СПОСОБ ОЧИСТКИ ПОТОКА БУТАДИЕНА УДАЛЕНИЕМ ПОБОЧНЫХ ПРОДУКТОВ, ОБРАЗОВАВШИХСЯ НА СТАДИИ ИЗБИРАТЕЛЬНОЙ ГИДРОГЕНИЗАЦИИ ПРИМЕСЕЙ

Изобретение относится к технологии выделения и очистки бутадиена, получаемого термокрекингом углеводородов, с последующим удалением тяжелых побочных продуктов из неочищенного потока бутадиена после избирательной гидрогенизации нежелательных примесей. Поток, выходящий из зоны реакции избирательной гидрогенизации, подают в испаритель для экстракции бутадиена, содержащий фракционную зону, которую орошают потоком рафината из зоны экстракции бутадиена. Из испарителя отводят паровую фазу, содержащую бутадиен с пониженной концентрацией тяжелых побочных продуктов, удаляют и направляют на стадию выделения концентрированную жидкую фазу, содержащую тяжелые побочные продукты реакции. Паровую фазу, содержащую бутадиен, возвращают в зону экстракции бутадиена. Фракционная зона содержит от 3 до 7 теоретических тарелок. В испарителе поддерживают температуру от 27 до 93°С и давление от 375 до 790 кПа. Технический результат - усовершенствование технологии получения очищенного бутадиена. 4 з.п. ф-лы, 1 ил.

СОЧЕТАНИЕ МЕМБРАННОГО СПОСОБА И АДСОРБЦИИ С ПЕРЕМЕННЫМ ДАВЛЕНИЕМ В УСТАНОВКЕ ПОЛУЧЕНИЯ ИЗОБУТАНА И АЗОТА

Изобретение в целом относится к производству полиэтилена. Способ разделения компонентов в системе производства полимеров включает: (а) разделение потока продукта полимеризации на поток газа и поток полимеров, при этом поток полимеров содержит полиэтилен, изобутан, этилен и этан; (b) контактирование по меньшей мере части потока полимера с продувочным газом в продувочном сосуде для производства потока продуваемого полимера и потока отработанного продувочного газа, при этом поток продуваемого полимера содержит полиэтилен и при этом поток отработанного продувочного газа содержит продувочный газ, изобутан, этилен и этан; (с) введение по меньшей мере части потока отработанного продувочного газа в компрессордля производства потока сжатого газа; (d) введение по меньшей мере части потока сжатого газа в первый блок разделения для производства первого потока углеводородов и сырьевого потока мембранного блока, при этом первый поток углеводородов содержит не менее чем 50% изобутана в потоке сжатого ...

СПОСОБЫ ПРИМЕНЕНИЯ ОКСИДА АЗОТА ДЛЯ ИНГИБИРОВАНИЯ ОБРАЗОВАНИЯ ГУБЧАТОГО ПОЛИМЕРА В ТЕЧЕНИЕ ПЕРЕРАБОТКИ БУТАДИЕНА

Настоящее изобретение относится к способу ингибирования образования губчатого полимера 1,3-бутадиена в течение экстракции и очистки. Способ включает введение потока углеводородов, содержащего 1,3-бутадиен, в дистилляционную установку, периодическое добавление в верхнюю часть дистилляционной установки газового потока, содержащего ингибитор полимеризации для уменьшения полимеризации 1,3-бутадиена. Ингибитор полимеризации включает оксид азота в концентрации 100-500 частей на миллион газового потока. После чего проводят дистилляцию 1,3-бутадиена из потока углеводородов. Также предложены варианты способа. Технический результат – эффективное ингибирование образования губчатого полимера в паровой фазе бутадиеновой дистилляционной установки. 3 н. и 6 з.п. ф-лы, 2 ил., 1 табл., 3 пр.

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Настоящее изобретение относится к способу выделения олефина из газового потока, содержащего олефин и, по меньшей мере, один другой компонент, при этом упомянутый способ включает ! (i) сжатие и охлаждение газового потока; ! (ii) отделение олефина от газового потока путем абсорбции олефина абсорбентом; ! (iii) выделение олефина из абсорбента путем десорбции; ! причем сжатие или охлаждение или сжатие и охлаждение на стадии (i) осуществляют, по меньшей мере, два раза. Применение данного способа позволяет более эффективно извлекать олефин из газового потока, а также выделять олефин из газового потока, содержащего кислород, путем абсорбции, без дополнительной подачи инертного газа. 22 з.п. ф-лы, 2 ил.

СПОСОБ ПОЛУЧЕНИЯ БУТАДИЕНА И ВОДОРОДА ИЗ ЭТАНОЛА В ДВЕ РЕАКЦИОННЫЕ СТАДИИ ПРИ НИЗКОМ РАСХОДЕ ВОДЫ И ЭНЕРГИИ

Изобретение относится к способу получения бутадиена из этанольного сырья, содержащего по меньшей мере 80 вес.% этанола, включающему по меньшей мере стадию A) превращения этанола в ацетальдегид, стадию B) превращения смеси этанол/ацетальдегид в бутадиен, стадию C1) обработки водорода, стадию D1) экстракции бутадиена, стадию D2) первой очистки бутадиена, стадию D3) дальнейшей очистки бутадиена, стадию E1) обработки выходящих потоков, стадию E2) удаления примесей и коричневых масел и стадию F) промывки водой. Предложенный способ позволяет увеличить производительность и уменьшить количество выбросов. 14 з.п. ф-лы, 2 пр., 7 ил.

СПОСОБ (ВАРИАНТЫ) И СИСТЕМЫ ПОЛУЧЕНИЯ ИЗОФТАЛЕВОЙ И ТЕРЕФТАЛЕВОЙ КИСЛОТ

Изобретение относится к усовершенствованному способу конверсии потока сырья, содержащего по меньшей мере одно C-ароматическое соединение, орто-ксилол, мета-ксилол, пара-ксилол и этилбензол, по меньшей мере в один поток продуктов, содержащий изофталевую кислоту и терефталевую кислоту (IPA/TA), который включает стадии: a) удаление этилбензола из указанного потока сырья с образованием потока сырья, обедненного этилбензолом; b) удаление opmo-ксилола из указанного обедненного этилбензолом потока сырья с образованием потока сырья, обедненного opmo-ксилолом, содержащего мета-ксилол и пара-ксилол; c) окисление указанного обедненного opmo-ксилолом потока сырья с образованием потока продуктов, содержащего IPA/TA в соотношении от 0,5% до 99,5% IPA и от 0,5 до 99,5% TA; d) сушка указанного потока продукта в сушилке для удаления остаточных растворителя и воды; e) удаление по существу очищенного потока продуктов IPA/TA; f) растворение указанного потока продуктов; и g) отделение указанного IPA и указанного ...

СПОСОБ ПОДГОТОВКИ УГЛЕВОДОРОДНОГО ГАЗА

Изобретение относится к способам подготовки углеводородных газов путем низкотемпературной сепарации и может быть использовано для подготовки попутного нефтяного газа в нефтяной промышленности. Углеводородный газ 1 компримируют на первой ступени 2 с охлаждением компрессата внешним хладагентом в условиях дефлегмации,с получением конденсата 4 и сжатого газа 5, который компримируют на второй ступени 6 с охлаждением компрессата внешним хладагентом (не показан) и газом низкотемпературной сепарации, который затем выводят в качестве подготовленного газа 7, с получением конденсата 8 и сжатого газа 9, который редуцируют с помощью устройства 10 и разделяют на подготовленный газ 7 и конденсат 12, который редуцируют с помощью устройства 13 и деэтанизируют в сепараторе 16 совместно с редуцированными в устройствах 14 и 15 конденсатами 4 и 8 первой и второй ступеней 2 и 6 с получением товарного конденсата 17 и газа деэтанизации 3, который рециркулируют на первую ступень 2 компримирования. При необходимости ...

ЭНЕРГОСБЕРЕЖЕНИЕ ПРИ ДИСТИЛЛЯЦИИ ТЯЖЕЛЫХ УГЛЕВОДОРОДОВ

Изобретение относится к способу производства отдельного изомера ксилола из исходных сырьевых потоков, содержащих ароматические соединения С8, ароматические соединения С9 и более тяжелые ароматические соединения. Способ включает: (а) процесс дистилляции, включающий использование двух ксилольных колонн, отделяющих ароматические соединения С8 от ароматических соединений С9 и более тяжелых ароматических соединений, содержащихся по меньшей мере в одном потоке сырья с более низкой температурой кипения и по меньшей мере в одном потоке сырья с более высокой температурой кипения, при этом указанный по меньшей мере один поток сырья с более высокой температурой кипения имеет более высокое содержание ароматических соединений С9 и более тяжелых ароматических соединений, по сравнению по меньшей мере с одним потоком сырья, имеющим более низкую температуру кипения; процесс дистилляции включает дистилляцию по меньшей мере одного потока исходного сырья, имеющего более высокую температуру кипения, в первой ...

СПОСОБ ОЧИСТКИ СТИРОЛА С ИСПОЛЬЗОВАНИЕМ СОВМЕСТНОГО ДЕЙСТВИЯ РЕБОЙЛЕРОВ C ПАДАЮЩЕЙ ПЛЕНКОЙ И ТЕХНОЛОГИИ ТЕПЛОВОГО НАСОСА С ЦЕЛЬЮ ПОЛУЧЕНИЯ ИСТОЧНИКА ТЕПЛА ДЛЯ РАЗДЕЛИТЕЛЬНОЙ КОЛОННЫ

Изобретение относится к способу очистки стирола с использованием ребойлеров с падающей пленкой и технологии теплового насоса с целью получения источника тепла, необходимого для разделительной колонны. Согласно способу, основанному на существующей энергосберегающей технологии соединенных колонн выделения этилбензола и стирола высокого и низкого давления, высококонцентрированный газообразный этилбензол, выделенный из верхней части колонны выделения этилбензола и стирола низкого давления, подвергается непосредственному сжатию компрессором, или рабочая среда теплового насоса газифицируется с использованием высококонцентрированного газообразного этилбензола, выделенного из верхней части колонны выделения этилбензола и стирола низкого давления, при этом газифицированная рабочая среда теплового насоса подвергается сжатию. Газообразный этилбензол высокой концентрации, подвергаемый непосредственному сжатию, или газифицированный и находящийся под давлением газообразный этилбензол высокой концентрации ...

СПОСОБ РАЗДЕЛЕНИЯ ПОТОКА, ВЫХОДЯЩЕГО С ЭТАПА ОЛИГОМЕРИЗАЦИИ

Изобретение относится к способу обработки потока, выходящего с этапа олигомеризации, включающему этап нейтрализации указанного потока с целью дезактивации каталитической композиции и последующий этап термического разделения нейтрализованного потока. Способ включает: первый этап выпаривания, выполняемый при давлении от 2,0 до 5,0 МПа и температуре от 70 до 150°C, позволяющий получить жидкую фракцию, направляемую на второй этап выпаривания, и газообразную фракцию, предпочтительно направляемую в секцию дистилляции, указанный второй этап выпаривания, проводимый при давлении от 0,5 до 3,0 МПа и температуре от 70 до 150°C, что позволяет получить жидкую фракцию и газообразную фракцию, и указанная газообразная фракция предпочтительно направляется в секцию дистилляции, причем давление на первом этапе выпаривания выше давления на втором этапе выпаривания по меньшей мере на 0,5 МПа. Использование предлагаемого способа позволяет повысить получение желаемых олефинов и ограничить расходы, связанные с ...

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 РАЗДЕЛЕНИЯ ГАЗОВОГО ПОТОКА И УСТРОЙСТВО ДЛЯ ЕГО ОСУЩЕСТВЛЕНИЯ (ВАРИАНТЫ)

Поток углеводородного газа, содержащего компоненты С1, С2 и С3, разделяют на летучую фракцию, включающую основную часть С1 и C2, и на более тяжелые углеводородные компоненты, содержащие основную часть пропана и пропилена. Поток охлаждается и/или расширяется до частичной конденсации, затем разделяется с получением первого потока пара, который направляется в контактирующее устройство (абсорбер), где отделяют третий поток пара и поток жидкости, содержащей C3. Поток жидкости, содержащей C3, направляется в дистилляционную колонну, где отделяется второй поток пара, содержащий основную часть компонентов C3 и более тяжелых углеводородных компонентов. Затем второй поток пара подвергается тепловому обмену с третьим потоком пара для охлаждения второго потока пара и конденсации, по крайней мере, его части с образованием конденсированного потока. По крайней мере, часть конденсированного потока направляется в контактирующее устройство (абсорбер) для тесного контакта с первым потоком пара. Оставшаяся ...

СИСТЕМА ОБРАБОТКИ ИОННО-ЖИДКОСТНОГО КАТАЛИЗАТОРА

Изобретение относится к усовершенствованному способу удаления ионной жидкости из технологического потока, включающему в себя стадии, на которых: вводят технологический поток в коалесцентное устройство для образования потока ионной жидкости и первого обработанного технологического потока, имеющего концентрацию ионной жидкости, меньшую её концентрации в технологическом потоке; и вводят первый обработанный технологический поток в разделительное устройство для образования второго обработанного технологического потока, при этом второй обработанный технологический поток имеет концентрацию ионной жидкости, меньшую её концентрации в первом обработанном технологическом потоке, причем указанное разделительное устройство выбрано из песочного фильтра, зоны электростатического разделения или их сочетания, причем концентрация ионной жидкости во втором обработанном технологическом потоке составляет меньше 40 мас. ч/млн. 5 з.п. ф-лы, 2 пр., 1 ил.

СПОСОБ ОБРАБОТКИ ДИЦИКЛОПЕНТАДИЕНОВОГО МОНОМЕРА

... 1. Способ обработки, включающий обработку, по меньшей мере, одной композиции мономера, полимеризуемой с помощью реакции метатезиса, имеющей чистоту меньше, чем 95% масс. дициклопентадиенового мономера, с помощью добавки для обработки, до полимеризации композиции мономера, полимеризуемого с помощью реакции метатезиса, так что для обработанной композиции, отверждаемой с помощью реакции метатезиса, используется пониженное количество катализатора реакции метатезиса, по сравнению с отверждаемой необработанной композицией.2. Способ по п. 1, в котором добавка для обработки содержит щелочной металл, окисленный щелочной металл или их смеси.3. Способ по п. 2, в котором щелочной металл содержит натрий, калий или смеси их.4. Способ по п. 2, в котором окисленный щелочной металл содержит NaO, KO или их смеси.5. Способ по п. 1, в котором добавка для обработки наносится в виде покрытия на твердый носитель, и твердый носитель выбирают из группы, состоящей из оксида алюминия, оксида кремния, углерода, цеолитов ...

СПОСОБ ОКИСЛИТЕЛЬНОГО ДЕГИДРИРОВАНИЯ С УЛУЧШЕННОЙ РЕГУЛИРУЕМОСТЬЮ ДЛЯ ПОЛУЧЕНИЯ БУТАДИОНА

... 1. Способ получения бутадиена из бутенобогащенного питания, содержащий следующие стадии:обеспечение бутенобогащенного углеводородистого питания, испаривания и перегревания указанного бутенобогащенного углеводородистого питания при температуре, по меньшей мере, примерно 345°C (650°F), смешение указанного бутенобогащенного углеводородистого питания с перегретым водяным паром и кислородобогащенным газом с образованием потока реакторного питания;обеспечение каталитического слоя гранул катализатора окислительного дегидрирования, прохождение указанного потока реакторного питания из впуска через указанный каталитический слой и образование в результате потока бутадиенобогащенного продукта;обеспечение указанного каталитического слоя катализатора окислительного дегидрирования связанным с ним множеством температуровоспринимающих устройств, предназначенных для измерения температуры в слое по направлению потока;регулирование условий на впуске указанного реактора, так что реакции окислительного дегидрирования ...

ДЕЗОДОРИРУЮЩАЯ СЕРООЧИСТКА ПРИРОДНОГО ГАЗА ПОСРЕДСТВОМ МЕМБРАННОГО КОНТАКТНОГО АППАРАТА

СПОСОБ УВЕЛИЧЕНИЯ ВЫХОДА ИЗ ЗОНЫ ИЗОМЕРИЗАЦИИ

Изобретение относится к способу увеличения выхода из зоны изомеризации, который включает отделение части Сциклических углеводородов от потока нафты, содержащего Суглеводороды, для получения потока, обедненного по Сциклическим углеводородам; отделение изоCуглеводородов, изоCуглеводородов и изоCуглеводородов от потока, обедненного по Сциклическим углеводородам; и направление по меньшей мере одного потока, обогащенного по изоСуглеводородам, изоCуглеводородам, изоCуглеводородам или их комбинации, в зону изомеризации. Способ позволяет эффективно и действенно превращать изоуглеводороды в нормальные парафины в одной и той же зоне изомеризации. 9 з.п. ф-лы, 1 ил., 1 табл.

УЛУЧШЕННАЯ РЕКУПЕРАЦИЯ ТЕПЛА НА УСТАНОВКЕ ПОЛУЧЕНИЯ ПАРАКСИЛОЛА

СПОСОБ ОЧИСТКИ ХИМИЧЕСКИХ СОЕДИНЕНИЙ СТОЧНЫХ ВОД ЦЕЛЛЮЛОЗНО-БУМАЖНЫХ КОМБИНАТОВ

... 1. Способ обогащения или выделения целевого соединения из сточных вод целлюлозно-бумажного комбината, при этом способ предусматривает следующие стадии:- получение конденсата из выпарного аппарата или ретентата процесса обратного осмоса (RO) конденсатов на целлюлозно-бумажном комбинате, или обоих, при этом конденсат, ретентат или оба из них по существу не содержат высокомолекулярную целлюлозу и/или лигнин, и/или происходящие из лигнина материалы,- экстрагирование конденсата органическим растворителем методом твердофазной экстракции (SPE), экстракции в системе жидкость-жидкость или твердое тело-жидкость с получением экстракта, содержащего указанные целевые соединения, и- необязательно очистка целевого соединения из экстракта путем термического фракционирования, хроматографического разделения (такого как нормально-фазовое, обращенно-фазовое, афинное или их комбинации), рекристаллизации, ионного обмена, хелатирования, адсорбции/десорбции, лиофилизации и сублимации или их комбинаций.2. Способ ...

СПОСОБ УДАЛЕНИЯ МЕТИЛАЦЕТИЛЕН/ПРОПАДИЕНА (МАПД) ИЗ УГЛЕВОДОРОДНЫХ ПОТОКОВ

... 1. Способ удаления метилацетилена и пропадиена из С3 и более высококипящего углеводородного потока, включающий стадии: (a) подачи С3 и более высококипящего потока, содержащего метилацетилен и пропадиен, в первую перегонную колонну, где С3 отбирают в виде первого головного потока, a C4 и более высококипяшие материалы отбирают в виде первого нижнего недогона; (b) подачи первого головного потока и водорода в перегонную колонну-реактор; (c) одновременно в указанной перегонной колонне-реакторе (i) контактирования указанных метилацетилена и пропадиена с водородом в реакционной зоне с катализатором гидрирования, в результате чего указанные метилацетилен и пропадиен реагируют с указанным водородом с образованием пропилена, и (ii) отделения содержащегося пропилена дробной перегонкой; (d) отведения отделенного пропилена вместе с любым количеством пропана и более легких соединений, включая непрореагировавший водород, из указанной перегонной колонны-реактора в виде второго головного потока. 2. Способ ...

