprising predominantly paraffins and a bottoms stream comprising predominantly aromatics; andc) passing the overhead stream to a cracking unit to provide a product stream comprising the light olefins.2. The process of claim 1 , wherein the hydrocarbon feedstream is a naphtha feedstream and the cracking unit is a catalytic naphtha cracker claim 1 , or a naphtha steam cracker.3. The process of claim 1 , wherein the mild reforming conditions comprise a temperature of about 300° C. to about 500° C.4. The process of claim 3 , wherein the mild reforming conditions comprise a temperature of about 400° C. to about 475° C.5. The ...

PROCESS FOR INCREASING THE CONCENTRATION OF NORMAL HYDROCARBONS IN A STREAM

A process increases the concentration of normal paraffins in a feed stream comprising separating a naphtha feed stream into a normal paraffin rich stream and a non-normal paraffin rich stream. The non-normal paraffin rich stream is isomerized over a first isomerization catalyst to convert non-normal paraffins to normal paraffins and produce a first isomerization effluent stream. An iso-C4 stream is separated from the first isomerization effluent stream and isomerized over a second isomerization catalyst to convert iso-C4 hydrocarbons to normal C4 hydrocarbons and produce a second isomerization effluent stream. The normal paraffin rich stream, the normal paraffins in the first isomerization effluent stream and/or the second isomerization effluent stream may be fed to a steam cracker. 1. A process for increasing the concentration of normal paraffins in a feed stream comprising:separating a naphtha feed stream into a normal paraffin rich stream and a non-normal paraffin rich stream;isomerizing the non-normal paraffin rich stream over a first isomerization catalyst to convert non-normal paraffins to normal paraffins and produce a first isomerization effluent stream;separating an iso-C4 stream from said first isomerization effluent stream;isomerizing said iso-C4 stream over a second isomerization catalyst to convert iso-C4 hydrocarbons to normal C4 hydrocarbons and produce a second isomerization effluent stream; andfeeding said second isomerization effluent stream to a steam cracker.2. The process of further comprising separating a C4 stream from said first isomerization effluent stream and separating said C4 stream into said iso-C4 stream and a normal C4 stream.3. The process of further comprising feeding said normal C4 stream to said steam cracker.4. The process of further comprising feeding said normal C4 stream to the step of separating a normal paraffins stream from non-normal paraffins stream and desorbing normal paraffins from an adsorbent.5. The process of ...

AROMATICS PRODUCTION PROCESS

Embodiments of the present disclosure include methods for producing aromatic products, the methods including separating a crude oil and condensate feed into at least a light naphtha stream, a heavy naphtha stream, and a bottoms stream, reforming at least a portion of the heavy naphtha stream to produce a reformate stream, feeding a cracker feed stream, comprising the light naphtha stream, the bottoms stream, and a reformate extraction raffinate, to an olefins cracker to produce cracker products comprising pyrolysis gasoline, and introducing an extractor feed stream comprising the pyrolysis gasoline and the reformate to an aromatic extraction unit to produce an aromatic product and the reformate extraction raffinate. 1. A method of producing aromatic products , the method comprisingseparating a crude oil and condensate feed into at least a light naphtha stream, a heavy naphtha stream, and a bottoms stream;reforming at least a portion of the heavy naphtha stream to produce a reformate stream;feeding a cracker feed stream, comprising the light naphtha stream, the bottoms stream, and a reformate extraction raffinate, to an olefins cracker to produce cracker products comprising pyrolysis gasoline; andintroducing an extractor feed stream comprising the pyrolysis gasoline and the reformate to an aromatic extraction unit to produce an aromatic product and the reformate extraction raffinate.2. The method of claim 1 , wherein the aromatic product is at least one aromatic compound selected from the group consisting of benzene claim 1 , toluene claim 1 , and xylene.3. The method of claim 1 , wherein the separating the crude oil and condensate feed comprises separating the crude oil and condensate feed in an atmospheric distillation unit.4. The method of claim 1 , wherein the separating the crude oil and condensate feed comprises separating the crude oil and condensate feed in a pyrolysis furnace.5. The method of claim 1 , further comprising mixing the pyrolysis gasoline with ...

INTEGRATION OF SIDE RISER FOR AROMATIZATION OF LIGHT PARAFFINS

Systems and methods are provided for conversion of light paraffinic gases to form liquid products in a two-stage reaction system. In a first stage, the light paraffinic gas is exposed to heat transfer particles in a side riser, where the heat transfer particles correspond to particles used in a separate process. Examples of a separate process include fluidized coking and fluid catalytic cracking. The conditions in the side riser can be selected to allow for conversion of at least a portion of the paraffins to olefins. After conversion, the converted olefin stream is passed to the second reaction stage while the heat transfer particles are returned to the separate process. The converted olefin stream is then exposed to a conversion catalyst under conditions for forming aromatics from the converted olefin stream in a second reaction stage. By performing the initial alkane conversion to olefins in the first reaction stage, the amount of coke formed during the aromatics formation process is reduced or minimized. 1. A method for processing a paraffin-containing feed , comprising:passing a first portion of heat transfer particles from a burner of a reaction system to a reactor of the reaction system;passing a second portion of heat transfer particles from the burner to a side riser;{'sub': '3+', 'exposing a feed comprising C paraffins to the second portion of heat transfer particles in the side riser under paraffin to olefin conversion conditions to form a side riser effluent comprising heat transfer particles including deposited coke and a gas phase effluent;'}separating a third portion of the heat transfer particles including deposited coke from the gas phase effluent;{'sub': 6', '12, 'exposing at least a portion of the gas phase effluent to one or more beds of a conversion catalyst to form an aromatic formation effluent comprising C-Caromatics;'}passing the third portion of the heat transfer particles into the reaction system;exposing a second feedstock to the first ...

