СМЕСЬ КЕРОСИНОВ НЕФТЯНОГО ПРОИСХОЖДЕНИЯ И ПОЛУЧАЕМЫХ ПО ФИШЕРУ-ТРОПШУ

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СПОСОБ И УСТРОЙСТВО ДЛЯ ПОЛУЧЕНИЯ ТОПЛИВА ИЗ СЫРЬЯ БИОЛОГИЧЕСКОГО ПРОИСХОЖДЕНИЯ ОДНОСТАДИЙНЫМ ГИДРИРОВАНИЕМ В ПРИСУТСТВИИ NiW КАТАЛИЗАТОРА

Изобретение относится к способу получения смеси компонентов топлива, причем способ включает использование сырья биологического происхождения. Способ получения смеси компонентов топлива включает: обеспечение сырья биологического происхождения, выбранного из таллового масла, сырого таллового масла и биомасла из гидропиролизованной древесины, одностадийное гидрирование указанного сырья биологического происхождения и газообразного водорода в присутствии каталитической системы, включающей NiW катализатор на носителе из цеолит-AlO, с образованием смеси компонентов топлива. Изобретение также относится к устройству для получения смеси компонентов топлива из сырья биологического происхождения. Технический результат - упрощение способа и устройства путем исключения промежуточных стадий и затрат. 2 н. и 15 з.п. ф-лы, 3 табл., 3 ил., 2 пр.

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

Низкосернистые судовые бункерные топлива и способы их получения

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СПОСОБЫ ПОЛУЧЕНИЯ НЕОЧИЩЕННОГО ПРОДУКТА

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

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Изобретение относится к нефтепереработке, в частности к составу автомобильного бензина, предназначенного для использования в качестве топлива для первой заправки автомобилей. Предложен бензин для первой заправки автомобилей, характеризующийся компаундированием следующих компонентов: алкилат установок получения бензинов кислотным алкилированием; изомеризат установки изомеризации легких бензиновых фракций с блоками предварительной гидроочистки; бутан-бутиленовой фракции с установок каталитического крекинга, метил-трет-бутилового эфира и многофункциональной присадки HITEC 6437 ЕСТО, при следующем соотношении, мас.%: алкилат 51÷75, изомеризат 15÷35, бутан-бутиленовая фракция ≤4, метил-трет-бутиловый эфир ≤15, многофункциональная присадка HITEC 6437 ECTO ≤0,1. Техническим результатом является получение бензина, обладающего высокими октановыми характеристиками, как по исследовательскому, так и по моторному методам, низким содержанием вредных выбросов, выделяемых в процессе сгорания, отсутствием ...

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Изобретение относится к области нефтепереработки. Предложен способ снижения выбросов в портах, включающий (a) технический анализ, проведенный из расчета в кВт/ч выбросов серы или металлов, возникающих в результате выработки электроэнергии на берегу системами, которые вырабатывают электроэнергию, обычно поставляемую электросети в порту или в месте, находящемся рядом, включая выбросы в атмосферу выхлопных газов такими системами, которые непосредственно связаны с использованием судном местного электроснабжения, когда судно находится в порту и подсоединено к электросети, поставляющей электричество, вырабатываемое на берегу; (b) технический анализ, проведенный из расчета в кВт/ч количества выбросов серы и металлов, возникающих в результате выработки на борту судна электроэнергии судном в порту в месте (a), затем сравнение (а) и (b), и если (b) выбросы, генерируемые судном для выработки электроэнергии, ниже, чем местные источники энергии (a), то судно передает всю или часть электроэнергии, выработанной ...

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Изобретение относится к композиции, содержащей лигнин. Композиция, содержащая лигнин для получения топлива или добавок для топлива, содержит лигнин, растворитель и жидкость-носитель, где лигнин составляет по меньшей мере 4 вес.% композиции, и где лигнин характеризуется средневесовым молекулярным весом не более 5000 г/моль, и где растворитель представляет собой спирт, простой эфир или органический сложный эфир, сульфоксид, кетон, альдегид или их комбинацию, или растворитель содержит диметилсульфоксид, пиридин, THF, 1,4-диоксан, фурфурол, дипропиленгликоль, полиэтиленгликоль или 1,3-пропандиол или их комбинацию; и где жидкость-носитель представляет собой смесь углеводородного масла и жирной кислоты, где углеводородное масло представляет собой газойль. Заявлены также способ получения композиции и ее применение. Технический результат – получение композиции для получения топлива или добавок в топливо менее сложным способом. 3 н. и 13 з.п. ф-лы, 3 ил., 250 пр.

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Изобретение раскрывает присадку для мазута, которая выполнена в виде суспензии из наноструктурированного гидроксида магния в количестве (45-55%) и смеси дизельного топлива с минеральным маслом - остальное, в соотношении между ними (0,5-1,25). Техническим результатом является обеспечение при использовании присадки более полного сгорания мазута с изменением при этом структуры отложений на поверхностях нагрева котла из липких и твердых в рыхлые и порошкообразные, легко удаляемые, а также снижение вредных веществ в выбрасываемых в атмосферу дымовых газах, загрязняющих атмосферу.

МЕТОДЫ ПРОИЗВОДСТВА ТОПЛИВА ДЛЯ РЕАКТИВНЫХ ДВИГАТЕЛЕЙ ИЗ НАТУРАЛЬНОГО МАСЛА КАК ИСХОДНОГО СЫРЬЯ С ПОМОЩЬЮ РЕАКЦИЙ ОБМЕНА

Изобретение относится к способам получения топлива для реактивных двигателей, характеризующимся проведением реакции между исходным сырьем, в состав которого входит натуральное масло, и легким олефином в присутствии катализатора реакции обмена в условиях, достаточных для образования продукта реакции обмена. Гидрирование продукта реакции обмена происходит в условиях, достаточных для образования топлива для реактивных двигателей. Также способы могут включать сепарирование воды и изомеризацию топлива для реактивных двигателей. Топлива, получаемые по заявленным способам, содержат увеличенный выход С-Салканов. 2 н. и 18 з.п. ф-лы, 1 ил., 3 пр., 1 табл.

ВОЗОБНОВЛЯЕМАЯ УГЛЕВОДОРОДНАЯ КОМПОЗИЦИЯ

Изобретение относится к углеводородной композиции. Углеводородная композиция, пригодная в качестве топлива или топливного компонента, содержит от 10 до 40 масс.% неразветвленных C-алканов, от 0,1 до 15 масс.% ароматических C-углеводородов, из которых, по меньшей мере, 90 масс.% являются моноароматическими, и не более чем 1 масс.% в сумме кислородсодержащих соединений; причем в данной композиции суммарное содержание C-алканов составляет от 50 до 95 масс.%, а суммарное содержание C-алканов, ароматических C-углеводородов и C-циклоалканов составляет, по меньшей мере, 95 масс.%; и данные количества вычислены по отношению к массе композиции. Кроме того, заявлен способ изготовления композиции, ее применение и смешанное топливо. Технический результат – получение углеводородной композиции, которую можно использовать в качестве топливного компонента или топлива. Малое содержание кислородсодержащих компонентов в составе композиции обеспечивает устойчивость при хранении и меньшую разрушаемость автомобильных ...

СПОСОБ И УСТРОЙСТВО ДЛЯ СНИЖЕНИЯ ЗАГРЯЗНИТЕЛЕЙ ОКРУЖАЮЩЕЙ СРЕДЫ В ТЯЖЕЛОМ СУДОВОМ ЖИДКОМ ТОПЛИВЕ

Изобретение относится к двум вариантам способа снижения загрязнителей окружающей среды в тяжелом судовом жидком топливе. Один из вариантов включает: смешивание некоторого количества сырья тяжелого судового жидкого топлива с некоторым количеством водородного газа в качестве активирующего газа с получением смеси исходного сырья; контактирование смеси сырья с катализаторами, в качестве которых используют по меньшей мере катализатор гидродеметаллирования и катализатор гидродесульфурации, с образованием технологической смеси из смеси сырья; получение указанной технологической смеси и отделение жидких компонентов продукта тяжелого судового жидкого топлива технологической смеси от газообразных компонентов и побочных углеводородных компонентов технологической смеси и выгрузку продукта тяжелого судового жидкого топлива, при этом осуществляют выборочное удаление загрязнений окружающей среды из исходного сырья тяжелого судового жидкого топлива с обеспечением контакта смеси сырья сначала со слоем катализатора ...

СПОСОБ ПОЛУЧЕНИЯ ТОПЛИВА И УСТРОЙСТВО ДЛЯ ЕГО ОСУЩЕСТВЛЕНИЯ

Изобретение относится к получению нефтяного топлива. Изобретение касается способа получения нефтяного топлива, в котором осуществляют смешение и проведение реакции гидролиза воды, содержащей фермент, с углеводородным нефтепродуктом, причем воду, содержащую фермент, получают путем перемешивания в воде природного растительного фермента, содержащего, по меньшей мере, липазу. Природный растительный фермент дополнительно может содержать целлюлазу. Изобретение также касается устройства для получения нефтяного топлива. Технический результат - повышение эффективности топлива, которое является стабильным, а также подавление образования опасных веществ. 2 н. и 8 з.п. ф-лы, 11 ил., 1 пр.

СПОСОБ ДЕОКСИГЕНАЦИИ СТЕАРИНОВОЙ КИСЛОТЫ НА КРИСТАЛЛИЧЕСКОМ И НАНЕСЁННОМ ФТАЛОЦИАНИНОВОМ КАТАЛИЗАТОРЕ

Изобретение относится к области нефтехимии, а именно к способу получения углеводородов, пригодных для использования в качестве компонентов дизельного топлива, заключающемуся в декарбонилировании/декарбоксилировании стеариновой кислоты в растворителе в атмосфере водорода при 350-400°С и давлении водорода 0,1-5 МПа в присутствии гетерогенного катализатора, представляющего собой октанатриевую соль 2,3,9,10,16,17,23,24-октакарбоксифталоцианина кобальта, нанесенную на оксид алюминия. Изобретение обеспечивает создание каталитического способа получения углеводородов из возобновляемых источников сырья с заменой дорогостоящего палладиевого катализатора на катализатор, не содержащий благородные металлы. 3 з.п. ф-лы, 1 табл., 7 пр.

МНОГОФУНКЦИОНАЛЬНАЯ ДОБАВКА К АВИАЦИОННЫМ БЕНЗИНАМ (ВАРИАНТЫ)

Изобретение раскрывает многофункциональную добавку к авиационным бензинам, которая включает тетраэтилсвинец, 1,2-дибромэтан и 2,6-ди-трет-бутил-4-метилфенол, добавка имеет температуру начала кристаллизации не выше минус 40°C и содержит углеводородную фракцию, имеющую температуру конца кипения не выше 201°C, давление насыщенных паров при 38,7°C не более 51 кПа, содержащую не менее 10% масс. ароматических и не более 2% масс. непредельных углеводородов, при следующем соотношении компонентов, % масс.: тетраэтилсвинец 5,0-50,0, 1,2-дибромэтан 3,0-30,0, 2,6-ди-трет-бутил-4-метилфенол 0,1-1,0, углеводородная фракция до 100. Также раскрывается многофункциональная добавка к авиационным бензинам, включающая этиловую жидкость TEL-B и углеводородную фракцию, имеющую температуру конца кипения не выше 201°С. Технический результат заключается в получении многофункциональной добавки, которая обладает лучшими низкотемпературными свойствами и при введении в авиационный бензин улучшает его антидетонационные ...

УСТАНОВКА ДЛЯ ПРОИЗВОДСТВА ТОПЛИВНЫХ КОМПОНЕНТОВ ИЗ ОТРАБОТАННЫХ НЕФТЕПРОДУКТОВ И НЕФТЕШЛАМОВ

Изобретение относится к нефтеперерабатывающей промышленности. Изобретение касается установки для производства топливных компонентов, содержащей соединенные трубопроводами с запорно-регулирующей арматурой емкость подачи исходного нефтепродукта, печь нагрева, ректификационную колонну, систему охлаждения и конденсации паров, емкости сбора готовых компонентов, насосы, пульт управления. Установка дополнительно содержит сборную промежуточную емкость и узел распределения потоков компонентов, ректификационная колонна дополнительно содержит в нижней части пластины, размещенные под углом к стенкам колонны и друг к другу, и вход над пластинами для подачи отработанных нефтепродуктов и нефтешламов с высоким содержанием парафинов, причем сборная промежуточная емкость с одной стороны трубопроводами соединена с системой охлаждения и конденсации паров, а с другой стороны с узлом распределения потоков компонентов, выходы которого соединены с емкостями сбора готовых компонентов: топливного компонента Д-22 ...

Стабильное низкосернистое остаточное судовое топливо

Изобретение относится к стабильному низкосернистому остаточному судовому топливу, содержащему компоненты с основой ароматических углеводородов, выбранных из группы, включающей в себя тяжелый газойль замедленного коксования и/или тяжелый газойль каталитического крекинга, компоненты с основой асфальтенов, выбранные из группы, включающей в себя асфальт, и/или, гудрон, и/или мазут, компоненты с основой алкановых углеводородов, выбранные из группы, включающей в себя вакуумный газойль гидроочищенный, и/или дизельное топливо летнее, и/или тяжелый остаток гидрокрекинга. При этом используют следующее соотношение компонентов: компоненты с основой ароматических углеводородов – 30-60%; компоненты с основой алкановых углеводородов – 20-41%; компоненты с основой асфальтенов – 15-30%. Техническим результатом является получение стабильного низкосернистого остаточного судового топлива с содержанием серы до 0,50% масс. 3 табл., 1 пр.

УСТАНОВКА ДЛЯ ОБРАБОТКИ ПРОДУКЦИИ СКВАЖИН

Изобретение относится к нефтедобывающей промышленности, в частности к подготовке товарной нефти. Установка подготовки продукции скважин включает подводящий трубопровод, устройство подогрева, узел разрушения бронирующих оболочек, соединенный с концевым делителем фаз, трехфазный сепаратор с линией отвода воды, нефтяную и водяную буферные емкости, линию выхода воды, соединенную посредством кустовой насосной станции с входом узла разрушения бронирующих оболочек, при этом концевой делитель фаз снабжен двумя дозвуковыми соплами с возбудителями акустических колебаний в виде упругих пластин, закрепленных на соплах поперек потока воды, первый из которых с постоянной настройкой, а второй - с возможностью изменения длины активной части, при этом сопла соединены с кустовой насосной станцией патрубком. Технический результат: повышение воздействия на бронирующие оболочки эмульсии за счет суммарной амплитуды двух возбудителей колебаний; расширение частотного диапазона колебаний за счет применения биений ...

СПОСОБ ПОЛУЧЕНИЯ КОТЕЛЬНОГО ТОПЛИВА

Способ получения котельного топлива, включающий вакуумную ректификацию прямогонного мазута, с получением утяжеленного гудрона и металлизированной фракции вакуумной ректификации, фракции вакуумного газойля с последующим висбрекингом утяжеленного гудрона с получением комбинированного продукта висбрекинга, при этом для получения котельного топлива смешивают гудрон утяжеленный, металлизированную фракцию вакуумной ректификации мазутов, смесь асфальта и экстракта производства масел, разбавитель - прямогонное дизельное топливо фракции 160-360°С, комбинированный продукт висбрекинга, характеризующийся тем, что в процессе вакуумной ректификации смесевого сырья дополнительно выделяют фракцию с температурой кипения 360-390°С и используют ее в качестве дополнительного компонента разбавителя котельного топлива, в котельное топливо дополнительно вводят фракцию каталитического газойля с температурой кипения 190-550°С, при следующем соотношении компонентов смешения в котельном топливе, мас. %: гудрон утяжеленный ...

ТОПЛИВНАЯ КОМПОЗИЦИЯ АВИАЦИОННОГО БЕНЗИНА

Изобретение раскрывает топливную композицию авиационного бензина с октановым числом не менее 91 и сортностью не менее 115, которая содержит алкилбензин, характеризующаяся тем, что дополнительно содержит смесь предельных углеводородов Си выше, выкипающих в интервале температур 25÷200°С, и толуол при следующем соотношении компонентов в композиции, мас. %: алкилбензин - 35 45; смесь предельных углеводородов Си выше, выкипающих в интервале температур 25÷200°С - 35÷45; толуол - до 100 с последующим введением антидетонационной присадки, антиокислительной присадки и красителя, при этом в качестве антидетонационной присадки используют тетраэтилсвинец в этиловой жидкости в количестве 0,1×0,15 мас. %, в пересчете на тетраэтилсвинец, в качестве антиокислительной присадки используют Агидол-1 в количестве 0,0010×0,0016 мас. %, в качестве красителя используют органический жирорастворимый зеленый антрахиноновый в количестве 0,00025÷0,0004 мас. %. Технический результат: получение топливной композиции авиационного ...

КОМБИНИРОВАННЫЙ СПОСОБ ПОЛУЧЕНИЯ СУДОВЫХ ВЫСОКОВЯЗКИХ ТОПЛИВ И НЕФТЯНОГО КОКСА

Изобретение раскрывает комбинированный способ получения судовых высоковязких топлив и нефтяного кокса, включающий использование легкого и тяжелого газойлей коксования, характеризующийся тем, что при перегонке нефти выделяют фракцию вакуумного газойля, 95% которого выкипает в пределах от 350 до 500°С, и гудрон-фракцию, выкипающую выше 500°С, при этом каталитическому крекингу с выделением тяжелой газойлевой фракции от 180 до 400°C подвергают фракцию вакуумного газойля от 350 до 500°С, предварительно гидроочищенную, висбрекингу - гудрон с выделением висбрекинг-остатка, а замедленному коксованию - смесь гудрона и тяжелого газойля каталитического крекинга, взятых в массовом соотношении 70-90:10-30, с выделением из продуктов реакций легкого газойля замедленного коксования от 180 до 360°C и нефтяного электродного кокса и последующим компаундированием висбрекинг-остатка (ВО) и легкого газойля замедленного коксования (ЛГЗК) от 180 до 360° для получения судовых высоковязких топлив, взятых в массовом ...

СПОСОБ ПОЛУЧЕНИЯ ФРАКЦИИ ГАЗОЙЛЯ И ОСТАТОЧНОГО БАЗОВОГО МАСЛА

... 1. Способ получения фракции газойля, фракции тяжелого дистиллята и фракции остаточного базового масла из полученного в синтезе Фишера-Тропша сырья, включающий:(a) направление сырья на стадию гидропереработки для получения по меньшей мере частично изомеризованного сырья;(b) разделения изомеризованного сырья с помощью перегонки на по меньшей мере фракцию газойля, фракцию тяжелого дистиллята и остаточную фракцию, причем остаточная фракция имеет температуру перегонки Т10 % масс. от 200°C до 450°C;(c) рециркулирования части остаточной фракции на стадию (а); и(d) каталитической депарафинизации остальной остаточной фракции с получением остаточного базового масла.2. Способ по п. 1, в котором фракция газойля и фракция тяжелого дистиллята разделяют на стадии (b) при температуре границы разделения от 300°C до 400°C.3. Способ по п. 1 или 2, в котором фракция тяжелого дистиллята и остаточная фракция разделяют на стадии (b) при температуре границы разделения от 450°C до 600°C.4. Способ по п. 1 или 2, ...

ТОПЛИВО ДЛЯ РЕАКТИВНОГО ДВИГАТЕЛЯ, ГАЗОВОЙ ТУРБИНЫ, РАКЕТНОГО ДВИГАТЕЛЯ И ДИЗЕЛЬНОГО ДВИГАТЕЛЯ

... 1. Топливная композиция для применения в реактивных двигателях, газовых турбинах, ракетных двигателях или дизельных двигателях, включающая (а) от 5 до 99% от массы топливной композиции соединений формулы (I) где А выбран из бензола, толуола, ксилола, циклогексана и их смеси, более предпочтительным А является бензол, толуол или циклогексан, наиболее предпочтительным - бензол; так, что A нетерминально присоединен к фрагменту L и дополнительно A напрямую соединен с фрагментом L; R′ выбран из водорода и С1-С3 алкила; R′ выбран из водорода и С1-С3алкила, где оба R′ и R′′ нетерминально присоединены к фрагменту L; фрагмент L является линейным ациклическим алифатическим углеводородным радикалом, так что общее число атомов углерода в фрагментах L, R′ и R′′ равна от 5 до 25 атомов углерода; (b) по крайней мере, примерно 0,01% топливных добавок; и (c) от 0 до 90% обычных смесей топливных компонентов для реактивного двигателя, газовой турбины, ракетного двигателя и дизельного двигателя, предпочтительно ...

СПОСОБЫ ПОЛУЧЕНИЯ НЕОЧИЩЕННОГО ПРОДУКТА И ВОДОРОДСОДЕРЖАЩЕГО ГАЗА

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

СПОСОБ ПОЛУЧЕНИЯ НЕОЧИЩЕННОГО ПРОДУКТА

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

Способ переоборудования обычного нефтеперерабатывающего предприятия в предприятие по получению топлива из биологического сырья

... 1. Способ переоборудования нефтеперерабатывающего предприятия, включающего систему, содержащую два блока, U1 и U2, гидродесульфирования, в предприятие по получению топлива из биологического сырья, включающее блок получения углеводородных фракций из смесей биологического происхождения, содержащих эфиры жирных кислот, посредством их гидродезоксигенирования (ГДО) и изомеризации (ИЗО),в котором каждый из блоков U1 и U2 гидродесульфирования включает:реактор гидродесульфирования, (A1) для блока U1 и (A2) для блока U2, при этом указанный реактор содержит катализатор гидродесульфирования;один или большее количество теплообменников для теплообмена между сырьем и потоком, выходящим из реактора;систему нагревания сырья, расположенную выше реактора по ходу технологического процесса;блок обработки кислого газа, расположенный ниже реактора по ходу технологического процесса и содержащий абсорбент (B) для HS, T1 в блоке U1 и T2 в блоке U2,причем указанный способ включает:установку между блоками U1 и U2 ...