СПОСОБЫ ПРИМЕНЕНИЯ ОКСИДА АЗОТА ДЛЯ ИНГИБИРОВАНИЯ ОБРАЗОВАНИЯ ГУБЧАТОГО ПОЛИМЕРА В ТЕЧЕНИЕ ПЕРЕРАБОТКИ БУТАДИЕНА

МЕМБРАНЫ ДЛЯ ОБРАТНОГО ОСМОСА УГЛЕВОДОРОДОВ И СПОСОБ ИХ ПОЛУЧЕНИЯ

СПОСОБЫ И УСТАНОВКИ ДЛЯ ИЗВЛЕЧЕНИЯ ЭТИЛЕНА ИЗ УГЛЕВОДОРОДОВ

Способ выделения ароматических углеводородов из их смесей с неароматическими

Способ выделения ароматических углеводородов

VERFAHREN ZUR KAPAZITAETSSTEIGERUNG EINER EXTRAKTIONSANLAGE ZUR GEWINNUNG VON BUTADIEN-(1,3) AUS C(PFEIL ABWAERTS)4(PFEIL ABWAERTS)-KOHLENWASSERSTOFFGEMISCHEN UNTER GLEICHZEITIGER GEWINNUNG VON BUTEN-(2)

Sepn. of highly pure ethylene and propylene - from gas mixts. obtd. by hydrogenation of pyrolysed petroleum distillates

The gaseous mixt. comprises H2, methane, ethylene, acetylene hydrocarbons propylene, propane and traces of satd. 4C hydrocarbons. It is first hydrogenated to remove the acetylene hydrocarbons, the residual mixt. being cooled to very low temps. to abtain a condensate and an H2/methane gas mixt. which is sepd. The condensate is demethanised by rectification to obtain a still residue contg. ethylene, ethane, propane, propylene and satd. 4C hydrocarbons. This still residue is then rectified at a still temp. of 52-60 degrees C to obtain highly pure ethylene; the still residue is further rectified to obtain ethane and the residue obtd. rectified again to obtain highly pure propylene. Sepn. of thje ethylene, ethane and propylene is effected in separate rectifying columns. A suitable plant is described. Economy in energy and cost is achieved; no compressors are needed. Ethylene and proplene are obtd. in purities of up to 99.9 vol. %.

Verfahren zur Entfernung von Kohlendioxid aus Biogas mittels einer aminhaltigen Waschlösung und Regeneration der anfallenden beladenen Waschlösung

Verfahren zur Entfernung von Kohlendioxid aus Biogas mittels einer aminhaltigen Waschlösung mit Aktivatorzusatz und Regeneration der anfallenden beladenen Waschlösung, die im Kreislauf gefahren wird, dadurch gekennzeichnet, dassa) das zu reinigende Biogas vor der Absorption auf einen Taupunkt von unter 20 °C entfeuchtet und mit einer Temperatur von 30 bis 70 °C mindestens einer Absorptionsstufe zugeführt wird,b) zur Absorption von COaus Biogas eine Waschlösung mit einer Temperatur von 40 bis 70 °C und einem Sauerstoffgehalt von unter 0,5 mg/l eingesetzt wird undc) die beladene Waschlösung zur Austreibung von COmindestens in einer Regenerationsstufe einer Behandlung mittels eines Strippprozesses unter Verwendung von Luft als Strippmedium bei einer Temperatur von 95 °C bis 115 °C unterzogen wird, wobei eine gereinigte Waschlösung mit einer Restbeladung von unter 45 g CO/l und einem Gehalt an Sauerstoff von ≤ 0,5 mg/l erhalten wird.

Verfahren zur Trennung von aromatischen C8-Kohlenwasserstoffmischungen

Verfahren zur Abtrennung von Isopren aus einer Kohlenwasserstofffraktion

Verfahren und Vorrichtung zur Abtrennung von AEthylen aus einem gasfoermigen Gemisch, welches leichtere und schwerere Bestandteile als AEthylen enthaelt

Verfahren zur Herstellung von Reinfraktionen aus Rohbenzol

VERFAHREN ZUR HERSTELLUNG VON BUTADIEN

Verfahren zur Abtrennung von Phenol

RÜCKGEWINNUNG EINES SEKUNDÄREN ÄTHYLENSTROMES AUS EINEM ÄTHYLENREINIGUNGSVERFAHREN

Verfahren und Anlage zur Herstellung von Olefinen aus Oxygenaten

Verfahren zur Herstellung von Olefinen aus Oxygenaten, umfassend die folgenden Schritte:(i) heterogen-katalysierte Umsetzung von wenigstens einem Oxygenat zu einem flüssige und gasförmige organische Verbindungen und Wasser enthaltenden Gesamtstrom und(ii) Auftrennung des Gesamtstroms in einer ersten Trenneinrichtung in eine zu wenigstens 90 Vol.-% die gasförmigen organischen Verbindungen des Gesamtstroms enthaltende Fraktion, in eine zu wenigstens 90 Gew.-% die flüssigen organischen Verbindungen des Gesamtstroms enthaltende Fraktion und in eine zu wenigstens 90 Gew.-% das Wasser des Gesamtstroms enthaltende Fraktion,iii) Auftrennen der zu wenigstens 90 Vol.-% die gasförmigen organischen Verbindungen des Gesamtstroms enthaltenden Fraktion in einer zweiten Trenneinrichtung in eine C-Verbindungen und Wasser enthaltende Fraktion und eine C-Verbindungen und Oxygenate enthaltende Fraktion,iv) Trocknen der die C-Verbindungen und Wasser enthaltenden Fraktion in einer dritten Trennvorrichtung, so ...

VERFAHREN ZUR ABSONDERUNG UND REINIGUNG VON ANTHRACEN AUS ANTHRACENOEL

VERFAHREN ZUR GEWINNUNG VON P-XYLOL

Verfahren zur Trennung von Kohlenwasserstoffgemischen

Process for preventing the formation of insoluble deposits on heating and evaporating crude benzene

In the purification of benzene by heating and evaporating, the formation of solid deposits is inhibited by pretreating with an aqueous alkaline wash liquid containing a reducing agent. The alkali is preferably caustic alkali of 1-50% concentration which may also contain small amounts of alkali sulphide or is volatile e.g. an amine or ammonia; the amount of wash liquid used is 1-30% by volume of the benzene. The reducing agent may be organic or inorganic, e.g. a phenol, amine, or aminophenol, or a sulphite, stannite, arsenite or aluminium or zinc powder; generally 0.01-1 g. per litre of benzene is used. Preferably the temperature is raised slightly, e.g. to 50 DEG C. to assist the process.

Method for producing para-xylene by high temperature crystallisation in at least one stage and partial crystal fusion

ISOPRENE RECOVERY PROCESS

... 1344219 Distilling hydrocarbons SHELL INTERNATIONALE RESEARCH MAATSCHAPPIJ NV 24 Aug 1972 [26 Aug 1971] 39416/72 Heading C5E Isoprene is recovered from a mixture containing also cyclopentadiene and other C 5 -unsaturated hydrocarbons by a process including two extractive-distillation steps and a solventstripping step. The greater part of the cyclopentadiene is taken off in bottoms from the first extractive distillation, the remainder with the isoprene in the bottoms from the second extractive distillation. This second bottoms is stripped and three streams obtained: isoprene overhead. a cyclopentadiene-enriched sidestream and solvent bottoms, which last is recycled, in part to the top of each extractive-distillation zone, and in part to the top of the stripping zone. Suitable solvents are acetonitrile, acetone, furfural, dimethylformamide, dioxane, phenol, N- methylpyrrolidone and their aqueous mixtures. As shown, a C 5 fraction obtained as a byproduct of the cracking of naphtha to ethylene ...

PRODUCTION OF PURE CONJUGATED C4 AND C5 DIOLEFINS FROM HYDROCARBON MIXTURES

... 1401875 Extracting C 4 or C 5 conjugated diolefins BADISCHE ANILIN-& SODAFABRIK AG 24 Nov 1972 [26 Nov 1971] 54360/72 Heading C5E Pure C 4 or C 5 conjugated diolefins are separated from hydrocarbon mixtures by countercurrent gas scrubbing liquid-liquid extraction, extractive distillation and/or countercurrent distribution using as selective solvent a mixture of:- (a) 5-95 wt. per cent of an N-alkylpyrrolidone which may contain an inert substituent; and (b) 5-95 wt. per cent of an N-hydroxyalkyl compound of the general formula in which Y is C 2 or C 3 alkylene or alkenylene, or o-phenylene which may be wholly or partly hydrogenated R is a linear or branched alkylene and Z is oxygen or two hydrogens. The solvent mixture may contain up to 25 wt. per cent water. Preferred solvent components are (a) N-methylpyrrolidone; (b) N-hydroxyethylphthalimide, N-hydroxyethylsuccinimide and N-hydroxyethylpyrrolidone. The diolefins which may be separated by the process of the invention are butadiene, isoprene ...

Improvements in or relating to process for segregation of c dienes

C5 diolefines are separated from a cracked petroleum distillate fraction containing appreciable amounts of isoprene together with piperylene and cyclodiolefines including cyclopentadiene, by heating said fraction in the liquid phase in a first thermal soaking zone, under such conditions of temperature and pressure and for such a time that at least half but not all of the cyclopentadiene is dimerized without substantially polymerizing or copolymerizing the isoprene and piperylene, distilling an isoprene-rich distillate from the heat-soaked fraction, heating the bottoms product in the liquid phase in a second thermal soaking zone under more severe conditions and for such a time that the dimerization of the cyclopentadiene is substantially completed, and distilling the piperylene from the cyclopentadiene dimer. The bottoms product from the isoprene distillation may be blended with a C5-C7 hydrocarbon stream, obtained from severely cracked petroleum oils and containing methylcyclopentadiene ...

Improvements in and relating to the Purification of Natural Gas

... 1,170,022. Natural gas separation process. R. R. TRACY and R. G. SPEAR. 16 Jan., 1968 [17 Jan., 1967; 27 Dec., 1967], No. 2244/68. Heading F4P. Separation of natural gas into a hydrocarbon rich fraction and into a relatively low boiling contaminant fraction e.g., nitrogen is effected by cooling compressed feed gas mixture by passage through parallel heat exchangers 24, 25, expansion with partial liquefication in valves 26, 27, separation into liquid and gaseous phases in a vessel 30, continuously withdrawing liquid and gas product streams from vessel 30 through lines 33, 31 and passing at least a portion of each product stream separately through said heat exchangers 24, 25 in counterflow to the feed gas mixture. The feed stream at well head pressure having been cooled, filtered and dried has its pressure reduced to 1500 p.s.i.a. at a valve 23 in feed line 22 and is expanded at valves 26, 27 to about atmospheric pressure; the return flow of liquid fraction through exchanger 24 being effected ...

Treatment of Hydrocarbon Streams.

... 1,187,899. Isoprene; piperylene; mono- and di-cyclopentadiene. MONSANTO CO. 26 April, 1968 [28 April, 1967], No. 19896/68. Addition to 1,187,898. Heading C5E. A C 5 hydrocarbon stream containing isoprene, piperylene and cyclopentadiene is separated by a process comprising the steps of: (1) treating said stream for 1-3 hours in a dimerization zone maintained at 90-110‹ C., the stream preferably being boiling, (2) fractionally distilling the effluent from (1) in a zone having a kettle temperature of 100-150‹ C., at least 5 distillation plates and a reflux ratio of at least 0-2 : 1 so as to obtain an overhead comprising mainly C 5 hydrocarbons and a bottoms comprising dicyclopentadiene, (3) fractionally distilling the overhead from (2) in a zone having at least 40 distillation plates and a reflux ratio of at least 8 : 1, so as to obtain an overhead comprising mainly hydrocarbons boiling lower than isoprene and a bottoms comprising isoprene and hydrocarbons boiling higher than isoprene (including ...

Process for producing a pure methane fraction

PROCESS FOR PRODUCING HIGHLY PURE ISOPRENE

... 1325932 Purifying isoprene JAPAN SYNTHETIC RUBBER CO Ltd 19 April 1971 [6 Feb 1970 23 Dec 1970] 21294/71 Heading C5E Purified isoprene is separated from a C 5 cracked fraction by (a) removing a major portion of cyclopentadiene and acetylenes by dimerization (by heat soaking) and distillation, and (b) treating the fraction with a composition made by mixing sodium metal and a C 1 -C 18 aliphatic monohydric alcohol to remove the remaining cyclopentadiene, acetylenes and sulphur compounds. The amount of alcohol should not be more than the equivalent of Na, which may be dispersed in an inactive hydrocarbon medium. Paraffin and mono-olefins may be removed before the Na treatment by extractive distillation. The acetylenes may be removed by azeotropic distillation with isopentane.

Hydrocarbon separation

Catalytic hydrodeoxygenation process

Hydrocarbons containing aluminium compounds and oxygen-containing compounds are purified by first removing the aluminium compounds followed by catalytic hydrogenation. The hydrocarbon may for example be the solvent stripper overhead obtained by stripping the product of oxidizing an aluminium alkyl to the corresponding alkoxide in the presence of a hydrocarbon solvent, e.g. kerosine. The aluminium contaminants are removed by distillation or by washing with dilute acid, e.g. 2-40% aqueous sulphuric acid. Hydrogenation is then effected at 60-1000 DEG F., above 200 p.s.i.g., 0.5-6 vol/vol/hour with 600-5,000 SCF of hydrogen per barrel over any hydrogenation catalyst, e.g. nickel-molybdena on alumina, cobalt-molybdena on alumina, iron oxide, barium-copper chromite, molybdenum disulphide on alumina, or nickel sulphide on alumina. The product may be distilled and used as refinery distillates or reused as diluents in organoaluminium chemistry.

Separations with ionic liquid solvents

PURIFICATION OF OLEFIN OLIGOMERS

Improvements in or relating to the processing of crude benzole

Aromatic hydrocarbons are recovered from benzole in pure form by first fractionating to obtain a lower boiling benzene fraction and a higher boiling fraction containing toluene and xylenes, then hydrofining each fraction. In a preferred embodiment forerunnings containing compounds more volatile than benzene are removed, e.g. cyclopentadiene and carbon disulphide. The benzene fraction should contain not more than 0.1% of toluene and other compounds less volatile than benzene; similar considerations apply to the toluene and xylene fraction. If desired the forerunnings may also be hydrofined together with the higher boiling fraction. Saturated materials are separated from the hydrofined products by fractionation and the higher boiling fraction may be separated into toluene and xylene. Specification 892,113 is referred to.

PURIFICATION OF OLEFIN OLIGOMERS

Process for the manufacture in pure form of 1-pentene or an alpha-olefin lower than 1-pentene

Improvements in the production of acetylene

Acetylene-containing gases obtained by cracking hydrocarbons are purified prior to solvent extraction by contact with 70-98% sulphuric acid at 25-40 DEG C. and a pressure such that the ethylene partial pressure is 0.5-1.4 atm. In a preferred embodiment the gas containing 5-15% vol. of acetylene at 5-24 atm. is contacted in a first stage at 25-40 DEG C. and atmospheric pressure with 40-90% acid (70-90% on entering) obtained from the subsequent main washing, contacting with aqueous alkali, compressing and contacting with 70-98% acid (90-98% on entering) in accordance with the invention, again contacting with alkali and passing to a solvent extraction process.

Method of separating the constituents of gaseous mixtures

... 456,773. Separating gases by liquefaction. AIR REDUCTION CO., Inc., 60, East 42nd Street, New York, U.S.A.-(Assignees of Wilkinson, W. ; Rye, Now York, and Schlitt, J. L. ; Darien, Connecticut, both in U.S.A.) May 17, 1935, No. 14487. Convention date, Aug. 1, 1934. [Class 8 (i)] A complex gas mixture containing ethylene and propylene is separated by partial condensation into two fractions one containing nearly all the ethylene and the other nearly all the propylene, these fractions being afterwards rectified. The mixture is passed under pressure through an exchanger 6 to the bottom section 8 of a rectifier. The propylene and less volatile constituents accumulate as liquid in the base and are transferred through an exchanger 76 to a rectifying column 67. The liquid from this column flows into a rectifier 83 from the top of which vapour flows back to rectifier 67 while the liquid containing butane, butylene, &c., is carried off through the exchanger 6. Vapour from an intermediate point of ...

Improvements in or relating to the working up of crude benzene

Purified fractions are produced from crude benzene containing pyridine bases and unsaturated compounds by pressure refining, comprising fractionally distilling the crude benzene to give a number of fractions in such a way that the said bases and the said unsaturated compounds are concentrated in some of these fractions, removing the said bases by treatment with dilute acid and removing, or recovering, the unsaturated compounds from these last-mentioned fractions by known means and then subjecting at least some of the fractions to pressure hydrogenation either severally or in admixture. In an example, crude benzene is fractionally distilled into the following fractions: (1) pre-runnings containing cyclopentadiene, (2) benzene containing 0.3 per cent cyclopentadiene, (3) benzene-toluene mixture, (4) toluene, (5) xylene containing styrene, (6) "solvent naphtha" containing coumarone and indene, and (7) materials boiling above 180 DEG C. Fraction 1 is heated in a pressurized vessel at 100 to ...

CONVERSION OF MONOALKYLBENZENES TO DIALKYLBENZENES

PROCESS FOR PRODUCING A GAS RICH IN METHANE FROM WASTE MATERIALS

Process of refining benzene

In the purification of benzene by a series of aqueous sulphuric acid washing steps followed by a series of neutralising washing steps and fractional distillation, the benzene, prior to the first neutralising step, is contacted with 0,15-2% by weight of a watersoluble aliphatic aldehyde and at least sufficient water to dissolve the aldehyde and agitating for sufficient time to react the aldehyde with all the thiophene sulphur present. Aqueous acetaldehyde may be used but commercial formalin is preferred and is added at the end of the second acid wash before the acid is separated.

Processes for the separation of mixtures of fluids by distillation and/or absorption

... Recovery of C3 hydrocarbons from cracked and distillation gases is effected in an absorption column 15 to which the gases are fed at 20 atmospheres pressure through a line 16 and to which a liquid gasoline fraction at 16 DEG C. is fed through a line 17 connected to the base of a distillation column 18 fed with loaded absorption liquid issuing from the base of column 15. The C3 hydrocarbon product is discharged from the column 18 at the top thereof and the purified gasoline leaving the base at 240 DEG C. has its temperature reduced to 16 DEG C. in a water cooler 25 and in exchangers 23, 21 cooled by gas from the top of column 15 after expansion in vortex tubes 20, 22. Specification 405,781 [Group XIII] is referred to.

Process for the separation of acetylene-free ethylene from gas mixtures

... Ethylene free from acetylene is obtained from a gas mixture containing low aliphatic hydrocarbons by separating therefrom a C2 hydrocarbon stream by rectification, removing ethane by rectification, absorbing acetylene in a selective liquid solvent at a temperature at or near the liquefaction temperature of the C2 hydrocarbon stream, separating liquid ethylene by rectification from the effluent and using part of the liquid ethylene so obtained as a scrubbing liquid during the separation by rectification of said liquid ethylene, the greater part of ethylene absorbed in the selective solvent being regenerated by heat exchange with regenerated solvent and regenerating the solvent by heating and recovering acetylene and residual ethylene; in a modification, ethane is not removed prior to the acetylene absorption and the ethane-ethylene mixture recovered from the solvent by heat exchange with regenerated solvent is rectified to obtain liquid ethylene part of which is used ...

Separation and purification of cyclodienes

A mixture of C5 and C6 cyclodiene monomers contaminated with C7 and higher boiling hydrocarbons, such as is obtained from a cracking zone, is separated by separating in a first fractionating zone an overhead stream of C5 and C6 dienes contaminated with up to 1.5% by weight of C7 hydrocarbons and separating the C5 from the C6 in a second zone operated with a reboiler temperature of 350-400 DEG F. such that any dimers formed in the second zone are cracked, thereby avoiding recycle of bottoms material. A C7-C9 purge is removed from the first zone and bottoms are recycled to the cracking zone in an amount of 400-500% by weight of fresh feed.

