СПОСОБ ПОЛУЧЕНИЯ БАЗОВОГО СМАЗОЧНОГО МАСЛА ИЗ ПАРАФИНОВОГО ГАЧА

Использование: нефтеперерабатывающая отрасль промышленности. Сущность: сырье, содержащее парафиновый гач, подвергают контактированию в присутствии водорода с сульфидированным катализатором гидрообессеривания, содержащим никель и вольфрам на кислотном и имеющим активность гидрообессеривания выше 30%. Далее проводят стадию снижения температуры застывания потока, выходящего со стадии контактирования. Технический результат: повышение качества целевого продукта. 23 з.п. ф-лы.

ПРОИЗВОДСТВО ВЫСОКОКАЧЕСТВЕННОГО ДИЗЕЛЬНОГО ТОПЛИВА И СМАЗОЧНЫХ МАТЕРИАЛОВ ИЗ АРОМАТИЧЕСКОГО УГЛЕРОДИСТОГО МАТЕРИАЛА С ВЫСОКОЙ ТЕМПЕРАТУРОЙ КИПЕНИЯ

Изобретение относится к способу удаления по меньшей мере 20% ароматических углеводородов, содержащихся во фракции, кипящей при температуре выше 190°С, из тяжелого углеводородного сырья, содержащего по меньшей мере 30 мас. % ароматических углеводородов, по меньшей мере 3000 мас. частей на миллион азота и по меньшей мере 0,5 мас. % кислорода, причем указанный способ осуществляют за одну стадию, в которой никакой промежуточный поток не выводят, и причем указанный способ включает следующие этапы: a) предоставление продукта, подаваемого в гидроочиститель, посредством смешивания указанного тяжелого углеводородного сырья с избыточным водородом; b) предоставление гидроочищенного углеводородного продукта, содержащего менее 30 мас. частей на миллион азота путем гидроочистки указанного продукта, подаваемого в гидроочиститель, посредством введения его в контакт с материалом, каталитически активным в гидроочистке в условиях гидроочистки; c) предоставление гидроочищенного продукта либо в виде гидроочищенного ...

СПОСОБ УЛУЧШЕНИЯ ТЕМПЕРАТУРЫ ПОТЕРИ ПОДВИЖНОСТИ УГЛЕВОДОРОДНОГО СЫРЬЯ, ПОЛУЧЕННОГО В ПРОЦЕССЕ ФИШЕРА-ТРОПША, ИСПОЛЬЗУЮЩИЙ КАТАЛИЗАТОР НА ОСНОВЕ ЦЕОЛИТА ZBM-30

Настоящее изобретение относится к способу депарафинизации сырья, полученного способом Фишера-Тропша, в котором обрабатываемое сырье приводится в контакт с катализатором, содержащим по крайней мере один цеолит ZBM-30, синтезированный в присутствии триэтилентетрамина, по крайней мере один гидрирующий-дегидрирующий элемент, предпочтительно выбранный из элементов группы VIB и группы VIII Периодической системы элементов, и по крайней мере одну неорганическую пористую матрицу. Изобретение позволяет осуществлять превращения с хорошим выходом сырья, имеющего повышенные температуры потери подвижности, по крайней мере в одну фракцию, имеющую низкую температуру потери подвижности и высокий индекс вязкости для базовых масел. 12 з.п. ф-лы, 1 ил., 2 табл.

СПОСОБ ПОЛУЧЕНИЯ ОСНОВЫ СМАЗОЧНОГО МАСЛА, КАТАЛИЗАТОР

Изобретение может быть использовано в нефтехимии. Основу смазочного масла получают контактированием в присутствии водорода углеводородного сырья с катализатором, который содержит компонент гидрогенизации, нанесенный на аморфный алюмосиликатный носитель, имеющий микропористость 5 - 50 об.%, общий объем пор 0,6-1, 2 мл/г, содержание оксида алюминия 5-75 мас.%. Предпочтительно сырьем являются парафиновый гач и синтетические парафины. Предпочтительный катализатор для использования в способе включает сочетание одного или нескольких металлов из числа кобальта, железа и никеля и одного или нескольких металлов из числа хрома, молибдена и вольфрама на аморфном алюмосиликатном носителе, имеющем макропористость 5 - 50 об.%, общий объем пор 0,6-1,2 мл/г, содержание оксида алюминия 5-75 мас.%. Такой катализатор является особенно предпочтительным, когда перерабатывают углеводородное сырье, содержащее значительные количества азот- или серусодержащих соединений. 2 с и 11 з.п. ф-лы, 3 табл.

СПОСОБ ПОЛУЧЕНИЯ РАЗВЕТВЛЕННОГО УГЛЕВОДОРОДНОГО КОМПОНЕНТА

... 1. Базовое масло, отличающееся тем, что базовое масло содержит разветвленные углеводороды, имеющие число атомов углерода по меньшей мере С18, оно содержит по меньшей мере 90% по весу насыщенных углеводородов, не более чем 15% по весу мононафтенов, и не более чем 1% по весу конденсированных динафтенов и полинафтенов, с индексом вязкости более чем 120, с базовым маслом биологического происхождения, и по меньшей мере 60% по весу насыщенных углеводородов, имеющих не более чем 5 атомов углерода. ! 2. Базовое масло по п.1, отличающееся тем, что базовое масло включает по меньшей мере 95% по весу насыщенных углеводородов, и по меньшей мере 75% по весу насыщенных углеводородов, имеющих не более чем 3 атома углерода. ! 3. Базовое масло по п.2, отличающееся тем, что оно включает по меньшей мере 97% по весу насыщенных углеводородов. ! 4. Базовое масло по любому из пп.1-3, отличающееся тем, что индекс вязкости базового масла составляет по меньшей мере 130. ! 5. Базовое масло по п.1, отличающееся тем ...

КОНВЕРСИЯ РАСТИТЕЛЬНЫХ МАСЕЛ В БАЗОВЫЕ МАСЛА И ТОПЛИВА ДЛЯ ТРАНСПОРТНЫХ СРЕДСТВ

... 1. Способ, включающий стадии ! а) переработки содержащего триглицериды растительного масла с протеканием олигомеризации компонентов на основе ненасыщенных жирных кислот, содержащихся в нем, с получением олигомеризованной смеси; ! b) изомеризации олигомеризованной смеси над катализатором изомеризации с получением изомеризованной смеси, причем изомеризованная смесь включает компонент базового масла и компонент дизельного топлива; ! с) удаление из изомеризованной смеси воды с получением сухой изомеризованной смеси, причем сухая изомеризованная смесь включает, по меньшей мере, 10 мас.% алканов с числом атомов углерода 30 или больше; ! d) разделения сухой изомеризованной смеси на низкокипящую фракцию, из которой впоследствии получают дизельное топливо, и высококипящую фракцию; и ! е) последующей дополнительной изомеризации, по меньшей мере, части высококипящей фракции с получением базового масла. ! 2. Способ по п.1, дополнительно включающий стадию очистки базового масла гидрированием с получением ...

СПОСОБ ГИДРООБРАБОТКИ В КИСЛОЙ СРЕДЕ ДЛЯ ПРОИЗВОДСТВА БАЗОВЫХ СМАЗОЧНЫХ МАСЕЛ

... 1. Способ получения базового смазочного масла, включающий:приведение гидроочищенного сырья и водородсодержащего газа в контакт с катализатором депарафинизации при условиях, эффективных для каталитической депарафинизации,где объединенное общее содержание серы в жидкой и газообразной формах, подававшейся на стадию приведения в контакт, составляет более 1000 мас.ч. на млн по отношению к гидроочищенному сырью, икатализатор депарафинизации включает по меньшей мере один недеалюминированный цеолит с одноразмерными порами, образованными десятичленными кольцами, по меньшей мере один металл группы VIII, и по меньшей мере одно огнеупорное связующее на основе оксида металла с низкой площадью поверхности.2. Способ по п.1, в котором до стадии приведения в контакт поток, выходящий из стадии гидроочистки, подают по меньшей мере в один сепаратор высокого давления для отделения газовой фракции гидроочищенного выходящего потока от жидкой фракции гидроочищенного выходящего потока.3. Способ по п.2, в котором ...

КАТАЛИТИЧЕСКАЯ СИСТЕМА ДЛЯ ДЕПАРАФИНИЗАЦИИ

СПОСОБ ПОЛУЧЕНИЯ ОСНОВЫ СМАЗОЧНЫХ МАСЕЛ, КАТАЛИЗАТОР

Предлагается способ получения основы смазочного масла, включающий приведение в контакт в присутствии водорода углеводородного сырья с катализатором, который содержит компонент гидрогенизации, нанесенный на аморфный алюмосиликатный носитель, имеющий макропористость в интервале от 5 до 40 об.%. Наиболее предпочтительным углеводородным сырьем являются парафиновый гач и синтетические парафины. Предпочтительный катализатор для использования в способе включает сочетание одного или нескольких металлов из числа кобальта, железа и никеля и одного или нескольких металлов из числа хрома, молибдена и вольфрама, на аморфном алюмосиликатном носителе, имеющем макропористость в интервале от 5 до 50 об.%. Такой катализатор является особенно редпочтительным, когда перерабатывают углеводородное сырье, содержащее значительные количества азот- или серусодержащих соединений.

СПОСОБ ПОЛУЧЕНИЯ БАЗОВОГО МАСЛА ДЛЯ СМАЗОЧНЫХ МАТЕРИАЛОВ

... 1. Способ получения базового масла для смазочных материалов, где базовое масло для смазочных материалов получаютна первой стадии, где сырьевое масло, содержащее нормальные парафины Сили более, подвергают реакции изомеризации таким образом, что содержание нормальных парафинов Сили более составляет 6-20 мас.% от общей массы углеводородов Сили более в полученном продукте реакции,на второй стадии, где фракцию смазочного масла, содержащую углеводороды Сили более, отделяют от продукта реакции первой стадии, и на третьей стадии, где фракцию смазочного масла, полученную на второй стадии, разделяют на депарафинизированное масло и парафин депарафинизацией растворителем.2. Способ получения базового масла для смазочных материалов по п.1, где все количество или часть отделенного на третьей стадии парафина повторно используют в качестве части сырьевого масла для первой стадии.3. Способ получения базового масла для смазочных материалов по п.1, где сырьевое масло для первой стадии включает парафин Фишера-Тропша ...

СПОСОБ ПОЛУЧЕНИЯ БАЗОВОГО СОСТАВА СМАЗОЧНОГО МАСЛА

... 1. Способ получения базового состава смазочного масла, включающийпервую стадию приведения в контакт исходных материалов, содержащих нормальные парафины, имеющие не менее 20 атомов углерода, с первым катализатором в присутствии молекулярного водорода с получением первого получаемого масла, ивторую стадию приведения в контакт первого получаемого масла со вторым катализатором в присутствии молекулярного водорода с получением второго получаемого масла, гдепервый катализатор содержит первый носитель, в котором доля количества NH, которое десорбируется при 300-800°C, в расчете на общее количество NH, которое может десорбироваться, составляет 80-90%, при десорбции NHс программируемым изменением температуры; первый металл, который представляет собой по меньшей мере один металл, выбранный из металлов, которые принадлежат к Группе VI Периодической таблицы, и нанесенный на первый носитель; и второй металл, который представляет собой по меньшей мере один металл, выбранный из металлов, которые принадлежат ...

КОНВЕРСИЯ И ИЗВЛЕЧЕНИЕ КЕРОНЕНА НА МЕСТЕ ЗАЛЕГАНИЯ

... 1. Способ извлечения продукта на основе керогена из погребенной сланцевой формации, содержащей погребенный сланец, включающий следующие стадии:доставку окислителя к керогену в погребенном сланце;контактирование керогена в погребенном сланце с окислителем при температуре в интервале от 0°C до 200°C, чтобы образовать органические кислоты; ипридание подвижности по меньшей мере части органических кислот из погребенной сланцевой формации, чтобы получить первый подвижный продукт на основе керогена.2. Способ по п. 1, в котором окислитель подают к керогену в погребенном сланце в реакционной текучей среде, и в котором данная реакционная текучая среда содержит окислитель в интервале от 0,1 мас.% до 40 мас.% и имеет pH в интервале от 7 до 9.3. Способ по п. 1, в котором окислитель подают к керогену в погребенном сланце в текучей среде в погребенной сланцевой формации, чтобы образовать пластовую текучую среду, и в котором пластовая текучая среда содержит от 0,1 мас.% до 40 мас.% окислителя и имеет pH ...

СПОСОБ ПОЛУЧЕНИЯ СМАЗОЧНОГО БАЗОВОГО МАСЛА

... 1. Способ получения смазочного базового масла, имеющего содержание насыщенных веществ выше, чем 90 вес.% и индекс вязкости выше, чем 90, в котором используют в качестве исходного сырья продукты вакуумной дистилятной перегонки путем проведения следующих стадий:(a) обработки продуктов вакуумной дистилляции растворителем для экстракции, избирательным в отношении экстракции ароматических соединений из продуктов вакуумной перегонки,(b) смешивания экстрагированного масла, полученного на стадии (а), с сырьем, включающим более чем 50 вес.% воска или включающим более чем 80 вес.% парафинов и имеющим температуру текучести выше, чем 0°С,(c) гидроочистки смеси, полученной на стадии (b),(d) каталитической депарафинизации гидроочищенного масла, полученного на стадии (с), для получения смазочного базового масла, и(e) контактирования депарафинизированного масла с катализатором насыщения ароматических веществ.2. Способ по п.1, в котором сырьем, включающим более чем 50 вес.% воска на стадии (b), является ...

Verfahren mit einer Katalysatorkombination für Isomerisation von Wachs

"VERFAHREN ZUR HERSTELLUNG VON KAELTEMASCHINENOELEN"

Verfahren zur Herstellung hochwertiger Schmieroele aus hochmolekularen Paraffinen der katalytischen Kohlenoxydhydrierung

Verfahren zur Herstellung von Basisoelen mit hohem Viskositaetsindex,welche sich zur Erzeugung von Schmieroelen eignen

Neue Katalysatoren und ihre Verwendung

VERFAHREN ZUR HERSTELLUNG VON SPINDELÖLEN, LEICHTEN MASCHINENÖLEN UND MITTLEREN MASCHINENÖLEN

Verfahren zur Herstellung naphthenischer Schmieroele

VERFAHREN ZUR HERSTELLUNG VON GRÜNDSCHMIERÖLE

Verfahren zum Regenerieren von gebrauchten Schmieroelen

KATALYSATOR FUER DIE HYDRIERENDE KRACKUNG VON VAKUUMDESTILATEN UND/ODER BITUMENFREIEN VAKUUMDESTILATIONSRUECKSTAENDEN

HYDROCRACKING PROCESS

... 1,250,038. Hydrocracking. SUN OIL CO. 24 Oct., 1969 [19 Nov., 1968], No. 52133/69. Heading C5E. Lube oils are made by hydrocracking a feed comprising a lube oil charge stock and 5-80 volume per cent of a diluent of viscosity 0À15- 17 centistokes at 100‹ F. Suitable diluents are hexane, heptane, naphtha, fuel oil and 60 S.U.S. neutral oil. Suitable feeds having initial boiling points of at least 650‹ F. are waxy and dewaxed vacuum distillates, deasphalted or Duo-Sol extracted residuum, and waxy and dewaxed deasphalted residua. The hydrocracking can be carried out at 650-875‹F. with a hydrogen partial pressure of 500-10,000 p.s.i. using a catalyst comprising at least one oxide or sulphide of Ni, W, Co or Mo on an alumina carrier. The catalyst can be used in two or more beds so that the feed can be fractionated and fed so that the heavier fractions can undergo more severe cracking. The lube oil products can be hydrogenated, extracted with furfural or rehydrocracked.

STABILITY OF HYDROCRACKED LUBRICATING OILS TO AIR AND LIGHT

... 1341296 Lubricating oils ESSO RESEARCH & ENG CO 19 April 1971 [16 March 1970] 22222/71 Heading C5E Lubricating oil is made by subjecting a distillate hydrocarbon fraction or a deasphalted residuum to catalytic hydrocracking, separating a lubricating oil fraction boiling above 650‹ F. from the hydrocracked effluent, and extracting this fraction with N-methyl-2-pyrrolidone to produce a raffinate which is resistant to deterioration upon exposure to light and air. In the example a blend of deasphalted oil and heavy vacuum gas oil is hydrocracked at 780‹ F. and 2500 p.s.i.g. using a catalyst of nickel and molybdenum on a silica-alumina support and separated to provide a SAE 10 lube oil distillate which is then dewaxed and extracted 5 times with N-methyl-2-pyrrolidone; as a comparison using aqueous phenol.

LUBRICATING OIL HYDROTREATING PROCESS

... 1414170 Hydrotreating lubricating oils GULF RESEARCH & DEVELOPMENT CO 20 Oct 1972 [20 Oct 1971 (2)] 48440/72 Heading C5E Lubricating oils are produced by fractionating a crude lubricating oil of which 10-90% by volume boils below 510‹ C. into a residual and a distillate fraction, hydrotreating the residual fraction at 343-454‹ C. and hydrotreating the distillate fraction at 371-482‹ C. under more severe conditions than those employed for hydrotreating the residual fraction; the conditions employed for hydrotreating both fractions comprise a pressure of 140-700 kg./cm.2, a CHSV of 0À1-10, a hydrogen feed rate of 35À6- 178 SCM per 100 litres of charge oil and are such that yields of at least 50% by volume, based upon the respective charge oils, of hydrotreated materials boiling above 329‹ C. are obtained. A suitable catalyst comprises nickel and tungsten on silicaalumina and is promoted with fluorine. Fig. 1 illustrates an embodiment in which an oil 10 is separated into a distillate ...

Process for making lubricating oils

PROCESS FOR THE PRODUCTION OF WHITE MINERAL OIL

... 1310320 White mineral oils ATLANTIC RICHFIELD CO 14 June 1971 27795/71 Heading C5E White mineral oil is produced from a raw, waxy mineral lubricating oil distillate by (a) hydrorefining at 600-800‹ F. using a sulphur resistant hydrogenation catalyst; (b) hydrogenating the hydrorefined oil at 600-950‹ F. using a hydroisomerization-hydrocracking catalyst comprising a major amount of silicaalumina, 10% alumina, 0À1 to 5 wt. per cent of a platinum group metal, and 3 to 25 wt. per cent of an at least 50% hydrogen exchanged crystalline aluminosilicate having a pore size of 8 to 15 Š and a silica : alumina mole ratio greater than 3 : 1; and (c) hydrogenating the product from (b) at 450-700‹ F. using a platinum group metal catalyst to saturate aromatics. The hydrorefining catalyst suitably comprises nickel molybdate on alumina and can be presulphided with H 2 S before use; the hydrogenation catalyst used in step (c) suitably comprises 0À01 to 2 wt. per cent platinum on alumina.

Process for converting waxy feeds into low haze heavy base oil

Integrated FT process having optimised H2 and pressure loops

An integrated process for producing Fischer-Tropsch derived products boiling in the range of liquid fuel and lubricating base oil comprises (a) recovering from a Fischer-Tropsch synthesis a Fischer-Tropsch wax 2 and a Fischer-Tropsch condensate 78; (b) hydroprocessing the wax in zone 6 and recovering a waxy intermediate 12 and a hydrogen-rich normally liquid fraction 72; (c) mixing the Fischer-Tropsch condensate 78 from step (a) and at least part of the hydrogen-rich normally liquid fraction 72 from step (b) to form a Fischer-Tropsch condensate mixture 74; (d) hydrotreating the Fischer-Tropsch condensate mixture in zone 76 and recovering a Fischer-Tropsch condensate product 78; (e) recovering from the Fischer-Tropsch condensate product a Fischer-Tropsch derived hydrocarbon boiling within the range of liquid fuel 96,98; (f) dewaxing the waxy intermediate from step (b) in a catalytic dewaxing zone 26 and recovering a base oil 32; (g) hydrofinishing 30 the base oil from step (f); (h) recovering ...

Integrated process for the production of lubricating base oils and liquid fuels from Fischer-Tropsch materials using split feed hydroprocessing

Process for making lubricating oils

Extending engine lubricant life

The present invention relates to a system and method for extending lubricant life in an engine fuelled by glycerine or other polyol-containingfuels. The system 6 is arranged to draw off a fraction of the lubricating oil from the engine 1, process this oil to remove the contaminants and then return the oil to the engine. In this process, the lubricating oil that is removed from the engine is passed over a heated surface under reduced pressure to vaporize the contaminants and remove them from the lubricating oil. The system 6 may be used to continuously remove contaminants from the lubricating oil without disrupting the running of the engine 1.

Improvements relating to the refining of lubricating oils

A hydrofining process for producing lubricating oils having improved colour and oxidation stability comprises treating the oils with hydrogen at elevated temperature and pressure, for example 150-370 DEG C. and 5-80 atmos., in the presence of a catalyst consisting of the oxides of cobalt and molybdenum incorporated with a mixture of iron and magnesium oxides prepared by coprecipitation. The preferred hydrogen feed rate is 5-150 v./vol. and the preferred oil feed rate is 0.5-6 v./vol. catalyst/hr. The iron oxide content is preferably at least 10% wt., the ratio magnesium oxide : iron oxide in the region 2 : 1, and the ratio molybdenum oxide : cobalt oxide at least 3 : 1. In an example, the catalyst is prepared by pouring a boiling solution of ferric nitrate and magnesium sulphate into a boiling solution of caustic soda, filtering, washing, drying, calcining, and granulating, pouring ammonium molybdate solution over the granules and drying, impregnating twice with cobalt nitrate solution, ...

Modified composite molecular sieve and preparation method and application thereof, and catalyst and application thereof

The present invention provides a modified composite molecular sieve, and a preparation method and an application of the modified composite molecular sieve. The modified composite molecular sieve comprises SiO2 and a composite molecular sieve that comprises molecular sieve MCM-22 and zeolite A selected from at least one of ZSM-22, ZSM-23 and ZSM-48, wherein the molecular sieve MCM-22 covers around the zeolite A. The SiO2 is loaded on the composite molecular sieve. A catalyst is also provided that comprises a carrier and a noble metal loaded on the carrier, wherein, the carrier comprises the modified composite molecular sieve. The use of the catalyst in paraffin isomerization is also claimed, wherein the raw material for isomerization is a waxy raw material with an initial boiling point equal to, or higher than, 140°C. Suitably, the raw material for isomerization is one or more of diesel oil, white oil, atmospheric heavy distillate, reduced pressure distillate, hydrocracking tail oil, lube ...