INTEGRATED HYDROTHERMAL PROCESS TO UPGRADE HEAVY OIL

An integrated hydrothermal process for upgrading heavy oil includes the steps of mixing a heated water stream and a heated feed in a mixer to produce a mixed fluid, introducing the mixed stream to a reactor unit to produce a reactor effluent that includes light fractions, heavy fractions, and water, cooling the reactor effluent in a cooling device to produce a cooled fluid, depressurizing the cooled fluid in a depressurizing device to produce a depressurized fluid, introducing the depressurized fluid to a flash drum configured to separate the depressurized fluid into a light fraction stream and a heavy fraction stream. The light fraction stream includes the light fractions and water and the heavy fraction stream includes the heavy fractions and water. The process further includes the step of introducing the heavy fraction stream to an aqueous reforming unit that includes a catalyst to produce an aqueous reforming outlet. 1. An integrated hydrothermal process for upgrading heavy oil , the integrated hydrothermal process comprising the steps of:mixing a heated water stream and a heated feed in a mixer to produce a mixed fluid, wherein the heated water stream is supercritical water, wherein the heated feed is at a feedstock temperature less than 300 deg C. and a feedstock pressure greater than the critical pressure of water;introducing the mixed stream to a reactor unit to produce a reactor effluent;allowing conversion reactions to occur in the reactor unit, wherein the reactor unit is maintained at a temperature greater than the critical temperature of water and at a pressure greater than the critical pressure of water, wherein the conversion reactions are operable to upgrade the hydrocarbons in the mixed fluid such that the reactor effluent comprises light fractions, heavy fractions, and water;cooling the reactor effluent in a cooling device to produce a cooled fluid, where the cooled fluid is at a temperature less than the critical temperature of water and less than ...

Catalyst composite for the reduction of olefins in the fcc naphtha stream

The present disclosure relates to a catalyst composition comprising (a) at least one rare earth metal, (b) at least one zeolite, and (c) at least one diluent, wherein, said rare earth metal is impregnated in at least one of (b) and (c); the ratio of said zeolite to said diluent ranges from 1:9 to 9:1; and the amount of said rare earth metal is in the range of 0.1 to 20 w/w %. The present disclosure also relates to a process for preparing a catalyst composition. Further, the present disclosure relates to a process for reducing the olefin content in a hydrocarbon stream using the catalyst of the present disclosure.

PROCESS FOR PRODUCTION OF LIGHT OLEFINS AND BTX USING AN FCC UNIT PROCESSING A HEAVY FEEDSTOCK OF THE HIGHLY HYDROTREATED VGO TYPE, COUPLED WITH A CATALYTIC REFORMING UNIT AND AN AROMATIC COMPLEX PROCESSING A NAPHTHA-TYPE FEEDSTOCK

The present invention relates to the FCC units processing heavy feedstocks enriched with hydrogen, such as for example a highly hydrotreated VGO, or the unconverted part at the end of hydrocracking this same type of VGO feedstock, feedstocks which have the characteristic of cracking to light olefins such as ethylene and propylene. The integration of an FCC with an aromatic complex allows the recovery by the aromatic complex of the BTX formed in the FCC, and the recovery by the FCC from the flow at the bottom of the column, of heavy aromatics from the aromatic complex. 1. Process for the production of light olefins and BTX from a first feedstock of the hydrotreated VGO or unconverted oil (UCO) type resulting from hydrocracking , or from any mixture of these two feedstocks , and from a second naphtha-type feedstock with an initial boiling point greater than 30° C. and final boiling point less than 220° C. , said process comprising a catalytic cracking (FCC) unit processing the hydrotreated VGO feedstock or the unconverted oil , a catalytic reforming unit (REF) processing a feedstock referred to as naphtha (30° C.-220° C.) , and an aromatic complex (CA) fed by the catalytic reforming (REF) effluents and the fraction referred to as LCN (IP-160° C.) of the FCC effluents , said process comprising the following sequence of operations:{'b': 2', '6', '8, 'The hydrotreated VGO feedstock or the unconverted oil UCO () or any mixture of the two is sent into an FCC unit which produces effluents () which are sent into a fractionation (FRAC) unit, from which a light fraction (), an LCN cut (IP-160° C.), an HCN cut (160° C.-220° C.), and a heavy fraction (220° C.+) are extracted,'}{'b': '8', 'The light fraction () is sent into a separation box, referred to as a cold box (SBF), making it possible to separate the light olefins, ethylene and propylene, the dry gases (H2 and CH4), and the C2, C3 and C4 light paraffins,'}{'b': 9', '5', '10, 'The gasoline cut (IP-160° C.) referred to as ...

PROCESS FOR THE PRODUCTION OF LIGHT OLEFINS AND BTX USING A CATALYTIC CRACKING UNIT, NCC, PROCESSING A NAPHTHA TYPE FEED, A CATALYTIC REFORMING UNIT AND AN AROMATICS COMPLEX

The present invention concerns a process for the production of light olefins and BTX using a catalytic cracking unit, NCC, processing a naphtha type feed, and an aromatics complex. It can be used to exploit the synergies between these two units. The thermal balance of the NCC, which is intrinsically deficient in coke, is resolved by the optimal use of heat from the reforming furnaces in order to preheat the feed for the NCC, and by introducing at least a portion of the raffinate obtained from the aromatics complex as a mixture with the naphtha. 1. A process for the production of light olefins and BTX starting from a naphtha cut with an initial boiling point of more than 30° C. and a final boiling point of less than 220° C. , said process comprising a catalytic cracking unit (NCC) processing a light naphtha type feed (30-T° C.) , a catalytic reforming unit (REF) processing a feed termed a heavy naphtha (T° C.-220° C.) , and an aromatics complex (CA) supplied with effluents from catalytic reforming (REF) and the 60+ fraction of the NCC effluents , said process comprising the following series of operations:{'b': '1', 'sending the naphtha feed () with an initial boiling point of at least 30° C. and a final boiling point of at least 220° C. to a hydrotreatment unit (HDT) which can eliminate the sulphur-containing and nitrogen-containing compounds it contains;'}{'b': 2', '1, 'sub': M', 'M', 'M, 'sending the hydrotreated naphtha feed () to a separation unit (SPLIT) which can separate a light fraction termed light naphtha, with a distillation range of 40° C.-T° C., and a heavy fraction termed heavy naphtha with a distillation range of T° C.-220° C., in which T° C. is in the range 80° C. to 160° C., preferably in the range 100° C. to 150° C., and highly preferably in the range 110° C. to 140° C.;'}{'b': '3', 'sending the light naphtha () to the NCC as a feed;'}{'b': '4', 'sending the heavy naphtha () as a feed for the catalytic reforming unit (REF);'}{'b': 6', '8, 'sub': 2', ...