PURIFICATION OF NATURAL GAS

Improvements in the purification of high molecular weight alkyl-aromatics

Alkyl aromatics obtained by Friedel-Crafts synthesis from alkylchlorides containing more than 10 carbon atoms and hydrocarbons of the benzene series are purified by treating the neutralized, anhydrous crude alkyl-aromatic with an aluminium halide in the presence of gaseous hydrogen halide: the aluminium halide double compound formed is then separated and the purified alkyl-aromatic is neutralized with alkaline water and then distilled. The FriedelCrafts catalyst may be aluminium chloride. The purifying treatment may be effected with hydrochloric or hydrobromic acids and aluminium chloride or bromide. Up to 5 per cent of the aluminium halide may be used. Hydrocarbons referred to are benzene, toluene and xylene. A specified alkyl aromatic is benzene reacted with a chlorinated petroleum fraction containing normal paraffins, isoparaffins and cycloparaffins. The crude anhydrous alkyl aromatic may first be fractionally distilled and only the last 30 per cent of the remaining monoalkylbenzene ...

Integrated stabilizer in deisobutanizer for isomerization of hydrocarbons and product separation

An isomerization method consists of a deisobutanizer column receives feed comprising n-butane. The deisobutanizer column delivers its bottoms a portion to a reboiler and another portion along with hydrogen is routed to a isomerization reactor and the reactor effluent is returned to the column. A stabilizer which is integrated with the column, an overhead stream used as a reflux and bottoms containing an iso-butane-rich stream that is the iso-butane product stream. The column overhead effluent is routed to separator, which splits the hydrocarbons and effluent, where the hydrocarbons are routed to deisobutanizer column and effluent recycled to stabilizer, where the stabilizer separates the reactor effluent into product streams contains an iso-butane product stream, a n-butane product stream, and a lighter hydrocarbon product stream.

Process of deodorization of liquified hydrocarbons, in particular of commercial butane.

Process of obtaining pure paraffinic hydrocarbons with right chain.

Process and device of purification of acetylene by washing to the sulphuric acid.

Process of separation of mixtures of hydrocarbons.

Process of separation of alkylated aromatic compounds or oligomerized compounds of an effluent of a zone of reaction.

PROCEDURE FOR EXTRACTING AROMATIC HYDROCARBONS FROM A COAL WATER MATERIAL MIXTURE

PROCEDURE FOR THE SEPARATION FROM OLEFINEN

PROCEDURE AND DEVICES FOR THE PRODUCTION OF NAPHTHALIN FROM COKE OVEN RAW GAS

DIAPHRAGM PROCEDURE FOR THE RECUPERATION OF LIQUID HYDROCARBONS.

PROCEDURE AND DEVICE FOR RUECKGEWINNUNG THE HEAVIEST HYDROCARBONS FROM A GAS MIXTURE.

PROCEDURE FOR the SEPARATION FROM AROMATIC C8 HYDROCARBON MIXTURES

PROCEDURE FOR DIVIDING A GAS MIXTURE.

PROCEDURE FOR THE PRODUCTION OF PURE ONES AROMATICS.

PROCEDURE FOR THE CLEANING OF MIDDLE OLEFINEN

PROCEDURE FOR THE PRODUCTION OF AN ALKYL-AROMATIC HYDROCARBON, PREFERRED WAY CUMOL

Process and apparatus for the purification of methane rich gas streams

Separation sequence for hydrocarbons from a gentle thermal cleavage

The invention describes a method for separating hydrocarbons in an installation for generating hydrocarbons from a hydrocarbon-containing charge by cleavage, wherein the product gas of the cleavage, which is produced as the raw gas (1) and which contains gaseous hydrocarbons is compressed (2a) and dried (5a,5b), and supplied as charge material into a separation stage (hereafter referred to as front end C3/C4 separation), in which the raw gas (1) is separated into a hydrocarbon fraction consisting of hydrocarbons having a maximum of 3 carbon atoms (15) and a hydrocarbon fraction consisting of hydrocarbons having at least 4 carbon atoms (17), wherein the front end C3/C4 separation comprises, in terms of process technology, a C4 absorber (6) and a depropanizer (8), wherein a hydrocarbon fraction consisting of hydrocarbons having a maximum of 3 carbon atoms is obtained as a gaseous overhead product (15) of the C4 absorber (6), and wherein a liquid hydrocarbon fraction consisting of hydrocarbons ...

Process for the removal of mapd from hydrocarbon streams

Distillation of a Fischer-Tropsch derived hydrocarbon stream

A method for processing an olefin-containing product stream

Process for preparing butene oligomers from field butanes

Hydrocarbon alkylation process

Process for production of paraxylene

PROCESS FOR SEPARATING HIGHLY PURE BUTENE-1 AND BUTENE-2

PROCESS TO DECREASE OR ELIMINATE CORROSION FROM THE DECOMPOSITION OF HALIDE CONTAINING OLEFIN CATALYSTS

A processes is provided to inhibit or limit the decomposition of a halide- containing olefin oligomerization catalyst system during recovery of an oligomerization product. The process includes deactivation of an olefin oligomerization catalyst system present in an olefin oligomerization reactor effluent stream by contact with an alcohol under conditions that minimize potential for deactivated catalyst system decomposition. Such conditions include minimization of the water content of the deactivation agent and concentration of the deactivation agent.

LEAN REFLUX-HIGH HYDROCARBON RECOVERY PROCESS

A two-tower scheme process for the recovery of propane and heavier components from a hydrocarbon gas stream is provided. Feed gas (12) is cooled (14), partially condensed, and then separated (24) to give a first liquid stream (22) and a first vapor stream (26). First liquid stream is sent to a distillation tower (28) that recovers at the bottoms a major portion of propane and heavier components (54) and produces an overhead gas stream (42). First vapor stream (26) is expanded (30) and sent as bottom feed (34) to the absorber. Absorber produces an absorber overhead stream (16) containing essentially all the ethane and lighter components and an absorber bottoms stream (18). Absorber bottoms stream is heated (14) and sent to the distillation tower (28) as middle feed (52). Absorber overhead stream is warmed (40) and optionally compressed (48, 49). A part of the compressed stream (20) is substantially condensed and sent to absorber as top feed. The process and apparatus can be used to recover ...

Selective CO Oxidation For Acetylene Converter Feed CO Control

A system and process for acetylene selective hydrogenation of an ethylene rich gas stream. An ethylene rich gas supply comprising at least H 2 S, CO 2 , CO, and acetylene is directed to a first treatment unit for removing H 2 S and optionally CO 2 from the gas stream. A CO oxidation reactor is used to convert CO to CO 2 and form a CO-depleted gas stream. A second treatment unit removes the CO 2 from the CO-depleted gas stream and an acetylene selective hydrogenation treats the CO-depleted gas stream.

Component Separations in Polymerization

A process for component separation in a polymer production system, comprising separating a polymerization product stream into a gas stream and a polymer stream, wherein the gas stream comprises ethane and unreacted ethylene, distilling the gas stream into a light hydrocarbon stream, wherein the light hydrocarbon stream comprises ethane and unreacted ethylene, contacting the light hydrocarbon stream with an absorption solvent system, wherein at least a portion of the unreacted ethylene from the light hydrocarbon stream is absorbed by the absorption solvent system, and recovering a waste gas stream from the absorption solvent system, wherein the waste gas stream comprises ethane, hydrogen, or combinations thereof.

METHOD FOR TREATING A CRACKED GAS STREAM FROM A HYDROCARBON PYROLYSIS INSTALLATION AND INSTALLATION ASSOCIATED THEREWITH

This method includes the separation of an upstream partly condensed cracked gas stream in an intermediate separator (B) in order to recover an intermediate liquid (), and an intermediate cracked gas stream () and the introduction of the intermediate liquid () into an intermediate demethanization column (). 1. A method for treating a cracked gas stream stemming from a hydrocarbon pyrolysis installation , comprising the following steps:upstream cooling and partial condensation of a crude cracked gas stream in at least one upstream heat exchange region;separating the partly condensed crude gas stream in at least one upstream separator in order to recover an upstream liquid and an upstream cracked gas stream;{'sub': '2', 'sup': '+', 'introducing the upstream liquid into an upstream demethanization column for recovering at the head of the upstream column, an upstream head stream rich in methane and, at the bottom of the upstream column, a first liquid stream rich in Chydrocarbons;'}intermediate cooling and partial condensation of the upstream cracked gas stream in at least one intermediate heat exchange region;separating the partly condensed upstream cracked gas stream in at least one intermediate separator for recovering at least one intermediate liquid and one intermediate cracked gas stream;{'sub': '2', 'sup': '+', 'introducing the or each intermediate liquid into an intermediate demethanization column in order to recover at the head of the intermediate column, an intermediate head stream, and at the bottom of the intermediate column, a second liquid stream rich in Chydrocarbons;'}introducing at least one portion of the upstream head stream from the upstream column into the intermediate column;downstream cooling and partial condensation of the intermediate cracked gas stream in at least one downstream heat exchange region;separating the intermediate partly condensed cracked gas stream in a downstream separation assembly for recovering a downstream liquid and a ...

Process to Decrease or Eliminate Corrosion from the Decomposition of Halide Containing Olefin Cataysts

A process is provided to inhibit or limit the decomposition of a halide-containing olefin oligomerization catalyst system during recovery of an oligomerization product. The process includes deactivation of an olefin oligomerization catalyst system present in an olefin oligomerization reactor effluent stream by contact with an alcohol under conditions that minimize potential for deactivated catalyst system decomposition. Such conditions include minimization of the water content of the deactivation agent and concentration of the deactivation agent. 1. A process to deactivate a halide-containing olefin oligomerization catalyst system and inhibit or limit the decomposition of the deactivated catalyst system during recovery of an olefin oligomerization product comprising the steps of:a) forming an intermediate stream by contacting an olefin oligomerization reactor effluent stream which comprises one or more olefin products, the catalyst system, and heavies with an alcohol that is soluble in any portion of the reactor effluent stream thereby deactivating the catalyst system; andb) separating the intermediate stream into at least one product stream comprising the olefin oligomerization product and at least one heavies stream, wherein separating the intermediate stream comprises distilling a material, wherein distilling the material comprises passing the material through a reboiler, wherein the material is maintained below about 190° C.2. The process of wherein the material is maintained below about 185° C.3. The process of wherein the material is maintained below about 175° C.4. The process of wherein distilling the material comprises passing the material through at least two distillation stages.5. The process of wherein the alcohol has a boiling point different from at least one of the one or more olefin products in the reactor effluent stream.6. The process of wherein the alcohol has 6 or more carbon atoms per molecule.7. The process of wherein the alcohol is selected ...

METHOD OF PROCESSING FEED STREAMS CONTAINING HYDROGEN SULFIDE

A method of processing feed streams high in hydrogen sulfide is provided. The method includes providing a feed gas stream that includes hydrocarbons and at least 5 vol % hydrogen sulfide. At least a portion of the feed gas stream is separated into a hydrogen sulfide stream and a hydrocarbon stream. The hydrocarbon gas stream is processed to produce natural gas. At least 34 mol. % of the hydrogen sulfide in the hydrogen sulfide stream is combusted with an oxidant to generate thermal power. Thermal power generated by the combustion is utilized in one or more of the steps of separating the feed gas stream into the hydrogen sulfide stream and the hydrocarbon gas stream, and processing the hydrocarbon gas stream to produce natural gas, compressed natural gas, or liquefied natural gas. 1. A method , comprising:providing a feed gas stream comprising hydrogen sulfide and hydrocarbons, wherein the feed gas stream comprises at least 5% by volume hydrogen sulfide;separating at least a portion of the feed gas stream into a hydrogen sulfide stream and a hydrocarbon gas stream, the hydrogen sulfide stream containing more hydrogen sulfide, by volume percent, than the feed gas stream, and the hydrocarbon gas stream containing less hydrogen sulfide, by volume percent, than the feed gas stream;processing the hydrocarbon gas stream to produce natural gas; andcombusting at least 34 mol % of the hydrogen sulfide in the hydrogen sulfide stream with an oxidant containing molecular oxygen to generate thermal power, where the molar ratio of molecular oxygen to hydrogen sulfide in the hydrogen sulfide stream and oxidant that are combusted is at least 1.4 to 1;utilizing the thermal power in one or more of the steps of separating the feed gas stream into the hydrogen sulfide stream and the hydrocarbon gas stream when processing the hydrocarbon gas stream to produce natural gas.2. The method of claim 1 , wherein processing the hydrocarbon gas stream to produce natural gas comprises performing ...

"process for removing oxygenated contaminants from an hydrocarbonstream"

The present invention is a process for removing oxygenated contaminants and water from an hydrocarbon stream comprising: introducing the contaminated hydrocarbon stream in a gaseous phase in an absorption zone, contacting said hydrocarbon stream in said absorption zone at a pressure of at least 5 bars, advantageously in the range 5 to 40 bars with an alcohol capable to absorb water and oxygenated contaminants at conditions effective to produce an overhead hydrocarbon stream having a reduced oxygenated contaminants and water content and an absorbent bottoms stream comprising the alcohol, hydrocarbons and having an enhanced oxygenated contaminants and water content, sending the overhead of the absorption zone to a wash column (referred to as the high pressure water wash column) at a pressure of at least 5 bars, advantageously in the range 5 to 40 bars, essentially washed with water at conditions effective to produce an overhead hydrocarbon stream having a reduced oxygenated contaminants and an aqueous bottoms stream having an enhanced oxygenated contaminants content. Advantageously the process is further comprising: sending the bottoms stream from the absorption zone to a distillation column (referred to as the alcohol distillation column) operating at a pressure of less than 3 bars absolute and advantageously at a pressure in the range 1-3 bars absolute at conditions effective to produce an overhead comprising essentially oxygenated contaminants and hydrocarbons, optionally treated to recover the hydrocarbons, an alcohol bottoms stream comprising water and essentially free of hydrocarbons and oxygenated contaminants, sending said alcohol bottoms to the process which has produced the hydrocarbon stream comprising oxygenated contaminants and water to be purified.

PROCESS FOR REMOVING OXYGENATED CONTAMINANTS FROM AN HYDROCARBON STREAM

The present invention is a process for removing oxygenated contaminants and water from an hydrocarbon stream comprising: 1. Process for removing oxygenated contaminants and water from an hydrocarbon stream comprising:introducing the contaminated hydrocarbon stream in a gaseous phase in an absorption zone, an overhead hydrocarbon stream having a reduced oxygenated contaminants and water content and', 'an absorbent bottoms stream comprising the absorbent, hydrocarbons and having an enhanced oxygenated contaminants and water content,', 'introducing the above absorbent bottoms stream in a stripping zone at conditions effective to produce', 'an absorbent bottoms stream essentially free of hydrocarbons, oxygenated contaminants and water and', 'an overhead stream comprising essentially hydrocarbons, water and the oxygenated contaminants,, 'contacting said hydrocarbon stream in said absorption zone with an absorbent capable to absorb water and oxygenated contaminants at conditions effective to produce'}recycling the absorbent bottoms stream of the stripping zone to the absorption zone,optionally fractionating the overhead stream from the stripping zone to recover the hydrocarbons,optionally sending the overhead of the absorption zone to a caustic wash to remove the acidic components and recovering an hydrocarbon stream essentially free of water and oxygenated contaminants.2. Process according to wherein the hydrocarbon stream comprising oxygenated contaminants and water is successively compressed and cooled in one or more steps to remove the major part of water and further fed to the absorption zone.3. Process according to wherein the stripping zone is a distillation column.4. Process according to wherein the overhead stream of said distillation column of the stripping zone is cooled to produce an aqueous phase comprising oxygenated contaminants and a gaseous phase comprising hydrocarbons and oxygenated contaminants claim 3 , a part of said aqueous phase is used as the ...

PROCESS FOR REMOVING OXYGENATED CONTAMINANTS FROM AN HYDROCARBON STREAM

The present invention is a process for removing oxygenated contaminants and water from an hydrocarbon stream comprising: 1. Process for removing oxygenated contaminants and water from an hydrocarbon stream comprising:introducing the contaminated hydrocarbon stream in a gaseous phase in an absorption zone,contacting said hydrocarbon stream in said absorption zone at a pressure of at least 5 bars, advantageously in the range 5 to 40 bars with an alcohol capable to absorb water and oxygenated contaminants at conditions effective to produce,an overhead hydrocarbon stream having a reduced oxygenated contaminants, and water content, andan absorbent bottoms stream comprising the alcohol, hydrocarbons and having an enhanced oxygenated contaminants and water content,sending the overhead of the absorption zone to a wash column (referred to as the high pressure water wash column) at a pressure of at least 5 bars, advantageously in the range 5 to 40 bars, essentially washed with water at conditions effective to produce,an overhead hydrocarbon stream having a reduced oxygenated contaminants, andan aqueous bottoms stream having an enhanced oxygenated contaminants content.2. Process according to wherein the alcohol is an aqueous solution comprising at least 80 w % of alcohol.3. Process according to wherein the overhead of the high pressure water wash column is sent to a caustic wash to remove the acidic components and recovering an hydrocarbon stream essentially free of oxygenated contaminants.4. Process according to further comprising:sending the bottoms stream from the absorption zone to a distillation column (referred to as the alcohol distillation column) operating at a pressure of less than 3 bars absolute and advantageously at a pressure in the range 1-3 bars absolute at conditions effective to produce,an overhead comprising essentially oxygenated contaminants and hydrocarbons, optionally treated to recover the hydrocarbons,an alcohol bottoms stream comprising water and ...

PROCESS FOR REMOVING OXYGENATED CONTAMINANTS FROM AN HYDROCARBONSTREAM

The present invention is a process for removing oxygenated contaminants and water from an hydrocarbon stream comprising: 1. Process for removing oxygenated contaminants and water from an hydrocarbon stream comprising:introducing the contaminated hydrocarbon stream in a gaseous phase in an absorption zone, an overhead hydrocarbon stream having a reduced oxygenated contaminants and water content and', 'an absorbent bottoms stream comprising the absorbent, hydrocarbons and having an enhanced oxygenated contaminants and water content,, 'contacting said hydrocarbon stream in said absorption zone with an absorbent capable to absorb water and oxygenated contaminants at conditions effective to produce'} an absorbent bottoms stream essentially free of hydrocarbons, oxygenated contaminants and water and', 'an overhead stream comprising essentially hydrocarbons, water and the oxygenated contaminants,, 'introducing the above absorbent bottoms stream in a stripping zone at conditions effective to produce'}recycling the absorbent bottoms stream of the stripping zone to the absorption zone,optionally fractionating the overhead stream from the stripping zone to recover the hydrocarbons,optionally sending the overhead of the absorption zone to a caustic wash to remove the acidic components and recovering an hydrocarbon stream essentially free of water and oxygenated contaminants.2. Process according to wherein the hydrocarbon stream comprising oxygenated contaminants and water is successively compressed and cooled in one or more steps to remove the major part of water and further fed to the absorption zone.3. Process according to wherein the stripping zone is a distillation column.4. Process according to wherein the overhead stream of said distillation column of the stripping zone is cooled to produce an aqueous phase comprising oxygenated contaminants and a gaseous phase comprising hydrocarbons and oxygenated contaminants claim 3 , a part of said aqueous phase is used as the reflux ...