PROCESS FOR THE PREPARATION OF LUBRICATING OILS

... 1440230 Lubricating oils SHELL INTERNATIONALE RESEARCH MAATSCHAPPIJ BV 2 Aug 1973 [4 Aug 1972] 36732/73 Heading C5E A feed composed of a vacuum distillate and/or deasphalted residual mineral oil is catalytically hydrocracked in the presence of hydrogen and a hydrocracking catalyst, the portion of the oil boiling above 350-400‹ C. is dewaxed to produce a high viscosity index lubricating oil and wax, the wax is subjected to catalytic hydroisomerization in the presence of hydrogen and a catalyst comprising (a) boron, (b) an oxidic carrier, (c) Fe, Co and/or Ni, and (d) Cr, Mo and/or W and lubricating oil of high viscosity index is obtained by dewaxing the hydroisomerization product. The hydrocracking can be carried out at 300-550‹ C. and 50-250 bar abs. using a catalyst such as nickel and molybdenum on alumina containing F and P. The hydroisomerization can be carried out at 310-150‹ C. and 50-200 bar; and the wax obtained by dewaxing this effluent can be recycled to the hydrocracking or hydroisomerization ...

Process of producing White Mineral Oil

... 1,177,155. Hydrofining. SINCLAIR RESEARCH Inc. 15 Aug., 1967 [16 Aug., 1966; 20 July, 1967], No. 37511/67. Heading C5E. A process for preparing a white mineral oil comprises hydrogenating a raw petroleum oil fraction of lubricating viscosity having a specific dispersion (as defined) below 180 by contact with hydrogen in the presence of a sulphur-resistant hydrogenation catalyst at a temperature of 600‹ to 750‹ F., a pressure of 1500 to 5000 p.s.i.g., a weight hourly space velocity of 0À1 to 0À5, and a hydrogen feed rate of 1000 to 5000 SCF/B to provide a hydrogenated oil, and further hydrogenating said hydrogenated oil by contact with hydrogen in the presence of a platinum group metal-alumina catalyst at a temperature of 500‹ to 700‹ F., and at least 50‹ F. lower than the temperature of the first hydrogenation stage, a pressure of 1000 to 5000 p.s.i.g., a weight hourly space velocity of 0À25 to 0À75, and a hydrogen feed rate of 500 to 5000 SCF/B to provide a white mineral oil product. The ...

PROCESS FOR PRODUCING HIGH VISCOSITY INDEX LUBRICATING OIL

... 1311431 Lubricating oils ATLANTIC RICHFIELD CO 6 Jan 1971 [26 Jan 1970] 701/71 Heading C5E Lubricating oils are produced by (a) contacting a deasphalted mineral lubricating oil fraction, containing at least 0À3% sulphur and at least 1000 ppm. nitrogen and derived from a waxy crude oil, with hydrogen in the presence of a sulphur-resistant hydrogenation catalyst at 600-800‹ F. and (b) contacting the effluent oil with hydrogen at 500-800‹ F. in the presence of a hydrogenation-hydrocracking catalyst, comprising a major amount of an at least 50% hydrogen- or rare-earth-exchanged crystalline aluminosilicate having pores of diameter 8-15Š and a silica to alumina mole ratio greater than 3 : 1 and a minor amount of a platinium group metal, to give a maximum of 50% conversion of the oil to materials boiling below 550‹ F. The sulphur-resistant catalyst can contain Sn, V, Cr, Mo, W, Fe, Co and/or Ni as such or as the oxides or sulphides, e.g. oxides or sulphides of Ni or Co together with Mo, W or Cr ...

PROCESS FOR IMPROVING THE VISCOSITY INDEX OF A LUBRICATING OIL FRACTION

... 1,216,510. Hydrogenating petroleum oils. SINCLAIR RESEARCH Inc. 3 Jan., 1968 [10 Jan., 1967], No. 379/68. Heading C5E. 1. A process for improving the viscosity index of a lubricating oil fraction distilling within the range of 700‹ to 1200‹ F. and having a viscosity index of from - 200 to + 50, comprises hydrogen processing said lubricating oil fraction over a Group VIII iron transition series metal promoted catalyst at a pressure of from 1000 to 3000 p.s.i.g. hydrogen partial pressure, a temperature of from 700‹ to 850‹ F., a space velocity of from 0.20 to 2.0 WHSV, and a hydrogen rate of from 500 to 3000 S.C.F. of molecular hydrogen per barrel of feed, flashing off the reactor effluent a major portion of the hydrogen and other gases, and thereafter stripping the hydrocracked components having a boiling point below 550‹ F., from the reactor effluent to yield a stripper bottoms primary product having a viscosity index at least 75 VI units greater than the viscosity index of the lubricating ...

PRODUCTION OF WHITE MINERAL OIL

... 1499570 Producing white mineral oil ATLANTIC RICHFIELD CO 9 April 1975 [11 April 1974] 14631/75 Heading C5E White mineral oil is produced from a mineral oil distillate of lubricating viscosity by first contacting the distillate with hydrogen in the presence of a sulphur-resistant catalyst to form a hydrogenated oil and then contacting at least a portion of the hydrogenated oil with hydrogen in the presence of a second catalyst to form a refined oil from which the white mineral oil is recovered, the second catalyst comprising a major amount of a support, a minor catalytically-effective amount of at least one palladium component and a minor amount of at least one halogen component sufficient to improve the hydrogenation activity of the second catalyst. The first contacting step may be effected at a temperature of 600‹-800‹ F., a pressure of 1500-5000 p.s.i.g., a weight hourly space velocity of 0À1-1À0 and a hydrogen to mineral oil distillate ratio of 1000-5000 s.c.f./b. and the second contacting ...

Improvements relating to the production of lubricating oils

Lubricating oils with a viscosity index of at least 125 are prepared from petroleum feedstocks with a viscosity index of at least 90 by solvent extracting the feedstock to give a raffinate with a content of carbon in the form of aromatic rings of less than 5%, treating the raffinate so obtained in the presence of hydrogen and a hydrogenation catalyst at 200-800 DEG F. and 1000-2000 p.s.i.g., and recovering a product having an increased viscosity index of at least 125. This product may then be fractionated to remove lower-boiling material and dewaxed. Finally clay treatment of hydrofinishing may be carried out. The hydrocatalytic treatment may be effected in a single stage in the presence of a sulphur insensitive catalyst such as tungsten-nickel sulphide, or in two stages, first with a sulphur-insensitive catalyst to effect desulphurization, and then with a sulphur-sensitive catalyst. The finished oil may have oxidation inhibitors added, for example, antimony diamyl dithiocarbamate blended ...

Process for production of lubricating oils

Naphthenic type lubricating oils are obtained by subjecting a mixed base lubricating oil distillate fraction to a solvent extraction and dewaxing treatment, the solvent extraction including the steps of extracting with an aromatic-selective solvent, for example, phenol, furfural, liquid SO2, nitrobenzene, and nitroparaffins, in a first stage to obtain a first extract phase, which extract phase is then separated into a second extract phase and a second raffinate phase, from which raffinate phase most of the paraffinic and aromatic compounds have been excluded, and hydrogenating the dewaxed second raffinate in the presence of a catalyst. The dewaxing step may either precede or preferably follow the solvent extraction. The separation of the first extract phase may be effected by at least one of the steps of cooling and injection of anti-solvent, for example water, if desired with concomitant extraction with an aromatic-selective solvent. The dewaxing may be effected by means of a solvent, ...

Perfectioonements relating to the treatment of the aromatic extracts.

Process of processing of lubricating mineral oils by spared hydrogeneration and catalysts for this process.

Hydrodewaxed hydrocarbon fluid used in the manufacture of fluids for industrial, agricultural, or domestic use.

HYDRODEWAXED HYDROCARBON FLUID USED IN THE MANUFACTURE OF FLUIDS FOR INDUSTRIEL, AGRICULTURAL OR DOMESTIC USE

Hydrodewaxed hydrocarbon fluid used in the manufacture of fluids for industrial, agricultural, or domestic use.

Process of refining to the hydrogen of lubricating oils.

Process of processing of lubricating mineral oils by spared hydrogenation and catalyst for this process.

Process of hydrocatalytic refining of lubricating oils, and catalyst for this process.

Hydrodewaxed hydrocarbon fluid used in the manufacture of fluids for industrial, agricultural, or domestic use.

MIXTURE, CONTAINING BASIC OILS OF THE GROUP OF III AND THE GROUP OF IV

PROCEDURE FOR THE PRODUCTION OF FUELS AND LUBRICATING OILS FROM FISCHER TROPSCH WAX

MINERAINSULIERÖL, PROCEDURES FOR THE PRODUCTION OF A MINERAINSULIERÖLS AND A PROCEDURE FOR THE USE OF A MINERAINSULIERÖLS

PROCEDURE FOR THE PRODUCTION OF HYDROCARBONS

PRODUCTION OF A HYDRAULIC TREATMENT CATALYST.

PROCEDURE FOR THE PRODUCTION OF LUBRICATING OILS FROM OLEFINEN BY ISOMERIZATION OVER A SILIKOALUMINOPHOSPHAT CATALYST.

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

CATALYST AND PROCEDURE FOR THE HYDROGEN TREATMENT.

Procedure for the catalytic transformation of hydrocarbons

PROCEDURE FOR THE PRODUCTION OF A MICRO-CRYSTALLINE WAX

PROCEDURES FOR THE PRODUCTION OF A HEAVY ONE AND AN EASY ONE LUBRICATE L-GRUND LS

PROCEDURE FOR THE PRODUCTION OF CRACK PRODUCTS WITH LOW SULFUR AND STICKSTOFFGEHALT

Procedure for the hydrauliccatalytic refining of lubricating oils

PROCEDURE FOR THE PRODUCTION OF A WAXLIKE RAFFINATE

Procedure for the production of lubricating oils with very high viscosity index

PROCESS FOR THE PREPARATION OF A LUBRICATING BASE OIL

CATALYTIC DEWAXING

Method for preparing lubricating oils

Fuels and lubricants using layered bed catalysts in hydrotreating waxy feeds, including Fischer-Tropsch wax

Gas distributor for a reactor

Zeolite cit-5

Hydrocracking of heavy feedstocks with improved hydrogen management

Hydroisomerization catalyst, process for producing the same, method of dewaxing hydrocarbon oil, and process for producing lube base oil

Systems and methods for separating oil and/or gas mixtures

A system for producing oil from an underground formation comprising a well above the formation; a mechanism to inject an enhanced oil recovery formulation into the formation, the enhanced oil recovery formulation comprising water and a solvent; a mechanism to produce the water, solvent, oil, and gas from the formation; a separator to separate the oil, water, and a first portion of the solvent from the gas and a second portion of the solvent; and an absorption tower to expose the gas and the second portion of the solvent to water to remove the second portion of the solvent from the gas.

Method for continuous use of a vaccum-set water knock-out circuit integrated with a hydraulic oil reservoir

The invention relates to a method for the continuous use of a vacuumized water knockout circuit integrated with a contaminated hydraulic-oil reservoir, a tank (1). A continuous process is based on a vacuum pump (12) keeping both a treatment column (8) and the tank (1) vacuumized at up to typically 98 %, contaminated hydraulic oil being pumped via the pump (3) up from the lowermost point in the inclined tank (1) through a circulation filter to a heating element (6) into the treatment column (8), where the moisture is extracted from the oil. Controlled oil flow, temperature and underpressure make water vapour be pushed continuously towards the vacuum pump (12) through a vapour cooler (13) into a condensate trap (15) which is emptied automatically via a valve (17), while gases are continuously evacuated from the vacuum pump (12) via a gas filter (18). Continuous transport of vapour out of the treatment column (8) is ensured by air being supplied via an air filter (21) through a fixed nozzle ...

PROCESS TO PREPARE A CATALYTICALLY DEWAXED GAS OIL OR GAS OIL BLENDING COMPONENT

Novel hydrocarbon base oil for lubricants with very high viscosity index

MOLECULAR SIEVE SSZ-64

Lubrication oil and internal-combustion engine fuel

The objective is to provide lubrication oil and internal-combustion engine fuel for reducing the fuel consumption and for reducing carbon dioxide and other exhaust 5 gas components. The lubrication oil is injected with lubrication oil impregnating agent composed of dimethylalkyl tertiary amine in the range from 0. 01 to 1 volume% and desirably in the range from 0.1 to 0.5 volume%. Petroleum oil fuel is injected with fuel 10 oil impregnating agent composed of dimethylalkyl tertiary amine in the range from 0.5 to 1 volume%. The petroleum oil fuel is light oil, kerosene, gasoline, or Bunker A. Any one or both of these lubrication oil and petroleum oil fuel is/are used for an internal-combustion engine. [FIG. 1] 3) a ...

Method for ketonisation of biological material

The present invention relates to a method for producing ketones which method comprises the steps of: a) providing a feedstock of biological origin comprising fatty acids and/or fatty acid derivatives having an average chain length of 24 C-atoms or less, b) subjecting said feedstock to a catalytic ketonisation reaction in the presence of a K ...

PREPARATION OF LUBRICATING OILS

Hydroconversion process using bulk group VIII/group VIB catalysts

HYDROISOMERIZATION

METHOD FOR ISOMERIZATION WAX TO LUBE BASE OILS USING A SIZED ISOMERIZATION CATALYST

Process for the preparation of lubricating base oils

HYDROGENATION PROCESS

BASE-OIL COMPOSITIONS

HYDROCARBON CONVERSION PROCESS

METHOD OF MAKING MINERAL LUBRICATING OIL BY TWO-STAGE HYDROTREATING

HYDROCARBON CONVERSION PROCESS

CATALYST COMPOSITION, ITS PREPARATION AND USE

An unsupported catalyst composition which comprises one or more Group VIb metals, one or more Group VIII metals, and a refractory oxide material which comprises 50 wt% or more titania, on oxide basis, which is prepared by precipitation techniques, finds use in the hydroprocessing of hydrocarbonaceous feedstocks.

HEAVY LUBE OIL FROM FISCHER-TROPSCH WAX

A heavy lubricant base stock is made by (a) producing a synthesis gas from natural gas, (b) reacting the H2 and CO in the gas in the presence of a cobalt Fischer-Tropsch catalyst, at reaction conditions effective to synthesize waxy hydrocarbons boiling in the heavy lubricant oil range, which are hydrodewaxed it at least two stages, with interstage separation and removal of the lighter material.

PRODUCTION OF LUBRICATING OILS

PROCESS FOR THE MANUFACTURE OF LUBRICATING OIL

DUAL CATALYST SYSTEM FOR HYDROISOMERIZATION OF FISCHER-TROPSCH WAX

The present invention relates to a process for converting Fischer~Tropsch wax to high quality lube basestocks using a molecular sieve Beta catalyst followed by a unidimensional intermediate pore molecular sieve with near circular pore structures having an average diameter of 0.50 run to 0.65 nm wherein the difference between the maximum diameter and the minimum is <= 0.05 nm. Both catalysts comprise one or more Group VIII metals. For example, a cascaded two- bed catalyst system consisting of a first bed Pt/Beta catalyst followed by a second bed Pt/ZSM-48 catalyst is highly selective for wax isoinerization and lube hydrodewaxing with minimal gas formation.

HYDROCRACKING PROCESS USING BULK GROUP VIII/GROUP VIB CATALYSTS

Hydrocracking process for hydrocracking petroleum and chemical feedstocks using bulk Group VIII/Group VIB catalysts. Preferred catalysts include those comprised of Ni-Mo-W.

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.

Oligomerization of propylene and longer chain alpha olefins to produce base oil products

We provide a process for making a base oil, comprising: mixing one or more longer chain alpha olefins comprising C6+ olefins with an olefin feed comprising propylene to make a mixed olefin feed; and oligomerizing the mixed olefin feed using an acidic chloroaluminate ionic liquid catalyst to form an oligomer; wherein the oligomer is a base oil that has: i. a kinematic viscosity at 100° C. greater than 10 mm 2 /s; ii. a viscosity index from 50 to 90; iii. a pour point less than −19° C.; and iv. a cloud point less than −50° C.

Lubricant additives

Processes are described for producing liquid, biobased lubricant additives containing from 50 to 100% biobased carbon according to ASTM D6866 from heat-bodied oils by transesterification with biobased or petroleum based alcohols and by hydrotreatment of at least the resulting diesters, triesters and polyesters.

Fuel and base oil blendstocks from a single feedstock

A method comprising the steps of providing a quantity of biologically-derived oil comprising triglycerides; processing the biologically derived oil so as to transesterify at least some of the triglycerides contained therein to yield a quantity of saturated monoesters and unsaturated monoesters; oligomerizing at least some of the unsaturated monoesters to yield a quantity of fatty acid ester oligomers; separating at least some of the saturated monoesters from the fatty acid ester oligomers; and hydrotreating at least some of the fatty acid ester oligomers to yield a quantity of alkanes.

Fuel and base oil blendstocks from a single feedstock

A method comprising providing a fatty acyl mixture comprising: (i) a C 10 -C 16 acyl carbon atom chain content of at least 30 wt. % wherein at least 80% of the C 10 -C 16 acyl carbon atom chains are saturated; and (ii) a C 18 -C 22 acyl carbon atom chain content of at least 20 wt. % wherein at least 50% of the acyl C 18 -C 22 carbon atom chains contain at least one double bond; hydrolyzing the mixture to yield a quantity of C 10 -C 16 saturated fatty acids and C 18 -C 22 unsaturated fatty acids; oligomerizing at least some of the C 18 -C 22 unsaturated fatty acids to yield a quantity of C 36+ fatty acid oligomers; hydrotreating at least some of the C 10 -C 16 saturated fatty acids and at least some of the C 36+ fatty acid oligomers to yield a quantity of diesel fuel blendstock and C 36+ alkanes; and separating at least some of the diesel fuel blendstock from the C 36+ alkanes.

Process for the dehydration of aqueous bio-derived terminal alcohols to terminal alkenes

A method and apparatus for dehydrating bio-1-alcohols to bio-l-alkenes with high selectivity. The bio-1-alkenes are useful in preparing high flashpoint diesel and jet biofuels which are useful to civilian and military applications. Furthermore, the bio-1-alkenes may be converted to biolubricants useful in the transporation sector and other areas requiring high purity/thermally stable lubricants.

Iron oxide magnetic nanoparticle, its preparation and its use in desulfurization

The present invention provides a method of preparing an iron oxide magnetic nanoparticle, comprising the steps of: i) reacting a water-soluble ferrous salt with a water-soluble ferric salt in a mole ratio of 1:2 in the presence of a base and a citrate to give an iron oxide particle surface-coated with the citrate (c-MNP); ii) reacting the c-MNP obtained in step (i) with a thiophilic compound to give a thiophilic compound-bounded iron oxide particle surface-coated with the citrate (thiophilic-c-MNP); and iii) modifying the thiophilic-c-MNP obtained in step (ii) using a surfactant for phase transfer of the thiophilic-c-MNP from aqueous phase to organic phase. The present invention also relates to the iron oxide magnetic nanoparticle prepared by the above-mentioned method and the use of the nanoparticle in desulfurization. The iron oxide magnetic nanoparticle of the present invention is capable of effective deep desulfurization.

Low viscosity oligomer oil product, process and composition

The present invention relates to a low viscosity lubricant process, product, and composition characterized by low Noack volatility, low pour point, useful low temperature viscometrics, and high viscosity index and more particularly concerns a PAO composition having a kinetic viscosity at 100° C. in the range of about 4 cSt.

Synthetic lubricant basestocks and methods of preparation thereof

This disclosure relates to vinyl terminated macromer (VTM) based synthetic basestocks and their methods of preparation, lubricant compositions, methods of lubrication and products so lubricated. The VTM based synthetic basestocks useful for fuels and lubricants include oligomerization or polymerization products of one or more allylic vinyl terminated macromers (VTMs) having a molecular weight from 84 to 10080. The one or more allylic VTMs are oligomerized or polymerized in the presence of a catalyst under oligomerization or polymerization conditions sufficient to give the VTM based synthetic basestock. The catalyst can be a metallocene catalyst or an acid catalyst, e.g., Lewis acid. The one or more allylic vinyl terminated macromers (VTMs) can be one or more allylic vinyl terminated atactic polypropylene macromers (VTM aPP) having a molecular weight from 84 to 2250 and having a terminal allylic vinyl olefin content of at least 90%.

METHOD FOR KETONISATION OF BIOLOGICAL MATERIAL

A method for producing ketones includes a) providing a feedstock of biological origin having fatty acids and/or fatty acid derivatives having an average chain length of 24 C-atoms or less; b) subjecting the feedstock to a catalytic ketonisation reaction in the presence of aK2O/TiO2-catalyst; and c) obtaining from the ketonisation reaction a product stream having ketones, which ketones have a longer average hydrocarbon chain length than the average hydrocarbon chain length in the feedstock, wherein step b) is carried out directly on the feedstock and in the presence of the K2O/TiO2-catalyst as the sole catalyst applied in the ketonisation reaction. 1. A method for producing ketones , which method comprises:a) providing a feedstock of biological origin containing fatty acids and/or fatty acid derivatives having an average chain length of 24 C-atoms or less;{'sub': 2', '2, 'b) subjecting said feedstock to a catalytic ketonisation reaction in a presence of a KO/TiO-catalyst; and'}c) obtaining from said ketonisation reaction a product stream containing ketones, which ketones have a longer average hydrocarbon chain length than the average hydrocarbon chain length in said feedstock;{'sub': 2', '2, 'wherein the subjecting is carried out directly on said feedstock and in a presence of said KO/TiO-catalyst as a sole catalyst applied in said ketonisation reaction.'}2. The method according to claim 1 , wherein the subjecting is carried out directly on said feedstock without preceding or simultaneous hydrogenation of double bonds present in the fatty acids and/or fatty acid derivatives in said feedstock.3. The method according to claim 1 , comprising:performing said ketonisation reaction by introducing the feedstock in liquid phase.4. The method according to claim 1 , wherein said feedstock of biological origin contains unsaturated fatty acids and/or fatty acid derivatives claim 1 , or esters.5. The method according to claim 1 , comprising:performing said ketonisation reaction ...