Process and System for Processing Petroleum Feed

A novel process/system for flexibly producing chemicals and fuels from a petroleum feed such as crude comprise a flashing drum, a first cracker (e.g., a fluidized bed pyrolysis cracker or an oxidative cracker), and an olefin-to-gasoline reaction zone. The process/system can also include a steam cracker and a hydrotreater. The process/system can convert crude oil into hydrogen, C2-C4 olefins, gas oil and distillates with various amounts by adjusting the cut point of the bottoms effluent exiting the flashing drum. 1. A process for processing a petroleum feed to produce a plurality of hydrocarbon products , the process comprising:(I) feeding the petroleum feed to a flashing drum;(II) obtaining a liquid bottoms effluent comprising bottoms hydrocarbons and a vapor overhead effluent comprising overhead hydrocarbons from the flashing drum, wherein the bottoms hydrocarbons optionally comprise a non-volatile component;(III) feeding at least a portion of the bottoms effluent to a first cracker through a first inlet on the first cracker;(IV) converting at least a portion of the bottoms hydrocarbons under a first set of cracking conditions in the first cracker to produce a first cracker product mixture comprising olefins;(V) feeding at least a portion of the first cracker product mixture into an olefin-to-gasoline (“OTG”) reaction zone;(VI) converting at least a portion of the first cracker product mixture into gasoline in the presence of an OTG catalyst in the OTG reaction zone; and(VII) obtaining an OTG product mixture from the OTG reaction zone.2. The process of claim 1 , wherein the flashing drum is operated at a cutpoint of the liquid bottoms effluent in the range from 371 to 482° C. (700 to 900° F.) at an absolute pressure in the range from 280 to 1850 kilopascal.3. The process of claim 1 , wherein the first set of cracking conditions comprise a residence time in the first cracker of no greater than 1 second claim 1 , preferably no greater than 0.4 second.4. The process ...

FLOW CONFIGURATIONS USING A NORMAL PARAFFIN SEPARATION UNIT WITH ISOMERIZATION IN THE REFORMING UNIT

A process is presented for recovering the hydrocarbon components from a naphtha feed to pass to a gasoline blending pool or to change the operations to increase the production of light olefins. The process includes the separation of the naphtha feedstock into a light naphtha stream and a heavy naphtha stream. The process further includes separating the light naphtha stream to recovery high quality non-normal hydrocarbons, and to separate normal hydrocarbons to the feed to the cracking unit. 1. A process for increasing light olefin yields from naphtha , comprising:passing a naphtha feedstream to a naphtha splitter to generate a light naphtha stream and a heavy naphtha stream, wherein the naphtha splitter is operated to split the naphtha stream around the normal boiling point of methylcyclopentane;passing the heavy naphtha stream to a reforming unit to generate a reformer effluent comprising aromatics;passing the light naphtha stream to a separation unit to generate an extract stream comprising normal hydrocarbons and a raffinate stream comprising non-normal hydrocarbons; andpassing the extract stream to a cracking unit.2. The process of wherein the naphtha splitter is operated increasing the temperature to split the naphtha stream around the normal boiling point of cyclohexane.3. The process of wherein the naphtha splitter is operated increasing the temperature to split the naphtha stream around the normal boiling point of dimethylpentane.4. The process of further comprising:passing the reformer effluent to an aromatics recovery unit to generate an aromatics stream and a recovery unit aromatics raffinate stream.5. The process of further comprising passing the recovery unit raffinate stream to the separation unit.6. The process of wherein the separation unit is an adsorption separation unit.7. The process of wherein the adsorption separation unit uses a light desorbent.8. The process of wherein the light desorbent is n-butane or n-pentane.9. The process of further ...

INTEGRATED HYDROTHERMAL PROCESS TO UPGRADE HEAVY OIL

An integrated hydrothermal process for upgrading heavy oil includes the steps of mixing a heated water stream and a heated feed in a mixer to produce a mixed fluid, introducing the mixed stream to a reactor unit to produce a reactor effluent that includes light fractions, heavy fractions, and water, cooling the reactor effluent in a cooling device to produce a cooled fluid, depressurizing the cooled fluid in a depressurizing device to produce a depressurized fluid, introducing the depressurized fluid to a flash drum configured to separate the depressurized fluid into a light fraction stream and a heavy fraction stream. The light fraction stream includes the light fractions and water and the heavy fraction stream includes the heavy fractions and water. The process further includes the step of introducing the heavy fraction stream to an aqueous reforming unit that includes a catalyst to produce an aqueous reforming outlet. 1. An integrated hydrothermal process for upgrading heavy oil , the integrated hydrothermal process comprising the steps of:mixing a heated water stream and a heated feed in a mixer to produce a mixed fluid, wherein the heated water stream is supercritical water, wherein the heated feed is at a feedstock temperature less than 300 deg C. and a feedstock pressure greater than the critical pressure of water;introducing the mixed stream to a reactor unit to produce a reactor effluent;allowing conversion reactions to occur in the reactor unit, wherein the reactor unit is maintained at a temperature greater than the critical temperature of water and at a pressure greater than the critical pressure of water, wherein the conversion reactions are operable to upgrade the hydrocarbons in the mixed fluid such that the reactor effluent comprises light fractions, heavy fractions, and water;cooling the reactor effluent in a cooling device to produce a cooled fluid, where the cooled fluid is at a temperature less than the critical temperature of water and less than ...

