СПОСОБ ГИДРОПЕРЕРАБОТКИ УГЛЕВОДОРОДНОГО СЫРЬЯ

Изобретение относится к усовершенствованному способу гидропереработки углеводородного сырья, содержащего серу- и/или азотсодержащие загрязняющие вещества. Указанный способ включает первое контактное взаимодействие углеводородного сырья с водородом в присутствии, по меньшей мере, одного первого катализатора на основе металлов VIII группы на кислотном носителе, причем носитель выбирают из группы цеолитов и цеолитсодержащих носителей, а затем поток, выходящий с первого катализатора, непосредственно контактирует с водородом в присутствии, по меньшей мере, одного второго катализатора на основе металла VIII группы на менее кислотном твердом носителе, причем указанный твердый носитель выбирают из группы носителей на основе диоксида кремния-оксида алюминия и других твердых носителей, не являющихся цеолитами. При указанной комбинации двух слоев катализатора появляется возможность перерабатывать сырье с высоким содержанием загрязняющих примесей без высокого уровня крекинга, связанного с использованием ...

СПОСОБ ОБРАБОТКИ УГЛЕВОДОРОДНОГО СЫРЬЯ

Изобретение касается способа обработки углеводородного сырья, содержащего водород и углеводороды, в том числе углеводороды C1-C4, согласно которому: a) разделяют углеводородное сырье на газовую фазу (6) и жидкую фазу, содержащую углеводороды (4); b) осуществляют первое повторное контактирование, приводя в контакт жидкую фазу с газовой фазой (8), выходящей с этапа c), до температуры от -20°C до 60°C, затем разделяют смесь с повторного контактирования на первый газовый поток, обогащенный водородом, и первый жидкий поток углеводородов; c) осуществляют второе повторное контактирование, приводя в контакт первый жидкий поток углеводородов (13) с газовой фазой (6), выходящей с этапа a), и рециркулирующим газом (14), выходящим с этапа f), при температуре в интервале от -20°C до 60°C, затем разделяют смесь повторного контактирования на второй газовый поток (17) и второй жидкий поток углеводородов (18; d) сжимают второй газовый поток (17) и отправляют указанный второй газовый поток в качестве газовой ...

СПОСОБ ПОЛУЧЕНИЯ СРЕДНИХ ДИСТИЛЛЯТОВ ГИДРОИЗОМЕРИЗАЦИЕЙ И ГИДРОКРЕКИНГОМ ДВУХ ФРАКЦИЙ ПРОДУКТОВ, ПОЛУЧЕННЫХ СИНТЕЗОМ ФИШЕРА-ТРОПША, И УСТАНОВКА ДЛЯ ЕГО ОСУЩЕСТВЛЕНИЯ

Использование: нефтехимия. Сущность: проводят фракционирование парафинового сырья с получением промежуточной фракции, имеющей начальную точку кипения в интервале 120-200°С и конечную точку кипения в интервале 300-410°С, легкой фракции, кипящей ниже промежуточной фракции, и тяжелой фракции, кипящей выше промежуточной фракции. По меньшей мере, часть промежуточной фракции подвергают гидроочистке и пропускают через аморфный катализатор гидроизомеризации/гидрокрекинга. По меньшей мере, часть тяжелой фракции пропускают через аморфный катализатор гидрокрекинга/гидроизомеризации при конверсии продуктов 370°+ в продукты 370°-, превышающей 80 мас.%. По меньшей мере, часть гидрокрекированных/гидроизомеризированных фракций подвергают дистилляции. Технический результат: повышение качества и выхода средних дистиллятов. 2 н. и 11 з.п. ф-лы, 1 ил., 12 табл.

СПОСОБЫ ПОЛУЧЕНИЯ НЕОЧИЩЕННОГО ПРОДУКТА

Изобретение относится к способу получения неочищенного сырья. При контактировании неочищенного сырья с одним или несколькими катализаторами получают суммарный продукт, который включает неочищенный продукт. Неочищенное сырье имеет содержание остатка, по меньшей мере, 0,2 грамма остатка на 1 грамм неочищенного сырья. Неочищенный продукт представляет собой жидкую смесь при 25°С и 0,101 МПа. Одно или несколько свойств этого неочищенного продукта можно изменить, по меньшей мере, на 10% относительно соответствующих свойств неочищенного сырья. В некоторых вариантах изобретения в результате контактирования неочищенного сырья с одним или несколькими катализаторами получают газ. Данные способы позволяют получать неочищенное сырье с улучшенными характеристиками. Изобретение также относится к неочищенному продукту или смеси и способу получения транспортного топлива. 5 н. и 17 з.п. ф-лы, 4 табл., 12 ил.

СПОСОБ ПОЛУЧЕНИЯ ДИЗЕЛЬНОГО ТОПЛИВА

Изобретение раскрывает способ получения дизельного топлива из углеводородного потока, включающий в себя: гидроочистку основного углеводородного потока и совместно подаваемого потока углеводородного сырья, содержащего дизельное топливо, в присутствии потока водорода и катализатора предварительной очистки, с получением предварительно очищенного выходящего потока; гидрокрекинг предварительно очищенного выходящего потока в присутствии катализатора гидрокрекинга и водорода с получением выходящего потока гидрокрекинга; разделение на фракции по меньшей мере части выходящего потока гидрокрекинга с получением потока дизельного топлива; и гидроочистку потока дизельного топлива в присутствии потока водорода для гидроочистки и катализатора гидроочистки с получением выходящего потока гидроочистки. Технический результат заключается в получении дизельного топлива с низким содержанием серы и аммиака. 9 з.п. ф-лы, 2 ил.

СПОСОБ ПОЛУЧЕНИЯ НИЗКОЗАСТЫВАЮЩЕГО ДИЗЕЛЬНОГО ТОПЛИВА

Изобретение относится к способу получения низкозастывающего дизельного топлива путем гидрогенизационной переработки нефтяного сырья в присутствии катализаторов, при повышенных температуре и давлении, и последующей ректификации гидрогенизата с выделением легкой и тяжелой дизельных фракций, которые в дальнейшем смешивают, где в качестве нефтяного сырья используют смесь газойля прямой перегонки нефти и широкой бензиновой фракции замедленного коксования, в соотношении от 95:5% масс., до 70:30% масс., которую подвергают последовательно гидроочистке, каталитической гидродепарафинизации и дополнительной гидроочистке, при этом объем катализаторов от общей загрузки составляет: гидроочистки - 45-65% масс., каталитической гидродепарафинизации - 20-35% масс., дополнительной гидроочистки - 10-30% масс. Предлагаемый способ позволяет расширить сырьевые ресурсы производства дефицитного низкозастывающего дизельного топлива для наземного транспорта, эксплуатируемого в условиях холодного и арктического климата ...

СПОСОБ ПОЛУЧЕНИЯ ПРОДУКТА С УМЕНЬШЕННЫМ СОДЕРЖАНИЕМ СЕРЫ (ВАРИАНТЫ)

... 1. Способ получения продукта с уменьшенным содержанием серы из исходного материала, который включает в себя содержащие серу органические загрязнения и содержит нормально жидкую смесь углеводородов, которая включает в себя олефины, причем способ предусматривает (a) введение в контакт исходного материала с катализатором модификации олефина по меньшей мере в одной зоне реакции модификации олефина при условиях, которые позволяют получать продукт, имеющий бромное число ниже, чем в исходном материале, причем продукт содержит рефракционные соединения серы; (b) фракционирование продукта из указанный зоны реакции модификации олефина с получением (i) первой фракции, которая включает в себя содержащие серу органические загрязнения и имеет конечную температуру перегонки менее чем ориентировочно 140°С; (ii) второй фракции с более высокой температурой кипения, чем первая фракция, включающей в себя содержащие серу органические загрязнения и имеет конечную температуру перегонки менее чем ориентировочно ...

ГИДРОПЕРЕРАБОТКА УГЛЕВОДОРОДНОГО СЫРЬЯ

... 1. Способ гидропереработки углеводородного сырья, содержащего серу- и/или азотсодержащие загрязняющие вещества, указанный способ включает первое контактное взаимодействие углеводородного сырья с водородом в присутствии, по меньшей мере, одного первого катализатора на основе металлов VIII группы на кислотном носителе, причем носитель выбирают из группы цеолитов и цеолитсодержащих носителей, а затем контактное взаимодействие сырья с водородом в присутствии, по меньшей мере, одного второго катализатора на основе металла VIII группы на менее кислотном твердом носителе, причем указанный твердый носитель выбирают из группы носителей на основе диоксида кремния-оксида алюминия и других твердых носителей, не являющихся цеолитами. 2. Способ по п.1, в котором указанная гидропереработка включает гидроконверсию, гидрокрекинг, гидрообработку, гидрирование, гидроочистку и гидроизомеризацию нефтяных типов сырья, таких как растворители и средний дистиллят. 3. Способ по п.1 или 2, в котором твердый носитель ...

СПОСОБЫ ПОЛУЧЕНИЯ НЕОЧИЩЕННОГО ПРОДУКТА И ВОДОРОДСОДЕРЖАЩЕГО ГАЗА

... 1. Способ получения газообразного водорода, в котором неочищенное сырье контактирует с одним или несколькими углеводородами в присутствии неорганического солевого катализатора и водой, причем число атомов углерода в углеводороде находится в диапазоне от 1 до 6, неочищенное сырье имеет содержание остатка, по меньшей мере, 0,2 г остатка на 1 г неочищенного сырья, и для неорганического солевого катализатора наблюдается точка перегиба при выделении газа в температурном диапазоне между 50 и 500°С, что определяется по методу Временного анализа продуктов (ВАП), и получают газообразный водород. 2. Способ по п.1, в котором углеводород, имеющий один или несколько атомов углерода в диапазоне от 1 до 6, включает в себя метан, этан, пропан, бутан, нафту или их смеси. 3. Способ по п.1 или 2, в котором вода представляет собой водяной пар. 4. Способ получения газового потока, в котором неочищенное сырье контактирует с неорганическим солевым катализатором в присутствии водяного пара, в котором неочищенное ...

СПОСОБ ПОЛУЧЕНИЯ НЕОЧИЩЕННОГО ПРОДУКТА

... 1. Способ получения неочищенного продукта, в котором вводят в контакт неочищенное сырье с источником водорода в присутствии неорганического солевого катализатора, чтобы получить суммарный продукт, который включает неочищенный продукт, при этом неочищенный продукт представляет собой жидкую смесь при 25°С и 0,101 МПа, неочищенное сырье имеет содержание остатка, по меньшей мере, 0,2 г остатка на 1 г неочищенного сырья; неорганический солевой катализатор содержит одну или несколько солей щелочных металлов, одну или несколько солей щелочно-земельных металлов или их смеси, в котором одна из солей щелочного металла представляет собой карбонат щелочного металла, где щелочной металл имеет атомный номер, по меньшей мере, 11; и регулируют условия контактирования: температуру, давление, скорость потока неочищенного сырья, потока суммарного продукта, время пребывания, скорость потока источника водорода или их сочетаний, чтобы получить суммарный продукт, который имеет содержание остатка, по большей мере ...

СПОСОБ ПОЛУЧЕНИЯ СРЕДНИХ ДИСТИЛЛЯТОВ ГИДРОИЗОМЕРИЗАЦИЕЙ И ГИДРОКРЕКИНГОМ СЫРЬЯ, ПОЛУЧЕННОГО СИНТЕЗОМ ФИШЕРА-ТРОПША

ÐÎÑÑÈÉÑÊÀß ÔÅÄÅÐÀÖÈß (19) RU (51) ÌÏÊ 7 (11) 2004 103 459 (13) A C 10 G 65/00 ÔÅÄÅÐÀËÜÍÀß ÑËÓÆÁÀ ÏÎ ÈÍÒÅËËÅÊÒÓÀËÜÍÎÉ ÑÎÁÑÒÂÅÍÍÎÑÒÈ, ÏÀÒÅÍÒÀÌ È ÒÎÂÀÐÍÛÌ ÇÍÀÊÀÌ (12) ÇÀßÂÊÀ ÍÀ ÈÇÎÁÐÅÒÅÍÈÅ (21), (22) Çà âêà: 2004103459/04, 26.06.2002 (30) Ïðèîðèòåò: 06.07.2001 FR 0108969 (43) Äàòà ïóáëèêàöèè çà âêè: 20.06.2005 Áþë. ¹ 17 (86) Çà âêà PCT: FR 02/02204 (26.06.2002) (72) Àâòîð(û): ÁÅÍÀÇÇÈ Ýðèê (FR), ÃÅÐÅ Êðèñòîô (FR) (74) Ïàòåíòíûé ïîâåðåííûé: Åãîðîâà Ãàëèíà Áîðèñîâíà Àäðåñ äë ïåðåïèñêè: 129010, Ìîñêâà, óë. Á.Ñïàññêà , 25, ñòð.3, ÎÎÎ "Þðèäè÷åñêà ôèðìà Ãîðîäèññêèé è Ïàðòíåðû", ïàò.ïîâ. Ã.Á. Åãîðîâîé R U Ôîðìóëà èçîáðåòåíè 1. Ñïîñîá ïîëó÷åíè ñðåäíèõ äèñòèëë òîâ èç ïàðàôèíîâîé çàãðóçêè, ïîëó÷åííîé ñèíòåçîì Ôèøåðà-Òðîïøà, ñîäåðæàùèé ñëåäóþùèå ïîñëåäîâàòåëüíûå ýòàïû: (a) ðàçäåëåíèå åäèíñòâåííîé ôðàêöèè, íàçûâàåìîé ò æåëîé, ñ íà÷àëüíîé òî÷êîé êèïåíè , ñîñòàâë þùåé 120-200°Ñ, (b) ãèäðîî÷èñòêà, ïî ìåíüøåé ìåðå, ÷àñòè âûøåóêàçàííîé ò æåëîé ôðàêöèè, (c) ôðàêöèîíèðîâàíèå, ïî ìåíüøåé ìåðå, íà 3 ôðàêöèè: ïî ìåíüøåé ìåðå, îäíó ïðîìåæóòî÷íóþ ôðàêöèþ, èìåþùóþ íà÷àëüíóþ òî÷êó êèïåíè Ò1, ñîñòàâë þùóþ îò 120 äî 200°Ñ, è êîíå÷íóþ òî÷êó êèïåíè Ò2, êîòîðà âûøå 300°Ñ è íèæå 410°Ñ, ïî ìåíüøåé ìåðå, îäíó ëåãêóþ ôðàêöèþ, êèï ùóþ íèæå ïðîìåæóòî÷íîé ôðàêöèè, ïî ìåíüøåé ìåðå, îäíó ò æåëóþ ôðàêöèþ, êèï ùóþ âûøå ïðîìåæóòî÷íîé ôðàêöèè, (d) ïðîïóñêàíèå, ïî ìåíüøåé ìåðå, ÷àñòè âûøåóêàçàííîé ïðîìåæóòî÷íîé ôðàêöèè ÷åðåç àìîðôíûé êàòàëèçàòîð ãèäðîèçîìåðèçàöèè/ãèäðîêðåêèíãà, (e) ïðîïóñêàíèå, ïî ìåíüøåé ìåðå, ÷àñòè âûøåóêàçàííîé ò æåëîé ôðàêöèè ÷åðåç àìîðôíûé êàòàëèçàòîð ãèäðîêðåêèíãà/ãèäðîèçîìåðèçàöèè, (f) äèñòèëë öè ãèäðîêðåêèðîâàííûõ/ãèäðîèçîìåðèçîâàííûõ ôðàêöèé äë ïîëó÷åíè ñðåäíèõ äèñòèëë òîâ, è ðåöèðêóëèðîâàíèå îñòàòî÷íîé ôðàêöèè, êèï ùåé âûøå óêàçàííûõ ñðåäíèõ äèñòèëë òîâ, íà ýòàï (å) íà àìîðôíûé êàòàëèçàòîð, îáðàáàòûâàþùèé ò æåëóþ ôðàêöèþ. 2. Ñïîñîá ïî ï.1, â êîòîðîì âûøåóêàçàííóþ ëåãêóþ ôðàêöèþ, ðàçäåëåííóþ íà ýòàïå (à), ïðîâîä ò íà ïàðîâîé êðåêèíã. Ñòðàíèöà: 1 A 2 0 0 4 1 0 3 4 5 9 A (54) ÑÏÎÑÎÁ ...

СПОСОБ ПОЛУЧЕНИЯ ОСНОВ НИЗКОЗАСТЫВАЮЩИХ АРКТИЧЕСКИХ МАСЕЛ

Настоящее изобретение относится к способу получения основ низкозастывающих арктических масел, при этом нефтяное сырье - фракция гидрокрекинга вакуумного газойля, выкипающая при температуре 280°C-КК, подвергается гидроизомеризации путем ее контактирования с водородом при объемном соотношении водорода к сырью 500-1000 нм/мна катализаторе, содержащем, мас.%: Pt - 0,30-0,35, WO- 3,0-4,0, SiO- 8,0-38,8, InO - 0,4-0,42, алюмосиликат - остальное, при температуре 240-320°C, парциальном давлении водорода 3,5-6,0 МПа, объемной скорости подачи сырья 0,5-2,0 чс получением маловязкой основы низкозастывающего арктического масла, имеющей кинематическую вязкость при температуре 100°C - 2,11-5,05 мм/с и температуру застывания продукта - минус 62 - минус 65°C, а для получения средневязкой и вязкой основы низкозастывающего арктического масла проводят гидрирование полученной маловязкой основы низкозастывающего арктического масла при температуре 240-260°C, парциальном давлении водорода 4,0-5,0 МПа, объемной ...

СПОСОБ ПЕРЕРАБОТКИ НЕФТИ

Способ переработки нефти путем смешивания не синтезированного растворителя с нефтью в составе от 8 до 15% от массы в обессоленную и обезвоженную нефть в течение 3-5 ч при температуре окружающей среды.

СПОСОБ ПОЛУЧЕНИЯ РАЗВЕТВЛЕННЫХ АЛКИЛАРИЛСУЛЬФОНАТОВ И КОМПОЗИЦИЙ РАЗВЕТВЛЕННЫХ АЛКИЛАРИЛСУЛЬФОНАТОВ

... 1. Способ получения разветвленных олефинов, указанный способ включает дегидрирование изопарафиновой композиции, содержащей 0,5% или менее четвертичных алифатических атомов углерода, на подходящем катализаторе, указанная изопарафиновая композиция получена гидрокрекингом и гидроизомеризацией парафина и включает парафины с количеством углеродов в диапазоне от 7 до 18, причем указанные парафины, по меньшей мере, часть их молекул, являются разветвленными, среднее количество ответвлений на молекулу парафина составляет от 0,5 до 2,5, и ответвления включают метильные и необязательно этильные ветви, указанные разветвленные олефины имеют содержание четвертичных алифатических углеродов 0,5% или менее, указанный парафин получен реакцией Фишера-Тропша. 2. Способ по п.1, где содержание разветвленных парафинов изопарафиновой композиции составляет, по меньшей мере, 50 мас.% от массы изопарафиновой композиции. 3. Способ по п.1 или 2, где количество метильных ветвей, присутствующих в изопарафиновой композиции ...

СПОСОБ ПОЛУЧЕНИЯ НЕОЧИЩЕННОГО ПРОДУКТА

... 1. Способ получения неочищенного продукта, образующегося в процессе нефтедобычи, вводят в контакт неочищенное сырье с источником водорода в присутствии неорганического солевого катализатора с получением суммарного продукта, который включает в себя неочищенный продукт, который представляет собой жидкую смесь при 25°С и 0,101 МПа, причем неочищенное сырье имеет содержание остатка, по меньшей мере, 0,2 г остатка на 1 г неочищенного сырья; неорганический солевой катализатор содержит, по меньшей мере, две неорганические соли металла, неорганический солевой катализатор содержит на 1 г неорганического солевого катализатора от 0 до 0,1 г композиций, которые образуют стекла при температурах, по меньшей мере 350°С, и для неорганического солевого катализатора наблюдается точка перегиба при выделении газа в диапазоне температур, который определяется по методу Временного анализа продуктов (ВАП), где точка перегиба при выделении газа находится в диапазоне температур между а) температурой дифференциальной ...

VERFAHREN ZUR HERSTELLUNG VON KOHLENWASSERSTOFFDESTILLATEN UND SCHMIEROELGRUNDMATERIALIEN

HYDROTREATING AND HYDROISOMERIZING C5 AND C6 HYDROCARBON STREAMS

Process of conversion of hydrocarbon oils.

Process of raw petroleum oil conversion.

Process of hydroraffinage of formative coke hydrocarbon distillates.

Process of hydrocraquage.

Process of hydrocraquage of hydrocarbon oils.

New process of oil conversion and desulphurization.

TWO-STAGE PROCEDURE FOR THE HYDROGENATION TREATMENT OF CENTRAL DISTILLATES WITH TWO HYDROGEN FEEDBACK LOOPS

CATALYTIC PROCEDURE FOR THE PRODUCTION OF LUBRICATING OILS WITH LOW SETTING POINT.

PROCEDURE FOR THE PRODUCTION OF KEROSENE AND/OR GAS OILS.

PROCEDURE FOR THE TRANSFORMATION OF HYDROCARBONS

PROCEDURE FOR THE PRODUCTION OF BASIS LUBRICATING OILS.

PROCEDURE FOR THE REDUCTION OF SULFUR AND CARBON INTO REFINING OF OIL

HYDROCRACK PROCEDURE WITH CENTER DISTILLATE SELECTIVITY

PROCEDURE FOR THE PRODUCTION OF DESULPHURISED GASOLINE FROM A CRACKBENZIN CONTAINING GASOLINE

Systems and methods of producing a crude product

GAS OILS

AN IMPROVED HYDROCRACKING PROCESS

Production of oilfield hydrocarbons

A process (20) to produce olefinic products suitable for use as or conversion to oilfield hydrocarbons includes separating (42) an olefins-containing Fischer-Tropsch condensate (64) into a light fraction (68), an intermediate fraction (82) and a heavy fraction (94), oligomerising (44) at least a portion of the light fraction (68) to produce a first olefinic product (72) which includes branched internal olefins, and carrying out either one or both of the steps of (i) dehydrogenating (50) at least a portion of the intermediate fraction (82) to produce an intermediate product (84) which includes internal olefins and alpha-olefins, and synthesising (52) higher olefins from the intermediate product which includes internal olefins and alpha-olefins to produce a second olefinic product (86), and (ii) dimerising (52) at least a portion of the intermediate fraction to produce a second olefinic product (86). At least a portion of the heavy fraction (94) is dehydrogenated (58) to produce a third olefinic ...

Separation process with modified enhanced hot separator system

A separation process with a modified enhanced hot separator system is described. The process eliminates undesirable entrainment while allowing for enhanced stripping of the net liquid only. The modified enhanced hot separator system combines a hot separator with a hot stripping column.