PROCESS FOR PREPARING A BASE OIL HAVING A REDUCED CLOUD POINT

The present invention relates to a process for preparing a residual base oil from a hydrocarbon feed which is derived from a Fischer-Tropsch process, the process comprises the steps of: (a) providing a hydrocarbon feed which is derived from a Fischer-Tropsch process; (b) subjecting the hydrocarbon feed of step (a) to a hydrocracking/hydroisomerisation step to obtain an at least partially isomerised product; (c) separating at least part of the at least partially isomerised product as obtained in step (b) into one or more lower boiling fractions and a hydrowax residue fraction; (d) catalytic dewaxing of the hydrowax residue fraction of step (c) to obtain a highly isomerised product; (e) separating the highly isomerised product of step (d) into one or more light fractions and a isomerised residual fraction; (f) mixing of the isomerised residual fraction of step (e) with a diluent to obtain a diluted isomerised residual fraction; (g) cooling the diluted isomerised residual fraction of step (f) to a temperature between 0° C. and −60° C.; (i) subjecting the mixture of step (g) to a centrifuging step at a temperature between 0° C. and −60° C. to isolate the wax from the diluted isomerised residual fraction; (j) separating the diluent from the diluted isomerised residual fraction to obtain a residual base oil. 1. A process for preparing a residual base oil from a hydrocarbon feed which is derived from a Fischer-Tropsch process , the process comprising the steps of:(a) providing a hydrocarbon feed which is derived from a Fischer-Tropsch process;(b) subjecting the hydrocarbon feed of step (a) to a hydrocracking/hydroisomerisation step to obtain an at least partially isomerised product;(c) separating at least part of the at least partially isomerised product as obtained in step (b) into one or more lower boiling fractions and a hydrowax residue fraction;(d) catalytic dewaxing of the hydrowax residue fraction of step (c) to obtain a highly isomerised product;(e) separating the ...

RESIDUAL BASE OIL

The present invention relates to a Fischer-Tropsch derived residual base oil having a kinematic viscosity at 100° C. according to ASTM D445 in the range of from 15 to 35 mm/s, an average number of carbon atoms per molecule Fischer-Tropsch derived residual base oil according to C-NMR in a range of from 25 to 50. 1. A Fischer-Tropsch derived residual base oil having a kinematic viscosity at 100° C. in the range of from 15 to 35 mm/s according to ASTM D445 , an average number of carbon atoms per molecule Fischer-Tropsch derived residual base oil according to C-NMR in a range of from 25 to 50.2. The Fischer-Tropsch derived residual base oil according to claim 1 , having an average number of carbon atoms per molecule Fischer-Tropsch derived residual base oil according to C-NMR of from 30 to 45 carbon atoms.3. The Fischer-Tropsch derived residual base oil according to claim 1 , having an average number of carbon atoms per molecule Fischer-Tropsch derived residual base oil according to C-NMR of from 31 to 45 carbon atoms.4. The Fischer-Tropsch derived residual base oil according to claim 1 , having an average number of carbons in the non-branched segment according to C-NMR of less than 14 carbon atoms.5. The Fischer-Tropsch derived residual base oil according to claim 1 , having an average number of branches normalized for a molecule of 50 carbon atoms in according to 13 C-NMR of at least 3.5.6. The Fischer-Tropsch derived residual base oil according to claim 1 , having a T10 wt. % recovery point in the range of from 470 to 590° C. claim 1 , a T50 wt. % recovery point in the range of from 550 to 710° C. claim 1 , a T80 wt. % recovery point of at least 630° C. and a T90 wt. % recovery point of at least 700° C. as measured with ASTM D7169.7. The Fischer-Tropsch derived residual base oil according claim 1 , having a pour point of less than −10 as measured according to ASTM D97.8. The Fischer-Tropsch derived residual base oil according to claim 1 , having a cloud point of ...

LUBRICANT BASESTOCK PRODUCTION WITH ENHANCED AROMATIC SATURATION

Systems and methods are provided for producing lubricant basestocks having a reduced or minimized aromatics content. A first processing stage can perform an initial amount of hydrotreating and/or hydrocracking. A first separation stage can then be used to remove fuels boiling range (and lower boiling range) compounds. The remaining lubricant boiling range fraction can then be exposed under hydrocracking conditions to a USY catalyst including a supported noble metal, such as Pt and/or Pd. The USY catalyst can have a desirable combination of catalyst properties, such as a unit cell size of 24.30 or less (or 24.24 or less), a silica to alumina ratio of at least 50 (or at least 80), and an alpha value of 20 or less (or 10 or less). In some aspects, the effluent from the second (hydrocracking) stage can be dewaxed without further separation. In such aspects, a portion of the dewaxed effluent can be used as a recycle quench stream to cool the hydrocracking effluent prior to entering the dewaxing reactor. 113.-. (canceled)14. A system for producing a lubricant boiling range product , comprising:a hydrotreating reactor comprising a hydrotreating feed inlet, a hydrotreating effluent outlet, and at least one fixed catalyst bed comprising a hydrotreating catalyst;a separation stage having a first separation stage inlet and a second separation stage inlet, the first separation stage inlet being in fluid communication with the hydrotreating effluent outlet, the separation stage further comprising a plurality of separation stage liquid effluent outlets, one or more of the separation stage liquid effluent outlets corresponding to product outlets;a hydrocracking reactor comprising a hydrocracking feed inlet, a hydrocracking effluent outlet, and at least one fixed catalyst bed comprising a hydrocracking catalyst, the hydrocracking feed inlet being in fluid communication with at least one separation stage liquid effluent outlet, and the hydrocracking catalyst comprising USY zeolite ...

Production of High Quality Base Oils

A process for creating higher quality and lower quality base oils from used lubricating oils and crude oils, wherein the higher quality base oils may be either Group III or Group II and the lower quality base oils may be either Group II or Group I. Vacuum gas oils produced from used lubricating oils and from crude oils are processed via two or more process steps, including solvent extraction, solvent or catalytic or iso dewaxing, and hydrotreating. Such process enables efficient conversion and operation of refineries formerly capable only of making Group I base oils, even as their ability to make heavier base oils, waxes, and bright stocks is preserved, substantially to the same extent as such products had been made prior to undertaking the conversion. 1. A method for making base oil , the method comprising steps of:blending together (a) vacuum gas oil made from crude oil (“CO-VGO”) and (b) vacuum gas oil made from used lubricating oil (“UO-VGO”) to form a blended VGO (“Blended VGO”); andprocessing the Blended VGO by means of at least two of solvent extraction, dewaxing, and hydrotreating to make a base oil.2. A method for making base oil by solvent extraction , de-waxing , and hydrotreating , the method comprising steps of:processing vacuum gas oil made from crude oil (“CO-VGO”) during a first period of time by at least two of solvent extraction, dewaxing, and hydrotreating to make at least one first base oil; andprocessing vacuum gas oil made from used lubricating oil (“UO-VGO”) during a second period of time by at least two of solvent extraction, dewaxing, and hydrotreating to make at least one second base oil.3. The method of wherein the UO-VGO is processed by hydrotreating prior to processing by solvent extraction.4. The method of wherein the UO-VGO is processed by solvent extraction prior to processing by hydrotreating.5. The method of wherein at least a portion of the effluent produced after processing the UO-VGO by hydrotreating is then processed by solvent ...

Production of lubricant oils from thermally cracked resids

Methods are provided for processing deasphalted gas oils derived from thermally cracked resid fractions to form Group I, Group II, and/or Group III lubricant base oils. The yield of lubricant base oils (optionally also referred to as base stocks) can be increased by thermally cracking a resid fraction at an intermediate level of single pass severity relative to conventional methods. By performing thermal cracking to a partial level of conversion, compounds within a resid fraction that are beneficial for increasing both the viscosity and the viscosity index of a lubricant base oil can be retained, thus allowing for an improved yield of higher viscosity lubricant base oils from a thermally cracked resid fraction.

RAFFINATE HYDROCONVERSION FOR PRODUCTION OF HIGH PERFORMANCE BASE STOCKS

Systems and methods are provided for production of base stocks with a viscosity index of at least 120 and/or a sulfur content of 300 wppm or less and/or a kinematic viscosity at 100° C. of 3.0 cSt to 8.0 cSt by hydroconversion of a raffinate from aromatic extraction of a feed. The base stocks can further have a reduced content of 3+ ring naphthenes, such as 4.0 wt % or less, or 1.0 wt % or less. The base stocks can be produced by performing an elevated amount of feed conversion relative to 370° C. during hydroconversion of the raffinate, and optionally additional conversion during catalytic dewaxing of the hydroconverted raffinate. The base stocks can optionally be blended with additional base stocks and/or lubricant additives for production of lubricant compositions. 1. A method for making a base stock , comprising:performing solvent extraction on a feedstock to form a raffinate comprising a solvent dewaxed viscosity index (VI) of 80 to 105 at a pour point of −18° C.;hydroconverting at least a portion of the raffinate under hydroconversion conditions to form a hydroconverted effluent, the hydroconversion conditions being effective for conversion of at least 15 wt % of the at least a portion of the raffinate relative to a conversion temperature of 370° C., the hydroconverted effluent comprising a VI at least 20 greater than the solvent dewaxed VI of the raffinate, a 343° C.+ portion of the hydroconverted effluent comprising a sulfur content of 50 wppm or less;separating at least a portion of the hydroconverted effluent to form at least a lower boiling fraction and a lubricant boiling range fraction having a T10 distillation point of at least 343° C.;dewaxing at least a portion of the lubricant boiling range fraction under catalytic dewaxing conditions to form a dewaxed effluent; andfractionating at least a portion of the dewaxed effluent to form a base stock comprising a viscosity index of greater than 120, a sulfur content of less than 300 wppm, and a saturates ...

PROCESSES FOR PRODUCING PETROCHEMICAL PRODUCTS THAT UTILIZE FLUID CATALYTIC CRACKING OF LESSER AND GREATER BOILING POINT FRACTIONS WITH STEAM

According to one more embodiments, presently disclosed are processes for producing petrochemical products from a hydrocarbon material. The process may include separating the hydrocarbon material into at least a lesser boiling point fraction and a greater boiling point fraction, combining steam with the greater boiling point fraction upstream of the cracking of the greater boiling point fraction, cracking at least a portion of the greater boiling point fraction in the presence of a first catalyst to produce a first cracking reaction product, combining steam with the lesser boiling point fraction upstream of the cracking of the lesser boiling point fraction, cracking at least a portion of the lesser boiling point fraction in the presence of a second catalyst to produce a second cracking reaction product, and separating the petrochemical products from one or both of the first cracking reaction product or the second cracking reaction product. 1. A process for producing petrochemical products from a hydrocarbon material , the process comprising:separating the hydrocarbon material into at least a lesser boiling point fraction and a greater boiling point fraction;combining steam with the greater boiling point fraction upstream of a cracking of the greater boiling point fraction such that the steam:oil mass ratio is at least 0.5 such that the partial pressure of the greater boiling point fraction is reduced;cracking at least a portion of the greater boiling point fraction in the presence of a first catalyst at a reaction temperature of from 500° C. to 700° C. to produce a first cracking reaction product;combining steam with the lesser boiling point fraction upstream of a cracking of the lesser boiling point fraction such that the steam:oil mass ratio is from 0.2 to 0.8 such that the partial pressure of the lesser boiling point fraction is reduced;cracking at least a portion of the lesser boiling point fraction in the presence of a second catalyst at a reaction temperature ...

Catalytic system for preparation of high branched alkane from olefins

The present invention discloses a catalytic system for preparing highly branched alkane from olefin, which contains novel nickel or palladium complexes. In the presence of the catalytic system, highly branched oily alkane mixture can be efficiently obtained from olefins (such as ethylene) under mild conditions. The alkane mixture has a low bromine number, and can be used as a processing aid(s) and lubricant base oil with high-performance. Provides also was a method for preparing the catalyst and a method for preparing an oily olefin polymer.

METHOD OF TREATING DRILLING MUD WITH OIL-BASED DRILLING FLUID

A method of treating drilling mud with oil-based drilling fluid contains: a mud homogenization step configured to homogenize drilling mud which is solidized mud; a 3-phase cyclone separation step in which water vapors are used as a cleaning agent; a petroleum gas oxidation and combustion step in which the petroleum gas is extracted out of the 3-phase separator by using an oil gas oxidation device, and the petroleum gas is thermal oxidized and combusted; a liquid catalyst extraction step executed in which porous substances and hydrocarbon are extracted out of solid waste by using a microbubble extracting and liquid catalyst; a liquid catalyst recycling step having two-stage molecular distillation means so as to recycle the liquid catalyst to the liquid catalyst extraction step and to eliminate the liquid catalyst from recycled base oil. The mud homogenization step is alternatively executed based on physical condition of the drilling mud. 1. A method of treating drilling mud with oil-based drilling fluid comprising:a mud homogenization step alternatively configured to homogenize drilling mud which is solidized mud;a 3-phase cyclone separation step in which water vapors are used as a cleaning agent, wherein the drilling mud is flushed and is heated in a cyclone tank of a 3-phase separator so as to dissolve hydrocarbon and to evaporate waste water and petroleum gas, thus separating oil, water, solid waste, and the petroleum gas; wherein the mud homogenization step is executed based on physical condition of the drilling mud, when the drilling mud is liquid, the mud homogenization step is eliminated so that the drilling mud is directly delivered to the 3-phase cyclone separation step;a petroleum gas oxidation and combustion step in which the petroleum gas is extracted out of the 3-phase separator by using an oil gas oxidation device, and the petroleum gas is thermal oxidized and combusted;a liquid catalyst extraction step executed after the 3-phase cyclone separation step ...

OLIGOMERIZATION OF OLEFINS DERIVED FROM OXYGENATES

Systems and methods are provided for conversion of oxygenate feeds to lubricant and/or distillate boiling range compounds with desirable properties by first selectively converting oxygenates to light olefins and then converting the light olefins to distillate and lubricant boiling range compounds with beneficial properties. The distillate boiling range products can have an unexpectedly high cetane, while the lubricant boiling range products can have an unexpectedly high viscosity index. The ability to form the distillate boiling range products and lubricant boiling range products is facilitated by using a Ni-enhanced oligomerization catalyst. 1. A method for conversion of oxygenates , comprising:{'sub': 3', '6', '5', '6', '4, 'exposing a feed comprising one or more oxygenates to an oxygenate conversion catalyst under conditions for producing an olefin-containing effluent, the olefin-containing effluent comprising 60 wt % or more of C-Colefins and 10 wt % or less aromatics relative to a weight of hydrocarbons in the olefin-containing effluent, a ratio of C-Colefins versus Colefins in the olefin-containing effluent being 1.0 or more, the methanol conversion catalyst comprising a zeotype framework structure having a largest pore channel corresponding to a 10-member ring pore channel;'}separating a light olefin effluent from the olefin-containing effluent, the light olefin effluent comprising 70 wt % or more total olefins relative to a weight of hydrocarbons in the light olefin effluent; andexposing at least a portion of the light olefin effluent to an oligomerization catalyst comprising Ni supported on a support comprising a zeotype framework structure having 1-D 10-member ring pore channels under oligomerization conditions to form an oligomerized effluent, the at least a portion of the light olefin effluent comprising 5.0 wt % or more ethylene relative to a weight of olefins in the at least a portion of the light olefin effluent,wherein the oligomerization conditions ...

Production of lubricant base oils from biomass

Systems and methods are provided for processing a feed derived from a biomass source that contains nitrogen in the form of fatty amides, e.g., derived from hydrothermal processing of a biomass source feed, while reducing/minimizing the amount of heteroatom removal performed during subsequent/concurrent hydroprocessing. Optionally, the feed can also contain free fatty acids. This is accomplished in part by first exposing the feed to a catalyst comprising a rare earth oxide, alkali oxide, and/or alkaline earth oxide, which can remove the nitrogen heteroatoms from the compounds within the feed or can convert the nitrogen to a form readily removed in subsequent hydroprocessing. The catalyst may also suitable for catalyzing coupling (such as condensation) or conversion reactions of amides, carboxylic acids, carboxylic acid derivatives, and/or other molecules in the feed suitable for participating in the coupling reaction.

DEWAXING USING A MOLECULAR SIEVE CATALYST

Methods are provided for using a molecular sieve catalyst for dewaxing formed using a synthesis mixture comprising a morphology modifier. The catalyst may be used, for example, for production of a lubricant base stock. For example, ZSM-48 crystals formed using the morphology modifier (and/or formulated catalysts made using such crystals) can have an increased activity and/or can provide an improved yield during catalytic dewaxing of lubricant base stocks. 2. The method of claim 1 , wherein in step a) a composition comprising a source of hydroxide ions claim 1 , a structure directing agent Q claim 1 , a source of a trivalent element Y claim 1 , a source of a pentavalent element Z claim 1 , a source of halide ions W claim 1 , a source of alkali metal ions M claim 1 , or a source of alkali earth metal cations M or any combination thereof is combined into the synthesis mixture.3. The method of claim 1 , wherein the catalyst has an alpha value of at least 125.4. The method of claim 1 , wherein the catalyst has been calcined.5. The method of claim 1 , wherein the catalyst further comprises a hydrogenation metal comprising Pt claim 1 , Pd claim 1 , Ni claim 1 , W claim 1 , Co claim 1 , Mo claim 1 , or a combination thereof claim 1 , the amount of hydrogenation metal being 0.1 wt % to 20 wt %.6. The method of claim 1 , wherein the catalyst further comprises a binder claim 1 , a surface area of the binder in the bound catalyst being 150 m/g or less.7. The method of claim 1 , wherein the effective dewaxing conditions comprise a temperature of from 200 to 450° C. claim 1 , a hydrogen partial pressure of from 1.8 MPag to 34.6 MPag (250 psig to 5000 psig) claim 1 , and a hydrogen treat gas rate of from 35.6 m/m(200 SCF/B) to 1781 m/m(10 claim 1 ,000 scf/B).8. The method of claim 1 , wherein the structure directing agent Q comprises diquat-5 claim 1 , diquat-6 claim 1 , or a combination thereof.9. The method of claim 1 , wherein the molar ratio L:X in the synthesis mixture is in ...

MANUFACTURING HYDROCARBONS

A system and methods for manufacturing a base oil stock from a light hydrocarbon stream are provided. An example method includes cracking a light hydrocarbon stream to form an impure olefinic stream, separating water from the impure olefinic stream, and oligomerizing the impure olefinic stream to form a raw oligomer stream. A light olefinic stream from the raw oligomer stream and linear alpha olefins are recovered from the light olefinic stream. A heavy olefinic stream is distilled from the raw oligomer stream and hydro-processed to form a hydro-processed stream. They hydro-processed stream is distilled to form the base oil stock. 1. A system for manufacturing a base oil stock from a light hydrocarbon stream , comprising:a cracker configured to form a raw hydrocarbon stream from the light hydrocarbon stream;a separator configured to separate a raw olefinic stream from the raw hydrocarbon stream;an oligomerization reactor configured to increase a number of carbon atoms in molecules of the raw olefinic stream forming a raw oligomer stream; a light olefinic stream, wherein the light olefinic stream is provided to another separator for the isolation of light linear alpha-olefins;', 'an intermediate olefinic stream; and', 'a heavy olefinic stream;, 'a distillation column configured to separate the raw oligomer stream intoa hydro-processing reactor configured to hydro-process the heavy olefinic stream to form a hydro-processed stream; anda product distillation column configured to separate the hydro-processed stream to form the base oil stock.2. The system of claim 1 , comprising a dimerization reactor configured to dimerize the intermediate olefinic stream and return a dimerized stream to the distillation column.3. The system of claim 1 , comprising an alkylation reactor configured to alkylate the intermediate olefinic stream and provide a raw alkylated stream to an alkylation distillation column.4. The system of claim 3 , wherein the alkylation distillation column is ...

MANUFACTURING HYDROCARBONS

Systems and a method for manufacturing a base stock from a hydrocarbon stream are provided. An example method includes cracking the hydrocarbon stream to form a raw hydrocarbon stream, separating an ethylene stream from the raw hydrocarbon stream and oligomerizing the ethylene stream to form a raw oligomer stream. A light olefinic stream is distilled from the raw oligomer stream and linear alpha olefins are recovered from the light olefinic stream. A heavy olefinic stream is distilled from the raw oligomer stream. The heavy olefinic stream is hydro-processed to form a hydro-processed stream. The hydro-processed stream is distilled to form the base stock. 1. A system for manufacturing a base stock from a hydrocarbon stream , comprising:a steam cracker configured to form a raw product stream from the hydrocarbon stream;a purification system configured to separate an ethylene stream from the raw product stream;an oligomerization reactor configured to oligomerize the ethylene stream to form a raw oligomer stream; a light olefinic stream for recovery of light linear alpha-olefins;', 'an intermediate olefinic stream; and', 'a heavy olefinic stream;, 'a distillation column configured to separate the raw oligomer stream intoa hydro-processing reactor configured to hydro-process the heavy olefinic stream to form a hydro-processed stream; anda product distillation column configured to separate the hydro-processed stream to form the base stock.2. The system of claim 1 , comprising a dimerization reactor configured to dimerize the intermediate olefinic stream and return a dimerized stream to the distillation column.3. The system of claim 1 , comprising an alkylation reactor configured to alkylate the intermediate olefinic stream and provide an alkylated stream to an alkylation distillation column.4. The system of claim 3 , wherein the alkylation distillation column is configured to separate an unreacted olefin stream from the alkylated stream and return the unreacted olefin ...

MANUFACTURING A BASE STOCK

Systems and a method for manufacturing a base stock from a light gas stream are provided. An example method includes oxidizing the light gas stream to form a raw ethylene stream. Water is removed from the raw ethylene stream, and carbon monoxide in the raw ethylene stream is oxidized. Carbon dioxide is separated from the raw ethylene stream, and the raw ethylene stream is oligomerized to form a raw oligomer stream. A light olefinic stream is distilled from the raw oligomer stream and a light alpha olefin is recovered from the light olefinic stream. A heavy olefinic stream is distilled from the raw oligomer stream. The heavy olefinic stream is hydro-processed to form a hydro-processed stream. the hydro-processed stream is distilled to form the base stock. 1. A system for manufacturing a base stock from a light gas stream , comprising:an oxidation reactor configured to form a raw ethylene stream from the light gas stream;a separation system configured to remove water from the raw ethylene stream;a catalytic reactor configured to oxidize carbon monoxide in the raw ethylene stream;a removal system configured to remove carbon dioxide from the raw ethylene stream;an oligomerization reactor configured to oligomerize the raw ethylene stream to form an oligomer stream; a light olefinic stream, wherein the distillation column is configured to recover a light alpha-olefin;', 'an intermediate olefinic stream; and', 'a heavy olefinic stream;, 'a distillation column configured to separate the oligomer stream intoa hydro-processing reactor configured to hydro-process the heavy olefinic stream to form a hydro-processed stream; anda product distillation column configured to separate the hydro-processed stream to form the base stock.2. The system of claim 1 , wherein the oxidation reactor is configured to perform an oxidative coupling of methane (OCM).3. The system of claim 1 , wherein the oxidation reactor is configured to perform an oxidative dehydration of ethane (ODE).4. The ...