PROCESS FOR PROVIDING A VAPOROUS PURIFIED CRUDE C4 CUT AS A FEED STREAM FOR AN EXTRACTIVE DISTILLATION WITH A SELECTIVE SOLVENT

Mixtures of hydrocarbons predominantly having 4 carbon atoms per molecule known as Ccuts are used in obtaining crude 1,3-butadiene by a thermal cracking process. Vaporous purified crude Ccuts are produced from liquid crude Ccuts, containing butanes, butenes, 1,3-butadiene, Chydrocarbons, Coligomers and polymers, and Chydrocarbons via an extractive distillation by fist removing the Coligomers and polymers and the Chydrocarbons and then vaporizing the liquid crude Ccut in a vaporizer vessel. The vaporizer vessel is directly or indirectly in contact with a stripping column where liquid Ccuts are supplied to the upper region, direct gas and liquid exchange with the vaporizer vessel occurs in the lower region, and vaporous purified crude Ccuts are removed from the top region. 1. A process for providing a vaporous purified crude Ccut (2) as a feed stream for an extractive distillation with a selective solvent to obtain crude 1 ,3-butadiene ,{'sub': 4', '3', '4', '5+', '4, 'claim-text': [{'sub': '5+', 'less than two thirds of the Chydrocarbons present in the feed stream and'}, {'sub': '4', 'less than 5% by weight of the Coligomers and polymers present in the feed stream,'}], 'proceeding from a liquid crude Ccut (1) as a feed stream, comprising not only butanes, butenes and 1,3-butadiene but also Chydrocarbons, Coligomers and polymers, and Chydrocarbons, said purified vaporous crude Ccut comprising'} [{'sub': 4', '5', '4, '1) removing the Coligomers and polymers and the C+hydrocarbons, in each case down to the residual contents specified above for the vaporous purified crude Ccut, and'}, {'sub': '4', '2) vaporizing the liquid crude Ccut in a vaporizer vessel (VK),'}], 'comprising the process steps of'}wherein{'sub': 4', '4, 'the vaporizer vessel (VK) is assigned a stripping column (K) having one or more plates, to which the liquid Ccut (1) is supplied in the upper region thereof, which is in direct gas and liquid exchange with the vaporizer vessel (VK) in the lower region ...

Production of high purity butene-1 from c4 olefins/paraffins mixed gas

A hybrid process comprising an adsorption process and a distillation process for the separation of butene-1 from a C4 hydrocarbon mixture gas including butene-1, trans-2-butene, cis-2-butene, normal butane, isobutane, etc. is provided. The hybrid process comprises introducing a gaseous C4 mixture into the adsorption tower loaded with adsorbents which adsorb olefins selectively to discharge C4 paraffins to the outlet of the tower, desorbing C4 olefins selectively adsorbed in the adsortion tower to produce high purity C4 olefins mixture gas in which isobutane and normal butane was removed, and separating the high C4 olefins mixture gas (a mixture of butene-1, trans-2-butene, cis-2-butene, and a trace amount of C4 paraffins) via distinction to obtain high purity butene-1 including a trace amount of isobutane in the top of the distillation tower and obtain a mixture gas including trans-2-butene, cis-2-butene and a trace amount of normal butane in the bottom of the tower.

DISPLACEMENT DESORPTION PROCESS FOR LIGHT OLEFIN SEPARATION

A process and apparatus for separating an olefin from mixed gases containing light olefins is provided. The process includes adsorbing the olefin of an olefin-containing mixed gas in an adsorption column packed with an adsorbent selectively adsorbing the olefin; discharging gases other than the olefin through the outlet of the adsorption column; desorbing the adsorbed olefin by displacement using a desorbent, and separating the olefin from the desorbent, thereby producing a high-purity olefin. The apparatus includes adsorption columns packed with an adsorbent selectively adsorbing an olefin, and at least two distillation columns for separating an olefin/desorbent mixture and an olefin poor stream/desorbent into their components. If the olefin concentration of the off-gas from an olefin rinse step is higher than that of a raw material gas, recovering the olefin from the off-gas is carried out before or after the adsorption step. 1. A method for separating an olefin from an olefin-containing mixed gas using at least one adsorption column and at least two distillation columns including a distillation column for separating an olefin rich stream from a desorbent and a distillation column for separating an olefin poor stream from a desorbent , comprises the steps of:i) introducing the olefin-containing mixed gas into an adsorption column packed with an olefin selective adsorbent to adsorb an olefin from the mixed gas, and sending unadsorbed components and a desorbent, fed into the adsorption column during desorption, through the outlet of the adsorption column to a distillation column for separating an olefin poor stream/desorbent mixture into components;ii) introducing a high-concentration olefin, obtained from a distillation column for separating an olefin from a desorbent, into the adsorption column, thereby removing paraffin and other gases from the adsorption column to increase the purity of the olefin in the adsorption column;iii) introducing a desorbent into the ...

METHOD FOR REMOVING ACID GASES FROM HYDROCARBON-COMPRISING FLUIDS

In a method for removing acid gases from hydrocarbon-comprising fluids, (a) a carbon dioxide-rich acid gas stream is separated off from the fluid by scrubbing with a liquid absorbent, (b) the fluid is contacted with a solid adsorbent for removing sulfur-comprising acid gases, and (c) the loaded solid adsorbent is regenerated by contacting with at least one purge gas under regeneration conditions. A carbon dioxide-rich acid gas stream separated off in step (a) is used as purge gas. 114.-. (canceled)15. A method for removing acid gases from hydrocarbon-comprising fluids , wherein(a) a carbon dioxide-rich acid gas stream is separated off from the fluid by scrubbing with a liquid absorbent,(b) the fluid is contacted with a solid adsorbent for removing sulfur-comprising acid gases, and(c) the loaded solid adsorbent is regenerated by contacting with at least one purge gas under regeneration conditions, wherein a carbon dioxide-rich acid gas stream separated off in step (a) is used as purge gas.16. The method according to claim 15 , wherein the liquid absorbent is a physically acting absorbent.17. The method according to claim 15 , wherein the liquid absorbent is a chemically acting absorbent.18. The method according to claim 17 , wherein the liquid absorbent is a solution of a base.19. The method according to claim 18 , wherein the liquid absorbent is an aqueous solution of a base selected from alkali metal carbonates claim 18 , amines claim 18 , amino acid-metal salts or combinations thereof.20. The method according to claim 15 , wherein the solid adsorbent is selected from zeolites claim 15 , carbon-based adsorbents claim 15 , silica gels claim 15 , activated aluminum oxides and combinations thereof.21. The method according to claim 20 , wherein the zeolites have a pore size of at least about 4.6 Å.22. The method according to claim 15 , wherein at least one further gas different from the carbon dioxide-rich acid gas stream is used as purge gas.23. The method according ...

Methods and Apparatus for Treating a Hydrocarbon Stream

Disclosed is an apparatus for removing water, nitrogen compounds, and unsaturated aliphatic compounds from a hydrocarbon feed stream including a water removal zone, a nitrogen removal zone, and an unsaturated aliphatic compound removal zone. By on aspect, the water removal zone includes a water selective adsorbent, the nitrogen removal zone includes a nitrogen selective adsorbent, and the unsaturated aliphatic compound removal zone includes an unsaturated aliphatic compound removal material.

Distillation column pressure control

Methods and systems for controlling the pressure of distillation columns, for example those operating under vacuum pressure and conventionally equipped with a steam ejector system, are described. Representative distillation columns are used in the separation of thermally unstable components, such as the physical solvent sulfolane, having relatively low volatility. Such columns are employed in aromatic hydrocarbon extraction processes for the recovery of purified C 6 -C 8 aromatic hydrocarbons from a hydrocarbon feed stream (e.g., obtained from the catalytic reforming of naphtha).

Methods for separating hydrocarbon gases

A process for separating a hydrocarbon gas into a fraction containing a predominant portion of the methane or ethane and lighter components and a fraction containing a predominant portion of the C2 or C3 and heavier components in which the feed gas is treated in one or more heat exchange and expansion steps; partly condensed feed gas is directed into a separator wherein a first residue vapor is separated from a C2 or C3-containing liquid; and C2 or C3-containing liquids at substantially the pressure of separation are directed into a distillation column wherein the liquid is separated into a second residue to recover a C2 or C3-containing product. A portion of the vapor and/or a portion of the liquid from the first hydrocarbon vapor/liquid separation is further cooled and introduced into a fractionation column to increase the C2 or C3 and heavier hydrocarbons recovery from the natural gas stream.

Process for treating an output from a hydrocarbon conversion with removal of hydrogen halides and subsequent wash

The present invention relates to a process for treating an output from a hydrocarbon conversion, wherein the hydrocarbon conversion is performed in the presence of an acidic ionic liquid. The hydrocarbon conversion is preferably an isomerization. First of all, the hydrogen halide is drawn off in an apparatus from a mixture which originates from the hydrocarbon conversion and comprises at least one hydrocarbon and at least one hydrogen halide, and then the mixture depleted of hydrogen halide is subjected to a wash.

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.

METHOD FOR IMPROVING PROPYLENE RECOVERY FROM FLUID CATALYTIC CRACKER UNIT

The present invention relates to a method for treating a cracked stream stemming from a fluid catalytic cracker unit (FCCU) in order to improve propylene recovery. The present invention also relates to the corresponding installation to implement the method. 1. Method for treating a cracked stream stemming from a fluid catalytic cracker unit (FCCU) comprising the following steps:compressing and partly condensing the gas stream from the main fractionator column overhead receiver of the FCCU;separating the partly condensed gas stream in order to recover an upstream liquid and an upstream gas;heating the upstream liquid;introducing this heated liquid into an upstream stripper for recovering at the top of the stripper a stream rich in C2 compounds and at the bottom a first liquid stream rich in C3+ hydrocarbons;introducing the first liquid stream rich in C3+ into a first heat exchanger and then into a second heat exchanger;introducing the liquid recovered from the second heat exchanger into a stabilizer column for recovering at the top of the stabilizer column a stream rich in C3 and C4 hydrocarbons and from the side of the stabilizer column a liquid stream rich in C5 and C6 hydrocarbons and from the bottom of the stabilizer column a liquid stream rich in C5, C6 and C7+ hydrocarbons;introducing the liquid stream rich in C5 and C6 hydrocarbons into the first heat exchanger;introducing a liquid stream from stabilizer column bottom into a primary absorber and introducing the upstream gas into a primary absorber for recovering at the top of the primary absorber a first gas stream; and at the bottom of the primary absorber a second liquid stream;introducing lean oil from FCCU main fractionator into a sponge absorber;cooling the first gas stream from primary absorber and introducing it into a propylene absorber;cooling the liquid stream rich in C5 and C6 hydrocarbons from the first heat exchanger;introducing the liquid stream rich in C5 and C6 hydrocarbons recovered from the ...

SORPTION PROCESS WITH ADDED DRYING SECTION

An adsorption process using a fractionation column including a drying section is described. The drying section dries the desorbent and removes water from the adsorption process resulting in increased capacity for the adsorbent bed. 1. A process for the separation of a desired normal paraffin from a feed mixture comprising at least the desired normal paraffin and a non-normal paraffin comprising:passing a feed stream comprising the feed mixture through a first bed of adsorbent comprising a shape selective adsorbent and located in an adsorbent chamber which contains a plurality of compartmentalized beds of the adsorbent separated by transfer points for streams used in the process, which adsorbent selectively retains the desired normal paraffin,passing a desorbent stream into the adsorbent chamber;withdrawing an extract stream comprising the desorbent and the desired normal paraffin from the adsorbent chamber;withdrawing a raffinate stream comprising the desorbent and the non-normal paraffin from the adsorbent chamber;periodically incrementing the transfer points in the adsorbent chamber of the feed, desorbent, extract and raffinate streams to simulate countercurrent movement of the beds of adsorbent and the feed stream;separating the desired normal paraffin from the desorbent in an extract column having a separation section comprising a rectifying section and a stripping section;separating the non-normal paraffin from the desorbent in a raffinate column having a separation section comprising a rectifying section and a stripping section;passing the desorbent through a column drying section to remove water from the desorbent, the column drying section comprising a plurality of drying trays, the column drying section positioned above the rectifying section in the raffinate column, the extract column, or both; andrecovering the desired normal paraffin.2. The process of further comprising recycling the dried desorbent to the adsorbent chamber.3. The process of wherein the ...

PROCESS FOR REMOVING ONE OR MORE SULFUR COMPOUNDS AND AN APPARATUS RELATING THERETO

An exemplary embodiment can be a process for removing one or more sulfur compounds in a gas hydrocarbon stream. The process may include feeding the gas hydrocarbon stream to a prewash zone containing an alkali stream and passing the gas hydrocarbon stream from the prewash zone to an extraction zone. Usually, the gas hydrocarbon stream includes one or more sulfur compounds and the prewash zone includes a hollow fiber membrane. 1. A process for removing one or more sulfur compounds in a gas hydrocarbon stream , comprising:A) feeding the gas hydrocarbon stream comprising one or more sulfur compounds to a prewash zone containing an alkali stream wherein the prewash zone comprises a hollow fiber membrane; andB) passing the gas hydrocarbon stream from the prewash zone to an extraction zone.2. The process according to claim 1 , wherein the alkali stream comprises at least one of an ammonia claim 1 , a potassium hydroxide and a sodium hydroxide.3. The process according to claim 1 , wherein the hollow fiber membrane comprises at least one of a ceramic claim 1 , cellulose acetate claim 1 , polypropylene claim 1 , polysulfone claim 1 , polyamide claim 1 , and polytetrafluoroethylene.4. The process according to claim 1 , wherein the hollow fiber membrane comprises at least one tube and a shell.5. The process according to claim 4 , wherein the gas hydrocarbon stream is provided to the at least one tube.6. The process according to claim 5 , wherein the at least one tube comprises multiple tubes.7. The process according to claim 1 , wherein the gas hydrocarbon stream comprises one or more C4hydrocarbons.8. The process according to claim 1 , wherein the gas hydrocarbon stream upstream of the prewash zone is operated at a temperature of about 30 - about 50° C. claim 1 , and a pressure of about 400 - about 1 claim 1 ,900 KPa.9. The process according to claim 1 , wherein the extraction zone comprises a vessel claim 1 , in turn comprising a plurality of trays.10. A process for removing ...

Membrane-Based Gas Separation Processes to Separate Dehydrogenation Reaction Products

Gas separation processes are provided for separating dehydrogenation reaction products from a raw gas stream to recover hydrocarbons, specifically olefins, such as propylene and iso-butene, as well as unreacted feedstock. The processes employ a sequence of partial condensation steps, interspersed with membrane separation steps to raise the hydrocarbon dewpoint of the uncondensed gas, thereby avoiding the use of low-temperature or cryogenic conditions. 1. A process for treating a raw product stream from dehydrogenation of a light paraffin , said raw product stream comprising at least one paraffin component , one olefin component and hydrogen , comprising the steps of:(a) compressing the raw product stream to create a compressed stream having a first hydrocarbon dewpoint;(b) partially condensing the compressed stream, including cooling and separating the compressed stream into a hydrocarbon condensate stream and an uncondensed gas stream;(c) withdrawing a first portion of the uncondensed gas stream as a purge stream;(d) heating a second portion of the uncondensed gas stream;(e) separating the second portion of the uncondensed gas stream from step (d) using a first membrane to remove a hydrogen-rich permeate gas stream and create a hydrocarbon-enriched residue gas stream having a first residue hydrocarbon dewpoint; and(f) recirculating the hydrocarbon-enriched residue gas stream back to a point in the process upstream of step (b).2. The process of claim 1 , wherein the olefin component is propylene.3. The process of claim 1 , wherein the olefin component is iso-butene.4. The process of claim 1 , wherein step (b) uses a water coolant.5. The process of claim 1 , wherein step (b) uses a refrigerant coolant.6. The process of claim 1 , wherein the compressed stream in step (b) is cooled to a temperature no lower than −30° C.7. The process of claim 1 , wherein step (b) reduces the dewpoint of the compressed stream between 20° C. and 50° C.8. The process of claim 1 , wherein ...

Membrane and Pressure Swing Adsorption Hybrid INRU Process

A process for component separation in a polymer production system, comprising: separating a polymerization product stream into a gas stream and a polymer stream; contacting the polymer stream with a purge gas to yield a purged polymer stream and a spent purge gas stream; introducing the spent purge gas stream to a compressor to produce a compressed gas stream; introducing the compressed gas stream to a first separation unit to produce a first hydrocarbon stream and a membrane unit feed stream; introducing the membrane unit feed stream to a membrane unit to produce a first recovered purge gas stream and a retentate stream; introducing the retentate stream to a second separation unit to produce a second hydrocarbon stream and a PSA unit feed stream; and introducing the PSA unit feed stream to a PSA unit to produce a second recovered purge gas stream and a tail gas stream.

Linear Alpha Olefin Processes

The present disclosure provides assemblies for producing linear alpha olefins and methods for producing linear alpha olefins. In at least one embodiment, a method for producing a linear alpha olefin includes oligomerizing an olefin in the presence of a catalyst and a process solvent in at least one reactor, quenching the reactor effluent, and subjecting the quenched effluent to separation steps to obtain a stream enriched in one or more linear alpha olefins. 1. A method for forming one or more linear alpha olefins , the method comprising the steps of:(a) providing a feed comprising an olefin, a catalyst, and a process solvent to a reaction zone including at least one reactor under oligomerization conditions to obtain a reactor effluent produced in the at least one reactor;(b) contacting at least a portion of the reactor effluent with a quench agent to obtain a quenched effluent;(c) separating at least a portion of the quenched effluent to obtain a vapor effluent and a liquid effluent;(d) separating at least a portion of the liquid effluent to obtain at least one aqueous phase enriched in catalyst and quench agent and an organic phase depleted in catalyst and quench agent;(e) separating at least a portion of the organic phase to obtain a stream enriched in one or more linear alpha olefins.2. The process of claim 1 , wherein the feed comprises <25 ppb water by weight.3. The method of claim 1 , wherein step (a) comprises:providing the feed to a first tubular reactor under oligomerization conditions to obtain a first effluent; andtransferring the first effluent to a second tubular reactor under oligomerization conditions to obtain the reactor effluent.4. The method of claim 3 , further comprising providing steam to a first steam jacket disposed around the first tubular reactor and providing steam to a second team jacket disposed around the second tubular reactor claim 3 ,optionally further comprising controlling the pressure of steam in the first steam jacket pressure ...

FRACTIONAL DISTILLATION SYSTEMS AND METHODS FOR LINEAR ALPHA OLEFIN PRODUCTION

A method for recovery of a product fraction from a mixture comprising an impurity and linear alpha olefins, the method comprising: introducing the mixture into a distillation column, wherein an overhead stream is separated from a bottom stream, wherein the overhead stream comprises a Cn product, a Cn+x product, and an impurity, wherein n is an integer from 4 to 30, wherein x is an integer from 0 to 26; directing the overhead stream into a fractionation column; and separating a Cn product fraction and a Cn+x product fraction in the fractionation column, wherein the Cn+x product fraction comprises at least a portion of the impurity, wherein, when an amount of the impurity is greater than 1 part per million in the Cn+x product fraction, at least a portion of the collected Cn+x product fraction is recycled to the distillation column. 1. A method for recovery of a product fraction from a mixture comprising an impurity and linear alpha olefins , the method comprising:introducing the mixture into a distillation column, wherein an overhead stream is separated from a bottom stream, wherein the overhead stream comprises a Cn product, a Cn+x product, and an impurity, wherein n is an integer from 4 to 30, wherein x is an integer from 0 to 26;directing the overhead stream into a fractionation column; andseparating a Cn product fraction and a Cn+x product fraction in the fractionation column, wherein the Cn+x product fraction comprises at least a portion of the impurity,wherein, when an amount of the impurity is greater than 1 part per million in the Cn+x product fraction, at least a portion of the collected Cn+x product fraction is recycled to the distillation column.2. The method of claim 1 , wherein the impurity comprises toluene claim 1 , benzene claim 1 , p-xylene claim 1 , m-xylene claim 1 , ethyl benzene claim 1 , paraffins claim 1 , naphthenes claim 1 , cyclo-paraffins or a combination comprising at least one of the foregoing.3. The method of claim 1 , wherein n equals 4 ...