НЕПРЕРЫВНЫЙ СПОСОБ КОНВЕРСИИ ЛИГНИНА В СОЕДИНЕНИЯ, ПОДХОДЯЩИЕ ДЛЯ ПРИМЕНЕНИЯ

... 1. Непрерывный способ конверсии лигнинового сырья, содержащего лигнин, причем указанный способ включает:дезоксигенирование лигнина до совокупности продуктов конверсии лигнина в реакторе для конверсии лигнина, содержащем содержимое реактора, содержащее жидкую композицию, содержащую по меньшей мере одно соединение, являющееся жидкостью при 1 бар и 25°C; и при этом одновременное непрерывное выведение по меньшей мере части совокупности продуктов конверсии лигнина из реактора;где конверсию лигнина проводят путем приведения лигнина в контакт с водородом и первым катализатором; иконверсию лигнина проводят при температуре конверсии лигнина и давлении конверсии лигнина, где температура конверсии лигнина находится в интервале выше температуры кипения указанной жидкой композиции при атмосферном давлении и ниже критической температуры жидкой композиции, а давление конверсии лигнина выше давления в пузырьке указанной жидкой композиции при температуре конверсии лигнина, при этом давление конверсии лигнина ...

ВЫСОКООКТАНОВЫЙ НЕЭТИЛИРОВАННЫЙ АВИАЦИОННЫЙ БЕНЗИН

... 1. Композиция неэтилированного авиационного топлива, имеющая МОЧ по меньшей мере 99,6, содержание серы меньше, чем 0,05 мас. %, содержание CHN по меньшей мере 98 мас. %, содержание кислорода меньше, чем 2 мас. %, уточненную теплоту сгорания по меньшей мере 43,5 МДж/кг, давление насыщенного пара в диапазоне от 38 до 49 кПа, включающая смесь, содержащую:от 35 об. % до 55 об. % толуола, имеющего МОЧ по меньшей мере 107;от 2 об. % до 10 об. % анилина;от 15 об. % до 30 об. % по меньшей мере одного алкилата или смеси алкилатов, имеющей температуру начала кипения в диапазоне от 32°С до 60°С и температуру конца кипения в диапазоне от 105°С до 140°С, имеющей точку выкипания Т40 меньше, чем 99°С, Т50 меньше, чем 100°С, Т90 меньше, чем 110°С, причем алкилат или смесь алкилатов содержит изопарафины, имеющие от 4 до 9 атомов углерода, 3-20 об. % С5 изопарафинов, 3-15 об. % С7 изопарафинов и 60-90 об. % С8 изопарафинов, в расчете на алкилат или смесь алкилатов, и меньше, чем 1 об. % углеводородов С10 ...

СУДОВОЕ ДИСТИЛЛЯТНОЕ НИЗКОСЕРНИСТОЕ ТОПЛИВО

Изобретение раскрывает судовое дистиллятное низкосернистое топливо, содержащее нефтяную фракцию, характеризующееся тем, что оно содержит керосино-газойлевую фракцию малосернистой нефти, выкипающую в пределах 150-300°С из малосернистой нефти с содержанием серы 0,25-0,5% масс., или керосино-газойлевую фракцию малосернистой нефти, выкипающую в пределах 150-380°С из малосернистой нефти с содержанием серы 0-0,25% масс., при этом температура вспышки обеих фракций составляет 63°С, 64°С, 67°С. Технический результат заключается в получении судового топлива с содержанием серы не более 0,1%, что соответствует требованиям показателей качества на судовое дистиллятное топливо марок DMX; DMA; DMZ; DMB международного и национального стандарта ISO 8217:2010. 1 табл., 3 пр.

ДИЗЕЛЬНОЕ ТОПЛИВО УНИФИЦИРОВАННОЕ ВСЕСЕЗОННОЕ

Изобретение раскрывает дизельное топливо унифицированное всесезонное на основе среднедистиллятных нефтяных фракций, содержащее в качестве базового компонента изодепарафинизированную дизельную фракцию, выкипающую в интервале 174-334°С, и противоизносную присадку в количестве 0,015-0,020 мас.%, добавленную на базовый компонент. Технический результат: применение данного топлива приведет к значительному снижению затрат при его производстве, транспортировании, хранении и эксплуатации техники, в том числе судовой, с возможностью его использования на всей территории Российской Федерации. 4 табл.

ОБРАБОТКА ПОСРЕДСТВОМ ГИДРООЧИСТКИ И ДЕПАРАФИНИЗАЦИИ ДЛЯ УЛУЧШЕНИЯ ТЕМПЕРАТУРЫ ЗАМЕРЗАНИЯ ТОПЛИВА ДЛЯ РЕАКТИВНЫХ ДВИГАТЕЛЕЙ

... 1. Способ получения топлива для реактивных двигателей из сырья керосиновой фракции, включающий: ! - гидроочистку сырья керосиновой фракции в присутствии катализатора гидроочистки в условиях гидроочистки с получением гидроочищенного сырья керосиновой фракции; ! - депарафинизацию гидроочищенного сырья керосиновой фракции в присутствии катализатора, включающего молекулярное сито 1-D с десятичленными кольцами, в условиях депарафинизации с получением гидродепарафинизированного сырья керосиновой фракции и ! - фракционирование гидродепарафинизированного сырья керосиновой фракции с получением топлива для реактивных двигателей. ! 2. Способ по п.1, в котором сырье керосиновой фракции имеет интервал температур кипения от 149 до 343°С. ! 3. Способ по п.1, в котором условия гидроочистки включают температуру от 280 до 400°С, давление от 1480 до 20786 кПа (от 200 до 3000 фунтов/кв. дюйм), часовую объемную скорость жидкости от 0,1 до 10 ч-1 и расход газообразного водорода для обработки от 89 до 1780 м3 ...

ПРИМЕНЕНИЕ ПОЛИАЛКИЛЕНГЛИКОЛЯ В КАЧЕСТВЕ ПРИСАДКИ ДЛЯ ТОПЛИВА

Способ сжигани в паровой фазе и соединени дл реализации указанного способа II

... 1. Состав топлива, включающий: 1) улучшающее сгорание количество C1-C12 спиртов, причем указанное соединение или смесь соединений имеет скрытую теплоту парообразования не менее 21 кДж/моль при средней температуре кипения, и 2) улучшающее сгорание количество по меньшей мере одного не содержащего свинца металла или элемента, включая соединения, являющиеся его органическими и неорганическими производными, выбранного из группы, состоящей из Be, F, Si, P, S, Cl, Ca, Sc, Ti, V, Cr, Co, Ni, Cu, Zn, Ga, Ge, As, Se, Br, Rb, Sr, Y, Zr, Nb, Mo, Tc, Ru, Rh, Pd, Ag, Cd, In, Sn, Sb, Те, J, Cs, Ba, Hf, Та, W, Re, Os, Ir, Pt, Au, Hg, Tl, Bi, Po, At, Fr, Ra, Ac, Th, Pa, U, Np, Pu, Am, Cm, Bk, Cf, Es, Fm, Md, No, Lr, Unq, Unp, Unh, Uns элементов Периодической системы элементов и их смесей, при этом указанный состав характеризуется тем, что имеет скорость ламинарного Бунзеновского пламени не менее 40 см/с. 2. Состав топлива, включающий: 1) улучшающее сгорание количество С1-C2 спиртов или их смесей и 2) улучшающее ...

СПОСОБ ПОЛУЧЕНИЯ ТОПЛИВА И УСТРОЙСТВО ДЛЯ ЕГО ОСУЩЕСТВЛЕНИЯ

... 1. Способ получения нефтяного топлива, в котором осуществляют смешение и проведение химической реакции воды, содержащей фермент, с углеводородным нефтепродуктом, причем воду, содержащую фермент, получают путем перемешивания в воде природного растительного фермента, содержащего, по меньшей мере, липазу. ! 2. Способ получения топлива по п.1, в котором природный растительный фермент дополнительно содержит целлюлозу. ! 3. Способ производства топлива по п.1, в котором вода, содержащая фермент, дополнительно содержит перемешанный с ней метанол. ! 4. Способ производства топлива по п.2, в котором вода, содержащая фермент, дополнительно содержит перемешанный с ней метанол. ! 5. Способ производства топлива по любому из пп.1-4, в котором для смешения и проведения химической реакции воды, содержащей фермент, с углеводородным нефтепродуктом, их пропускают при вихревом движении через конический смесительный аппарат, содержащий множество установленных в нем штырей. ! 6. Способ производства топлива по ...

УДАЛЕНИЕ СЕРОВОДОРОДА В ВИДЕ СУЛЬФАТА АММОНИЯ ИЗ ПАРОВ ПРОДУКТА ГИДРОПИРОЛИЗА

... 1. Способ переработки биомассы на углеводородное топливо, включающий:переработку биомассы в реакторе гидропиролиза, дающую углеводородное топливо, уголь и поток технологического пара;охлаждение потока технологического пара до температуры конденсации;разделение потока технологического пара на первичный поток охлажденного парообразного продукта, поток жидких углеводородов и первичный водный поток:где первичный поток охлажденного парообразного продукта включает неконденсирующиеся технологические пары, H, сероводород, CO и CO, поток жидких углеводородов включает конденсирующиеся углеводороды, и первичный водный поток включает воду, аммиак, сероводород и сульфид аммония;обработку первичного водного потока в колонне для отпарки кислых вод;концентрирование сероводорода и аммиака в поток охлажденной технологической воды и второй поток очищенной воды;направление потока охлажденной технологической воды в каталитический реактор;впрыск воздуха в каталитический реактор с получением концентрированного ...

ПРОЦЕСС И УСТРОЙСТВО ДЛЯ ПРОИЗВОДСТВА ТОПЛИВНОГО УГЛЕВОДОРОДНОГО МАСЛА

СПОСОБ ПОЛУЧЕНИЯ БИОРАЗЛАГАЕМЫХ УГЛЕВОДОРОДНЫХ ЖИДКОСТЕЙ

УДАЛЕНИЕ СЕРОВОДОРОДА В ВИДЕ СУЛЬФАТА АММОНИЯ ИЗ ПАРОВ ПРОДУКТА ГИДРОПИРОЛИЗА

ГИДРООБРАБОТКА ПРОДУКТОВ ТЕРМИЧЕСКОГО КРЕКИНГА

Способ уменьшения выбросов серы в порту

ПОЛУЧЕНИЕ ЖИРНЫХ СПИРТОВ С ПОМОЩЬЮ ОБРАЗУЮЩИХ ЖИРНЫЕ СПИРТЫ АЦИЛ-КОА-РЕДУКТАЗ (FАR)

... 1. Способ получения композиции жирных спиртов, включающий в себя:a) культивирование рекомбинантного микроорганизма в подходящей культуральной среде, где рекомбинантный микроорганизм содержит ген, кодирующий гетерологичный фермент редуктазу жирных ацилов (FAR), обладающий по меньшей мере 75% идентичностью последовательности (по меньшей мере 80%, по меньшей мере 85%, по меньшей мере 90% и по меньшей мере 95% идентичностью последовательности) с SEQ ID NO: 2, SEQ ID NO: 6, SEQ ID NO: 14, или их функциональными фрагментами, иb) обеспечение экспрессии указанного гена, где указанная экспрессия приводит к получению композиции жирных спиртов.2. Способ по п.1, где фермент FAR обладает по меньшей мере 85% идентичностью последовательности (по меньшей мере 90% и по меньшей мере 95% идентичностью последовательности) с SEQ ID NO: 2 или ее функциональными фрагментами.3. Способ по п.1, где фермент FAR содержит последовательность из SEQ ID NO: 2, SEQ ID NO: 6, SEQ ID NO: 14 или их функциональные фрагменты ...

НЕ ТРЕБУЮЩИЙ ФРАКЦИОНИРОВАНИЯ СПОСОБ ПОЛУЧЕНИЯ НИЗКОКИПЯЩЕГО ТОПЛИВА ИЗ СЫРОЙ НЕФТИ ИЛИ ЕЕ ФРАКЦИЙ

... 1. Способ получения жидкого топлива из газа, содержащего, по меньшей мере, примерно 50 об.% метана, указанный способ включает:(a) приведение в контакт указанного газа с (i) жидкими исходными материалами, состоящими из сырой нефти или жидкой нефтяной фракции, и (ii) с сеткой из металлического катализатора, как указанные жидкие исходные материалы, так и указанная сетка из металлического катализатора содержатся в реакционной емкости при температуре примерно 80°C или выше, но ниже температуры кипения указанной сырой нефти, указанная сетка из металлического катализатора содержит витки переходного металла, закрепленные на железной раме;(b) извлечение газообразного продукта реакции, сформированного в указанной реакционной емкости; и(c) конденсирование указанного газообразного продукта реакции до указанного жидкого топлива.2. Способ по п.1, где указанный газ содержит, по меньшей мере, примерно 70 об.% метана.3. Способ по п.1, где указанный газ содержит, по меньшей мере, примерно 85 об.% метана.4 ...

КОМПОЗИЦИИ ЖИДКОГО ТОПЛИВА НА ОСНОВЕ КАТАЛИТИЧЕСКИ ДЕОКСИГЕНИРОВАННЫХ И КОНДЕНСИРОВАННЫХ ОКСИГЕНИРОВАННЫХ УГЛЕВОДОВ

... 1. Композиция жидкого топлива, содержащая фракцию перегонки компонента, содержащего, по меньшей мере, одно С4+ соединение, произведенное из растворимого в воде оксигенированного углеводорода, и полученного по способу, включающему: ! подачу воды и растворимого в воде оксигенированного углеводорода, содержащего C1+O1+ углеводород, в водной жидкой фазе и/или паровой фазе; ! подачу Н2; ! проведение каталитической реакции в жидкой и/или паровой фазе между оксигенированным углеводородом и Н2 в присутствии катализатора деоксигенирования при температуре деоксигенирования и давлении деоксигенирования для получения оксигената, содержащего в реакционном потоке C1+O1-3 углеводород; и ! проведение каталитической реакции в жидкой и/или паровой фазе для оксигената в присутствии катализатора конденсации при температуре конденсации и давлении конденсации для получения С4+ соединения, ! где С4+ соединение включает представителя, выбираемого из группы, состоящей из С4+ спирта, С4+ кетона, С4+ алкана, С4+ ...

СПОСОБ И КАТАЛИЗАТОР ГИДРОПЕРЕРАБОТКИ

... 1. Способ производства углеводородного топлива из возобновляемого органического материала биологического происхождения, предусматривающий стадии: ! (a) формирования исходного сырья путем комбинирования ископаемого углеводородного топлива с возобновляемым органическим материалом, где содержание возобновляемого органического материала составляет от 1 до 35 об.%; ! (b) смешивания исходного сырья из стадии (а) с обогащенным водородом газом и проведения объединенного потока на стадию гидродезоксигенирования путем контакта указанного объединенного потока с катализатором гидродезоксигенирования, ! где катализатор гидродезоксигенирования представляет собой нанесенный Мо катализатор, имеющий содержание Мо от 0,1 до 20 мас.%, причем носитель выбран из оксида алюминия, диоксида кремния, диоксида титана и их комбинаций, и указанный носитель имеет бимодальную пористую структуру с порами с диаметром более 50 нм, которые составляют по меньшей мере 2 об.% общего объема пор. ! 2. Способ по п.1, где обогащенный ...

СПОСОБ И УСТРОЙСТВО ДЛЯ ПОЛУЧЕНИЯ УГЛЕВОДОРОДНОГО ТОПЛИВА И КОМПОЗИЦИИ

... 1. Способ получения углеводородного топлива, который включает в себя:- суспензионный гидрокрекинг тяжелого сырья с получением продуктов суспензионного гидрокрекинга;- разделение указанных продуктов суспензионного гидрокрекинга с получением потока пека и потока тяжелого ВГО;- смешивание, по меньшей мере, части пекового потока с растворителем для того, чтобы растворить часть пека в растворителе; и- смешивание растворенной части пека, по меньшей мере, с частью потока тяжелого ВГО с образованием смешанного продукта.2. Способ по п.1, который дополнительно включает выделение растворенной части пека из растворителя до указанной стадии смешивания.3. Способ по п.1, в котором суспензионный гидрокрекинг указанного тяжелого сырья включает в себя превращение пека, по меньшей мере, на 85 масс.%.4. Способ по п.1, в котором указанный растворитель имеет плотность не больше, чем плотность гептана.5. Устройство для получения углеводородного топлива, которое включает:- реактор суспензионного гидрокрекинга ...

СПОСОБЫ ПРОИЗВОДСТВА БИОТОПЛИВА

... 1. Способ производства биотоплива, причем способ включает:обработку органического вещества водным растворителем и по меньшей мере одним дополнительным катализатором, который выбран из группы, состоящей из: катализатора на основе формиата щелочного металла; катализатора на основе карбоната щелочного металла; катализатора на основе переходного металла; катализатора на основе соли переходного металла; катализатора на основе формиата переходного металла; катализатора на основе соли щелочного металла; катализатора на основе соли щелочноземельного металла; кислотного катализатора; твердокислотного катализатора; катализатора конверсии водяного пара; катализатора на основе цеолита или алюмосиликата; катализатора на основе переходного металла на подложке; сульфидного катализатора; и основного катализатора, который представляет собой соль щелочного металла или соль переходного металла; при температуре между примерно 250°С и примерно 400°С и под давлением между примерно 100 бар и примерно 300 бар, ...

ПРОИЗВОДСТВО ХИМИЧЕСКИХ ВЕЩЕСТВ И ТОПЛИВ ИЗ БИОМАССЫ

... 1. Способ преобразования биомассы в полученные из биомассы топлива и химические вещества, включающий:обеспечение потока подачи биомассы, содержащего растворитель и компонент биомассы, содержащий целлюлозу, гемицеллюлозу или лигнин;осуществление каталитической реакции потока подачи биомассы с водородом и катализатором разложения при температуре разложения и давлении разложения для получения потока продукта, содержащего паровую фазу, жидкую фазу и твердую фазу, причем паровая фаза содержит один или несколько легкоиспаряющихся оксигенатов СО, жидкая фаза содержит воду и один или несколько оксигенированных углеводородов СО, а твердая фаза содержит экстрактивы;отделение легкоиспаряющихся оксигенатов СОот жидкой фазы и твердой фазы; иосуществление каталитической реакции легкоиспаряющихся оксигенатов СОв присутствии катализатора конденсации при температуре конденсации и давлении конденсации для получения соединения С, содержащего элемент, выбранный из группы, состоящей из спирта С, кетона С, алкана ...

СПОСОБ ПОЛУЧЕНИЯ И ИСПОЛЬЗОВАНИЯ УГЛЕВОДОРОДНОГО ТОПЛИВА

... 1. Способ получения и использования углеводородного топлива, включающий либо добычу COиз дымового газа объекта, сжигающего покупное углеводородное топливо, либо COсо стороны, либо добычу СОиз воздуха, либо одновременное или частичное использование всех трех указанных источников СО, и включающий добычу Низ воды способом ее электролиза с использованием электроэнергии ВЭУ, с последующим соединением СОи Н, реакция которых дает углеводородное топливо, отличающийся тем, что ВЭУ выполняют с ветротурбиной (ветротурбинами), имеющей вертикальную ось вращения, и эта ВЭУ функционирует в единой технологической схеме на общей производственной площадке с объектом, сжигающим углеводородное топливо, а комплексная технология прототипа получения углеводородного топлива осуществляется внутри строительного объема опорной башни ВЭУ.2. Способ по п.1, отличающийся тем, что объект, сжигающий углеводородное топливо, размещают и он функционирует внутри строительного объема опорной башни ВЭУ.

СПОСОБ ПОЛУЧЕНИЯ НЕОЧИЩЕННОГО ПРОДУКТА

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

Verfahren zum Herstellen von Produkten mit wenig Wasserstoffhalogenid

Verfahren zum Herstellen von Produkten mit wenig Wasserstoffhalogenid, umfassend: a) Strippen oder Destillieren eines Ausflusses aus einem Reaktor in eine erste Fraktion mit einer Menge eines Wasserstoffhalogenids, und eine zweite Fraktion mit einer reduzierten Menge des Wasserstoffhalogenids; wobei der Reaktor Folgendes umfasst: einen ionischen Flüssigkatalysator mit einem Metallhalogenid, und ein Wasserstoffhalogenid oder ein organisches Halogenid; und b) Gewinnen von einem oder mehreren Produktströmen aus der zweiten Fraktion mit weniger als 25 Gew.-ppm des Wasserstoffhalogenids. In einer Ausführungsform weist der ionische Flüssigkatalysator Metallhalogenid auf; und die Gewinnung gewinnt Propan, n-Butan und Alkylatbenzin mit weniger als 25 Gew.-ppm Wasserstoffhalogenid. In einer anderen Ausführungsform benutzt das Gewinnen eine Destillierkolonne mit schlechter Korrosionsbeständigkeit gegenüber dem Wasserstoffhalogenid, wobei die Destillierkolonne keine Korrosion zeigt. Außerdem wird ...

Verfahren zur katalytischen Druckhydrierung von an mehrkernigen aromatenreichen Produkten

KEROSINZUSAMMENSETZUNG

High octane unleaded aviation gasoline

High octane unleaded aviation gasoline (AVGAS) having a MON at least 99.6, a low aromatics content and a T10 of at most 75°C, T40 of at least 75° C, a T50 of at most 105°C, a T90 of at most 135°C, a final boiling point of less than 210°C, an adjusted heat of combustion of at least 43.5 MJ/kg, a vapor pressure in the range of 38 to 49 lcPa and a freezing point of less than -58 °C is provided. The composition comprises toluene, toluidine, at least one alkylate or alkylate blend, a diethyl carbonate and isopentane in certain proportions, and less than 1 vol % of C8 aromatics.

Alternative fuel for internal combustion engine, containing biobutanol

COAL-TAR MIXTURES

Production of fuels, particularly jet and diesel fuels, and constituents thereof

A first aspect of the invention is concerned with fuels and particularly jet and diesel fuels which comprise blends of substituted mono cyclohexane material and two ring non-fused cyloalkane material. The first material may be n-propylcyclohexane or n-butylcyclohexane. The second material may be nuclear substituted bicyclohexyl and may include cyclohexylbenzene. A second aspect of the invention concerns producing constituents for the fuel from heavy aromatic materials by breaking down the heavy aromatics to naphthas, separating light napthas and other constituents of the fuel before reforming a heavy naptha fraction to provide a BTX fraction which may be treated by hydroalkylation or pyrolysis to provide two ring non-fused cycloalkanes. The product may be enriched by hydrogenation.