MANUFACTURING HYDROCARBON FLUIDS

A system and methods for manufacturing a base stock from a light hydrocarbon stream. An exemplary method includes cracking the light hydrocarbon stream to form a raw product stream. Water is removed from the raw product stream to form an oligomerization feed stream. The oligomerization feed stream is oligomerized to form an intermediate stream. A heavy olefinic stream is distilled from the intermediate stream. The heavy olefinic stream is hydro-processed to form a hydro-processed stream. The hydro-processed stream is distilled to form the base stock. 1. A system for manufacturing a base stock from a light hydrocarbon stream , comprising:a cracker configured to form a raw product stream from the light hydrocarbon stream;a separator configured to remove water from the raw product stream forming an oligomerization feed stream;an oligomerization reactor configured to increase a molecular weight of the oligomerization feed stream forming a raw oligomer stream;a distillation column configured to separate a heavy olefinic stream from the raw oligomer stream;a hydro-processing reactor configured to hydro-process the heavy olefinic stream to form a hydro-processed stream; anda product distillation column configured to separate the hydro-processed stream to form the base stock.2. The system of claim 1 , wherein the light hydrocarbon stream comprises ethane claim 1 , butane claim 1 , propane claim 1 , or naphtha claim 1 , or any combinations thereof.3. The system of claim 1 , wherein the cracker comprises a steam cracking reactor.4. The system of claim 1 , wherein the separator comprises a quench fractionator.5. The system of claim 1 , comprising:a primary fractionator configured to remove tar and steam cracking gas oil (SCGO) from the raw product stream;a caustic tower configured to remove hydrogen sulfide from the raw product stream; anda dryer configured to remove the water from the raw product stream.6. The system of claim 1 , wherein the oligomerization reactor is ...

METHOD AND SYSTEM FOR RE-REFINING AND UPGRADING USED OIL

A method for re-refining used oils comprises contacting feedstock comprising purified used oil with extraction solvent to perform continuous liquid-liquid solvent extraction, to produce an extract stream comprising the extraction solvent and an extract dissolved in the extraction solvent. The feedstock and the extraction solvent are agitated by a variable speed agitator during the solvent extraction at a selected agitation speed. The extract is separated from the extraction solvent and subjected to a continuous flow liquid phase hydrogenation treatment to produce an oil product. A system for performing the method includes a purification unit for purifying the used oil; an extraction column for extracting the extract from the feedstock; and a continuous flow liquid phase hydrogenation unit. The extraction column comprises an agitator configured to agitate the feedstock and the extraction solvent flowing through the extraction column at a variable agitation speed. 1. A method comprising:contacting a feedstock comprising purified used oil with an extraction solvent to perform continuous liquid-liquid solvent extraction, to produce an extract stream comprising the extraction solvent and an extract dissolved in the extraction solvent, wherein the feedstock and the extraction solvent are agitated by a variable speed agitator during the solvent extraction at a selected agitation speed;separating the extract from the extraction solvent; andsubjecting the extract to a continuous flow liquid phase hydrogenation treatment to produce an oil product having a viscosity index of at least 80.2. The method of claim 1 , wherein the liquid phase hydrogenation treatment comprises:adding a diluent to the extract to increase solubility of hydrogen in the extract, thus forming a liquid mixture comprising the diluent and the extract;adding hydrogen to the liquid mixture to dissolve the hydrogen in the liquid mixture; andheating the liquid mixture with dissolved hydrogen in the presence of ...

Oil degradation prevention device

Provided is an oil deterioration prevention device with which the trapping effect with respect to oil deteriorated components can be improved and with which the oil passage resistance can be reduced, thereby suppressing a rise in pressure loss. This oil deterioration prevention device is equipped with a filter unit equipped with a filter material that filters oil; and a deterioration prevention unit equipped with a powdery deterioration suppressing agent that suppresses oil deterioration. The deterioration prevention unit contains a mesoporous inorganic material, and of the oil fed from an oil storage unit, the oil filtered by the filter unit is fed to parts which are to be lubricated, and the oil in which deterioration has been suppressed by the deterioration prevention unit is returned to the oil storage unit or is fed to the parts to be lubricated.

Base Oil Upgrading by Co-Feeding a Ketone or Beta-Keto-Ester Feedstock

This invention discloses a process for making high viscosity index lubricating base oils having a viscosity index of at least 110 by co-feeding a ketone or a beta-keto-ester feedstock with a lubricant oil feedstock directly to a hydrocracking unit to produce a hydrocracked stream. Then at least a portion of the hydrocracked stream is treated under hydroisomerization conditions to produce a high viscosity index lubricating base oil. The process may involve bypassing a hydrotreating or hydrofinishing step, which may result in improved efficiency and economics in producing high viscosity index lubricating base oils.

SEPARATION OF CONTAMINANTS FROM A LIQUID MIXTURE

The present invention provides method for separating contaminants from a liquid mixture comprising the steps of a) providing a feed of said liquid mixture to be purified, b) adding a separation aid to the liquid mixture to be purified, wherein said separation aid is capable of binding said contaminants and c) supplying a flow of compressed air into said feed after step b) has been performed to provide a feed comprising air. The method further comprises steps d) removing air from said feed comprising air to provide a deaerated feed; and e) supplying said deaerated feed to a separator, and f) separating a phase comprising contaminants and said separation aid from said liquid mixture in said separator, wherein the separation aid added in step b) is insoluble in said liquid mixture at the separation conditions in step f). The present invention further provides a system for separating contaminants from a liquid mixture. 1. A method for separating contaminants from a liquid mixture comprising the steps of:a) providing a feed of said liquid mixture,b) adding a separation aid to the liquid mixture, wherein said separation aid is capable of binding said contaminants;c) supplying a flow of compressed air into said feed of liquid mixture after step b) has been performed, in order to provide a feed of liquid mixture comprising air;d) removing air from said feed of liquid mixture comprising air, in order to provide a deaerated feed of liquid mixture;e) supplying said deaerated feed of liquid mixture to a separator, andf) separating a phase comprising contaminants and said separation aid from said liquid mixture in said separator, wherein the separation aid added in step b) is insoluble in said liquid mixture at separation conditions prevailing in step f).2. The method according to claim 1 , wherein said flow of compressed air is supplied in step c) to said feed of liquid mixture with a pressure so that the flow of air has a higher velocity than the feed of liquid mixture.3. The ...

Hydroconversion of renewable feedstocks

A hydroconversion process comprises contacting a feedstock comprising renewable materials under hydroprocessing conditions with a promoted catalyst selected from a self-supported catalyst, a supported catalyst and combinations thereof, wherein the reaction conditions can be tailored to directly convert the renewable feedstock to the desired product(s) including fatty alcohols, esters, normal paraffins, or combinations thereof. The catalyst comprising at least a Group VIB metal selected from molybdenum and tungsten, a Group VIII metal selected from cobalt and nickel to convert the feedstock into any of fatty alcohols, esters, and normal paraffins. In some embodiments, the process further comprising additional steps to generate various desirable products, including α-olefins (or PAO, by dehydrating the fatty alcohol products), lubricants and bright stocks (from the oligomerizing of the PAO), and Group 3 lubricants (from co-oligomerizing of the PAO with some short chain olefins).

Method of producing lubricating base oil from feedstock comprising diesel fraction, and lubricating base oil produced thereby

Disclosed is a method of producing a lubricating base oil, including providing a feedstock including a diesel fraction, subjecting the feedstock to catalytic dewaxing, and recovering a lubricating base oil from a product of the catalytic dewaxing. A lubricating base oil produced thereby and a lubricant product including the lubricating base oil are also provided.

LUBRICANT BASESTOCK PRODUCTION WITH ENHANCED AROMATIC SATURATION

Systems and methods are provided for producing lubricant basestocks using a process flow that includes a conversion catalyst that can provide a desired improvement in viscosity index at a reduced or minimized amount of feed conversion. An initial processing stage can be used to produce a lubricant boiling range fraction with a reduced or minimized heteroatom content. After a separation, at least a portion of the lubricant boiling range portion can be exposed to a conversion catalyst that has an effective pore size of at least 8.0 Angstroms, a total surface area of at least 200 m/g, and/or an Alpha value of 20 or less, where the conversion catalyst includes a supported Group 8-10 noble metal. The methods can allow for increased yields of high viscosity index lubricant boiling range products from a process flow for lubricant base stock and/or blend stock production. 1. A method for producing a lubricant boiling range product , comprising:{'sup': '2', 'converting a feedstock comprising a lubricant boiling range portion in the presence of a conversion catalyst under conversion conditions to form a converted effluent, the conversion catalyst comprising a surface area of at least 200 m/g, an Alpha value of 20 or less, and an effective pore size of at least 8.0 Angstroms, the conversion catalyst further comprising 0.01 wt % to 5.0 wt % of a Group 8-10 noble metal supported on the conversion catalyst;'}dewaxing at least a portion of the converted effluent under catalytic dewaxing conditions to form a dewaxed effluent; andfractionating at least a portion of the dewaxed effluent to form at least a lubricant boiling range product.2. The method of claim 1 , wherein the conversion catalyst comprises a surface area of at least 500 m/g claim 1 , or wherein the conversion catalyst comprises an Alpha value of 10 or less claim 1 , or wherein the conversion catalyst comprises an effective pore size of at least 12 Angstroms claim 1 , or a combination thereof.3. The method of claim 1 , ...

PROCESS FOR MANUFACTURING LUBRICATION BASE OILS

Methods and systems for manufacturing lubrication oils are disclosed. In one embodiment, a method for manufacturing a lubrication oil includes the steps of receiving into an adsorber unit an unconverted oil (UCO) feedstock comprising five and six ring polynuclear aromatic (PNA) compounds and contacting the UCO feedstock with an adsorbent to remove PNA compounds, thereby forming a treated UCO feedstock with a low concentration of five and six ring PNAs. 1. A process for manufacturing a lubrication oil , the process comprising contacting a UCO feedstock with a PNA adsorbent to remove PNA compounds with five and six aromatic rings , thereby providing a treated UCO feedstock with no more than 100 wppm of five and six aromatic rings.2. The process of claim 1 , wherein the PNA adsorbent is an activated carbon.3. The process of claim 2 , further comprising contacting the treated UCO feedstock with a dewaxing catalyst and a hydrofinishing catalyst.4. The process of claim 1 , further comprising contacting said UCO feedstock with a HPNA adsorbent to remove HPNA compounds having at least seven aromatic rings.5. The process of claim 4 , wherein said HPNA adsorbent is contacted with said UCO feedstock before said PNA adsorbent is contacted with said UCO feedstock.6. The process of claim 4 , wherein said HPNA adsorbent has a different composition than said PNA adsorbent.7. The process of claim 4 , wherein said HPNA adsorbent and said PNA adsorbent are activated carbons.8. The process of claim 1 , further comprising contacting a hydrocarbon feed stream with hydrocracking catalyst to provide a hydrocracked stream and fractionating the hydrocracked stream to provide a UCO stream and taking said UCO feedstock from said UCO stream.9. The process of claim 8 , further comprising fractionating said UCO stream to provide a heavy UCO stream comprising said UCO feedstock.10. The process of claim 8 , further comprising fractionating said UCO stream to provide a light UCO stream comprising ...

METHOD FOR PRODUCING OIL-BASED COMPONENTS

A method of producing oil-based components is disclosed which includes providing VGO and slack wax; combining the VGO as a major component and the slack wax as a minor component to provide a feedstock; subjecting the feedstock to hydrocracking to provide a first effluent; fractionating the first effluent to provide at least a bottom fraction and a middle distillate fraction; recovering the bottom fraction and the middle distillate fraction. A method for improving a viscosity index of base oil includes subjecting the bottom fraction to a dewaxing step to provide a second effluent; fractionating the second effluent to provide at least a middle distillate and base oil; and recovering the middle distillate and the base oil. 1. A method of producing oil-based components , comprising:providing VGO and slack wax;combining the VGO as a major component and the slack wax as a minor component to provide a feedstock;subjecting the feedstock to hydrocracking to provide a first effluent;fractionating the first effluent to provide at least a bottom fraction and a middle distillate fraction; andrecovering the bottom fraction and the middle distillate fraction.2. The method of claim 1 , comprising:subjecting the bottom fraction to dewaxing to provide a second effluent;fractionating the second effluent to provide at least a middle distillate and base oil; andrecovering the middle distillate and the base oil.3. A method for improving a viscosity index of base oil claim 1 , comprising:providing VGO and slack wax;combining the VGO as a major component and the slack wax as a minor component to provide a feedstock;subjecting the feedstock to a hydrocracking step to provide a first effluent;fractionating the first effluent to provide at least a bottom fraction and a middle distillate fraction;subjecting the bottom fraction to dewaxing to provide a second effluent;fractionating the second effluent to provide at least a middle distillate and base oil; andrecovering the middle distillate and ...

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. 19.-. (canceled)10. A supported catalyst comprising:a support comprising at least one of a zeolitic support and a mesoporous support, the support having an Alpha value of at least 100; and0.1 wt % to 5.0 wt %, based on a weight of the supported catalyst, of a combined amount of platinum and Group VIII metal on the support, a weight ratio of platinum and Group VIII metal being from 0.1 to 10, the Group VIII metal comprising Pd, Ni, Rh, Ir, Ru, Co, or a combination thereof,wherein the supported catalyst has a catalyst width and an average platinum content per volume, and wherein a peak platinum content per volume across the catalyst width differs from the average platinum content per volume by less than 100% of the average platinum content per volume.11. The supported catalyst of claim 10 , wherein the supported catalyst has an average combined platinum and Group VIII metal content per volume claim 10 , and wherein a peak combined platinum and Group VIII metal content per volume across the catalyst width differs from the average combined platinum and Group VIII metal content per volume by less than 100% of the average combined platinum and Group VIII metal content per volume.12. The supported catalyst of claim 10 , ...

PRODUCTION OF RENEWABLE BASE OIL AND DIESEL BY PRE-FRACTIONATION OF FATTY ACIDS

Methods are disclosed for producing renewable base oil and a diesel oil from low-value biological oils. Low-value biological oils containing free fatty acids and fatty acid esters can be processed into a renewable base oil and a renewable diesel oil by first separating at least part of the saturated free fatty acids from the feedstock and then processing separately this saturated free acid feed in a ketonisation reaction followed by hydrodeoxygenation and hydroisomerisation reactions to yield a renewable base oil stream. The remaining free fatty acid depleted feed may be processed in a separate hydrodeoxygenation and hydroisomerisation step to yield a renewable diesel stream. 1. A method for producing a renewable base oil from a feedstock of biological origin , the method comprising:a) providing a feedstock, the feedstock containing at least 5 wt % of a mixture of saturated free fatty acids and at most a remainder of one or more compounds selected from the list consisting of: unsaturated free fatty acids, fatty acid esters, fatty amides, fatty alcohols, as well as fatty acid glycerols such as mono-glycerides, di-glycerides and tri-glycerides of fatty acids; {'sub': 'n', 'a saturated fatty acid feed containing at least 90 wt % saturated Cfree fatty acids, no more than 3 wt % unsaturated free fatty acids, where n is selected from one of the integer values; 10, 11, 12, 13, 14, 15, 16, 17, 18, 19, 20, 21, 22, 23, 24; and one or more saturated fatty acid depleted feed(s);'}, 'b) separating the feedstock into at leastc) subjecting the saturated fatty acid feed to ketonisation reaction conditions where two fatty acids react to yield a ketone stream, the ketone stream including as a major part saturated ketones having a carbon number of 2n−1; andd) subjecting the ketone stream to both hydrodeoxygenation reaction conditions and to hydroisomerisation reaction conditions, simultaneously or in sequence, to yield a deoxygenated and isomerised base oil stream containing the ...

Properties of Hydroprocessed Base Oils

Solvent extraction is applied to a hydrotreated base oil to create at least one higher quality product stream and at least one lower quality product stream, wherein the at least one higher quality product stream includes an improvement over the hydrotreated base oil in at least one of viscosity index, low temperature properties, volatility, and oxidation stability relative to that of the feedstock. 1. A method comprising the step of applying to a hydrotreated base oil a solvent treatment comprising at least one solvent to produce at least one first base oil , and one or more additional base oils , wherein the at least one first base oil has a higher paraffinic content than occurred in the hydrotreated base oil.2. The method of wherein the hydrotreated base oil feedstock is derived from one of a crude oil feedstock and a used lubricating oil feedstock.3. The method of wherein the hydrotreated base oil has been hydrotreated under a pressure of at least 600 psig.4. The method of claim 1 , further comprising a step of utilizing in the solvent treatment at least one of a preferentially selective paraffinic solvent claim 1 , and at least one of a preferentially selective solvent for at least one of aromatic claim 1 , polar claim 1 , and naphthenic constituents.5. A method for controlling at least one of volatility and viscosity of a base oil product by applying to a hydrotreated base oil feedstock a solvent treatment in which a first base oil is created that has a VI that is greater than that of the hydrotreated base oil feedstock and a further fractionation step comprising no less than two of:a. removal of solvent from the raffinate from which the first base oil was made,b. volatility of the first base oil that is at least one of (1) less than or equal to 15% or (2) less than or equal to 13%, in each case as measured by ASTM D-5800, andc. viscosity of the first base oil that is less than that of the hydrotreated base oil feedstock.6. The method of wherein the ...

Modified Composite Molecular Sieve and Preparation Method Thereof, and Paraffin Isomerization Catalyst

The present invention provides a modified composite molecular sieve, and a preparation method and an application of the modified composite molecular sieve. The modified composite molecular sieve comprises SiO 2 and a composite molecular sieve that comprises molecular sieve MCM-22 and zeolite A selected from at least one of ZSM-22, ZSM-23 and ZSM-48, wherein, the molecular sieve MCM-22 covers around the zeolite A. The present invention further provides a catalyst and an application of the catalyst. The catalyst comprises a carrier and a noble metal loaded on the carrier, wherein, the carrier comprises a modified composite molecular sieve that is the modified composite molecular sieve provided in the present invention or the modified composite molecular sieve obtained with the method provided in the present invention. The catalyst that utilizes the composite molecular sieve as a carrier not only can decrease the solidifying point of waxy raw oil, but also can improve the yield of liquid product, is especially applicable to the isomerization dewaxing process of lube distillate, and has an advantage of remarkably improving the viscosity index of lube base oil.

SYSTEM FOR CONVERSION OF CRUDE OIL TO PETROCHEMICALS AND FUEL PRODUCTS INTEGRATING DELAYED COKING OF VACUUM RESIDUE

Process scheme configurations are disclosed that enable conversion of crude oil feeds with several processing units in an integrated manner into petrochemicals. The designs utilize minimum capital expenditures to prepare suitable feedstocks for the steam cracker complex. The integrated process for converting crude oil to petrochemical products including olefins and aromatics, and fuel products, includes mixed feed steam cracking and gas oil steam cracking. Feeds to the mixed feed steam cracker include light products and naphtha from hydroprocessing zones within the battery limits, recycle streams from the C3 and C4 olefins recovery steps, and raffinate from a pyrolysis gasoline aromatics extraction zone within the battery limits. Feeds to the gas oil steam cracker include gas oil range intermediates from the vacuum gas oil hydroprocessing zone. Furthermore, vacuum residue is processed in a delayed coker unit to produce coker naphtha, which is hydrotreated and passed as additional feed to aromatics extraction zone and/or the mixed feed steam cracker, and coker gas oil range intermediates as additional feed to the gas oil hydroprocessing zone. 119.-. (canceled)20. An integrated system for producing petrochemicals and fuel products comprising:an atmospheric distillation unit (ADU) operable to receive and separate a feed, and discharge a first ADU fraction comprising naphtha, a second ADU fraction comprising at least a portion of middle distillates from the feed, and a third ADU fraction comprising atmospheric residue;a vacuum distillation unit (VDU) operable to receive and separate the third ADU fraction, and discharge a first VDU fraction comprising vacuum gas oil and a second VDU fraction comprising vacuum residue;a delayed coking zone operable to receive and convert the second VDU fraction comprising vacuum residue into a coker naphtha stream, a coker gas oil stream and petroleum coke;a distillate hydroproces sing (DHP) zone operable to receive and convert middle ...

RAFFINATE HYDROCONVERSION FOR PRODUCTION OF HIGH PERFORMANCE BASE STOCKS

Systems and methods are provided for production of base stocks with a viscosity index of at least 120 and/or a sulfur content of 300 wppm or less and/or a kinematic viscosity at 100° C. of 3.0 cSt to 8.0 cSt by hydroconversion of a raffinate from aromatic extraction of a feed. The base stocks can further have a reduced content of 3+ ring naphthenes, such as 4.0 wt % or less, or 1.0 wt % or less. The base stocks can be produced by performing an elevated amount of feed conversion relative to 370° C. during hydroconversion of the raffinate, and optionally additional conversion during catalytic dewaxing of the hydroconverted raffinate. The base stocks can optionally be blended with additional base stocks and/or lubricant additives for production of lubricant compositions. 116-. (canceled)17. A base stock comprising a viscosity index (VI) of at least 130 , a sulfur content of 50 wppm or less , a saturates content of at least 90 wt % , a Noack volatility of 14 wt % or less , a pour point of −15° C. or less , and a kinematic viscosity at 100° C. of 3.5 to 4.5 cSt , the base stock further comprising a 3+ ring naphthene content of 1.0 wt % or less.18. The base stock of claim 17 , wherein the 3+ ring aromatic content is 0.5 wt % or less.19. The base stock of claim 17 , wherein the base stock is derived from a feedstock that comprises at least 50 wt % of a mineral feedstock.20. The base stock of claim 17 , wherein the base stock comprises a Group III base stock.21. A lubricant composition comprising the base stock of and at least 5 wt % of a base stock having a kinematic viscosity at 100° C. of 4.5 cSt to 8.0 cSt.22. A base stock comprising a viscosity index (VI) of at least 135 claim 17 , a sulfur content of 50 wppm or less claim 17 , a saturates content of at least 90 wt % claim 17 , a Noack volatility of 14 wt % or less claim 17 , a pour point of −15° C. or less claim 17 , and a kinematic viscosity at 100° C. of 3.5 to 4.5 cSt claim 17 , the base stock further comprising a ...