PROCESS TO PRODUCE OLEFINS FROM A CATALYTICALLY CRACKED HYDROCARBONS STREAM

Processes to produce olefins from a hydrocarbons stream obtained from a catalytic cracking unit are described. The process includes the integration of metathesis of Colefin process and a hydrocarbon catalytically cracking process to produce commercially valuable products (for example, Colefins and a C gasoline hydrocarbons). 1. A process for producing olefins , the process comprising:{'sub': 5', '6', '5', '1', '4, '(a) catalytically cracking a hydrocarbons stream comprising Cand Chydrocarbons under conditions sufficient to form a cracked hydrocarbons stream comprising C+ gasoline hydrocarbons, and gaseous Cto Chydrocarbons;'}{'sub': 5', '1', '4', '5, '(b) fractionating the first stream to produce at least (1) a first stream comprising C+ gasoline hydrocarbons, and (2) a gaseous stream comprising the Cto Chydrocarbons and residual C+ hydrocarbons;'}{'sub': 4', '3', '5, '(c) separating the gaseous stream into a gaseous mixed Chydrocarbons stream comprising n-butene and iso-butene, a gaseous Chydrocarbons stream, and a C+ gasoline hydrocarbons stream;'}{'sub': 4', '5, '(d) contacting the mixed Cgaseous stream with a metathesis catalyst under conditions sufficient to produce a second gaseous stream comprising methane, ethylene and/or propylene, and a product stream comprising C+ gasoline hydrocarbons; and'}(e) mixing the step (d) second gaseous stream with the step (c) gaseous stream.2. The process of claim 1 , further comprising mixing the C+ gasoline hydrocarbons product stream with the C+ gasoline hydrocarbons stream.3. The process of claim 1 , wherein separating the gaseous stream of step (c) comprises(i) producing a gaseous product stream comprising C1 and C2 hydrocarbons and a gaseous C3+ hydrocarbons stream comprising the gaseous mixed C4 hydrocarbons, the gaseous C3 hydrocarbons, and the residual C5+ gasoline hydrocarbons; and(ii) separating the gaseous C3+ hydrocarbons stream into a gaseous C3 hydrocarbons stream, a gaseous mixed C4 hydrocarbons stream ...

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 Purification of Raffinate-2 streams

본 발명은 라피네이트-2 스트림으로부터 1-부텐을 고순도 고수율로 분리 정제하는 방법에 관한 것으로서, 이중효과 증류에 의해 에너지 회수량을 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 provides a method for recovering 1-butene in high purity and high yield while maximizing the amount of energy recovery by double-effect distillation. to provide.

丙烯和芳香族烃的制造方法以及其制造装置

本发明的目的在于，提供在使用含有中间细孔径沸石的催化剂，从含有碳原子数4～12的烯烃的烃原料来制造丙烯和芳香族烃的方法中，可以简单的方法改变两个成分的产量结构、并且可有效且稳定地制造的、经改良的工序。采用本发明，公开了一种制造方法，其由如下工序构成：使用特定的沸石催化剂，从反应混合物中取出碳原子数4以上的烃成分，根据需要将其一部分直接循环的丙烯制造工序；将该碳原子数4以上的烃成分作为原料的一部分或全部的芳香族烃制造工序。

Process for production of propylene and aromatic hydrocarbon, and apparatus for the process

본 발명은, 중간세공 직경 제올라이트 함유 촉매를 사용하여, 탄소수 4∼12의 올레핀을 함유하는 탄화수소 원료로 프로필렌 및 방향족 탄화수소를 제조하는 방법에 있어서, 두 성분의 수율 구조를 간편한 방법으로 변경할 수 있고, 효율적이고 안정적으로 제조할 수 있는, 개량된 프로세스를 제공하는 것을 목적으로 한다. 본 발명에 의하면, 특정 제올라이트 촉매를 사용하여 반응 혼합물로부터 탄소수 4 이상의 탄화수소 성분을 추출하고, 필요에 따라 상기 일부를 그대로 재순환하는 프로필렌 제조 공정과, 상기 탄소수 4 이상의 탄화수소 성분을 원료의 일부 또는 전부로 하는 방향족 탄화수소 제조 공정으로 구성되는 제조 방법을 개시한다. According to the present invention, in the process for producing propylene and aromatic hydrocarbon from a hydrocarbon raw material containing an olefin having 4 to 12 carbon atoms using a mesoporous diameter zeolite-containing catalyst, the yield structure of the two components can be changed by a simple method, It is an object of the present invention to provide an improved process that can be efficiently and stably manufactured. According to the present invention, a propylene production step of extracting a hydrocarbon component having 4 or more carbon atoms from a reaction mixture using a specific zeolite catalyst and recycling the portion as it is, and the hydrocarbon component having 4 or more carbon atoms as part or all of the raw materials Disclosed is a production method comprising an aromatic hydrocarbon production process.

生产芳烃和烯烃的方法

本公开的主题提供了由焦化石脑油产生烯烃和/或芳烃的方法。在非限制性实施方案中，用于产生芳烃的方法包括在第一催化剂的存在下氢化焦化石脑油流以除去二烯烃和硫(如果存在)，以获得氢化流，并在第二催化剂的存在下使氢化流经历芳构化，以产生包含苯、甲苯和二甲苯的富含芳烃的流。在某些实施方案中，用于产生烯烃的方法包括在第一催化剂的存在下氢化焦化石脑油流以除去二烯烃和硫(如果存在)，以获得氢化流，并在第二催化剂的存在下使氢化流经历催化裂化，以产生包含乙烯、丙烯和芳烃的富含烯烃的流。

Monocyclic aromatic hydrocarbon production method

精炼萃余液-2的方法

本发明涉及一种用于从萃余液‑2流中以高纯度和高产率分离和精炼1‑丁烯的方法，该方法包括如下步骤：将含有正丁烷、异丁烷和1‑丁烯的萃余液‑2供给到第一蒸馏塔，以从第一蒸馏塔的下部获得含有正丁烷的重质萃余液‑3并且从第一蒸馏塔的上部回收含有1‑丁烯的上部馏分；以及将含有1‑丁烯的上部馏分供给到第二蒸馏塔，以从第二蒸馏塔的下部回收富含1‑丁烯的第一下部馏分并且从第二蒸馏塔的上部回收含有异丁烯的轻质萃余液‑3，其中，从第一蒸馏塔的上部回收的上部馏分的热通过第一热交换器供给到第二蒸馏塔的下部，因此能够以高纯度和高产率回收1‑丁烯，同时通过双效蒸馏使能量回收量最大化。

method for the production of aromatic hydrocarbons

Method for producing a mixture of hydrocarbons

A method for producing a mixture hydrocarbons; a blend for producing a mixture of hydrocarbons; a mixture of hydrocarbons; and use of the mixture of hydrocarbons for producing chemicals and/or polymers.