Three stage hydroprocessing including a vapor stage

PROCEDURE FOR THE DESULFURIZATION OF GASOLINE INVOLVING DESULFURIZATION OF THE HEAVY AND INTERMEDIATE FRACTIONS PRODUCED BY ONE FRACTIONATION STAGE AND AT LEAST THREE CUTS

L'invention concerne un procédé de production d'essence à faible teneur en soufre, à partir d'une charge contement du soufre. Ce procédé comprend au moins une étape a1 d'hydrogénation sélective des dioléfines et des composés acétylèniques, au moins une séparation de l'essence (étape b) obtenue à l'étape a1 en au moins trois fractions, au moins une étape c1 de traitement de l'essence lourde séparée à l'étape b sur un catalyseur permettant de décomposer ou d'hydrogéner au moins partiellement les composés soufrés insaturés, et au moins une étape d de désulfuration et déazotation d'au moins une fraction intermédiaire, suivie d'un reformage catalytique.

ISOPARAFFINIC BASE STOCKS BY DEWAXING FISCHER-TROPSCH WAX HYDROISOMERATE OVER PT/H-MORDENITE

A high VI and low pour point lubricant base stock is made by hydroisomerizing a high purity, waxy, paraffinic Fischer-Tropsch synthesized hydrocarbon fraction having an initial boiling point in the range of 343-399.degree.C (650- 750.degree.F), followed by catalytically dewaxing the hydroisomerate using a dewaxing catalyst comprising a catalytic platinum component and an H-mordenite component. The hydrocarbon fraction is preferably synthesized by a slurry Fischer-Tropsch using a catalyst containing a catalytic cobalt component. This combination of the process, high purity, waxy paraffinic feed and the Pt/H-mordenite dewaxing catalyst, produce a relatively high yield of premium lubricant base stock.

PROCESS FOR THE DESULPHURISATION OF OLEFIN-CONTAINING FEEDSTOCKS BY CONTROLLING THE OLEFIN CONTENT

The invention relates to a method and a device for desulfurizing an olefin- and hydrogen-containing charge flow, which can be mixed with additional hydrogen, and which is separated into at least two feed flows. The first charge flow is separately introduced into the reactor and impinges on a first catalyst bed comprising the catalyst pellets on a suitable holding device or a grating. There, the charge flow is heated by the hydrogenation reaction. Downstream of the first catalyst bed, an additional charge flow is supplied, thus cooling down the reaction gas and allowing the gas to be conducted through a second catalyst bed. Downstream of the second catalyst bed, further catalyst beds and further charge flow feeding devices may be provided. The catalyst beds may be placed in the reactor in any quantity, type, or shape. By carrying out the reaction in this manner, a product gas is obtained that substantially contains hydrogen sulfide only as a sulfur compound. The temperature in the catalyst ...

METHOD FOR HYDROTREATING HEAVY HYDROCARBON FEEDSTOCKS USING PERMUTABLE REACTORS, INCLUDING AT LEAST ONE STEP OF GRADUAL PERMUTATION

Procédé d'hydrotraitement d'une fraction lourde d'hydrocarbures utilisant un système de zones de garde permutables en lits fixes contenant chacune au moins un lit catalytique incluant au moins une étape au cours de laquelle le flux de la charge alimentant la première zone de garde mise en contact avec la charge est en partie basculé vers la prochaine zone de garde en aval, de préférence de façon progressive.

METHOD OF UPGRADING RESIDUA

... 2104112 9217561 PCTABS00016 Residua can be upgraded by first partitioning a hydrocracked residua into a vapor fraction and a liquid fraction. The vapor fraction is hydrotreated forming a first hydrotreated product. The liquid fraction is partitioned into a residua fraction and a light liquid fraction. The light liquid fraction can be hydrotreated or hydrocracked to form a hydroprocessed product. The hydrotreated product and the hydroprocessed product are then combined forming a substantially upgraded synthetic crude product refinable as a routine crude in a refinery into products that meet stringent specifications. In particular, residua can be upgraded to make a quality jet fuel fraction and a naphtha fraction containing less than 1 ppmw sulfur and nitrogen.

IMPROVED PROCESS FOR SELECTIVE HYDROGENATION OF HIGHLY UNSATURATED COMPOUNDS AND ISOMERIZATION OF OLEFINS IN HYDROCARBON STREAMS

A process for treating C3 to C12 petroleum fractions, such as a light cracked naphtha to be used as an etherification feed stock in which H2S is removed by distillation of at least the C3 fraction and mercaptans and diolefins are removed simultaneously in a distillation column reactor (20) using a dual catalyst bed (22, 24). The mercaptans and H2S are reacted with the diolefins in the presence of a reduced nickel catalyst (22) to form sulfides which are higher boiling than the portion of the feed which is fractionated to an upper hydrogenation catalyst bed of palladium (24) for hydrogenating diolefins and acetylenes. The higher boiling sulfides are removed as bottoms (110) along with heavier materials. Any diolefins not converted to sulfides and acetylenes are selectively hydrogenated to mono-olefins in the presence of a palladium oxide catalyst in an upper bed (24), producing overheads (116), substantially free of sulfur compounds, diolefins and acetylenes.

PROCESS USING STAGGERED BYPASSING OF REACTION ZONES FOR INCREASED CAPACITY

The operation of multistage catalytic hydrocarbon conversion system in whic h hydrocarbons flow serially through at least two reaction zones is improved b y using staggered by-passing of a portion of the change to each zone such that the first zone processes only a first portion of the feed and the second zone processes the remaining portion of the feed and at least a portion of the effluent from the first zone. Where three reaction zones are used, processing of the effluent stream from the first reaction zone is split between the second and third reaction zones so that a portion of the charge to each zone always is directed around the zone and processed in the next reaction zone. One portion of the effluent stream is combined with hydrocarbons that bypassed the first reaction zone, and the combined stream is passed to the second reaction zone. The other portion of the first reaction zone effluent stream and at least a portion of the effluent stream of the second reaction zone are passed ...

PROCESS FOR INCREASED OLEFIN YIELDS FROM HEAVY FEEDSTOCKS

A process for upgrading petroleum feedstocks boiling in the distillate plus range, which feedstocks, when cracked, result in unexpected high yields of olefins. The feedstock is hydroprocessed in at least one reaction zone countercurrent to the flow of a hydrogen-containing treat gas. The hydroprocessed feedstock is then subjected to thermal cracking in a steam cracker or to catalytic cracking in a fluid catalytic cracking process. The resulting product slate will contain an increase in olefins compared with the same feedstock, but processed in by a conventional co-current hydroprocessing process.

LOW-SULPHUR SPECIES PRODUCTION METHOD

L'invention concerne un procédé de production d'essence à faible teneur en soufre comprenant au moins les étapes suivantes : a1) au moins une hydrogénation sélective des dioléfines. a2) éventuellement au moins une étape visant à augmenter le poids moléculaire des produits soufrés légers présents dans l'essence. b) au moins une séparation de l'essence obtenue à l'étape a1 ou a2 en deux fractions : essence légère et essence lourde. c) au moins un traitement de l'essence lourde séparée à l'étape b sur un catalyseur permettant de décomposer ou d'hydrogéner au moins partiellement les composés soufrés insaturés. d) au moins un traitement de l'essence lourde obtenue à l'étape c, sans élimination de l'H2S formé au cours de cette étape, sur un catalyseur permettant de décomposer les composés soufrés et plus préférentiellement les composés saturés linéaires et/ou cycliques.

Verfahren zur Raffination koksbildender Kohlenwasserstoffdestillate

Verfahren zur Konversion eines Kohlenwasserstoff enthaltenden Ausgangsmaterials und nach dem Verfahren erhaltene Mischung

METHOD OF PROCESSING CRUDE OIL

METHOD OF PRODUCING LPG AND BTX

METHOD OF PRODUCING C2 AND C3 HYDROCARBONS

СПОСОБ ПОЛУЧЕНИЯ КАТАЛИЗАТОРА ПЕРЕХОДНОГО МЕТАЛЛА И ПРИМЕНЕНИЕ КАТАЛИЗАТОРА В СПОСОБЕ ПОЛУЧЕНИЯ НЕОЧИЩЕННОГО ПРОДУКТА

Изобретение относится к способу получения катализатора, представляющего собой сульфид переходного металла. Данный катализатор применяют для получения неочищенного продукта из неочищенного сырья. Неочищенное сырье имеет содержание остатка по меньшей мере 0,2 г остатка на 1 г неочищенного сырья. Неочищенный продукт представляет собой жидкую смесь при 25°С и 0,101 МПа. Одну или несколько характеристик этого неочищенного продукта можно изменять по меньшей мере на 10% относительно соответствующих характеристик неочищенного сырья.

СПОСОБ УДАЛЕНИЯ СЕРЫ ИЗ СОДЕРЖАЩЕГО ОЛЕФИНЫ СЫРЬЯ ПУТЕМ РЕГУЛИРОВАНИЯ СОДЕРЖАНИЯ ОЛЕФИНОВ

Изобретение относится к способу и установке для десульфуризации содержащего олефины и водород потока сырья, который может быть смешан с дополнительным количеством водорода и который разделяют по меньшей мере на два потока сырья. Первый поток сырья отдельно подают в реактор, и он поступает на первый слой катализатора, который содержит частицы катализатора на соответствующем удерживающем устройстве или на колосниковой решетке. Здесь поток сырья нагревается при реакции гидрирования. Ниже по потоку относительно первого слоя катализатора подают дополнительный поток сырья, вследствие чего реакционный газ охлаждается, и благодаря этому его можно пропускать через второй слой катализатора. Ниже по потоку относительно второго слоя катализатора могут быть расположены дополнительные слои катализатора и могут быть обеспечены дополнительные устройства для подачи потока сырья. Слои катализатора могут быть размещены в реакторе в любом количестве и иметь любые тип и форму. Благодаря такому проведению реакции ...

METHOD AND DEVICE FOR MANUFACTURING OF MIXED RAW OIL AND FUEL

METHOD AND INSTALLATION FOR CONVERSION OF CRUDE OIL IN PETROCHEMICAL PRODUCTS WITH INCREASE EFFECTIVENESS AS CARBON NNOI

СПОСОБ ПОЛУЧЕНИЯ КАТАЛИЗАТОРА, КАТАЛИЗАТОР, СПОСОБ ПОЛУЧЕНИЯ НЕОЧИЩЕННОГО ПРОДУКТА И НЕОЧИЩЕННЫЙ ПРОДУКТ

При контакте неочищенного сырья с одним или несколькими катализаторами получают суммарный продукт, который включает в себя неочищенный продукт. Неочищенное сырье имеет содержание остатка по меньшей мере 0,2 г на 1 г неочищенного сырья. Неочищенный продукт представляет собой жидкую смесь при 25°С и 0,101 МПа. Одну или несколько характеристик этого неочищенного продукта можно изменять по меньшей мере на 10% относительно соответствующих характеристик неочищенного сырья. В некоторых вариантах осуществления изобретения получают газ в результате контактирования неочищенного сырья с одним или несколькими катализаторами.

СПОСОБ ПОЛУЧЕНИЯ КАТАЛИЗАТОРА, КАТАЛИЗАТОР, СПОСОБ ПОЛУЧЕНИЯ НЕОЧИЩЕННОГО ПРОДУКТА И НЕОЧИЩЕННЫЙ ПРОДУКТ

При контакте неочищенного сырья с одним или несколькими катализаторами получают суммарный продукт, который включает в себя неочищенный продукт. Неочищенное сырье имеет содержание меньшей мере 0,2 г остатка на 1 г неочищенного сырья. Неочищенный продукт представляет собой жидкую смесь при 25°С и 0,101 МПа. Одну или несколько характеристик этого неочищенного продукта можно изменять по меньшей мере на 10% относительно соответствующих характеристик неочищенного сырья. В некоторых вариантах осуществления изобретения получают газ в результате контактирования неочищенного сырья с одним или несколькими катализаторами.

КОМБИНИРОВАННЫЙ СПОСОБ КОНВЕРСИИ С ПРОТИВОТОКОМ ВОДОРОДА

Описан комбинированный способ гидрокрекинга и гидроочистки разнородных исходных материалов с использованием одного контура рекуперации и рециркуляции водорода. При комбинированном способе водород, рекуперированный из первой реакционной зоны, улавливается и проходит без существенного охлаждения во вторую реакционную зону. Жидкие продукты из первой реакционной зоны в возможном варианте могут проходить вместе с рекуперированным водородом во вторую реакционную зону. Водород, рекуперированный из второй реакционной зоны, подвергают очистке и используют в качестве источника водорода для первой реакционной зоны. Международная заявка была опубликована вместе с отчетом о международном поиске.

СПОСОБ ГИДРОГЕНИЗАЦИИ УГЛЕВОДНОГО СЫРЬЯ И СПОСОБ ГИДРОГЕНИЗАЦИИ НЕФТЯНОЙ ФРАКЦИИ

Способ гидрогенизации углеводного сырья включает взаимодействие основного количества углеводного сырья с водородом противотоком в первой реакционной зоне при гидрогенизационных условиях реакции в присутствии гидрогенизационных катализаторов, по крайней мере, в первом каталитическом слое, где существует поток жидкости в конечной части в первой реакционной зоне и где существует водородосодержащий газообразный поток в верхней части первой реакционной зоны, и взаимодействие незначительной порции углеводного сырья с указанным водородосодержащим газообразным потоком прямотоком во второй реакционной зоне, которая имеет каталитический слой, размещенный для получения водородосодержащего потока первой реакционной зоны.

СПОСОБ УДАЛЕНИЯ СЕРЫ ИЗ СОДЕРЖАЩЕГО ОЛЕФИНЫ СЫРЬЯ ПУТЕМ РЕГУЛИРОВАНИЯ СОДЕРЖАНИЯ ОЛЕФИНОВ

Изобретение относится к способу и установке для десульфуризации содержащего олефины и водород потока сырья, который может быть смешан с дополнительным количеством водорода и который разделяют по меньшей мере на два потока сырья. Первый поток сырья отдельно подают в реактор, и он поступает на первый слой катализатора, который содержит частицы катализатора на соответствующем удерживающем устройстве или на колосниковой решетке. Здесь поток сырья нагревается при реакции гидрирования. Ниже по потоку относительно первого слоя катализатора подают дополнительный поток сырья, вследствие чего реакционный газ охлаждается, и благодаря этому его можно пропускать через второй слой катализатора. Ниже по потоку относительно второго слоя катализатора могут быть расположены дополнительные слои катализатора и могут быть обеспечены дополнительные устройства для подачи потока сырья. Слои катализатора могут быть размещены в реакторе в любом количестве и иметь любые тип и форму. Благодаря такому проведению реакции ...

METHOD OF OBTAINING THE CATALYST, CATALYST, THE METHOD OF OBTAINING THE UNPURIFIED PRODUCT AND THE UNPURIFIED PRODUCT

СПОСОБ ПРОИЗВОДСТВА УГЛЕВОДОРОДОВ БИОЛОГИЧЕСКОГО ПРОИСХОЖДЕНИЯ

Данное изобретение относится к углеводородам, в частности к производству углеводородных компонентов, пригодных в качестве авиационного топлива или топлива для реактивных двигателей и в качестве компонентов смешивания для авиационного топлива. Процесс включает этапы, причем на первом этапе масляный загрузочный материал биологического происхождения и газообразный водород подвергают действию условий, достаточных для осуществления гидродезоксигенирования, в присутствии катализатора гидродезоксигенирования для получения н-парафинов; на втором этапе н-парафины и газообразный водород подвергают действию условий, достаточных для получения изопарафинов и распределения фракций; и рециркуляцию фракции, которая закипает при температуре более при атмосферном давлении, полученном на втором этапе, на реизомеризацию, причем изомеризацию осуществляют в присутствии катализатора изомеризации.

НЕОЧИЩЕННЫЙ ПРОДУКТ ПРОЦЕССОВ НЕФТЕДОБЫЧИ И СПОСОБ ЕГО ПЕРЕРАБОТКИ

При контакте неочищенного сырья с одним или несколькими катализаторами получают суммарный продукт, который включает в себя неочищенный продукт. Неочищенное сырье имеет содержание остатка по меньшей мере 0,2 г остатка на 1 г неочищенного сырья. Неочищенный продукт представляет собой жидкую смесь при 25°С и 0,101 МПа. Одну или несколько характеристик этого неочищенного продукта можно изменять по меньшей мере на 10% относительно соответствующих характеристик неочищенного сырья. В некоторых вариантах осуществления изобретения получают газ в результате контактирования неочищенного сырья с одним или несколькими катализаторами.

Способ многостадийной гидроконверсии остаточного мазута, объединенной со стадиями гидроконверсии газойлей

... 1. Способ обработки потока сырья на основе тяжелых углеводородов, содержащего мазут вакуумной перегонки, при котором: a) указанный поток углеводородов подают в реактор с кипящим слоем первой стадии гидроконверсии мазута и осуществляют гидроконверсию мазута вакуумной перегонки с получением выходящего потока, кипящего выше 343 °С и содержащего 50-100 мас. % продукта, кипящего выше 524 °С, b) указанный поток, выходящий из реактора с кипящим слоем первой стадии гидроконверсии мазута, разделяют в межстадийном сепараторе на паровую фазу, содержащую преимущественно вакуумный газойль и дизельное топливо, и жидкую фазу, содержащую преимущественно мазут вакуумной перегонки, c) жидкую фазу из указанного межстадийного сепаратора подают в реактор с кипящим слоем второй стадии гидроконверсии мазута и осуществляют дополнительную гидроконверсию мазута вакуумной перегонки с получением выходящего потока, d) паровую фазу из указанного межстадийного сепаратора подают в первый находящийся ниже по потоку дистиллятный ...

ИЗОМЕРИЗАЦИЯ БЕНЗИНА В ТРЕХ ЗОНАХ КАТАЛИТИЧЕСКИХ РЕАКЦИЙ ВНУТРИ РЕКТИФИКАЦИОННОЙ КОЛОННЫ

Предложена реакционно-ректификационная система для получения высокооктановых компонентов бензина, содержащая по меньшей мере три реакционные зоны, одна из которых является зоной гидроизомеризации бензола, другая является зоной изомеризации гексанов и третья является зоной изомеризации пентана, причем зона гидроизомеризации бензола расположена ниже всех остальных реакционных зон и находится в нижней части колонны, зона изомеризации гексанов находится выше зоны питания и ниже зоны изомеризации пентана, система также содержит по меньшей мере один боковой отбор, расположенный выше зоны изомеризации гексанов и ниже зоны изомеризации пентана.

СПОСОБ ДЕСУЛЬФУРИЗАЦИИ ОЛЕФИНСОДЕРЖАЩИХ ПОДАВАЕМЫХ ГАЗОВ

Изобретение относится к способу и устройству для гидродесульфуризации олефин- и водородсодержащего подаваемого газа. Подаваемый газ можно смешать с дополнительным водородом и разделить по меньшей мере на два сырьевых потока. Первый поток подаваемого газа отдельно вводят в реактор и пропускают через первый слой катализатора, который содержит гранулы катализатора, расположенные на подходящей основе или сетке. Сырьевой поток нагревается в реакции гидрогенизации. Снизу по потоку от первого слоя катализатора подают дополнительный подаваемый газ, который служит для охлаждения подаваемого газа, позволяя затем пропускать газ через второй слой катализатора. Снизу по потоку от второго слоя катализатора могут находиться дополнительные слои катализатора и дополнительные устройства подачи подаваемого газа. Слои катализатора могут быть установлены в реакторе в любом количестве, любого типа и любой формы. Данные технологические условия гарантируют, что получают газовый продукт, который, по существу, не ...

СПОСОБ И УСТАНОВКА ДЛЯ КОНВЕРСИИ СЫРОЙ НЕФТИ В НЕФТЕХИМИЧЕСКИЕ ПРОДУКТЫ С ПОВЫШЕННОЙ ЭФФЕКТИВНОСТЬЮ ПО УГЛЕРОДУ

Изобретение относится к комбинированному способу конверсии сырой нефти в нефтехимические продукты, включающему перегонку сырой нефти, гидрокрекинг и синтез олефинов, при этом способ включает в себя стадии, на которых сырье установки гидрокрекинга подвергают гидрокрекингу с образованием СНГ и БТК и подвергают СНГ, полученный в указанном способе, синтезу олефинов. Кроме того, изобретение относится к технологической установке для конверсии сырой нефти в нефтехимические продукты, содержащей установку перегонки сырой нефти, содержащую ввод для сырой нефти и по меньшей мере один вывод для одной или более фракций, выбранных из нафты, керосина и газойля; установку гидрокрекинга, содержащую ввод для сырья установки гидрокрекинга, вывод для СНГ и вывод для БТК; и установку для синтеза олефинов, содержащую ввод для СНГ, образованного комбинированной нефтехимической технологической установкой, и вывод для олефинов. Сырье установки гидрокрекинга, используемое в способе и технологической установке изобретения ...

Установка гидроочистки дизельной фракции

... 1. Установка гидроочистки дизельной фракции, включающая реакторный блок, состоящий из печи и трех реакторов, блок стабилизации и разделения и обвязки трубопроводов, отличающаяся тем, что первый реактор расположен последовательно по отношению к параллельно соединенным между собой второму и третьему реакторам.

Способ получения авиационного топлива

Использование: нефтеперерабатывающая промышленность. Задача: расширение сырьевой базы авиационных топлив, увеличение выхода авиационного топлива, отвечающего современным международным требованиям. Сущность изобретения: способ включает первичную перегонку углеводородного сырья в атмосферной колонне при температуре сырья на входе атмосферной колонны 330-354°С, температуре верха атмосферной колонны 150-185°С, с использованием верхнего циркуляционного орошения при 150-195°С и среднего циркуляционного орошения при 195-230°С, выделение керосиновой фракции, выкипающей в пределах 130-300°C, ее отпаривание в отпарной колонне, демеркаптанизацию выделенной фракции на установке демеркаптанизации. В качестве углеводородного сырья для получения авиационного топлива используют смесь нефти и газового конденсата в массовом соотношении от 5 : 95 до 95 : 5, а отпаривание в отпарной колонне осуществляют путем подачи пара при его расходе 0,2-2,5 т/ч. Также в состав топлива возможно введение антистатических, ...

Способы получения жидкого топлива

Использование: нефтеперерабатывающая промышленность. Задача: увеличение выходов целевых компонентов жидкого топлива при производстве жидкого топлива из парафиновых углеводородов гидроочисткой или гидрокрекингом. Сущность изобретения: способ включает стадию, на которой сырье, полученное синтезом Фишера-Тропша, содержащее нормальные парафины, кислородсодержащие соединения и олефины и имеющее конечную точку кипения при дистилляции не выше, чем 360°C, фракционируют при граничной температуре в интервале 130-160°C на первую фракцию, чья конечная точка кипения при дистилляции составляет не выше, чем граничная температура, и вторую фракцию, чья начальная температура кипения при дистилляции не ниже чем граничная температура; стадию, на которой первую фракцию подвергают гидроочистке с использованием первого катализатора, включающего содержащий твердую кислоту, носитель, выбранный из группы кристаллических алюмосиликатов и аморфных твердых кислот и палладия и/или платины, нанесенных на носитель, и ...