Process for the Separation of Linear Alpha-Olefins Using a Dividing Wall Column

Many linear alpha olefin (LAO) syntheses form a range of LAO products when oligomerizing ethylene in the presence of a Ziegler-type catalyst. The range of products typically requires a plurality of distillation columns to separate the LAO products up to a desired carbon count, but such approaches may be energy- and capital-intensive. LAO product separation using at least one dividing wall column may lessen these burdens. Methods for separating LAOs may comprise: providing a pre-processed product stream comprising Cg+ linear alpha olefins (LAOS) to a first of a series of distillation columns, at least one member of the series of distillation columns comprising a dividing wall column; and separating an overhead stream comprising a first LAO from the dividing wall column and one or more side streams from the dividing wall column, each side stream comprising a different LAO that also differs from the first LAO. 1. A method comprising:{'sub': '8+', 'providing a pre-processed product stream comprising C linear alpha olefins (LAOS) to a first of a series of distillation columns, at least one member of the series of distillation columns comprising a dividing wall column; and'}separating an overhead stream comprising a first LAO from the dividing wall column and one or more side streams from the dividing wall column, each side stream comprising a different LAO that also differs from the first LAO.2. The method of claim 1 , further comprising:{'sub': '6+', 'providing a light olefin-depleted product stream comprising C LAOs and a solvent to a first distillation column upstream from the series of distillation columns; and'}{'sub': 6', '8+, 'separating CLAOs as an overhead stream from the first distillation column and C LAOs as a bottoms stream from the first distillation column, the bottoms stream being provided as the pre-processed product stream to the series of distillation columns.'}3. The method of claim 2 , further comprising:separating the solvent as a side stream from ...

Methane Gas Concentration Method

Adsorption towers are filled with adsorbents that adsorb methane gas in coal mine gas and perform a PSA cycle. For each of adsorption towers, a plurality of different pressure states of the internal pressure of the adsorption tower are set as an intermediate pressure state. As a pressure equalization step, an initial pressure equalization step of transferring the gas in one of the adsorption towers that is in a high pressure state to another one of the adsorption towers that is in an intermediate pressure state, and a final pressure equalization step of transferring the gas in one of the adsorption towers that is in the high pressure-side intermediate pressure state to another one of the adsorption towers that is in the low pressure state are performed. 1. A methane gas concentration method comprising:providing four or more adsorption towers each filled with an adsorbent that adsorbs methane gas in a methane-containing gas; andperforming, for each of the adsorption towers, a PSA cycle of repeating in order:an adsorption step of receiving supply of the methane-containing gas in a high pressure state near atmospheric pressure from a lower portion of the adsorption tower, adsorbing the methane gas on the adsorbent, and releasing offgas composed mainly of air from an upper portion of the adsorption tower;a pressure equalization (depressurizing) step of transferring the gas in the adsorption tower that has finished the adsorption step and is in the high pressure state to another adsorption tower in a lower pressure state so as to bring the inside of the adsorption tower into an intermediate pressure state;a decompression step of, after the internal pressure of the tower has been lowered by the pressure equalization (depressurizing) step, further decompressing the adsorbent to a low pressure state so as to desorb the methane gas adsorbed on the adsorbent, and recovering said methane gas from the lower portion of the adsorption tower;a pressure equalization (pressurizing) ...

METHOD FOR COLLECTING ISOPRENE CONTAINED IN FERMENTED GAS, AND METHOD FOR PRODUCING PURIFIED ISOPRENE

Methods include contacting a fermented gas including isoprene with a porous adsorbent and desorbing isoprene adsorbed on the porous adsorbent. The fermented gas may be obtained by culturing a microorganism having an ability to produce isoprene.

METHOD AND PROCESS FOR CONVERTING THE ETHYLENE PRESENT IN THE OVERHEAD EFFLUENT FROM A FCC IN A MANNER SUCH AS TO INCREASE THE PROPYLENE PRODUCTION

The present invention describes a process for fractionating the gaseous fraction leaving overhead from the fractionation column of a catalytic cracking unit (FCC) using a unit for the conversion of ethylene into propylene, in order to upgrade the ethylene contained in the fuel gas. 1. A device for fractionating the gaseous fraction leaving the head of the fractionation column of a catalytic cracking unit , the fraction containing LPG , light gasoline , and a residual gas termed “fuel gas” which itself contains a certain quantity of ethylene , the device comprising:{'b': 6', '15', '10, 'a first absorption section () which can be used to separate the fuel gas () and the light gasoline and LPG stream (), said section being present in an existing catalytic cracking unit,'}{'b': 22', '15, 'a unit () for the catalytic conversion of ethylene into propylene and other products of interest, wherein the feed is constituted by the fuel gas (), in which a large portion of the ethylene is essentially converted into propylene and also into aromatics and other products of interest, in the presence of a catalyst based on zeolite,'}{'b': 31', '22', '31', '11, 'a novel absorption section () which admits the effluents from the conversion unit () after recompression, the propylene, butene and the gasoline fractions contained in said effluents being recovered in said novel absorption section (), by using the gasoline arriving from the existing debutanizer (),'}{'b': 16', '33', '31, 'a second absorption section (), which admits the gas () obtained from the novel absorption section (),'}{'b': 35', '34', '31', '36', '37, 'a debutanization section () which admits the LPG and gasoline fractions () obtained from the novel absorption section () and which produces a stabilized gasoline () and a light LPG fraction ().'}222223227224223227225227228. The device for fractionating the gaseous fraction leaving the head of the fractionation column of a catalytic cracking unit as claimed in claim 1 , in ...

METHOD FOR PREPARING 1,3-BUTADIENE FROM N-BUTENES BY OXIDATIVE DEHYDROGENATION

The invention relates to a method for producing butadiene from n-butenes having the steps: 110.-. (canceled)11. A method for producing butadiene from n-butenes having the steps:A) providing a feed gas stream a comprising n-butenes;B) feeding the feed gas stream a comprising n-butenes and an oxygen-comprising gas into at least one oxidative dehydrogenation zone and oxidatively dehydrogenating n-butenes to butadiene, wherein a product gas stream b comprising butadiene, unreacted n-butenes, steam, oxygen, low-boiling hydrocarbons, high-boiling minor components, optionally carbon oxides and optionally inert gases is obtained;Ca) cooling the product gas stream b by contacting it with a refrigerant and condensing at least a part of the high-boiling minor components;Cb) compressing the remaining product gas stream b in at least one compression stage, wherein at least one aqueous condensate stream c1 and a gas stream c2 comprising butadiene, n-butenes, steam, oxygen, low-boiling hydrocarbons, possibly carbon oxides and possibly inert gases are obtained;{'sub': 4', '4, 'Da) separating off non-condensable and low-boiling gas components comprising oxygen, low-boiling hydrocarbons, possibly carbon oxides and possibly inert gases as gas stream d2 from the gas stream c2 by absorbing the Chydrocarbon-comprising butadiene and n-butenes in an absorbent, wherein an absorbent stream loaded with Chydrocarbons and the gas stream d2 are obtained, and'}{'sub': 4', '4, 'Db) subsequent desorption of the Chydrocarbons from the loaded absorbent stream in a desorption column, wherein a Cproduct gas stream d1 is obtained,'}wherein a polymerization inhibitor is added in step Db) at the column head of the desorption column.12. The method according to further comprising:{'sub': '4', 'E) separating the Cproduct stream d1 by extractive distillation using a solvent selective for butadiene into a material stream e1 comprising butadiene and the selective solvent, and a material stream e2 comprising n- ...

Transalkylation Processes for Converting Aromatic Hydrocarbons Comprising Alkyl-Demethylation

Alkyl-demethylation of C2+-hydrocarbyl substituted aromatic hydrocarbons can be utilized to treat one or more of a heavy naphtha reformate stream, a hydrotreated SCN stream, a C8 aromatic hydrocarbon isomerization feed stream, a C9+ aromatic hydrocarbon transalkylation feed stream, and similar hydrocarbon streams to produce additional quantity of xylene products.

Oligomerization Reactor Wash Process Using By-Product Solvent Recovered Using a Thin Film Evaporator

A method for washing an oligomerization reactor using by-product solvent recovered from the reactor can include: catalytically converting a monomer in a reactor section in a reaction mode in the presence of a catalyst to form a product stream comprising an oligomer, a by-product solvent, and a polymeric by-product; separating the product stream into a first fraction comprising the oligomer and a second fraction comprising a mixture of the by-product solvent and the polymeric by-product; and separating, in a thin film evaporator, the second fraction into a third fraction comprising the by-product solvent and a fourth fraction comprising the polymeric by-product. 1. A method comprising:catalytically converting a monomer in a reactor section in a reaction mode in the presence of a catalyst to form a product stream comprising an oligomer, a by-product solvent, and a polymeric by-product;separating the product stream into a first fraction comprising the oligomer and a second fraction comprising a mixture of the by-product solvent and the polymeric by-product; andseparating, in a thin film evaporator, the second fraction into a third fraction comprising the by-product solvent and a fourth fraction comprising the polymeric by-product.2. The method of claim 1 , further comprising delivering a recycled portion of the by-product solvent to the reactor section in a wash mode; wherein the recycled portion of the by-product solvent comprises the third fraction.3. The method of claim 1 , wherein the product stream claim 1 , the second fraction claim 1 , and the fourth fraction each further comprise at least a portion of the catalyst.4. The method of claim 1 , further comprising:delivering the recycled portion of the by-product solvent to a collection vessel in the reaction mode; anddelivering the recycled portion of the by-product from the collection vessel to the reactor section in the wash mode.5. The method of claim 1 , wherein the first fraction comprises further comprises ...

Processes for producing polymer grade light olefins from mixed alcohols

Processes for providing a high purity olefin product are described. The processes involve dehydrating a feedstream comprising a mixture of alcohols having 3 to 8 carbon atoms and forming a mixed olefin stream and a water stream, the mixed olefin stream comprising a mixture of olefins having 3 to 8 carbon atoms. The mixed olefin stream is separated into at least a C 3 olefin stream comprising olefins having 3 carbon atoms and a C 4-8 olefin stream comprising olefins having 4 to 8 carbon atoms. The C 4-8 olefin stream is separated into a C 4 olefin stream comprising olefins having 4 carbon atoms and a C 5-8 olefin stream comprising olefins having 5 to 8 carbon atoms. At least one of the C 3 olefin stream and the C 4 olefin stream is purified.

NAPHTHA COMPLEX WITH THERMAL OXIDATION SYSTEM

A process for treating effluent streams in a naphtha complex is described. One or more of the sour water stripping unit for the NHT sour water from the NHT, the amine treatment unit and the caustic treatment unit for the NHT stripper off-gas, the caustic scrubber unit or other chloride treatment unit for the off-gas from the C-Cisomerization zone and the Cisomerization zone, and the caustic scrubber unit or other chloride treatment unit for the regenerator off-gas are replaced with a thermal oxidation system. 1. A process for treating off-gas and water effluent streams in a naphtha complex comprising:{'sub': 5', '6', '5', '6', '4', '4, 'claim-text': [{'sub': 5', '6', '4', '2', '2', '2', '2', '2, 'thermally oxidizing the at least one of the NHT stripper off-gas stream, the C-Cisomerization stabilizer off-gas stream, the regenerator off-gas stream, the Cisomerization stabilizer off-gas stream, and the NHT sour water stream in a thermal oxidizing section forming flue gas consisting essentially of at least one of HO, CO, N, O, SOx, NOx, HCl, Cl, dioxins, and furans;'}, 'optionally recovering waste heat from the flue gas in a waste heat recovery section;', {'sub': 2', '2', '2', '2', '2', '2, 'claim-text': quenching the flue gas in a quench section to form quenched flue gas after recovering the waste heat; and', {'sub': 3', '2', '2', '3', '2', '4', '2', '3', '2', '3', '4', '2', '4', '4, 'contacting a caustic solution or an NHbased solution with the quenched flue gas in scrubbing section to form the de-SOx outlet flue gas and a liquid stream comprising at least one of HO, NaSO, NaSO, NaHSO, NaCO, NaCl, (NH)SO, and NHCl;'}, 'or', {'sub': 2', '2', '2', '2', '2', '3', '2', '4', '3', '2', '4', '3', '3', '2', '2', '3', '4', '3', '2', '2', '3', '3', '2', '3', '2', '3', '2', '2, 'reacting the flue gas with a reactant in an SOx reaction section to form a reaction section flue gas consisting essentially of at least one of HO, CO, N, O, NaCl, NaCO, NaSO, NaNO, CaCl, CaSO, CaCO, Ca( ...

SYSTEM FOR RECOVERY OF PROPYLENE FROM A PROPANE DEHYDROGENATION PROCESS

In a propane dehydrogenation (PDH) process, the purpose of the deethanizer and chilling train systems is to separate the cracked gas into a methane-rich tail gas product, a C2, and a C3 process stream. By the use of staged cooling, process-to-process inter-change against propane feed to the reactor and use of high efficiency heat exchangers and distributed distillation techniques, refrigeration power requirements are reduced and a simple and reliable design is provided by the process described herein. 1. A system for recovering propylene from a propane dehydrogenation (PDH) process comprising a PDH Reactor , the system comprising:a Process Gas Dryer configured to feed dried process gas to a First Deethanizer Feed Chiller and chill it against propane;a First Deethanizer Feed Drum configured to receive the dried process gas from the First Deethanizer Feed Chiller;a Deethanizer configured to receive liquid from the First Deethanizer Feed Drum;a Process Gas Compressor (PGC) configured to receive overhead vapors from the First Deethanizer Feed Drum;a Second Deethanizer Feed Chiller configured to cool discharge from the PGC against propane;a Third Deethanizer Feed Chiller configured to cool discharge from the PGC with propylene refrigerant;a Second Deethanizer Feed Drum configured to receive discharge from the Third Deethanizer Feed Chiller and to send feed liquid to the Deethanizer;a Cold Box configured to receive, chill, and partially condense vapor from the Second Deethanizer Feed Drum;a First Cold Drum configured to separate process effluent from the Cold Box into vapor and liquid phases and recycling vaporized liquid to a first stage of the PGC;an overhead Deethanizer Condenser configured to partially condense overhead vapor against Propylene refrigerant;a Deethanizer Reflux Drum configured to separate process effluent from the overhead Deethanizer Condenser into vapor and liquid, sending a vapor phase to the Cold Box;a line directing the liquid from the Deethanizer ...

SEPARATION SEQUENCE FOR HYDROCARBONS FROM A GENTLE THERMAL CLEAVAGE

The invention describes a method for separating hydrocarbons in an installation for generating hydrocarbons from a hydrocarbon-containing charge by cleavage. The product gas of the cleavage, which contains gaseous hydrocarbons, is compressed, dried, and supplied as charge material into a separation stage (a front end C3/C4 separation). The front end C3/C4 separation comprises a C4 absorber and a depropanizer. A hydrocarbon fraction consisting of hydrocarbons having a maximum of 3 carbon atoms is obtained as a gaseous overhead product of the C4 absorber. A liquid hydrocarbon fraction consisting of hydrocarbons having at least 4 carbon atoms is obtained as a bottom product of the depropanizer. The front end C3/C4 separation comprises an additional process technological C2/C4 separation stage is arranged between the C4 absorber and the depropanizer. 1. A method for separating hydrocarbons in a facility for generating hydrocarbons from a hydrocarbonaceous feed by cleavage{'b': 1', '2', '5', '5, 'i': a', 'a', 'b, 'wherein the product gas of the cleavage which is formed as raw gas () and contains gaseous hydrocarbons is compressed () and dried (, ),'}and is conducted as feedstock into a separation stage (hereinafter: front end C3/C4 separation){'b': 1', '15', '17, 'in which the raw gas () is separated into a hydrocarbon fraction of hydrocarbons having a maximum of 3 carbon atoms () and a hydrocarbon fraction of hydrocarbons having at least 4 carbon atoms (),'}{'b': 6', '8, 'wherein the front end C3/C4 separation comprises in terms of the process a C4 absorber () and a depropanizer (),'}{'b': 15', '6, 'wherein a hydrocarbon fraction of hydrocarbons having a maximum of 3 carbon atoms is obtained as a gaseous overhead product () of the C4 absorber (),'}{'b': 17', '8, 'and wherein a liquid hydrocarbon fraction of hydrocarbons having at least 4 carbon atoms is obtained as a bottom product () of the depropanizer (), characterized in that'}{'b': '7', 'the front end C3/C4 ...

INTEGRATED PROCESSES FOR PARA-XYLENE PRODUCTION

Para-xylene production processes are disclosed, with such processes being integrated with extractive distillation or other separation to effectively separate, for example to remove and recover, ethylbenzene and other components that co-boil with the isomers of xylene. This allows for xylene isomerization, downstream of the separation of para-xylene from its other isomers, to be operated under milder conditions (e.g., liquid phase, absence of added hydrogen) without the need for ethylbenzene conversion. The associated decreased yields of byproducts such as light gases and non-aromatic hydrocarbons, together with the generation of purified ethylbenzene having value for styrene monomer production, can significantly improve overall process economics. 1. A process for producing para-xylene , the process comprising:{'sub': 8', '9, 'sup': '+', 'in a xylene column, separating a Caromatic hydrocarbon stream and a C hydrocarbon stream, from an impure ethylbenzene-containing feed;'}{'sub': '8', 'in a xylene separation zone, separating a para-xylene rich product from at least a portion of the Caromatic hydrocarbon stream, to provide a para-xylene-depleted effluent;'}in an isomerization zone, isomerizing at least a portion of the para-xylene-depleted effluent, to provide a xylene-equilibrated isomerate;recycling at least a portion of the xylene-equilibrated isomerate to the xylene column, and{'sub': 8', '8, 'separating, in an ethylbenzene (EB) separation unit, an ethylbenzene-rich product from (i) all or a portion of the impure ethylbenzene-containing feed to provide an ethylbenzene-depleted feed, (ii) a portion of the Caromatic hydrocarbon stream to provide an ethylbenzene-depleted Caromatic hydrocarbon stream, (iii) a portion of the para-xylene-depleted effluent to provide an ethylbenzene-, para-xylene-depleted effluent, (iv) a portion of the xylene-equilibrated isomerate to provide an ethylbenzene-depleted, xylene-equilibrated isomerate, or (v) any combination of (i), (ii), ( ...