SYSTEM FOR CONVERSION OF CRUDE OIL TO PETROCHEMICALS AND FUEL PRODUCTS INTEGRATING VACUUM RESIDUE CONDITIONING AND BASE OIL PRODUCTION

Process scheme configurations are disclosed that enable conversion of crude oil feeds with several processing units in an integrated manner into petrochemicals. The designs utilize minimum capital expenditures to prepare suitable feedstocks for the steam cracker complex. The integrated process for converting crude oil to petrochemical products including olefins and aromatics, and fuel products, includes mixed feed steam cracking and gas oil steam cracking. Feeds to the mixed feed steam cracker include one or more naphtha fractions from hydroprocessing zones within the battery limits, including vacuum residue hydrocracking, within the battery limits, recycle streams from the C3 and C4 olefins recovery steps, and raffinate from a pyrolysis gasoline aromatics extraction zone within the battery limits. Feed to the gas oil steam cracker in certain embodiments includes gas oil range intermediates from the vacuum residue hydrocracking zone. In addition, a base oil production center is integrated to provide base oils product used for production of synthetic lubes or corresponding lube oil feedstocks 129.-. (canceled)30. An integrated system for producing petrochemicals and fuel products comprising:an atmospheric distillation unit (ADU) operable to receive and separate a feed, and discharge a first ADU fraction comprising naphtha, a second ADU fraction comprising at least a portion of middle distillates from the feed, and a third ADU fraction comprising atmospheric residue;a vacuum distillation unit (VDU) operable to receive and separate the third ADU fraction, and discharge a first VDU fraction comprising vacuum gas oil and a second VDU fraction comprising vacuum residue;a distillate hydroprocessing (DHP) zone operable to receive and convert middle distillates from the second ADU fraction into a first DHP fraction and a second DHP fraction, wherein the first DHP fraction comprises naphtha and the second DHP fraction is used for diesel fuel production;a gas oil ...

HYDROCRACKING CATALYST AND PROCESS FOR PRODUCING LUBE BASE STOCKS

Hydrocracking catalysts and hydrocracking processes for the selective production of lube base stocks are disclosed. The hydrocracking catalyst contains a low acidity, highly dealuminated USY zeolite having a zeolite acid site density of from 1 to 100 micromole/g, a catalyst support, and one or more metals. The hydrocracking catalysts can maximize lube base stock yield while providing for effective impurity removal and VI enhancement at lower hydrocracking conversions. 1. A hydrocracking catalyst , comprising: (a) a USY zeolite component having a SiO/AlOmole ratio of at least 50 , an alpha value of not more than 5 , and a zeolite acid site density of from 1 to 100 micromole/g; (b) an amorphous cracking component; and (c) at least one hydrogenation metal component selected from the group consisting of a Group VIB metal , a Group VIII metal , and mixtures thereof.2. The catalyst of claim 1 , wherein the zeolite component has a SiO/AlOmole ratio of from 80 to 150.3. The catalyst of claim 1 , wherein the zeolite component has an alpha value of from 0.01 to 3.4. The catalyst of claim 1 , wherein the zeolite component has a zeolite acid site density of from 1 to 50 micromole/g.5. The catalyst of claim 1 , wherein the hydrocracking catalyst has a residual zeolite micropore volume of at least 50%.6. The catalyst of claim 1 , wherein the hydrocracking catalyst has a residual zeolite micropore volume of at least 80%.7. The catalyst of claim 1 , wherein the amorphous cracking component is a silica-alumina containing SiOin an amount of from 10 to 70 wt. % of the bulk dry weight of the carrier as determined by ICP elemental analysis and having a mean mesopore diameter of from 7 to 13 nm claim 1 , a BET surface area of from 450 to 550 m/g claim 1 , and a total pore volume of from 0.57 to 1.05 mL/g.8. The catalyst of claim 1 , wherein the hydrogenation metal component is selected from the group consisting of molybdenum claim 1 , tungsten claim 1 , nickel claim 1 , cobalt claim 1 , ...

HIGH VISCOSITY BASE STOCK COMPOSITIONS

Methods are provided for producing Group I base stocks having high viscosity and also having one or more properties indicative of a high quality base stock. The resulting Group I base stocks can have a viscosity at 100° C. and/or a viscosity at 40° C. that is greater than the corresponding viscosity for a conventional Group I bright stock formed by solvent processing. Additionally, the resulting Group I base stocks can have one or more properties that are indicative of a high quality base stock. 1. A base stock composition having a number average molecular weight (M) of 600 g/mol to 3000 g/mol , a weight average molecular weight (M) of 900 g/mol to 10000 g/mol , a polydispersity (M/M) of at least 1.4 , a pour point of 0° C. or less , a kinematic viscosity at 100° C. of at least 35 cSt , a kinematic viscosity at 40° C. of at least 600 cSt , and a viscosity index of at least 50.2. The composition of claim 1 , wherein the polydispersity is at least 1.7.3. The composition of claim 1 , wherein the composition has 23.5 wt % or less of epsilon carbons as determined by C-NMR.4. The composition of claim 1 , wherein the number average molecular weight (M) is at least 900 g/mol.5. The composition of claim 1 , wherein the weight average molecular weight (M) is at least 1500 g/mol.6. The composition of claim 1 , wherein the composition has a glass transition temperature of −40° C. or less; or wherein the composition has a crystallization temperature of −20° C. or less; or a combination thereof.7. The composition of claim 1 , wherein the composition has a sulfur content of 0.5 wt % or less.8. The composition of claim 1 , wherein the composition has a) a kinematic viscosity at 40° C. of at least 700 cSt; b) a kinematic viscosity at 100° C. of at least 40 cSt; or c) a combination thereof.9. The composition of claim 1 , wherein the viscosity index is at least 80.10. The composition of claim 1 , wherein the viscosity index is at least 100.11. The composition of claim 1 , wherein the ...

PROCESS FOR THE PRODUCTION OF BIODEGRADABLE HYDROCARBON FLUIDS BASED ON SYNGAS

The invention provides for a fluid having a boiling point in the range of from 100 to 400° C. and comprising more than 95% isoparaffins and containing less than 100 ppm aromatics by weight, obtainable by the process comprising the step of catalytically hydrogenating a feed comprising more than 95% by weight of a feedstock originating from syngas, at a temperature from 80 to 180° C. and at a pressure from 50 to 160 bars. The invention also provides for a fluid having a boiling point in the range of from 100 to 400° C. and a boiling range below 80° C., said fluid comprising more than 95% isoparaffins and less than 3% of naphthens by weight and having a ratio of isoparaffins to n-paraffins of at least 12:1, a biodegradability at 28 days of at least 60%, as measured according to the OECD 306 standard, a biocarbon content of at least 95% by weight, and containing less than 100 ppm aromatics by weight. The invention finally provides for uses of the fluid. 1. Fluid having a boiling point in the range of from 100 to 400° C. and comprising more than 95% isoparaffins and containing less than 100 ppm aromatics by weight , obtainable by the process comprising the step of catalytically hydrogenating a feed comprising more than 95% by weight of a feedstock originating from syngas , at a temperature from 80 to 180° C. , at a pressure from 50 to 160 bars , a liquid hourly space velocity of 0.2 to 5 hr-1 and an hydrogen treat rate up to 200 Nm3/ton of feed.2. Fluid of claim 1 , obtainable by the process wherein the hydrogenation conditions are the following.Pressure: 80 to 150 bars, and preferably 90 to 120 bars;Temperature: 120 to 160° C. and preferably 150 to 160° C.;Liquid hourly space velocity (LHSV): 0.4 to 3, and preferably 0.5 to 0.8;Hydrogen treat rate be up to 200 Nm3/ton of feed3. Fluid of claim 1 , wherein the feed comprises more than 98% claim 1 , preferably more than 99% of a feedstock originating from syngas.4. Fluid of claim 1 , wherein the feedstock is originating ...

USE OF RENEWABLE OIL IN HYDROTREATMENT PROCESS

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

PROCESS AND SYSTEM FOR CONVERSION OF CRUDE OIL TO PETROCHEMICALS AND FUEL PRODUCTS INTEGRATING DELAYED COKING OF VACUUM RESIDUE

Process scheme configurations are disclosed that enable conversion of crude oil feeds with several processing units in an integrated manner into petrochemicals. The designs utilize minimum capital expenditures to prepare suitable feedstocks for the steam cracker complex. The integrated process for converting crude oil to petrochemical products including olefins and aromatics, and fuel products, includes mixed feed steam cracking and gas oil steam cracking. Feeds to the mixed feed steam cracker include light products and naphtha from hydroprocessing zones within the battery limits, recycle streams from the C3 and C4 olefins recovery steps, and raffinate from a pyrolysis gasoline aromatics extraction zone within the battery limits. Feeds to the gas oil steam cracker include gas oil range intermediates from the vacuum gas oil hydroprocessing zone. Furthermore, vacuum residue is processed in a delayed coker unit to produce coker naphtha, which is hydrotreated and passed as additional feed to aromatics extraction zone and/or the mixed feed steam cracker, and coker gas oil range intermediates as additional feed to the gas oil hydroprocessing zone. 1. An integrated process for producing petrochemicals and fuel products from a crude oil feed comprising: a first ADU fraction comprising straight run naphtha,', 'a second ADU fraction comprising at least a portion of middle distillates from the crude oil feed, and', 'a third ADU fraction comprising atmospheric residue;, 'separating from the crude oil feed, in an atmospheric distillation unit (ADU), at least'} a first VDU fraction comprising vacuum gas oil, and', 'a second VDU fraction comprising vacuum residue;, 'separating from the third ADU fraction, in a vacuum distillation unit (VDU), at least'}coking at least a portion of the vacuum residue to a delayed coking zone and recovering a coker naphtha stream, a coker gas oil stream and petroleum coke;hydroprocessing in a distillate hydroprocessing (DHP) zone middle distillates ...

PROCESS AND SYSTEM FOR CONVERSION OF CRUDE OIL TO PETROCHEMICALS AND FUEL PRODUCTS INTEGRATING VACUUM RESIDUE CONDITIONING AND BASE OIL PRODUCTION

Process scheme configurations are disclosed that enable conversion of crude oil feeds with several processing units in an integrated manner into petrochemicals. The designs utilize minimum capital expenditures to prepare suitable feedstocks for the steam cracker complex. The integrated process for converting crude oil to petrochemical products including olefins and aromatics, and fuel products, includes mixed feed steam cracking and gas oil steam cracking. Feeds to the mixed feed steam cracker include one or more naphtha fractions from hydroprocessing zones within the battery limits, including vacuum residue hydrocracking, within the battery limits, recycle streams from the C3 and C4 olefins recovery steps, and raffinate from a pyrolysis gasoline aromatics extraction zone within the battery limits. Feed to the gas oil steam cracker in certain embodiments includes gas oil range intermediates from the vacuum residue hydrocracking zone. In addition, a base oil production center is integrated to provide base oils product used for production of synthetic lubes or corresponding lube oil feedstocks 1. An integrated process for producing petrochemicals and fuel products from a crude oil feed comprising: a first ADU fraction comprising straight run naphtha,', 'a second ADU fraction comprising at least a portion of middle distillates from the crude oil feed, and', 'a third ADU fraction comprising atmospheric residue;, 'separating from the crude oil feed, in an atmospheric distillation unit (ADU), at least'} 'a first VDU fraction comprising vacuum gas oil;', 'separating from the third ADU fraction, in a vacuum distillation unit (VDU), at least'}hydroprocessing a distillate hydroprocessing (DHP) zone middle distillates from the second ADU fraction, and recovering at least a first DHP fraction and a second DHP fraction, wherein the first DH-IP fraction comprises naphtha and the second DHP fraction is used for diesel fuel production;hydroprocessing in a gas oil hydroprocessing ( ...

High pressure hydrofinishing for lubricant base oil production

Systems and methods are provided for catalytic hydroprocessing to form lubricant base oils. The methods can include performing high pressure hydrofinishing after fractionating the hydrotreated and/or hydrocracked and/or dewaxed effluent. Performing hydrofinishing after fractionation can allow the high hydrogen pressure for hydrofinishing to be used on one or more lubricant base oil fractions that are desirable for high pressure hydrofinishing. This can allow for improved aromatic saturation of a lubricant base oil product while reducing or minimizing the hydrogen consumption. The high pressure hydrofinishing can be performed at a hydrogen partial pressure of at least about 2500 psig (˜17.2 Mpa), or at least about 2600 psig (˜18.0 Mpa), or at least about 3000 psig (˜20.6 MPa). The high pressure hydrofinishing can allow for formation of a lubricant base oil product with a reduced or minimized aromatics content, a reduced or minimized 3-ring aromatics content, or a combination thereof.

Base Oil Production via Dry Reforming

A system and method for converting (dry reforming) natural gas (methane) and carbon dioxide via reformer catalyst in a dry reformer into syngas including carbon monoxide and hydrogen, and discharging the syngas to a Fischer-Tropsch (FT) reactor. Supplemental hydrogen is generated via water electrolysis and added to the syngas in route to the FT reactor to increase the molar ratio of hydrogen to carbon monoxide in the syngas. The syngas may be converted via FT catalyst in the FT reactor into FT waxes. 1. A method of producing base oil , comprising:providing a feed to a dry reformer vessel, the feed comprising carbon dioxide and natural gas comprising methane;converting the methane and the carbon dioxide via reformer catalyst in the dry reformer vessel into syngas comprising carbon monoxide and hydrogen, wherein the converting comprises dry reforming and does not comprise autothermal reforming (ATR);discharging the syngas from the dry reformer vessel to a Fischer-Tropsch (FT) reactor vessel;subjecting water to electrolysis to generate supplemental hydrogen;adding the supplemental hydrogen to the syngas in route to the FT reactor vessel to increase a molar ratio of hydrogen to carbon monoxide in the syngas to at least 1.2; andconverting the syngas via FT catalyst in the FT reactor vessel into intermediate products comprising FT waxes.2. The method of claim 1 , wherein the reformer catalyst comprises magnesium oxide (MgO) nanoparticles promoted with nickel and molybdenum.3. The method of claim 1 , wherein an operating pressure of the dry reformer vessel is greater than an operating pressure of the FT reactor vessel to give a pressure differential adequate as a motive force for flow of the syngas from the dry reformer vessel to the FT reactor vessel.4. The method of claim 1 , wherein the FT waxes are at least 50% of the intermediate products by weight.5. The method of claim 4 , wherein the FT waxes each comprise at least nineteen carbons.6. The method of claim 1 , ...

CIRCULAR ECONOMY FOR PLASTIC WASTE TO POLYETHYLENE AND LUBRICATING OIL VIA CRUDE AND ISOMERIZATION DEWAXING UNITS

Provided is a continuous process for converting waste plastic into recycle for polyethylene polymerization. In one embodiment, the process comprises selecting waste plastics containing polyethylene and/or polypropylene and passing the waste plastics through a pyrolysis reactor to thermally crack at least a portion of the polyolefin waste and produce a pyrolyzed effluent. The pyrolyzed effluent is separated into offgas, a naphtha/diesel fraction, a heavy fraction, and char. The naphtha/diesel fraction is passed to a crude unit distillation column in a refinery where a straight run naphtha (C-C) fraction or a propane/butane (C-C) fraction is recovered. The straight run naphtha fraction (C-C) or the propane/butane (C-C) fraction is passed to a steam cracker for ethylene production. The heavy fraction from the pyrolysis unit can also be passed to an isomerization dewaxing unit to produce a base oil. 1. A continuous process for converting waste plastic into recycle for polyethylene polymerization comprising:(a) selecting waste plastics containing polyethylene and/or polypropylene;(b) passing the waste plastics from (a) through a pyrolysis reactor to thermally crack at least a portion of the polyolefin waste and produce a pyrolyzed effluent;(c) separating the pyrolyzed effluent into offgas, a naphtha/diesel fraction, a heavy fraction, and char;(d) passing the naphtha/diesel fraction to a crude unit in a refinery;{'sub': 5', '8, '(e) recovering a straight run naphtha (C-C) fraction from the crude unit;'}{'sub': 5', '8, '(f) passing the straight run naphtha fraction (C-C) to a steam cracker for ethylene production; and'}(g) passing the heavy fraction to an isomerization dewaxing unit to produce a base oil.2. The process of claim 1 , wherein the naphtha/diesel fraction of (c) is passed directly to a refinery crude unit and the contaminants are removed in a crude unit desalter.3. The process of claim 1 , wherein contaminants are removed at the pyrolysis site.4. The process of ...

CIRCULAR ECONOMY FOR PLASTIC WASTE TO POLYPROPYLENE AND LUBRICATING OIL VIA REFINERY FCC AND ISOMERIZATION DEWAXING UNITS

A continuous process for converting waste plastic into recycle for polypropylene polymerization is provided. The process integrates refinery operations to provide an effective and efficient recycle process. The process comprises selecting waste plastics containing polyethylene and polypropylene and then passing the waste plastics through a pyrolysis reactor to thermally crack at least a portion of the polyolefin waste and produce a pyrolyzed effluent. The pyrolyzed effluent is separated into offgas, a naphtha/diesel fraction, a heavy fraction, and char. The naphtha/diesel fraction is passed to a refinery FCC unit, from which is recovered a liquid petroleum gas Colefin/paraffin mixture. The Cparaffins and Colefins are separated into different fractions with a propane/propylene splitter. The Colefin fraction is passed to a propylene polymerization reactor. The Cparaffin fraction is optionally passed to a dehydrogenation unit to produce additional propylene and then the resulting Colefin is passed to a propylene polymerization reactor. The heavy fraction of pyrolyzed oil is passed to an isomerization dewaxing unit to produce a lubricating base oil. 1. A continuous process for converting waste plastic into recycle for polypropylene polymerization comprising:(a) selecting waste plastics containing polyethylene and/or polypropylene;(b) passing the waste plastics from (a) through a pyrolysis reactor to thermally crack at least a portion of the polyolefin waste and produce a pyrolyzed effluent;(c) separating the pyrolyzed effluent into offgas, a naphtha/diesel fraction, a heavy fraction, and char;(d) passing the naphtha/diesel fraction to a refinery FCC unit;{'sub': '3', '(e) recovering a liquid petroleum gas Colefin/paraffin mixture from the FCC unit;'}{'sub': 3', '3, '(f) separating the Cparaffin and Colefin into different fractions;'}{'sub': '3', '(g) passing the Colefin to a propylene polymerization reactor; and'}(h) passing the heavy fraction to an isomerization ...

Multi-Purpose Paraffin Additives for Deposit Control, Anti-Settling and Wax Softening in Oil-Based Fluids

An additive may be added to an oil-based fluid having at least one wax foulant therein. The additive may be or include an alpha olefin copolymer, an alkyl phenol-formaldehyde resin, an alkyl acrylate, a polyalkyl methacrylate, ethylene vinyl acetate co-polymer, ethylene vinyl acetate terpolymer, imidazoline, and combinations thereof. The additive may alter at least one property of the wax foulant as compared to an otherwise identical oil-based fluid absent the additive. The altered property may be or include the amount of wax foulant deposited, the amount of paraffinic wax dispersed, settling rate of the paraffinic wax foulant, viscosity of the paraffinic wax foulant, shape of the paraffinic wax foulant, such as but not limited to softening the wax foulant, and combinations thereof.

INTEGRATED PROCESSES AND APPARATUSES FOR UPGRADING A HYDROCARBON FEEDSTOCK

Methods and apparatuses are disclosed for upgrading a hydrocarbon feedstream comprising passing the hydrocarbon feedstream to a first hydroprocessing reactor in a reaction vessel to produce a first hydroprocessed effluent stream. The first hydroprocessed effluent stream is separated in a hot separator to produce a vapor stream and a liquid hydrocarbon stream. At least a portion of the liquid hydrocarbon stream is passed to a second hydroprocessing reactor disposed in the reaction vessel above the first hydroprocessing reactor, to produce a second hydroprocessed effluent stream. A liquid product stream is separated from the second hydroprocessing effluent stream. The vapor stream from the hot separator is mixed with the liquid product stream to provide a combined stream. 1. An integrated process for upgrading a hydrocarbon feedstream comprising:passing the hydrocarbon feedstream to a first hydroprocessing reactor in a reaction vessel, the first hydroprocessing reactor containing at least one bed of a first hydroprocessing catalyst, wherein the hydrocarbon feedstream is contacted with the first hydroprocessing catalyst under first hydroprocessing conditions in the presence of hydrogen to produce a first hydroprocessed effluent stream;separating the first hydroprocessed effluent stream in a hot separator to produce a vapor stream and a liquid hydrocarbon stream;passing at least a portion of the liquid hydrocarbon stream to a second hydroprocessing reactor disposed in the reaction vessel above the first hydroprocessing reactor, the second hydroprocessing reactor containing at least one bed of a second hydroprocessing catalyst, wherein the liquid hydrocarbon stream is contacted with the second hydroprocessing catalyst under second hydroprocessing conditions in the presence of hydrogen to produce a second hydroprocessed effluent stream;separating a liquid product stream from the second hydroprocessing effluent stream; andmixing the vapor stream from the hot separator with ...

METHOD FOR PRODUCING AN AMERICAN PETROLEUM INSTITUTE STANDARDS GROUP III BASE STOCK FROM VACUUM GAS OIL

A method for producing an American Petroleum Institute Standards Group III Base Stock from vacuum gas oil, by injecting hydrogen, heating, saturating the mixture through hydrogen reactors connected in series with a liquid hourly space velocity (LHSV)from 0.5 to 2.5, forming a saturated heated base oil, and coproduct. The method fractionates the saturated heated base oil while simultaneously refluxing a cooled light oil fraction forming an American Petroleum Institute Standards Group III Base Stock with less than 0.03% sulfur, with greater than 90% saturates and a viscosity index greater than 120 as defined by ASTM D-2270, a viscosity from 2 to 10 centistokes as defined by ASTM D-445 a boiling point range from 600 degrees F. to 1050 degrees F. as defined by ASTM D-86, and a cold crank viscosity (CCS) between 1200 and 5000 centipoise at minus 25 degrees C. and as defined by ASTM D-5293. 1. A method for producing an American Petroleum Institute Standards Group III base stock from vacuum gas oil derived from used oil , comprising:a. combining a petroleum derived product having a viscosity index greater than 120 into a vacuum gas oil derived from used oil forming a vacuum gas oil mixture with a combined boiling point range from 450 degrees F. to 1050 degree F. as defined by ASTM D-86;b. increasing temperature of the vacuum gas oil mixture to a temperature from 450 degrees Fahrenheit to 600 degrees Fahrenheit, forming a heated vacuum gas oil mixture while simultaneously increasing pressure on the heated vacuum gas oil mixture from 50 psig to a pressure from 1000 psig and 1500 psig by injection of hydrogen;{'sup': '−1', 'c. saturating the heated vacuum gas oil mixture forming a first partially saturated heated base oil then a fully saturated heated base with hydrogen through a plurality of hydrogen reactors connected in series, having a liquid hourly space velocity (LHSV)through the hydrogen reactors from 0.5 to 2.5;'}d. separating a saturated heated base oil from a ...