ИЗОМЕРИЗАЦИЯ БЕНЗИНА В ТРЕХ ЗОНАХ КАТАЛИТИЧЕСКИХ РЕАКЦИЙ ВНУТРИ РЕКТИФИКАЦИОННОЙ КОЛОННЫ

Предложена реакционно-ректификационная система для получения высокооктановых компонентов бензина, содержащая по меньшей мере три реакционные зоны, одна из которых является зоной гидроизомеризации бензола, другая является зоной изомеризации гексанов и третья является зоной изомеризации пентана, причем зона гидроизомеризации бензола расположена ниже всех остальных реакционных зон и находится в нижней части колонны, зона изомеризации гексанов находится выше зоны питания и ниже зоны изомеризации пентана, система также содержит по меньшей мере один боковой отбор, расположенный выше зоны изомеризации гексанов и ниже зоны изомеризации пентана. Пункты: 2 независ. 20 завис. Фиг.: 3 ...

Hydrogenation method of heavy hydrocarbon multi-segment fluidized bed

The invention discloses a hydrogenation method of a heavy hydrocarbon multi-segment fluidized bed. The technical process comprises the steps of: mixing thick heavy hydrocarbon raw materials with gas phase material flow which is discharged from a fluidized bed hydrogenation-desulfuration reactor and a hydrogenation-denitrification reactor to enter into a hydrogenation-demetalization reactor; cooling and purifying reacted gas phase material flow to be taken as recycle hydrogen; mixing the demetallized liquid phase material flow with hydrogen to enter into the fluidized bed hydrogenation-desulfuration reactor; mixing the desulfurated liquid phase material flow with hydrogen to enter into the hydrogenation-desulfuration reactor; and leading the denitrified liquid phase material flow to enter into a separating device. The technology adopts a new reactor assembly mode to machine heavy oil raw materials with high viscosity and bad quality, can provide a new flexible, high-efficiency and energy-saving ...

Hydro-conversion combination method for coal tar fraction with different boiling ranges

The invention relates to a hydro-conversion combination method for a coal tar fraction with different boiling ranges, which comprises the following steps that: a first hydrogen fraction containing a coal tar naphtha potential fraction is converted at a first hydrogen refining reaction part; a second hydrogen fraction containing a coal tar diesel oil potential fraction is converted at a second hydrogen refining reaction part; and a first hydrogen refining reaction effluent and a second hydrogen refining reaction effluent are mixed, separated and reclaimed. The method can select respective proper hydrogen refining reaction conditions for the coal tar fraction with different boiling ranges, has the advantages of improving the quality of products, stabilizing the operation, simplifying the flow and the like, and is particularly suitable for medium-scale classified combined hydro-conversion of low-temperature coal tar light fractions.

Process for producing diesel

A process is disclosed for hydrocracking a primary hydrocarbon feed and a diesel co-feed in a hydrocracking unit and hydrotreating a diesel product from the hydrocracking unit in a hydrotreating unit. The diesel stream fed through the hydrocracking unit is pretreated to reduce sulfur and ammonia and can be upgraded with noble metal catalyst.

Hydrogenation and quality improvement method for reducing sulfur and olefin content of inferior gasoline

Diesel oil hydrogenation modification process

Production of intermediate fractional oil from Fischer-Tropsch synthetic oil

Combined distillate oil hydroprocessing method

Gas oil and residual oil hydrotreating process for producing catalytically cracked material

The process of hydrogenating gas oil and residual oil to produce catalytically cracked material includes the following steps: contacting and reacting the mixture of gas oil and hydrogen with optional hydrogenation protecting agent and hydrogenation refining catalyst in the first reaction area; directly mixing the produced oil with residual oil, contacting and reacting the mixture with hydrogenation protecting agent, hydrogenating and demetallizing catalyst and hydrotreating catalyst successively in the second reaction area; cooling and separating the reacted products to obtain hydrogen-rich liquid and gas products. The present invention makes it possible to produce high quality catalytically cracked material via adding residual oil in 5-50 wt% into gas oil.

PROCESS OF CONVERSION INCLUDING/UNDERSTANDING A HYDROCONVERSION OF THE LOAD THEN A VISCOREDUCTION AND A FRACTIONATION

L'invention concerne un procédé de conversion comprenant une étape a d'hydroconversion de la charge, une étape b de réduction de la viscosité de l'effluent obtenu à l'étape a, une étape c de fractionnement d'une partie de l'effluent issu de l'étape b, et une étape d d'hydrotraitement.

HYDROCRACKING PROCESS FOR THE PRODUCTION OF MIDDLE DISTILLATES

PROCESS FOR PRODUCING LOW SULFUR GASOLINE COMPRISING A HYDROGENATION, FRACTIONATION, A STEP AND A DESULFURIZING SULFUR COMPOUNDS

PROCESS OF PRODUCTION OF AVERAGE DISTILLATES BY HYDROISOMERISATION ETHYDROCRAQUAGE OF LOADS RESULTING FROM PROCESS FISCHER-TROPSCH

COMPRESSOR HAS SPIRAL TEAM Of a DEFLECTOR Compared to the OPENING Of ASPIRATIONMENAGE IN ITS ENVELOPE

CATALYTIC DEWAXING

PROCESS FOR STABILIZATION OF DIOLEFIN?CONTAINING HYDROCARBONS

Process for producing lubricating oils

MOVING BED REACTOR CONVERSION PROCESS FOR PARTICULATE CONTAINING HYDROCARBONS SUCH AS SHALE OIL AND TAR?SANDS OIL

FLEXIBLE PROCESS IMPROVES OF PRODUCTION OF BASES OILS AND OF DISTILLATES BY UNECONVERSION-HYDROISOMERISATION ON a CATALYST SLIGHTLY DISPERSES FOLLOWED CATALYTIC UNDEPARAFFINAGE

PROCESS OF PRODUCTION Of OILS HAVING a HIGH INDEX OF VISCOSITY

Hydrocracking process intended for the production of middle distillates

PROCESS OF PRODUCTION OF AVERAGE DISTILLATES BY HYDROCRAQUAGE OF LOADS RESULTING FROM PROCESS FISCHER-TROPSCH WITH A CATALYST CONTAINING AN AMORPHOUS MATERIAL

HYDROCRACKING PROCESS WITH FLUORINE TREAT TO AVOID CONDENSED POLYAROMATICS

PROCESS FOR INCREASING THE OCTANE NUMBER OF A LIGHT GASOLINE FRACTION

HYDROTREATMENT OF FOSSIL FUELS

Low pour-point lubricants

PROCESS FOR THE CONVESION OF A HYDROCARBON OIL CONTAINING RESIDUAL MATERIAL

CONVERSION OF BIOMASS OR RESIDUAL WASTE MATERIAL TO BIOFUELS

The present invention provides a process for producing liquid hydrocarbon products from solid biomass and/or residual waste feedstocks, said process comprising the steps of: a) hydropyrolysing the solid feedstock in a hydropyrolysis reactor vessel in the presence of molecular hydrogen and one or more deoxygenation catalyst, producing a product stream comprising partially deoxygenated hydropyrolysis product, HO, H, CO, CO, C-Cgases, char and catalyst fines; b) removing said char and catalyst fines from said product stream; c) hydroconverting said partially deoxygenated hydropyrolysis product in a hydroconversion reactor vessel in the presence of one or more hydroconversion catalyst and of the HO, CO, CO, H, and C-Cgas generated in step a), producing a vapour phase product comprising substantially fully deoxygenated hydrocarbon product, HO, CO, CO, and C-Cgases; d) condensing the vapour phase product of step d) to provide a liquid phase product comprising substantially fully deoxygenated C4+ hydrocarbon liquid and aqueous material and separating said liquid phase product from a gas phase product comprising H, CO, CO, and C-Cgases; e) removing the aqueous material from the substantially fully deoxygenated C4+ hydrocarbon liquid; and f) hydroprocessing at least a portion of the substantially fully deoxygenated C4+ hydrocarbon liquid in a hydroprocessing reactor vessel in the presence of hydrogen and one or more hydroprocessing catalysts, each hydroprocessing catalyst comprising at least one reduced metal on a solid support, in order to provide an upgraded liquid hydrocarbon stream. 1. A process for producing liquid hydrocarbon products from solid biomass and/or residual waste feedstocks , said process comprising the steps of:{'sub': 2', '2', '2', '1', '3, 'a) hydropyrolysing the solid feedstock in a hydropyrolysis reactor vessel in the presence of molecular hydrogen and one or more deoxygenation catalyst, producing a product stream comprising partially deoxygenated ...

MULTI-STAGE UPGRADING PYROLYSIS TAR PRODUCTS

A first hydroprocessed product and a second hydroprocessed product produced from a multi-stage process for upgrading pyrolysis tar, such as steam cracker tar, are provided herein. Fuel blends including the first hydroprocessed product and/or the second hydroprocessed product are also provided herein as well as methods of lowering pour point of a gas oil using the first hydroprocessed product and the second hydroprocessed product. 1. A first hydroprocessed product comprising:aromatics in an amount ≥about 50 wt %;paraffins in an amount ≤about 5.0 wt %; andsulfur in an amount from about 0.10 wt % to <0.50 wt %; a boiling point distribution of about 145° C. to about 760° C. as measured according to ASTM D6352;', 'a pour point of ≤about 0.0° C., as measured according to ASTM D7346; and', {'sup': 2', '2, 'a kinematic viscosity at 50° C. from 20 mm/s to 200 mm/s, as measured according to ASTM D7042.'}], 'wherein the first hydroprocessed product has2. The first hydroprocessed product of further comprising asphaltenes in an amount from about 2.0 wt % to 10 wt %.3. The first hydroprocessed product of claim 1 , wherein the aromatics are present in an amount of ≥about 80 wt %.5. The first hydroprocessed product of having a pour point of ≤−5.0° C. claim 1 , as measured according to ASTM D7346.6. The first hydroprocessed product of having one or more of the following:(i) a Bureau of Mines Correlation Index (BMCI) of ≥about 100;{'sub': 'n', '(ii) a solubility number (S) of ≥about 130; and'}(iii) an energy content of ≥about 35 MJ/kg.7. A second hydroprocessed product comprising:aromatics in an amount ≥about 50 wt %;paraffins in an amount ≤about 5.0 wt %; andsulfur in an amount ≤0.30 wt %; a boiling point distribution of about 140° C. to about 760° C. as measured according to ASTM D6352;', 'a pour point of ≤about 12° C., as measured according to ASTM D5949; and', {'sup': 2', '2, 'a kinematic viscosity at 50° C. from 100 mm/s to 800 mm/s, as measured according to ASTM D7042.'}], ' ...

METHOD AND APPARATUS FOR IMPROVING HYDROGEN UTILIZATION RATE OF HYDROGENATION APPARATUS

A method and apparatus for improving a hydrogen utilization rate in a hydrogenation hot high-pressure separation process. Hydrogenated distillate oil, a gas product and hydrogen pass through an inertia separation distributor arranged in an inlet of a hot high-pressure separator under high pressure for preliminary gas-liquid separation, and a gas phase goes to a subsequent system; a liquid phase goes into a hot low-pressure separator. Releases a part of low-pressure separated gas (mainly hydrogen) after preliminary separation through an injection flash separator in the hot low-pressure separator, and is divided into a gas phase and a liquid phase based on gravitational settling; hydrogen and some micro bubbles that are still dissolved in hot low-pressure separated oil under the pressure are separated from the oil through a centrifugal degassing device; the gas phase exits from the apparatus after carried liquid droplets are removed completely through hydrocyclone separation or coalescence separation, and distillate oil goes to a subsequent facility. 1. A method for improving the hydrogen utilization in a hydrogenation high pressure hot separation process , characterized in that , it comprises the following steps:Step 1: distillate oil and hydrogen mixture undergo high pressure separation, comprising the following steps:Step 1.1: the distill oil and hydrogen mixture undergoes inertial separation of distribution to realize initial gas-liquid separation, and the gas-liquid mixture after separation is radially uniformly distributed in a hot high-pressure separator, wherein the pressure drop of the inertial separation is 0.0001-0.01 MPa;Step 1.2: the gas-liquid mixture after inertia separation undergoes a second gas-liquid separation via gravity settling;Step 2: the liquid phase after high pressure separation undergoes hot low-pressure separation, comprising the following steps:Step 2.1: the gas phase dissolved in the liquid phase is separated via jet flash, wherein the ...

PROCESS FOR PRODUCING C2 AND C3 HYDROCARBONS

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

PROCESS FOR PARTIAL UPGRADING OF HEAVY AND/OR EXTRA-HEAVY CRUDE OILS FOR TRANSPORTATION

The present invention relates to a process for the partial upgrading of properties of heavy and/or extra-heavy crude oil by low severity catalytic hydrotreatment in only one reaction step. The process of the present invention is obtained upgraded oil with properties required for its transportation from offshore platforms either to maritime terminal or to refining centers. The process reduces the viscosity of heavy and/or extra-heavy crude oil, and decreases the concentration of impurities, such as sulfur, nitrogen, and metals, in such a way that heavy and/or extra-heavy crude oils can be transported to maritime terminals or to refining centers. The process increases the lifetime of the catalyst and decreased operating costs by reducing consumption of utilities because the operation of the process is carried out at lower severity. The partially upgraded oils obtained in this process can be transported directly to the maritime terminals or to existing refineries. 2. The process according to claim 1 , wherein the desalters employed in step 1) are of the dielectric type claim 1 , for crude oil containing less than 200 pounds salt per 1 claim 1 ,000 barrels.3. The process according to claim 1 , wherein step 1) is carried out under pressure of 7 to 14 kg/cmand temperature of 125 to 150° C.4. The process according to claim 1 , wherein in step 1) the pressure value is preferably at least 2 kg/cmabove the vapor pressure of a crude oil-water mixture at the operating temperature.5. The process according to claim 1 , wherein the catalytic hydrotreatment of crude oil in step 2) is performed in a fixed bed reactor with a catalyst containing metals selected from the group consisting of Pt claim 1 , Pd claim 1 , Ni claim 1 , Mo and Co.6. The process according to claim 1 , wherein the catalyst employed in step 2) has a low metal loading: molybdenum from 2 to 8 weight % and nickel or cobalt from 0.1 to 3 weight % in the catalyst claim 1 , supported on gamma alumina claim 1 , with ...

PROCESS FOR THE CATALYTIC CONVERSION OF MICRO CARBON RESIDUE CONTENT OF HEAVY HYDROCARBON FEEDSTOCKS AND A LOW SURFACE AREA CATALYST COMPOSITION FOR USE THEREIN

An improved process for the hydroconversion of micro carbon residue content of heavy hydrocarbon feedstocks by the use of a catalyst composition that is especially useful in the conversion of micro carbon residue of such feedstocks. The catalyst composition is a low surface area composition that further has a specifically define pore structure the combination of which provides for its enhance micro carbon residue conversion property. 1. A process for converting at least a portion of an MCR content of a heavy hydrocarbon feedstock to yield a product having a reduced MCR content , wherein said process includes contacting said heavy hydrocarbon feedstock with a catalyst under MCR conversion process conditions and yielding said product , wherein the improvement comprises: enhancing the conversion of said MCR content of said heavy hydrocarbon feedstock by using as said catalyst in said process a calcined particulate of a co-mulled mixture , wherein said co-mulled mixture that is formed into a particulate , which is subsequently calcined to provide said calcined particulate , comprises a molybdenum component , a nickel component , an uncalcined pseudo-boehmite powder prepared by a two-step precipitation process and comprising at least 90 weight percent pseudo-boehmite , a mineral acid , and a catalyst fines portion having a particle size between 5 and 50 microns (μm) and a mean pore diameter between 40 Å and 150 Å , and wherein said calcined particulate is prepared under conditions so that it has specifically defined physical properties including:{'sup': 2', '2, '(a) a total surface area of greater than 160 m/g and less than 240 m/g;'}(b) a median pore diameter in the range of from 85 Å to 120 Å;(c) from 8% to 22% of the total pore volume of said calcined particulate in the macropores having a pore diameter of 250 Å or greater; and(d) greater than 40% and no more than 60% of the total pore volume of said calcined particulate within its pores having a diameter in the range ...

POWER GENERATION FROM WASTE HEAT IN INTEGRATED HYDROCRACKING AND DIESEL HYDROTREATING FACILITIES

A power generation system includes a heating fluid circuit thermally coupled to multiple heat sources from at least an integrated hydrocracking plant and diesel hydro-treating plant of a petrochemical refining system. A first subset of the heat sources includes diesel hydro-treating plant heat exchangers coupled to streams in the diesel hydro-treating plant. A second subset of the heat sources includes hydrocracking plant heat exchangers coupled to streams in the hydrocracking plant. The heat exchangers are connected to a power generation system that includes an organic Rankine cycle (ORC) including a working fluid that is thermally coupled to the heating fluid circuit to heat the working fluid, an expander configured to generate electrical power from the heated first working fluid, and a control system configured to activate a set of control valves to selectively thermally couple the heating fluid circuit to at least a portion of the heat sources. 1. A power generation system comprising: wherein a first subset of the plurality of heat sources comprises a plurality of diesel hydro-treating plant heat exchangers coupled to streams in the diesel hydro-treating plant,', 'wherein a second subset of the plurality of heat sources comprises a plurality of hydrocracking plant heat exchangers coupled to streams in the hydrocracking plant;, 'a heating fluid circuit thermally coupled to a plurality of heat sources from a plurality of sub-units of a petrochemical refining system, wherein the plurality of sub-units comprises a hydrocracking plant and a diesel hydro-treating plant,'}a first power generation system that comprises an organic Rankine cycle (ORC), the ORC comprising (i) a working fluid that is thermally coupled to the heating fluid circuit to heat the working fluid, and (ii) an expander configured to generate electrical power from the heated first working fluid; anda control system configured to activate a set of control valves to selectively thermally couple the ...

SYSTEMS AND METHODS FOR HYDROPROCESSING HEAVY OIL

A system and method for preparing and conditioning a heavy oil feedstock for hydroprocessing in a hydroprocessing system includes forming metal sulfide catalyst particles in situ within the heavy oil feedstock. The metal sulfide catalyst particles are formed in situ by (1) premixing a catalyst precursor with a hydrocarbon diluent to form a diluted precursor mixture, (2) mixing the diluted precursor mixture with the heavy oil feedstock to form a conditioned feedstock, and (3) heating the conditioned feedstock to decompose the catalyst precursor and cause or allow metal from the precursor to react with sulfur in the heavy oil feedstock to form metal sulfide catalyst particles in situ in the heavy oil feedstock. The in situ formed metal sulfide catalyst particles catalyze beneficial upgrading reactions between the heavy oil feedstock and hydrogen and eliminates or reduces formation of coke precursors and sediment. 1. A system for preparing and conditioning a heavy oil feedstock for hydroprocessing in a hydroprocessing system , comprising:a catalyst precursor;a hydrocarbon diluent;a heavy oil feedstock separate from the hydrocarbon diluent;a first mixing vessel configured for receiving and mixing the catalyst precursor with the hydrocarbon diluent below a temperature at which a significant portion of the catalyst precursor decomposes to form a diluted precursor mixture comprising mixture products of the catalyst precursor and the hydrocarbon diluent;a second mixing vessel, downstream from the first mixing vessel, configured for receiving and mixing the diluted precursor mixture with the heavy oil feedstock without heating to a temperature at which a substantial portion of the catalyst precursor decomposes to form a conditioned feedstock comprising mixture products of the catalyst precursor, the hydrocarbon diluent, and the heavy oil feedstock; anda heater, downstream from the second mixing vessel and upstream from a hydroprocessing reactor and/or that comprises the ...

UPGRADED EBULLATED BED REACTOR WITH INCREASED PRODUCTION RATE OF CONVERTED PRODUCTS

An ebullated bed hydroprocessing system is upgraded using a dual catalyst system that includes a heterogeneous catalyst and dispersed metal sulfide particles to increase rate of production of converted products. The rate of production is achieved by increasing reactor severity, including increasing the operating temperature and at least one of throughput or conversion. The dual catalyst system permits increased reactor severity and provides increased production of converted products without a significant increase in equipment fouling and/or sediment production. In some cases, the rate of production of conversion products can be achieved while decreasing equipment fouling and/or sediment production. 1. A method of upgrading an ebullated bed hydroprocessing system that includes one or more ebullated bed reactors to increase rate of production of converted products from heavy oil , comprising:operating an ebullated bed reactor using a heterogeneous catalyst to hydroprocess heavy oil at initial conditions, including an initial reactor severity and an initial rate of production of converted products;thereafter upgrading the ebullated bed reactor to operate using a dual catalyst system comprised of dispersed metal sulfide catalyst particles and heterogeneous catalyst; andoperating the upgraded ebullated bed reactor using the dual catalyst system at higher reactor severity and increased rate of production of converted products than when operating the ebullated bed reactor at the initial conditions.2. The method of claim 1 , wherein the heavy oil comprises at least one of heavy crude oil claim 1 , oil sands bitumen claim 1 , residuum from refinery processes claim 1 , atmospheric tower bottoms having a nominal boiling point of at least 343° C. (650° F.) claim 1 , vacuum tower bottoms having a nominal boiling point of at least 524° C. (975° F.) claim 1 , resid from a hot separator claim 1 , resid pitch claim 1 , resid from solvent extraction claim 1 , or vacuum residue3. The ...

UPGRADED EBULLATED BED REACTOR USED WITH OPPORTUNITY FEEDSTOCKS

An ebullated bed hydroprocessing system is upgraded using a dual catalyst system that includes a heterogeneous catalyst and dispersed metal sulfide particles to hydroprocess opportunity feedstocks (i.e., lower quality heavy oils or lower quality feedstock blends) while maintaining or increasing the rate of production of converted products. The dual catalyst system improves the ability of the upgraded ebullated bed hydroprocessing system to accommodate and withstand negative effects of periodic use of opportunity feedstocks (e.g., without significantly increasing equipment fouling and/or sediment production). In some cases, an upgraded ebullated bed reactor using the dual catalyst system can hydroprocess opportunity feedstocks while decreasing equipment fouling and/or sediment production. 1. A method of upgrading an ebullated bed hydroprocessing system that includes one or more ebullated bed reactors to hydroprocess lower quality heavy oil , comprising:initially operating an ebullated bed reactor using a heterogeneous catalyst to hydroprocess an initial heavy oil feedstock at an initial rate of production of converted products;thereafter upgrading the ebullated bed reactor to operate using a dual catalyst system comprised of dispersed metal sulfide catalyst particles and heterogeneous catalyst; andoperating the upgraded ebullated bed reactor using the dual catalyst system to hydroprocess a lower quality heavy oil and/or a lower quality feedstock blend while maintaining a rate of production of converted products at least as high as the initial rate.2. The method of claim 1 , wherein the lower quality heavy oil and/or the lower quality feedstock blend has at least one lower quality characteristic compared to the initial heavy oil feedstock selected from claim 1 , but not limited to:higher boiling point;higher concentration of sulfur;higher concentration of nitrogen;higher concentration of metals;higher molecular weight;lower hydrogen to carbon ratio;higher asphaltene ...

Systems for recovery and re-use of waste energy in crude oil refining and aromatics complex

Configurations and related processing schemes of specific inter-plants and hybrid, intra- and inter-plants waste heat recovery schemes for thermal energy consumption reduction in integrated refining-petrochemical facilities synthesized for grassroots medium grade crude oil semi-conversion refineries to increase energy efficiency from specific portions of low grade waste heat sources are described. Configurations and related processing schemes of specific inter-plants and hybrid, intra- and inter-plants waste heat recovery schemes for thermal energy consumption reduction in integrated refining-petrochemical facilities synthesized for integrated medium grade crude oil semi-conversion refineries and aromatics complex for increasing energy efficiency from specific portions of low grade waste sources are also described.