A method for producing a mixture of hydrocarbons

A method for producing a mixture hydrocarbons; a blend for producing a mixture of hydrocarbons; a mixture of hydrocarbons; and use of the mixture of hydrocarbons for producing chemicals and/or polymers.

Catalyst system and process for conversion of hydrocarbon feed using the catalyst system

본 발명은 i. 탄화수소 전환 촉매의 제 1 층으로서, 상기 탄화수소 전환 촉매는, 고체 지지체 상에 탈수소화 활성 금속을 포함하는 제 1 조성물; 및 무기 지지체 상에 전이 금속을 포함하는 제 2 조성물;을 포함하는 제 1 층; ii. 분해 촉매(cracking catalyst)를 포함하는 제 2 층을 포함하는 촉매 시스템 및 이 촉매 시스템을 이용한 탄화수소 공급물의 전환 공정에 관한 것이다. The present invention provides i. A first layer of a hydrocarbon conversion catalyst, the hydrocarbon conversion catalyst comprising: a first composition comprising a dehydrogenation active metal on a solid support; and a second composition comprising a transition metal on the inorganic support; a first layer comprising; ii. A catalyst system comprising a second bed comprising a cracking catalyst and a process for converting a hydrocarbon feed using the catalyst system.

Conversion of heavy fuel oil to chemical products

고유황 연료유를 석유화학제품으로 전환하기 위한 시스템 및 공정으로서, 분해된 연료유 유출액을 형성하기 위하여 연료유 수소첨가분해기에서 상기 고유황 연료유를 수소첨가분해하는 단계를 포함하고, 이 때 경질 분획 및 중질 분획으로 분리될 수 있다. 상기 중질 분획은 합성가스를 생성하기 위하여 기화될 수 있고, 상기 합성가스 또는 상기 합성가스로부터 회수된 수소는 상기 연료유 수소첨가분해기로 공급될 수 있다. 상기 경질 분획은 증류액 수소첨가분해기에서 수소첨가분해되어 분해된 유출액을 형성할 수 있고, 이 때 수소 분획, 경질 탄화수소 분획, 경질 나프타 분획, 및 중질 나프타 분획으로 분리될 수 있다. 상기 중질 나프타 분획은 개질되어 수소, 그리고 벤젠, 톨루엔, 및 자일렌 중 적어도 하나를 생성할 수 있다. 상기 경질 탄화수소 분획 및/또는 상기 경질 나프타 분획은 증기 분해되어 에틸렌, 프로필렌, 벤젠, 톨루엔, 및 자일렌 중 적어도 하나를 생성할 수 있다. A system and process for converting high sulfur fuel oil into petrochemicals, comprising hydrocracking the high sulfur fuel oil in a fuel oil hydrocracker to form a cracked fuel oil effluent, wherein the light It can be separated into a fraction and a heavy fraction. The heavy fraction may be vaporized to produce syngas, and the syngas or hydrogen recovered from the syngas may be supplied to the fuel oil hydrocracker. The light fraction may be hydrocracked in a distillate hydrocracker to form a cracked effluent, which may be separated into a hydrogen fraction, a light hydrocarbon fraction, a light naphtha fraction, and a heavy naphtha fraction. The heavy naphtha fraction may be reformed to produce hydrogen and at least one of benzene, toluene, and xylene. The light hydrocarbon fraction and/or the light naphtha fraction may be steam cracked to produce at least one of ethylene, propylene, benzene, toluene, and xylene.

Aromatic hydrocarbon production process

본 방향족 탄화수소의 제조 방법에서는 에틸렌 제조 장치로부터 얻어지는 열분해 중질유의 수소화 처리유를 포함하는 원료유를, 결정성 알루미노실리케이트를 포함하는 단환 방향족 탄화수소 제조용 촉매와 접촉시켜 방향족 탄화수소를 제조하는 방향족 탄화수소의 제조 방법이다. 원료유로서 증류 성상의 종점이 400℃ 이하인 것을 이용한다. 원료유와 단환 방향족 탄화수소 제조용 촉매의 접촉을 0.1MPaG 내지 1.5MPaG의 압력하에서 행한다.

Process for production of light olefins and btx

本发明涉及处理富含氢的重质原料的FCC单元，所述重质原料例如像高度加氢处理的VGO，或在加氢裂化该相同类型的VGO原料结束时未转化的部分，原料具有裂化至轻质烯烃(例如乙烯和丙烯)的特性。FCC与芳族联合装置集成允许通过芳族联合装置回收在FCC中形成的BTX，并且通过FCC从塔底部的流回收来自芳族联合装置的重质芳族物质。

A process for catalytically reforming naphtha

In the present invention, naphtha is contacted with a reforming catalyst under a condition of a pressure of 0.15 to 3.0 MPa, a temperature of 300 to 540 캜 and a volumetric space velocity of 2.1 to 50 h -1 in the presence of hydrogen gas to perform a shallow catalytic reforming reaction by high conversion rate and naphthenes, less than 30% by weight paraffins and C 4 of the arene than 85 mass%, discloses a catalyst system for reforming naphtha way to achieve conversion of a hydrocarbon. The process can be used to maximize the production of paraffins from the production of arenes from naphtha, so that the naphtha can be made into a feedstock for the production of a good quality ethylene cracker as well as the production of arene.

The system and method related to synthesis gas olefin process

本文公开了一种能够由产物流产生苯的系统和方法。

A method for producing a mixture of hydrocarbons

A method for producing a mixture hydrocarbons; a blend for producing a mixture of hydrocarbons; a mixture of hydrocarbons; and use of the mixture of hydrocarbons for producing chemicals and/or polymers.

Processes for an improvement to gasoline octane for long-chain paraffin feed streams

Method for making higher-octane fuel components from a feed stream of C8+ paraffins, including catalytically cracking the C8+ paraffins using a Zeolite catalyst to produce a reaction product of mid-chain paraffins and olefins and short-chain paraffins and olefins. The reaction product comprises liquid phase paraffins having an increased Octane Value over the feed stream paraffins. The reaction product further comprises a gas phase of short-chain paraffins which are separated from the liquid phase. In embodiments, the short chain olefins are hydrogenated to form mid-chain paraffins and a gas phase containing short chain paraffins.