Use of renewable oil in hydrotreatment process

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

PROCESSES FOR PRODUCING A FUEL RANGE HYDROCARBON AND A LUBRICANT BASE OIL

Apparatuses and processes for producing at least one lubricant base oil and at least one hydrocarbon fuel range product. A deasphalted oil and a VGO stream and passed to a first hydroprocessing zone. After the first hydroprocessing zone, the hydrocarbon fuel range product may be recovered. After recovering the hydrocarbon fuel range product, the unconverted material may be separated into one or more lubricant base oil streams, and a recycle stream. The lubricant base oil streams may be upgraded, while the recycle stream may be hydroprocessed in a second hydroprocessing zone. The effluents can be combined to allow for efficient separation and recovery of the desired products. 1. A process for the production of a fuel range hydrocarbon and a lubricant base oil stock comprising:separating a residue stream in a first separation zone into a pitch stream and a deasphalted oil stream with a solvent;hydroprocessing the deasphalted oil stream in a first hydroprocessing zone;hydroprocessing a vacuum gas oil stream in the first hydroprocessing zone;separating an effluent stream from the first hydroprocessing zone in a second separation zone into a fuel range hydrocarbon stream and an unconverted oil stream;separating the unconverted oil stream in a third separation zone into one or more lubricant base oil streams and a recycle stream;hydroprocessing the recycle stream in a second hydroprocessing zone; and,separating an effluent stream from the second hydroprocessing zone in the second separation zone.2. The process of further comprising:upgrading at least a portion of the unconverted oil stream in a dewaxing zone.3. The process of wherein the dewaxing zone is disposed downstream of the third separation zone.4. The process of wherein the dewaxing zone is disposed upstream of the third separation zone.5. The process of further comprising:combining the deasphalted oil stream and the vacuum gas oil stream.6. The process of further comprising:combining the effluent stream from the ...

BASE OILS AND METHODS OF MAKING THE SAME

A process for the preparation of saturated hydrocarbon base oils is provided, comprising oligomerization of a feed mixture that has an average carbon number in the range of 14 to 18 to produce an oligomer product comprising dimers, trimers, and higher oligomers, where the dimer has a branching proximity (BP) of 20 or greater, isomerization of at least the dimer portion, and hydrogenation of the isomerized product. The dimer portion is separated from the oligomer product, and a saturated hydrocarbon base oil is obtained comprising greater than 90% dimers having an average carbon number in the range of from 29 to 36, and the dimer portion having a weight average molecular weight in the range of 422 to 510, where the dimers have an average Branching Index (BI) in a range of 22 to 26 and an average paraffin branching proximity (BP) in a range of from 18 to 26. 1. A process for the preparation of a saturated hydrocarbon base oil , comprising:forming an oligomerization reaction mixture comprising an oligomerization catalyst system and an olefin monomer feed mixture, wherein the olefin monomer feed mixture has an average carbon number in the range of 14 to 18;oligomerizing the olefin monomer feed mixture in the reaction mixture to produce an oligomer product comprising dimers, trimers, and higher oligomers;isomerizing at least the dimer portion of the oligomer product in the presence of an acid catalyst to form a mixture of branched hydrocarbons;{'sub': '2', 'hydrogenating the isomerized branched hydrocarbons, to a Bromine Index below 1000 mg Br/100 g as determined in accordance with ASTM D2710-09; and'}separating the dimer portion of the hydrogenated oligomer product, whereby a saturated hydrocarbon base oil is obtained comprising greater than 90 wt % dimers having an average carbon number in the range of from 29 to 36, the dimer portion having a weight average molecular weight in the range of from 422 to 510,{'sub': '2', 'wherein the dimers of the oligomer product, in a ...

PROCESS FOR THE PREPARATION OF A LUBRICANT BASE STOCK COMPRISING THE SELECTIVE THERMAL DECOMPOSITION OF PLASTIC POLYOLEFIN POLYMER

The present invention relates to a process for the preparation of a lubricant base stock from the thermal decomposition of plastic polymer. The present invention provides a process for preparing a lubricant base stock from the thermal decomposition of plastic polyolefin polymer, the method comprising the steps of: 152-. (canceled)53. A process for preparing a lubricant base stock from the thermal decomposition of plastic polyolefin polymer , the method comprising the steps of:i) introducing plastic polyolefin polymer into a thermal reaction zone of a vacuum pyrolysis reactor;{'sub': 20', '60, 'ii) heating the plastic polyolefin polymer at sub-atmospheric pressure, wherein the temperature in the thermal reaction zone of the reactor is from 500° C. to 750° C., to induce thermal decomposition of the plastic polyolefin polymer and to form a thermal decomposition product effluent which comprises a major portion by weight of a Cto Cwax fraction;'}iii) condensing a vapor component of the thermal decomposition product effluent from the vacuum pyrolysis reactor; and{'sub': 20', '60, 'iv) subjecting the Cto Cwax fraction of the thermal decomposition product to catalytic hydroisomerization in a hydroisomerization reactor in the presence of hydrogen to form the lubricant base stock,'}wherein the plastic polyolefin polymer comprises polyethylene and polypropylene in a polyethylene to polypropylene weight ratio of from 60:40 to 90:10.54. A process according to claim 53 , wherein the plastic polyolefin polymer is introduced into the pyrolysis reactor by means of an extruder.55. A process according to claim 53 , wherein at least one member of a group consisting of: the temperature in the thermal reaction zone of the reactor is from 525 to 650° C. claim 53 , and the pressure in the thermal reaction zone of the vacuum pyrolysis reactor is less than 75 kPa absolute.56. A process according to wherein at least one member of a group consisting of:the plastic polyolefin polymer comprises ...

BRIGHT STOCK AND HEAVY NEUTRAL PRODUCTION FROM RESID DEASPHALTING

Methods are provided for forming lubricant base stocks from feeds such as vacuum resid or other 510° C.+ feeds. A feed can be deasphalted and then catalytically and/or solvent processed to form lubricant base stocks, including bright stocks that are resistant to haze formation. 1. A method for making lubricant base stock , comprising:{'sub': 3', '4, 'performing solvent deasphalting using a Cor Csolvent under effective solvent deasphalting conditions on a feedstock having a T5 boiling point of at least 370° C., the effective solvent deasphalting conditions producing a yield of deasphalted oil of 40 wt % or less of the feedstock;'}hydroprocessing at least a portion of the deasphalted oil under first effective hydroprocessing conditions to form a hydroprocessed effluent having a sulfur content of 300 wppm or less and a nitrogen content of 100 wppm or less, the at least a portion of the deasphalted oil having an aromatics content of at least about 50 wt %;separating the hydroprocessed effluent to form at least a fuels boiling range fraction and a bottoms fraction; andhydroprocessing at least a portion of the hydroprocessed bottoms fraction under second effective hydroprocessing conditions, the second effective hydroprocessing conditions comprising catalytic dewaxing conditions, to form a catalytically dewaxed effluent,wherein the catalytically dewaxed effluent comprises a 950° F.+ (510° C.+) portion having a VI of at least 80, a pour point of −6° C. or less, and a cloud point of −2° C. or less.2. The method of claim 1 , wherein the catalytically dewaxed effluent comprises a saturates content of at least 90 wt %.3. The method of claim 1 , wherein the catalytically dewaxed effluent has a pour point of −10° C. or less; or a cloud point of −10° C. or less; or a combination thereof.4. The method of claim 1 , wherein the second effective hydroprocessing conditions further comprise hydrocracking conditions and/or aromatic saturation conditions.5. The method of claim 1 , ...

BRIGHT STOCK PRODUCTION FROM LOW SEVERITY RESID DEASPHALTING

Methods are provided for forming lubricant base stocks from feeds such as vacuum resid or other 510° C.+ feeds. A feed can be deasphalted and then catalytically and/or solvent processed to form lubricant base stocks, including bright stocks that are resistant to haze formation. 1. A method for making lubricant base stock , comprising:{'sub': 4', '5, 'performing solvent deasphalting using a Cor Csolvent under effective solvent deasphalting conditions on a feedstock having a T5 boiling point of at least 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 to form a hydroprocessed effluent having a sulfur content of 100 wppm or less and a nitrogen content of 100 wppm or less, the at least a portion of the deasphalted oil having an aromatics content of at least about 50 wt %;separating the hydroprocessed effluent to form at least a fuels boiling range fraction and a bottoms fraction; andhydroprocessing at least a portion of the hydroprocessed bottoms fraction under second effective hydroprocessing conditions, the second effective hydroprocessing conditions comprising catalytic dewaxing conditions, to form a catalytically dewaxed effluent; and at least one ofa) solvent extracting at least a portion of the catalytically dewaxed effluent to form a solvent processed effluent,b) solvent dewaxing at least a portion of the catalytically dewaxed effluent to form a solvent processed effluent, wherein the catalytically dewaxed effluent is underdewaxed,wherein the solvent processed effluent comprises a 950° F.+ (510° C.+) portion having a VI of at least 80, a pour point of −6° C. or less, and a cloud point of −2° C. or less.2. The method of claim 1 , wherein at least a portion of the catalytically dewaxed effluent is solvent extracted claim 1 , the solvent processed effluent comprising a 950° ...

BRIGHT STOCK PRODUCTION FROM LOW SEVERITY RESID DEASPHALTING

Methods are provided for forming lubricant base stocks from feeds such as vacuum resid or other 510° C.+ feeds. A feed can be deasphalted and then catalytically and/or solvent processed to form lubricant base stocks, including bright stocks. The catalytic processing can correspond to processing in at least two stages. The amount of conversion performed in each stage can be varied to produce bright stocks with various properties. 1. A method for making lubricant base stock , comprising:{'sub': '4+', 'performing solvent deasphalting using a C 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 a first wt % conversion relative to 370° C. to form a hydroprocessed effluent, the at least a portion of the deasphalted oil having an aromatics content of at least about 50 wt %;separating the hydroprocessed effluent to form at least a fuels boiling range fraction and a bottoms fraction; andhydroprocessing at least a portion of the hydroprocessed bottoms fraction under second effective hydroprocessing conditions comprising a second wt % conversion relative to 370° C. of 10 wt % to 70 wt %, the second effective hydroprocessing conditions comprising hydrocracking conditions and catalytic dewaxing conditions, to form a catalytically dewaxed effluent,wherein a combined conversion of the at least a portion of the deasphalted oil from the first effective hydroprocessing conditions and the second effective hydroprocessing conditions is at least 50 wt % relative to 370° C., the first wt % conversion relative to 370° C. comprising at least 30 wt % conversion, andwherein the catalytically dewaxed effluent comprises a 950° F.+ (510° C.+) portion having a VI of at least 80 and ...

INTEGRATED RESID DEASPHALTING AND GASIFICATION

Systems and methods are provided for integration of use deasphalted resid as a feed for fuels and/or lubricant base stock production with use of the corresponding deasphalter rock for gasification to generate hydrogen and/or fuel for the fuels and/or lubricant production process. The integration can include using hydrogen generated during gasification as a fuel to provide heat for solvent processing and/or using the hydrogen for hydroprocessing of deasphalted oil. 1. A method for hydroprocessing deasphalted oil , comprising:performing solvent deasphalting under effective solvent deasphalting conditions on a feedstock having a T5 boiling point of at least about 400° C. to form a first fraction comprising deasphalted oil and a solvent and a second fraction comprising deasphalter rock and the solvent, the effective solvent deasphalting conditions producing a yield of deasphalted oil of at least about 50 wt % of the feedstock;{'sub': '2', 'recovering solvent from at least one of the first fraction and the second fraction, the recovering comprising generating heat for the recovering by combustion of a solvent recovery fuel comprising H;'}gasifying at least a portion of the deasphalter rock to form synthesis gas, the solvent recovery fuel comprising at least a portion of the synthesis gas;desulfurizing at least a portion of the synthesis gas;{'sub': '2', 'separating at least a portion of the desulfurized synthesis gas to form an H-enriched stream; and'}{'sub': 2', '2', '2, 'hydroprocessing at least a portion of the deasphalted oil under first effective hydroprocessing conditions in the presence of an H-containing gas to form a hydroprocessed effluent comprising a sulfur content of 500 wppm or less, the H-containing gas comprising at least a portion of the H-enriched stream.'}2. The method of claim 1 , further comprising combusting at least a portion of the synthesis gas claim 1 , the H-enriched stream claim 1 , or a combination thereof in a combustion zone of a gas ...

SEQUENTIAL DEASPHALTING FOR BASE STOCK PRODUCTION

Methods are provided for producing lubricant base stocks from deasphalted oils formed by sequential deasphalting. The deasphalted oil can be exposed a first deasphalting process using a first solvent that can provide a lower severity of deasphalting and a second deasphalting process using a second solvent that can provide a higher severity of deasphalting. This can result in formation of at least a deasphalted oil and a resin fraction. The resin fraction can represent a fraction that traditionally would have been included as part of a deasphalter rock fraction. 1. A method for making lubricant base stock , comprising:{'sub': '5+', 'performing solvent deasphalting using a C solvent under first solvent deasphalting conditions on a feedstock having a T5 boiling point of at least about 400° C. to produce a first deasphalted oil and a first deasphalter residue, the effective solvent deasphalting conditions producing a yield of first deasphalted oil of at least 70 wt % of the feedstock{'sub': 3', '4, 'performing solvent deasphalting on at least a portion of the first deasphalted oil under second solvent deasphalting conditions using a Csolvent, a Csolvent, or a combination thereof to form a second deasphalted oil and a second deasphalter resin;'}hydroprocessing at least a portion of the second deasphalted oil under first effective hydroprocessing conditions to form a hydroprocessed effluent, the at least a portion of the second deasphalted oil having an aromatics content of at least about 50 wt %, the hydroprocessed effluent having a sulfur content of 300 wppm or less, and a nitrogen content of 100 wppm or less;separating the hydroprocessed effluent to form at least a fraction comprising a fuels boiling range fraction and a bottoms fraction; andhydroprocessing at least a portion of the hydroprocessed bottoms fraction under second effective hydroprocessing conditions, the second effective hydroprocessing conditions comprising catalytic dewaxing conditions, to form a ...

DEWAXING CATALYST WITH IMPROVED AROMATIC SATURATION ACTIVITY

Methods are provided for dewaxing distillate feeds using a dewaxing catalyst with improved aromatic saturation activity. The dewaxing can be performed using a catalyst including a zeolitic molecular sieve with a beneficial ratio of zeolitic molecular sieve to binder and/or using a catalyst including a zeolitic molecular sieve with a reduced ratio of silica to alumina. 1. A method of dewaxing a feed , comprising:exposing a feed comprising a lubricant boiling range portion, the feed having an aromatics content of at least 5 wt % and an organic sulfur content of at least 50 wppm, to a dewaxing catalyst under effective dewaxing conditions to form a dewaxed effluent, the dewaxing catalyst comprising a zeolitic molecular sieve, a mesoporous binder, and at least 0.1 wt % of a Group VIII metal, the dewaxing catalyst have a ratio of zeolitic molecular sieve to binder of at least 75:25.2. The method of claim 1 , wherein the zeolitic molecular sieve comprises a molecular sieve having a ZSM-48 framework claim 1 , a molecular sieve having a silica to alumina ratio of 70:1 or less claim 1 , or a combination thereof.3. The method of claim 1 , wherein the zeolitic molecular sieve comprises a molecular sieve having a largest pore channel size corresponding to a 10-member ring.4. The method of claim 1 , wherein the zeolitic molecular sieve has a silica to alumina ratio of 60:1 to 70:1.5. The method of claim 1 , wherein the zeolitic molecular sieve has a silica to alumina ratio of 50:1 to 60:1.6. The method of claim 1 , wherein the zeolitic molecular sieve has a silica to alumina ratio of 40:1 to 50:1.7. The method of claim 1 , wherein the zeolitic molecular sieve has a silica to alumina ratio of 30:1 to 40:1.8. The method of claim 1 , wherein the dewaxing catalyst has a ratio of zeolite to binder of 75:25 to 85:15.9. The method of claim 1 , wherein the dewaxing catalyst comprises 0.1 wt % to 2.0 wt % of a Group VIII noble metal.10. The method of claim 9 , wherein the Group VIII noble ...

Process for low-hydrogen-consumption conversion of renewable feedstocks to alkanes

A process relating to the manufacture of hydrocarbons, particularly paraffins/alkanes, from fatty acid feedstocks. More specifically, a process relating to the manufacture of paraffins/alkanes from fatty acid feedstocks comprising an olefinic bond saturation followed by a deoxygenation process carried out using decarboxylation achieving a maximum feedstock conversion to a paraffin product while consuming a minimum amount of hydrogen.

Process for the preparation of a lubricant base stock comprising the selective thermal decomposition of the plastic polyolefin polymer

The present invention relates to a process for the preparation of a lubricant base stock from the thermal decomposition of plastic polymer. The present invention provides a process for preparing a lubricant base stock from the thermal decomposition of plastic polyolefin polymer, the method comprising the steps of: i) introducing plastic polyolefin polymer into a thermal reaction zone of a vacuum pyrolysis reactor; ii) heating the plastic polyolefin polymer at sub-atmospheric pressure, wherein the temperature in the thermal reaction zone of the reactor is from 500° C. to 750° C., to induce thermal decomposition of the plastic polyolefin polymer and to form a thermal decomposition product effluent which comprises a major portion by weight of a C 20 to C 60 wax fraction; iii) condensing a vapour component of the thermal decomposition product effluent from the vacuum pyrolysis reactor in a multistage condensation comprising a plurality of condensation stages connected in series; and iv) subjecting the C 20 to C 60 wax fraction of the thermal decomposition product to catalytic hydroisomerization in a hydroisomerization reactor in the presence of hydrogen to form the lubricant base stock.

BLOCK PROCESSING 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. 1. A method for making lubricant base stock , comprising:performing solvent deasphalting, 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 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 viscosity at 100° C. than the first fraction;'}hydroprocessing at least a portion of the first fraction under second effective hydroprocessing conditions, the second effective hydroprocessing conditions comprising catalytic dewaxing conditions, to form a first ...

SOLVENT EXTRACTION FOR CORRECTION OF COLOR AND AROMATICS DISTRIBUTION OF HEAVY NEUTRAL BASE STOCKS

Systems and methods are provided for performing solvent extraction on heavy neutral base stocks. The aromatic extraction can reduce aromatics content while have a reduced or minimized impact on lubricant properties. This can allow, for example, for correction of color and/or haze for heavy neutral base stocks, such as heavy neutral base stocks formed from a deasphalted oil. 1. A method for making lubricant base stock , comprising:hydroprocessing a deasphalted oil comprising a 370° C.+ fraction under first effective hydroprocessing conditions to form a hydroprocessed effluent, 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 or a nitrogen content of 100 wppm or less, or a combination thereof;separating the hydroprocessed effluent to form at least a first fraction comprising a T5 distillation point of at least 370° C. and a kinematic viscosity at 100° C. of 6 cSt to 20 cSt;hydroprocessing at least a portion of the first fraction under second effective hydroprocessing conditions, the second effective hydroprocessing conditions comprising catalytic dewaxing conditions, to form a catalytically dewaxed effluent comprising a 370° C.+ portion; andsolvent extracting at least a portion of the 370° C.+ portion of the catalytically dewaxed effluent to form a solvent processed effluent.2. A method for making lubricant base stock , comprising:{'sub': '4+', 'performing solvent deasphalting, optionally using a C solvent, under effective solvent deasphalting conditions on a feedstock having a T5 boiling point of at least about 370° C. (or at least about 400° C., or at least about 450° C., or at least about 500° 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 to form a ...

Processes for Preparing Low Viscosity Lubricants

Disclosed are processes for forming an oligomer product by contacting a feedstock olefin containing trisubstituted olefins with a solid acid catalyst. The oligomer product can be formed at an oligomerization temperature in a range from −20° C. to 40° C. Polyalphaolefins produced from the oligomer product can have reduced viscosities at low temperatures. 1. A process comprising:(a) contacting a feedstock olefin with a solid acid catalyst to form an oligomer product at an oligomerization temperature in a range from −20° C. to 40° C., wherein the feedstock olefin comprises trisubstituted olefins;(b) removing at least a portion of the oligomer product from the feedstock olefin and the solid acid catalyst; and(c) hydrogenating the portion of the oligomer product to form a polyalphaolefin, wherein the polyalphaolefin has a kinematic viscosity at −40° C. in a range from 4,500 to 9,500 cSt.2. The process of claim 1 , wherein the solid acid catalyst comprises an acidic ion exchange resin.3. The process of claim 1 , wherein the solid acid catalyst comprises a functionalized styrene-divinylbenzene polymer claim 1 , a 4-vinylpyridine divinylbenzene polymer claim 1 , a tetrafluoroethylene polymer modified with perfluorovinyl ether groups terminated with sulfonate groups claim 1 , or a combination thereof.4. The process of claim 1 , wherein the solid acid catalyst comprises an AMBERLYST® resin claim 1 , a NAFION® resin claim 1 , or a combination thereof.5. The process of claim 1 , wherein the solid acid catalyst comprises AMBERLYST® 15 resin.6. The process of claim 1 , wherein:the oligomerization temperature is in a range from 15° C. to 35° C.; and{'sub': 16', '24, 'the feedstock olefin comprises at least 75 wt. % Cto Ctrisubstituted olefins.'}7. The process of claim 1 , wherein the feedstock olefin is produced by a process comprising isomerizing a vinylidene composition comprising a Cto Cvinylidene.8. The process of claim 1 , wherein the feedstock olefin is produced by a process ...