PROCESS AND APPARATUS FOR SELECTIVELY HYDROGENATING NAPHTHA

The process and apparatus of the present invention selectively hydrogenates a heavier olefinic naphtha stream in an upstream catalyst bed and the hydrogenated effluent and a lighter olefinic naphtha stream in a downstream catalyst bed. The heavier di-alkenes are less re-active and are contacted with more hydrogenation catalyst than the lighter di-alkenes which are more re-active. 1. A process for selective hydrogenation comprising:mixing hydrogen with a heavy naphtha stream containing di-alkenes and having a first end point;selectively hydrogenating said heavy naphtha stream over a hydrogenation catalyst to produce a heavy hydrogenated naphtha stream with a lower concentration of di-alkenes;adding a lighter naphtha stream containing di-alkenes and having a second end point that is lower than the first end point to the heavy hydrogenated naphtha stream; andselectively hydrogenating the heavy hydrogenated naphtha stream and the lighter naphtha stream over hydrogenation catalyst to produce a product naphtha stream depleted of di-alkenes.2. The process of further including separating a naphtha stream into said lighter naphtha stream and said heavy naphtha stream.3. The process of wherein the cut point between said lighter naphtha stream and said heavy naphtha stream is between about 55° and about 75° C.4. The process of further comprising hydrodesulfurizing said product naphtha stream over a hydrodesulfurization catalyst.5. The process of further comprising contacting said naphtha stream with an alkaline stream to produce sulfides before the separation step.6. The process of further comprising separating said naphtha stream into a light naphtha stream claim 2 , an intermediate naphtha stream which is said lighter naphtha stream claim 2 , and said heavy naphtha stream.7. The process of further comprising selectively hydrogenating said light naphtha stream separately from selectively hydrogenating the heavy naphtha stream and the lighter hydrogenated naphtha stream to ...

PROCESS FOR HYDRODESULPHURIZING AN OLEFINIC GASOLINE

A process for the treatment of a gasoline containing sulphur-containing compounds, olefins and diolefins: 1. A process for the treatment of a gasoline containing sulphur-containing compounds , olefins and diolefins , comprising the following steps: a light gasoline cut LCN;', 'a primary intermediate gasoline cut, MCN; and', 'a primary heavy gasoline cut HHCN;, 'a) fractionating the gasoline into at least{'sup': −1', '3', '3', '3', '3', '3', '3, 'b) desulphurizing the primary intermediate gasoline cut MCN alone and in the presence of a hydrodesulphurization catalyst and hydrogen, at a temperature in the range 160° C. to 450° C., at a pressure in the range 0.5 to 8 MPa, with a liquid space velocity in the range 0.5 to 20 hand with a ratio between the flow rate of hydrogen, expressed in normal mper hour, and the flow rate of feed to be treated, expressed in mper hour under standard conditions, in the range 50 Nm/mto 1000 Nm/min a manner such as to produce an at least partially desulphurized primary intermediate gasoline cut MCN;'}{'sup': −1', '3', '3', '3', '3', '3', '3, 'c) desulphurizing the primary heavy gasoline cut HHCN alone in the presence of a hydrodesulphurization catalyst and hydrogen, at a temperature in the range 200° C. to 450° C., at a pressure in the range 0.5 to 8 MPa, with a liquid space velocity in the range 0.5 to 20 hand with a ratio between the flow rate of hydrogen, expressed in normal mper hour, and the flow rate of feed to be treated, expressed in mper hour under standard conditions, in the range 50 Nm/mto 1000 Nm/min a manner such as to produce an at least partially desulphurized primary heavy gasoline cut HHCN;'}{'sub': '2', 'd) sending, as a mixture, the partially desulphurized primary intermediate gasoline cut MCN which has not undergone treatment following step b) and the partially desulphurized primary heavy cut HHCN which has not undergone treatment following step c) to a separation column in order to separate a gaseous stream containing ...

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

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

PROCESS FOR PRODUCING HYDROCARBONS

The present invention relates to a process for converting feedstock comprising materials of biological origin into hydrocarbons, said process comprising the steps where a) feedstock comprising at least one material of biological origin is subjected to purification treatment to obtain purified feedstock, and b) the purified feedstock is subjected to hydroprocessing in the presence of at least one hydrodeoxygenation catalyst, at least one hydrodewaxing catalyst and at least one hydrodearomatization catalyst to obtain a hydroprocessing product. 1. A process for converting feedstock comprising materials of biological origin to hydrocarbons , said process comprising the steps wherefeedstock comprising at least one material of biological origin is subjected to purification treatment to obtain purified feedstock,the purified feedstock is subjected to hydroprocessing in the presence of at least one hydrodeoxygenation catalyst, at least one hydrodewaxing catalyst and at least one hydrodearomatization catalyst to obtain a hydroprocessing product.2. The process according to claim 1 , wherein the hydroprocessing is carried out in one step or in more than one steps.3. The process according to claim 1 , wherein the purification treatment comprises at least one purification step selected from filtration claim 1 , degumming claim 1 , bleaching claim 1 , solvent extraction claim 1 , hydrolysis claim 1 , ion-exchange resin treatment claim 1 , mild acid wash claim 1 , evaporative treatment claim 1 , and any combination thereof.4. The process according to claim 1 , wherein the purification treatment is evaporative treatment carried out in an evaporation unit comprising at least one evaporator claim 1 , preferably three or four evaporators.5. The process according to claim 1 , wherein the purified feedstock is subjected pretreatment carried out using super-critical extraction technology or with one or more guard beds.6. The process according to claim 5 , wherein the guard beds are ...

SYSTEM AND PROCESS FOR HYDROCRACKING AND HYDROGENATION

Herein disclosed is a method for hydrogenation comprising: supersaturating a hydrocarbonaceous liquid or slurry stream in a high shear device with a gas stream comprising hydrogen and optionally one or more C1-C6 hydrocarbons to form a supersaturated dispersion; and introducing the supersaturated dispersion into a reactor in the presence of a hydrogenation catalyst to generate a product stream. In some embodiments, the catalyst is present as a slurry or a fluidized or fixed bed of catalyst. In some embodiments, the hydrogenation catalyst is mixed with the hydrocarbonaceous liquid or slurry stream and the gas stream in the high shear device. In some embodiments, the method further comprises recycling at least a portion of an off gas from the reactor, recycling at least a portion of the product stream from the reactor, or both. Also disclosed herein is a system for hydrogenation. 1. A method for hydrogenation comprising:supersaturating a hydrocarbonaceous liquid or slurry stream in a high shear device with a gas stream comprising hydrogen and optionally one or more C1-C6 hydrocarbons to form a supersaturated dispersion;introducing the supersaturated dispersion into a reactor in the presence of a hydrogenation catalyst to generate a product stream.2. The method of wherein the catalyst is present as a slurry or a fluidized or fixed bed of catalyst.3. The method of wherein the hydrogenation catalyst is mixed with said hydrocarbonaceous liquid or slurry stream and said gas stream in the high shear device.4. The method of further comprising recycling at least a portion of an off gas from the reactor claim 1 , recycling at least a portion of the product stream from the reactor claim 1 , or both.5. The method of wherein said off gas comprises hydrogen claim 4 , and optionally one or more C1-C6 hydrocarbons claim 4 , and wherein said off gas is introduced into said high shear device.6. The method of wherein said product stream comprises an improved product distribution of ...

PROCESS FOR THE CATALYTIC CONVERSION OF MICRO CARBON RESIDUE CONTENT OF HEAVY HYDROCARBON FEEDSTOCKS AND A LOW SURFACE AREA CATALYST COMPOSITION FOR USE THEREIN

An improved process for the hydroconversion of micro carbon residue content of heavy hydrocarbon feedstocks by the use of a catalyst composition that is especially useful in the conversion of micro carbon residue of such feedstocks. The catalyst composition is a low surface area composition that further has a specifically define pore structure the combination of which provides for its enhance micro carbon residue conversion property. 1. A process for converting at least a portion of an MCR content of a heavy hydrocarbon feedstock to yield a product having a reduced MCR content , wherein said process includes contacting said heavy hydrocarbon feedstock with a catalyst under MCR conversion process conditions and yielding said product , wherein the improvement comprises: enhancing the conversion of said MCR content of said heavy hydrocarbon feedstock by using as said catalyst in said process a calcined particulate of a co-mulled mixture comprising a molybdenum component , a nickel component , pseudo-boehmite powder , and a mineral acid , wherein said calcined particulate is prepared under conditions so that it has specifically defined physical properties including: (a) a total surface area of greater than 160 m/g and less than 240 m/g; (b) a median pore diameter (measured by mercury intrusion) in the range of from 85 Å to 120 Å; (c) from 5% to 30% of the total pore volume of said calcined particulate in the macropores having a pore diameter of 250 Å or greater; and (d) no more than 60% of the total pore volume of said calcined particulate within its pores having a diameter in the range of from 55 Å to 115 Å.2. A catalyst suitable for use in the catalytic conversion of an MCR content of a heavy hydrocarbon feedstock , wherein said catalyst comprises: a calcined particulate of a co-mulled mixture , wherein said co-mulled mixture comprises a molybdenum component , a nickel component , pseudo-boehmite powder , and a mineral acid , and wherein said calcined particulate is ...

Fuel composition for gci engines and method of production

GCI fuel compositions and methods of making them are described. The GCI fuel compositions comprises a fuel blend having an initial boiling point in a range of about 26° C. to about 38° C. and a final boiling point in a range of about 193° C. to less than 250° C., a density of about 0.72 kg/l to about 0.8 kg/l at 15° C., a research octane number of about 70 to about 85, and a cetane number of less than about 27, the fuel blend comprising a naphtha stream and a kerosene stream.

PRODUCTION OF OILFIELD HYDROCARBONS

A process to produce olefinic products suitable for use as or conversion to oilfield hydrocarbons includes separating an olefins-containing Fischer-Tropsch condensate into a light fraction, an intermediate fraction and a heavy fraction, oligomerising at least a portion of the light fraction to produce a first olefinic product which includes branched internal olefins, and carrying out either one or both of the steps of (i) dehydrogenating at least a portion of the intermediate fraction to produce an intermediate product which includes internal olefins and alpha-olefins, and synthesising higher olefins from the intermediate product which includes internal olefins and alpha-olefins to produce a second olefinic product, and (ii) dimerising at least a portion of the intermediate fraction to produce a second olefinic product. At least a portion of the heavy fraction is dehydrogenated to produce a third olefinic product which includes internal olefins. Also provided is a process to produce paraffinic products suitable for use as or conversion to oilfield hydrocarbons which includes separating a Fischer-Tropsch wax into at least a lighter fraction and a heavier fraction, hydrocracking the heavier fraction to provide a cracked intermediate, and separating the cracked intermediate into at least a naphtha fraction, a heavier than naphtha paraffinic distillate fraction suitable for use as or conversion to oilfield hydrocarbons, and a bottoms fraction which is heavier than the paraffinic distillate fraction. 1. A process to produce paraffinic products for use as or conversion to oilfield hydrocarbons and to produce lubricant base oils , the process including{'sub': 23', '50', '50, 'separating a Fischer-Tropsch wax into a light fraction and a C-Cintermediate fraction and a C+ heavier fraction;'}{'sub': 23', '50, 'hydro-isomerising the C-Cintermediate fraction using a hydro-isomerisation catalyst to provide a hydro-isomerised intermediate product;'}separating the hydro-isomerised ...

CATALYST SUPPORT AND CATALYSTS PREPARED THEREFROM

A supported catalyst useful in processes for chemically refining hydrocarbon feedstocks is prepared, the catalyst comprising a metal from Group 6 of the Periodic Table, a metal from Groups 8, 9 or 10 and optionally phosphorous, wherein the metals, and phosphorous when present, are carried on a foraminous carrier or support, the carrier or support, preferably comprises porous alumina having a total pore volume (TPV) of about 0.6 cc/g to about 1.1 cc/g and comprising: (a) equal to or greater than about 78% to about 95% of TPV in pores having a diameter of less than about 200 Angstroms (Å); (b) greater than about 2% to less than about 19% of the TPV in pores having a diameter of about 200 (Å) to less than about 1000 Å; (c) equal to or greater than 3% to less than 12% of the TPV in pores having a diameter equal to or greater than about 1000 Å; and (d) a pore mode equal to or greater than about 90 Å and less than about 160 Å. Preferably the support exhibits a d50 greater than about 100 Å and less than about 150 Å. 2. The process of claim 1 , wherein the hydrocarbon feedstock comprises at least one member selected from the group consisting of atmospheric gas oils claim 1 , straight run gas oils claim 1 , and vacuum gas oils.3. The process of claim 1 , wherein the hydrocarbon feedstock comprises at least one member selected from the group consisting of demetallized oils and deasphalted vacuum residue.4. The process of claim 1 , wherein the hydrocarbon feedstock comprises at least one member selected from the group consisting of coker distillates and cat cracker distillates.5. The process of claim 1 , wherein the hydrocarbon feedstock comprises at least one member selected from the group consisting of shale oil claim 1 , tar sand oil and coal liquids.6. The process of claim 1 , wherein the hydrocarbon feedstock comprises deasphalted vacuum residue.7. The process of claim 1 , wherein the metal of Group 6 is molybdenum and the metal of Groups 8 claim 1 , 9 and 10 is selected ...

Method for Preparing Noble Metal Hydrogenation Catalyst, Noble Metal Hydrogenation Catalyst and Use Thereof

Disclosed are a method for preparing a noble metal hydrogenation catalyst comprising preparing a carrier from a molecular sieve having a 10-member ring structure and/or an amorphous porous material; preparing a noble metal impregnation solution from one or more of compounds of noble metals Pt, Pd, Ru, Rh, Re, and Ir and deionized water or an acid solution; and preparing noble metal impregnation solutions in a concentration gradient ranging from 0.05 to 5.0 wt % with deionized water, and sequentially impregnating the carrier with the impregnation solutions from low to high concentrations during the carrier impregnation process, or preparing a noble metal impregnation solution at a low concentration ranging from 0.05 to 0.5 wt % and impregnating the carrier by gradually increasing the concentration of the noble metal impregnation solution to 2.0 to 5.0 wt % in the impregnation process, followed by homogenization, drying, and calcination, as well as a noble metal hydrogenation catalyst, use thereof, and a method for preparing lubricant base oil. The catalyst according to the present invention has high activity and stability, and the produced lubricant base oil shows a high viscosity index and a low pour point. 1. A method for preparing a noble metal hydrogenation catalyst , characterized in that said method comprises:step 1: preparing a carrier from a molecular sieve having a 10-member ring structure and/or an amorphous porous material, wherein the molecular sieve having a 10-member ring structure is selected from one or more of ZSM-5, SAPO-11, EU-1, ITQ-13, ZSM-22, MCM-22, NU-87, and ZSM-23, the mass fraction of the amorphous porous material contained in the carrier is 10 to 90 wt %, and the mass faction of the molecular sieve having a 10-member ring structure contained therein is 5 to 80 wt %;step 2: preparing a noble metal impregnation solution from one or more of compounds of noble metals Pt, Pd, Ru, Rh, Re, and Ir and deionized water or an acid solution, wherein ...

METHODS AND SYSTEMS FOR OPTIMIZING MECHANICAL VAPOR COMPRESSION AND/OR THERMAL VAPOR COMPRESSION WITHIN MULTIPLE-STAGE PROCESSES

The present invention utilizes mechanical vapor compression and/or thermal vapor compression integrating compression loops across multiple process stages. A sequential network of compressors is utilized to increase the pressure and condensing temperature of the vapors within each process stage, as intra-vapor flow, and branching between process stages, as inter-vapor flow. Because the vapors available are shared among and between compressor stages, the number of compressors can be reduced, improving economics. Balancing vapor mass flow through incremental compressor stages which traverse multiple process stages by splitting vapors between compressor stages enables the overall vapor-compression system to be tailored to individual process energy requirements and to accommodate dynamic fluctuations in process conditions. 1. A multiple-stage , energy-integrated system comprising:(a) a plurality of process sub-systems collectively configured for continuously or semi-continuously converting a feedstock into one or more products, wherein said plurality of process sub-systems is configured to utilize vapor-liquid phase changes; and(b) a vapor-compression sub-system, wherein said vapor-compression sub-system includes at least a first vapor compressor and a second vapor compressor, wherein said first vapor compressor is a mechanical vapor compressor or a thermal vapor compressor, and wherein said second vapor compressor is a mechanical vapor compressor or a thermal vapor compressor,wherein said first and second vapor compressors are sequentially arranged and configured to increase pressure and condensing temperature of first vapors within a first process sub-system and second vapors within a second process sub-system that is physically separated from, but in flow communication with, said first process sub-system;wherein said first vapor compressor is in flow communication with said second process sub-system, or a third process sub-system, via a first compressed-vapor line, ...

METHOD FOR OPTIMIZING CATALYST LOADING FOR HYDROCRACKING PROCESS

The invention relates to a method for optimizing layered catalytic processes. This is accomplished by testing various catalysts with a compound found in a feedstock to be tested, to determine the facility of the catalyst in hydrogenating, hydrosulfurizing, or hydrodenitrogenating the molecule, and hence the feedstock. In a preferred embodiment, the Double Bond Equivalence of the feedstock and molecule are determined, and catalysts are pre-selected based upon their known ability to work with materials of this DBE value. In preferred embodiments, the layered catalysts include a demetallization catalyst, used before hydrocracking. In additional preferred embodiments, the test feedstock contains 500 ppmw or less asphaltenes, preferably C-asphaltenes. 1. A method for optimizing a layered catalytic process , comprising (i) contacting a model compound capable of (a) being hydrocracked , (b) being demetalized , and (c) hydrodenitrogenation , as at least one of (ii) hydrogenation , hydrosulfurization and hydrodenitrogenation to a plurality of catalysts to determine an optimal catalyst for each of (b) and (c) following by layering the optimal catalyst for each of (b) and (c) in a reaction chamber based on their activity reacting with said model compound , wherein said catalyst capable of demetallizing said model compound is placed at top of said reaction chamber , and (c) contacting a feedstock to the layered catalysts under condition favoring formation of lower weight hydrocarbon from said hydrocarbon containing feedstock , wherein said model compound boils in the range of 180° C.-520° C. and is selected from the group consisting of methylnaphthalene , dibenzothiophene , and alkylated or naphtalated derivative thereof , a basic nitrogen compound and a carbazole molecule.2. The method of claim 1 , further comprising determining double bond equivalence (DBE claim 1 ,) of said feedstock claim 1 , and contacting said model compound to a plurality of catalysts suitable for ...

PROCESS FOR THE HYDROCONVERSION OF HEAVY OILS

A process for the conversion of heavy oils comprising sending the heavy oil to hydrotreatment, of the high severity type, in the presence of high concentrations of a suitable hydrogenation catalyst dispersed in slurry phase, effected in a suitable solid accumulation reactor capable of operating stably in the presence of solids deriving from and generated by the feedstock charged, wherein the hydrogen or mixtures thereof is fed at suitable flow-rates and suitably distributed, obtaining the conversion products in vapour phase directly in the reactor. 1. A process for the hydroconversion of heavy oils , selected from crude oils , heavy crude oils , bitumens from tar sands , distillation residues , heavy distillation cuts , deasphalted distillation residues , vegetable oils , oils deriving from coke and oil shales , oils obtained from the thermodecomposition of waste products , polymers , biomasses , effected in a suitable solid accumulation reactor with a specific hydrogenation catalyst in slurry phase and with the introduction of hydrogen or a mixture of hydrogen and HS ,{'sub': '1', 'sup': 3', '3, 'comprising sending the heavy oil to a hydroconversion step with a high severity index, producing a quantity of products insoluble in tetrahydrofuran (THF) of at least 3 kg per ton of feedstock converted, and with a high concentration of a catalyst based on molybdenum in slurry phase, the quantity of molybdenum being at least 5 kg per mreferring to the reaction medium, effected in a reactor of the bubbling tower type, operating with an accumulation of solids in the reaction medium of at least 50 kg/mconsisting of coke and metallic sulphides deriving from the feedstock, wherein the hydrogen introduced is in a weight ratio of at least 0.3 with respect to the feedstock, obtaining the conversion products in vapour phase directly in the reactor.'}2. The process according to claim 1 , wherein the non-converted heavy oil remains constantly in the reaction medium.3. The process ...

Process to prepare middle distillates and base oils

A process to prepare a first middle distillates fraction, a second middle distillates fraction, a distillate base oil and a residual base oil by providing a Fischer-Tropsch product stream; separating the Fischer-Tropsch product stream to obtain at least a low boiling fraction, boiling below a temperature ranging from 300 to 450° C., and a high boiling fraction, boiling above a temperature ranging from 300 to 450° C.; subjecting the high boiling fraction to a hydrocracking/hydroisomerization step to obtain a partially isomerised product stream; separating the partially isomerised product stream to obtain a first middle distillates fraction, a heavy distillates fraction and a residual fraction, the residual fraction having a T5 wt. % boiling point between 400 and 650° C.; dewaxing the low boiling fraction to obtain a second middle distillates fraction; dewaxing the heavy distillates fraction to obtain a distillate base oil; and dewaxing the residual fraction to obtain a residual base oil.

SEQUENTIAL IMPREGNATION FOR NOBLE METAL ALLOY FORMATION

Methods are provided for forming noble metal catalysts comprising both platinum and a second Group VIII metal, such as palladium, with improved aromatic saturation activity. Instead of impregnating a catalyst with both platinum and another Group VIII metal at the same time, a sequential impregnation can be used, with the Group VIII metal being impregnated prior to platinum. It has been discovered that by forming a Group VIII metal-impregnated catalyst first, and then impregnating with platinum, the distribution of platinum throughout the catalyst can be improved. The improved distribution of platinum can result in a catalyst with enhanced aromatic saturation activity relative to a catalyst with a similar composition formed by simultaneous impregnation. 1. A method of making a supported catalyst , the method comprising:impregnating a support comprising at least one of a zeolitic support and a mesoporous support with a Group VIII metal salt, the Group VIII metal comprising Pd, Ni, Rh, Ir, Ru, Co, or a combination thereof;calcining the support under first effective calcining conditions to form a Group VIII metal-impregnated support;impregnating the Group VIII metal-impregnated catalyst with a platinum salt; andcalcining the Group VIII metal-impregnated catalyst under second effective calcining conditions to form a platinum- and Group VIII metal-impregnated catalyst,wherein the platinum- and Group VIII metal-impregnated catalyst comprises a combined amount of platinum and Group VIII metal of 0.1 wt %-5.0 wt % based on the weight of the catalyst.2. The method of claim 1 , wherein the support comprises a mesoporous M41S support.3. The method of claim 1 , wherein the Group VIII metal comprises palladium.4. The method of claim 3 , wherein the platinum- and Group VII metal-impregnated catalyst comprises a combined amount of platinum and palladium of 0.1 wt % to 2.0 wt %.5. The method of claim 3 , wherein the platinum- and palladium-impregnated catalyst comprises a platinum ...