Process for Removing Light Components from an Ethylene Stream

A process for removing light components from an ethylene stream may include providing a dried ethylene stream containing ethylene, ethane, CO, CO, H, CH, and C hydrocarbons. The process may include sending the dried ethylene stream to a stripper to produce an overhead stream containing ethylene, CO, Hand CH, and a bottom stream containing ethylene, ethane, CO, and C hydrocarbons. The gaseous phase on top of the stripper may be condensed in a heat exchanger cooled by a refrigerant stream to get a first gaseous phase and a first liquid phase. The first gaseous phase may be condensed in a heat exchanger cooled by liquid ethane or liquid ethylene to get a second gaseous phase containing ethylene CO, Hand CHand a second liquid phase. The first and second liquid phases may be the reflux of the stripper. 119-. (canceled)20. A process for removing light components from an ethylene stream comprising:{'sub': 2', '2', '4', '3+, 'a) providing a dried ethylene stream (A) comprising ethylene, ethane, CO, CO, H, CH, C hydrocarbons and optionally oxygenates;'} [{'sub': 2', '4, 'an overhead gaseous stream (B) comprising ethylene, CO, Hand CH; and'}, {'sub': 2', '3+, 'a bottom stream (C) comprising ethylene, ethane, CO, C hydrocarbons and optionally oxygenates;'}], 'b) separating from said dried ethylene stream (A) in a separation mean that is a demethanizer or a stripper to formc) cooling the overhead gaseous stream (B) to a temperature ranging from −10° C. to −45° C. to get a first gaseous stream (D) and a first liquid stream (E);{'sub': 2', '4, 'd) cooling the first gaseous stream (D) to a temperature ranging from −10° C. to −45° C. lower than the temperature of step c) to get a second gaseous stream (F) comprising ethylene CO, Hand CHand a second liquid stream (G); and'}e) sending the first and second liquid streams (E) and (G) to the separation mean as a reflux.21. The process according to claim 20 , wherein the cooling of step c) is performed with a refrigerant stream that ...

HEPTANE FROM A PLANT SOURCE, FOR THE EXTRACTION OF NATURAL PRODUCTS

The present description relates to heptane obtained from a plant source, wherein the plant source comprises . Uses of said heptane in perfumery, cosmetics and food flavoring are also described. 1Commiphora wildiiCommiphora wildii. A heptane composition obtained from a plant source , wherein the plant source comprises , and wherein the heptane composition is prepared by a process of extraction comprising hydrodistilling or steam distilling a resin of to obtain an essential oil.2. (canceled)3. The heptane composition as claimed in claim 1 , wherein the process further comprises physically purifying the essential oil.4. The heptane composition as claimed in claim 3 , wherein physically purifying comprises distilling by fractional distillation or by molecular distillation.5. The heptane composition as claimed in claim 1 , wherein a content of linear isomer n-heptane is above 99.0%.6. The heptane composition as claimed in claim 1 , wherein the essential oil is obtained in an amount of about 5.5% based on a fresh weight of resin.7. The heptane composition as claimed in claim 1 , wherein the process further comprises collecting resin from plants of a cultivated type or wild type.8. The heptane composition as claimed in claim 1 , wherein the process further comprises collecting resin from a whole plant.9. A method of using the heptane composition as claimed in claim 1 , the method comprising extracting one or more natural products with a solvent comprising the heptane composition.10mimosa. The method as claimed in claim 9 , wherein the natural product comprises rose claim 9 , jasmine claim 9 , lily claim 9 , violet claim 9 , claim 9 , tuberose or any other plant useful in perfumery claim 9 , cosmetics and food flavoring.11. (canceled) The present description relates to heptane obtained from a plant source, for example by a process of extraction including distilling a resin from a plant source. The present description also relates to methods of using the heptane in perfumery ...

METHOD OF PRODUCING A FUEL ADDITIVE

A method of producing a fuel additive includes passing a feed stream comprising C hydrocarbons through a hydrogenation unit producing a hydrogenated stream; passing the hydrogenated stream through a distillation unit producing a first stream and a second stream; producing an isobutylene stream by passing the first stream through a molecular sieve unit; passing the isobutylene stream to a hydration unit as a feedstock for the fuel additive; and forming the fuel additive in the hydration unit. 1. A method of producing a fuel additive , comprising:passing a feed stream comprising C4 hydrocarbons through a hydrogenation unit producing a hydrogenated stream;passing the hydrogenated stream through a distillation unit producing a first stream and a second stream;producing an isobutylene stream by passing the first stream through a molecular sieve unit;passing the isobutylene stream to a hydration unit as a feedstock for the fuel additive; andforming the fuel additive in the hydration unit.2. The method of claim 1 , wherein the feed stream comprises at least one of propylene claim 1 , ethyl acetylene claim 1 , vinyl acetylene claim 1 , propadiene claim 1 , 1 claim 1 ,3-butadiene claim 1 , 1 claim 1 ,2-butadiene claim 1 , isobutylene claim 1 , cis-2-butene claim 1 , trans-2-butene claim 1 , 1-butene claim 1 , isobutane claim 1 , n-butane claim 1 , or propene.3. The method of claim 1 , wherein the first stream comprises isobutane and isobutylene.4. The method of claim 1 , wherein the second stream comprises 1-butene and 2-butene.5. The method of claim 1 , wherein greater than or equal to 85% by weight of any butadiene present in the feed stream is converted to 1-butene and/or 2-butene within the hydrogenation unit.6. The method of claim 1 , further comprising passing a water stream through the hydration unit.7. The method of claim 1 , further comprising adding tertiary butyl catechol and/or hydrogen to the feed stream prior to passing through the hydrogenation unit.8. The ...

INTEGRATION METHODS OF GAS PROCESSING PLANT AND NITROGEN REJECTION UNIT FOR HIGH NITROGEN FEED GASES

Gas processing plants and methods are contemplated in COis effectively removed to very low levels from a feed gas to an NRU unit by adding a physical solvent unit that uses waste nitrogen produced by the NRU as stripping gas to produce an ultra-lean solvent, which is then used to treat the feed gas to the NRU unit. Most preferably, the physical solvent unit includes a flash unit and stripper column to produce the ultra-lean solvent. 1. A gas treatment plant for treatment of a feed gas that includes COand N , comprising:{'sub': 2', '2, 'a primary COremoval unit configured to receive a feed gas from a feed gas source, and further configured to remove from the feed gas COto a first concentration to so form a treated feed gas;'}{'sub': 2', '2', '2', '2', '2, 'a secondary COremoval unit fluidly coupled to the primary COremoval unit and configured to receive the treated feed gas, and further configured to use an ultra-lean solvent in an absorber to produce a CO-loaded solvent and a CO-depleted feed gas having residual COat a second concentration; and'}{'sub': 2', '2', '2, 'a nitrogen rejection unit configured to remove Nfrom the CO-depleted feed gas and to produce a Nwaste stream and a pipeline gas;'}{'sub': 2', '2', '2, 'wherein the secondary COremoval unit comprises a flash unit and a stripping column fluidly coupled to the absorber, wherein the flash unit is configured to flash the CO-loaded solvent and to produce a flashed solvent, and wherein the stripping column is configured to use the Nwaste stream as a stripping gas for the flashed solvent to thereby produce the ultra-lean solvent.'}2. The plant of wherein the feed gas source is a hydrocarbon production well and wherein the feed gas has a Nconcentration of at least 10 mol % and a COconcentration of at least 2 mol %.3. The plant of wherein the feed gas source is a hydrocarbon production well and wherein the feed gas a pressure of at least 1000 psig.4. The plant of wherein the primary COremoval unit comprises an ...

Process and Apparatus for Recovering Aromatic Hydrocarbons

The present invention relates to an improved extractive distillation process for recovering aromatic hydrocarbons from non-aromatic hydrocarbons in naphtha streams containing heavy hydrocarbon contaminants wherein each contaminant is characterized as having a boiling point in the range of between that of the separated non-aromatic hydrocarbons and the extractive distillation solvent utilized to recover and purify the aromatic hydrocarbons.

METHOD FOR ISOLATION OF CYMENE

The invention relates to a method of isolating cymene comprising the following steps: a) providing a solution comprising cymene and monoterpenes, b) adding sulphuric acid to the solution in a) such that the concentration of sulphuric acid in the solution is at least 0.5% (w/w), such as 1-25% (w/w), c) distilling the solution mixture from step b) such that a target chemical stream enriched in cymene is obtained and separated from a residual stream. 114.-. (canceled)15. A method of isolating cymene comprising:a) providing a solution comprising cymene and monoterpenes,b) adding sulphuric acid to the solution in a) such that the concentration of sulphuric acid in the solution is at least 0.5% (w/w),c) distilling the solution mixture from b) such that a target chemical stream enriched in cymene is obtained and separated from a residual stream.16. The method according to claim 15 , the concentration of sulphuric acid in the solution is 1-25% (w/w).17. The method according to claim 15 , the concentration of sulphuric acid in the solution is 3-25%.18. The method according to claim 15 , wherein at least part of the monoterpenes from step a) react to one of the following selected from diterpenes claim 15 , triterpenes claim 15 , oligoterpenes and polyterpenes in one or both of b) and c).19. The method according to claim 15 , wherein the majority of the terpenes in the residual stream in c) is in the form of one of the following selected from diterpenes claim 15 , triterpenes claim 15 , oligoterpenes and polyterpenes.20. The method according to claim 19 , wherein at least 50% of the terpenes in the residual stream in c) is in the form of one of the following selected from diterpenes claim 19 , triterpenes claim 19 , oligoterpenes and polyterpenes.21. The method according to claim 19 , wherein at least 90% of the terpenes in the residual stream in c) is in the form of one of the following selected from diterpenes claim 19 , triterpenes claim 19 , oligoterpenes and polyterpenes. ...

PRODUCTION OF BIOMETHANE USING MULTIPLE TYPES OF MEMBRANE

The invention relates to a process for recovering methane from digester biogas or landfill gas. More specifically, the invention pertains to a method for producing biomethane that removes impurities from a compressed digester biogas with staged membrane modules of at least two different types, to produce a biomethane having at least 94% CH, below 3% of CO, and below 4 ppm of HS. 1. A method for producing biomethane , comprising:compressing a biogas feed in a compressor to produce a compressed feed stream;passing said compressed feed stream to a first separation stage comprising at least one polymeric gas separation membrane to retain a first gas mixture comprising at least 60% of methane, and to permeate a first low-quality gas mixture comprising impurities present in said biogas feed stream and less than 20% of methane;sending a stream of said first gas mixture into a second separation stage comprising at least one polymeric gas separation membrane, to retain a second gas mixture containing at least 94% of methane, and to permeate a second permeate gas mixture comprising impurities present in said biogas feed stream and less than 70% of methane;recycling a stream of said second permeate gas mixture to said compressor; andwithdrawing said second gas mixture from said second separation stage as biomethane, wherein said membrane of said first separation stage is substantially different from said membrane of said second separation stage, and said method excludes the use of regenerable adsorbent.2. The method of claim 1 , wherein said biogas feed contains 40-75% of methane (“CH”) claim 1 , and impurities of:{'sub': '2', 'up to 10% nitrogen (“N”);'}{'sub': '2', 'up to 1% oxygen (“O”);'}{'sub': '2', '20-55% of carbon dioxide (“CO”);'}{'sub': '2', 'up to 5,000 ppm of hydrogen sulfide (“HS”);'}siloxanes;up to 2,000 ppm of VOC's; andwater.3. The method of claim 1 , further comprising a step of passing said compressed feed stream to a water removal apparatus to remove water ...

METHOD FOR SEPARATING MATERIALS BY MEANS OF AN EXTRACTIVE DISTILLATION PROCESS

A method for separating a mixture of materials A and B by extractive distillation, using an extraction medium having a higher affinity to B than to A, wherein a feed stream comprising A and B is conducted towards the extraction medium in a column, wherein an overhead fraction comprising A and also a liquid fraction comprising B and extraction medium are obtained, the liquid fraction is collected on a collecting tray and heated and partially evaporated in a first indirect heat exchanger, the resultant vapor is released into the column and a non-evaporated proportion of the liquid fraction is collected as sump fraction in the sump of the column, the sump fraction is successively heated in a second indirect heat exchanger and a third indirect heat exchanger and in part evaporated, wherein the resultant vapor is at least in part released into the column, the sump fraction is separated in a stripper into a fraction comprising B and an extraction medium fraction, the extraction medium fraction is used as heating medium for the second heat exchanger, wherein a partially cooled extraction medium fraction is obtained, and an external heating medium is used for the third heat exchanger, and the partially cooled extraction medium fraction is used as heating medium for the first heat exchanger. 1: A method for separating a mixture of a material A and a material B by extractive distillation , using an extraction medium having a higher affinity to B than to A , wherein the method comprises:a) conducting a feed stream comprising A and B towards the extraction medium in a column, wherein an overhead fraction comprising A, and also a liquid fraction comprising B and extraction medium, are obtained,b) collecting the liquid fraction on a collecting tray and heating and partially evaporating the liquid fraction in a first indirect heat exchanger, where a first resultant vapor is released into the column and a non-evaporated proportion of the liquid fraction is collected as a sump ...

Xylene Production Processes and Systems

A process and related system for producing para-xylene (PX). In an embodiment, the process includes (a) separating a feed stream comprising C aromatic hydrocarbons into a toluene containing stream and a C hydrocarbon containing stream and (b) contacting at least part of the toluene containing stream with a methylating agent in a methylation unit to convert toluene to xylenes and produce a methylated effluent stream. In addition, the process includes (c) recovering PX from the methylated effluent stream in (b) to produce a PX depleted stream and (d) transalkylating the PX depleted stream to produce a transalkylation effluent stream. The transalkylation effluent stream includes a higher concentration of toluene than the PX depleted stream. Further, the process includes (e) converting at least some ethylbenzene (EB) within the C hydrocarbon containing stream into toluene and (f) flowing the toluene converted in (e) to the contacting in (b). 1. A process for producing para-xylene (PX) , the process comprising:{'sub': 6+', '8+, '(a) separating a feed stream comprising C aromatic hydrocarbons into at least a toluene containing stream and a C hydrocarbon containing stream;'}(b) contacting at least part of the toluene containing stream with a methylating agent in a methylation unit under conditions effective to convert toluene to xylenes and produce a methylated effluent stream;(c) recovering PX from the methylated effluent stream in (b) to produce a PX depleted stream;(d) transalkylating the PX depleted stream to produce a transalkylation effluent stream, wherein the transalkylation effluent stream includes a higher concentration of toluene than the PX depleted stream;{'sub': '8+', '(e) converting at least some ethylbenzene (EB) within the C hydrocarbon containing stream into toluene; and'}(f) flowing the toluene converted in (e) to the contacting in (b).2. The process of claim 1 , further comprising:{'sub': 7', '8+, '(g) separating from the transalkylation effluent stream ...

SYSTEMS AND METHODS OF PRODUCING AROMATIC PRODUCTS

Systems and methods for producing aromatic products are provided. An aromatic stream is provided with aromatic compounds and olefins. The olefins are reacted with aromatic compounds to form colored bodies, and the aromatic stream is distilled to produce an overhead stream and reboiler stream. The colored bodies are in the reboiler stream, and the reboiler stream is passed through an absorbent to remove the colored bodies. 1. A method of producing toluene , the method comprising the steps of:processing a feed naphtha stream with a naphtha processing unit to produce a processed naphtha stream;separating the processed naphtha stream into an aromatic stream and a non-aromatic stream, wherein the aromatic stream primarily comprises toluene and benzene;reacting olefins remaining in the aromatic stream to produce colored bodies;distilling the aromatic stream to produce an overhead stream and a reboiler stream, wherein the reboiler stream comprises toluene and colored bodies; andremoving the colored bodies from the reboiler stream by passing the reboiler stream through an absorbent, wherein the absorbent selectively absorbs colored bodies over toluene.2. A method of producing aromatic products , the method comprising the steps of:providing an aromatic stream, where the aromatic stream comprises aromatic compounds and olefins;reacting the olefins with the aromatic compounds in the aromatic stream to form colored bodiesdistilling the aromatic stream to produce an overhead stream and a reboiler stream, wherein the reboiler stream comprises the colored bodies; andpassing the reboiler stream through an absorbent to remove the colored bodies.3. The method of where providing the aromatic stream further comprises providing an aromatic stream primarily comprising benzene and toluene.4. The method of wherein providing the aromatic stream further comprises processing a feed naphtha stream with a reforming process claim 3 , wherein aromatic compounds are produced in the reforming ...

PROCESSES AND APPARATUSES FOR PRODUCTION OF BUTADIENE

Processes and apparatuses for the production of butadienes are provided. In an embodiment, a process for production of butadienes includes passing a reactor feed stream comprising a hydrocarbon stream comprising butene, a steam stream and a oxygen rich stream to a dehydrogenation reactor. The reactor feed stream is oxidatively dehydrogenated in the dehydrogenation reactor in presence of an oxidative dehydrogenation catalyst to provide an effluent stream comprising butadiene. The effluent stream is cooled in a quench tower to provide a cooled effluent stream and a bottoms water stream. The cooled effluent stream is passed to an aldehyde scrubber to provide a scrubbed effluent stream and a spent water stream comprising aldehydes. A first portion of the bottoms water stream is passed from the quench tower to the aldehyde scrubber. 1. A process for the production of butadienes comprising:a) passing a reactor feed stream comprising a hydrocarbon stream comprising butene, a steam stream and a oxygen rich stream to a dehydrogenation reactor;b) oxidatively dehydrogenating the reactor feed stream in the dehydrogenation reactor in presence of an oxidative dehydrogenation catalyst to provide an effluent stream comprising butadiene;c) cooling the effluent stream in a quench tower to provide a cooled effluent stream and a bottoms water stream;d) passing the cooled effluent stream to an aldehyde scrubber to provide a scrubbed effluent stream and a spent water stream comprising aldehydes; ande) passing a first portion of the bottoms water stream from the quench tower to the aldehyde scrubber.2. The process of further comprising passing the scrubbed effluent stream and an absorption oil stream to the absorber column claim 1 , wherein C4's including butadiene in the scrubbed effluent stream are absorbed in the absorption oil and an overhead absorber stream comprising light gases is separated.3. The process of further comprising passing the absorption oil comprising the C4's through ...

METHODS FOR EXTRACTING ESSENTIAL OILS, TERPENES, TERPENOIDS AND OTHER ORGANIC MATTER FROM PLANTS; AND RELATED SYSTEMS AND DEVICES

A method for extracting resins and oils from a plant includes: 1) tumbling, inside a container at a temperature of at most 50 degrees Fahrenheit with a tumbler, plant fibers having one or more portions that contain resins and/or oils; 2) colliding the tumbler with the plant fibers to release the one or more portions that contain resins and/or oils from the remainder of the plant fibers; and 3) segregating the one or more portions that contain resins and/or oils from the remainder of the plant fibers. 1. A method for extracting resins and oils from a plant; the method comprising:tumbling, inside a container at a temperature of at most 50 degrees Fahrenheit with a tumbler, plant fibers having one or more portions that contain resins and/or oils;colliding the tumbler with the plant fibers to separate the one or more portions that contain resins and/or oils from the remainder of the plant fibers; andsegregating the one or more portions that contain resins and/or oils from the remainder of the plant fibers.2. The method of wherein the temperature inside the container is 34 degrees Fahrenheit.3. The method of wherein the tumbler includes COin the solid phase.4. The method of wherein the tumbler includes fifty individual tumblers each separate from all the others.5. The method of wherein the plant fibers include lavender.6. The method of wherein the plant fibers include hops.7. The method of wherein the portions of the hops that contain resins and oils include lupulin glands of the hops.8. The method of wherein colliding the tumbler with a plant fiber includes the tumbler falling onto the plant fiber.9. The method of wherein colliding the tumbler with the plant fibers includes the tumbler forcing a plant fiber against the container's side.10. The method of wherein segregating the one or more portions that contain resins and oils from the remainder of the plant fibers claim 1 , includes filtering the portions from the remainder of the plant fibers with a screen that forms ...