Process for production of light olefins and BTX using an FCC unit processing a heavy feedstock of the highly hydrotreated VGO type, coupled with a catalytic reforming unit and an aromatic complex processing a naphtha-type feedstock

The present invention relates to the FCC units processing heavy feedstocks enriched with hydrogen, such as for example a highly hydrotreated VGO, or the unconverted part at the end of hydrocracking this same type of VGO feedstock, feedstocks which have the characteristic of cracking to light olefins such as ethylene and propylene. The integration of an FCC with an aromatic complex allows the recovery by the aromatic complex of the BTX formed in the FCC, and the recovery by the FCC from the flow at the bottom of the column, of heavy aromatics from the aromatic complex.

PROCESS FOR CONVERTING A HEAVY FUEL AND PROPYLENE LOAD HAVING A MODULATE YIELD STRUCTURE

La présente invention décrit un procédé de conversion d'une charge lourde présentant une grande flexibilité sur la production de propylène et d'essence. Le procédé fait appel à une unité de craquage catalytique suivie d'une unité d'oligomérisation des oléfines en C3/4, C4, ou C4/C5 selon la production choisie. Le procédé selon l'invention couvre les cas où le craquage catalytique est effectué dans un seul réacteur ou deux réacteurs distincts, chaque réacteur pouvant fonctionner en écoulement ascendant ou descendant. En option, une unité d'hydrogénation des coupes oléfiniques peut être placée en amont de l'unité d'oligomérisation. The present invention describes a method of converting a heavy load having a high flexibility on the production of propylene and gasoline. The process uses a catalytic cracking unit followed by an oligomerization unit of C3 / 4, C4 or C4 / C5 olefins depending on the production chosen. The process according to the invention covers the cases where the catalytic cracking is carried out in a single reactor or two separate reactors, each reactor being able to operate in upward or downward flow. Optionally, a hydrogenation unit of the olefinic cuts can be placed upstream of the oligomerization unit.

Process for producing aromatic hydrocarbons

PROCESS FOR CONVERTING A HEAVY FUEL AND PROPYLENE LOAD HAVING A MODULATE YIELD STRUCTURE

Integrated process for producing benzene and xylenes from heavy aromatics

本发明提供了用于最大程度地由重质重整油产生苯和对二甲苯的系统和工艺。一体化工艺和系统可包括C9脱烷基化反应器、烷基转移反应器和C10+脱烷基化反应器。用于产生苯和对二甲苯的一体化工艺和系统可配置成当存在氢气时另外产生烷烃，或者当不存在氢气时另外产生烯烃。烷基转移反应器可进行来自C9脱烷基化反应器的产物的烷基转移以及二甲苯异构化。

Catalyst system and process for converting hydrocarbon feedstock using the same

本发明涉及一种催化剂体系和使用这种催化剂体系转化烃进料的方法，该催化剂体系包含：i.烃转化催化剂的第一层，烃转化催化剂包含：第一组合物，其包含固体载体上的铂族金属；和第二组合物，其包含无机载体上的过渡金属；ii.包含裂化催化剂的第二层。

Aromatic hydrocarbon production process

本发明的芳香族烃的制造方法是使含有由乙烯制造装置得到的热裂化重质油的加氢处理油的原料油与含有结晶性铝硅酸盐的单环芳香族烃制造用催化剂接触来制造芳香族烃的芳香族烃的制造方法。使用蒸馏性质的终点为400℃以下的原料油作为原料油。在0.1MPaG～1.5MPaG的压力下进行原料油与单环芳香族烃制造用催化剂的接触。

Process to produce olefins from a catalytically cracked hydrocarbons stream

Processes to produce olefins from a hydrocarbons stream obtained from a catalytic cracking unit are described. The process includes the integration of metathesis of C 4 olefin process and a hydrocarbon catalytically cracking process to produce commercially valuable products (for example, C 2-3 olefins and a C 5+ gasoline hydrocarbons).

Process and system for 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 catalytic conversion to produce additional gasoline and higher-quality aromatic compounds.

Integrated process for maximizing recovery of hydrogen

An integrated process for maximizing recovery of hydrogen is provided. The process comprises: providing a hydrocarbonaceous feed comprising naphtha, and a hydrogen stream to a reforming zone, wherein the hydrogen stream is obtained from at least one of a hydrocracking zone, a transalkylation zone, and an isomerization zone. The hydrocarbonaceous feed is reformed in the reforming zone in the presence of the hydrogen stream and a reforming catalyst to provide a reformate effluent stream. At least a portion of the reformate effluent stream is passed to a debutanizer column of the reforming zone to provide a net hydrogen stream and a fraction comprising liquid petroleum gas (LPG). At least a portion of the net hydrogen stream is recycled to the reforming zone as the hydrogen stream.

Enhanced aromatics production by low pressure end point reduction and selective hydrogenation and hydrodealkylation

A reforming process includes an endpoint reduction zone for converting C 11+ components via selective hydrogenation and hydrodealkylation to lower boiling point aromatics, such as benzene, toluene, and xylene, or their single ring aromatic C 9 -C 10 precursors.

Iso-olefin production and etherification process

A process for increasing iso-butylene and iso-pentene yield from a refinery naptha comprising contacting a olefinic naptha stream comprising C₅-C₉ olefins with a low acidic crystalline silicate catalyst at a pressure of less than 300 psig and a temperature of between about 500 to about 900 F to produce a product stream rich in iso-butylene and iso-pentene.