PROCESS OF CONVERTING NATURAL PLANT OILS TO BIOFUELS

The conversion of renewable feedstock, particularly oil, into jet fuel and other high-value chemicals. The conversion comprises the processes of alkene metathesis, dehydrogenation, hydrogenation, and vacuum distillation. 1. A method of preparing a transportation fuel comprising:(a) Providing a renewable feedstock comprising an unsaturated fatty acid glyceryl ester;{'sub': 2', '5', '2', '5', '2', '5, '(b) contacting a mixture of the feedstock and C-Colefins with a metathesis catalyst whereby the unsaturated fatty acid glyceryl ester and C-Colefin undergo a cross-metathesis reaction, thereby forming a metathesis product comprising medium-chain fatty glyceryl esters, acyclic olefins, cyclic olefins, and optionally unreacted C-Colefins;'}{'sub': 2', '5, '(c) dehydrogenating the metathesis product in the presence of a hydrogenation catalyst and substantially less than a stoichiometric amount of hydrogen gas relative to the amount of unsaturated bonds in the metathesis product, thereby forming a dehydrogenated metathesis product comprising medium-chain fatty glyceryl esters, acyclic olefins, cyclic olefins, optionally unreacted C-Colefins, and aromatics;'}(d) hydrogenating the dehydrogenated metathesis product in the presence of a hydrogenation catalyst and hydrogen, thereby forming a hydrogenated mixture comprising medium-chain saturated fatty glyceryl esters, acyclic and cyclic saturated hydrocarbons, and aromatics,wherein the hydrogenated mixture, or a blend comprising at least 50% of the hydrogenated mixture and a fuel blendstock, meets or exceeds the specifications of jet fuel.2. The method of claim 1 , further comprising:(e) distilling the hydrogenated mixture,wherein at least one fraction obtained from the distilling of step (e), or a blend comprising at least 50% of the at least one fraction and a fuel blendstock, meets or exceeds the specifications of jet fuel.3. The method of claim 2 , wherein at least one other fraction obtained from the distilling of step (e) ...

Method for converting heavy hydrocarbon feedstocks

The invention concerns a process for the conversion of a heavy hydrocarbon feed, said process comprising the following steps: a) a step for hydroconversion of the heavy hydrocarbon feed in the presence of hydrogen in at least one or more three-phase reactors disposed in series or in parallel, containing at least one hydroconversion catalyst, so as to obtain a liquid effluent with a reduced Conradson carbon, metals, sulphur and nitrogen content, b) one or more optional steps for separating the effluent obtained from step a) in order to obtain at least one light liquid fraction boiling at a temperature of less than 350° C. and a heavy liquid fraction boiling at a temperature of more than 350° C., c) a step for hydroconversion of the liquid effluent obtained from the hydroconversion step a) in the case in which the separation step b) is not carried out, or of the heavy liquid fraction obtained from the separation step b) when said step b) is carried out, in the presence of hydrogen in at least one or more three-phase reactors disposed in series or in parallel and containing at least one hydroconversion catalyst, in which process the overall hourly space velocity employed is in the range 0.05 to 0.18 h −1 .

PROCESS FOR PREPARING HYDROCRACKING CATALYST

Process for preparing a sulphided hydrocracking catalyst comprising the steps of (a) treating an amorphous silica alumina carrier with one or more Group VIB metal components, one or more Group VIII metal components and a C-Cpolyhydric compound, (b) drying the treated catalyst carrier at a temperature of at most 200° C. to form an impregnated carrier, and (c) sulphiding the impregnated carrier to obtain a sulphided catalyst. 1. The process for preparing a sulphided hydrocracking catalyst comprising the steps of{'sub': 3', '12, '(a) treating an amorphous silica alumina carrier with one or more Group VIB metal components, one or more Group VIII metal components and a C-Cpolyhydric compound,'}(b) drying the treated catalyst carrier at a temperature of at most 200° C. to form an impregnated carrier, and(c) sulphiding the impregnated carrier to obtain a sulphided catalyst.2. The process according to claim 1 , wherein the C-Cpolyhydric compound is present in the sulphided catalyst in an amount of 3-30 wt %.3. The process according to or claim 1 , wherein the carrier further comprises a zeolite.4. The process according to claim 3 , wherein the carrier comprises an amount of 1 to 10 wt % of zeolite claim 3 , based on total weight of the carrier.5. The process according to claim 1 , wherein the C-Cpolyhydric compound is a sugar claim 1 , a sugar alcohol and/or a sugar acid.6. The process according to claim 5 , wherein the C-Cpolyhydric compound is sucrose and/or gluconic acid.7. A process for hydrocracking a hydrocarbon stream comprising contacting the hydrocarbon stream in the presence of hydrogen with catalyst prepared by a process according to .8. The process according to claim 7 , in which the catalyst is part of a stack of multiple catalyst beds wherein the other catalyst(s) in the stack is (are) alumina-based catalysts.9. The process according to claim 8 , wherein the catalyst prepared by a process is the bottom bed catalyst.10. The process according to claim 9 , ...

RECOVERY AND RE-USE OF WASTE ENERGY IN INDUSTRIAL FACILITIES

Configurations and related processing schemes of specific inter-plants and hybrid, intra- and inter-plants waste heat recovery schemes for thermal energy consumption reduction in integrated refining-petrochemical facilities synthesized for grassroots medium grade crude oil semi-conversion refineries to increase energy efficiency from specific portions of low grade waste heat sources are described. Configurations and related processing schemes of specific inter-plants and hybrid, intra- and inter-plants waste heat recovery schemes for thermal energy consumption reduction in integrated refining-petrochemical facilities synthesized for integrated medium grade crude oil semi-conversion refineries and aromatics complex for increasing energy efficiency from specific portions of low grade waste sources are also described. 1. A system comprising:a first plurality of oil refining plants in a crude oil refining facility, each of the first plurality of plants configured to perform at least one oil refining process;a second plurality of oil refining plants in the crude oil refining facility, each of the second plurality of plants configured to perform at least one oil refining process, the first plurality of plants being different from the second plurality of plants; flow a first plurality of streams in the first plurality of plants to a plurality of heat exchangers, wherein the first plurality of plants comprises an amine regeneration plant comprising an acid gas regenerator bottoms stream comprising a weak amine salt, an aromatics complex benzene extraction unit benzene column bottoms stream, a raffinate column bottom stream, a naphtha splitter column bottom stream, the aromatics complex comprising at least one of benzene, toluene or xylene, a sour water stripper plant comprising a stripper bottom stream, a sulfur recovery plant comprising an amine regenerator bottoms stream, a gas separation plant comprising a C3/C4 splitter column bottom stream and a de-ethanizer column ...

PRODUCTION OF OILFIELD HYDROCARBONS

A process () to produce olefinic products suitable for use as or conversion to oilfield hydrocarbons includes separating () an olefins-containing Fischer-Tropsch condensate () into a light fraction (), an intermediate fraction () and a heavy fraction (), oligomerising () at least a portion of the light fraction () to produce a first olefinic product () which includes branched internal olefins, and carrying out either one or both of the steps of (i) dehydrogenating () at least a portion of the intermediate fraction () to produce an intermediate product () which includes internal olefins and alpha-olefins, and synthesising () higher olefins from the intermediate product which includes internal olefins and alpha-olefins to produce a second olefinic product (), and (ii) dimerising () at least a portion of the intermediate fraction to produce a second olefinic product (). At least a portion of the heavy fraction () is dehydrogenated () to produce a third olefinic product () which includes internal olefins. Also provided is a process () to produce paraffinic products suitable for use as or conversion to oilfield hydrocarbons which includes separating () a Fischer-Tropsch wax () into at least a lighter fraction () and a heavier fraction (), hydrocracking () the heavier fraction () to provide a cracked intermediate (), and separating () the cracked intermediate () into at least a naphtha fraction (), a heavier than naphtha paraffinic distillate fraction () suitable for use as or conversion to oilfield hydrocarbons, and a bottoms fraction () which is heavier than the paraffinic distillate fraction (). 135-. (canceled)36. A process to produce olefinic products in the carbon range C-Csuitable for use as or conversion to oilfield hydrocarbons , the process comprising:{'sub': 5', '7', '8', '15', '16', '22, 'separating an olefins-containing Fischer-Tropsch condensate into a light fraction which is a C-Cfraction, an intermediate fraction which is a C-Cfraction which includes ...

HYDROGENATION CATALYST FOR HEAVY HYDROCARBON OIL, PRODUCTION METHOD FOR HYDROGENATION CATALYST FOR HEAVY HYDROCARBON OIL, AND HYDROGENATION METHOD FOR HEAVY HYDROCARBON OIL

The hydrogenation catalyst for heavy hydrocarbon oil, includes: as a carrier, phosphorous-zinc-containing alumina that contains 0.1% by mass to 4% by mass, in terms of oxide based on the carrier, of phosphorous and 1% by mass to 12% by mass, based on the carrier, of zinc oxide particles, and supporting, on the carrier, 8% by mass to 20% by mass, in terms of oxide based on the catalyst, of at least one selected from metals in Group 6 of the periodic table and 2% by mass to 6% by mass, in terms of oxide based on the catalyst, of at least one selected from metals in Groups 8 to 10 of the periodic table, and the average particle diameter of the zinc oxide particles being 2 μm to 12 μm. 1. A hydrogenation catalyst for heavy hydrocarbon oil using as a carrier phosphorous-zinc-containing alumina that contains 0.1% by mass to 4% by mass , in terms of oxide based on the carrier , of phosphorous and 1% by mass to 12% by mass , based on the carrier , of zinc oxide particles , and supporting , on the carrier , 8% by mass to 20% by mass , in terms of oxide based on the catalyst , of at least one selected from metals in Group 6 of the periodic table and 2% by mass to 6% by mass , in terms of oxide based on the catalyst , of at least one selected from metals in Groups 8 to 10 of the periodic table ,wherein the average particle diameter of the zinc oxide particles is 2 μm to 12 μm.2. A production method for a hydrogenation catalyst for heavy hydrocarbon oil , comprising:a step of preparing an alumina gel;a step of kneading the alumina gel with a phosphorous compound and a zinc compound such that 0.1% by mass to 4% by mass, in terms of oxide based on a carrier, of phosphorous, and 1% by mass to 12% by mass, based on a carrier, of zinc oxide particles having an average particle diameter of 2 μm to 12 μm are incorporated;a step of obtaining a phosphorous-zinc-containing alumina carrier by molding the obtained kneaded mixture, and drying and calcining a molded product; anda step of ...

BLOCK PROCESSING CONFIGURATIONS FOR BASE STOCK PRODUCTION FROM DEASPHALTED OIL

Systems and methods are provided for block operation during lubricant and/or fuels production from deasphalted oil. During “block” operation, a deasphalted oil and/or the hydroprocessed effluent from an initial processing stage can be split into a plurality of fractions. The fractions can correspond, for example, to feed fractions suitable for forming a light neutral fraction, a heavy neutral fraction, and a bright stock fraction, or the plurality of fractions can correspond to any other convenient split into separate fractions. The plurality of separate fractions can then be processed separately in the process train (or in the sweet portion of the process train) for forming fuels and/or lubricant base stocks. The separate processing can allow for selection of conditions for forming lubricant fractions, such as bright stock fractions, that have a cloud point that is lower than the pour point. 110.-. (canceled)11. A method for making lubricant base stock , comprising:performing solvent deasphalting using a C4+ solvent under effective solvent deasphalting conditions on a feedstock having a T5 boiling point of at least about 370° C., the effective solvent deasphalting conditions producing a yield of deasphalted oil of at least about 50 wt % of the feedstock;hydroprocessing at least a portion of the deasphalted oil under first effective hydroprocessing conditions comprising first hydrocracking conditions to form a hydroprocessed effluent, the at least a portion of the deasphalted oil having an aromatics content of at least about 50 wt %, the hydroprocessed effluent comprising a sulfur content of 300 wppm or less, a nitrogen content of 100 wppm or less, or a combination thereof;{'sub': 5', '5, 'separating the hydroprocessed effluent to form at least a fuels boiling range fraction, a first fraction having a Tdistillation point of at least 370° C., and a second fraction having a Tdistillation point of at least 370° C., the second fraction having a higher kinematic ...

REFORMATE HYDROTREATMENT METHOD

Provided is a reformate hydrotreatment method, the method comprising: under liquid phase hydrotreatment conditions, bringing the reformate and a catalyst having a catalytic hydrogenation effect into contact in a hydrogenation reactor, the hydrogen used in the hydrotreating process at least partially coming from the hydrogen dissolved in the reformate. According to the method of the present invention, the reformate separated from a reformate products separating tank can directly undergo liquid phase hydrotreatment; therefore not only can the hydrogen dissolved in the reformate be fully utilized, but the olefins in the reformate can also be removed, while eliminate the requirements for recycle hydrogen and a recycle device thereof. The reformate obtained by the method of the present invention reduces the bromine index to below 50 mgBr/100 g, and has an arene loss of less than 0.5 wt %. 1. A method for hydroprocessing reformate , comprising contacting reformate with a catalyst having a catalytic hydrogenation action under a liquid-phase hydroprocessing condition in a hydrogenation reactor , at least part of hydrogen gas for hydroprocessing is from dissolved hydrogen contained in the reformate.2. The method according to claim 1 , wherein the hydroprocessing is carried out in presence of supplemental hydrogen gas claim 1 , the supplemental hydrogen gas is hydrogen gas injected into the reformate in one time or in several times before contacting and/or during contacting.3. The method according to claim 2 , wherein the supplemental hydrogen gas is injected into the reformate through pores with an average pore diameter in nanometer size.4. The method according to claim 3 , wherein the supplemental hydrogen gas is injected into the reformate through pores with an average pore diameter in nanometer size by means of a mixing device claim 3 , the mixing device comprises at least one liquid passage for accommodating the reformate and at least one gas passage for accommodating ...

PROCESS AND APPARATUS FOR PRODUCING HYDROCARBONS

The invention relates to a process and an apparatus for producing hydrocarbon components in the presence of a hydrodesulphurization catalyst. The components obtained by the process are suitable for use as fuel composition as such or as an additive in fuel compositions, and in cosmetics or pharmaceutical products. 2. The fuel composition of claim 1 , wherein the fuel composition is selected from a group consisting of gasoline claim 1 , diesel claim 1 , naphtha and jet fuel.3. The fuel composition of claim 1 , wherein the fuel composition comprises a mixture of 1-isopropyl-4-methylbenzene claim 1 , 1-isopropyl-4-methylcyclohexane and 2 claim 1 ,6-dimethyloctane or isomers thereof.4. The fuel composition of claim 3 , wherein the fuel composition further comprises bicyclic C10 compounds.5. The fuel composition of claim 1 , wherein the fuel composition comprises polycyclic hydrocarbons claim 1 , monocyclic hydrocarbons claim 1 , acyclic hydrocarbons claim 1 , and aromatic hydro-carbons.6. The fuel composition of claim 1 , for use in cosmetics or pharmaceutical products.7. The fuel composition of claim 1 , for use as an additive in fuel compositions.8. A fuel composition comprising 10-15% polycyclic hydrocarbons claim 1 , 20-50% monocyclic hydrocarbons claim 1 , 7-15% acyclic hydrocarbons claim 1 , and 15-50% aromatic hydrocarbons.9. The fuel composition of claim 9 , comprising a mixture of 1-isopropyl-4-methylbenzene claim 9 , 1-isopropyl-4-methylcyclohexane and 2 claim 9 ,6-dimethyloctane or isomers thereof. This application is a divisional application of U.S. patent application Ser. No. 13/382,823, filed Jan. 6, 2012, which is a 371 of International Application No. PCT/FI2010/050573, filed Jul. 2, 2010, which claims priority to Finland Application No. 20095767, filed Jul. 7, 2009 and Finland Application No. 20105092, filed Feb. 2, 2010, the contents of which are incorporated hereby in their entirety.The present invention relates to a process and an apparatus for ...

CATALYST AND PROCESS FOR HYDROCONVERSION OF A HEAVY FEEDSTOCK

A hydroconversion catalyst comprising a Group VIB metal component, a Group VIII metal component and a carrier material is disclosed wherein the catalyst has a total pore volume of 0.5 to 0.9 cc/g; and a pore volume distribution such that greater than 60% of pore volume are in pores present as micropores of diameter between 55 and 115 Å, less than 0.12 cc/g of pore volume are in pores present at pores of diameter greater than 160 Å and greater than 5% of the total pore volume is in pores of diameter greater than 210 Å. 1. A hydroprocessing catalyst for treating heavy hydrocarbon feedstocks , wherein said catalyst comprises: a calcined particle comprising a co-mulled mixture made by co-mulling inorganic oxide powder or powders , solution or solutions containing molybdenum and Group VIII metals and optionally water , acid and flocculating agent , and then forming said co-mulled mixture into a particle that is calcined to thereby provide said calcined particle , said calcined particles having: a total pore volume of 0.5 to 0.9 cc/g; and a pore volume distribution such that greater than 60% of pore volume are in pores present as micropores of diameter between 55 and 115 Å , less than 0.12 cc/g of pore volume are in pores present at pores of diameter greater than 160 Å and greater than 5% of the total pore volume in pores of diameter greater than 210 Å.2. The catalyst of claim 1 , wherein said calcined particle has a shape comprising a first end claim 1 , a second end and a wall disposed between said ends claim 1 , said wall comprising 3 or 4 lobes formed in the length of the wall.3. The catalyst of claim 1 , wherein said inorganic oxide material is selected from the group consisting of alumina claim 1 , silica and alumina-silica.4. The catalyst of claim 1 , wherein said calcined mixture has a molybdenum content in the range of from 1 weight percent to 24 weight percent with the weight percent being based upon the molybdenum as MoOand the total weight of the calcined ...

Process for Hydrocracking of Hydrocarbon Streams and Pyrolysis Oils

A process for hydrocracking of a hydrocarbon stream includes contacting the hydrocarbon stream with a hydroprocessing catalyst in the presence of hydrogen to yield a hydrocarbon product which meets steam cracker requirements for boiling end point, and in additional embodiments, chloride content and olefin content. 1. A process for hydrocracking a hydrocarbon stream comprising:contacting the hydrocarbon stream with a hydroprocessing catalyst in the presence of hydrogen to yield a hydrocarbon product, wherein the hydrocarbon stream comprises heavy hydrocarbon molecules and one or more sulphides; andrecovering a treated hydrocarbon stream from the hydrocarbon product, wherein a concentration of the heavy hydrocarbon molecules in the treated hydrocarbon stream is less than a concentration of the heavy hydrocarbon molecules in the hydrocarbon stream due to hydrocracking of at least a portion of the heavy hydrocarbon molecules from the hydrocarbon stream during the step of contacting.2. The process of claim 1 , wherein the hydrocarbon stream further comprises one or more chloride compounds in a concentration of 5 ppm or more based on a total weight of the hydrocarbon stream claim 1 , wherein the treated hydrocarbon stream comprises the one or more chloride compounds in a concentration of less than 5 ppm based on a total weight of the treated hydrocarbon stream.3. The process of claim 1 , wherein the hydrocarbon stream further comprises one or more olefins claim 1 , wherein the treated hydrocarbon stream further comprises the one or more olefins in a concentration of less than 1 wt. % based on the total weight of the treated hydrocarbon stream.4. The process of claim 1 , further comprising:doping the hydrocarbon stream with the one or more sulphides, wherein the one or more sulphides are added to the hydrocarbon stream in an amount such that a sulphur content of the hydrocarbon stream is about 0.5 wt % to about 5 wt % based on the total weight of the hydrocarbon stream.5. ...

Process for Preparation of Hydrocracking Catalyst for Use in Hydrocracking of Hydrocarbon Streams

A process for activating and maintaining a catalyst for use in hydrocracking a hydrocarbon stream includes continuously contacting a hydrocarbon stream with a hydroprocessing catalyst in the presence of hydrogen. Sulphides and chloride compounds in the hydrocarbon stream are used such that the hydroprocessing catalyst has the ability to hydrogenate, dechlorinate, and hydrocrack components of the hydrocarbon stream. 1. A process for activating and maintaining a catalyst for use in hydrotreating a hydrocarbon stream to simultaneously reduce heavier boiling components , chlorides , and olefins , comprising:continuously contacting the hydrocarbon stream with a hydroprocessing catalyst in the presence of hydrogen, wherein the hydrocarbon stream comprises one or more chloride compounds and one or more sulphides.2. The process of claim 1 , wherein the one or more sulphides comprise dimethyl disulphide claim 1 , mercaptans claim 1 , carbon disulphide claim 1 , hydrogen sulphide claim 1 , or combinations thereof.3. The process of claim 1 , wherein the one or more sulfides of the hydrocarbon stream are present in an amount such that a sulphur content of the hydrocarbon stream is about 0.5 wt % to about 5 wt % based on a total weight of the hydrocarbon stream.4. The process of claim 1 , further comprising:before the step of continuously contacting the hydrocarbon stream with the hydroprocessing catalyst in the presence of hydrogen, contacting a catalyst activating stream with the hydroprocessing catalyst, wherein the catalyst activating stream comprises one or more sulphides.5. The process of claim 4 , wherein the one or more sulfides of the catalyst activating stream are present in an amount such that a sulphur content of the catalyst activating stream is about 0.5 wt % to about 5 wt % based on a total weight of the catalyst activating stream.6. The process of claim 4 , wherein after the step of contacting and during the step of continuously contacting claim 4 , the ...

EBULLATED BED PROCESS FOR HIGH CONVERSION OF HEAVY HYDROCARBONS WITH A LOW SEDIMENT YIELD

An ebullated bed process for the hydroconversion of heavy hydrocarbon feedstocks that provides for high conversion of the heavy hydrocarbon with a low sediment yield. The process uses for its catalyst bed small particles of a specifically defined shaped hydroprocessing catalyst which is contacted with the heavy hydrocarbon feedstock under hydroconversion conditions and yields a hydrocarbon conversion having a relatively low sediment content. 1. A process that uses an ebullated bed reactor system for the hydroconversion of a heavy hydrocarbon feedstock providing high conversion of said heavy hydrocarbon feedstock with a low sediment yield , wherein said process comprises:{'sup': −1', '−1, 'introducing said heavy hydrocarbon feedstock into an ebullated bed reaction zone contained within a reactor volume defined by an ebullated bed reactor vessel, wherein said reactor volume includes an upper zone above said ebullated bed reaction zone and a lower zone below said ebullated bed reaction zone; and wherein said ebullated bed reaction zone comprises a catalyst bed of shaped hydroprocessing catalyst particles having a geometry providing for a first ratio of the cross section perimeter-to-cross sectional area that is in the range of from 5 mmto 10 mm;'}contacting under hydroconversion reaction conditions said heavy hydrocarbon feedstock with said shaped hydroprocessing catalyst particles within said ebullated bed reaction zone; andyielding from said upper zone a heavy hydrocarbon conversion product having a low sediment content.2. A process as recited in claim 1 , wherein said geometry of said shaped hydroprocessing catalyst particles is that of a trilobe shape having a trilobe particle length and a nominal trilobe diameter.3. A process as recited in claim 2 , wherein said trilobe shape is further characterized by a second ratio of the trilobe cross sectional area-to-trilobe particle volume that is in the range of from 5 mmto 15 mm.4. A process as recited in claim 3 , ...