TiO2 CATALYST IN KETONISATION REACTIONS TO PRODUCE RBO

A method for producing a renewable base oil from a feedstock of biological origin includes providing a feedstock, the feedstock including: 2-95 wt % of a mixture of free fatty acids; 5-98 wt % fatty acid glycerols selected from mono-glycerides, di-glycerides and tri-glycerides of fatty acids; 0-50 wt % of one or more compounds selected from the list consisting of: fatty acid esters of the non-glycerol type, fatty amides and fatty alcohols; a major part of the feedstock being a mixture of free fatty acids and fatty acid glycerols; subjecting all or part of the feedstock to ketonisation reaction conditions where two free fatty acids react to yield a ketone stream, and subjecting the ketone stream to both hydrodeoxygenation and to hydroisomerisation reaction conditions, to yield a deoxygenated and isomerised base oil product stream containing the renewable base oil. 1. A for producing a renewable base oil from a feedstock of biological origin , the method comprising:a) providing a feedstock, the feedstock including 2-95 wt % of a mixture of free fatty acids; 5-98 wt % fatty acid glycerols selected from mono-glycerides, di-glycerides and tri-glycerides of fatty acids; 0-50 wt % of one or more compounds selected from a list consisting of: fatty acid esters of the non-glycerol type, fatty amides and fatty alcohols; wherein a major part of the feedstock is a mixture of free fatty acids and fatty acid glycerols;b) subjecting all or part of the feedstock to ketonisation reaction conditions in a presence of a ketonisation catalyst selected as a metal oxide catalyst essentially containing titanium as the metal, and where two free fatty acids react to yield a ketone stream, the ketone stream including as a major part saturated ketones; andc) subjecting the ketone stream to both hydrodeoxygenation reaction conditions and to hydroisomerisation reaction conditions, simultaneously or in sequence, to yield a deoxygenated and isomerised base oil product stream containing the ...

PROCESS FOR THE PRODUCTION OF RENEWABLE BASE OIL, DIESEL AND NAPHTHA

Hydrotreatment of biological oil is disclosed for producing renewable base oil and a diesel oil from low value biological oils. Low value biological oils containing free fatty acids and fatty acid esters can be processed into a renewable base oil and a renewable diesel oil in an efficient manner by first separating at least part of the free fatty acids from the feedstock and then processing separately this free acid feed in a ketonisation reaction followed by hydrodeoxygenation and hydroisomerisation reactions to yield a renewable base oil stream. The remaining free fatty acid depleted feed is processed in a separate hydrodeoxygenation and hydroisomerisation step to yield a renewable diesel stream. 1. Method for producing a renewable base oil and a diesel fuel from a feedstock of biological origin , the method comprising:a) providing a feedstock, the feedstock containing 2-95 wt % of a mixture of free fatty acids; 5-98 wt % fatty acid glycerols selected from mono-glycerides, di-glycerides and tri-glycerides of fatty acids; 0-50 wt % of one or more compounds selected from a list consisting of: fatty acid esters of the non-glycerol type, fatty amides, and fatty alcohols; wherein a major part of the feedstock is the mixture of free fatty acids and fatty acid glycerols; [{'sub': 10', '24, 'a free fatty acid feed having a higher concentration of free fatty acids than the feedstock, the free fatty acids containing C-Cfatty acids; and'}, 'one or more free fatty acid depleted feed(s) having higher concentration of the compounds selected from mono-glycerides, di-glycerides and tri-glycerides of fatty acids, and having a higher boiling point than the free fatty acid feed;, 'b) separating the feedstock into at leastc) subjecting the free fatty acid feed to ketonisation reaction conditions where two fatty acids react to yield a ketone stream, the ketone stream containing as a major part saturated ketones; andd) subjecting the ketone stream to both hydrodeoxygenation reaction ...

SOLVENT FOR USE IN AROMATIC EXTRACTION PROCESS

Oxidized disulfide oil (ODSO) compounds, derived from by-product disulfide oil (DSO) compounds produced as by-products from the generalized mercaptan oxidation (MEROX) in the practice of the process, are effective as aromatic extraction solvents. This use of ODSO compounds as an extraction solvent converts an otherwise DSO waste oil product into a valuable commodity that has utility in improving the extraction of aromatics from hydrocarbons derived from fossil fuels. 1. An aromatic extraction solvent that is an oxidized disulfide oil (ODSO) selected from the group consisting of (R—SOO—SO—R′) , (R—SOO—SOO—R′) , (R—SO—SOO—OH) , (R—SOO—SOO—OH) , (R—SO—SO—OH) , and (R—SOO—SO—OH) , and mixtures thereof , where R and R′ are alkyl groups comprising 1 to 10 carbon atoms.2. The aromatic extraction solvent of claim 1 , wherein the number of carbon atoms in the ODSO is in the range of from 1 to 20.3. The aromatic extraction solvent of claim 1 , wherein the solvent is water soluble.4. The aromatic extraction solvent of claim 1 , wherein the ODSO of the solvent has at least three oxygen atoms.5. The aromatic extraction solvent of claim 1 , wherein the density of the solvent is greater than 1.0 g/cc.6. The aromatic extraction solvent of claim 1 , wherein the density of the solvent is in the range of from 1.1 g/cc to 1.7 g/cc.7. The aromatic extraction solvent of claim 1 , wherein the solvent has an average boiling point greater than 80° C.8. The aromatic extraction solvent of claim 1 , wherein the solvent comprises water in the range of from 0.1 W %-50 W % of the solvent.9. The aromatic extraction solvent of claim 1 , wherein the solvent comprises water in the range of from 1.0 W %-30 W %10. The aromatic extraction solvent of claim 1 , wherein the solvent is a mixture of one or more other aromatic extraction solvents.11. The aromatic extraction solvent of claim 10 , wherein the one or more other solvents is selected from the group consisting of diethyleneglycol claim 10 , ...

LOW VISCOSITY POLY-A-OLEFIN LUBRICATING OIL AND SYNTHESIS METHOD THEREOF

The present invention provides a low viscosity poly-α-olefin lubricating oil and a synthesis method thereof. The method comprises: (1) the α-olefin raw material is subjected to dehydration treatment so that the water content in the raw material is ≤10 ppm; (2) a reaction of the dehydration treated α-olefin raw material is carried out in the presence of a complex catalyst and gaseous BFto obtain a reaction product, wherein the pressure of the gaseous BFis 0.01 to 1 MPa; (3) the reaction product obtained in step (2) is sequentially subjected to flash distillation, gas stripping, centrifugation, and washing treatment to obtain an intermediate product; (4) the intermediate product obtained in step (3) is subjected to distillation under reduced pressure to separate the unreacted α-olefin raw material and α-olefin dimers, and the remaining heavy fractions are subjected to hydrogenation saturation treatment followed by fractionation and cutting-off. 1. A synthesis method for low viscosity poly-α-olefin lubricating oils , comprising the following steps:(1) dehydration treatment: the α-olefin raw material is subjected to dehydration treatment so that the water content in the raw material is ≤10 ppm;{'sub': 3', '3, '(2) polymerization reaction: the reaction of the dehydration treated α-olefin raw material is carried out in the presence of a complex catalyst and gaseous BFto obtain a reaction product, wherein the pressure of the gaseous BFis 0.01 to 1 MPa;'} [{'sub': '3', 'a. flash distillation: the reaction product obtained in step (2) is subjected to flash distillation to obtain a first oil phase and gaseous BF;'}, {'sub': '3', 'b. gas stripping: the first oil phase obtained in step a is subjected to gas stripping to obtain a second oil phase and a stripping gas containing BF;'}, {'sub': 2', '3, 'c. centrifugation: the second oil phase obtained in step b is subjected to separation by centrifugation using a continuous liquid-liquid separation centrifuge to obtain a recycled ...

SELECTION OF BRIGHT STOCK PROCESSING CONDITIONS BASED ON SAMPLE CHARACTERIZATION

Systems and methods are provided for modifying or selecting processing conditions for bright stock formation based on compositional characterization of the feedstock and/or bright stock products. In some aspects, the compositional information can include Z-class characterization of the components of a feed and/or bright stock product, optionally in combination with carbon number and/or molecular weight for the components. The compositional information can be used to select processing conditions to allow for removal and/or modification of selected components within a bright stock in order to improve throughput and/or provide desirable cold flow properties. 1. A method for forming a bright stock , comprising:performing FTICR on a sample of a feedstock to determine amounts of one or more Z-classes within the feedstock, to determine amounts of one or more homologous series of compounds within the feedstock, or a combination thereof;characterizing waxy components within the sample of the feedstock based on the one or more determined Z-classes, the determined one or more homologous series of compounds, or the combination thereof;selecting at least one of a pour point, a feed rate, a dewaxing temperature, a solvent to oil ratio, and a dewaxing solvent based on the characterization of the waxy components; andperforming solvent dewaxing on at least a portion of the feedstock under solvent dewaxing conditions to form a dewaxed oil, the dewaxed oil comprising a bright stock portion having a kinematic viscosity at 100° C. of 20 cSt or more, the solvent dewaxing conditions comprising the at least one of the pour point, the feed rate, the dewaxing temperature, the solvent to oil ratio, and the dewaxing solvent.2. The method of claim 1 , further comprising selecting a filter cake size for the solvent dewaxing conditions.3. The method of claim 1 , wherein the waxy components are characterized based on a measured amount of compounds in the feedstock having a Z-class of 2 to −60 (or ...

GROUP III BASE STOCKS AND LUBRICANT COMPOSITIONS

Disclosed are Group III base stocks comprising greater than or equal to about 90 wt. % saturated hydrocarbons (saturates); a viscosity index from 120 to 145; a unique ratio of molecules with multi-ring naphthenes to single ring naphthenes (2R+N/1RN); a unique ratio of branched carbons to straight chain carbons (BC/SC); a unique ratio of branched carbons to terminal carbons (BC/TC); and unique MRV behavior as a function of base stock naphthene ratio (2R+N/1RN). A method for preparing the base stocks is also disclosed. Also disclosed is a lubricating oil having the base stock as a major component, and an additive as a minor component. 1. A Group III base stock comprising;at least 90 wt. % saturated hydrocarbons:kinematic viscosity at 100° C. of 4.0 cSt to 5.0 cSt;a viscosity index of 120 to 140;a ratio of multi-ring naphthenes to single ring naphthenes (2R+N/1RN) of less than 0.52; anda ratio of branched carbons to straight chain carbons (BC/SC) less than or equal to 0.21.2. The base stock of having a ratio of branched chain carbons to terminal carbons (BC/TC) less than or equal to 2.3.3. The base stock of claim 1 , wherein the kinematic viscosity at 100° C. of from 4.0 cSt up to 4.7 cSt.4. A Group III base stock comprising:at least 90 wt. % saturated hydrocarbons;kinematic viscosity at 100° C. of 5.0 cSt to 12.0 cSt;a viscosity index of 120 to 140;a ratio of multi-ring naphthenes to single ring naphthenes (2R+N/1RN) of less than 0.59; anda ratio of branched carbons to straight chain carbons (BC/SC) less than or equal to 0.216.5. The base stock of claim 4 , wherein the base stock has a ratio of branched chain carbons to terminal carbons (BC/TC) less than or equal to 2.3.6. The base stock of claim 4 , wherein the Kvioo is from 5.5 cSt to 7.0 cSt.7. The base stock of claim 5 , wherein the Kvioo is from 5.5 cSt to 7.0 cSt.8. A method for producing a diesel fuel and an API Group III base stock claim 5 , comprising:providing a feed stock comprising a vacuum gas oil feed; ...

GROUP III BASE STOCKS AND LUBRICANT COMPOSITIONS

Disclosed are Group III base stocks comprising at least 30 wt % naphthenes, a viscosity index from 120 to 145; and a unique ratio of molecules with multi-ring naphthenes to single ring naphthenes (2R+N/1RN). A method for preparing the base stocks is also disclosed. Also disclosed is a lubricating oil having the base stock as a major component, and an additive as a minor component. 1. A Group III base stock comprising:at least about 30 wt % of naphthenes;wherein the Group III base stock has a viscosity index of from 120 up to 133; andwherein the Group III base stock has a ratio of molecules with multi-ring naphthenes to single ring naphthenes, 2R+N/1RN, of less than about 0.46.2. The base stock of claim 1 , wherein the base stock has an amount of saturated hydrocarbons of at least 95 wt. %.3. The base stock of claim 1 , wherein the base stock has a KV100 of from 2 cSt to 14 cSt.4. The base stock of claim 1 , wherein the base stock has a KV100 of 4.0 cSt to 5.0 cSt.5. The base stock of claim 1 , wherein the base stock has a KV100 of 5.0 cSt to 12.0 cSt.6. The base stock of claim 1 , wherein the base stock has a KV100 of 5.5 cSt to 11.0 cSt.7. The base stock of claim 4 , wherein the viscosity index is 120-133 and is less than or equal to 142*(1−0.0025 exp(8*(2R+N/1RN))).8. The base stock of claim 5 , wherein the viscosity index is 120to133 and is less than or equal to 150.07*(1−0.0106*exp(4.5*(2R+N/1RN))).9. A lubricating composition comprising the base stock of and an additive.10. The lubricating composition of claim 9 , wherein the base stock has a viscosity index of 120 to 133 that is less than or equal to 142*(1−0.0025 exp(8*(2R+N/1RN))).11. The lubricating composition of claim 9 , wherein the base stock has a viscosity index of 120 to 133 that is less than or equal to 150.07*(1−0.0106*exp(4.5*(2R+N/1RN))).12. A method for producing a diesel fuel and a base stock claim 9 , comprising:providing a feed stock comprising a vacuum gas oil;hydrotreating the feed stock ...

Integrated hydrocracking and dewaxing of hydrocarbons

An integrated process for producing naphtha fuel, diesel fuel and/or lubricant base oils from feedstocks under sour conditions is provided. The ability to process feedstocks under higher sulfur and/or nitrogen conditions allows for reduced cost processing and increases the flexibility in selecting a suitable feedstock. The sour feed can be delivered to a catalytic dewaxing step without any separation of sulfur and nitrogen contaminants. The integrated process includes an initial dewaxing of a feed under sour conditions, optional hydrocracking of the dewaxed feed, and a separation to form a first diesel product and a bottoms fraction. The bottoms fraction is then exposed to additional hydrocracking and dewaxing to form a second diesel product and optionally a lubricant base oil product. Alternatively, a feedstock can be hydrotreated, fractionated, dewaxed, and then hydrocracked to form a diesel fuel and a dewaxed, hydrocracked bottoms fraction that is optionally suitable for use as a lubricant base oil.

Method for recycling liquid waste

A process includes continuous steps and batch steps for recycling waste oil, fuel or antifreeze. The continuous steps include determining the volume of waste; pumping waste toward a distillation vessel; mixing waste with heated waste, and while flowing the waste into the distillation vessel performing steps of: maintaining a vacuum; heating the waste; returning a first portion of heated waste to the distillation vessel and a second-portion to mix with the waste feed; sending gaseous vapors to a condenser; returning some condensed liquid to the distillation vessel; and delivering condensed liquid as a product. The batch steps include: stopping waste flow into the distillation vessel; reducing pressure; heating the waste; returning the heated waste to the distillation vessel; condensing gaseous vapors; returning some condensed effluent to the distillation vessel; delivering some condensed effluent as a first product; and delivering heated waste as a second product.

LUBRICANT BASE STOCK PRODUCTION FROM DISADVANTAGED FEEDS

Methods are provided for upgrading disadvantaged feeds for use in lubricant base stock production. A disadvantaged feed can be upgraded by hydroprocessing the feed to form a hydroprocessed bottoms fraction. The hydroprocessed bottoms fraction can then be used as a feed for forming Group I and/or Group II lubricant base stocks, optionally in combination with a conventional feed for lubricant production. The remaining portions of the hydroprocessing effluent can optionally be used for FCC processing and/or for other conventional applications of naphtha and distillate fractions. 1. A method for forming a lubricant base stock , comprising:hydroprocessing a feed having at least one of a) a total aromatics content of at least 60 wt % and b) a paraffin content of 10 wt % or less under first effective hydroprocessing conditions to form a hydroprocessed effluent comprising at least 50 wt % of hydroprocessed bottoms, the hydroprocessed bottoms having a paraffin content of at least 10 wt % and a total aromatics content of 60 wt % or less;performing a solvent extraction on at least a portion of the hydroprocessed bottoms to form an extract fraction and a raffinate fraction;hydroprocessing at least a portion of the raffinate fraction under second effective hydroprocessing conditions to form a hydroprocessed raffinate; andcatalytically dewaxing at least a portion of the hydroprocessed raffinate to form a catalytic dewaxing effluent, the catalytic dewaxing effluent having a VI of at least 80, an aromatics content of 10 wt % or less, and a sulfur content of 300 wppm or less.2. The method of claim 1 , further comprising hydrofinishing at least a portion of the catalytic dewaxing effluent claim 1 , the at least a portion of the hydroprocessed raffinate claim 1 , or a combination thereof.3. The method of claim 1 , further comprising separating the hydroprocessed bottoms to form at least a lubricant boiling range fraction claim 1 , the at least a portion of the hydroprocessed bottoms ...

Liquid-Phase Hydroisomerization System And Process Therefor And Use Thereof

Provided are a liquid-phase hydroisomerization system and a process therefor and use thereof. The system comprises a gas-liquid mixer (), a hydroisomerization reactor () and a fractionating column (). An oil product and hydrogen are mixed as a liquid hydrogen-oil mixture, and are introduced into the hydroisomerization reactor for a hydroisomerization reaction, and after being fractionated, a target product is led out. A supplemental hydrogen-dissolving inner member is provided at least between a group of two adjacent catalyst bed layers in order to supplement hydrogen to the reactants. The process cancels a circulating hydrogen compressor, has a simple process flow, and can be applied to the production of a lubricant base oil by the hydroisomerization of a lubricant raw material or the production of a low freezing point diesel by the hydroisomerization of and the reduction in the freezing point of a diesel raw material. 1. A liquid-phase hydroisomerization system , characterized in that the system comprises:a hydrogen-dissolving unit, a hydroisomerization reactor, and a fractionating column;wherein the hydrogen-dissolving unit comprises an oil feed line, a hydrogen feed line and a hydrogen-oil-mixture line, the hydrogen-oil-mixture line is in communication with the bottom of the hydroisomerization reactor, and the top of the hydroisomerization reactor is in communication with the fractionating column;the hydroisomerization reactor includes at least two catalyst beds, and an internal dissolved-hydrogen replenishment member is provided between at least one pair of two adjacent catalyst beds;the internal dissolved-hydrogen replenishment member comprises a bottom sieve separating plate, a middle mixing space and a top separating plate, the top separating plate is provided with multiple liquid discharging pipes, and the middle mixing space is provided with a hydrogen inlet and a hydrogen outlet; hydrogen and oil are mixed in the middle mixing space, the liquid phase in ...

FUEL-OIL REFINING DEVICE

The present invention is characterized by comprising: a main unit which incorporates a fuel-inflow port for fuel oil supply, a fuel-discharge port for discharging fuel oil that has finished being refined and a drainage discharge pipe for collecting and discharging untreated fuel oil, and a sludge box for storing sludge that has been separated out from the fuel oil; an ultrasound tank which receives fuel oil supplied from the fuel-inflow port, and adjusts the particle size of the fuel oil and the viscosity and surface tension of the fuel oil by means of ultrasound; a vacuum chamber which receives fuel oil supplied from the ultrasound tank, and of which the inside is maintained in a vacuum state such that the specific volume and the surface area of the fuel oil are maximized via a baffle panel; a water-fraction elimination tank of which one side is connected to the vacuum chamber and the other side is connected to a vacuum pump, and which eliminates the water fraction from the fuel oil by using air heated to a high temperature and the reduced pressure of the vacuum state created due to the vacuum chamber; an oil-refining filter which receives fuel oil supplied from the vacuum chamber and filters the received supply of fuel oil by means of centrifugation so as to trap sludge contained in the fuel oil; an ion chamber which eliminates and bums particles including fine foreign matter remaining in the fuel oil in the state after the sludge has been eliminated; and a control panel which is constituted on one surface of the main unit, sets the operating conditions of the ultrasound tank, vacuum chamber and water-fraction elimination tank, and controls whether to provide power for refining the fuel oil. 1. A fuel-oil refining device comprising:a main body portion including a fuel inlet port for supplying a fuel oil, a fuel discharge port for discharging the refinement-completed fuel oil, a drain pipe for collecting and discharging the untreated fuel oil, and a sludge box for ...

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 ...

HIGH VISCOSITY BASE STOCK COMPOSITIONS

Methods are provided for producing Group I base stocks having high viscosity and also having one or more properties indicative of a high quality base stock. The resulting Group I base stocks can have a viscosity at 100° C. and/or a viscosity at 40° C. that is greater than the corresponding viscosity for a conventional Group I bright stock formed by solvent processing. Additionally, the resulting Group I base stocks can have one or more properties that are indicative of a high quality base stock. 113-. (canceled)14. A method of forming a base stock composition , comprising:introducing a feedstock having a viscosity index of 50 to 120, a kinematic viscosity at 100° C. of 12 cSt or less, and at least one of a sulfur content greater than 0.03 wt % and an aromatics content greater than 10 wt %, into a coupling reaction stage under effective coupling conditions to form a coupled effluent; and{'sub': w', 'n, 'fractionating at least a portion of the coupled effluent to form at least a first product fraction having a viscosity index of at least 50, a polydispersity (M/M) of at least 1.4, a kinematic viscosity at 100° C. of at least 35 cSt, a kinematic viscosity at 40° C. of at least 600 cSt, and a pour point of 0° C. or less.'}15. The method of claim 14 , wherein the effective coupling conditions comprise exposing the feedstock to at least 20 wt % dialkyl peroxide relative to a combined weight of feedstock and peroxide.16. The method of claim 14 , wherein the effective coupling conditions comprise acid-catalyzed coupling conditions.17. The method of claim 14 , further comprising exposing at least a portion of the coupled effluent to a catalyst under effective catalytic processing conditions to form a catalytically processed effluent claim 14 , wherein fractionating at least a portion of the coupled effluent comprises fractionating at least a portion of the catalytically processed effluent.18. The method of claim 17 , wherein the effective catalytic processing conditions ...