Process for the preparation of and composition of a feedstock usable for the preparation of lower olefins

Lignocellulose conversion processes and products

Anti-foam fuel composition

This invention relates to a fuel composition comprising a base fuel having a final boiling point above 150{C and an anti-foam, characterised in that the anti-foam comprises di-isobutylene in an amount greater than 2.5 % by volume based on the total fuel composition. The addition of this anti-foam reduces the break-up time for any foam formed significantly.

Synthetic aviation fuel

The invention relates to a Fischer Tropsch derived aviation fuel, which fuel is used either as a fuel on its own or as a component in an aviation fuel blend, said fuel having an iso: n paraffins mass ratio above 3, at least 0.1 mass % naphthenes, <0.01 mass % polyaromatics, and <0.5 mass % aromatics.

Fully synthetic jet fuel

Synthetic Fuel

Low sulphur diesel fuel and aviation turbine fuel

Improved method for manufacturing heating oil

A mineral heating oil composition, boiling within the range 300-750 DEG F., having little tendency to deposit carbon when burnt and also useful as a diesel fuel, is prepared by contacting a virgin heating oil with hydrogen in the presence of a hydrogenation catalyst, under temperature and pressure conditions such that the consumption of hydrogen is not more than 60 cubic feet per barrel, and blending the product with a heating oil obtained in a cracking operation. A process is described in which crude petroleum is fractionated by distillation to yield a virgin heating oil fraction, a gas oil fraction and other fractions. The virgin heating oil fraction is partially desulphurized by hydrofining with the above-mentioned hydrogen consumption, for example at 400-700 DEG F. and 50-250 lbs./sq. in. pressure using a cobalt molybdate or molybdenum oxide catalyst supported on a carrier such as alumina. The hydrofined fraction may be steam stripped or washed with caustic alkali to remove traces of ...

Production of jet and motor fuel

Jet and motor fuels are obtained from a hydrocarbon fraction having an end point of 240-320 DEG C. and containing predominantly C4-C12 saturated hydrocarbons by separating n-paraffins for use as jet fuel by means of a selective sorbent for n-paraffins and subjecting the raffinate of iso- and cyclo-paraffins to catalytic reforming in the presence of hydrogen at below 455 DEG C. to obtain motor fuel. Separation is effected with activated carbon or alumina, urea (solid or in solution) or preferably a 5 <\>rA molecular sieve. Reforming is preferably effected at 345-455 DEG C. and 34-204 atmospheres.

Improved Jet and Rocket Fuel

... 1,182,610. Exo-tetrahydrodicyclopentadiene compounds and their use as fuels. ESSO RESEARCH & ENG. CO. 28 July, 1967 [15 Aug., 1966], No. 34858/67. Headings C5E and C5G. Fuels for jet or rocket engines comprise exotetrahydrodicyclopentadiene, its mono- or dimethyl derivative or any mixture thereof. They may be stabilized by phenolic or amine antioxidants. Exo-tetrahydrodicyclopentadiene may be obtained by any of the following methods, similar methods also applying for the mono- and dimethyl derivatives: (1) treatment of endo-tetrahydrodicyclopentadiene with a mineral or Lewis acid; (2) treatment of endo-dicyclopentadiene with a protonating agent, e.g. sulphuric acid, to form exo - hydroxy - exo - dihydrodicyclopentadiene, hydrogenating this to the exo-hydroxy-tetrahydro compound, and then dehydrating this and hydrogenating the dehydrated compounds; (3) hydrogenating endo-dicyclopentadiene to the dihydro-derivative, thermally treating this to convert it to the exo-isomer, and then completing ...

Stable, moderately unsaturated distillate fuel blend stocks prepared by low pressure hydroprocessing of Fischer-Tropch products

Desulphurisation of heavy fuel oil

The sulphur content of a high sulphur oil residue is reduced in a process which comprises in a first stage splitting up the residue (A) into a high asphalt and ash phase (C) and a low asphalt and ash phase (B) by vacuum distillation or by solvent extraction with a hydrocarbon, for example propane, butane, or pentane, and thereafter hydrodesulphurizing phase (B) at 140 atmospheres or above, and preferably 300-450 DEG C. to yield a desulphurized heavy fuel oil phase (E). Phase (E) may be mixed with phase (A) and/or phase (C) to produce a low-sulphur heavy fuel oil (F) of desired quality. Part of phase (C) may be used for the production of bitumen or industrial gas. By-products, especially light fractions, may be separated from phase (E). Specification 834,292 is referred to.

An emergency fuel

Method for producing a fuel using renewable hydrogen

There is provided a method of producing fuel having renewable content, the method comprising: providing renewable hydrogen for a hydroprocessing unit; hydrogenating crude oil derived liquid hydrocarbon in the hydroprocessing unit; and determining the renewable content of crude oil derived liquid hydrocarbon hydrogenated in the hydroprocessing unit, the renewable content dependent on the renewable hydrogen provided, wherein determining the renewable content comprises: a) measuring an amount of hydrogen, carbon, or a combination thereof in crude oil derived liquid hydrocarbon fed to the hydroprocessing unit; and b) measuring an amount of hydrogen, carbon, or a combination thereof in crude oil derived liquid hydrocarbon produced by the hydroprocessing unit, wherein determining the renewable content comprises using a difference between: (i) a relative amount of carbon and hydrogen in the crude oil derived liquid hydrocarbon fed to the hydroprocessing unit determined using at least one measured ...

Converting biomass to jet-fuel

The invention relates to a process and system for forming a hydrocarbon feedstock from a biomass material, and the hydrocarbon feedstock formed therefrom. The invention also relates to a process and system for forming a bio‐derived jet fuel from a hydrocarbon feedstock, and the bio‐derived jet fuel formed therefrom, as well as intermediate treated hydrocarbon feedstocks formed during the process. The process comprises the following: A. providing a biomass derived hydrocarbon feedstock comprising certain percentages of C8 compounds, C10 compounds, C12 compounds, C16 compounds and C18 compounds, B. processing this feedstock to produce a refined bio-oil, wherein the process comprises i. at least partially removing sulphur containing components from the hydrocarbon feedstock, ii. hydro-treating and iii. hydro-isomerising the hydrocarbon feedstock, and C. fractionating the resulting refined bio-oil to obtain a bio-derived jet fuel fraction.

Processes for producing high biogenic concentration Fischer-Tropsch liquids derived from municipal solid wastes (MSW) feedstocks

Fuels and fuel additives that have high biogenic content derived from renewable organic feedstock

Method for producing a fuel using renewable hydrogen

Method for joint production of low octane number gasoline and high octane number gasoline

Method of refining and producing fuel from naturaloil feedstocks.

Heavy synthetic fuel

Method for joint production of low octane number gasoline and high octane number gasoline

Novel fuel composition

Vapor phase combustion method and compositions II.

Method reduced temperature metallic vapor phase combustion for jet, turbine, diesel, fuel oil, and gasoline combustion system. More particularly, it relates to methods and composition of metal containing fuels comprised of enhanced combusition structure capable of increasing combustion burning velocity and reducing combustion temperature.

METHODS OF REFINING AND PRODUCING FUEL FROM NATURAL OIL FEEDSTOCKS

PROCESSING BIOMASS

Heavy synthetic fuel

PROCESSING BIOMASS

A hydrocarbon condensate stabilizer and a method for producing a stabilized hydrocarbon condenstate stream

Method of refining and producing fuel from naturaloil feedstocks.

Processing biomass

Kerosene base material production method and kerosene base material

Method of preparation of gasoline with high octane number.

Method of refining and producing fuel from naturaloil feedstocks.

PROCESSING BIOMASS

A hydrocarbon condensate stabilizer and a method for producing a stabilized hydrocarbon condenstate stream

Novel fuel composition

Kerosene base material production method and kerosene base material

Processing biomass

Methods for deoxygenating biomass-derived pyrolysis oils

Methods for deoxygenating treated biomass-derived pyrolysis oil are provided. The treated biomass-derived pyrolysis oil is exposed to a catalyst having a neutral catalyst support such as a non-alumina metal oxide support, a theta alumina support, or both. The non-alumina metal oxide support may be a titanium oxide (TiO 2 ) support, a silicon oxide support, a zirconia oxide (ZrO 2 ) support, a niobium oxide (Nb 2 O 5 ) support, or a support having a mixture of non-alumina metal oxides. The catalyst may include a noble metal or a Group VIII non-noble metal and a Group VIB non-noble metal on the neutral catalyst support. The treated biomass-derived pyrolysis oil is introduced into a hydroprocessing reactor in the presence of the catalyst under hydroprocessing conditions to produce low oxygen biomass-derived pyrolysis oil.

Dimethyl ether fuel compositions and uses thereof

The present invention provides useful fuel compositions which may be produced substantially from renewable resources, such as biomass, to provide green fuel compositions, methods, and systems. In some embodiments, fuel compositions include dimethyl ether and one or more C 2 or larger alcohol, such as ethanol, 1-propanol, 2-propanol, 1-butanol, 2-butanol, isobutanol, or tert-butanol. In some embodiments, fuel compositions include dimethyl ether and one or more C 2 or larger hydrocarbons, such as propane, propylene, propyne, and propadiene, n-butane, isobutane, isobutylene, 1-butene, 2-butene, or 1,3-butadiene. Methods of making these novel DME-based fuel compositions, particularly from biomass-derived syngas, are described. Various applications and methods of using the fuel compositions, such as portable cylinder fuels for camping, are disclosed. Additionally, principles of burner design for these fuel compositions are disclosed herein.

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.

Methods for producing fuels and solvents

Described herein are methods for producing fuels and solvents from fatty acid resources. Also disclosed herein are fuels and solvents produced by the methods described herein.

Method of making a catalyst

Presented are one or more aspects and/or one or more embodiments of catalysts, methods of preparation of catalyst, methods of deoxygenation, and methods of fuel production.

Methods of deoxygenation and systems for fuel production

Presented are one or more aspects and/or one or more embodiments of catalysts, methods of preparation of catalyst, methods of deoxygenation, and methods of fuel production.

Composition of matter comprising of the creation of a low molecular weight hydrocarbon fluid exhibiting oligomerized pentenes mainly comprised of 2-Methyl-2-Butene subunits as well as related plant isoprenoids composed of 2-Methyl-1-Butene subunits and other hydrocarbons from hydrocarbon-bearing woody biomass and a process for the extraction and refinement in making the same composition through the creation of solvent permeable woody biomass particles and a multi-phase solvent extraction

A composition of matter with of the creation of a low molecular weight hydrocarbon fluid called Wood Phytoleum from woody Pinaceae and Myrtaceae biomass and a process for the extraction and refinement in making the same composition of matter through the reduction of the particle size of the raw woody biomass to form a solvent permeable particle and a phased multi-wash solvent system of extraction and refinement. A preferred embodiment includes the steps of the reduction of the particle size of the raw woody biomass to form a solvent permeable particle by shearing and chipping, the application of a phased multi-wash solvent system to the solvent permeable particle utilizing a non-polar solvent together with a bridge solvent soluble in both the non-polar solvent and in water, the application of a final bridge solvent wash to the solvent permeable particle, a mechanism for washing the particles of the woody biomass within the multi-wash solvent system, a mechanism for the collection of the solvent and Wood Phytoleum solution from the multi-wash solvent system, the extraction of the solvent from the solvent saturated particles of the woody biomass and the discharge for continued use of the woody biomass, and a process and mechanism for the extraction, collection and refinement of the solvent and Wood Phytoleum solution to discharge the solvents for reuse and to collect the Wood Phytoleum liquid oil including Pinene A and Pinene B and other oligomerized pentenes.

Composition of matter comprising of the creation of a low molecular weight hydrocarbon fluid exhibiting mainly oligomerized pentenes mainly comprised of 2-Methyl-2-Butene subunits as well as related plant isoprenoids composed of 2-Methyl-1-Butene subunits and other hydrocarbons from Euphorbia tirucalli biomass and a process for the extraction and refinement in making the same composition through the creation of solvent permeable batting mat and a multi-phase solvent extraction

A composition of matter with of the creation of low molecular weight hydrocarbon fluid called Phytoleum from Euphorbia tirucalli biomass and a process for the extraction and refinement in making the same composition through the creation of a batting mat and multi-phase solvent extraction. A preferred embodiment includes the steps of manufacturing a fibrous batting mat from the raw biomass, crushing the biomass, shearing the biomass with a rotating knives blade array, compressing the biomass by passing the biomass through press rollers, amalgonating the biomass into a Batting Mat, subjecting the Batting Mat to a phased multi-wash solvent system, extracting the solvents and oils liquid solution for recovery, subjecting the liquid solution to a centrifugation system to extract the Phytoleum hydrocarbon oil from the other components, and refining the final product to yield Phytoleum which is a composition of matter including Tirucallene A and Tirucallene B and other oligomerized pentenes.

Method and systems for making distillate fuels from biomass

The present invention provides methods, reactor systems and catalysts for converting biomass and biomass-derived feedstocks to C 8+ hydrocarbons using heterogenous catalysts. The product stream may be separated and further processed for use in chemical applications, or as a neat fuel or a blending component in jet fuel and diesel fuel, or as heavy oils for lubricant and/or fuel oil applications.

Method for producing aviation fuel oil base and aviation fuel oil composition

A method for producing an aviation fuel oil base includes obtaining a first generated oil by hydrotreating a feedstock by bringing a feedstock which includes an oxygen-containing hydrocarbon compound derived from an animal or vegetable oils and fat into contact with a first dual functional catalyst which has dehydrogenation and hydrogenation functions and which includes a metal of group 6A of the periodic table, a metal of group 8, and an amorphous solid acidic substance, in the presence of hydrogen; and obtaining a second generated oil including an aviation fuel oil base by hydroisomerizing the first generated oil by bringing the first generated oil into contact with a second dual functional catalyst which has dehydrogenation and hydrogenation functions and which includes a metal of the group 8 of the periodic table and a crystalline solid acidic substance, in the presence of hydrogen.

Methods for producing fuels and solvents substantially free of fatty acids

Described herein are methods for producing fuels and solvents from fatty acid re-extraction sources. In general, the pyrolysis products of fatty acids are extracted in order to remove residual fatty acids and produce very pure hydrocarbon compositions composed of alkanes and alkenes. The fatty acids removed from the extraction step can be further pyrolyzed to produce additional hydrocarbons or, in the alternative, the fatty acids can be isolated and used in other applications. Also disclosed herein are fuels and solvents produced by the methods described herein.

Catalytic dechlorination processes to upgrade feedstock containing chloride as fuels

Processes for the catalytic dechlorination of one or more hydrocarbon products involve contacting a mixture comprising the hydrocarbon product(s) and a carrier gas with a dechlorination catalyst under catalytic dechlorination conditions to provide a dechlorinated hydrocarbon product, HCl, and the carrier gas. The dechlorinated hydrocarbon product may be separated from the HCl and the carrier gas to provide liquid fuel or lubricating base oil.

Production of chemicals and fuels from biomass

The present invention provides methods, reactor systems, and catalysts for converting in a continuous process biomass to fuels and chemicals. The invention includes methods of converting the water insoluble components of biomass, such as hemicellulose, cellulose and lignin, to volatile C 2+ O 1-2 oxygenates, such as alcohols, ketones, cyclic ethers, esters, carboxylic acids, aldehydes, and mixtures thereof. In certain applications, the volatile C 2+ O 1-2 oxygenates can be collected and used as a final chemical product, or used in downstream processes to produce liquid fuels, chemicals and other products.

Production of fatty alcohols with fatty alcohol forming acyl-coa reductases (far)

The disclosure relates to methods of producing fatty alcohols from recombinant host cells comprising genes encoding heterologous fatty acyl-CoA reductase (FAR) enzymes. The disclosure further relates to FAR enzymes and functional fragments thereof derived from marine bacterium and particularly marine gamma proteobacterium such as Marinobacter and Oceanobacter ; polynucleotides encoding the FAR enzymes and vectors and host cells comprising the same.

PROCESS AND APPARATUS FOR PRODUCING HYDROCARBONS FROM FEED-STOCKS COMPRISING TALL OIL AND TERPENE-COMPOUNDS

The invention relates to a process for producing hydrocarbon components, comprising: providing a feedstock comprising tall oil and terpene-based compounds; subjecting the feedstock and a hydrogen gas feed to a hydroprocessing treatment in the presence of a hydroprocessing catalyst to produce hydrocarbon components including n-paraffins, and subjecting the hydrocarbon components including n-paraffins to isomerisation in the presence of a dewaxing catalyst to form a mixture of hydrocarbon components. The invention also relates to an apparatus for implementing the process. The invention further relates to a use of the hydrocarbon components produced by the process as a fuel or as an additive in fuel compositions. The invention also relates to a use of a NiW catalyst on a support selected from AlO, zeolite, zeolite-AlO, and AlO—SiOfor producing fuel or an additive for fuel compositions from a feedstock comprising tall oil and terpene-based compounds. 123-. (canceled)24. A process for producing hydrocarbon components , comprising:providing a feedstock comprising tall oil and terpene-based compounds;{'sub': 3', '2', '3, 'subjecting the feedstock and a hydrogen gas feed to a hydroprocessing treatment in the presence of a NiO/MoOcatalyst on an AlOsupport to produce hydrocarbon components including n-paraffins, and'}{'sub': 2', '3, 'subjecting the hydrocarbon components including n-paraffins to isomerisation in the presence of a NiW catalyst on a zeolite-AlOsupport and in the presence of hydrogen to form a mixture of hydrocarbon components.'}25. The process according to wherein the terpene-based compounds are obtained from plants claim 24 , terpene oils claim 24 , distillation bottoms from terpene distillation and flavorants and/or fragrance industry.26. The process of wherein the feedstock comprises crude tall oil and crude sulphate turpentine derived from kraft pulping of wood.27. The process of wherein the crude tall oil is purified prior to subjecting it to the ...

Raw petroleum coke composition for anode material for lithium ion secondary battery

Provided is a raw petroleum coke composition as a raw material of an anode carbon material that can improve, when a battery is discharged at a high current, the ratio capable of maintaining the capacity obtained during discharge at a low current. More specifically, provided is a raw petroleum coke composition for an anode carbon material of a lithium ion secondary battery, the raw petroleum coke composition being produced by subjecting a heavy-oil composition to a delayed coking process, and comprising an atomic ratio of hydrogen atoms H to carbon atoms C(H/C atomic ratio) of 0.30 to 0.50, and a micro-strength of 7 to 17% by weight. Further provided are a method for producing an anode carbon material of a lithium ion secondary battery, comprising the steps of: pulverizing the raw petroleum coke composition into particles having an average particle diameter of 5 to 30 μm, and subjecting the particles to carbonization and/or graphitization; and a lithium ion secondary battery comprising an anode comprising such a carbon material.

Fuel compositions containing an isomerized component of a single carbon number and methods of preparing the fuel compositions

Fuel compositions containing an isomerized component of a single carbon number may contain at least 97 wt. %, based on the total weight of the fuel composition, of an isomerized component consisting of aliphatic paraffin isomers all having the formula C n H 2n+2 , where 10≦n≦22 and n has the same value for each aliphatic paraffin isomer in the isomerized component. The fuel compositions have a normal alkane content of less than 10 wt. %, based on the total weight of the fuel composition. Methods for preparing the fuel compositions include hydroisomerizing a normal alkane starting material to form an isomerized mixture and subsequently removing remnant normal alkanes from the isomerized mixture by solvent dewaxing and/or distillation. Some of the fuel compositions may have freezing points at or below −47° C., making them amenable for use a surrogate fuels in the place of JP-8.

FUEL COMPOSITION

Unleaded blend composition having a Motor Octane Number (MON) of at least 80 having less than 42% of aromatic compounds, and at least 2% by volume of the total composition of component (a′), which is a substantially aliphatic hydrocarbon refinery stream of MON value of at least 85. At least 70% in total of the stream is branched chain alkanes, the stream being obtained by distillation from a refinery material as a cut having Initial Boiling Point of at least 15° C. and Final Boiling Point of at most 160° C. The Boiling Points are measured according to ASTMID2892. At least 5% of at least one paraffin, aromatic hydrocarbon compound or olefinic hydrocarbon has a bp 60-160° C., with not more than 5% of the total composition of hydrocarbon having a bp more than 160° C. Less than 5% 2,2,3-trimethylbutane or 2,2,3-trimethylpentane is present. 1142-. (canceled)143. An unleaded blend composition having a Motor Octane Number (MON) of at least 80 comprising less than 42% of aromatic compounds , and at least 2% (by volume of the total composition) of component (a′) , which is a substantially aliphatic hydrocarbon refinery stream of MON value of at least 85 , at least 70% in total of said stream being branched chain alkanes , said stream being obtained by distillation from a refinery material as a-cut having Initial Boiling Point of at least 15° C. and Final Boiling Point of at most 160° C. , said Boiling Points being measured according to ASTMID2892 , and at least 5% of at least one paraffin , aromatic hydrocarbon compound or olefinic hydrocarbon of b.p. 60-160° C. , with not more than 5% of the total composition of hydrocarbon of bp more than 160° C. , and less than 5% 2 ,2 ,3-trimethylbutane or 2 ,2 ,3-trimethylpentane.144. An unleaded blend composition having a Motor Octane Number (MON) of at least 80 comprising less than 42% of aromatic compounds at least 5% (by volume of the total composition) of component (a′) , which is at least one branched chain alkane of MON value of ...