METHOD OF OPERATING AN EBULLATED BED PROCESS TO REDUCE SEDIMENT YIELD

An improved method of operating a conventional ebullated bed process for the hydroconversion of heavy hydrocarbon feedstocks so as to provide for low or reduced sediment content in the conversion product without the loss of hydrodesulfurization function. 1. A method of operating an ebullated bed process for the hydroconversion of a heavy hydrocarbon feedstock , wherein said method comprises:{'sup': '−1', 'providing an ebullated bed reactor system, comprising an ebullated bed reactor vessel that defines a reactor volume within which is an ebullated bed reaction zone defined by a catalyst bed comprising first shaped hydroprocessing catalyst particles having a first geometry providing for a first ratio of the cross section perimeter-to-cross sectional area that is less than 5 mm, and wherein said reactor volume further includes an upper zone above said ebullated bed reaction zone and a lower zone below said ebullated bed reaction zone;'}introducing said heavy hydrocarbon feedstock into said ebullated bed reaction zone, which is operated under hydroconversion reaction conditions;removing a portion of said first shaped hydroprocessing catalyst particles from said catalyst bed;{'sup': '−1', 'adding to said catalyst bed an incremental amount of a second shaped hydroprocessing catalyst particles having a second geometry providing for a second ratio of the cross section perimeter-to-cross sectional area that is at least 5 mm; and'}yielding from said reactor volume a heavy hydrocarbon conversion product having a reduced sediment content.2. The method of claim 1 , wherein said first shaped hydroprocessing catalyst particles comprise an inorganic oxide powder in an amount in the range of from about 75 wt. % to 96 wt. % claim 1 , a molybdenum compound in an amount in the range of from 3 wt. % to 15 wt. % claim 1 , and a nickel compound in an amount in the range of from 0.5 wt. % to 6 wt. % claim 1 , wherein each wt. % is based on the total weight of said first shaped ...

MULTI-BED REACTOR WITH MIXING DEVICE

A mixing device mounted between two catalyst beds in a multi-bed catalytic reactor with a cylindrical shape. The mixing device has a circular outer rim which corresponds to the inner wall of the reactor, and includes a collecting section for collecting fluid from an up-stream catalytic bed, a mixing section for mixing the collected fluid, and a discharging section for discharging the mixed fluid to a down-stream catalytic bed. The collecting section, the mixing section and the discharging section are disposed outside the center of the circular cross-section of the reactor.

METHOD OF PROCESSING HEAVY OILS AND RESIDUA

There is provided a process of treating a heavy hydrocarbon-comprising material, comprising: contacting a feed material with at least a catalyst material within a contacting zone to effect generation of a total product such that a contacting zone material is disposed within the contacting zone and consists of the catalyst material and a feed/product-comprising mixture comprising the feed material and the total product, wherein the feed/product-comprising mixture includes a Conradson carbon residue content of at least 12 weight percent, based on the total weight of the feed/product-comprising mixture, and also includes an asphaltene content of less than two (2) weight percent, based on the total weight of the feed/product-comprising mixture, and wherein the feed material includes deasphalted heavy hydrocarbon-comprising material. A heavy hydrocarbon-containing feed for a catalytic hydroprocessing or catalytic hydrocracking process is also provided, wherein the feed comprises a deasphalted heavy hydrocarbon-comprising material having a Conradson carbon residue, CCR, content greater than about 12 wt % and an asphaltene content less than about 2 wt %. The feed results in reduced catalyst deactivation or catalyst coking during the catalytic hydroprocessing or catalytic hydrocracking process. 1. A process of treating a heavy hydrocarbon-comprising material , comprising: contacting a feed material with at least a catalyst material within a contacting zone to effect generation of a total product such that a contacting zone material is disposed within the contacting zone and consists of the catalyst material and a feed/product-comprising mixture comprising the feed material and the total product , wherein the feed/product-comprising mixture includes a Conradson carbon residue content of at least 12 weight percent , based on the total weight of the feed/product-comprising mixture , and also includes an asphaltene content of less than two weight percent , based on the total ...

Process for producing lpg and btx

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

SYSTEM AND PROCESS FOR INCREASING HEAVY OILS CONVERSION CAPACITY

System and corresponding process for the hydroconversion of heavy oils essentially comprising a reactor, a liquid-vapor separator and a section for stripping conversion products outside the reactor comprising an inlet conduit for the stripping gases located at a point on the conduit providing a connection between the head of the reactor and the liquid-vapor separator inclined, at least from the point of entry, upwards with a gradient of between 2% and 20%, preferably between 3% and 12%, with respect to a horizontal plane. The inlet conduit for the stripping gases is inclined with respect to the axis of the conduit providing a connection between the reactor head and the liquid-vapor separator through an angle of between 20° and 65°, more preferably between 30° and 60°, even more preferably between 40° and 50°. The stripping gas delivered to the connection conduit between the head of the reactor and the separator flows in a downward direction. 2. The system according to claim 1 , wherein said supply conduit of the stripping gas is inclined to the axis of said connection conduit between said reactor head and said liquid-vapor separator at an angle of between 20° and 65°.3. The system according to claim 1 , wherein the stripping gas flow entering said connection conduit between said reactor head and said liquid-vapor separator is in a downward direction.4. The system according to claim 1 , wherein said supply conduit lies in the vertical plane passing through the axis of said connection conduit.5. The system according to wherein said reactor is a bubble column or ebullated bed reactor.6. The system according to claim 1 , wherein said connection conduit between said reactor head and said liquid-vapor separator claim 1 , at least from the point of supply of the stripping gas claim 1 , is inclined upward with a gradient of between 3% and 12%.7. The system according to claim 1 , wherein obstacles of suitable geometry are inserted inside said connection conduit between said ...

Heavy Oil Hydrotreating System and Heavy Oil Hydrotreating Method

A heavy oil hydrotreating system has a prehydrotreating reaction zone, a transition reaction zone, and a hydrotreating reaction zone that are connected in series successively, sensor units, and a control unit. In the initial reaction stage, the prehydrotreating reaction zone includes at least two prehydrotreating reactors connected in parallel, and the transition reaction zone includes or doesn't include prehydrotreating reactors; in the reaction process, the control unit controls material feeding to and material discharging from each prehydrotreating reactor in the prehydrotreating reaction zone according to pressure drop signals of the sensor units, so that when the pressure drop in any of the prehydrotreating reactors in the prehydrotreating reaction zone reaches a predetermined value, the prehydrotreating reactor in which the pressure drop reaches the predetermined value is switched from the prehydrotreating reaction zone to the transition reaction zone.

DUAL CATALYST SYSTEM FOR EBULLATED BED UPGRADING TO PRODUCE IMPROVED QUALITY VACUUM RESIDUE PRODUCT

An ebullated bed hydroprocessing system is upgraded using a dual catalyst system that includes a heterogeneous catalyst and dispersed metal sulfide particles to improve the quality of vacuum residue. The improved quality of vacuum residue can be provided by one or more of reduced viscosity, reduced density (increased API gravity), reduced asphaltene content, reduced carbon residue content, reduced sulfur content, and reduced sediment. Vacuum residue of improved quality can be produced while operating the upgraded ebullated bed reactor at the same or higher severity, temperature, throughput and/or conversion. Similarly, vacuum residue of same or higher quality can be produced while operating the upgraded ebullated bed reactor at higher severity, temperature, throughput and/or conversion. 1. A method of upgrading an ebullated bed hydroprocessing system that includes one or more ebullated bed reactors to improve vacuum residue quality , comprising:operating an ebullated bed reactor using a heterogeneous catalyst to hydroprocess heavy oil at an initial rate of production of converted products and produce an initial rate and quality of bottoms product;thereafter upgrading the ebullated bed reactor to operate using a dual catalyst system comprised of dispersed metal sulfide catalyst particles and heterogeneous catalyst; andoperating the upgraded ebullated bed reactor using the dual catalyst system to hydroprocess heavy oil at a rate of production of converted products at least as high as the initial rate and producing bottoms product with a higher quality than the initial quality.2. The method of claim 1 , wherein the heavy oil comprises at least one of heavy crude oil claim 1 , oil sands bitumen claim 1 , residuum from refinery processes claim 1 , atmospheric tower bottoms having a nominal boiling point of at least 343° C. (650° F.) claim 1 , vacuum tower bottoms having a nominal boiling point of at least 524° C. (975° F.) claim 1 , resid from a hot separator claim 1 , ...

Combined Hydrogenation Process Method for Producing High-Quality Fuel by Medium-Low-Temperature Coal Tar

A combined hydrogenation process method for producing high-quality fuel by medium-low-temperature coal tar, wherein a medium-low-temperature coal tar is fractionated to obtain a final product through a thermal hydrocracking unit, a first atmospheric fractionation unit, a hydro-refining, unit, a vacuum fractionation unit, a diesel and wax oil hydro-upgrading unit, a wax oil hydro-cracking unit, a gasoline and diesel precious metal hydrogenation unit and a fourth atmospheric fractionation unit. The present invention can effectively improve the quality of naphtha, aviation kerosene and diesel products, and produce high-end products with high yield and high value, and thus it has a great prospect of promotion and application.

PROCESS FOR THE REFINING OF CRUDE OIL

Process for the refining of crude oil comprising at least one atmospheric distillation unit for separating the various fractions, a sub-atmospheric distillation unit, a conversion unit of the heavy fractions obtained, a unit for enhancing the quality of some of the fractions obtained by actions on the chemical composition of their constituents and a unit for the removal of undesired components, characterized in that the sub-atmospheric distillation residue is sent to one of the conversion units, said conversion unit comprises at least one hydroconversion reactor in slurry phase, into which hydrogen or a mixture of hydrogen and ¾ S, is fed, in the presence of a suitable dispersed hydrogenation catalyst with dimensions ranging from 1 nanometer to 30 microns. 1. A process for the refining of crude oil comprising the following steps:feeding the crude oil to one or more atmospheric distillation units in order to separate various streams;feeding the heavy residue(s) separated in the atmospheric distillation unit(s), to the sub-atmospheric distillation unit, separating at least two liquid streams;{'sub': '2', 'feeding the vacuum residue separated in the sub-atmospheric distillation unit to the conversion unit comprising at least one hydroconversion reactor in slurry phase into which hydrogen or a mixture of hydrogen and HS is fed in the presence of a suitable dispersed hydrogenation catalyst with dimension ranging from 1 nanometer to 30 microns in order to obtain a product in vapour phase, which is subjected to one or more separation steps obtaining fractions in both vapour phase and liquid phase, and a by-product in slurry phase;'}feeding the lighter separated fraction obtained in the sub-atmospheric distillation unit to a hydrodesulfurization unit of light gasoils (HDS1);feeding the liquid fraction separated in the hydroconversion unit, having a boiling point higher than 350° C., to a hydrodesulfurization and/or hydrocracking unit of heavy gasoils (HDS/HDC);feeding the ...

Process and installation for the conversion of crude oil to petrochemicals having an improved carbon-efficiency

The present invention relates to an integrated process to convert crude oil into petrochemical products comprising crude oil distillation, hydrocracking and olefins synthesis, which process comprises subjecting a hydrocracker feed to hydrocracking to produce LPG and BTX and subjecting the LPG produced in the process to olefins synthesis. Furthermore, the present invention relates to a process installation to convert crude oil into petrochemical products comprising: a crude distillation unit comprising an inlet for crude oil and at least one outlet for one or more of naphtha, kerosene and gasoil; a hydrocracker comprising an inlet for a hydrocracker feed, an outlet for LPG and an outlet for BTX; and a unit for olefins synthesis comprising an inlet for LPG produced by the integrated petrochemical process installation and an outlet for olefins. The hydrocracker feed used in the process and the process installation of the present invention comprises one or more of naphtha, kerosene and gasoil produced by crude oil distillation in the process; and refinery unit-derived light-distillate and/or refinery unit-derived middle-distillate produced in the process. The process and process installation of the present invention have an increased production of petrochemicals at the expense of the production of fuels and an improved carbon efficiency in terms of the conversion of crude oils into petrochemicals.

BASE STOCKS AND LUBRICANT COMPOSITIONS CONTAINING SAME

Systems and methods are provided for block operation during lubricant and/or fuels production from deasphalted oil. During “block” operation, a deasphalted oil and/or the hydroprocessed effluent from an initial processing stage can be split into a plurality of fractions. The fractions can correspond, for example, to feed fractions suitable for forming a light neutral fraction, a heavy neutral fraction, and a bright stock fraction, or the plurality of fractions can correspond to any other convenient split into separate fractions. The plurality of separate fractions can then be processed separately in the process train (or in the sweet portion of the process train) for forming fuels and/or lubricant base stocks. This can allow for formation of unexpected base stock compositions. 114-. (canceled)15. A lubricant base stock composition comprising a viscosity index of 80 or more; a saturates content of 95 wt % or more; a sulfur content of 300 wppm or less; a kinematic viscosity at 100° C. of 8.5 cSt to 15 cSt; 2.8 wt % or less of 4+-ring naphthenes; and 9.0 epsilon carbon atoms or less per 100 carbon atoms in the composition.16. The composition of claim 15 , further comprising a cycloparaffin performance ratio of 1.20 to 1.34.17. The composition of claim 15 , further comprising 1.10 terminal and pendant propyl groups or more per 100 carbon atoms of the composition.18. The composition of claim 15 , further comprising 74.0 wt % or more of total naphthenes relative to the total weight of saturates and aromatics in the composition.19. The composition of claim 15 , further comprising 1.6 wt % or less of 4-ring naphthenes relative to the total weight of saturates and aromatics in the composition.20. The composition of claim 15 , wherein the composition comprises 2.6 wt % or less of 4+-ring naphthenes relative to the total weight of saturates and aromatics in the composition; or wherein the composition comprises 10.0 wt % or less of 3+-ring naphthenes; or a combination thereof. ...

使用高活性浆料催化剂组合物进行重油改质的方法

申请人开发了新的渣油完全加氢转化浆料反应器系统，该系统允许所述催化剂、未转化的油和转化了的油以连续混合物的形式循环遍及整个反应器，而对所述混合物没有限制。所述混合物在所述反应器之间被部分分离以仅移出所述产物和氢气，而允许未转化的油和浆料催化剂继续进入下一个后续反应器。然后将一部分未转化的油转化成较低沸点的烃，再次产生未转化的油、产物、氢气和浆料催化剂的混合物。可以在另外的反应器中进行进一步加氢处理，完全转化所述油。可以将额外的油加入到级间原料入口，原料有可能与浆料混合。可以交替地部分转化所述油，留下位于未转化的油中的高度浓缩的催化剂，可将其直接再循环到所述第一反应器中。

Upgraded ebullated bed reactor with increased production rate of converted products

An ebullated bed hydroprocessing system is upgraded using a dual catalyst system that includes a heterogeneous catalyst and dispersed metal sulfide particles to increase rate of production of converted products. The rate of production is achieved by increasing reactor severity, including increasing the operating temperature and at least one of throughput or conversion. The dual catalyst system permits increased reactor severity and provides increased production of converted products without a significant increase in equipment fouling and/or sediment production. In some cases, the rate of production of conversion products can be achieved while decreasing equipment fouling and/or sediment production.

Process for increased olefin yields from heavy feedstocks

A process for upgrading petroleum feedstocks boiling in the distillate plus range, which feedstocks, when cracked, result in unexpected high yields of olefins. The feedstock is hydroprocessed in at least one reaction zone countercurrent to the flow of a hydrogen-containing treat gas. The hydroprocessed feedstock is then subjected to thermal cracking in a steam cracker or to catalytic cracking in a fluid catalytic cracking process. The resulting product slate will contain an increase in olefins compared with the same feedstock, but processed in by a conventional co-current hydroprocessing process.

Дизельное топливо унифицированное всесезонное

Изобретение раскрывает дизельное топливо унифицированное всесезонное на основе среднедистиллятных нефтяных фракций, содержащее в качестве базового компонента изодепарафинизированную дизельную фракцию, выкипающую в интервале 174-334°С, и противоизносную присадку в количестве 0,015-0,020 мас.%, добавленную на базовый компонент. Технический результат: применение данного топлива приведет к значительному снижению затрат при его производстве, транспортировании, хранении и эксплуатации техники, в том числе судовой, с возможностью его использования на всей территории Российской Федерации. 4 табл. РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 655 606 C1 (51) МПК C10G 45/58 (2006.01) C10L 1/00 (2006.01) C10L 1/04 (2006.01) C10G 65/02 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК C10G 45/58 (2018.02); C10L 1/00 (2018.02); C10L 1/04 (2018.02); C10G 65/00 (2018.02) (21)(22) Заявка: 2017127593, 02.08.2017 (24) Дата начала отсчета срока действия патента: Дата регистрации: 29.05.2018 (45) Опубликовано: 29.05.2018 Бюл. № 16 2 6 5 5 6 0 6 R U (56) Список документов, цитированных в отчете о поиске: RU 2559877 C1, 20.08.2015. RU 2549617 C1, 27.04.2015. RU 2623088 C1, 22.06.2017. А.В. Камешков и др. Получение дизельных топлив с улучшенными низкотемпературными свойствами (обзор). Известия Санкт-Петербургского государственного технологического института (технического университета), 2015, 29(55),49-60. EP 2078744 A1 15.07.2009. US 6773578 B1 (см. прод.) (54) ДИЗЕЛЬНОЕ ТОПЛИВО УНИФИЦИРОВАННОЕ ВСЕСЕЗОННОЕ (57) Реферат: Изобретение раскрывает дизельное топливо 0,020 мас.%, добавленную на базовый компонент. унифицированное всесезонное на основе Технический результат: применение данного среднедистиллятных нефтяных фракций, топлива приведет к значительному снижению содержащее в качестве базового компонента затрат при его производстве, транспортировании, изодепарафинизированную дизельную фракцию, хранении и эксплуатации техники, в том числе ...

Method of producing hydrocarbon mixtures with high octane number via hydrogenation of hydrocarbon mixtures which contain fractions of branched olefins

FIELD: chemistry. ^ SUBSTANCE: method of producing hydrocarbon mixtures with high octane number via hydrogenation of hydrocarbon mixtures which contain fractions of branched C8, C12 and C16 olefins is characterised by supply of the said mixture as it is or fractionated into two streams, one mainly containing a fraction of branched C8 olefins, and the other mainly containing a fraction of branched C12 and C16 olefins, into a hydrogenation zone or into two parallel hydrogenation zones respectively. Only the stream which mainly contains saturated C8 hydrocarbons, obtained via fractionation of a stream produced in one hydrogenation zone or obtained from the hydrogenation zone fed by the fractionated stream which mainly contains a fraction of branched C8 olefins, is at least partially recycled back to one hydrogenation zone or the hydrogenation zone fed by the fractionated stream which mainly contains a fraction of branched C8 olefins, and a hydrocarbon mixture with high octane number is obtained by fractionating the stream produced in one hydrogenation zone or obtained from the hydrogenation zone fed by the fractionated stream which mainly contains branched C12 and C16 olefins. ^ EFFECT: novel method of producing hydrocarbon mixtures with high octane number. ^ 11 cl, 3 ex, 3 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2 377 277 (13) C2 (51) МПК C10G 65/14 (2006.01) C10G 69/12 (2006.01) C10G 50/00 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ, ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (21), (22) Заявка: 2006111054/04, 06.10.2004 (24) Дата начала отсчета срока действия патента: 06.10.2004 R U (30) Конвенционный приоритет: 10.10.2003 IT MI2003A 001951 (72) Автор(ы): КАТАНИ Роберто (IT), ДИ ДЖИРОЛАМО Марко (IT), КОНТЕ Массимо (IT), ГУСБЕРТИ Амброджио (IT) (73) Патентообладатель(и): Снампроджетти С.п.А. (IT) (43) Дата публикации заявки: 20.11.2007 2 3 7 7 2 7 7 (45) Опубликовано: 27.12.2009 Бюл. № 36 (56) Список документов, цитированных в ...

Method and equipment for multi-stage liquefying of carbon-containing solid fuel

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

ｐ-자일렌의 제조를 위한 통합공정

본 발명은 하기 단계를 포함하는 p-자일렌의 제조를 위한 통합공정을 제공한다: A) 벤젠, 톨루엔, C 8 방향족 탄화수소, C 9 및 그 이상의 방향족 탄화수소, 및 비-방향족 탄화수소를 함유하는 혼합 원료를 개질 유닛(reforming unit)으로부터 분리하여, 제1 벤젠 스트림, 제1 톨루엔 스트림, 제1 C 8 방향족 탄화수소 스트림, C 9 및 그 이상의 방향족 탄화수소 스트림, 및 비-방향족 탄화수소 스트림을 얻는 단계; B) 단계 A)로부터의 C 9 및 그 이상의 방향족 탄화수소 스트림을 수소의 존재하에서 탈알킬화 반응이 일어나는 C 9 및 그 이상의 방향족 탄화수소 탈알킬화 유닛에 공급하고, 반응 방출액을 분리하여 제2 벤젠 스트림, 제2 톨루엔 스트림 및 제2 C 8 방향족 탄화수소 스트림을 얻는 단계; C) 수소의 존재하에서 톨루엔 선택적 불균등화 반응이 일어나는 톨루엔 선택적 불균등화 유닛에 상기 제1 톨루엔 스트림과 제2 톨루엔 스트림을 모두 공급하여 p-자일렌과 벤젠을 포함하는 C 8 방향족 탄화수소를 함유하는 스트림을 제조하는 단계로서, 이 스트림은 분리되어 제3 C 8 방향족 탄화수소 스트림, 제3 톨루엔 스트림, 및 제3 벤젠 스트림이 얻어지고, 상기 제3 톨루엔 스트림은 이 유닛의 입구로 반송되는, 단계; D) 제1 C 8 방향족 탄화수소 스트림 및 제2 C 8 방향족 탄화수소 스트림을 흡착분리 유닛에 공급하여 제1 p-자일렌 생성물 스트림과 제5 C 8 방향족 탄화수소 스트림을 얻고, 상기 제5 C 8 방향족 탄화수소 스트림은 이성체화 유닛으로 이송되는 단계; E) 제3 C 8 방향족 탄화수소 스트림을 결정화 분리 유닛에 공급하여 제4 C 8 방향족 탄화수소 스트림과 제2 p-자일렌 생성물 스트림을 얻고, 상기 제4 C 8 방향족 탄화수소 스트림은 상기 흡착분리 유닛 또는 이성체화 유닛으로 이송되는 단계; 및 F) 이성체화 유닛의 방출액을 흡착분리 유닛의 입구에 공급하는 단계. p-자일렌, 벤젠, 불균등화 공정, 톨루엔 선택적 불균등화 반응, 결정화, 이성체화

Method for obtaining hydrocarbons

FIELD: chemistry.SUBSTANCE: invention relates to a method for converting feedstock comprising materials of biological origin into hydrocarbons. Method for converting feedstock comprising materials of biological origin into hydrocarbons comprises steps, where feedstock comprising at least one material of biological origin is subjected to purification to obtain purified feedstock, the purified feedstock is subjected to hydroprocessing in two steps, wherein at the first hydroprocessing step, the purified feedstock is brought into contact with at least one hydrodeoxygenation catalyst comprising NiMo, CoMo or mixture Ni, Mo and Co, and with at least one hydrodewaxing catalyst including NiW, at a temperature of 330-430°C, to obtain a product of the first hydroprocessing step. At the second hydroprocessing step, the product of the first hydroprocessing step is brought into contact with a hydrodearomatisation catalyst comprising metals selected from Pt, Pd, Ir, Ru, Rh, Re, Ni, Co, Mo, W, CoMo, NiMo and NiW, at a temperature of 180-350°C, wherein the temperature at the second step is lower than at the first step, to obtain a hydroprocessing product, and hydrodearomatisation is carried out after hydrodeoxygenation and hydrodewaxing.EFFECT: technical result is the production of hydrocarbons with low aromatic content.21 cl, 2 dwg, 1 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 663 669 C2 (51) МПК C10G 3/00 (2006.01) C10G 45/44 (2006.01) C10G 45/46 (2006.01) C10G 65/08 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК C10G 3/00 (2006.01); C10G 45/44 (2006.01); C10G 45/46 (2006.01); C10G 65/08 (2006.01) (21)(22) Заявка: 2016102730, 11.07.2014 (24) Дата начала отсчета срока действия патента: Дата регистрации: 08.08.2018 12.07.2013 FI 20135770 (43) Дата публикации заявки: 16.08.2017 Бюл. № 23 (56) Список документов, цитированных в отчете о поиске: WO 2012/069706 A2, 31.05.2012. US 2013/0067801 A1, 21.03.2013. RU 2464297 C2, ...