Green Oil Removal From Ethylene Plants

A method may comprise: feeding a backend deethanizer overhead stream comprising ethylene, ethane, and acetylene to a hydrogenation reactor; hydrogenating at least a portion of the acetylene in the backend deethanizer overhead stream to form a reactor effluent stream comprising ethylene, ethane, and green oil; feeding the reactor effluent stream to a gas/liquid coalescer; and removing at least a portion of the green oil from the reactor effluent stream to produce a cleaned effluent stream. 16.-. (canceled)7. A method comprising: a front steering wheel assembly,', 'a rear wheel assembly,', 'a sensor package,', 'a corrosion package,', 'a tapered spring joint, and', 'a ported housing;, 'running a mud sensing hole finder into a borehole, wherein the mud sensing hole finder is capable of attachment to a wireline logging tool-string, wherein the mud sensing hole finder comprisesdiverting, with the ported housing, mud flow passed the sensor package and the corrosion package while the mud sensing hole finder is moving in a borehole;pulling the mud sensing hole finder from the borehole; andreversing a direction of the mud flow through the ported housing.8. The method of claim 7 , wherein the tapered spring joint is pivotable to facilitate lateral movement of the front steering wheel assembly passed obstructions in a borehole.9. The method of claim 7 , wherein the mud sensing hole finder further comprises a pressure sealed crossover to a logging vendor's wireline tool-string connection.10. The method of claim 7 , wherein the mud sensing hole finder further comprises a mandrel that holds a common axle and a set of profiled and grooved wheels.11. The method of claim 7 , further comprising acquiring data with a logging package for borehole diagnostics and wireline conveyance optimization.12. The method of claim 7 , further comprising providing corrosion analysis claim 7 , mechanical testing claim 7 , archiving claim 7 , or any combinations thereof.13. The method of claim 7 , ...

Method for decommisioning and regenerating a reactor for the oxidative dehydrogenation of n-butenes

The invention relates to a process for preparing butadiene from n-butenes in n reactors R 1 to Rn operated in parallel, wherein the process in the production phase of a reactor Rm in the n reactors comprises the steps: A) provision of a feed gas stream a 1 m comprising n-butenes; B) feeding of the feed gas stream a 1 m comprising n-butenes, an oxygen-comprising gas stream a 2 m and a substream d 2 m of an oxygen-comprising total recycle gas stream d 2 into the oxidative dehydrogenation zone of the reactor and oxidative dehydrogenation of n-butenes to butadiene, giving a product gas substream bm comprising butadiene; C) combination of the product gas substream bm with further product gas substreams to form a total product gas stream b and cooling and compression of the total product gas stream b and condensation of at least part of the high-boiling secondary components, giving at least one aqueous condensate stream c 1 and a gas stream c 2 comprising butadiene; D) feeding of the gas stream c 2 into an absorption zone and separation of incondensable and low-boiling gas constituents as gas stream d from the gas stream c 2 by absorption of the C 4 -hydrocarbons in an absorption medium, giving an absorption medium stream d 1 loaded with C 4 -hydrocarbons and a recycle gas stream d 2 , and recirculation of a substream d 2 m of the total recycle gas stream d 2 into the reactor Rm, and during the regeneration phase of the reactor Rm further reactors are in the production phase and the regeneration phase of the reactor Rm comprises the steps in the order i) to v): i) reduction of the feed gas stream a 1 m comprising n-butenes and of the oxygen-comprising gas stream a 2 m and the feeding of an inert gas stream a 4 m into the reactor Rm; ii) further reduction of the feed gas stream a 1 m comprising n-butenes down to 0, reduction of the recycle gas substream d 2 m and increase of the inert gas stream a 4 m until the oxygen content in the reactor Rm is from 2 to 3% by volume; ...

METHODS FOR GENERATING PURIFIED CYCLOPROPENES

The present invention relates to methods of preparing purified cyclopropylene (1-methylcyclopropylene) gas employing one or more non-reactive purification processes to purify substances including, without limitation, cyclopropene (1-methylcyclopropylene) gas and/or lithio-cyclopropene. 1. A method of preparing a purified cyclopropene gas , comprising:reacting a lithium-based precursor of a cyclopropene gas with water to generate an unpurified 1-methylcyclopropene gas; andproducing a purified 1-methylcyclopropene gas by scrubbing the unpurified 1-methylcyclopropene gas with non-reactive scrubber, wherein the non-reactive scrubber is a polar or non-polar, non-reactive and at least partially removes synthesis and/or reaction contaminants from the generated unpurified 1-methylcyclopropene gas,wherein the purified 1-methylcyclopropene gas has an impurity presence of less than 0.1% for any of the at least one synthesis and/or reaction contaminant impurities.2. The method of claim 1 , further comprising synthesizing the lithium-based precursor by reacting an allyl compound with a non-nucleophilic strong base claim 1 , wherein the ratio of the allyl compound claim 1 , including but not limited to an allylic halide claim 1 , to strong base is from 20:1 claim 1 , to 10:1 claim 1 , to 5:1 claim 1 , to 1:1 to 1:2.3. The method of claim 1 , wherein the lithium-based precursor can be a lithio-cyclopropene and the ratio of water to the lithio-cyclopropene can range from 20:1 claim 1 , to 15:1 claim 1 , to 10:1 claim 1 , to 1:1 claim 1 , to 1:2.4. The method of claim 1 , wherein the lithium-based precursor can be suspended in a mineral oil having a viscosity range from 2 to 350 mm/s at 40° C. claim 1 , or from 3 to 310 mm/s at 40° C.5. The method of claim 1 , wherein the non-reactive scrubber can be at least one of a polar and/or non-polar claim 1 , non-reactive water and/or solvent-based mixture claim 1 , and the number of each non-reactive scrubber employed can range from 1 to 10 ...

SIMULATED MOVING BED SEPARATORS AND METHODS FOR ISOLATING A DESIRED COMPONENT

A simulated moving bed separator and methods for isolating a desired component are provided. A method includes removing a raffinate from a raffinate bed of a simulated moving bed separator. The raffinate includes an undesired component, and the simulated moving bed separator includes a plurality of adsorbent beds circularly coupled together, a distributor, and a plurality of conduits coupling the distributor to the plurality of adsorbent beds. The adsorbent beds include the raffinate bed, a desorbent bed, and a zone 4 flush bed positioned between the raffinate bed and the desorbent bed. Desorbent is added to the desorbent bed through a desorbent conduit. The zone 4 flush conduit is flushed to the desorbent conduit, where the zone 4 flush conduit is coupled to the zone 4 flush bed. 1. A method of separating a desired component from a mixed feed , the method comprising the steps of:removing a raffinate from a raffinate bed of a simulated moving bed separator, wherein the raffinate comprises an undesired component, wherein the simulated moving bed separator comprises a plurality of adsorbent beds circularly coupled together, a distributor, and a plurality of conduits fluidly coupling the distributor to the plurality of adsorbent beds, and wherein the plurality of adsorbent beds comprises the raffinate bed, a desorbent bed, and a zone 4 flush bed positioned between the raffinate bed and the desorbent bed;adding a desorbent to the desorbent bed through a desorbent conduit; andflushing a zone 4 flush conduit to the desorbent conduit, wherein the zone 4 flush conduit is fluidly coupled to the zone 4 flush bed.2. The method of wherein flushing the zone 4 flush conduit comprises flushing the zone 4 flush conduit wherein the zone 4 flush bed is directly adjacent to the raffinate bed.3. The method of wherein flushing the zone 4 flush conduit comprises increasing a net negative flow in the zone 4.4. The method of further comprising:changing the zone 4 flush bed to the raffinate ...

REACTOR EFFLUENT WASH TO REMOVE AROMATICS

A process is presented for the removal or aromatics from a hydrocarbon stream. The hydrocarbon stream is generated by a dehydrogenation process that generates aromatics. The process includes a two contact cooler system with the first and second contact coolers using different coolants. The second coolant is a non-aromatic hydrocarbon coolant that will absorb aromatics. 1. A process for removing aromatics from a process stream , comprising:passing the process stream comprising paraffins, olefins and trace aromatics to a first contact cooler using a first coolant to generate a first stream;passing the first stream to a compressor to generate a second stream; andpassing the compressed stream to a second contact cooler using a second coolant to generate a third stream comprising olefins and paraffins.2. The process of further comprising:passing a hydrocarbon stream comprising paraffins to a dehydrogenation reactor to generate the process stream comprising olefins and paraffins.3. The process of further comprising passing the third stream to a cryogenic separation unit to generate an olefin and paraffin product stream.4. The process of wherein the first coolant comprises an aromatic solvent as a coolant.5. The process of wherein the second coolant comprises a paraffinic solvent or an alkylate solvent.6. The process of wherein the first stream is cooled to a temperature between 10° C. and 45° C.7. The process of wherein the first stream is compressed to a pressure between 250 kPa and 600 kPa.8. The process of wherein the first stream has a reduced aromatics content.9. The process of wherein the first stream has an aromatics content below 1500 ppmw.10. The process of wherein the third stream has an aromatics content below 100 ppmw.11. The process of wherein the third stream is cooled to a temperature between 10° C. and 45° C.12. A process for the production of olefins from paraffins claim 1 , comprising:passing a hydrocarbon stream comprising paraffins to a dehydrogenation ...

PROCESSES AND APPARATUSES FOR RECOVERY OF ETHYLENE FROM HYDROCARBONS

Embodiments of methods and apparatuses for recovery of ethylene from FCC absorber off-gas comprising a heavy cut comprising ethylene, ethane and heavier hydrocarbons and a light cut comprising hydrogen, nitrogen and methane. An exemplary method includes passing the FCC absorber off-gas to an adsorption zone containing an adsorbent selective for the adsorption of the light cut, the adsorption zone adsorbing at least a portion of the light cut and recovering an adsorption zone effluent stream comprising the heavy cut. The adsorption zone effluent is passed to a demethanizer column to provide an overhead stream comprising hydrogen, nitrogen, methane, ethylene and ethane and a net bottoms stream comprising ethylene, ethane and the heavier hydrocarbons. 1. A process for the concentration and recovery of a heavy cut comprising ethylene , ethane and heavier hydrocarbons from a hydrocarbon feed stream comprising a light cut and the heavy cut , the light cut comprising hydrogen , nitrogen and methane , the process comprising the following steps:a) passing the hydrocarbon feed stream to an adsorption zone containing an adsorbent selective for the adsorption of the light cut, the adsorption zone adsorbing at least a portion of the light cut and recovering an adsorption zone effluent stream comprising the heavy cut; andb) passing the adsorption zone effluent to a demethanizer column to provide an overhead stream comprising hydrogen, nitrogen, methane, ethylene and ethane and a net bottoms stream comprising ethylene, ethane and the heavier hydrocarbons.2. The process of further comprising recycling the overhead stream to the adsorption zone.3. The process of further comprising sending the net bottoms stream to a Csplitter for recovery of ethylene.4. The process of claim 1 , wherein the adsorption zone adsorbs at least about 70% of methane present in the light cut.5. The process of claim 1 , wherein the adsorption zone adsorbs at least about 80% of each of hydrogen and nitrogen ...

COUPLING OF UNIT FOR EXTRACTING METHYL-SUBSTITUTED AROMATICS WITH UNIT FOR HYDROGENOLYSING ALKYL-AROMATICS

The present invention relates to a device and a process for converting aromatic compounds, wherein: methyl-substituted aromatic compounds are extracted from a hydrocarbon feedstock () comprising aromatic compounds having at least 8 carbon atoms in an extraction unit (), to produce at least one effluent enriched in methyl-substituted aromatic compounds (A, B) and an effluent depleted in methyl-substituted aromatic compounds (); and C2+ alkyl chains of the aromatic compounds of the depleted effluent () are converted into methyl groups in a hydrogenolysis unit () placed downstream of the extraction unit (), to produce a hydrogenolysis effluent enriched in methyl-substituted aromatic compounds ().

ETHYLENE SEPARATIONS USING SMALL PORE ZEOLITES CONTAINING DOUBLE-SIX RINGS AND CAGES

The present invention describes a process to separate ethylene products from impurities such as nitrogen, hydrogen, ethane, propane and isobutane without the need for distillation processes. 1. A method for removing impurities from a feed gas stream of ethylene-containing stranded gas including impurities and ethylene , comprising:(a) alternating an input of the feed gas stream between an at least two beds of a one or more adsorbent particles made from a homogeneous mixture, wherein the one or more adsorbent particles comprise a zeolite SSZ-98 or a zeolite SSZ-105;(b) wherein the feed gas stream contacts one of the at least two beds at a given time by an adsorption step and a product gas stream is simultaneously vented from another of the at least two beds by a desorption step;(c) wherein a contacting in the one of the at least two beds occurs at a feed pressure of from about 345 kPa to about 3450 kPa for a sufficient time to preferentially adsorb the ethylene from the feed gas stream and thereby producing a product gas stream during the desorption step containing no greater than about 2 mol % impurities, at least about 98 mol % of the ethylene recovered from the feed gas stream; and(d) wherein the feed gas stream is input at a feed end of each of the at least two beds, the product gas stream is removed from the feed end of each of the at least two beds during the desorption step, and the impurity-enriched gas stream is produced from the tail gas end of the at least two beds.2. The method of wherein the impurities are nitrogen claim 1 , hydrogen claim 1 , propane claim 1 , isobutane and ethane.3. The method of claim 1 , wherein the zeolite SSZ-98 or the zeolite SSZ-105 has a Si:Al mole ratio of from 5 to 100.4. The method of claim 1 , wherein the zeolite SSZ-98 or the SSZ-105 has a cation as a framework ion and the cation is selected from the group consisting of a sodium claim 1 , a calcium claim 1 , a potassium claim 1 , a lithium claim 1 , a magnesium claim 1 , a ...

SEPARATION OF OFF GASES FROM C3 HYDROCARBONS IN PROPANE DEHYDROGENATION PROCESS

Methods and systems for separating Chydrocarbons from lighter hydrocarbons, carbon monoxide, carbon dioxide, and water are provided. In certain embodiments, the methods include feeding a gaseous mixture including C, C, and Chydrocarbons and benzene solvent to the absorber column where benzene solvent selectively absorbs Chydrocarbons. The methods can further include removing a first stream comprising benzene solvent and absorbed Chydrocarbons from the absorber column, and feeding the first stream to a stripper column where benzene solvent is separated from Chydrocarbons, and removing a second stream comprising Chydrocarbons from the stripper column. 1. A method for separating Chydrocarbons from a gaseous mixture comprising C , C , and Chydrocarbons , the method comprising:(a) feeding the gaseous mixture to an absorber column;{'sub': '3', '(b) feeding benzene solvent to the absorber column, wherein benzene solvent selectively absorbs Chydrocarbons;'}{'sub': '3', '(c) removing a first stream comprising benzene solvent and absorbed Chydrocarbons from the absorber column;'}{'sub': '3', '(d) feeding the first stream to a stripper column where benzene solvent is separated from Chydrocarbons; and'}{'sub': '3', '(e) removing a second stream comprising Chydrocarbons from the stripper column.'}2. The method of claim 1 , wherein the gaseous mixture further comprises hydrogen claim 1 , carbon monoxide claim 1 , carbon dioxide claim 1 , water or combinations thereof.3. The method of claim 1 , wherein the Chydrocarbons comprise methane.4. The method of claim 1 , wherein the Chydrocarbons comprise ethane claim 1 , ethylene claim 1 , or combinations thereof.5. The method of claim 1 , wherein the Chydrocarbons comprise propane claim 1 , propylene claim 1 , or combinations thereof.6. The method of claim 1 , further comprising removing a third stream comprising Cand Chydrocarbons from the absorber column.7. The method of claim 6 , further comprising removing a fourth stream comprising ...

Membrane permeation treatment with adjustment of the temperature of the first retentate as a function of the ch4 concentration in the third and/or fourth permeate

A facility and method for membrane permeation treatment of a feed gas flow containing at least methane and carbon dioxide that includes a compressor, a pressure measurement device, at least one valve, and first, second, third, and fourth membrane separation units for separation of CO 2 from CH 4 to permeates enriched in CO 2 and retentates enriched in CH 4 , respectively. A temperature of the first retentate is adjusted at an inlet of the second membrane separation unit with at least one heat exchanger as a function of the measured CH 4 concentration in such a way so as to reduce the determined difference.

MEMBRANE PERMEATION TREATMENT WITH ADJUSTMENT OF THE NUMBER OF MEMBRANES USED AS A FUNCTION OF THE PRESSURE OF THE FEED GAS FLOW

A facility and method for membrane permeation treatment of a feed gas flow containing at least methane and carbon dioxide that includes a compressor, a pressure measurement device, at least one valve, and first, second, third, and fourth membrane separation units for separation of COfrom CHto permeates enriched in COand retentates enriched in CH, respectively. The at least one valve adjusts the number of membranes combined and connected to the flow of gas entering into at least one of the membrane separation units as a function of the pressure recorded by the pressure measurement device. 1. A facility for the membrane permeation treatment of a feed gas flow containing at least methane and carbon dioxide , comprising:a compressor for compressing the feed gas flow;a first membrane separation unit able to receive a flow of gas from the compressor and supply a first permeate and a first retentate, the first membrane separation unit comprising a plurality of membranes;a second membrane separation unit able to receive the first retentate and supply a second permeate and a second retentate, the second membrane separation unit comprising a plurality of membranes;a third membrane separation unit able to receive the first permeate and supply a third permeate and a third retentate, the third membrane separation unit comprising a plurality of membranes;a fourth membrane separation unit able to receive the third retentate and supply a fourth permeate and a fourth retentate, the fourth membrane separation unit comprising a plurality of membranes;a pressure measurement device able to measure a pressure of a flow of gas flowing into or out of the first membrane separation unit; andat least one valve able to adjusting a number of the plurality of membranes in at least one of the membrane separation units that receive a flow of gas therein as a function of the measured pressure.2. The facility of claim 1 , wherein the pressure measurement device measures a pressure of gas flow at an ...

Production and Use of 3,4' and 4,4'-Dimethylbiphenyl Isomers

Processes are described for separating 3,4′- and 4,4′-dimethylbiphenyl from a mixture comprising at least 3,3′-, 3,4′- and 4,4′-dimethylbiphenyl. In the processes, the mixture is cooled to produce a crystallization product comprising at least of the 4,4′-dimethylbiphenyl from the feed mixture and a first mother liquor product. The first mother liquor product is distilled to produce a bottoms stream enriched in 4,4′-dimethylbiphenyl as compared with the first mother liquor product and an overhead stream deficient in 4,4′-dimethylbiphenyl as compared with the first mother liquor product. The overhead stream is then cooled to produce a second crystallization product comprising at least part of the 3,4′-dimethylbiphenyl from the overhead stream and a second mother liquor product. 1. A process for producing 3 ,4′- and 4 ,4′-dimethylbiphenyl , the process comprising:(a) cooling a feed mixture comprising at least 3,3′-, 3,4′- and 4,4′-dimethylbiphenyl to produce (i) a first crystallization product comprising at least part of the 4,4′-dimethylbiphenyl from the feed mixture, and (ii) a first mother liquor product;(b) distilling at least part of the first mother liquor product to produce a bottoms stream enriched in 4,4′-dimethylbiphenyl as compared with the first mother liquor product and an overhead stream depleted in 4,4′-dimethylbiphenyl as compared with the first mother liquor product; and(c) cooling at least part of the overhead stream to produce (i) a second crystallization product comprising at least part of the 3,4′-dimethylbiphenyl from the overhead stream, and (ii) a second mother liquor product.2. The process of claim 1 , wherein the cooling step (a) comprises cooling the feed mixture to a first temperature from −30 to 40° C.3. The process of claim 2 , wherein the cooling step (a) comprises cooling the feed mixture to a first temperature from −6 to 40° C.4. The process of claim 1 , wherein the cooling step (c) comprises cooling at least part of the overhead stream ...