CATALYST COMPOSITIONS FOR CONVERSION OF VEGETABLE OILS TO HYDROCARBON PRODUCTS IN THE DIESEL BOILING RANGE AND PROCESS OF PREPARATION THEREOF

The present invention relates to a catalyst composition for conversion of vegetable oils to hydrocarbon products in the diesel boiling range, comprising a porous support; Group III A or VA element in the range of 1-10 wt %; Group VI B elements in the range of 1 to 20 wt %; Group VIII B elements in range of 0.01 to 10 wt %. The present invention further provides the process for preparing the catalyst composition for conversion of vegetable oils to hydrocarbon products in the diesel boiling range. The present invention also provides the process for conversion of vegetable oils to hydrocarbon products in the diesel boiling range using the catalyst composition or discarded refinery spent hydro-treating catalyst. 1. A catalyst composition for conversion of vegetable oils to hydrocarbon products in the diesel boiling range comprising:(i) a porous support 85-95 wt %(ii) Group III A or VA elements in the range of about 1 to 10 wt %(iii) Group VI B elements in the range of about 1 to 20 wt %(iv) Group VIII B elements in range of about 0.01 to 10 wt %.2. The catalyst composition as claimed in claim 1 , wherein said porous support comprises at least 25% of aluminium oxide.3. The catalyst composition as claimed in claim 2 , wherein said porous support has unimodel pore size distribution in the range of about 20 to 250 Å; surface area in the range of about 200-250 m/g; bulk density in the range of about 0.80 to 0.85 g/cc; and pore volume in the range of about 0.5 to 0.8 cc/g.4. The catalyst composition as claimed in claim 1 , wherein said Group IIIA element is Boron in the range of about 1 to 10 wt % preferably about 1 to 5 wt %.5. The catalyst composition as claimed in claim 1 , wherein said Group VA element is Phosphorus about 1 to 10 wt % preferably 1 to 5 wt %.6. The catalyst composition as claimed in claim 1 , wherein said Group VIB element is Molybdenum in the range of about 10 to 15 wt % claim 1 , more preferably in the range of about 12 to 14 wt % or Tungsten preferably ...

DIESEL ENGINE INJECTOR FOULING IMPROVEMENTS WITH A HIGHLY PARAFFINIC DISTILLATE FUEL

The invention provides the use of a highly paraffinic distillate fuel in a diesel fuel composition for reducing the formation of injector nozzle deposits when combusted in a diesel engine having a high pressure fuel injection system, wherein the distillate fuel has an aromatics content less than 0.1 wt %, a sulphur content less than 10 ppm and a paraffinic content of at least 70 wt %, such that the diesel fuel composition has a relative fouling behaviour of 70% or less and a density of more than 0.815 g.cm(at 15° C.). 1. A highly paraffinic distillate fuel for use in a diesel fuel composition for reducing the formation of injector nozzle deposits when combusted in a diesel engine having a high pressure fuel injection system , wherein the highly paraffinic distillate fuel has an aromatics content less than 0.1 wt % , a sulphur content less than 10 ppm and a paraffinic content of at least 70 wt % , such that the diesel fuel composition has a relative fouling behaviour of 70% or less and a density of more than 0.815 g.cm(at 15° C.).2. The highly paraffinic distillate fuel of claim 1 , wherein the diesel fuel composition has a relative fouling behaviour of 60% or less.3. The highly paraffinic distillate fuel of claim 1 , wherein the diesel fuel composition has a relative fouling behaviour of 50% or less and a density of more than 0.79 g.cm(at 15° C.).4. The highly paraffinic distillate fuel of claim 1 , wherein the highly paraffinic distillate fuel is derived from a Fischer Tropsch process claim 1 , a hydrogenated renewable oil claim 1 , or a combination thereof.5. The highly paraffinic distillate fuel of claim 1 , wherein the highly paraffinic distillate fuel has a cetane number greater than 70.6. The highly paraffinic distillate fuel of claim 1 , wherein the diesel fuel composition comprises a petroleum-derived distillate fuel claim 1 , a bio-derived fuel claim 1 , or a combination thereof.7. The highly paraffinic distillate fuel of claim 1 , wherein the diesel fuel ...

System and process for biomass conversion to renewable fuels with byproducts recycled to gasifier

This invention relates generally to a method and system for improving the conversion of carbon-containing feed stocks to renewable fuels, and more particularly to a thermal chemical conversion of biomass to renewable fuels and other useful chemical compounds, including gasoline and diesel, via a unique combination of unique processes. More particularly, this combination of processes includes (a) a selective pyrolysis of biomass, which produces volatile hydrocarbons and a biochar; (b) the volatile hydrocarbons are upgraded in a novel catalytic process to renewable fuels, (c) the biochar is gasified at low pressure with recycled residual gases from the catalytic process to produce synthesis gas, (d) the synthesis gas is converted to dimethyl ether in a novel catalytic process, and (e) the dimethyl ether is recycled to the selective pyrolysis process.

CATALYTIC HYDROGENATION OF HYDROXYCYCLOALKANES AND USE OF THE PRODUCT IN BIOFUEL COMPOSITIONS FOR AVIATION

This invention relates to a new biofuel alternative to be used in aviation sector, starting from obtention and production routes of renewable sources compounds, that may act as load for aviation kerosene composition. Naphthenic compounds (cycloalkanes) obtained from renewable sources are used as enrichment or addition loads of aviation kerosene. The process is based on hydrogenolysis catalytic reactions, from hydroxycycloalkanes derevatives substrata, like menthol and isopulegol. The catalytic system is constituted of a physical mixture of hydrogenation heterogeneous catalysts, acid heterogeneous catalysts, and hydrogenating metallic catalysts in acid supports. The hydrogenation catalysts used envolve noble metals from groups 6, 7, 8, 9 and 10 of periodic table, whose content ranges from 0.01-10%. The heterogeneous catalysts suitable acids are represented by acidic sulfonated polymer resins, protonated zeolites and sulfated zirconia. The catalytic reaction conditions involving a temperature range of 70-250° C., pressure between 1-70 and agitation ranging from 100-1000 rpm. The composition involving the biofuel, obtained by catalytic hydrogenation process, is obtained as a mixture composed by cycloalkanes and aviation fuel in ratio 1:100 to 100:1, in volume. 1. A biomass hydrogenolysis catalytic process comprising:a catalytic hydrogenation reaction of hydroxycycloalkanes derivatives to obtain biofuel for aviation, biokerosene composed mainly by cycloalkanes.2. The process according to claim 1 , wherein the catalytic system includes mixtures of hydrogenation heterogeneous catalysts and acid heterogeneous catalysts claim 1 , or bifunctional catalysts constituted of acid support and active phase by hydrogenating metal.3. The process according to claim 2 , wherein the mass ratio of hydrogenation heterogeneous catalyst:acid heterogeneous catalyst comprises 5:1 to 1:5 range claim 2 , more preferably the range between 2:1 and 1:2.4. The process according to claim 2 , ...

EVEN CARBON NUMBER PARAFFIN COMPOSITION AND METHOD OF MANUFACTURING SAME

Paraffin compositions including mainly even carbon number paraffins, and a method for manufacturing the same, is disclosed herein. In one embodiment, the method involves contacting naturally occurring fatty acid/glycerides with hydrogen in a slurry bubble column reactor containing bimetallic catalysts with equivalent particle diameters from about 10 to about 400 micron. The even carbon number compositions are particularly useful as phase change material. 1. A composition comprising C-Cparaffins , wherein:the paraffins are produced from a renewable biological feedstock by a process comprising hydrogenation and hydrogenolysis; andthe paraffins are predominately even carbon number paraffins.2. The composition of claim 1 , wherein the even carbon number paraffins comprise n-hexadecane and n-octadecane.3. The composition of claim 1 , wherein the even carbon number paraffins comprise n-dodecane and n-tetradecane.4. The composition of claim 1 , wherein at least 75 wt % of the paraffins are even carbon number paraffins.5. The composition of claim 1 , wherein at least 80 wt % of the paraffins are even carbon number paraffins.6. The composition of claim 1 , wherein the renewable biological feedstock is selected from the group consisting of vegetable oils claim 1 , plant oils claim 1 , algal oils claim 1 , animal fats claim 1 , tall oil fatty acid claim 1 , products of the food industry claim 1 , and a combination of any two or more thereof.7. The composition of claim 1 , wherein the renewable biological feedstock is selected from the groups consisting of soybean oil claim 1 , corn oil claim 1 , cottonseed oil claim 1 , canola oil claim 1 , coconut oil claim 1 , sunflower oil claim 1 , palm oil claim 1 , palm kernel oil claim 1 , rapeseed oil claim 1 , and a combination of any two or more thereof.8. The composition of claim 1 , wherein the renewable biological feedstock is selected from the group consisting of soybean oil claim 1 , canola oil claim 1 , palm oil claim 1 , palm ...

RENEWABLE JET FUEL DERIVED FROM BIOMASS

A single pass direct conversion of biomass derived oxygenates to longer chain hydrocarbons is described. The longer chain hydrocarbons include higher naphthene content which is quite useful in the distillate range fuels or more particularly, the jet and diesel range fuels. Naphthenes help the biomass derived hydrocarbons meet product specifications for jet and diesel while really helping cold flow properties. 1. A renewable jet fuel derived at least in part from biomass comprising:approximately 0 to 10 wt % n-paraffins,approximately 5 to 20 wt % iso-paraffins,approximately 15% to 95 wt % naphthenes,approximately 5 to 50 wt % 1-ring naphthenes,approximately 0 to 50 wt % 2-ring naphthenes,approximately 0 to 10 wt % 3-ring naphthenes, andapproximately 0 to 25 wt % aromatics.2. A renewable jet fuel according to comprising at least 25 weight percent naphthenes.3. A renewable jet fuel according to comprising at least 45 weight percent naphthenes.4. A renewable jet fuel according to comprising at least 70 weight percent naphthenes.5. A renewable jet fuel according to comprising up to a maximum of 90 weight percent naphthenes.6. The renewable jet fuel according to having a freeze point of less than −40 degrees Fahrenheit.7. The renewable jet fuel according to having a flashpoint greater than 100 degrees Fahrenheit.8. The renewable jet fuel according to wherein at least 95% of the jet fuel is derived from biomass.9. The renewable jet fuel according to wherein at least 90% of the jet fuel is derived from biomass.10. The renewable jet fuel according to wherein the jet fuel is a drop in jet fuel that meets all specifications for Jet A and JP-8. This application is a non-provisional application which claims benefit under 35 USC §119(e) to U.S. Provisional Application Ser. No. 61/567,287 filed Dec. 6, 2011, entitled “Direct Conversion of Biomass Oxygenates to Distillate-Range Hydrocarbons,” which is incorporated herein in its entirety. This application is also a non-provisional ...

RENEWABLE DIESEL FUEL DERIVED FROM BIOMASS

A single pass direct conversion of biomass derived oxygenates to longer chain hydrocarbons is described. The longer chain hydrocarbons include higher naphthene content which is quite useful in the distillate range fuels or more particularly, the jet and diesel range fuels. Naphthenes help the biomass derived hydrocarbons meet product specifications for jet and diesel while really helping cold flow properties. 1. A renewable diesel fuel derived at least in part from biomass comprising:approximately 0 to 10 wt % n-paraffins,approximately 5 to 20 wt % iso-paraffins,approximately 15% to 95 wt % naphthenes,approximately 5 to 50 wt % 1-ring naphthenes,approximately 5 to 50 wt % 2-ring naphthenes,approximately 0 to 15 wt % 3-ring naphthenes, andapproximately 0 to 25 wt % aromatics.2. A renewable diesel fuel according to comprising at least 25 weight percent naphthenes.3. A renewable diesel fuel according to comprising at least 45 weight percent naphthenes.4. A renewable diesel fuel according to comprising at least 70 weight percent naphthenes.5. A renewable diesel fuel according to comprising up to a maximum of 92 weight percent naphthenes.6. The renewable diesel fuel according to having a cloud point of less than −20 degrees Fahrenheit and a pour point of less than −20 degrees Fahrenheit.7. The renewable diesel fuel according to having a flashpoint greater than 125 degrees F.8. The renewable diesel fuel according to having a cetane rating of at least 40.9. The renewable diesel fuel according to wherein at least 95% of the diesel fuel is derived from biomass.10. The renewable diesel fuel according to wherein at least 90% of the diesel fuel is derived from biomass.11. The renewable diesel fuel according to wherein the jet fuel is a drop in diesel fuel that meets all specifications for Number 2 Diesel. This application is a non-provisional application which claims benefit under 35 USC §119(e) to U.S. Provisional Application Ser. No. 61/567,287 filed Dec. 6, 2011, entitled “ ...

Renewable gas oil derived from biomass

A single pass direct conversion of biomass derived oxygenates to longer chain hydrocarbons is described. The longer chain hydrocarbons include higher naphthene content which is quite useful in the distillate range fuels or more particularly, the jet and diesel range fuels. Naphthenes help the biomass derived hydrocarbons meet product specifications for jet and diesel while really helping cold flow properties.

Processing of Dielectric Fluids with Mobile Charge Carriers

Provided herewith is a novel method of controllably processing a dielectric fluid by creating discharges within the dielectric fluid from mobile charge carriers contained within the dielectric fluid. Generally, the dielectric fluid and the mobile charge carriers are between two electrodes which apply a voltage to the charge carriers. In one embodiment, the dielectric fluid is a hydrocarbon fluid such as a heavy crude oil or a fuel. In one embodiment the charge carrier comprises water droplets. In another embodiment, the mobile charge carriers are metallic balls. In both instances the discharges initiate from the mobile charge carriers.

PROCESSES FOR PRODUCING HYDROCARBON PRODUCTS

The present invention relates to processes for producing industrial products such as hydrocarbon products from non-polar lipids in a vegetative plant part. Preferred industrial products include alkyl esters which may be blended with petroleum based fuels. 2. The process of claim 1 , wherein the step of physically processing the vegetative plant part comprises one or more of rolling claim 1 , pressing claim 1 , crushing or grinding the vegetative plant part.3. The process of claim 1 , which prior to step ii) further comprises the steps of:(a) extracting at least some of the non-polar lipid content from the vegetative plant part as non-polar lipid, and(b) recovering the extracted non-polar lipid.4. The process of claim 3 , wherein(i) the extracted non-polar lipid comprises triacylglycerols, wherein the triacylglycerols comprise at least 90% (w/w) of the extracted non-polar lipid, and/or(ii) the extracted non-polar lipid comprises free sterols, steroyl esters, steroyl glycosides, waxes or wax esters, or any combination thereof.5. The process of claim 3 , wherein step (a) uses an organic solvent.6. The process of which comprises one or more ofa) recovering the extracted non-polar lipid by collecting it in a container,b) one or more of degumming, deodorising, decolourising, drying or fractionating the extracted non-polar lipid,c) removing at least some waxes and/or wax esters from the extracted non-polar lipid, andd) analysing the fatty acid composition of the extracted non-polar lipid.7. The process of in which the volume of the extracted non-polar lipid is at least 1 litre.8. The process of claim 1 , wherein the industrial product is a hydrocarbon product such as fatty acid esters claim 1 , preferably fatty acid methyl esters and/or a fatty acid ethyl esters claim 1 , an alkane such as methane claim 1 , ethane or a longer-chain alkane claim 1 , a mixture of longer chain alkanes claim 1 , an alkene claim 1 , a biofuel claim 1 , carbon monoxide and/or hydrogen gas claim ...

Methods and Systems for the Production of Hydrocarbon Products

Methods and systems for the production of hydrocarbon products, including providing a substrate comprising CO to a bioreactor containing a culture of one or more micro-organisms; and fermenting the culture in the bioreactor to produce one or more hydrocarbon products. The substrate comprising CO is derived from an industrial process selected from the group comprising steam reforming processes, refinery processes, steam cracking processes, and reverse water gas shift processes.

Methods for making and distributing batches of butane-enriched gasoline

Disclosed are automated methods and systems for certifying the volatility of butane-enriched gasoline downstream of a butane blending operation. Such automated methods and systems provide significant advantages to comply with volatility requirements imposed by EPA or state regulations.

EXPANSION OF FUEL STREAMS USING MIXED HYDROCARBONS

Methods and systems for blending multiple batches of mixed hydrocarbons into fuel streams downstream of the refinery are provided that do not compromise the octane value of the fuel and do not cause the volatility of the fuel to exceed volatilities imposed by government regulation. 2) A method for making mixed pentane enriched fuel without depressing the octane of the fuel , comprising the steps: i) a first enclosed conduit transmitting a fuel stream,', 'ii) a second enclosed conduit transmitting an additive stream, wherein the additive stream comprises mixed pentanes, and', 'i) an outlet in the second enclosed conduit forming a fluid connection with an inlet in the first enclosed conduit,, 'a) providing a fuel blending unit characterized by i) a volatility for the additive stream (the “additive stream volatility”),', 'ii) a flow rate for the fuel stream (the “fuel stream flow rate”),', 'iii) an octane value for the fuel stream (the “fuel stream octane value”), and, 'b) providingiv) a maximum blended volatility for the fuel stream (the “maximum blended volatility”),c) measuring the fuel stream for its actual volatility (the “fuel stream volatility”), i) the fuel stream volatility,', 'ii) the additive stream volatility, and', 'iii) the fuel stream flow rate,, 'd) calculating a rate (the “additive stream flow rate”) at which the additive stream can be added to the fuel stream so as not to exceed the maximum blended volatility, wherein the calculating is based upone) adding the additive stream to the fuel stream at the additive stream flow rate at the fluid connection to make pentane enriched fuel, andf) adding ethanol to the pentane enriched fuel in an amount sufficient to overcome the depression in octane caused by n-pentane in the mixed pentanes.3) A method for blending heterogeneous batches of mixtures of light hydrocarbons into a primary fuel stream (the “fuel stream”) comprising: i) a mixed hydrocarbon stream (the “additive stream”) comprising a plurality of ...

HIGH PERFORMANCE LIQUID ROCKET PROPELLANT

Disclosed is a high performance hydrocarbon fuel characterized by a hydrogen content greater than 14.3% by weight, a hydrogen to carbon atomic ratio greater than 2.0 and/or a heat of combustion greater than 18.7 KBtu/lb. The disclosed fuels generally have a paraffin content that is at least 90% by mass and a C-Cisoparaffin content of at least 40% by mass. 1. A hydrocarbon fuel having a range of components that provide a boiling point range of at least 100° F. , and having a hydrogen content greater than 14.3% on a mass basis.2. A hydrocarbon fuel having a range of components that provide a boiling point range of at least 100° F. , and having a hydrogen to carbon ratio greater than 2.0 on an atomic basis.3. The hydrocarbon fuel of having a net heat of combustion greater than 18.7 KBtu/lb.4. A hydrocarbon fuel in accordance with which is a blend of an isoparaffin and a highly paraffinic kerosene.5. The hydrocarbon fuel of claim 4 , in which the isoparaffin is comprised of at least one isododecane claim 4 , at least one isohexadecane claim 4 , at least one isoeicosane claim 4 , or a mixture of these.6. A hydrocarbon fuel in accordance with which is a blend of an isoparaffin and a naphthenic kerosene.7. The hydrocarbon fuel of claim 6 , in which the isoparaffin is comprised of at least one isododecane claim 6 , at least one isohexadecane claim 6 , at least one isoeicosane claim 6 , or a mixture of these.8. (canceled)9. (canceled)10. A fuel composition comprising:a total paraffin content of at least 90% by mass; andwherein the composition contains at least 40% by mass of isoparaffins having from 12 to 20 carbon atoms.11. The composition of claim 10 , in which a net heat of combustion is greater than 18 claim 10 ,700 BTU/lb.12. The composition of claim 10 , in which the hydrogen content is greater than 14.5% by mass.13. The composition of wherein the total paraffin content is at least 95% by mass.14. The composition of wherein the composition contains at least 60% by mass ...

FUEL COMPOSITION

A fuel composition for use in an internal combustion engine comprising at least one liquid fuel and at least one gaseous fuel, the gaseous fuel having an effective solubility in the liquid fuel at twenty degrees Celsius and one atmosphere in the range of 0.0000001 g/kg to 0.0002 g/kg, wherein dispersion of the gaseous fuel within the liquid fuel before introduction of the fuel composition to the injection system of the engine is such that molecules of the liquid and gaseous fuels are substantially equidistant one from another, liquid from liquid and gas from gas, within a variance preferably of no more than one hundred percent (±100%), more preferably of no more than fifty percent (±50%), and most preferably of no more than twenty-five percent (±25%), whereby the fuel composition is substantially homogeneous so as to promote the atomization of the liquid fuel and thus improve combustion. 1. An internal combustion engine fuel composition comprising:at least one liquid fuel; andat least one gaseous fuel, the gaseous fuel having an effective solubility in the liquid fuel at twenty degrees Celsius and one atmosphere in the range of 0.0000001 g/kg to 0.0002 g/kg, wherein dispersion of the gaseous fuel within the liquid fuel before introduction of the fuel composition to an internal combustion engine is such that molecules of the liquid and gaseous fuels are substantially equidistant one from another, liquid from liquid and gas from gas, within a variance of no more than one hundred percent (±100%),whereby the fuel composition is substantially homogeneous before being introduced to the internal combustion engine such that upon injection the rapid expansion of the gaseous fuel dispersed within the liquid fuel promotes the atomization of the liquid fuel and thus improves combustion, andwherein the time between mixture of the gaseous fuel into the liquid fuel to form the fuel composition and introduction of the fuel composition into the internal combustion engine is at least ...

Processing biomass and petroleum containing materials

Biomass (e.g., plant biomass, animal biomass, and municipal waste biomass) is processed to produce useful products, such as fuels. For example, systems can use feedstock materials, such as cellulosic and/or lignocellulosic materials and/or starchy materials, to produce ethanol and/or butanol, e.g., by fermentation.

Methods for converting petroleum based oil into fuel

Methods for converting petroleum based oil into fuel generally include forming a conversion mixture of an alcohol and a base, and adding the conversion mixture to petroleum based oil, such as used motor oil, to form a reaction mixture. The methods can also include adding a high nitrate compound and an amino acid to the reaction mixture and ozonizing the reaction mixture. The result of the methods can include a three phase system in which the bottom phase is asphalt oil, the middle phase is diesel fuel or jet fuel, and the top phase is sulfuric acid. The three phases can be separated to obtain the final diesel fuel or jet fuel product.

Processing Biomass Containing Materials

Biomass (e.g., plant biomass, animal biomass, and municipal waste biomass) is processed to produce useful products, such as fuels. For example, systems can use feedstock materials, such as cellulosic and/or lignocellulosic materials and/or starchy materials, to produce ethanol and/or butanol, e.g., by fermentation.