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

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

Improved method of converting heavy hydrocarbon feedstock

FIELD: chemistry. SUBSTANCE: present invention relates to a method of converting a heavy hydrocarbon feedstock, involving the following steps: a) a step for hydroconversion of heavy hydrocarbon material in the presence of hydrogen in at least one or more three-phase reactors, installed in series or in parallel, containing at least one hydroconversion catalyst, wherein step a) of hydroconversion is carried out at absolute pressure of 2 to 35 MPa, temperature of 300 to 550 °C and with amount of hydrogen mixed with raw material from 50 to 5000 normal cubic meters (Nm 3 ) per cubic meter (m 3 ) of raw material to obtain a liquid stream with reduced content of coke residue according to Conradson, metals, sulphur and nitrogen, b) one or more optional steps of separating the stream coming from step a), allowing to obtain at least one light liquid fraction boiling at temperature below 350 °C, and at least one heavy liquid fraction boiling at temperature higher than 350 °C, c) stage of hydroconversion of liquid flow leaving hydroconversion stage a), in case, when b) separation is not applied, or stage of hydroconversion of heavy liquid fraction coming from separation stage b), when said stage b) is applied, in the presence of hydrogen in at least one or more three-phase reactors, installed in series or in parallel, containing at least one hydroconversion catalyst, wherein step (c) of the hydroconversion is carried out at an absolute pressure of 2 to 38 MPa, temperature of 300 to 550 °C and with amount of hydrogen from 50 to 5000 normal cubic meters (Nm 3 ) per cubic meter (m 3 ) of liquid material under standard conditions by temperature and pressure, wherein the hydroconversion catalyst at step a) and/or c) comprises an alumina substrate, wherein the catalyst at step a) and/or c) is used in the form of extrudates or balls, and the total volume hourly rate used in said method ranges from 0.05 to 0.09 h -1 . EFFECT: disclosed method increases stability of effluents at a given ...

Multi-bed reactor with mixing device

The present invention relates to a mixing device mounted between two catalyst beds in a multi-bed catalytic reactor with a cylindrical shape, wherein said mixing device has a circular outer rim which corresponds to the inner wall of the reactor, the mixing device comprises collecting means disposed in a collecting section for collecting fluid from an upstream catalytic bed, mixing means disposed in a mixing section for mixing the collected fluid, and discharging means disposed in a discharging section for discharging the mixed fluid to a downstream catalytic bed, characterized in that the mixing device has a donut shape and the collecting section, the mixing section and the discharging section are disposed outside the center of the circular cross-section of the reactor, as well as associated methods for mixing and the use of such a mixing device in catalytic reactors.

C2 및 c3 탄화수소 제조 방법

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

Method for hydraulic processing of hydrocarbon raw materials

FIELD: oil and gas industry. SUBSTANCE: method involves mixing heated liquid hydrocarbon raw mwterial with a diluent and hydrogen, contacting homogeneous raw mixture with catalyst in at least one reactor with at least one layer of catalyst to obtain hydrogenation, separation of the latter into the diluent and balance hydrogenate which is divided into commercial product, light hydrocarbon fraction and exhaust gas. Mixing is carried out to obtain homogeneous raw mixture, the catalyst contacts in the reactor with radial feed of raw material and at least two heat-exchange blocks located in catalyst layer, the balance hydrogenate is pre-reduced and heated in iiner space of at least one of the blocks of the heat-exchange elements, at that coolant is supplied to the inner space of the remaining units of the heat-exchange elements. EFFECT: simplification of the method, exclusion of temperature rise in the reactor. 4 cl, 1 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 630 774 C1 (51) МПК C10G 45/00 (2006.01) C10G 49/00 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ На основании пункта 1 статьи 1366 части четвертой Гражданского кодекса Российской Федерации патентообладатель обязуется заключить договор об отчуждении патента на условиях, соответствующих установившейся практике, с любым гражданином Российской Федерации или российским юридическим лицом, кто первым изъявил такое желание и уведомил об этом патентообладателя и федеральный орган исполнительной власти по интеллектуальной собственности. (21)(22) Заявка: 2016138946, 03.10.2016 03.10.2016 (73) Патентообладатель(и): Курочкин Андрей Владиславович (RU) Дата регистрации: 13.09.2017 Приоритет(ы): (22) Дата подачи заявки: 03.10.2016 (45) Опубликовано: 13.09.2017 Бюл. № 26 2 6 3 0 7 7 4 R U (54) СПОСОБ ГИДРОПЕРЕРАБОТКИ УГЛЕВОДОРОДНОГО СЫРЬЯ (57) Реферат: Изобретение относится к способу осуществляют с получением гомогенной сырьевой гидропереработки углеводородного сырья и смеси, ...

Method of processing liquid hydrocarbon product

FIELD: oil industry. SUBSTANCE: present invention relates to a method for treatment of a liquid hydrocarbon flow of oil or gas-condensate origin, involving hydrogenation, isomerisation of raw product in cavitation mode of its mixture with water. Surfactant is fed into flow of mixture, and mixture is treated by continuous scheme in cavitation mode, created by a pump-cavitator, at temperature +20…+90 °C. As a rule, amount of water in mixture is 10÷25 vol% of raw product, and amount of surfactant is 0.1÷0.5 vol% water, and treatment is carried out in one or more steps. EFFECT: technical result of present invention is simplification of technological process. 3 cl, 4 dwg, 3 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 607 087 C2 (51) МПК C10G 45/00 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ФОРМУЛА (21)(22) Заявка: ИЗОБРЕТЕНИЯ К ПАТЕНТУ РОССИЙСКОЙ ФЕДЕРАЦИИ 2014142726, 22.10.2014 (24) Дата начала отсчета срока действия патента: 22.10.2014 (72) Автор(ы): Архипов Алексей Сергеевич (RU) (73) Патентообладатель(и): Архипов Алексей Сергеевич (RU) Дата регистрации: (56) Список документов, цитированных в отчете о поиске: RU2143312 C1, 27.12.1999. Приоритет(ы): (22) Дата подачи заявки: 22.10.2014 (43) Дата публикации заявки: 20.05.2016 Бюл. № 14 Адрес для переписки: 443093, г.Самара, ул. М.Тореза,4,кв.33,А.С. Архипову 2 6 0 7 0 8 7 R U (57) Формула изобретения 1. Способ обработки жидкого углеводородного потока нефтяного или газоконденсатного происхождения, включающий гидрогенизацию, изомеризацию исходного продукта в режиме кавитации его смеси с водой, отличающийся тем, что в поток смеси вводят поверхностно-активное вещество (ПАВ), а смесь обрабатывают по непрерывной схеме в режиме кавитации, создаваемой насосом-кавитатором, при температуре +20…+90°С. 2. Способ по п. 1, отличающийся тем, что количество воды в смеси составляет 10÷25 об. % на исходный продукт, а количество ПАВ составляет 0,1÷0,5 об. % на воду. 3. Способ по п. 1, отличающийся тем, что ...

Heavy oil hydrofining system and heavy oil hydrofining method

FIELD: oil and gas industry.SUBSTANCE: present invention relates to the field of hydrofining of heavy oil, in particular to the heavy oil hydrofining system and the heavy oil hydrofining method. Method for heavy oil hydrofining involves mixing heavy crude oil with hydrogen and then feeding the mixture through a pre-hydrofining reaction zone, an intermediate reaction zone and a hydrofining reaction zone which are connected in series, where the sensor units are configured to detect pressure drop in each pre-hydrofining reactor in the pre-hydrofining reaction zone, and control unit is configured to receive pressure drop signals from sensor units; at the initial reaction stage, the pre-hydrofining reaction zone includes 3–6 pre-hydrofining reactors connected in parallel, transient reaction zone includes or does not include pre-hydrofining reactors; further, when the pressure drop in one of the pre-hydrofining reactors reaches a predetermined value, the pre-hydrofining reactor is switched from the pre-hydrofining reaction zone to the transition reaction zone and is referred to as the disconnected pre-hydrofining reactor I, wherein the pre-hydrofining reaction zone, the disconnected pre-hydrofining reactor I and the hydrofining reaction zone are connected in series; when the pressure drop in the next pre-hydrofining reactor reaches a predetermined value, the pre-hydrofining reactor is switched from the pre-hydrofining reaction zone to the transition reaction zone and is referred to as the disconnected pre-hydrofining reactor II, wherein the pre-hydrofining reaction zone, the disconnected pre-hydrofining reactor II, the disconnected pre-hydrofining reactor I and the hydrofining reaction zone are connected in series; other pre-hydrofining reactors are treated in the above method until all pre-hydrofining reactors are connected in series; wherein preset differential pressure in pre-hydrofining reactors makes 50–80 % of designed upper pressure drop for pre-hydrofining ...

Method of converting hydrocarbon material containing shale oil by hydroconversion in fluidised bed, fractionation using atmospheric distillation and hydrocracking

FIELD: technological processes. SUBSTANCE: invention relates to a method of converting shale oil or a mixture of shale oil with nitrogen content at least 0.1 wt%, comprising following steps: a) raw material is introduced in part for hydroconversion in presence of hydrogen, wherein said part comprises at least a reactor with fluidised bed, which operates in mode of gaseous and liquid flow and comprises at least one hydroconversion catalyst on a substrate, b) output stream obtained at step a) is at least partially in fractionation zone, from which, by means of atmospheric distillation are output gaseous fraction, naphtha fraction, gas oil fraction and a fraction heavier than gas oil, c) said naphtha fraction is processed at least partially in first part for hydrotreatment in presence of hydrogen, wherein said part comprises at least one reactor with fixed layer, containing at least one catalyst for hydrotreatment, d) said gas oil fraction is processed at least partially in second part for hydrotreatment in presence of hydrogen, wherein said part comprises at least one reactor with fixed layer, containing at least one catalyst for hydrotreatment, e) fraction heavier than gas oil fraction is processed at least partially in part for hydrocracking in presence of hydrogen. Invention also relates to shale oil processing using said method. EFFECT: invention provides maximisation of output fuel base. 28 cl, 2 dwg, 2 tbl, 1 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (51) МПК C10G 5/00 C10G 1/00 C10L 1/02 C10G 35/04 C10G 45/02 C10G 45/08 ФЕДЕРАЛЬНАЯ СЛУЖБА C10G 47/12 ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ C10G 47/26 C10G 65/10 C10G 65/12 (12) ОПИСАНИЕ (21)(22) Заявка: (13) 2 592 688 C2 (2006.01) (2006.01) (2006.01) (2006.01) (2006.01) (2006.01) (2006.01) (2006.01) (2006.01) (2006.01) ИЗОБРЕТЕНИЯ К ПАТЕНТУ 2013134377/04, 16.12.2011 (24) Дата начала отсчета срока действия патента: 16.12.2011 24.12.2010 FR 1061246 (45) Опубликовано: 27.07.2016 Бюл. № 21 C 2 C 2 (56) Список документов, ...

Способ конверсии углеводородного сырья, содержащего сланцевое масло, путем гидроконверсии в кипящем слое, фракционирования с помощью атмосферной дистилляции и гидрокрекинга

1. Способ конверсии сланцевого масла или смеси сланцевых масел, имеющих содержание азота по меньшей мере 0,1%, часто по меньшей мере 1% и очень часто по меньшей мере 2 мас.%, отличающийся тем, что он содержит следующие стадии:a) сырье вводится в часть для гидроконверсии в присутствии водорода, причем указанная часть содержит по меньшей мере реактор с кипящем слоем, работающий в режиме газообразного и жидкого восходящего потока и содержащий по меньшей мере один катализатор гидроконверсии на подложке,b) выходящий поток, полученный на стадии a), вводится, по меньшей мере частично и часто полностью, в зону фракционирования, из которой, посредством атмосферной дистилляции, выходят газообразная фракция, фракция лигроина, фракция газойля и фракция, более тяжелая, чем фракция газойля,c) указанная фракция лигроина обрабатывается, по меньшей мере частично и часто полностью, в первой части для гидрообработки в присутствии водорода, причем указанная часть содержит по меньшей мере один реактор с фиксированным слоем, содержащий по меньшей мере один катализатор гидрообработки,d) указанная фракция газойля обрабатывается, по меньшей мере частично и часто полностью, во второй части для гидрообработки в присутствии водорода, причем указанная часть содержит по меньшей мере один реактор с фиксированным слоем, содержащий по меньшей мере один катализатор гидрообработки,e) фракция, более тяжелая, чем фракция газойля, обрабатывается, по меньшей мере частично и часто полностью, в части для гидрокрекинга в присутствии водорода.2. Способ по п.1, в котором выходящие потоки гидрокрекинга, полученные в конце стадии e), фракционируются на вторую газ� РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2013 134 377 A (51) МПК C10G 5/00 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21)(22) Заявка: 2013134377/04, 16.12.2011 (71) Заявитель(и): ТОТАЛЬ РАФФИНАЖ МАРКЕТИНГ (FR), АКСЕНС (FR) Приоритет(ы): (30) Конвенционный приоритет: 24.12.2010 FR 1061246 (85) Дата начала ...

Cracking intermediate liquid product returns to the hydrocarbon heat from hydrogenation cracking method inferior of pre-add hydrogen

裂化中间液体产物返回预加氢的劣质烃加氢热裂化方法，特别适合于胶状沥青状组分含量高的煤焦油F1的悬浮床加氢热裂化反应过程，采用“加氢精制性预加氢反应R10过程→浅度加氢热裂化反应过程R21→浅度加氢热裂化反应液体产物R21PLR返回R10”操作模式，增加加氢精制反应R10在总体反应中的比重及时对R21热缩合物进行芳烃加氢饱和，降低深度加氢热裂化反应过程R22的原料中胶状沥青状组分含量和稠环度，可降低最终热裂解液体产物中胶状沥青状组分含量和稠环度，利于延长操作周期，提高轻质油收率。

Catalyst and method of purifying liquid hydrocarbons from total sulfur

FIELD: petroleum chemistry. SUBSTANCE: invention relates to petrochemistry, specifically to methods of purifying diesel fuel (DF), hydrocarbons and motor fuels from sulfur derivatives. Catalyst is a mixed heteropoly compound applied on a solid mineral carrier. Heteropoly compound used is a product of reaction of sodium tungstate, sodium hydrophosphate, hydrochloric acid and zinc salt. Method is catalytic oxidative conversion of sulfur derivatives in hydrocarbon solutions in the presence of hydrogen peroxide and said catalyst. Purification of hydrocarbons is carried out by repeating cycles of desulphurisation with removal of sulfur conversion products before the next cleaning cycle. EFFECT: technical result is obtaining fuel according to Euro-5 standard with residual sulfur content of 10 ppm while simplifying the method. 8 cl, 4 tbl, 32 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 693 699 C1 (51) МПК B01J 31/34 (2006.01) C10G 45/00 (2006.01) B01J 21/00 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК B01J 31/34 (2019.05); C10G 45/00 (2019.05); B01J 21/00 (2019.05) (21)(22) Заявка: 2019106160, 05.03.2019 (24) Дата начала отсчета срока действия патента: Дата регистрации: 04.07.2019 (45) Опубликовано: 04.07.2019 Бюл. № 19 (73) Патентообладатель(и): Общество с ограниченной ответственностью "Салф-инжиниринг" (RU) Адрес для переписки: 125368, Москва, а/я 84, А.А. Щитову (56) Список документов, цитированных в отчете о поиске: RU 2619946 C1, 22.05.2017. RU 2 6 9 3 6 9 9 R U (54) Катализатор и способ очистки жидких углеводородов от общей серы (57) Реферат: Изобретение относится к области нефтехимии, производных серы в растворах углеводородов в а именно к способам очистки дизельного топлива присутствии перекиси водорода и указанного (ДТ), углеводородов и моторных топлив от катализатора. Очистку углеводородов проводят производных серы. Катализатор представляет путем повторения циклов сероочистки с собой смешанное ...

Multi-staged hydroprocessing process and system

Methods and systems of processing a hydrocarbonaceous feed stock flows are provided. In one aspect, the method includes providing two or more hydroprocessing stages disposed in sequence, each hydroprocessing stage having a hydroprocessing reaction zone with a hydrogen requirement and each stage in fluid communication with the preceding stage. A hydrogen source is provided substantially free of hydrogen from a hydrogen recycle compressor. The hydrocarbonaceous feed stock flow is separated into an portions of fresh feed for each hydroprocessing stage, and then supplying the first portion of fresh feed with hydrogen from the hydrogen source in an amount satisfying substantially all of the hydrogen requirements of the hydroprocessing stages to a first hydroprocessing zone.

Process for selective hydrogenation of petroleum stocks

Three stage hydroprocessing including a vapor stage

A three stage hydroprocessing process includes two liquid and one vapor reaction stages, with a hydrogen containing vapor effluent produced in both liquid stages. The second liquid stage vapor effluent comprises part of the first liquid stage feed and the first liquid stage vapor effluent is the feed for the vapor stage. At least a portion of the hydrogen for the first liquid stage and vapor stage reactions is respectively provided by the hydrogen in the second and first liquid stage vapor effluents.

Hydrocracking process

A hydrocracking process wherein a hydrocarbonaceous feedstock and a hot hydrocracking zone effluent containing hydrogen is passed to a denitrification and desulfurization reaction zone to produce hydrogen sulfide and ammonia to thereby clean up the fresh feedstock. The resulting hot, uncooled effluent from the denitrification and desulfurization zone is hydrogen stripped in a stripping zone maintained at essentially the same pressure as the preceding reaction zone with a hydrogen-rich gaseous stream to produce a vapor stream comprising hydrogen, hydrocarbonaceous compounds boiling at a temperature below the boiling range of the fresh feedstock, hydrogen sulfide and ammonia, and a liquid hydrocarbonaceous stream.

Multireactor parallel flow hydrocracking process

Heavy hydrocarbons are upgraded to higher value distillates in a hydrocarbon conversion process which employs several parallel reaction zones which each contain both hydrotreating and hydrocracking catalyst beds. The feed and liquid recycle from the bottom of the reaction zone is charged to the top of the uppermost catalyst bed. Hydrogen flow is countercurrent to the descending liquid, and products are removed overhead through vapor-liquid contactors. The flow of feed to one of the reaction zones is periodically stopped to allow sequential on-stream hydrogenative regeneration of the catalysts within the reaction zone.

Hydrocracking process product recovery method

A feed stream is first processed in a hydrotreating reaction zone and then the effluent is separated into three fractions in an augmented first high pressure separator. Controlled portions of the middle and heavy boiling point range hydrocarbon fractions from this separator are recycled through a low conversion hydrocracking zone, while the remaining portions of these two fractions are passed into a second high pressure separator for recovery. The recycled hydrocarbons flow into a hydrocracking zone and the effluent of this zone flows into the hydrotreating reaction zone.

Hydrocarbon conversion process

A process for the conversion of a feedstock containing light cycle oil and vacuum gas oil to produce naphtha boiling range hydrocarbons and a higher boiling range hydrocarbonaceous stream having a reduced concentration of sulfur.

method and apparatus for processing a hydrocarbon feedstock.

Upgrading raw shale-derived crude oils to hydrocarbon distillate fuels

Integrated processes for upgrading crude shale-derived oils, such as those produced by oil shale retorting or by in situ extraction or combinations thereof. Processes disclosed provide for a split-flow processing scheme to upgrade whole shale oil. The split flow concepts described herein, i.e., naphtha and kerosene hydrotreating in one or more stages and gas oil hydrotreating in one or more stages, requires additional equipment as compared to the alternative approach of whole oil hydrotreating. While contrary to conventional wisdom as requiring more capital equipment to achieve the same final product specifications, the operating efficiency vis a vis on-stream time efficiency and product quality resulting from the split flow concept far exceed in value the somewhat incrementally higher capital expenditure costs.

HYDROCARBONATE CHARGING CONVERSION PROCESS COMPRISING SCHIST OIL BY BOILING BED HYDROCONVERSION, ATMOSPHERIC DISTILLATION FRACTIONATION, AND HYDROCRACKING

Upgrading raw shale-derived crude oils to hydrocarbon distillate fuels

Integrated processes for upgrading crude shale-derived oils, such as those produced by oil shale retorting or by in situ extraction or combinations thereof. Processes disclosed provide for a split-flow processing scheme to upgrade whole shale oil. The split flow concepts described herein, i.e., naphtha and kerosene hydrotreating in one or more stages and gas oil hydrotreating in one or more stages, requires additional equipment as compared to the alternative approach of whole oil hydrotreating. While contrary to conventional wisdom as requiring more capital equipment to achieve the same final product specifications, the operating efficiency vis a vis on-stream time efficiency and product quality resulting from the split flow concept far exceed in value the somewhat incrementally higher capital expenditure costs.

Process for upgrading heavy oil using a highly active slurry catalyst composition

Applicants have developed a new residuum full hydroconversion slurry reactor system that allows the catalyst, unconverted oil and converted oil to circulate in a continuous mixture throughout an entire reactor with no confinement of the mixture. The mixture is partially separated in between the reactors to remove only the products and hydrogen gas, while permitting the unconverted oil and the slurry catalyst to continue on into the next sequential reactor. A portion of the unconverted oil is then converted to lower boiling point hydrocarbons, once again creating a mixture of unconverted oil, products, hydrogen, and slurry catalyst. Further hydroprocessing may occur in additional reactors, fully converting the oil. Additional oil may be added at the interstage feed inlet, possibly in combination with slurry. The oil may alternately be partially converted, leaving a highly concentrated catalyst in unconverted oil which can be recycled directly to the first reactor.