The system and method related to synthesis gas olefin process

本文公开了一种能由产物流产生丁二烯的系统和方法。

Olefin and single-ring aromatic hydrocarbon production method, and ethylene production device

본 발명의 올레핀 및 단환 방향족 탄화수소의 제조 방법은, 분해로와, 분해로의 분해 생성물로부터 올레핀, 단환 방향족 탄화수소를 분리 회수하는 생성물 회수 장치를 구비한 에틸렌 제조 장치로부터 얻어지는 열분해 중질유이면서 또한 증류 성상의 90용량％ 유출 온도가 390℃ 이하인 원료유를 촉매와 접촉, 반응시켜서, 올레핀, 단환 방향족 탄화수소를 포함하는 생성물을 얻는 분해 개질 반응 공정과, 분해 개질 반응 공정에서 얻어진 생성물을 에틸렌 제조 장치의 생성물 회수 장치로 처리함으로써, 올레핀, 단환 방향족 탄화수소를 각각 회수하는 생성물 회수 공정을 갖는다.

Integrated process for maximizing hydrogen recovery

本发明提供了一种用于使氢的回收最大化的整合方法。该方法包括：向重整区提供包含石脑油的含烃进料以及氢料流，其中氢料流从氢化裂解区、烷基转移区和异构化区中的至少一个获得。在氢料流和重整催化剂的存在下在重整区中重整含烃进料，以提供重整产品流出物料流。将重整产品流出物料流的至少一部分传递到重整区的脱丁烷塔，以提供净氢料流和包含液化石油气(LPG)的馏分。将净氢料流的至少一部分作为氢料流再循环到重整区。

Enhanced aromatics production by low pressure end point reduction and selective hydrogenation and hydrodealkylation

A reforming process includes an endpoint reduction zone for converting C 11+ components via selective hydrogenation and hydrodealkylation to lower boiling point aromatics, such as benzene, toluene, and xylene, or their single ring aromatic C 9 -C 10 precursors.

Process for the catalytic treatment of hydrocarbons

Synthetic hydrocarbon products

The invention includes a process for producing synthetic middle distillates and synthetic middle distillates produced therefrom. In one embodiment, the process comprises fractionating a hydrocarbon synthesis product to at least generate a light middle distillate, a heavy middle distillate, and a waxy fraction; thermally cracking the waxy fraction; and isomerizing the heavy middle distillate. A synthetic diesel or blending component is formed by the combination of at least a portion of the light middle distillate; at least a portion or fraction of the thermally cracked product; and at least a portion or fraction of the isomerized product. In some embodiments, the hydrocarbon synthesis product and/or the thermally cracked product may be hydrotreated. In other embodiments, a synthetic middle distillate comprises at least two fractions: a light fraction with not more than 10% branched hydrocarbons, and a heavy fraction with at least 30% branched hydrocarbons.

Isomerization and catalytic activation of pentane-enriched hydrocarbon mixtures

The present disclosure relates to processes that catalytically convert a hydrocarbon feed stream predominantly comprising both isopentane and n-pentane to yield upgraded hydrocarbon products that are suitable for use either as a blend component of liquid transportation fuels or as an intermediate in the production of other value-added chemicals. The hydrocarbon feed stream is isomerized in a first reaction zone to convert at least a portion of the n-pentane to isopentane, followed by catalytic-activation of the isomerization effluent in a second reaction zone with an activation catalyst to produce an activation effluent. The process increases the conversion of the hydrocarbon feed stream to olefins and aromatics, while minimizing the production of C1-C4 light paraffins. Certain embodiments provide for further upgrading of at least a portion of the activation effluent by either oligomerization or alkylation.

Process for the production of high-octane gasoline

Pyrolysis of plastic waste to produce light gaseous hydrocarbons and integration with an ethylene cracker

Processes for using pyrolysis gas as a feedstock or a co-feedstock for making a variety of chemicals, for example, circular ethylene, circular ethylene polymers and copolymers, and other circular products. In these processes, pyrolysis reactor conditions can be selected to increase or optimized the production of pyrolysis gas over pyrolysis oil, and the pyrolysis gas which is usually used as fuel or flared can be fed downstream of the steam cracker furnace for economic use to form circular chemicals. Operating parameters of the pyrolysis unit may be adjusted to increase or decrease the proportion of pyrolysis gas relative to pyrolysis liquid as a function of their relative economic values.

Olefin and single-ring aromatic hydrocarbon production method, and ethylene production device

A method for producing an olefin and a monocyclic aromatic hydrocarbon of the present invention includes a cracking and reforming reaction step of obtaining a product containing an olefin and a monocyclic aromatic hydrocarbon by bringing a feedstock oil which is a thermally-cracked heavy oil obtained from an apparatus for producing ethylene which includes a cracking furnace and a product collection device that separates and collects an olefin and an aromatic hydrocarbon from a cracked product produced in the cracking furnace and which has a 90 volume% distillate temperature, as a distillation characteristic, of 390°C or lower into contact with a catalyst and reacting the feedstock oil; and a product collection step of collecting the olefin and the monocyclic aromatic hydrocarbon respectively by treating the product obtained in the cracking and reforming reaction step using the product collection device in the apparatus for producing ethylene.

Method for purifying raffinate-2

The present invention relates to a method for separating and purifying 1-butene from raffinate-2 stream at high purity and a high yield, the method comprising the steps of: supplying raffinate-2 including n-butane, isobutane and 1-butene to a first distillation column to obtain heavy raffinate-3 including n-butane from the lower part of the first distillation column and recovering an upper fraction including 1-butene from the upper part thereof; and supplying the upper fraction including 1-butene into a second distillation column to recover a first lower fraction, enriched with 1-butene, from the lower part of the second column and recovering light raffinate-3 including isobutene from the upper part thereof, wherein the heat of the upper fraction recovered from the upper part of the first distillation column is supplied to the lower part of the second distillation column through a first heat exchanger, and 1-butene at high purity and high yield can be recovered while an energy recovery amount is maximized by means of a double effect distillation.