LIQUID FUEL

A liquid fuel formed by the mixture of toluene, meta-xylene and n-hexane, in proportions of between 50 and 70% of toluene, between 10 and 20% of meta-xylene and between 20 and 30% of n-hexane. 1. A liquid fuel , wherein it is obtained by blending only three basic components , which are toluene , meta-xylene , and n-hexane.2. The liquid fuel claim 1 , in full accordance with claim 1 , wherein the volume percentages of the three components are: toluene 50-70% claim 1 , meta-xylene 10-20% claim 1 , and n-hexane 20-30% by volume.3. The liquid fuel claim 1 , in full accordance with claim 1 , wherein the volume percentages of the three components are: toluene 60% claim 1 , meta-xylene 10% claim 1 , and n-hexane 30% by volume.4. The liquid fuel claim 2 , in full accordance with claim 2 , wherein the volume percentages of the three components are: toluene 60% claim 2 , meta-xylene 10% claim 2 , and n-hexane 30% by volume. The present invention relates to a liquid fuel and more particularly to the so-called gasolines used as fuel for internal combustion engines with spark ignition. Gasoline is obtained by mixing light liquid hydrocarbons obtained from crude oil, after various petrochemical processes carried out at a refinery.There is a variety of hydrocarbons grouped into families, among which are the alkanes, which are hydrocarbons having carbon atoms joined by single covalent bonds. Most oil hydrocarbons belong to that family.In general, gasoline is obtained in a refinery from straight run naphtha, which is the lightest liquid fraction from oil (excluding gases). Naphtha is also obtained from the conversion of heavy oil fractions (vacuum gasoil) in process units known as FCC (fluid catalytic cracking) or hydrocracking units. Gasoline is a mixture of hundreds of individual hydrocarbons from C(butanes and butenes) to Csuch as, for example, methylnaphthalene.To this mixture of hundreds of individual hydrocarbons it is necessary to add another series of additives that enable ...

RENEWABLE FUEL COMPOSITION AND METHOD OF USING THE SAME

Disclosed is an alternative fuel composition derived from the conversion of biomass at an elevated temperature, with conversion optionally in the presence of a catalyst, which is capable of reducing, and thereby improving, a low temperature property of a distillate. A process is also disclosed for mixing such renewable composition with the distillate. 1. A distillate fuel comprising: (i) a renewable distillate produced by a Fischer-Tropsch process;', '(ii) a non-renewable distillate produced by a Fischer-Tropsch process; and', '(iii) a renewable component of a hydroprocessed/hydrotreated triglyceride or triglyceride derived fatty acid alkyl ester; and, 'a) an aromatic-lean component selected from the group consisting ofb) an aromatic-rich component comprising an at least partially hydrotreated bio-distillate fraction produced from the conversion of biomass at an elevated temperature wherein the boiling range of the aromatic-lean component and the aromatic-rich component are about the same.2. The distillate fuel of claim 1 , wherein the non-renewable distillate produced by a Fischer-Tropsch process is gasoline claim 1 , jet fuel or diesel fuel.3. The distillate fuel of claim 1 , wherein the amount of aromatic hydrocarbons in the aromatic-rich component is from 30% to about 50%4. The distillate fuel of claim 1 , wherein the amount of aromatic hydrocarbons in the aromatic-lean component is less than 20%.5. The distillate fuel of claim 1 , wherein the amount of aromatic-rich component in the distillate fie; is from about 10% to about 50%.6. The distillate fuel of claim 1 , wherein the aromatic-rich component is prepared by hydrotreating an oil derived by the thermal conversion of biomass over a catalyst.7. The distillate fuel of claim 6 , wherein the catalyst comprises a zeolite.8. The distillate fuel of claim 1 , wherein the aromatic-lean component of (i) is prepared by gasification of a biomass claim 1 , subjecting the resulting syngas product to a Fischer-Tropsch ...

Process for the Production of Hydrocarbons for Fuels, Solvents, and Other Hydrocarbon Products

Catalytic processes for converting carboxylic acids obtained from biomass and other natural or industrial sources into paraffinic or olefinic hydrocarbons through decarboxylation, along with products formed from such hydrocarbons, in which the carbon chain length, the ratio of carbon-14 to carbon-12, and the ratio of odd number to even number of carbons in the chain are among factors which are indicative or otherwise useful for the detection of hydrocarbons formed by undergoing the claimed processes.

RENEWABLE JET FUEL BLENDSTOCK FROM ISOBUTANOL

The present invention in its various embodiments is directed to methods for preparing a renewable jet fuel blendstock, and blendstocks prepared by such methods, comprising fermenting a biomass-derived feedstock to form one or more C—Calcohols such as isobutanol, catalytically dehydrate and oligomerize the alcohols to form higher molecular weight olefins (e.g., C—Colefins), hydrogenating at least a portion of the higher molecular weight olefins to form a renewable jet fuel blendstock comprising Cand Calkanes which meet or exceed the requirements of ASTM D7566-10a for hydroprocessed synthesized paraffinic kerosene (SPK). 1. A process for preparing renewable jet fuel blendstock comprising:(a) treating biomass to form a feedstock;(b) fermenting the feedstock with one or more species of microorganism, thereby forming isobutanol;(c) dehydrating at least a portion of the isobutanol obtained in step (b), thereby forming a dehydration product comprising isobutene;{'sub': 8', '12', '16, '(d) oligomerizing at least a portion of the dehydration product, thereby forming a product comprising one or more C, one or more C, and one or more Cunsaturated oligomers;'}{'sub': '8', '(e) separating at least a portion of said one or more Cunsaturated oligomers produced in step (d);'}(f) combining the separated portion of step (e) with the dehydration product of step (c) prior to said oligomerization step (d):{'sub': 12', '16, '(g) hydrogenating at least a portion of the product of step (d) in the presence of hydrogen, thereby forming a renewable jet fuel blendstock comprising one or more Cand one or more Csaturated alkanes; and'}{'sub': 12', '16, '(h) adjusting the ratio of Cand Csaturated alkanes provided by step (eg) to form a renewable jet fuel blendstock which meets or exceeds the requirements of ASTM D7566-10a for hydroprocessed synthesized paraffinic kerosene (SPK).'}2. The process of claim 1 , wherein said dehydrating is carried out in the presence of a dehydration catalyst claim 1 ...

Renewable Engine Fuel And Method Of Producing Same

The present invention provides high-octane fuel, and a method of producing same. These fuels may be formulated to have a wide range of octane values and energy, and may effectively be used to replace 100 LL aviation fuel (known as AvGas), as well as high-octane, rocket, diesel, turbine engine fuels, as well as two-cycle, spark-ignited engine fuels. 1. A 100 octane aviation fuel comprising: (a) 70-85 wt % of sym-trimethyl benzene (mesitylene); and (b) 15-30 wt % of isopentane , wherein the fuel has a motor octane number of 99.5 or greater , and a Reid vapor pressure of from 5.5 to 7.1 psi.2. A 100 octane aviation fuel consisting essentially of: (a) 70-85 wt % of sym-trimethyl benzene (mesitylene); and (b) 15-30 wt % of isopentane , wherein the fuel has a motor octane number of 99.5 or greater , and a Reid vapor pressure of from 5.5 to 7.1 psi.3. A 100 octane aviation fuel consisting of: (a) 70-85 wt % of sym-trimethyl benzene (mesitylene); and (b) 15-30 wt % of isopentane , wherein the fuel has a motor octane number of 99.5 or greater , and a Reid vapor pressure of from 5.5 to 7.1 psi.4. (canceled)5. A high octane aviation fuel comprising: (a) 60-85 wt % of sym-trimethyl benzene (mesitylene) , and (b) 15-40 wt % of isopentane , wherein the fuel has a motor octane number of 99.5 or greater , and a Reid vapor pressure of from 5.5 to 7.1 psi.611-. (canceled)12. The aviation fuel of claim 5 , wherein the mesitylene is present in an amount of between about 70 to 85 wt %.13. The aviation fuel of claim 5 , wherein the isopentane is present in an amount of between about 15 to 30 wt %.1422-. (canceled)23. A high octane fuel comprising: (a) 70-85 wt % of sym-trimethyl benzene (mesitylene); and (b) 15-30 wt % of isopentane claim 5 , wherein the fuel is an aviation fuel having a motor octane number of 99.5 or greater claim 5 , and a Reid vapor pressure of from 5.5 to 7.1 psi.24. A 100 octane aviation fuel comprising: (a) 70-85 wt % of sym-trimethyl benzene (mesitylene); and (b) ...

C HEAVY OIL COMPOSITION AND METHOD FOR PRODUCING SAME

The present invention provides a method for producing a C heavy oil composition which unlikely forms sludge, has excellent ignitability and combustibility, and enable the stable operation of a combustion device such as an external combustion device, a diesel device, and a gas turbine device. The method of the present invention is comprises method for producing a C heavy oil composition with a bicyclic aromatic hydrocarbon content of 10 percent by volume or more and 45 percent by volume or less, comprising blending a cracked reformed base oil with a total aromatic content of 80 percent by volume or more and a 15° C. density of 0.90 to 1.20 g/cmin an amount of 1 percent by volume or more and 45 percent by volume or less on the basis of the total mass of the composition. 1. A method for producing a C heavy oil composition with a bicyclic aromatic hydrocarbon content of 10 percent by volume or more and 45 percent by volume or less , comprising blending a cracked reformed base oil with a total aromatic content of 80 percent by volume or more and a 15° C. density of 0.90 to 1.20 g/cm3 in an amount of 1 percent by volume or more and 45 percent by volume or less on the basis of the total mass of the composition.2. The method for producing a C heavy oil composition according to claim 1 , wherein the cracked reformed base oil has a 50° C. kinematic viscosity of 0.3 to 10 mm2/s claim 1 , a sulfur content of 8000 mass ppm or less claim 1 , and a nitrogen content of 100 mass ppm or less.3. The method for producing a C heavy oil composition according to claim 1 , wherein the cracked reformed base oil has a 10 vol. % distillation temperature (T10) of 130 to 270° C. claim 1 , a 50 vol. % distillation temperature (T50) of 190 to 290° C. claim 1 , and a 90 vol. % distillation temperature (T90) of 230 to 390° C.4. The method for producing a C heavy oil composition according to claim 1 , wherein the cracked reformed base oil is produced by bringing a feedstock having a 10 vol. % ...

CHARACTERIZATION OF PRE-REFINED CRUDE DISTILLATE FRACTIONS

Methods are provided for qualifying jet fuel fractions that are derived at least in part from pre-refined crude oil sources. The methods allow for determination of the stability of a jet fuel product over time by using an accelerated aging test. The methods are beneficial for verifying the stability of a jet fuel fraction that includes a portion derived from a pre-refined crude oil. 1. A method for preparing a jet fuel or kerosene product , comprising:determining a breakpoint for a first sample of a distillate fraction, the distillate fraction having an initial boiling point of at least about 284° F. (140° C.) and a final boiling point of about 572° F. (300° C.) or less, at least a portion of the distillate fraction being derived from a first pre-refined crude oil;maintaining a second sample of the distillate fraction at a temperature of at least about 40° C. for an aging period;determining a breakpoint for the aged second sample of the distillate fraction, the breakpoint for the aged second sample being at least about 265° C.; andpreparing a jet fuel product comprising a kerosene portion derived from a second pre-refined crude oil, the second pre-refined crude oil being derived from the same source as the first pre-refined crude oil, a volume percentage of the kerosene portion derived from the second pre-refined crude in the jet fuel product being about 110% or less of a volume percentage corresponding to the portion of the distillate fraction derived from the first pre-refined crude oil, the initial boiling point of the jet fuel product being at least about the initial boiling point of the distillate fraction, and the final boiling point of the jet fuel product being less than or equal to the final boiling point of the distillate fraction.2. The method of claim 1 , further comprising:obtaining a portion of the distillate fraction; andsplitting the portion of the distillate fraction to form at least the first sample and the second sample.3. The method of claim 1 , ...

Even carbon number paraffin composition and method of manufacturing same

Paraffin compositions including mainly even carbon number paraffins, and a method for manufacturing the same, is disclosed herein. In one embodiment, the method involves contacting naturally occurring fatty acid/glycerides with hydrogen in a slurry bubble column reactor containing bimetallic catalysts with equivalent particle diameters from about 10 to about 400 micron. The even carbon number compositions are particularly useful as phase change material.

Generating cellulosic-renewable identification numbers in a refinery

The present application generally relates to methods of generating cellulosic-renewable identification numbers by thermally processing a cellulosic biomass to form a renewable fuel oil, and then co-processing the renewable fuel oil with a petroleum fraction in a refinery to form a cellulosic-renewable identification number-compliant fuel.

System and process for converting plastics to petroleum products

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

Processes for recovering valuable components from a catalytic fast pyrolysis process

Methods of separating products from the catalytic fast pyrolysis of biomass are described. In a preferred method, a portion of the products from a pyrolysis reactor are recovered and separated using a quench system and solvent contacting system that employs materials produced in the pyrolysis process.

Processes for converting biomass to btx with low sulfur, nitrogen and olefin content via a catalytic fast pyrolysis process

Methods of separating and purifying products from the catalytic fast pyrolysis of biomass are described. In a preferred method, a portion of the products from a pyrolysis reactor are recovered and purified using a hydrotreating step that reduces the content of sulfur, nitrogen, and oxygen components, and hydrogenates olefins to produce aromatic products that meet commercial quality specifications.

Process of Making Biochar From Beneficiated Organic-Carbon-Containing Feedstock

A process for making a biochar composition by passing renewable organic-carbon-containing feedstock through a beneficiation sub-system to reduce water content followed by introducing beneficiated feedstock into an oxygen-deficient thermal sub-system to result in renewable processed biochar having an energy density of at least 17 MMBTU/ton (20 GJ/MT) a water content of less than 10 wt %, and water-soluble salt that is decreased by at least 60 wt % on a dry basis from that of the unprocessed organic-carbon-containing feedstock. 1. A process of making processed biochar comprising:passing renewable unprocessed organic-carbon-containing feedstock that includes free water, intercellular water, intracellular water, intracellular water-soluble salts, and at least some plant cells comprising cell walls that include lignin, hemicellulose, and microfibrils within fibrils through a beneficiation sub-system to produce processed organic-carbon-containing feedstock having a water content of less than 20 wt % and a salt content that is reduced by at least 60 wt % on a dry basis from that of the unprocessed organic-carbon-containing feedstock; andpassing the processed organic-carbon-containing feedstock an oxygen-deprived thermal sub-system process to produce processed biochar having an energy density of at least 17 MMBTU/ton (20 GJ/MT) a water content of less than 10 wt %, and water-soluble salt that is decreased by at least 60 wt % on a dry basis from that of the unprocessed organic-carbon-containing feedstock.2. The process of claim 1 , wherein the beneficiation sub-system process comprises:exposing the unprocessed feedstock to hot solvent under pressure for a time at conditions specific to the feedstock to make some regions of the cell walls comprising crystallized cellulosic fibrils, lignin, and hemicellulose more able to be penetrable by water-soluble salts without dissolving more than 25 percent of the lignin and hemicellulose;removing the pressure so as to penetrate the more ...

Production Processes, Systems, Methods, and Apparatuses

The present disclosure provides production processes that can include exposing a carbon-based material to liquid media to form hydrocarbon fuel. Waste to fuel conversion processes as well as waste material processing reactors are provided that can be configured to convert waste to fuel. Heat exchangers, power generation processes and combustion turbine exhaust apparatus are also provided. Fuel generation processes and generation systems are provided. Reaction media conduit systems as well as processes for servicing reactant media pumps coupled to both inlet and outlet conduits containing reactant media, are also provided. 110-. (canceled)11. A fuel generation system comprising:a reactor configured to house a liquid reaction media and receive solid carbon based material;a distillation apparatus coupled to the reactor and configured to receive gaseous hydrocarbon fuel from the reactor; anda combustion turbine coupled to the distillation apparatus and configured to receive distillate portions from the distillation apparatus.12. The system of further comprising a conveyor apparatus associated with reactor claim 11 , the conveyor apparatus configured to convey material to a receiving portion of the apparatus.13. The system of further comprising a heat exchanger coupled to the reactor claim 11 , the heat exchanger configured to heat the liquid reaction media by providing heat from a heat exchanger fluid.14. The system of wherein the heat exchanger is coupled to the combustion turbine.15. The system of wherein at least a portion of the heat exchanger fluid of the heat exchanger circulates within an exhaust apparatus of the combustion turbine.16. The system of wherein the reactor comprises a media circulating conduit configured to circulate the liquid reaction media.17. The system of wherein conduit comprises a fluid pump claim 16 , the conduit further configured to have the fluid pump removed from the conduit while maintaining substantially all the fluid within the conduit ...

AVIATION FUEL COMPOSITION

The present invention relates to an aviation fuel composition comprising an aviation range fuel component and a diesel range fuel component originating from renewable sources, the diesel range fuel component having a cloud point of at most about −20° C. and existent gum more than about 7 mg/100 ml, wherein existent gum of the aviation fuel composition is at most about 7 mg/100 ml. 1. An aviation fuel composition comprising:a) an aviation range fuel component; andb) a diesel range fuel component of renewable origin, having a cloud point of at most about −20° C., and existent gum more than about 7 mg/100 ml, wherein existent gum of the aviation fuel composition is at most about 7 mg/100 ml.2. The aviation fuel composition of claim 1 , wherein component a) is selected from petroleum-based aviation range fuel claim 1 , aviation range fuel of renewable origin claim 1 , and a mixture thereof.3. The aviation fuel composition of claim 1 , wherein component a) complies with at least one of aviation fuel standards selected from ASTM D1655 claim 1 , ASTM D7566 and DEFSTAN 91-91.4. The aviation fuel composition of claim 1 , wherein component b) is paraffinic diesel produced from Fischer-Tropsch synthesis products or at least one of hydrogenated fatty acid and triglyceride materials.5. The aviation fuel composition of claim 4 , wherein the paraffinic diesel is an isomerized paraffinic diesel.6. The aviation fuel composition of claim 1 , wherein component b) comprises:aromatic compounds in an amount of at most about 0.5 vol-%, iso-paraffins in an amount from about 80 vol-% to about 95 vol-%, the rest being n-paraffins.7. The aviation fuel composition of claim 1 , wherein existent gum of component b) is at most about 15000 mg/ml.8. The aviation fuel composition of claim 1 , wherein the composition comprises:a petroleum-based diesel range fuel.9. The aviation fuel composition of claim 1 , wherein the composition comprises up to about 20 vol-% of component b).10. The aviation fuel ...

Fluidized catalytic cracking apparatus

The present application generally relates to a fluidized catalytic cracking apparatus having one or more ports for injecting a renewable fuel oil for co-processing the renewable fuel oil and a petroleum fraction.

ONLINE ANALYZER FOR BIOFUEL PRODUCTION

Disclose is an online analyzer to monitor conversion of a biofeedstock in a first hydrotreating stage to avoid catalyst poisoning in a subsequent stage. An example method of processing a biofeedstock may comprise hydrotreating the biofeedstock by reaction with hydrogen to form a hydrotreated biofeedstock. The method may further comprise monitoring conversion of the biofeedstock in the hydrotreating with an online analyzer. 1. A method of processing a biofeedstock , comprising:hydrotreating the biofeedstock by reaction with hydrogen to form a hydrotreated biofeedstock;monitoring conversion of the biofeedstock in the hydrotreating with an online analyzer; andcontrolling recycle of the hydrotreated biofeedstock to the hydrotreating in response to the monitoring conversation of the biofeedstock.2. The method of claim 1 , wherein the biofeedstock comprises at one component selected from the group consisting of a vegetable oil claim 1 , an animal fat claim 1 , a fish oil claim 1 , a pyrolysis oil claim 1 , algae lipid claim 1 , an algae oil claim 1 , and combinations thereof.3. The method of claim 1 , wherein the biofeedstock comprises lipid compounds.4. The method of claim 1 , wherein the hydrotreated biofeedstock comprises paraffin products.5. The method of claim 1 , wherein the online analyzer comprises a spectrometer.6. The method of claim 1 , wherein the online analyzer is an infrared spectrometer claim 1 , a near infrared spectrometer claim 1 , or a Raman spectrometer.7. The method of claim 1 , wherein the monitoring conversion of the biofeedstock comprises determining oxygen removal from the biofeedstock.8. The method of claim 1 , wherein the monitoring conversion comprises correlating measurements from the online analyzer with conversion of the biofeedstock.9. The method of claim 1 , wherein the monitoring conversion comprises measuring carbonyl group concentration in the hydrotreated biofeedstock.10. The method of claim 1 , wherein the online analyzer is ...

Systems and Methods for Renewable Fuel

The present application generally relates to the introduction of a renewable fuel oil as a feedstock into refinery systems or field upgrading equipment. For example, the present application is directed to methods of introducing a liquid thermally produced from biomass into a petroleum conversion unit; for example, a refinery fluid catalytic cracker (FCC), a coker, a field upgrader system, a hydrocracker, and/or hydrotreating unit; for co-processing with petroleum fractions, petroleum fraction reactants, and/or petroleum fraction feedstocks and the products, e.g., fuels, and uses and value of the products resulting therefrom. 1. A fuel , comprising:a product of a fluidized catalytic cracker co-processing a petroleum fraction and an RFO/VGO mixture,said RFO/VGO mixture comprising a mixture of petroleum and renewable fuel oil.2. The fuel of claim 1 , wherein the RFO/VGO mixture comprises between 1-99 wt. % renewable fuel oil.3. The fuel of claim 1 , wherein the RFO/VGO mixture comprises between 1-20 wt. % renewable fuel oil.4. The fuel of claim 1 , wherein the RFO/VGO mixture comprises between 20-40 wt. % renewable fuel oil.5. The fuel of claim 1 , wherein the RFO/VGO mixture comprises between 40-60 wt. % renewable fuel oil.6. The fuel of claim 1 , wherein the RFO/VGO mixture comprises between 60-80 wt. % renewable fuel oil.7. The fuel of claim 1 , wherein the RFO/VGO mixture comprises between 80-99 wt. % renewable fuel oil.8. The fuel of claim 1 , wherein the RFO/VGO mixture comprises about 50 wt. % renewable fuel oil.9. The fuel according to claim 1 , wherein the RFO/VGO mixture is produced by a high shear mixer.10. The fuel according to claim 1 , wherein the RFO/VGO mixture is produced by an ultrasonic mixer.11. The fuel according to claim 1 , wherein the RFO/VGO mixture is produced by a mix atomizer.12. The fuel according to claim 1 , wherein the RFO/VGO mixture is produced by an in line mixer.13. The fuel according to claim 1 , wherein the RFO/VGO mixture further ...