Catalyst preparation reactors from catalyst precursor used for feeding reactors to upgrade heavy hydrocarbonaceous feedstocks

The invention concerns a process for upgrading heavy hydrocarbonaceous feedstocks in at least one hydroconversion reactor for hydroconversion of said heavy hydrocarbonaceous feedstocks and in at least one hydrotreatment reactor for hydrotreatment of said heavy hydrocarbonaceous feedstocks, said process comprising the preparation of two or more catalysts, each catalyst being prepared from one or more catalyst precursor in at least one specific preparation reactor, said catalyst precursor containing at least one transition metal selected from group IIA, IIIB, IVB, VB, VIB, VIIB, VIII, IB or IIB of the periodic table of elements, and each preparation reactor feeding one or more hydroconversion or hydrotreatment reactor, each catalyst contained in preparation reactors being dedicated to hydroconversion or hydrotreatment of said feedstocks. Such a process permits to obtain, under continuous operating conditions, products of better quality.

Process for partial upgrading of heavy oil

A process is provided to partially upgrade heavy oil using two or more reaction zones connected in series, each reaction zone being a continuous stirred tank maintained at hydrocracking conditions. The heavy oil feedstock and a solid particulate catalyst are stirred to form a pumpable slurry which is heated to a target hydrocracking temperature and then continuously fed to the first reaction zone. Hydrogen is continuously introduced to the reaction zone to achieve hydrocracking and to produce a volatile vapour stream carried upwardly by the hydrogen to produce an overhead vapour stream. The hydrocracked heavy oil slurry from one reaction zone is fed to a next reaction zone also maintained under hydrocracking conditions with a continuous hydrogen feed to produce a volatile vapour stream carried upwardly by the hydrogen. The overhead vapour stream from each reactor zone is continuously removed, and the hydrocracked heavy oil slurry from the last of the reaction zones is removed to provide a partially upgraded heavy oil slurry.

Multi-stage hydrocracking process

Method of upgrading an ebullated bed reactor for increased production rate of converted products

Process for partial upgrading of heavy oil

A process is provided to partially upgrade heavy oil using two or more reaction zones connected in series, each reaction zone being a continuous stirred tank maintained at hydrocracking conditions. The heavy oil feedstock and a solid particulate catalyst are stirred to form pumpable slurry which is heated to a target hydrocracking temperature and then continuously fed to the first reaction zone. Hydrogen is continuously introduced to the reaction zone to achieve hydrocracking and to produce a volatile vapor stream carried upwardly by the hydrogen to produce an overhead vapor stream. The hydrocracked heavy oil slurry from one reaction zone is fed to a next reaction zone also maintained under hydrocracking conditions with a continuous hydrogen feed to produce a volatile vapor stream. The overhead vapor stream from each reactor zone is continuously removed, and the hydrocracked heavy oil slurry from the last of the reaction zones is removed.

Crude oil desulfurization

This invention relates to a crude oil desulfurization process which comprises hydrodesulfurizing a crude oil feed in a crude desulfurization unit. The desulfurized crude oil is then separated into a light gas oil fraction, a vacuum gas oil fraction and a vacuum residuum fraction. The vacuum gas oil is hydrocracked to form at least one low sulfur fuel product. The light gas oil fraction is hydrotreated. The vacuum gas oil may be hydrocracked in one or more stages. Hydrocracking in the second stage, if present, will convert of at least 20% of the first zone effluent, to create a low sulfur light gas oil fraction. The light gas oil fraction may then be hydrotreated.

Process for upgrading heavy oil using a highly active slurry catalyst composition

Applicants have developed a new residuum full hydroconversion slurry reactor system that allows the catalyst, unconverted oil and converted oil to circulate in a continuous mixture throughout an entire reactor with no confinement of the mixture. The mixture is partially separated in between the reactors to remove only the products and hydrogen gas, while permitting the unconverted oil and the slurry catalyst to continue on into the next sequential reactor. A portion of the unconverted oil is then converted to lower boiling point hydrocarbons, once again creating a mixture of unconverted oil, products, hydrogen, and slurry catalyst. Further hydroprocessing may occur in additional reactors, fully converting the oil. Additional oil may be added at the interstage feed inlet, possibly in combination with slurry. The oil may alternately be partially converted, leaving a highly concentrated catalyst in unconverted oil which can be recycled directly to the first reactor.

Production of field hydrocarbons

Изобретение относится к способу получения парафиновых продуктов, подходящих для использования в качестве промысловых углеводородов или для превращения в промысловые углеводороды. Способ включает в себя разделение воска Фишера-Тропша на, по меньшей мере, более легкую фракцию и промежуточную фракцию С-С, и указанную более тяжелую фракцию C+, гидроизомеризацию промежуточной С-Спри использовании катализатора гидроизомеризации для получения гидроизомеризованного промежуточного продукта, разделение гидроизомеризованного промежуточного продукта на две или более фракции базового масла, гидрокрекинг более тяжелой фракции с получением крекированного промежуточного продукта и разделение крекированного промежуточного продукта на, по меньшей мере, фракцию нафты и более тяжелую, чем нафта, фракцию парафинового дистиллята, содержащего по меньшей мере 50% по массе углеводородов, имеющих длину углеродной цепи от 12 до 22 атомов углерода в молекуле, при этом более тяжелая, чем нафта, фракция парафинового дистиллята подходит для использования в качестве промысловых углеводородов или для превращения в промысловые углеводороды, и донную фракцию, которая тяжелее, чем фракция парафинового дистиллята. Предлагаемый способ является более эффективным. 13 з.п. ф-лы, 2 табл., 2 ил. РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (51) МПК C10G 57/02 C10G 65/02 C10G 65/12 C10G 65/14 (11) (13) 2 720 409 C2 (2006.01) (2006.01) (2006.01) (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК C10G 57/02 (2019.08); C10G 65/02 (2019.08); C10G 65/12 (2019.08); C10G 65/14 (2019.08) (21)(22) Заявка: 2019118802, 22.07.2015 (24) Дата начала отсчета срока действия патента: (73) Патентообладатель(и): СЭСОЛ ТЕКНОЛОДЖИ ПРОПРАЙЭТЕРИ ЛИМИТЕД (ZA) Дата регистрации: 29.04.2020 28.07.2014 ZA 2014/05559 Номер и дата приоритета первоначальной заявки, из которой данная заявка выделена: 2017106166 28.07.2014 (56) Список документов, цитированных в отчете о поиске: WO 2006/067174 A1, 29. ...

Method of producing branched olefins, branched alkyl aromatic hydrocarbon of branched alkylaryl sulphonates

Изобретение относится к способу получения разветвленных олефинов, указанный способ включает дегидрирование изопарафиновой композиции, содержащей 0,5% или менее четвертичных алифатических атомов углерода, на подходящем катализаторе, указанная изопарафиновая композиция получена гидроизомеризацией парафиновой композиции и включает парафины с количеством углеродов в диапазоне от 7 до 18, причем указанные парафины, по меньшей мере, часть их молекул, являются разветвленными, где содержание разветвленных парафинов изопарафиновой композиции составляет, по меньшей мере, 50 мас.% от массы изопарафиновой композиции, среднее количество ответвлений на молекулу парафина составляет от 0,5 до 2,5, и ответвления включают метильные и необязательно этильные ветви, указанные разветвленные олефины имеют содержание четвертичных алифатических углеродов 0,5% или менее, причем указанная парафиновая композиция получена способом Фишера-Тропша. Также изобретение относится к способам получения разветвленного алкилароматического углеводорода и разветвленных алкиларилсульфанатов, включающих приведенный выше способ. Предлагаемое изобретение является более универсальным и экономически более выгодным, чем известные способы. 3 н. и 4 з.п. ф-лы. РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2 430 078 (51) МПК C07C C07C C07C C07C C07C C07C ФЕДЕРАЛЬНАЯ СЛУЖБА C11D ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ, B01F ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ C10G C10G (12) ОПИСАНИЕ 11/02 5/333 15/107 2/66 303/04 309/24 1/22 17/12 65/02 69/12 (2006.01) (2006.01) (2006.01) (2006.01) (2006.01) (2006.01) (2006.01) (2006.01) (2006.01) (2006.01) (13) C2 C10G 45/58 (2006.01) C07C 303/30 (2006.01) ИЗОБРЕТЕНИЯ К ПАТЕНТУ (21)(22) Заявка: 2006140980/04, 15.02.2002 (24) Дата начала отсчета срока действия патента: 15.02.2002 (73) Патентообладатель(и): ШЕЛЛ ИНТЕРНЭШНЛ РИСЕРЧ МААТСХАППИЙ Б.В. (NL) 2 4 3 0 0 7 8 (43) Дата публикации заявки: 27.05.2008 Бюл. № 15 2 4 3 0 0 7 8 R U (56) Список документов, цитированных в отчете о поиске: WO 0105755 А, 25.01.2001. ...

Method used for producing clean diesel oil

一种生产清洁柴油的方法。将二次加工柴油进行切割，分为轻二次加工柴油馏分和重二次加工柴油馏分，其中，轻二次加工柴油馏分中4,6-二甲基二苯并噻吩的含量为0～300μg/g，将重二次加工柴油馏分送入渣油加氢反应器进行反应，将轻二次加工柴油馏分和直馏柴油一起进入柴油加氢反应器进行反应，柴油加氢反应流出物依次经分离和分馏后，得到汽油馏分II和柴油馏分II，其中柴油馏分II的硫含量低于10μg/g。本发明将柴油加氢精制和渣油加氢处理进行联合，加工大量二次加工柴油，在较缓和的条件下生产满足欧V排放标准的柴油产品，延长催化剂的操作周期。

Method of converting hydrocarbon material containing shale oil by hydroconversion in fluidised bed, fractionation using atmospheric distillation and extraction liquid/liquid in heavy fraction

FIELD: technological processes. SUBSTANCE: present invention relates to a method of conversion of shale oil or a mixture of shale oil with nitrogen content at least 1 wt%. Method involves following steps: a) raw material is processed in a part of conversion in presence of hydrogen, wherein said part comprises at least one reactor with fluidised bed, which operates in mode of gaseous and liquid flow and comprising at least one catalyst on support; b) output stream obtained at step a) is fed, at least partially and frequently completely, into fractionation zone, from which, by means of atmospheric distillation, come out gaseous fraction, naphtha fraction, gas oil fraction and fraction heavier than gas oil; c) said naphtha fraction is processed, at least partially and frequently completely, in part for hydrotreatment in presence of hydrogen, wherein said part comprises at least one reactor with fixed layer, containing at least one hydraulic treatment catalyst; and d) said gas oil fraction is processed, at least partially and frequently completely, in other part for hydrotreatment in presence of hydrogen, wherein said part comprises at least one reactor with fixed layer, containing at least one hydraulic treatment catalyst; e) fraction heavier than gas oil fraction is subjected to liquid/liquid extraction to produce purified oil product and extract. EFFECT: proposed method allows to obtain products of high quality with low content of sulphur and nitrogen. 16 cl, 2 dwg, 2 tbl, 1 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (51) МПК C10G 67/04 (13) 2 592 690 C2 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ (21)(22) Заявка: ИЗОБРЕТЕНИЯ К ПАТЕНТУ 2013134382/04, 16.12.2011 (24) Дата начала отсчета срока действия патента: 16.12.2011 Приоритет(ы): (30) Конвенционный приоритет: (43) Дата публикации заявки: 27.01.2015 Бюл. № 3 (45) Опубликовано: 27.07.2016 Бюл. № 21 (73) Патентообладатель(и): ТОТАЛЬ РАФФИНАЖ МАРКЕТИНГ (FR), АКСЕНС (FR) (85) Дата начала ...

METHOD FOR PRODUCING DIESEL FUEL

РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2015 125 481 A (51) МПК C10G 45/00 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21)(22) Заявка: 2015125481, 25.11.2013 (71) Заявитель(и): ЮОП ЛЛК (US) Приоритет(ы): (30) Конвенционный приоритет: 28.11.2012 US 13/687,757 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 29.06.2015 R U (43) Дата публикации заявки: 11.01.2017 Бюл. № 02 (72) Автор(ы): КОКАЕФФ Питер (US), ЦИММЕРМАН Пол Р. (US) (86) Заявка PCT: (87) Публикация заявки PCT: WO 2014/085278 (05.06.2014) R U (54) СПОСОБ ПОЛУЧЕНИЯ ДИЗЕЛЬНОГО ТОПЛИВА (57) Формула изобретения 1. Способ получения дизельного топлива из углеводородного потока, включающий в себя: гидроочистку основного углеводородного потока и совместно подаваемого потока углеводородного сырья, содержащего дизельное топливо, в присутствии потока водорода и катализатора предварительной очистки, с получением предварительно очищенного выходящего потока; гидрокрекинг предварительно очищенного выходящего потока в присутствии катализатора гидрокрекинга и водорода с получением выходящего потока гидрокрекинга; разделение на фракции по меньшей мере части выходящего потока гидрокрекинга с получением потока дизельного топлива; и гидроочистку потока дизельного топлива в присутствии потока водорода для гидроочистки и катализатора гидроочистки с получением выходящего потока гидроочистки. 2. Способ по п. 1, дополнительно включающий в себя разделение выходящего потока гидрокрекинга на парообразный выходящий поток гидрокрекинга, содержащий водород, и жидкий выходящий поток гидрокрекинга; сжатие парообразного выходящего потока гидрокрекинга вместе со сжатым потоком подпиточного водорода с образованием сжатого потока водорода и отбор потока водорода для гидроочистки из сжатого потока Стр.: 1 A 2 0 1 5 1 2 5 4 8 1 A Адрес для переписки: 109012, Москва, ул. Ильинка, 5/2, ООО "Союзпатент" 2 0 1 5 1 2 5 4 8 1 US 2013/071561 (25.11.2013) A 2 0 1 5 1 2 5 4 8 1 R U A 2 0 1 5 1 2 ...

Method of production of the mean distillates by hydroisomerization and hydrocracking of the raw materials produced by fisher-tropsh synthesis and the installation for the method realization

FIELD: petrochemical industry; the methods and devices for production of the mean distillates. SUBSTANCE: the invention is pertaining to petrochemical industry, in particular, to the method and equipment for production of the mean distillates. The method provides for separation of the heavy fraction with the initial boiling-point of 120-200°С. Then at least a part of this fraction is subjected to hydrocleaning. The hydrocleaning flow is fractionated into at least three fractions: the mean fraction having the boiling point of 120-200°С the final boiling point within the interval of 300-410°С; the light fraction with the boiling point below in the mean fraction; the heavy fraction with the boiling point above that in the mean fraction. At least a part of the mean fraction is gated through the amorphous catalytic agent of the hydroisomerization and hydrocracking. The subjected to the hydroisomerization and hydrocracking fractions are subjected to distillation with production of the mean distillates. The residual fraction boiling above the boiling point of the mean distillates is recycled into the amorphous catalytic agent used at the treatment of the heavy fraction. The technical result of the invention is improvement of the quality and the production output of the mean distillates. EFFECT: the invention ensures the improved quality and the production output of the mean distillates. 16 cl, 10 tbl, 1 ex ÐÎÑÑÈÉÑÊÀß ÔÅÄÅÐÀÖÈß (19) RU (11) 2 283 339 (13) C2 (51) ÌÏÊ C10G 65/12 (2006.01) ÔÅÄÅÐÀËÜÍÀß ÑËÓÆÁÀ ÏÎ ÈÍÒÅËËÅÊÒÓÀËÜÍÎÉ ÑÎÁÑÒÂÅÍÍÎÑÒÈ, ÏÀÒÅÍÒÀÌ È ÒÎÂÀÐÍÛÌ ÇÍÀÊÀÌ (12) ÎÏÈÑÀÍÈÅ ÈÇÎÁÐÅÒÅÍÈß Ê ÏÀÒÅÍÒÓ (21), (22) Çà âêà: 2004103459/04, 26.06.2002 (72) Àâòîð(û): ÁÅÍÀÇÇÈ Ýðèê (FR), ÃÅÐÅ Êðèñòîô (FR) (24) Äàòà íà÷àëà îòñ÷åòà ñðîêà äåéñòâè ïàòåíòà: 26.06.2002 (43) Äàòà ïóáëèêàöèè çà âêè: 20.06.2005 R U (73) Ïàòåíòîîáëàäàòåëü(è): ÝÍÑÒÈÒÞ ÔÐÀÍÑÝ ÄÞ ÏÅÒÐÎËÜ (FR), ÝÍÈ Ñ.Ï.À. (IT), ÝÍÈÒÅÊÍÎËÎÄÆÈÅ Ñ.Ï.À. (IT) (30) Êîíâåíöèîííûé ïðèîðèòåò: 06.07.2001 FR 0108969 (45) Îïóáëèêîâàíî: 10. ...

Flexible hydrocracking of slurry hydrocracking products

FIELD: chemistry. SUBSTANCE: present invention relates to hydrotreatment of a product using a slurry hydrocracking (SHC) method. Described is a hydrotreating method of a product of a hydrocracking process with a suspended layer, comprising separating a hydrocracking product with a suspended layer in a hot separator into a first fluid stream and a first vapor stream, fractionating said first fluid stream into at least two fractions in a first fractionation zone, wherein said at least two fractions include at least a first fraction and a second fraction, wherein said second fraction has a boiling point T5 which is higher than the boiling temperature T5 of said first fraction, hydrotreating said first fraction and at least a portion of said first steam stream in the presence of hydrogen and a hydrotreating catalyst in a first hydrotreating reactor to form a first hydrotreated product, separating said first hydrotreated product into at least two fractions in a separation zone, wherein at least two fractions contain at least a product naphtha fraction, a diesel product fraction, and hydrofining and hydrocracking said second fraction in the presence of hydrogen, a hydrotreating catalyst and a hydrocracking catalyst in a hydrotreating and hydrocracking reactor to form a second hydrotreated product, wherein said first hydrotreated product separation into at least two fractions comprises separation of said first hydrotreated product into at least said product naphtha fraction, said diesel product fraction and product gas fraction from vacuum gas oil. EFFECT: technical result is significant saving of costs and providing comparable improved properties of product due to use of combined system for hydrotreatment. 10 cl, 7 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 718 540 C1 (51) МПК C10G 65/12 (2006.01) C10G 45/00 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК C10G 65/12 (2019.08); C10G 45/00 (2019.08) (21)(22) ...

Residue hydrocracking processing

FIELD: chemistry.SUBSTANCE: invention relates to methods for hydroconversion of hydrocarbon fractions. Method for upgrading residuum hydrocarbons includes: solvent deasphalting a residuum hydrocarbon fraction to produce a deasphalted oil fraction and an asphalt fraction; feeding the asphalt fraction obtained by solvent deasphalting into a first fluidised bed hydrocracking reactor system; contacting the asphalt fraction and hydrogen with a first hydroconversion catalyst in a first fluidised bed hydrocracking reactor system, resulting in removal of sulphur ranging from about 40% by weight to about 80% by weight, removal of metals ranging from about 60% by weight to about 85% by weight, and removal of Conradson carbon residue (CCR) ranging from about 30% by weight to about 65% by weight; recovering effluent from the first fluidised bed hydrocracking reactor system; fractionating the effluent from the first fluidised bed hydrocracking reactor system to recover one or more hydrocarbon fractions; contacting the deasphalted oil fraction and hydrogen with a hydrodesulphurisation catalyst in a fixed bed hydrodesulphurisation unit, wherein the deasphalted oil fraction has a metal content of less than 80 parts per million and a Conradson carbon residue (CCR) content less than 10% by weight; recovering the effluent from the fixed bed hydrodesulphurisation unit; contacting the effluent from the fixed bed hydrodesulphurisation unit or a portion thereof with a third hydrocracking catalyst in a second fluidised bed hydrocracking reactor system. Four versions of the conversion method are disclosed.EFFECT: technical result is a wider residue conversion range, while obtaining petroleum fuel with a low content of impurities.20 cl, 2 tbl, 4 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 663 896 C2 (51) МПК C10G 21/14 (2006.01) C10G 65/14 (2006.01) C10G 67/04 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК C10G 21/14 (2006.01); ...

Manufacturing method of fuel oil base material

원료유에서보다 낮은 황함량 및 0.05 질량%이하의 건조침전물 함량을 가진 연료유 베이스재료를 제조하는 방법에 있어서, 1.0 내지 10 질량%의 황 함량 및 0 내지 5.0 질량%의 건조침전물 함량을 가진 원료유를 두 단계로 수소화처리하는 것으로 이루어지고, 제1단계 수소화처리의 온도가 340 내지 450℃이고, 제2단계 수소화처리의 온도는 200 내지 440℃이고 또 상기 제1단계 수소화처리 온도보다 낮은 온도로 유지되는 것을 특징으로 하는 연료유 베이스재료의 제조방법이 제공된다. A method for producing a fuel oil base material having a lower sulfur content and a dry precipitate content of less than 0.05 mass% in a feed oil, characterized in that the feedstock base material has a sulfur content of 1.0 to 10 mass% and a dry precipitate content of 0 to 5.0 mass% Wherein the temperature of the first step hydrogenation treatment is 340 to 450 ° C, the temperature of the second step hydrogenation treatment is 200 to 440 ° C, and the temperature of the first step hydrogenation treatment is lower than the first step hydrogenation temperature Of the fuel oil base material.

Three-stage hydrogen treatment method including steam stage

Method of producing hexadecahydropyrene

Изобретение относится к способу получения гексадекагидропирена, включающему: введение исходного материала - углеводородного масла, содержащего соединения пирена, в реакцию гидрирования в присутствии катализатора гидрирования для получения гексадекагидропирена. Соединения пирена выбраны из по меньшей мере одного вещества из пирена и его ненасыщенных продуктов гидрирования, катализатор гидрирования содержит носитель и активный металлический компонент, нанесенный на носитель, активный металлический компонент представляет собой Pt и/или Pd, носитель содержит мелкокристаллический цеолит Y, оксид алюминия и аморфный алюмосиликат, мелкокристаллический цеолит Y имеет средний диаметр зерен 200-700 нм, молярное отношение SiO 2 /Al 2 O 3 40-120, относительную кристалличность ≥ 95%, удельную площадь поверхности 900-1200 м 2 /г, и доля объема вторичных пор диаметром 1,7-10 нм составляет 50% или более от общего объема пор. Процесс реакции гидрирования включает две стадии реакции, которые выполняют последовательно, процентное содержание х 1 активного металлического компонента в катализаторе гидрирования, используемом на первой стадии реакции, ниже процентного содержания х 2 активного металлического компонента в катализаторе гидрирования, используемом на второй стадии реакции, и процентное содержание у 1 мелкокристаллического цеолита Y в катализаторе гидрирования, используемом на первой стадии реакции, выше процентного содержания у 2 мелкокристаллического цеолита Y в катализаторе гидрирования, используемом на второй стадии реакции. Технический результат - получение гексадекагидропиренового продукта высокой чистоты с высоким выходом. 20 з.п. ф-лы, 14 пр., 7 табл., 2 ил. РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (51) МПК C10G 65/02 C10G 45/44 C10G 45/54 B01J 29/00 (11) (13) 2 717 334 C1 (2006.01) (2006.01) (2006.01) (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК C10G 65/02 (2020.01); C10G 45/44 (2020.01); C10G 45/54 (2020.01); B01J 29/ ...