Method for vaporizing liquid propane and vaporizer for use in the method

本发明提供一种使作为原料供应至石脑油裂化反应器的液态丙烷汽化的方法。所述方法可以将液态丙烷的压力降低至比现有技术方法显著更低的压力，使得液态丙烷中包含的各个汽化潜热或汽化热可以用作制冷剂，并且还可以减少在供应至石脑油裂化反应器之前的预热工艺中消耗的热能。

Treatment system and treatment method for gasoline component

本发明提供一种汽油组分的处理系统和处理方法，该系统包括：(1)芳构化单元(A)，用于汽油组分原料进行反应和分离，获得C 4 ‑ 组分，C 5 组分，C 6 ‑C 7 组分，C 8 组分及C 9 + 组分；(2)裂解与芳烃转化单元(B)，用于C 6 ‑C 7 组分及C 9 + 组分进行芳烃转化和分离，获得C 4 ‑ 组分，C 5 组分，C 6 ‑C 7 组分，C 8 组分及C 9 + 组分；(3)芳烃提纯单元(C)，用于C 8 组分提纯，分离出C 4 ‑ 组分，C 5 组分，C 6 + 组分和高纯C8芳烃；(4)蒸汽裂解单元(D)，用于C 4 ‑ 组分进行烯烃裂解；(5)轻质汽油调和单元(E)，用于C 5 组分进行汽油调和。本发明可有效将混合烃类组分(如催化汽油组分、LPG)定向转化为碳八芳烃，并副产低碳烯烃及高品质轻质汽油，实现高效的综合利用。

Producing C6-C8 aromatics from FCC heavy naphtha

A method of forming C 6 -C 8 aromatics may include selectively dealkylating a Fluid Catalytic Cracking (FCC) heavy cut naphtha that has at least C 9+ aromatics to selectively crack C 2+ alkyl chains from the C 9+ aromatics, thereby forming the C 6 -C 8 aromatics. The selectively de-alkylated heavy cut naphtha is then combined with a FCC middle cut naphtha, and aromatics including the C 6 -C 8 aromatics are separated from the combined stream. A system for forming C 6 -C 8 aromatics may include a fluid catalytic cracking unit for producing a FCC heavy cut naphtha comprising at least C 9+ aromatics; a de-alkylation reactor for selectively cracking C 2+ alkyl chains from the C 9+ aromatics, thereby forming the C 6 -C 8 aromatics; and an aromatic extraction unit for extracting at least a portion of the C 6 -C 8 aromatics.

Method for vaporizing liquid propane and vaporizing apparatus used therefor

The present invention relates to a method for vaporizing liquid propane to supply liquid propane to a naphtha cracking reactor as a raw material. The method can reduce pressure of liquid propane to a much lower pressure than a conventional method, and thus can not only utilize all the evaporation latent heat or vaporization heat included in liquid propane as a refrigerant but also can reduce heat energy consumed in a preheat process before liquid propane is supplied to a naphtha cracking reactor.

Method for Purifying Raffinate-2

Process for the production of light olefins and btx using an fcc unit processing a heavy feedstock of the highly hydrotreated vgo type, coupled with a catalytic reforming unit and an aromatic complex processing a naphtha-type feedstock

본 발명은 수소가 농후화된 중질 공급원료들, 예를 들어 고도로 수소처리된 VGO 또는 이러한 동일한 종류의 VGO 공급원료의 수소분해 종료시에 미전환된 부분을 처리하는 FCC 유닛들에 관한 것으로서, 상기 FCC 유닛들의 공급원료들은 에틸렌 및 프로필렌과 같은 경질 올레핀들에 대한 분해 특성을 가진다. 방향족 컴플렉스와 FCC 의 통합은, FCC 에 형성된 BTX 의 방향족 컴플렉스에 의한 회수 그리고 방향족 컴플렉스로부터의 중질 방향족들의 칼럼의 바닥에서의 유동으로부터의 FCC 에 의한 회수를 가능하게 한다. The present invention relates to FCC units for processing the unconverted fraction at the end of hydrocracking of hydrogen-enriched heavy feedstocks, such as highly hydrotreated VGO or VGO feedstocks of the same type, said FCC units. The feedstocks of the units have cracking properties for light olefins such as ethylene and propylene. The integration of the aromatics complex with the FCC enables the recovery by the aromatics complex of BTX formed in the FCC and the recovery by the FCC from the flow at the bottom of the column of heavy aromatics from the aromatics complex.

Production of aromatics from noncatalytically cracked fatty acid based oils.

Se describe un método para producir compuestos aromáticos a partir de aceites de ácidos grasos incluye calentar un aceite de ácido graso a una temperatura de entre aproximadamente 100 °C a aproximadamente 800 °C a una presión entre aproximadamente condiciones de vacío y aproximadamente 1.378 MPa (200 psia) durante un tiempo suficiente para craquear el aceite y producir un aceite de ácido graso craqueado; remover materiales no deseados, aceite no reaccionado, fracciones pesadas y fracciones ligeras del aceite de ácido graso craqueado; calentar el aceite de ácido graso craqueado purificado resultante a una temperatura de entre aproximadamente 100 °C a aproximadamente 800 °C a una presión de entre condiciones de vacío y aproximadamente 1.378 MPa (200 psia) durante un tiempo suficiente para reformar alquenos y alcanos en el aceite de ácido graso craqueado a compuestos aromáticos y producir un aceite de ácido graso reformado; y extraer componentes del aceite de ácido graso reformado para producir una mezcla de productos químicos que contiene entre 5 % y 90 % en peso de compuestos aromáticos.

Hydrocarbon Conversion Catalyst System

본 발명은, 고체 지지체 상의 탈수소반응 활성 금속을 포함하는 제1 조성물; 및 무기 지지체 상의 전이 금속을 포함하는 제2 조성물을 포함하는 탄화수소 전환 촉매 시스템, 및 상기 탄화수소 전환 촉매 시스템을 이용하는 탄화수소 전환 방법에 관한 것이다.

Process for producing aromatic hydrocarbons

Reforming process with integrated fluid catalytic cracker gasoline and hydroprocessed cycle oil

重整方法包括联合催化裂化产物石脑油脱氢和来自加氢裂化区的石脑油并将它们供入脱氢区中。脱氢区包含来自催化剂再生器的第一部分重整催化剂，其向下移动通过脱氢区。来自脱氢区的产物流流入芳烃装置中并分离成富芳烃萃取物和萃余物。将直馏石脑油和萃余物引入第一重整区中，所述第一重整区包含第二部分重整催化剂。重整催化剂移动通过第一重整区，然后从第一重整区和脱氢区各自的底部除去并供入第二重整区中。将来自第一重整区的流出物供入多个重整区中。重整催化剂向下移动通过多个重整区，然后进入再生器中。