METHODS TO INCREASE GASOLINE YIELD

The present application generally relates to methods to increase the gasoline and/or light cycle oil yield of a fluidized catalytic cracker processing a petroleum fraction by injecting a stream comprising a renewable fuel oil into a riser of a fluidized catalytic cracker, and the resulting fuels therefrom. 1. A method to increase the gasoline and/or light cycle oil yield of a fluidized catalytic cracker processing a petroleum fraction , comprising:injecting a stream comprising a renewable fuel oil with a pH of less than 6.5 into a riser of a fluidized catalytic cracker in a ratio in the range of 2-11 wt. % renewable fuel oil to petroleum fraction; andcontacting the renewable fuel oil with a catalyst.2. The method of claim 1 , wherein the petroleum fraction is VGO.3. The method of claim 1 , wherein the method further comprises introducing the petroleum fraction into the riser above the injecting the renewable fuel oil.4. The method of claim 1 , wherein the injecting occurs in the lower third of the riser.5. The method of claim 1 , wherein the injecting is via a lift steam line located at the bottom of the riser.6. The method of claim 1 , wherein the renewable fuel oil has a pH of less than 3.0.7. The method of claim 1 , wherein the stream further comprises the petroleum fraction.8. The method of claim 7 , wherein the injecting is via a recycle lift vapor line.9. The method of claim 7 , wherein the stream has a TAN of 0.05 to 1.0.10. The method of claim 1 , wherein the yield claim 1 , computed on an equivalent carbon basis or an equivalent energy input basis claim 1 , is higher than that achieved under the same conditions in a fluidized catalytic cracker processing the petroleum fraction alone.11. A method to reduce the heavy cycle oil and/or slurry oil yield of a fluidized catalytic cracker processing a petroleum fraction claim 1 , comprising:injecting a stream comprising a renewable fuel oil with a pH of less than 6.5 into a riser of a fluidized catalytic cracker in ...

PREPARING A FUEL FROM LIQUID BIOMASS

The present application generally relates to methods to prepare a fuel from a liquid biomass by first producing the liquid biomass from a solid biomass by a thermal process, and then processing the liquid biomass with a petroleum fraction in the presence of a catalyst. 1. A method to prepare a fuel from a liquid biomass , comprising:producing the liquid biomass from a solid biomass by a thermal process; andprocessing the liquid biomass with a petroleum fraction as reactants in the presence of a catalyst.2. The method of claim 1 , wherein the thermal process comprises pyrolysis.3. The method of claim 2 , wherein the pyrolysis comprises rapid thermal processing.4. The method of claim 1 , wherein the solid biomass comprises a wood claim 1 , wood residue claim 1 , or agricultural residue.5. The method of claim 1 , wherein the processing occurs in a continuous conversion unit.6. The method of claim 5 , wherein the continuous conversion unit is a fluidized catalytic cracking unit.7. The method of claim 1 , wherein the petroleum fraction and the liquid biomass are co-processed in a continuous conversion unit.8. The method of claim 7 , wherein the continuous conversion unit is a fluidized catalytic cracking unit.9. The method of claim 1 , wherein the liquid biomass makes up less than 10 wt. % of the reactants.10. The method of claim 1 , wherein the producing and processing occur in a refinery.11. The method of claim 1 , wherein the petroleum fraction is VGO.12. The method of claim 1 , wherein the liquid biomass has a pH in the range of 0.5 to 7.13. The method of claim 1 , wherein the liquid biomass as a carbon content in the range of 35-80 wt. % and an oxygen content in the range of 20-50 wt. % claim 1 , on a moisture-free basis.14. The method of claim 1 , wherein the liquid biomass has a water content in the range of 10-40 wt. %.15. The method of claim 1 , wherein the fuel is a transportation fuel.16. A fuel prepared from a liquid biomass claim 1 , comprising: (i) liquid ...

COMPOSITION COMPRISING PARAFFIN FRACTIONS OBTAINED FROM BIOLOGICAL RAW MATERIALS AND METHOD OF PRODUCING SAME

A composition, including 40-50 wt-% C14 paraffins, based on the total weight of the composition, and 35-45 wt-% C15 paraffins, based on the total weight of the composition, wherein the C14 and C15 paraffins are produced from a biological raw material. 119-. (canceled)20. A composition , comprising:40-50 wt-% C14 isoparaffins, based on the total weight of the composition, and35-45 wt-% C15 isoparaffins, based on the total weight of the composition,wherein the C14 and C15 isoparaffins are produced from a biological raw material,wherein the total C14 and C15 isoparaffinic content of the composition is in a range from 80.36 wt-% to 95 wt-%, based on the total weight of the composition.21. The composition according to claim 20 , wherein the composition comprises 45-50 wt-% C14 isoparaffins claim 20 , and 40-45 wt-% C15 isoparaffins claim 20 , based on the total weight of the composition.22. The composition according to claim 20 , wherein the composition comprises less than 9 wt-% C13 and lighter paraffins and less than 7 wt-% C16 and heavier paraffins claim 20 , based on the total weight of the composition.23. The composition according to claim 20 , wherein the composition comprises less than 5 wt-% C13 and lighter paraffins and less than 3 wt-% C16 and heavier paraffins claim 20 , based on the total weight of the composition.24. The composition according to claim 20 , wherein the total isoparaffinic content of the composition is more than 93 wt-% claim 20 , based on the total weight of the composition.25. The composition according to claim 20 , wherein the total isoparaffinic content of the composition is more than 97 wt-% claim 20 , based on the total weight of the composition.26. The composition according to claim 20 , wherein the total aromatic hydrocarbon content of the composition is less than 1500 ppm weight basis.27. The composition according to claim 20 , wherein the total aromatic hydrocarbon content of the composition is less than 1300 ppm weight basis.28. The ...

FUEL COMPOSITIONS

Low sulphur marine fuel compositions are provided. Embodiments comprise 10 to 50 wt. % of a residual hydrocarbon component, with the remaining 50 to 90 wt. % selected from a non-hydroprocessed hydrocarbon component, a hydroprocessed hydrocarbon component, and a combination thereof. Embodiments of the marine fuel composition can have a sulphur content of about 0.1 wt. % or less. 1. A marine fuel composition comprising:greater than 25 wt. % to 50 wt. % of a residual hydrocarbon component comprising an atmospheric tower bottoms (ATB) residues with a kinematic viscosity at ˜50 degrees C. of at least 100 cSt; andwherein the marine fuel composition has a kinematic viscosity at ˜50 degrees C. of at least 10 cSt.2. The marine fuel composition of wherein the sulphur content is in a range of 400 to 1000 wppm.3. The marine fuel composition of which exhibits at least one of the following:a hydrogen sulfide content of at most 2.0 mg/kg; an acid number of at most 2.5 mg KOH per gram; a sediment content of at most 0.1 wt. %; a water content of at most 0.5 vol %; and an ash content of at most 0.15 wt. %.4. The marine fuel composition of which has at least one of the following: a density at 15 degrees C. in a range of 0.870 to 1.010 g/cm claim 1 , a pour point of −30 to 35 degrees C. claim 1 , and a flash point of at least 60 degrees C.5. The marine fuel composition of wherein the density is at least 0.890 g/cm.6. The marine fuel composition of wherein the kinematic viscosity is less than 12 cSt.7. The marine fuel composition of further comprising:at least 30 wt. % of the residual hydrocarbon component; andat least 10 wt. % of a non-hydroprocessed hydrocarbon component comprising at least one of light cycle oil (LCO), heavy cycle oil (HCO), fluid catalytic cracking (FCC) cycle oil, FCC slurry oil, pyrolysis gas oil, cracked light gas oil (CLGO), cracked heavy gas oil (CHGO), pyrolysis light gas oil (PLGO), pyrolysis heavy gas oil (PHGO), thermally cracked residue, thermally cracked ...

PROCESS OF GENERATING A RENEWABLE BIOFUEL FROM A HYDROTREATED STREAM OF CONDENSED OXYGENATES

A renewable fuel may be obtained from a bio-oil containing C-Coxygenates. In a first step, the bio-oil is subjected to a condensation reaction in which the oxygenates undergo a carbon-carbon bond forming reaction to produce a stream containing C+ oxygenates. In a second step, the stream is hydrotreated to produce C+ hydrocarbons. 2. The process of claim 1 , wherein prior to step (a):(i) biomass is converted in a biomass conversion reactor into gaseous, liquid and solid components;(ii) the gaseous components and solid components are separated from the liquid components;{'sub': 3', '5, '(iii) the liquid components are separated into an aqueous phase and an organic stream containing C-Coxygenates; and'}{'sub': 3', '5, '(iv) the aqueous phase is then separated into another organic stream containing C-Coxygenates.'}3. The process of claim 1 , wherein the condensation reaction is an aldol condensation.4. The process of claim 1 , wherein the renewable biofuel is produced from liquid bio-oil.6. The process of claim 5 , wherein prior to step (a):(i) biomass is converted in a biomass conversion reactor into gaseous, liquid and solid components;(ii) the gaseous components and solid components are separated from the liquid components;{'sub': 3', '5, '(iii) the liquid components are separated into an aqueous phase and an organic stream containing C-Coxygenates; and'}{'sub': 3', '5, '(iv) the aqueous phase is then separated into another organic stream containing C-Coxygenates.'}7. The process of claim 5 , wherein condensation occurs in the single reactor in the presence of a heterogeneous acid catalyst.8. The process of claim 7 , wherein the heterogeneous acid catalyst is selected from the group consisting of organic sulfonic acids; perfluoroalkylsulfonic acids; zeolites; sulfated transition metal oxides claim 7 , and perfluorinated ion exchange polymers containing pendant sulfonic acid claim 7 , carboxylic acid claim 7 , or sulfonic acid groups; sulfonated copolymers of styrene ...

Methods for converting motor oil into fuel

Methods for converting motor oil into fuel generally include forming a conversion mixture of an alcohol and a base, and adding the conversion mixture to motor oil, to form a reaction mixture. The methods can also include adding a high nitrate compound and an amino acid to the reaction mixture and ozonizing the reaction mixture. The result of the methods can include a three phase system in which the bottom phase is asphalt oil, the middle phase is diesel fuel or jet fuel, and the top phase is sulfuric acid. The three phases can be separated to obtain the final diesel fuel or jet fuel product.

METHOD FOR CATALYTIC CONVERSION OF KETOACIDS AND HYDROTREAMENT TO HYDROCARBONS

Catalytic conversion of ketoacids is disclosed, including methods for increasing the molecular weight of ketoacids. An exemplary method includes providing in a reactor a feedstock having at least one ketoacid. The feedstock is then subjected to one or more C—C-coupling reaction(s) in the presence of a catalyst system having a first metal oxide and a second metal oxide. 1. A method for increasing the molecular weight of a ketoacid , the method comprising:providing in a reactor a feedstock having at least one ketoacid; andsubjecting the feedstock to one or more C—C-coupling reaction(s), wherein the C—C-coupling reaction(s) are conducted in a presence of a solid acid catalyst system having a first metal oxide and a second metal oxide, and wherein a content of the at least one ketoacid in the feedstock is at least 30 wt-%.2. The method according to claim 1 , wherein the catalyst system has a specific surface area of from 10 to 500 m/g.3. The method according to claim 1 , wherein a total amount of the acid sites of the catalyst system ranges between 30 and 500 μmol/g.4. The method according to claim 1 , wherein the at least one ketoacid is a γ-ketoacid acid.5. The method according to claim 1 , wherein the content of the at least one ketoacid in the feedstock is at least 40 wt-% claim 1 , and/or the content of water in the feedstock is less than 5.0 wt-%.6. The method according to claim 1 , wherein the first metal oxide comprises:an oxide of one of W, Be, B, Mg, Si, Ca, Sc, Ti, V, Cr, Mn, Fe, Co, Ni, Cu, Zn, Ga, Sr, Y, Zr, Nb, Mo, Cd, Sn, Sb, Bi, La, Ce, Th, and the second metal oxide comprises:an oxide of one of Zr, Ti, Si, Al, V, Cr or a combination of these, the first metal oxide not being same as the second metal oxide.7. The method according to claim 1 , wherein the first metal oxide is supported on a metal oxide carrier claim 1 , wherein the carrier is selected from the group consisting of zirconia claim 1 , titania claim 1 , silica claim 1 , vanadium oxide claim 1 ...

Renewable High-Density, High-Octane Fuels

A method/fuels for making high-density, high-octane fuels, the high-density, high-octane including, dimerizirig terpene monomer(s), crude mixture of terpene(s), and/or oxygenated terpenoid(s) with at least one heterogeneous dimerization acid catalyst at temperatures ranging from about 25° C. to about 160° C. to produce a mixture of residual/isomerized monomer(s) cymene(s), and terpene dimer(s), hydrogenating the mixture of residual/isomerized monomer(s), p-cymene(s), and terpene dimer(s) with at least one heterogenous catalyst(s) under a hydrogen atmosphere to produce a hydrogenated mixture of cymene(s), saturated cyclic molecules of terpene(s), other aromatic(s), and/or saturated terpene dimer(s), and isolating the hydrogenated mixture of cymene(s), saturated cyclic terpene(s), other aromatic(s), and saturated terpene dimer(s) by fractional distillation to yield a high boiling fraction composed of terpene dimers and mixture low boiling fraction composed of hydrogenated monomer(s) and cymenes. 1. A method for making a high-density , high-octane fuel , comprising:dimerizing terpene monomer(s), crude mixture of terpene(s), and/or oxygenated terpenoid(s) with at least one heterogeneous dimerization acid catalyst at temperatures ranging from about 25° C. to about 170° C. to produce a mixture of residual/isomerized monomer(s), cymene(s), and terpene dimer(s);hydrogenating said mixture of residual/isomerized monomer(s), cymene(s), and terpene dimer(s) with at least one catalyst under a hydrogen atmosphere to produce a hydrogenated mixture of cymene(s), saturated cyclic molecules of terpene(s), other aromatic(s), and/or saturated terpene dimer(s); andisolating said hydrogenated mixture of cymene(s), saturated cyclic terpene(s), other aromatic(s), and saturated terpene dimer(s) by fractional distillation to yield a high boiling fraction composed of terpene dimers and boiling between about 280 and 350° C. under standard conditions, and a low boiling fraction composed of ...

Renewable High Density Turbine and Diesel Fuels

A method for synthesizing cyclic hydrocarbons with linear hydrocarbon side chains from a renewable source, or biomass by naturally occurring or bioengineered fungal strains, or hydrodistillation of plants. 1. A method of synthesizing fuels , comprising:isolating 1-octene-3-ol from waste biomass or a renewable source by hydrodistillation of plant material, enzymatic cleavage of fatty acids, or direct biosynthesis with fungi or bacteria;dehydrating said 1-octene-3-ol with at least one acid catalyst to produce a mixture of isomers of 1,3-octadiene and internal octadienes;cyclodimerizing said mixture of isomers of 1,3-actadiene and internal octadienes under modest pressure having a range from about 1 atm to about 200 atm and heating with a range from about −20° C. to about 350° C. with at least one homogeneous or heterogenous Lewis acid catalyst to effect a Diels-Alder cycloaddition to produce a mixture of unsaturated cyclic olefins;catalytically hydrogenating said unsaturated cyclo-olefins with hydrogen to produce a mixture of saturated cyclic hydrocarbons; andpurifying said saturated cyclic hydrocarbons by distillation to produce fuel mixtures with densities greater than 0.8 g/mL.2. The method according to claim 1 , further comprising isolating by degradation of said waste biomass includes naturally occurring or bioengineered fungal strains.3. The method according to claim 1 , wherein said renewable source comprises at least one linoleic acid claim 1 , other fatty acids claim 1 , triglycerides claim 1 , or mixtures thereof.4Melittis melissophyllum.. The method according to claim 1 , further comprising obtaining alcohol by hydrodistillation of a renewable source including plants being5. The method according to claim 1 , wherein said acid catalyst comprises at least one inorganic acid selected from the group consisting of phosphoric acid claim 1 , sulfuric acid claim 1 , and hydrochloric acid claim 1 , other mineral acids claim 1 , and supported mineral acids.6. The ...

High Density Cyclic Fuels Derived From Linear Sesquiterpenes

A method to generate cyclic hydrocarbons from farnesene to increase both the density and net heat of combustion of the product fuels. The high density hydrocarbons produced by this method have applications for missile, UAV, jet, and diesel propulsion.

Multi-Stage Process and Device for Treatment Heavy Marine Fuel Oil and Resultant Composition and the Removal of Detrimental Solids

A multi-stage process for reducing the environmental contaminants in an ISO8217 compliant Feedstock Heavy Marine Fuel Oil involving a core desulfurizing process and a Detrimental Solids removal unit as either a pre-treating step or post-treating step to the core process. The Product Heavy Marine Fuel Oil complies with ISO 8217 for residual marine fuel oils and has a sulfur level has a maximum sulfur content (ISO 14596 or ISO 8754) between the range of 0.05 mass % to 1.0 mass and a Detrimental Solids content less than 60 mg/kg. A process plant for conducting the process is also disclosed. 1. A process for reducing the environmental contaminants and detrimental solids in a Feedstock Heavy Marine Fuel Oil , the process comprising: contacting a Feedstock Heavy Marine Fuel Oil with Detrimental Solids removal unit to give a pre-treated Feedstock Heavy Marine Fuel Oil; mixing a quantity of the pre-treated Feedstock Heavy Marine Fuel Oil with a quantity of Activating Gas mixture to give a Feedstock Mixture; contacting the Feedstock Mixture with one or more catalyst materials under reactive conditions to form a Process Mixture from said Feedstock Mixture; receiving said Process Mixture and separating the Product Heavy Marine Fuel Oil liquid components of the Process Mixture from the gaseous components and by-product hydrocarbon components of the Process Mixture and , discharging the Product Heavy Marine Fuel Oil.2. The process of wherein said Feedstock Heavy Marine Fuel Oil complies with ISO 8217 (2017) and has a sulfur content (ISO 14596 or ISO 8754) between the range of 5.0 mass % to 1.0 mass %.3. The process of claim 1 , wherein said Product Heavy Marine Fuel Oil complies with ISO 8217 (2017) and has a maximum sulfur content (ISO 14596 or ISO 8754) between the range of 0.01 mass % to 1.0 mass %.4. The process of claim 1 , wherein said Feedstock Heavy Marine Fuel Oil has: a maximum of kinematic viscosity at 50° C. (ISO 3104) between the range from 180 mm/s to 700 mm/s; a ...

Multi-Stage Process and Device for Treatment Heavy Marine Fuel Oil and Resultant Composition Including Ultrasound Promoted Desulfurization

A multi-stage process for reducing the environmental contaminants in an ISO8217 compliant Feedstock Heavy Marine Fuel Oil involving a core desulfurizing process and a ultrasound treatment process as either a pre-treating step or post-treating step to the core process. The Product Heavy Marine Fuel Oil complies with ISO 8217 for residual marine fuel oils and has a sulfur level has a maximum sulfur content (ISO 14596 or ISO 8754) between the range of 0.05 mass % to 1.0 mass. A process plant for conducting the process is also disclosed. 1. A process for reducing the environmental contaminants in a Feedstock Heavy Marine Fuel Oil , the process comprising: contacting a Feedstock Heavy Marine Fuel Oil with ultrasound having a frequency in the range of about 20 kHz and about 100 megahertz and a sonic energy in the range of about 30 watts/cmto about 300 watts/cm , in the presence of desulfurization reaction inducer selected from the group consisting of aqueous peroxides or one or more transition metal catalysts in the presence of hydrogen , to give a pre-treated Feedstock Heavy Marine Fuel Oil; mixing a quantity of the pre-treated Feedstock Heavy Marine Fuel Oil with a quantity of Activating Gas mixture to give a Feedstock Mixture; contacting the Feedstock Mixture with one or more transition metal catalysts under reactive conditions to form a Process Mixture from said Feedstock Mixture; receiving said Process Mixture and separating the Product Heavy Marine Fuel Oil liquid components of the Process Mixture from the gaseous components and by-product hydrocarbon components of the Process Mixture and , discharging the Product Heavy Marine Fuel Oil.2. The process of wherein said Feedstock Heavy Marine Fuel Oil complies with ISO 8217 (2017) except that it has a sulfur content (ISO 14596 or ISO 8754) between the range of 5.0 wt % to 1.0 wt % and wherein the Product Heavy Marine Fuel Oil complies with ISO 8217 (2017) and has a a sulfur content (ISO 14596 or ISO 8754) between the ...

RENEWABLE ENERGY-DRIVEN CARBON CYCLE ECONOMIC AND ECOLOGICAL OPERATING SYSTEMS

An integrated system for exploiting renewable energy sources based upon carbon dioxide captured from the atmosphere is provided, the system comprising: a solar energy collector; apparatus for capturing COfrom the atmosphere; a wind power driven electrical generator; water power driven electrical generator; electric power distribution control means from the renewable energy sources; energy storage systems; water desalinating means and water electrolysis means powered by the renewably generated electricity; hydrocarbon fuel preparation means utilizing the hydrogen and the carbon dioxide generated by this system; and a body of saline water adjacent the land on which the integrated system is built. 1. An integrated productive system for exploiting renewable energy sources while removing carbon from the atmosphere , the system comprising a geographic region including a sea coast region with an adjacent body of tidal salt water[Atlantic Ocean) , together with the availability of regular winds [para 0007]; desert regions where solar light is available during a large proportion of the year [para 0027] , dams and tidal power [para 0012] , where hydropower is naturally available , and regular prevailing winds [ , the integrated productive system further comprising:a. a plurality of solar energy collectors for generating electric power;b. wind power driven electrical generators;c. hydropower driven electrical generators from dams and tidal power;d. energy storage systems selected from the group consisting of electrical storage batteries, hydrogen fuel storage, liquid hydrocarbon fuel storage and heat-insulated storage means for holding extremely hot liquid, for storing renewable energy;{'sub': '2', 'e. apparatus for carrying out a process for capturing and storing COfrom the atmosphere, interconnected with at least one of the sources of generated electric power;'}f. desalinating means interconnected with at least one of the sources of generated electric power or an energy ...