HIGH VISCOSITY BASE STOCK COMPOSITIONS

Methods are provided for producing Group III base stocks having high viscosity and also having one or more properties indicative of a high quality base stock. The resulting Group III base stocks can have a viscosity at 100° C. and/or a viscosity at 40° C. that is greater than the corresponding viscosity for a conventional Group III base stock. Additionally, the resulting Group III base stocks can have one or more properties that are indicative of a high quality base stock. 110.-. (canceled)11. A base stock composition having a number average molecular weight (M) of 2500 g/mol to 10000 g/mol , a weight average molecular weight (M) of 4000 g/mol to 30000 g/mol , a polydispersity (M/M) of at least 1.6 , a sulfur content of 0.03 wt % or less , an aromatics content of 10 wt % or less , a kinematic viscosity at 100° C. of at least 2500 cSt , a viscosity at 40° C. of at least 350 cSt , and a viscosity index of 120 to 180.12. The composition of claim 11 , wherein the polydispersity is at least 2.0.13. The composition of claim 11 , wherein the composition has 24.0 wt % or less of epsilon carbons as determined by C-NMR.14. The composition of claim 11 , wherein the weight average molecular weight (M) is at least 5000 g/mol.15. The composition of claim 11 , wherein the composition has a density of 0.86 g/cmto 0.91 g/cm.16. The composition of claim 11 , wherein the composition has a) a kinematic viscosity at 40° C. of at least 3000 cSt; b) a kinematic viscosity at 100° C. of at least 350 cSt; or c) a combination thereof.17. The composition of claim 11 , wherein the viscosity index is at least 130.18. A method of forming a base stock composition claim 11 , comprising:introducing a feedstock having a viscosity index of 50 to 150, a kinematic viscosity at 100° C. of 12 cSt or less, a sulfur content less than 0.03 wt %, and an aromatics content less than 10 wt %, into a coupling reaction stage under effective coupling conditions to form a coupled effluent; and{'sub': w', 'n, ' ...

PARAMETER OPTIMIZATION METHOD FOR DOUBLE-FIELD COUPLING DEHYDRATOR

A double-field coupling dehydrator and an optimization method for parameters. Parameters to be optimized is determined. Simulations to the double-field coupling dehydrator is carried out according to the parameters to be optimized, individually. Optimal ranges of the parameters to be optimized are determined according to simulation results. Optimized parameter combinations of the parameters to be optimized are determined separately. Separation efficiencies of the double-field coupling dehydrator under different optimized parameter combinations are obtained to determine an optimal parameter combination. The method considers both influences of single parameters and interactions between the parameters on the separation efficiency. Based on numerical simulation results of the double-field coupling dehydrator, these influences are analyzed by a software Design-Expert to obtain an optimal parameter combination. 1. A method of parameter optimization for a double-field coupling dehydrator , the double-field coupling dehydrator comprising an overflow pipe , a plurality of inlets , a straight pipe , a first truncated cone , a second truncated cone , and an underflow pipe; the overflow pipe and the plurality of inlets being provided on the straight pipe; the inlets being arranged on an outer wall of the straight pipe and are tangential to a wall of the straight pipe so as to allow a liquid to enter the straight pipe at a certain speed and rotate along an inner wall of the straight pipe; the overflow pipe being arranged along an axis of the straight pipe; a high-voltage electric field being arranged between an outer wall of the overflow pipe in the straight pipe and the inner wall of the straight pipe; and the straight pipe , the first truncated cone , the second truncated cone and the underflow pipe being connected sequentially;a joint between the first truncated cone and the second truncated cone having a nominal diameter D of 20-22 mm; the first truncated cone having a first ...

ETHYLENE OLIGOMERIZATION PROCESS FOR MAKING HYDROCARBON LIQUIDS

Provided herein are processes for ethylene oligomerization in the presence of an ionic liquid catalyst and a co-catalyst to produce a hydrocarbon product comprising C-Coligomers. 1. A hydrocarbon product made by a process comprising:a. selecting a feed comprising an olefin, wherein the olefin comprises greater than 10 wt % ethylene and less than 10 wt % isoparaffins, wherein a molar ratio of the isoparaffins to the ethylene is less than 0.1;b. charging the feed, an ionic liquid catalyst, and a co-catalyst comprising a halide to a reactor; wherein a second molar ratio of the ethylene to the halide in the reactor is from 10 to 50; andc. oligomerizing the olefin in the reactor to produce the hydrocarbon product, wherein greater than 30 wt % of the ethylene is converted to the hydrocarbon product, and wherein greater than 40 wt % of the hydrocarbon product has a boiling point distribution from 250° F. to 700° F.2. The hydrocarbon product of claim 1 , wherein the hydrocarbon product has less than 2 mole % olefinic hydrogens by H NMR claim 1 , less than 0.1 mole % aromatic hydrogens by H NMR claim 1 , an average carbon number from 15 to 40 claim 1 , and a branching index from 45 to 70%.3. The hydrocarbon product of claim 1 , wherein from 1 wt % to 15 wt % of the hydrocarbon product has a lower boiling point distribution from 215° F. to 250° F.4. A hydrocarbon product having less than 2 mole % olefinic hydrogens by H NMR claim 1 , less than 0.1 mole % aromatic hydrogens by H NMR claim 1 , an average carbon number from 15 to 40 claim 1 , a branching index from 45 to 70% claim 1 , and wherein greater than 40 wt % of the hydrocarbon product has a boiling point distribution from 250° F. to 700° F.5. The hydrocarbon product of having less than 2 mole % olefinic hydrogens by H NMR.6. The hydrocarbon product of having 0.1-1.5 mole % olefinic hydrogens by H NMR.7. The hydrocarbon product of having less than 0.1 mole % aromatic hydrogens by H NMR.8. The hydrocarbon product of ...

Chemical Composition of Matter for the Liquefaction and Dissolution of Asphaltene and Paraffin Sludges into Petroleum Crude Oils and Refined Products at Ambient Temperatures and Method of Use

A chemical composition of matter comprising a wax plasticizing agent (plasticizer) tributoxyethyl phosphate, a mixture of selected long chain fatty acids (preferably C 10 to C 22 ), and a mixture of selected low-surface tension surfactants, which when added in solution to crude oil or refined products has been shown to lower both the B.S. & W. (rag layer) and the coefficient of friction of crude oils and refined products. This chemical composition of matter is particularly useful as a wax liquefaction, dispersant, and solubilization agent for asphaltene and paraffins in crude oil and refined products. The reduction in the co-efficient of friction resulting from the addition of this product to crude oil will allow crude oil to pump through pipelines with a minimum amount of resistance due to friction (drag).

Process for preparing liquid hydrocarbons by the fischer-tropsch process integrated into refineries

The present invention relates to a process for preparing liquid hydrocarbons by the Fischer-Tropsch process integrated into refineries, in particular comprising recycling streams from the steam reforming hydrogen production process as the feedstock for the Fischer-Tropsch process.

CATALYTIC PROCESSES AND SYSTEMS FOR BASE OIL PRODUCTION USING ZEOLITE SSZ-32X

Processes and catalyst systems are provided for dewaxing a hydrocarbon feedstock to form a lubricant base oil. A layered catalyst system of the present invention may comprise a first hydroisomerization dewaxing catalyst disposed upstream from a second hydroisomerization dewaxing catalyst. Each of the first and second hydroisomerization dewaxing catalysts may be selective for the isomerization of n-paraffins. The first hydroisomerization catalyst may have a higher level of selectivity for the isomerization of n-paraffins than the second hydroisomerization dewaxing catalyst. At least one of the first and second hydroisomerization dewaxing catalysts comprises small crystallite zeolite SSZ-32x. 1. A process for catalytically dewaxing a waxy hydrocarbon feedstock , comprising:a) contacting the hydrocarbon feedstock in a first hydroisomerization zone under first hydroisomerization dewaxing conditions with a first hydroisomerization catalyst comprising SSZ-32x to provide a first isomerization stream; andb) contacting at least a portion of the first isomerization stream in a second hydroisomerization zone under second hydroisomerization dewaxing conditions with a second hydroisomerization catalyst which comprises a molecular sieve and a Group VIII metal to provide a second isomerization stream.2. The process according to claim 1 , wherein the second hydroisomerization catalyst comprises a 1-D claim 1 , 10-ring molecular sieve.3. The process according to claim 1 , wherein the first hydroisomerization catalyst comprises SSZ-32x doped with a metal modifier selected from the group consisting of Mg claim 1 , Ca claim 1 , Sr claim 1 , Ba claim 1 , K claim 1 , La claim 1 , Pr claim 1 , Nd claim 1 , Cr claim 1 , and combinations thereof.4. The process according to claim 3 , wherein the first hydroisomerization catalyst has a first level of selectivity for the isomerization of n-paraffins in the feedstock claim 3 , the second hydroisomerization catalyst has a second level of ...

REMOVAL OF POLYNUCLEAR AROMATICS FROM SEVERELY HYDROTREATED BASE STOCKS

Adsorbents for aromatic adsorption are used to improve one or more properties of base stocks derived from deasphalted oil fractions. The adsorbents can allow for removal of polynuclear aromatics from an intermediate effluent or final effluent during base stock production. Removal of polynuclear aromatics can be beneficial for improving the color of heavy neutral base stocks and/or reducing the turbidity of bright stocks. 1. A method for making lubricant base stock , comprising:performing solvent deasphalting, under effective solvent deasphalting conditions on a feedstock having a T5 boiling point of 370° C. or more and a T50 of 510° C. or more, the effective solvent deasphalting conditions producing a yield of deasphalted oil of 40 wt % or more of the feedstock;hydroprocessing at least a portion of the deasphalted oil under first effective hydroprocessing conditions to form a hydroprocessed effluent, the at least a portion of the deasphalted oil having an aromatics content of 60 wt % or more, 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, from the hydroprocessed effluent, at least a fuels boiling range fraction, a first fraction comprising polynuclear aromatics and 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 viscosity at 100° C. than the first fraction;'}hydroprocessing at least a portion of the first fraction under second effective hydroprocessing conditions, the second effective hydroprocessing conditions comprising catalytic dewaxing conditions, to form a twice-hydroprocessed effluent comprising a 370° C.+ portion having a first kinematic viscosity at 100° C.; andi) exposing the at least a portion of the first fraction, prior to the hydroprocessing under second effective hydroprocessing conditions, to an adsorbent under ...

METHODS FOR FRACTIONATION OF LUBRICANT FEEDS

Systems and methods are provided for the fractionation of lubricant feeds. A lubricant feed can be introduced into a vacuum distillation tower having a reduced pressure and a reduced or minimized water vapor partial pressure. The lubricant feed can be separated into a plurality of lubricant boiling range products. The can allow an overlap in boiling ranges of one or more products separated from the lubricant feed to be reduced or minimized. 1. A method for the fractionation of a lubricant boiling range feed , comprising:introducing a lubricant boiling range feed into a flash zone of a distillation tower, the distillation tower having a pressure of 3.5 kPa-a or less and a water vapor partial pressure of 0.5 kPa-a or less; andseparating the lubricant boiling range feed into at least a first lubricant boiling range product and a second lubricant boiling range product, wherein the first lubricant boiling range product has a T95 boiling point that is greater than a T5 boiling point of the second lubricant boiling range product by 14° C. or less, and wherein a T95 boiling point of the second lubricant boiling range product is greater than the T95 boiling point of the first lubricant boiling range product.2. The method of claim 1 , wherein the T95 boiling point of the first lubricant boiling range product is greater than the T5 boiling point of the second lubricant boiling range product by 11° C. or less.3. The method of claim 1 , further comprising withdrawing a fraction of the lubricant boiling range feed from the distillation tower and passing a portion of the fraction through a reboiler loop.4. The method of claim 1 , further comprising withdrawing a fraction of the lubricant boiling range feed from the distillation tower and passing a portion of the fraction through a stripper claim 1 , wherein a stripper medium in the stripper comprises a heated vapor stream from a reboiler loop associated with the stripper claim 1 , and wherein the heated vapor stream comprises a ...

HIGH PRESSURE HYDROFINISHING FOR LUBRICANT BASE OIL PRODUCTION

Systems and methods are provided for catalytic hydroprocessing to form lubricant base oils. The methods can include performing high pressure hydrofinishing after fractionating the hydrotreated and/or hydrocracked and/or dewaxed effluent. Performing hydrofinishing after fractionation can allow the high hydrogen pressure for hydrofinishing to be used on one or more lubricant base oil fractions that are desirable for high pressure hydrofinishing. This can allow for improved aromatic saturation of a lubricant base oil product while reducing or minimizing the hydrogen consumption. The high pressure hydrofinishing can be performed at a hydrogen partial pressure of at least about 2500 psig (˜17.2 Mpa), or at least about 2600 psig (˜18.0 Mpa), or at least about 3000 psig (˜20.6 MPa). The high pressure hydrofinishing can allow for formation of a lubricant base oil product with a reduced or minimized aromatics content, a reduced or minimized 3-ring aromatics content, or a combination thereof. 1. A method for forming a lubricant base stock , comprising:hydrocracking a lubricant boiling range feed under hydrocracking conditions;dewaxing the at least a portion of a lubricant boiling range feed under dewaxing conditions to form a hydroprocessed effluent, the dewaxing occurring prior to the hydrocracking, during the hydrocracking, after the hydrocracking, or a combination thereof;fractionating the hydroprocessed effluent to form one or more hydroprocessed lubricant boiling range fractions; and a) a hydrogen partial pressure that is at least 250 psi (1.7 MPa) greater than a hydrogen partial pressure of the dewaxing conditions, and', 'b) a hydrogen partial pressure of greater than 2000 psig (13.8 MPa), the hydrogen partial pressure of the hydrofinishing conditions being greater than the hydrogen partial pressure of the dewaxing conditions., 'hydrofinishing at least one hydroprocessed lubricant boiling range fraction under hydrofinishing conditions to form at least one hydrofinished ...

Lubricant basestock production with enhanced aromatic saturation

Systems and methods are provided for producing lubricant basestocks having a reduced or minimized aromatics content. A first processing stage can perform an initial amount of hydrotreating and/or hydrocracking. A first separation stage can then be used to remove fuels boiling range (and lower boiling range) compounds. The remaining lubricant boiling range fraction can then be exposed under hydrocracking conditions to a USY catalyst including a supported noble metal, such as Pt and/or Pd. The USY catalyst can have a desirable combination of catalyst properties, such as a unit cell size of 24.30 or less (or 24.24 or less), a silica to alumina ratio of at least 50 (or at least 80), and an alpha value of 20 or less (or 10 or less). In some aspects, the effluent from the second (hydrocracking) stage can be dewaxed without further separation. In such aspects, a portion of the dewaxed effluent can be used as a recycle quench stream to cool the hydrocracking effluent prior to entering the dewaxing reactor.

Base stocks and lubricant compositions containing same

A base stock having at least 90 wt. % saturates, an amount and distribution of aromatics, as determined by ultra violet (UV) spectroscopy, including an absorptivity between 280 and 320 nm of less than 0.015 l/gm-cm, a viscosity index (VI) from 80 to 120, and having a cycloparaffin performance ratio greater than 1.05 and a kinematic viscosity at 100° C. between 4 and 6 cSt. A base stock having at least 90 wt. % saturates, an amount and distribution of aromatics, as determined by UV spectroscopy, including an absorptivity between 280 and 320 nm of less than 0.020 l/gm-cm, a viscosity index (VI) from 80 to 120, and having a cycloparaffin performance ratio greater than 1.05 and a kinematic viscosity at 100° C. between 10 and 14 cSt. A lubricating oil having the base stock as a major component, and one or more additives as a minor component. Methods for improving oxidation performance and low temperature performance of formulated lubricant compositions through the compositionally advantaged base stock.

Method for Producing Base Lubricating Oil from Waste Oil

A method for recovering base oil from waste lubricating oil by separating base oil range constituents from a waste lubricating oil mixture, thereafter separating higher quality base oil constituents and lower quality base oil constituents from the base oil recovered from the waste lubricating oil mixture and thereafter treating the lower quality base oil constituents to produce marketable base oil. The total base oil produced from a waste lubricating oil mixture by this process is greater than the quantity producible by previous processes using only base oil separation from the waste lubricating oil mixture or processes which use only treatment of the base oil recovered from the waste lubricating oil mixture to produce the product base oil. 1. A method for separating a liquid stream comprising a plurality of constituents of varied boiling points by flash distillation in at least one distillation zone comprising at least one flash distillation vessel to produce at least one overhead stream and at least one bottom stream , the method comprising:a) passing the liquid stream into a heated liquid layer contained in a flash distillation vessel and producing an overhead stream and a bottom stream and having up to one theoretical plate;b) heating the bottom stream to a selected temperature and passing a portion of the heated bottom stream to the flash distillation vessel to maintain the heated liquid layer at a selected temperature and at a selected level in the flash distillation vessel in a lower portion of the vessel;c) heating the heated liquid layer in the flash distillation vessel at a temperature sufficient to flash a portion of the liquid feed stream to the flash distillation vessel thereby producing the bottom stream and the overhead stream;d) passing at least a portion of the distillate overhead stream out of the distillation vessel.2. The method of wherein a plurality of flash distillation vessels are used.3. The method of wherein at least one of the flash ...

METHOD FOR MANUFACTURING LUBRICANT BASE OIL

A method for producing a base oil for lubricant oils comprising: a first step of hydrocracking a petroleum slack wax having a content percentage of a heavy matter having 30 or more carbon atoms of 80% by mass or more and a content percentage of an oil of 15% by mass or less so that a crack per mass of the heavy matter is 5 to 30% by mass to obtain a hydrocracked oil comprising the heavy matter and a hydrocracked product thereof; and a second step of obtaining the base oil for lubricant oils from the hydrocracked oil. 1. A method for producing a base oil for lubricant oils comprising:hydrocracking a petroleum slack wax having a content percentage of a heavy matter having 30 or more carbon atoms of 80% by mass or more and a content percentage of an oil of 15% by mass or less so that a crack per mass of the heavy matter is 5 to 30% by mass to obtain a hydrocracked oil comprising the heavy matter and a hydrocracked product thereof; andobtaining the base oil for lubricant oils from the hydrocracked oil.2. The method according to claim 1 , wherein obtaining the base oil for lubricant oils from the hydrocracked oil comprises:obtaining a dewaxed oil by hydroisomerization dewaxing the hydrocracked oil;obtaining a hydrorefined oil by hydrorefining the dewaxed oil; andobtaining the base oil for lubricant oils by distilling the hydrorefined oil.3. The method according to claim 1 , wherein obtaining the base oil for lubricant oils from the hydrocracked oil comprises:obtaining a base oil fraction comprising the hydrocracked product by distilling the hydrocracked oil;obtaining a dewaxed oil by hydroisomerization dewaxing the base oil fraction;obtaining a hydrorefined oil by hydrorefining the dewaxed oil; andobtaining the base oil for lubricant oils by distilling the hydrorefined oil.4. The method according to claim 1 , further comprising obtaining the petroleum slack wax from a high-oil-content slack wax having a content percentage of an oil of greater than 15% by mass.5. The ...

HYDROCRACKING PROCESS FOR HIGH YIELDS OF HIGH QUALITY LUBE PRODUCTS

A process for producing high yields of higher quality (API Group II, Group III′) lubricating oil basestock fractions which allows the production of two or more types of high quality lubes in continuous mode (no blocked operation mode) without transition times and feed or intermediate product tankage segregation. Two consecutive hydroprocessing steps are used: the first step processes a wide cut feed at a severity needed to match heavy oil lube properties. The second step hydroprocesses a light oil after fractionation of the liquid product from the first step at a severity higher than for the heavy oil fraction. The two hydroprocessing steps will normally be carried out in separate reactors but they may be combined in a single reactor which allows for the two fractions to be processed with different degrees of severity. 1. A process for producing at least two lube boiling range fractions including a light oil lube fraction and a heavy oil lube fraction , which comprises:hydrocracking a hydrocarbon feed in a first hydrocracking step under a first hydrocracking regime to provide a hydrocrackate with a boiling range suitable for the heavy oil fraction,fractionating the hydrocrackate to separate at least a first portion for the light oil fraction and a second portion for the heavy oil fraction;hydrocracking the portion for the light oil fraction in a second hydrocracking step under a second hydrocracking regime to form a second light oil hydrocrackate with a boiling range suitable for the light oil fraction, combining the hydrocrackate portion for the heavy oil and the second light oil hydrocrackate to form a combined hydrocrackate,processing the combined hydrocrackate to meet product specifications for the light oil lube fraction and the heavy oil lube fraction and form a combined stream of a finished light oil lube fraction and a finished heavy oil lube fraction, andfractionating the combined stream to separate the finished light oil lube fraction and the finished ...

Production of lubricant oils from thermally cracked resids

Methods are provided for processing deasphalted gas oils derived from thermally cracked resid fractions to form Group I, Group II, and/or Group III lubricant base oils. The yield of lubricant base oils (optionally also referred to as base stocks) can be increased by thermally cracking a resid fraction at an intermediate level of single pass severity relative to conventional methods. By performing thermal cracking to a partial level of conversion, compounds within a resid fraction that are beneficial for increasing both the viscosity and the viscosity index of a lubricant base oil can be retained, thus allowing for an improved yield of higher viscosity lubricant base oils from a thermally cracked resid fraction.

DOUBLE-FIELD COUPLING DEHYDRATOR AND PARAMETER OPTIMIZATION THEREFOR

The invention discloses a double-field coupling dehydrator and an optimization method for parameters thereof. The optimization method includes: determining parameters to be optimized; carrying out simulations to the double-field coupling dehydrator according to the parameters to be optimized, separately; determining optimal ranges of the parameters to be optimized according to simulation results; determining optimized parameter combinations of the parameters to be optimized, separately; carrying out simulations to the double-field coupling dehydrator according to the optimized parameter combinations, separately; obtaining separation efficiencies of the double-field coupling dehydrator under different optimized parameter combinations; and determining an optimal parameter combination according to the separation efficiencies of the double-field coupling dehydrator. The method considers both influences of single parameters and interactions between the parameters on the separation efficiency. Based on numerical simulation results of the double-field coupling dehydrator, these influences are analyzed by a software Design-Expert to obtain an optimal parameter combination.

Process for Reducing Haze in Heavy Base Oil and Hydroisomerization Catalyst System Having Reduced Haze

A process for reducing haze in a heavy base oil includes: obtaining a first effluent oil by contacting a hydrocarbon feedstock with a first catalyst including a zeolite of the ZSM-12 family; and obtaining a second effluent oil by contacting the first effluent oil with a second catalyst including a zeolite of the ZSM-48 family. A hydroisomerization catalyst system having reduced haze includes: a first catalytic region having a first catalyst disposed therein, the first catalyst including a zeolite of the ZSM-12 family; and a second catalytic region having a second catalyst disposed therein, the second catalyst including a zeolite of the ZSM-48 family. The first catalytic region is disposed upstream of the second catalytic region.