Renewable transportation fuel process with thermal oxidation sysem

A process for treating effluent streams in a renewable transportation fuel production process is described. One or more of the sour water stream and an acid gas stream are treated directly in thermal oxidation section. The process allows the elimination or size reduction of a sour water stripper unit, waste water treatment plant, and sulfur recovery unit.

FUEL COMPOSITIONS FROM LIGHT TIGHT OILS AND HIGH SULFUR FUEL OILS

Methods are provided to prepare a low sulfur fuel from hydrocarbon sources, such as light tight oil and high sulfur fuel oil, often less desired by conventional refiners, who split crude into a wide range of differing products and may prefer presence of wide ranges (C3 or C5 to C20 or higher) of hydrocarbons. These fuels can be produced by separating feeds into untreated and treated streams, and then recombining them. Such fuels can also be formulated by combinations of light, middle and heavy range constituents in a selected manner as claimed. Not only low in sulfur, the fuels of this invention are also low in nitrogen and essentially metals free. Fuel use applications include on-board large marine transport vessels but also on-shore for large land based combustion gas turbines, boilers, fired heaters and transport vehicles and trains. 138-. (canceled)393241. Combustion in marine or land based engines , combustion gas turbines , or fired heaters of a fuel derived from light tight oil () and crude oil () , either alone or with added high sulfur fuel oil () , comprising combination of treated and untreated streams having an initial boiling point being the lowest boiling point of any fraction within untreated streams combined in said fuel and highest boiling point being the highest boiling portion of deasphalted oil effluent from solvent separation of an unconverted oil which is subsequently treated by hydroconversion and forms a portion said fuel.4055-. (canceled)56. Combustion of a fuel in accordance with wherein said fuel comprises a portion or all of a light tight oil and streams of processed high sulfur fuel oil claim 39 , processed alone or with added crude oil claim 39 , comprising:(a) unstabilized wild straight run naphtha and distillation fraction at or below sulfur breakpoint cut without added treatment,(b) distillate hydrotreater effluent of distillate range distillation fraction above sulfur breakpoint cut comprising wild naphtha and at least a portion of ...

METHODS AND SYSTEMS FOR OBTAINING LONG CHAIN CARBONS FROM PETROLEUM BASED OIL

Methods and system for obtaining long chain carbons that generally include forming a conversion mixture of an alcohol and a base, adding the conversion mixture to oil (such as petroleum based oil, crude oil, used oil, used motor oil, and new motor oil) to form a reaction mixture, adding a high nitrate compound the reaction mixture, and separating out the long chain carbons for use as an input by other processing such as pharmaceutical and/or additional petro-chemical processing. Additional cooling and/or filtering processes may be utilized to complete and/or optimize oil conversion.

FUEL OIL

PURPOSE: The present invention provides a fuel oil which emits a reduced amount of exhaust gas such as NOX and THC and is used in an internal-combustion engine comprising a combustion chamber which is adapted so that a fuel oil and gas comprising 65% by volume or more of oxygen are subjected to combustion in the combustion chamber. 1. A fuel oil for an internal-combustion engine comprising a combustion chamber which is adapted so that the fuel oil and gas comprising 65% by volume or more of oxygen are subjected to combustion in the combustion chamber , wherein the fuel oil meets at least one of the following requirements (1) to (7):(1) the fuel oil comprises 60% by volume or more of a hydrocarbon oil, wherein an amount of saturated hydrocarbons is 30% by volume or more relative to the total volume of the hydrocarbon oil, an amount of olefinic hydrocarbons is 35% by volume or less relative to the total volume of the hydrocarbon oil and an amount of aromatic hydrocarbons is 50% by volume or less relative to the total volume of the hydrocarbon oil;(2) the fuel oil comprises 60% by volume or more of a hydrocarbon oil, wherein an amount of saturated hydrocarbons is 30% by volume or more relative to the total volume of the hydrocarbon oil, an amount of olefinic hydrocarbons is 40% by volume or less relative to the total volume of the hydrocarbon oil and an amount of aromatic hydrocarbons is 50% by volume or less relative to the total volume of the hydrocarbon oil; and the fuel oil has an initial boiling point of 21 to 80 degrees C., a 10% by volume distillation temperature of 35 to 90 degrees C., a 90% by volume distillation temperature of 100 to 190 degrees C. and a final boiling point of 130 to 230 degrees C.;(3) the fuel oil comprises 60% by volume or more of a hydrocarbon oil, wherein an amount of saturated hydrocarbons is 15% by volume or more relative to the total volume of the hydrocarbon oil, an amount of olefinic hydrocarbons is 35% by volume or less relative to ...

Simultaneous Production of Base Oil and Fuel Components from Renewable Feedstock

The present invention provides a method for simultaneous production of components suitable for production of base oil and fuel components. In the method a feedstock comprising fatty acids and/or fatty acid esters is entered into a reaction zone and subjected to a ketonisation reaction in the presence of a dual catalyst system. This system is configured to perform a ketonisation reaction and a hydrotreatment reaction, under hydrogen pressure. Subsequently ketones are obtained. 1. A method for simultaneous production of components suitable for production of base oil and fuel components , comprising the steps of:a) introducing a feedstock comprising fatty acids and/or fatty acid esters into a reaction zone, andb) subjecting said feedstock to a ketonisation reaction in said reaction zone in the presence of a dual catalyst system configured to perform a ketonisation reaction and a hydrotreatment reaction, under hydrogen pressure, andc) obtaining from said ketonisation reaction ketones in addition to linear hydrocarbons from said fatty acids and/or fatty acid esters.2. The method according to claim 1 , wherein said obtained ketones are further hydrodeoxygenated to form linear hydrocarbons.3. The method according to claim 1 , wherein said fatty acid esters are triglycerides.4. The method according to claim 1 , wherein said feedstock is at least partly claim 1 , preferably completely claim 1 , in liquid form when entered into said reaction zone.5. The method according to claim 1 , wherein the pressure in said reaction zone is less than 10 MPa claim 1 , preferably from 0.1 to 5 MPa.6. The method according to claim 1 , wherein the temperature in said reaction zone is from 200 to 450° C.7. The method according to claim 1 , wherein the ratio of hydrogen to feedstock is from 100 to 600 NI/I claim 1 , preferably from 100 to 500 NI/I.8. A method for simultaneous production of base oil components and fuel components claim 1 , comprising the steps of(i) introducing a feedstock ...

Method for Production of Hydrocarbons by Increasing Hydrocarbon Chain Length

The present invention provides a method for increasing hydrocarbon chain length. The method comprises providing a feedstock comprising fatty acids and/or fatty acid esters with hydrocarbon chain length below C into a reaction zone in which ketonisation is conducted in the presence of a hydrotreatment catalyst under hydrogen pressure. The obtained ketones have a hydrocarbon chain length of from C to C The present invention further provides a method for simultaneous production of base oil components and fuel components. 1. A method for increasing hydrocarbon chain length , comprising the steps of:(i) providing a feedstock comprising fatty acids and/or fatty acid esters with hydrocarbon chain length below C23, and(ii) introducing said feedstock into a reaction zone in which ketonisation of said fatty acids and/or fatty acid esters is conducted in the presence of a hydrotreatment catalyst under hydrogen pressure, and(iii) obtaining from said reaction zone ketones with hydrocarbon chain length of from C24 to C43.2. The method according to wherein the obtained ketones are further hydrodeoxygenated in a final hydrodeoxygenation step to form linear hydrocarbons.3. The method according to claim 1 , wherein the ketonization and final hydrodeoxygenation step are performed in the same reaction zone.4. The method according to claim 2 , wherein the final hydrodeoxygenation step is performed in a separate reaction zone subsequent to the ketonization reaction.5. The method according to claim 1 , wherein the pressure in the ketonisation reaction zone is less than 2 MPa.6. The method according to claim 1 , wherein the temperature in the ketonisation reaction zone is from 350 to 450° C.7. The method according to claim 1 , wherein the ratio of hydrogen to feedstock is from 100 to 600 Nl/l in the ketonisation reaction zone.8. The method according to claim 1 , wherein said hydrotreatment catalyst is a metal catalyst wherein the metal is selected from the group consisting of Fe claim 1 , ...

MULTI-STAGE UPGRADING PYROLYSIS TAR PRODUCTS

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

MESITYLENE AS AN OCTANE ENHANCER FOR AUTOMOTIVE GASOLINE, ADDITIVE FOR JET FUEL, AND METHOD OF ENHANCING MOTOR FUEL OCTANE AND LOWERING JET FUEL CARBON EMISSIONS

A motor fuel comprising gasoline comprising 70-99 wt % gasoline and 1 to 30 wt % of mesitylene. This fuel can advantageously contain conventional additives used in gasoline. The use of mesitylene in gasoline blend yields a fuel blend with a higher research octane number and motor octane number. In addition, an improved jet fuel is provided, having from 1-10 wt % mesitylene added to the jet fuel, having improved carbon emission characteristics while maintaining required specifications. Further, an improved bio-fuel is provided, which may function as a replacement for conventional Jet A/JP-8 fuel and has lowered carbon emission specifications, the bio-fuel comprised of 75-90 wt % synthetic parafinnic kerosene (SPK) and 10-25 wt % mesitylene. 1. A motor fuel comprising 70-99 wt % gasoline and 1-30 wt % mesitylene.2. The motor fuel of comprising 80-99 wt % gasoline and 1-20 wt % mesitylene.3. The motor fuel of comprising 80-95 wt % gasoline and 5-20 wt % mesitylene.4. The motor fuel of comprising 80-90 wt % gasoline and 10-20 wt % mesitylene.5. The motor fuel of in which the motor fuel has a FBP max of 225° C. claim 1 , a MON of 80 to 94 claim 1 , and an RVP of 38-103 kPa.6. The motor fuel of in which the motor fuel has a FBP of 170° C. to 225° C.7. The motor fuel of in which the motor fuel has a 90% BP max of 185° C.8. The motor fuel of in which the motor fuel has a 90% BP of 130° C. to 185° C.9. The motor fuel of in which the motor fuel has a MON of at least 91.10. The motor fuel of in which the motor fuel has a FBP of 170° C. to 225° C.11. The motor fuel of in which the motor fuel has an RVP of 38-49 kPa.12. The motor fuel of in which the motor fuel has a FBP of 170° C. to 225° C.13. The motor fuel of in which the motor fuel has a MON of at least 91.14. The motor fuel of in which the motor fuel has a FBP of 170° C. to 225° C.15. The motor fuel of in which the motor fuel has a 90% BP max of 185° C.16. The motor fuel of in which the motor fuel has a 90% BP of 130° C. ...

FUEL COMPOSITIONS FROM LIGHT TIGHT OILS AND HIGH SULFUR FUEL OILS

Methods are provided to prepare a low sulfur fuel from hydrocarbon sources, such as light tight oil and high sulfur fuel oil, often less desired by conventional refiners, who split crude into a wide range of differing products and may prefer presence of wide ranges (C3 or CS to C20 or higher) of hydrocarbons. These fuels can be produced by separating feeds into untreated and treated streams, and then recombining them. Such fuels can also be formulated by combinations of light, middle and heavy range constituents in a selected manner as claimed. Not only low in sulfur, the fuels of this invention are also low in nitrogen and essentially metals free. Fuel use applications include on-board large marine transport vessels but also on-shore for large land based combustion gas turbines, boilers, fired heaters and transport vehicles and trains. 129-. (canceled)30. A fuel derived from combining(a) light oil and (1) said unconverted oils passed to solvent separation to remove insoluble remaining metals and asphaltenes to form soluble deasphalted oil, and', (i) an actual sulfur content of 0.5 wt. % or less, and', '(ii) initial boiling point being that of lowest boiling component of light tight oil or lighter materials from said hydroconversion so combined and', '(iii) highest boiling point being that of highest boiling component of said treated soluble deasphalted oil derived from high sulfur fuel oil or other residuals so combined., '(2) said soluble deasphalted oil subsequent treated either by additional hydrotreating or additional hydroconversion to form said treated soluble deasphalted oil, said fuel having'}], '(b) hydroconversion reaction effluent comprising treated soluble deasphalted oil and lighter materials derived from hydroconversion of high sulfur fuel oil, or other residuals processed by residue hydroconversion to form said effluent comprising treated liquids and unconverted oils,'}3150-. (canceled)51. A fuel characterized by comprising:(a) all or a portion of a ...

FUEL COMPOSITIONS FROM LIGHT TIGHT OILS AND HIGH SULFUR FUEL OILS

Methods are provided to prepare a low sulfur fuel from hydrocarbon sources, such as light tight oil and high sulfur fuel oil, often less desired by conventional refiners, who split crude into a wide range of differing products and may prefer presence of wide ranges (C3 or C5 to C20 or higher) of hydrocarbons. These fuels can be produced by separating feeds into untreated and treated streams, and then recombining them. Such fuels can also be formulated by combinations of light, middle and heavy range constituents in a selected manner as claimed. Not only low in sulfur, the fuels of this invention are also low in nitrogen and essentially metals free. Fuel use applications include on-board large marine transport vessels but also on-shore for large land based combustion gas turbines, boilers, fired heaters and transport vehicles and trains. 1. A process for conversion of hydrocarbonaeous feeds comprising sulfur and metals to form a fuel characterized in that feed comprises light tight oil and high sulfur fuel oil , said process comprising{'b': 41', '401, 'claim-text': [{'b': 411', '420, '(1) reactor zone effluent which is separated into hydroconverted liquids () and purge gases () comprising hydrogen and sulfur,'}, {'b': 409', '301', '311', '401', '351', '501, '(2) unconverted oils () which are directed to solvent separation () to form (A) soluble deasphalted oil () which is recycled as feed to said hydroconversion zone (), either separately or combined with added high sulfur fuel oil feed to said reactor and (B) insoluble pitch () which is directed to pitch treatment (), and'}], '(a) feeding one or more high sulfur fuel oils () to a residue hydroconversion zone () and contacting such oil with hydrogen in presence of catalyst at residue hydroconversion conditions in an ebullated-bed reactor to form'}{'b': 1', '411', '600, '(b) combining all or one or more portions of a light tight oil () with said hydroconverted liquids () to form a fuel ().'}2. A process in accordance ...

Fuel compositions from light tight oils and high sulfur fuel oils

Methods are provided to prepare a low sulfur fuel from hydro-carbon sources, such as light tight oil and high sulfur fuel oil, often less desired by conventional refiners, who split crude into a wide range of differing products and may prefer presence of wide ranges (C3 or C5 to C20 or higher) of hydrocarbons. These fuels can be produced by separating feeds into untreated and treated streams, and then recombining them. Such fuels can also be formulated by combinations of light, middle and heavy range constituents in a selected manner as claimed. Not only low in sulfur, the fuels of this invention are also low in nitrogen and essentially metals free. Fuel use applications include on-board large marine transport vessels but also on-shore for large land based combustion gas turbines, boilers, fired heaters and transport vehicles and trains.

FUEL COMPOSITIONS FROM LIGHT TIGHT OILS AND HIGH SULFUR FUEL OILS

Methods are provided to prepare a low sulfur fuel from hydrocarbon sources, such as light tight oil and high sulfur fuel oil, often less desired by conventional refiners, who split crude into a wide range of differing products and may prefer presence of wide ranges (C3 or C5 to C20 or higher) of hydrocarbons. These fuels can be produced by separating feeds into untreated and treated streams, and then recombining them. Such fuels can also be formulated by combinations of light, middle and heavy range constituents in a selected manner as claimed. Not only low in sulfur, the fuels of this invention are also low in nitrogen and essentially metals free. Fuel use applications include on-board large marine transport vessels but also on-shore for large land based combustion gas turbines, boilers, fired heaters and transport vehicles and trains. 144-. (canceled)45. A formulated combination useful as a fuel characterized in that it is formed by combining a range of hydrocarbons of (L)+(M)+(H) and the resulting combination is from 30% to 70% by volume of (M) range constituents and the remainder is equal parts of (L) and (H) at (L)/(H) in ratio of 0.9/1 to 1/0.9 , for 100 volume percent total , and final combination density is within 820 to 880 Kg/M3 at 15° C. , total sulfur is 0.25 wt. % or less and metals are 40 ppmwt or less(a) wherein (L) comprises components of naphtha and kerosene range materials, which are refined or partially refined, unrefined or extracted and used without being subject to any fractionation, hydrotreating or other treatment process, except optional separation of light gases or water, having an initial boiling point of 38° C. (100° F.) or less having a ninety percent (90%) plus final boiling point of 190° C. (374° F.) to about 205° C. (401° F.), where (L) range components contribute to (L) range bulk density and to final combination density even though individual constituents of (L) may fall outside said combination density range(b) wherein (M) ...

PETROLEUM SUBSTITUTE COMPRISED OF AN ORGANIC SOLVENT EXTRACT OF HERBACEOUS PLANT BIOMASS

A preferred embodiment of the present invention is directed generally to a composition of matter and, more specifically, to a composition comprising a petroleum substitute produced from renewable, herbaceous plant-based sources through a solvent extraction process. The plant sources are typically hydrocarbon-bearing plants capable of producing significant quantities of liquid terpenes such that the process of extracting hydrocarbons from the plant material is economically viable. In a preferred embodiment of the invention, the plant species is Euphorbia tirucalli, a species that contains relatively large quantities of relatively low molecular weight hydrocarbons. A raw plant biomass is milled and formed into a batt of plant material having generally uniform properties. Naturally occurring hydrocarbons found in the plant material are then extracted using an organic solvent extraction process. The extracted hydrocarbon oils are then separated from the solvent and may be used as a petroleum substitute, while the solvent may be reused in the extraction operation. 1.) A composition used as a petroleum substitute comprising an organic solvent extract of Euphorbia tirucalli plant material.2.) The composition of claim 1 , said extract comprising hydrocarbons formed from oligomerized pentenes.3.) The composition of claim 2 , said pentenes comprising 2-methyl-2-butene.4.) The composition of claim 2 , said pentenes comprising 2-methyl-1-butene.5.) The composition of claim 1 , said extract comprising plant isoprenoids formed from 2-methyl-1-butene subunits.6.) The composition of claim 1 , said composition having a naphtha fraction comprised of 2 claim 1 ,6-dimethyl-2 claim 1 ,6-octadiene and 2 claim 1 ,7-dimethyl-2 claim 1 ,6-octadiene.7.) The composition of claim 6 , said naphtha fraction further comprising monoterpene compounds.)8.) The composition of claim 6 , said naphtha fraction comprising greater than ⅓ of the extracted material.9.) The composition of claim 6 , said ...

Blends of synthetic diesel fuel and petroleum diesel fuel with improved performance characteristics

The present invention provides a blended fuel and methods for producing the blended fuel, wherein a synthetic fuel derived from a alternative resources such as natural gas, associated gas, biomass, or other feedstocks is blended with a traditional, petroleum derived fuel. A blended fuel which includes greater than 5% by volume of the synthetic fuel has an overall improved lifecycle greenhouse gas content of about 2.5% or more compared to the petroleum derived fuel. Also, blending of the low carbon fuel to the traditional, petroleum fuel improves various performance characteristics of the traditional fuel by at least 5%. 1. A blended fuel comprising:(a) about 5% to about 95%, by volume, of a petroleum fuel; and(b) about 95% to about 5%, by volume, of a synthetic fuel produced from a natural gas feedstock, using a thermochemical or biochemical conversion process:wherein the synthetic fuel has a well-to-wheels greenhouse gas content which is at least about 20% lower than a well-to-wheels greenhouse gas content of the petroleum fuel, and the synthetic fuel has at least two performance characteristic values measurable by ASTM tests which are at least about 40% improved than corresponding performance characteristic values of the petroleum fuel; andwherein the blended fuel has a well-to-wheels greenhouse gas content which is at least 1% lower than the well-to-wheels greenhouse gas content of the petroleum fuel, and the blended fuel has at least two performance characteristic values measurable by ASTM tests which are at least about 2% improved than corresponding performance characteristic values of the petroleum fuel.2. The blended fuel of claim 1 , wherein the blended fuel is produced by a process comprising converting a natural gas feedstock into a syngas andreacting the syngas with a catalyst to produce the synthetic fuel.3. The blended fuel of claim 1 , wherein the performance characteristic values are any one of a cetane number claim 1 , a lubricity value claim 1 , a ...

HIGH POWER FUEL COMPOSITIONS

A fuel composition is prepared by blending a petroleum derived low sulphur diesel with a Fischer-Tropsch derived gasoil and a Fischer-Tropsch derived base oil wherein the amount of the petroleum derived low sulphur diesel is from 60% up to 80% v/v of the total composition; the amount of Fischer-Tropsch derived gasoil is from 10% up to 30% v/v of the total composition; the amount of Fischer-Tropsch derived base oil is from 10% up to 30% v/v of the total composition; the amounts of the Fischer-Tropsch derived gas oil and Fischer-Tropsch derived base oil together being at least 20% v/v of the total composition. 1. A fuel composition prepared by blending a petroleum derived low sulphur diesel comprising <50 ppm of sulphur with a Fischer-Tropsch derived gasoil and a Fischer-Tropsch derived base oil wherein the amount of the petroleum derived low sulphur diesel is from 60% up to 80% v/v of the total composition; the amount of Fischer-Tropsch derived gasoil is from 10% up to 30% v/v of the total composition; the amount of Fischer-Tropsch derived base oil is from 10% up to 30% v/v of the total composition; the amounts of the Fischer-Tropsch derived gas oil and Fischer-Tropsch derived base oil together being at least 20% v/v of the total composition; and wherein the petroleum derived low sulphur diesel has a density of 0.81 to 0.865 g/cmat 15° C. and a kinematic viscosity (ASTM D445) from 1.5 to 4.5 mm/s at 40° C.; the Fischer-Tropsch derived gasoil has a density of 0.76 to 0.80 g/cmat 15° C. and a kinematic viscosity (ASTM D445) from 2.0 to 4.5 mm/s at 40° C.; the Fischer-Tropsch derived base oil has a density of 0.79 to 0.82 g/cmat 15° C. and a kinematic viscosity (ASTM D445) from 7.5 to 12.0 mm/s at 40° C.; and wherein the composition has increased power performance in a diesel engine when compared to fuel compositions comprising only a petroleum derived low sulphur diesel comprising <50 ppm of sulphur and a Fischer-Tropsch derived gasoil.2. The fuel composition of claim ...

PYROLYSIS REACTIONS IN THE PRESENCE OF AN ALKENE

Described herein are methods for producing branched alkanes and branched alkenes from the pyrolysis of radical precursors in the presence of one or more alkenes. The branched alkanes and branched alkene have numerous applications as fuels, plat form chemicals, and solvents. 1. A method for producing a fuel or solvent comprising a branched alkane , a branched alkene , or a combination thereof comprising heating a fatty acid in the presence of one or more alkenes to produce the fuel or solvent , wherein the fuel or solvent has less than 5% by weight aromatic compounds.2. A method for producing a fuel or solvent comprising a branched alkane , a branched alkene , or a combination thereof from a fatty acid comprising heating the fatty acid in the presence of one or more alkenes , wherein the fatty acid is separated from a fatty acid resource prior to heating in the presence of the alkene.3. The method of claim 2 , wherein the method for separating the fatty acid from the fatty acid resource comprises (a) separating one or more triglycerides from the fatty acid resource claim 2 , (b) hydrolyzing the triglyceride to produce the free fatty acid claim 2 , and (c) isolating the free fatty acid.4. The method of claim 2 , wherein the fatty acid resource comprises a monoglycerides claim 2 , a diglyceride claim 2 , a triglyceride claim 2 , a lipid claim 2 , a free fatty acid or salt thereof claim 2 , or any combination thereof.5. The method of claim 2 , wherein the fatty acid resource comprises vegetable oil claim 2 , animal fats claim 2 , spent cooking oil claim 2 , lipids derived from biosolids claim 2 , lipids claim 2 , phospholipids claim 2 , triglycerides claim 2 , or a biooil.6. The method of claim 5 , wherein the vegetable oil comprises corn oil claim 5 , cottonseed oil claim 5 , canola oil claim 5 , rapeseed oil claim 5 , olive oil claim 5 , palm oil claim 5 , peanut oil claim 5 , ground nut oil claim 5 , safflower oil claim 5 , sesame oil claim 5 , soybean oil claim 5 , ...

CONFIGURATIONS AND METHOD OF INTEGRATING A GAS TO LIQUIDS (GTL) PLANT IN A REFINERY

A crude oil processing plant that comprises a Fischer-Tropsch reactor is disclosed. The crude oil processing plant comprises a crude oil processing section and a hydrogen production section. The hydrogen production section is coupled to a hydrocracker in the crude oil processing section to deliver a high purity hydrogen stream. The Fischer-Tropsch reactor receives a syngas stream from the hydrogen production section and produces a hydrocarbon stream. When light crude oil is processed, the hydrocracker typically has excess capacities to upgrade the hydrocarbon stream from the Fischer-Tropsch reactor. 1. A crude oil processing plant having a crude oil processing section and a hydrogen production section , wherein the crude oil processing section includes a distillation unit and a hydrocracker , wherein the hydrogen production section includes a steam methane reformer and a shift reactor , and wherein the hydrogen production section is coupled to the hydrocracker to deliver a high purity hydrogen stream , the plant comprising:a Fischer-Tropsch reactor coupled to the steam methane reformer, and the hydrocracker, wherein the Fischer-Tropsch reactor is configured to receive a first portion of a steam methane reformer product stream and produce (i) a hydrocarbon stream to deliver to the hydrocracker and (ii) a tail gas stream to deliver to at least one of the shift reactor and the steam methane reformer.2. The plant of claim 1 , wherein the hydrocracker is configured to receive the hydrocarbon stream claim 1 , the high purity hydrogen stream claim 1 , and a fractionated crude oil from the distillation unit to produce a mixture of a naphtha claim 1 , jet fuel claim 1 , and a diesel product.3. The plant of claim 2 , wherein the hydrocracker is configured to produce the diesel product having a cetane number of at least 45.4. The plant of claim 2 , wherein the distillation column is configured to receive a light crude oil to produce the fractionated crude oil.5. The plant of ...

BIOMASS CONVERSION PROCESS TO HYDROCARBONS

A process for the production of a higher hydrocarbon useful to produce diesel components from solid biomass is provided. The process provides for improved production of diesel components by contacting the stable oxygenated hydrocarbon intermediate containing diols produced from digestion and hydrodoxygenation of the solid biomass to an amorphous silica alumina catalyst to reduce the diols content, and removing water prior to contacting with the condensation catalyst to produce the higher hydrocarbon. 1. A process for the production of a higher hydrocarbon from solid biomass , said process comprising:a. providing a biomass solid containing cellulose, hemicellulose, and lignin;b. digesting and hydrodeoxygenating the biomass solid in a liquid digestive solvent, said digestive solvent containing a solvent mixture having a boiling point of at least 40° C. in the presence of a hydrothermal hydrocatalytic catalyst in the presence of hydrogen at a temperature in the range of from 110° C. to less than 300° C. at a pressure in a range of from 20 bar to 200 bar to form a stable oxygenated hydrocarbon intermediate product having a viscosity of less than 100 centipoise (at 50° C.), a diol content of at least 2 wt %, less than 2wt % of sugar, and less than 2wt % acid (based on acetic acid equivalent), based on the intermediate product, and at least 60% of carbon exists in molecules having 9 carbon atoms or less;c. reacting at least a portion of the stable oxygenated hydrocarbon intermediate product with an acidic amorphous silica alumina catalyst at a temperature in the range from 300° C. to 400° C. thereby producing monooxygenated stream containing water and monooxygenates having a boiling point of at least 40° C.;d. condensing the monooxygenated stream to liquid phase producing an aqueous phase and an organic phase;e. removing at least a portion of aqueous phase from the organic phase to provide a condensed organic stream containing the monooxygenates;f. contacting the ...

PROCESS FOR THE HYDROTREATMENT OF RENEWABLE MATERIALS, WITH AN OPTIMIZED GAS RECYCLE

A process for the hydrotreatment of a feed obtained from renewable sources in which the total stream of feed F is divided into a number of different part-streams of feed F1 to Fn equal to the number of catalytic zones n, where n is 1 to 10. The mass flow rate of hydrogen sent to the first catalytic zone represents more than 80% by weight of the total mass flow rate of hydrogen used. The effluent from the reactor outlet undergoes at least one separation step. A portion of the liquid fraction is recycled to the catalytic zones in a manner such that the local recycle ratio for each of the beds is 2 or less, and the local dilution ratio over each of the beds is less than 4. 1. A process for the hydrotreatment of a feed obtained from renewable sources in order to produce paraffinic hydrocarbons carried out in the presence of hydrogen in a fixed bed reactor having a plurality of catalytic zones disposed in series and each comprising at least one hydrotreatment catalyst , in which:{'sup': −1', '−1', '3', '3, 'a) the total stream of feed F is divided into a number of different part-streams of feed F1 to Fn equal to the number of catalytic zones n, where n is a whole number in the range 1 to 10, in the reactor, the first part-stream of feed F1 being injected into the first catalytic zone Z1, the second part-stream of feed F2 being injected into the second catalytic zone Z2 and so on if n is greater than 2, the hydrotreatment process being operated at a temperature in the range 180° C. to 400° C., at a pressure in the range 0.1 MPa to 15 MPa, at an hourly space velocity in the range 0.1 hto 10 h, and with a ratio of the flow rate of hydrogen to the flow rate of feed in the range 150 to 1500 Nm/m, the mass flow rate of hydrogen sent to the first catalytic zone representing more than 80% by weight of the total mass flow rate of hydrogen used in the hydrotreatment process, in order to produce at least one effluent containing paraffinic hydrocarbons from the reactor outlet,'}b) ...

Gas recycle loops in process for converting municipal solid waste into ethanol

Facilities and processes for generating ethanol from municipal solid waste (MSW) in an economical way via generating a syngas, passing the syngas through a catalytic synthesis reactor, separating fuel grade ethanol, extracting energy at particular strategic points, and recycling undesired byproducts.

SYSTEMS AND METHODS FOR ORGANIC COMPOUND STORAGE AND TRANSFER

A method for mitigating gas and vapor absorption into organic compounds includes degassing an organic compound to generate a degassed organic compound that includes an Ocontent less than or equal to 50% of a saturated value of the organic compound. The method includes transferring the degassed organic compound while preventing contamination of the organic compound through gas absorption. The method includes storing the degassed organic compound in a storage receptacle to mitigate gas and vapor absorption. An organic compound storage and transfer system includes an organic compound source. An organic compound from the organic compound source includes an Ocontent less than or equal to 50% of a saturated value of the organic compound. A storage receptacle is in fluid communication with the organic compound source. An inert gas source is in fluid communication with the storage receptacle to purge the storage receptacle of other gasses and vapors. 1. A method for mitigating gas and vapor absorption into organic compounds , the method comprising:{'sub': '2', 'degassing an organic compound to generate a degassed organic compound that includes an Ocontent less than or equal to 50% of a saturated value of the organic compound;'}transferring the degassed organic compound while preventing contamination of the organic compound through gas absorption; andstoring the degassed organic compound in a storage receptacle to mitigate gas and vapor absorption.2. A method as recited in claim 1 , wherein degassing the organic compound includes degassing by using a membrane.3. A method as recited in claim 1 , further comprising supplying inert gas to the storage receptacle claim 1 , wherein transferring the degassed organic compound includes pumping the degassed organic compound into the storage receptacle supplied with the inert gas.4. A method as recited in claim 3 , wherein supplying inert gas to the storage receptacle includes supplying the inert gas with an on-board inert gas ...

REMOVAL OF HYDROGEN SULFIDE AS AMMONIUM SULFATE FROM HYDROPYROLYSIS PRODUCT VAPORS

A system and method for processing biomass into hydrocarbon fuels that includes processing a biomass in a hydropyrolysis reactor resulting in hydrocarbon fuels and a process vapor stream and cooling the process vapor stream to a condensation temperature resulting in an aqueous stream. The aqueous stream is sent to a catalytic reactor where it is oxidized to obtain a product stream containing ammonia and ammonium sulfate. A resulting cooled product vapor stream includes non-condensable process vapors comprising H, CH, CO, CO, ammonia and hydrogen sulfide.

SYSTEMS AND METHODS FOR HOLISTIC LOW CARBON INTENSITY FUEL PRODUCTION

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

FUEL COMPOSITIONS FROM LIGHT TIGHT OILS AND HIGH SULFUR FUEL OILS

Methods are provided to prepare a low sulfur fuel from hydrocarbon sources, such as light tight oil and high sulfur fuel oil, often less desired by conventional refiners, who split crude into a wide range of differing products and may prefer presence of wide ranges (C3 or C5 to C20 or higher) of hydrocarbons. These fuels can be produced by separating feeds into untreated and treated streams, and then recombining them. Such fuels can also be formulated by combinations of light, middle and heavy range constituents in a selected manner as claimed. Not only low in sulfur, the fuels of this invention are also low in nitrogen and essentially metals free. Fuel use applications include on-board large marine transport vessels but also on-shore for large land based combustion gas turbines, boilers, fired heaters and transport vehicles and trains. 115-. (canceled)16. A process for conversion of one or more hydrocarbonaeous feeds comprising sulfur and metals characterized in that said conversion is directed to a single liquid fuel product , said process comprising{'b': 2', '3', '100', '200, 'claim-text': [{'b': '6', '(i) light overhead still gases (),'}, {'b': '16', '(ii) liquid fractions at or below sulfur breakpoint (), and'}, [{'b': 24', '26', '28', '32, '(A) distillate range fractions comprising sulfur (,,, )'}, {'b': 36', '38, '(B) vacuum gas oil range fractions comprising sulfur (, ) and'}, {'b': '50', '(C) vacuum residue comprising sulfur (), and associated purge gases comprising sulfur'}], '(iii) fractions above sulfur breakpoint comprising'}], '(a) separating said feed (, ) by atmospheric () and vacuum distillation (), into'}{'b': 10', '600, '(b) directing the liquid fractions at or below the sulfur breakpoint (), as untreated liquids, to a combination zone ()'}{'b': 16', '20', '430', '16', '39', '460, 'claim-text': [{'b': 65', '75', '600, '(1) one or more treated liquids (, ) which are directed to a combination zone (), and'}, {'b': '428', '(2) purge gases comprising ...

FUEL COMPOSITIONS FROM LIGHT TIGHT OILS AND HIGH SULFUR FUEL OILS

Methods are provided to prepare a low sulfur fuel from hydrocarbon sources, such as light tight oil and high sulfur fuel oil, often less desired FIG. by conventional refiners, who split crude into a wide range of differing products and may prefer presence of wide ranges (C3 or C5 to C20 or higher) of hydrocarbons. These fuels can be produced by separating feeds into untreated and treated streams, and then recombining them. Such fuels can also be formulated by combinations of light, middle and heavy range constituents in a selected manner as claimed. Not only low in sulfur, the fuels of this invention are also low in nitrogen and essentially metals free. Fuel use applications include on-board large marine transport vessels but also on-shore for large land based combustion gas turbines, boilers, fired heaters and transport vehicles and trains. 114-. (canceled)15. Combustion in marine or land based engines , combustion gas turbines , or fired heaters of a fuel comprising light tight oil and processed high sulfur fuel oil , wherein{'b': 41', '401, 'claim-text': [{'b': '411', '(1) hydroconverted liquids () and'}, {'b': 409', '301', '311', '401, '(2) unconverted oils () directed to solvent separation () to form soluble deasphalted oil () for recycle as feed to said hydroconversion zone (), either separately or combined with added high sulfur fuel oil feed to said reactor and'}], '(a) said processed high sulfur fuel oil () has been processed in a residue hydroconversion zone () by contact with hydrogen in presence of catalyst at residue hydroconversion conditions in an ebullated-bed reactor to form'}{'b': 1', '15, 'i': 'a', '(b) all or one or more portions of a light tight oil () is combined with said processed high sulfur fuel oil of .() to form said fuel.'}1628-. (canceled)29. Combustion in marine or land based engines , combustion gas turbines , or fired heaters of a single fuel product of one or more hydrocarbonaeous feeds comprising sulfur and metals , said fuel ...

FUEL COMPOSITIONS FROM LIGHT TIGHT OILS AND HIGH SULFUR FUEL OILS

Methods are provided to prepare a low sulfur fuel from hydrocarbon sources, such as light tight oil and high sulfur fuel oil, often less desired by conventional refiners, who split crude into a wide range of differing products and may prefer presence of wide ranges (C3 or C5 to C20 or higher) of hydrocarbons. These fuels can be produced by separating feeds into untreated and treated streams, and then recombining them. Such fuels can also be formulated by combinations of light, middle and heavy range constituents in a selected manner as claimed. Not only low in sulfur, the fuels of this invention are also low in nitrogen and essentially metals free. Fuel use applications include on-board large marine transport vessels but also on-shore for large land based combustion gas turbines, boilers, fired heaters and transport vehicles and trains. 147-. (canceled)48. A formulated combination useful as a fuel characterized in that it is formed by combining a range of hydrocarbons of (L)+(M)+(H) and the resulting final combination has the following properties:(a) sulfur from 0.05 wt. % (500 ppmwt) to 0.25 wt. % (2500 ppmwt),(b) final combination density from 820 to 880 Kg/M3 at 15° C.,(c) total metals of 25 ppmwt or less,(d) HHV from 43.81 to 45.15 MJ/kg, and(e) LHV from 41.06 to 42.33 MJ/kgwherein,(f) wherein (L) comprises components of naphtha and kerosene range materials, which are refined or partially refined, unrefined or extracted and used without being subject to any fractionation, hydrotreating or other treatment process, except optional separation of light gases or water, having an initial boiling point of 38° C. (100° F.) or less having a ninety percent (90%) plus final boiling point of 190° C. (374° F.) to about 205° C. (401° F.), where (L) range components contribute to (L) range bulk density and to final combination density even though individual constituents of (L) may fall outside said combination density range(g) wherein (M) comprises refined or partially refined ...

Low sulfur fuel with adequate combustion quality

Fuel compositions that are low sulfur and have adequate combustion quality are disclosed. An example fuel composition that is low sulfur may have the following enumerated properties: a sulfur content of about 0.50% or less by weight of the fuel composition; a calculated carbon aromaticity index of about 870 or less; a density at 15° C. of about 900 kg/m3 to about 1,010 kg/m3; a kinematic viscosity at 50° C. of about 100 centistokes to about 700 centistokes; and an estimated cetane number of about 7 or greater.

SYSTEMS AND METHODS FOR HOLISTIC LOW CARBON INTENSITY FUEL PRODUCTION

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

Renewable High Density Turbine And Diesel Fuels From Sesquiterpenes

A fuel and method for conversion of sesquiterpenes to high density fuels. The sesquiterpenes can be either extracted from plants or specifically produced by bioengineered organisms from waste biomass. This approach allows for the synthesis of high performance renewable fuels. 1. A method for manufacturing jet and diesel fuels , comprising:providing pure and/or mixed sesquiterpenes isolated from plant extracts and/or biosynthesized from biomass;purifying said pure and/or mixed sesquiterpenes to produce single components or mixtures of sesquiterpenes; directly hydrogenating said single component or mixed sesquiterpenes with at least one hydrogenation catalyst under hydrogen pressure; or', 'isomerizing either with or without a solvent, said single component or mixed sesquiterpenes with at least one heterogeneous acid catalyst to produce isomers and hydrogenating said isomers with at least one hydrogenation catalyst under hydrogen pressure; and, 'converting said single component or mixed sesquiterpenes by either,'}distilling either said hydrogenated single component or mixed sesquiterpenes or said hydrogenated isomers to produce high density fuels.2. The method according to claim 1 , wherein said pure and/or mixed sesquiterpenes are selected from the group consisting of valencene claim 1 , premnaspirodiene claim 1 , caryophyllene claim 1 , humulene claim 1 , clovene claim 1 , neoclovene claim 1 , panasinsene claim 1 , thujopsene claim 1 , longifolene claim 1 , cubebene claim 1 , zizaene claim 1 , santalene claim 1 , longipinene claim 1 , isomers of the above sesquiterpenes claim 1 , other cyclic terpenes claim 1 , and any mixtures thereof.3. The method according to claim 1 , wherein said single component or mixed sesquiterpenes are selected from the group consisting of caryophyllene claim 1 , valencene claim 1 , premnaspirodiene claim 1 , or any mixture thereof.4. The method according to claim 1 , wherein said isomers are at least one isomer selected from the group ...

METHOD FOR PRODUCING FUEL OIL

Provided is a method that is for producing fuel oil and that can cheaply and highly efficiently produce a fuel oil—or starting material thereof—having as the primary component n-paraffin or isoparaffin from a starting material oil containing a fatty acid alkyl ester, even while reducing hydrogen pressure. The method for producing fuel oil has a step for producing fuel oil having one or both of n-paraffin and isoparaffin as the primary component by contacting hydrogen gas and a starting material oil containing a fatty acid alkyl ester under the condition of a hydrogen pressure of no greater than 1 MPa to a catalyst resulting from supporting on a porous metal oxide support one or more metal elements belonging to group nine or group ten of the periodic table, and one or more group six element oxides belonging to group six of the periodic table. The weight ratio of the group six elements to the metal elements contained in the catalyst is no greater than 1.0 in terms of the metal. 1. A method for producing fuel oil , comprising:a step for producing a fuel oil composed mainly of one or both of n-paraffin and isoparaffin by contacting:a base oil containing fatty acid alkyl ester, andhydrogen gaswith a catalyst, obtained by supporting one or a plurality of metal elements belonging to group 9 or group 10 of the periodic table and one or a plurality of group 6 element oxides belonging to group 6 of the periodic table on a porous metal oxide support, under conditions of a hydrogen pressure of 1 MPa or less;wherein,the weight ratio as metal of the group 6 element contained in the catalyst to the metal element does not exceed 1.0.2. The method for producing fuel oil according to claim 1 , wherein the metal element is nickel and/or cobalt claim 1 , and the group 6 element is molybdenum and/or tungsten.3. The method for producing fuel oil according to claim 2 , wherein the metal element is nickel and the group 6 element is molybdenum.4. The method for producing fuel oil according ...

HYDROCARBON SYNTHESIS METHODS, APPARATUS, AND SYSTEMS

Embodiments of the invention include apparatus and systems for hydrocarbon synthesis and methods regarding the same. In an embodiment, the invention includes a method for creating a hydrocarbon product stream comprising reacting a reaction mixture in the presence of a catalyst inside of a reaction vessel to form a product mixture, the reaction mixture comprising a carbon source and water. The temperature inside the reaction vessel can be between 450 degrees Celsius and 600 degrees Celsius and the pressure inside the reaction vessel can be above supercritical pressure for water. In an embodiment, the invention includes an extrusion reactor system for creating a hydrocarbon product stream. The temperature inside the extrusion reactor housing between 450 degrees Celsius and 600 degrees Celsius. Pressure inside the reaction vessel can be above supercritical pressure for water. Other embodiments are also included herein. 1. A method for creating a hydrocarbon product stream comprising:reacting components of a reaction mixture in the presence of a catalyst to form a product mixture, the reaction mixture comprising a carbon source and water, wherein the reaction takes place inside a reaction vessel;wherein the temperature inside the reaction vessel is between 450 degrees Celsius and 600 degrees Celsius and the pressure inside the reaction vessel is above supercritical pressure for water;wherein the catalyst comprises a metal oxide.2. The method of claim 1 , wherein the reaction mixture includes at least about 50% water by mass.3. The method of claim 1 , wherein the carbon source includes one or more selected from the group consisting of carboxylic acids claim 1 , fatty acids claim 1 , triglycerides claim 1 , and carbohydrates.4. The method of claim 1 , wherein the reaction vessel is part of an extrusion system.5. The method of claim 1 , wherein the catalyst comprises a metal oxide that is stable at temperatures above 450 degrees Celsius in the presence of supercritical ...

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

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