METHOD FOR SEPARATING AROMATIC HYDROCARBON USING EXTRACTIVE DISTILLATION

A method for separating aromatic hydrocarbons by an extractive distillation, comprising introducing a hydrocarbon mixture containing aromatic hydrocarbons into the middle of an extractive distillation column (); introducing an extraction solvent into the upper part of the extractive distillation column; after an extractive distillation, a raffinate containing benzene is discharged from the top of the column, wherein the benzene content is 3-40% by mass, and sent to the lower part of the extraction column (); the extraction solvent is introduced to the upper part of the extraction column for a liquid-liquid extraction; a raffinate liquid free of aromatic hydrocarbons is discharged from the top of the extraction column; a rich solvent containing benzene is discharged from the bottom of the column and enters the upper-middle part of the extractive distillation column; the rich solvent obtained at the bottom of the extractive distillation column is sent to the solvent recovery column to separate the aromatic hydrocarbons and the solvent. By combining an extractive distillation with a liquid-liquid extraction ingeniously, the method can achieve the separation of aromatic hydrocarbons with a high purity and a high recovery rate, and a significant decrease of the energy consumption in the extraction and separation process. 1. A method for separating aromatic hydrocarbons by an extractive distillation , comprising following operations:(1) introducing a hydrocarbon mixture containing aromatic hydrocarbons is introduced into the middle part of an extractive distillation column; introducing an extraction solvent into the upper part of the extractive distillation column; after an extractive distillation, discharging a raffinate containing benzene from the top of the extractive distillation column, wherein the benzene content is 3-40% by mass; and a rich solvent rich in aromatic hydrocarbons is obtained at the bottom of the extractive distillation column,(2) sending the ...

SEPARATION METHODS AND SYSTEMS FOR OXIDATIVE COUPLING OF METHANE

The present disclosure provides a method for generating higher hydrocarbon(s) from a stream comprising compounds with two or more carbon atoms (C), comprising introducing methane and an oxidant (e.g., O) into an oxidative coupling of methane (OCM) reactor. The OCM reactor reacts the methane with the oxidant to generate a first product stream comprising the C compounds. The first product stream can then be directed to a separations unit that recovers at least a portion of the C compounds from the first product stream to yield a second product stream comprising the at least the portion of the C compounds. 1134.-. (canceled)135. A method for generating compounds with two or more carbon atoms (C compounds) , comprising:{'sub': 2', '4', '2', '4', '2', '4', '2', '6', '2', '6', '2', '4', '2+', '2', '4', '2', '6', '1', '4, '(a) directing oxygen (O) and methane (CH) into an oxidative coupling of methane (OCM) reactor having a first section and a second section downstream of said first section, to produce a product stream, which first section reacts said Oand CHin an OCM process to yield ethylene (CH), ethane (CH), and heat, which second section uses said heat to convert said CHfrom said first section into CHin a non-OCM process, and which product stream comprises (i) C compounds including CHand CHand (ii) Ccompounds including un-reacted CH;'}{'sub': 2', '4', '2', '6', '1, '(b) directing said product stream into a first separations unit containing a metal organic framework (MOF) that produces (i) a first stream comprising said CH, (ii) a second stream comprising said CH, and (iii) a third stream comprising said Ccompounds;'}(c) directing said second stream into said second section;{'sub': 2', '1', '2', '2, '(d) directing said third stream into a second separations unit comprising a COseparations unit to create a fourth stream comprising said Ccompounds, which COseparation unit employs sorbent or solvent separation of CO; and'}(e) directing said fourth stream into said first ...

PROCESS FOR THE PRODUCTION OF HIGH PURITY PARA-XYLENE AND HIGH PURITY TOLUENE

A process for the production of high purity toluene and para-xylene is described. More specifically, the process involves the production of high purity toluene produced via a light-desorbent selective adsorption process for para-xylene production, such as light desorbent para-xylene extraction, without the need for dedicated solvent extraction or olefin removal from the toluene stream. 1. A process for producing high purity toluene and para-xylene in a para-xylene complex comprising:separating an extract stream comprising para-xylene and toluene from an adsorbent chamber into an overhead stream comprising C6− compounds and a bottoms stream comprising para-xylene and toluene in a first para-xylene fractionation column;separating the bottoms stream from the first para-xylene fractionation column in a second para-xylene fractionation column into a sidedraw stream comprising high purity para-xylene, an overhead stream comprising toluene, and a bottoms stream comprising C9+ aromatics;recovering the sidedraw stream as a high purity para-xylene stream; andrecovering at least a portion of the overhead stream from the second para-xylene fractionation column as a high purity toluene product stream.2. The process of wherein the overhead stream from the second para-xylene fractionation column comprises high purity toluene.3. The process of further comprising;separating the overhead stream from the second para-xylene fractionation column in a toluene fractionation column into an overhead stream comprising high purity toluene and a bottom stream comprising xylenes, and wherein the high purity toluene product stream comprises the overhead stream from the toluene fractionation column.4. The process of further comprising:introducing a mixed xylenes stream and a toluene stream into the adsorption chamber comprising a para-xylene selective adsorbent; andseparating the mixed xylenes stream and the toluene stream into the extract stream and a stream comprising ortho-xylene, meta-xylene, ...

Efficiency of a Gas Conditioning System via Hydrate Inhibitor Injection

A gas conditioning system is described herein. The system includes a slug catcher configured to separate a hydrocarbon feed stream into a liquid stream and a gas stream, and a first hydrate inhibitor injection unit configured to lower a hydrate formation temperature of the gas stream using a first hydrate inhibitor. The system includes a pressure reduction unit, a first separation unit configured to remove a first liquid stream including the first hydrate inhibitor from the gas stream, a mercury removal unit, and an acid gas removal unit. The system also includes a second hydrate inhibitor injection unit configured to further lower the hydrate formation temperature of the gas stream using a second hydrate inhibitor, a cooling unit, a second separation unit configured to remove a second liquid stream including the second hydrate inhibitor from the gas stream, and a dehydration unit configured to produce a final treated gas stream. 1. A gas conditioning system , comprising:a slug catcher configured to separate a hydrocarbon feed stream into a liquid stream and a gas stream;a first hydrate inhibitor injection unit configured to inject a first hydrate inhibitor into the gas stream such that a hydrate formation temperature of the gas stream is altered from a first hydrate formation temperature to a second, lowered hydrate formation temperature;a pressure reduction unit configured to reduce a pressure of the gas stream;a first separation unit configured to remove a first liquid stream comprising condensed water combined with the first hydrate inhibitor and condensed hydrocarbons from the gas stream;a mercury removal unit configured to remove mercury from the gas stream;an acid gas removal unit configured to remove acid gases from the gas stream;a second hydrate inhibitor injection unit configured to inject a second hydrate inhibitor into the gas stream such that the hydrate formation temperature of the gas stream is altered from a third hydrate formation temperature to a ...

Systems and Methods for Deep Crystallization of Xylene Streams

Methods for the production of para-xylene include flowing a xylenes-containing stream comprising PX, meta-xylene (MX), and ortho-xylene (OX), to a first crystallization stage. In addition, the methods include lowering a temperature of the xylenes-containing stream to below the eutectic point of the xylenes-containing stream within the first crystallization stage to crystallize at least some of the PX and at least some of one of both of the MX and the OX within the xylenes-containing stream. Further, the methods include separating the xylenes-containing stream into a first crystallization effluent stream and a first filtrate stream. 1. A process , comprising:(a) flowing a xylenes-containing stream comprising para-xylene (PX), meta-xylene (MX), and ortho-xylene (OX), to a first crystallization stage;(b) lowering a temperature of the xylenes-containing stream to 10° F. or more below the eutectic point of the xylenes-containing stream within the first crystallization stage to crystallize at least some of the PX and at least some of one of both of the MX and the OX within the xylenes-containing stream; and(c) separating the xylenes-containing stream into a first crystallization effluent stream and a first filtrate stream after (b).2. The process of claim 1 , wherein the first filtrate stream comprises about 6 to 7 wt. % PX or less based on the total weight of xylenes within the first filtrate stream.3. The process of claim 2 , further comprising:(d) flowing at least a portion of the first filtrate stream to a first liquid phase isomerization unit to produce a first isomerized stream; and(e) recycling the first isomerized stream to the first crystallization stage.4. The process of claim 3 , further comprising:(f) flowing a feed stream to a separation tower before (a) to produce the xylenes-containing stream;(g) separating the xylenes-containing stream from the feed stream within the separation tower;(h) flowing at least a portion of the first filtrate stream to a vapor ...

Process for Recovering Olefins from Manufacturing Operations

A process for treating an effluent gas stream arising from a manufacturing operation that produces an olefin or an olefin derivative to recover unreacted olefin. The process involves compressing the effluent gas stream, which comprises an olefin, a paraffin, and a third gas, to produce a first compressed stream, then directing the first compressed stream to a membrane separation pretreatment step. The permeate stream withdrawn from this step is enriched in olefin and is sent to a second compressor, which produces a second compressed stream that is then cooled and condensed. The condensation step produces a liquid condensate and an uncondensed gas stream. The uncondensed gas stream undergoes a second membrane separation step to produce another olefin-enriched permeate stream, which is recirculated within the process prior to the second compression step, and an olefin-depleted residue stream, which may be purged from the process.

REMOVAL OF CARBONYLS FROM GASEOUS HYDROCARBON STREAMS

Disclosed are methods and systems for removing a highly reactive polymer precursor such as acetaldehyde and acetone from a hydrocarbon gas stream. Embodiments may disclose a method for removal of carbonyls comprising providing a hydrocarbon gas stream comprising a carbonyl, providing a liquid bisulfite stream, and contacting the hydrocarbon gas stream and liquid bisulfite stream in a mass transfer device wherein at least a portion of the carbonyl reacts with the bisulfite to form a solid adduct that is soluble in the liquid bisulfite stream. 1. A method for removal of carbonyls comprising:providing a hydrocarbon gas stream comprising at least one carbonyl;providing a liquid bisulfite stream comprising at least one bisulfite; andcontacting the hydrocarbon gas stream and the liquid bisulfite stream in a mass transfer device wherein at least a portion of the carbonyls react with the bisulfite to form a solid adduct that is soluble in the liquid bisulfite stream.2. The method of claim 1 , wherein the mass transfer device is a column and wherein the column comprises internals selected from the group consisting of packing and trays.3. The method of claim 1 , wherein the mass transfer device is a static mixer.4. The method of claim 1 , wherein the mass transfer device is a bottoms section of a caustic tower.5. The method of claim 1 , wherein the metal bisulfite is selected from the group consisting of sodium bisulfite claim 1 , potassium bisulfite claim 1 , magnesium bisulfite claim 1 , strontium bisulfite claim 1 , and combinations thereof.6. The method of claim 1 , wherein the hydrocarbon gas stream further comprises an acid gas wherein the acid gas comprises at least one acid gas selected from the group consisting of CO claim 1 , HS claim 1 , and combinations thereof; andwherein the hydrocarbon gas stream is further contacted with an acid gas removing agent after the step of contacting with the liquid bisulfite stream.7. The method of claim 6 , wherein the acid gas ...

Process for separating and recovering NGLs from hydrocarbon streams

This process comprises using unconventional processing of hydrocarbons, e.g. natural gas, for recovering C2+ and NGL hydrocarbons that meet pipeline specifications, without the core high capital cost requirement of a demethanizer column, which is central to and required by almost 100% of the world's current NGL recovery technologies. It can operate in Ethane Extraction or Ethane Rejection modes. The process uses only heat exchangers, compression and simple separation vessels to achieve specification ready NGL. The process utilizes cooling the natural gas, expansion cooling, separating the gas and liquid streams, recycling the cooled streams to exchange heat and recycling selective composition bearing streams to achieve selective extraction of hydrocarbons, in this instance being NGLs. The compactness and utility of this process makes it feasible in offshore applications as well as to implementation to retrofit/revamp or unload existing NGL facilities. Many disparate processes and derivatives are anticipated for its use. 1. A process for separating less volatile hydrocarbons from more volatile hydrocarbons while also producing stabilized condensates or NGL , comprising the steps of:a. providing a pressurized feedstock stream comprising hydrocarbons;b. directing the feedstock stream as a feed stream to a heat exchanger and then cooling the feed stream in the heat exchanger;c. further cooling the feed stream from the heat exchanger via a first gas expansion assembly;d. directing the further cooled stream from the first gas expansion assembly to a first gas/liquid mixer and separation vessel assembly and separating the further cooled stream into gas and liquid streams, wherein the first gas/liquid mixer and separation vessel assembly is capable of receiving one or more recycle streams from one or more downstream processing steps;e. directing the liquid stream from the first gas/liquid mixer and separation vessel assembly to a splitter pump capable of directing fractions ...

Integrated coalescing system for separating dispersed ionic liquid from liquid hydrocarbon

An integrated coalescing system for separating ionic liquid from a liquid hydrocarbon is provided, comprising: a. a bulk settler, that separates an emulsion comprising the dispersed ionic liquid with a wide range of droplet sizes into a clean ionic liquid phase and a separated liquid hydrocarbon phase comprising retained droplets; b. a pre-coalescer that receives the separated liquid hydrocarbon phase, separates out solid particles from the separated liquid hydrocarbon phase, and begins to form coalesced droplets of the retained droplets; and c. a coalescer that receives an effluent from the pre-coalescer, wherein the at least one coalescer comprises multiple layers of media having a fine pore size, and produces a clean hydrocarbon stream that is free of the dispersed ionic liquid and additional amounts of the clean ionic liquid phase. Also, a process is provided for separating an ionic liquid from a liquid hydrocarbon, using the integrated coalescing system.

PROCESS FOR PRODUCING A SWEETENED HYDROCARBON STREAM

A process of producing a sweetened liquid hydrocarbon stream. In order to prevent the forming of acid species in a sweetening zone, a oxygenate removal zone is disposed upstream of the sweetening zone. The oxygenate removal zone may comprise a water wash or an adsorbent zone, including a regenerable adsorbent. The sweetened stream is formed from a least a portion of liquid natural gas stream which may be scrubbed free of hydrogen sulfide and dehydrated before passing to the oxygenate removal zone. 1. A process for producing a sweetened hydrocarbon stream , the process comprising:passing a liquid hydrocarbon stream to an oxygenate removal zone;removing oxygenates from the liquid hydrocarbon stream in the oxygenate removal zone to form an oxygenate lean stream;passing the oxygenate lean stream to a sweetening zone to convert mercaptans in the oxygenate lean stream in disulfide and produce a sweetened hydrocarbon stream.2. The process of wherein the oxygenates comprise at least one of glycols claim 1 , poly glycols claim 1 , organic acids claim 1 , aldehydes claim 1 , ketones claim 1 , ethers claim 1 , esters and alcohols claim 1 , and the oxygenate removal zone comprises a water wash.3. The process of wherein the oxygenate removal zone comprises an adsorbent zone.4. The process of wherein the adsorbent zone comprises a regenerable adsorbent.5. The process of further comprising:desorbing oxygenates from the regenerable adsorbent to provide a desorbent stream rich in oxygenates; and,combining the desorbent stream rich in oxygenates with the sweetened hydrocarbon stream.6. The process of wherein the sweetening zone includes a catalyst.7. The process of wherein the catalyst includes cobalt.8. The process of wherein the liquid hydrocarbon stream comprises a C+ hydrocarbon stream.9. The process of wherein the liquid hydrocarbon stream comprises a bottoms stream from a separation zone.10. The process of wherein the liquid hydrocarbon stream is lean in disulfides.11. A ...

PROCESS FOR THE RECOVERY OF PARAFFINS FROM AN ISOMERIZATION EFFLUENT

A process for the recovery of Chydrocarbons from a C/Cisomerization zone. A portion of the effluent stream from the C/Cisomerization zone comprising Chydrocarbons is combined in a stabilizer section with an effluent from a Cisomerization zone. In order to increase the Chydrocarbons in the effluent stream from the C/Cisomerization zone, a chilling zone may be used. 1. A process for the recovery of Chydrocarbons comprising:{'sub': '4', 'stabilizing and separating a first effluent stream in a first stabilization zone into an overhead stream, a C− liquid stream, and a bottoms stream, wherein the first effluent stream is from a first isomerization zone;'}stabilizing a second effluent stream from a second isomerization zone in a second stabilization zone;{'sub': '4', 'passing at least a portion of the C− liquid stream to the second stabilization zone; and,'}{'sub': 4', '4', '3, 'separating the second effluent stream and the at least a portion of the C− liquid stream into a Cstream and a C− stream.'}2. The process of further comprising:{'sub': 4', '4', '4, 'separating the Cstream into an iCstream and a nCstream.'}3. The process of further comprising:{'sub': '4', 'passing the iCstream to the second isomerization zone.'}4. The process of wherein the first stabilization zone comprises a stabilizer claim 1 , a receiving zone and a chilling zone.5. The process of further comprising:{'sub': '4', 'passing a C− stream from the stabilizer to the receiver;'}{'sub': 4', '4, 'separating the C− stream in the receiver into a vapor stream and a liquid stream, the liquid stream comprising the C− liquid stream.'}6. The process of further comprising:cooling the vapor stream from the receiver in the chilling zone.7. The process of further comprising:{'sub': '3', 'combining a portion of the vapor stream from the receiver and the C− stream of the second stabilization zone.'}8. The process of further comprising:operating the first isomerization zone under isomerization conditions, in the ...

Removal of carbonyls from gaseous hydrocarbon streams

Disclosed are methods and systems for removing a highly reactive polymer precursor such as acetaldehyde and acetone from a hydrocarbon gas stream. Embodiments may disclose a method for removal of carbonyls comprising providing a hydrocarbon gas stream comprising a carbonyl, providing a liquid bisulfite stream, and contacting the hydrocarbon gas stream and liquid bisulfite stream in a mass transfer device wherein at least a portion of the carbonyl reacts with the bisulfite to form a solid adduct that is soluble in the liquid bisulfite stream.

PROCESS FOR PURIFYING HYDROCARBON STREAMS USING LOW REACTIVITY ADSORBENTS

This present disclosure relates to processes for removing contaminants from hydrocarbon streams, e.g. removing chlorides, CO, COS, HS, AsH, methanol, mercaptans and other S- or O-containing organic compounds from olefins, paraffins, aromatics, naphthenes and other hydrocarbon streams. The process involves contacting the stream with an adsorbent which comprises a zeolite, an alumina component and a metal component e.g. sodium, in an amount at least 30% of the zeolite's ion exchange capacity. 1. A process for removing contaminants from hydrocarbon streams comprising contacting the hydrocarbon stream comprising olefins , paraffins , aromatics , naphthenes having a boiling point of about 50° C. to about 180° C. , preferably about 50° C. to about 115° C. with an adsorbent at adsorption conditions to remove a portion of at least one chloride containing contaminant wherein the adsorbent comprising a zeolite component , a binder , and a metal component to produce a hydrocarbon product stream.2. The process of claim 1 , wherein the zeolite is selected from the group consisting of zeolite X claim 1 , zeolite Y claim 1 , zeolite A claim 1 , and mixtures thereof.3. The process of claim 1 , wherein the binder is selected from the group consisting of alumina claim 1 , silica claim 1 , clay claim 1 , alumina silicate claim 1 , tinania claim 1 , zirconia claim 1 , and mixtures thereof.4. The process of claim 2 , wherein the zeolite is zeolite X.5. The process of claim 1 , wherein the adsorbent has a silica to alumina ratio of between about 2.0 to about 2.5 claim 1 , preferably about 2.1.6. The process of claim 1 , wherein the adsorption conditions include a temperature of about 50° C. to about 150° C. claim 1 , preferably about 120° C.7. The process of claim 1 , wherein the metal component is an alkali metal selected from the group consisting of sodium claim 1 , potassium claim 1 , lithium claim 1 , rubidium claim 1 , cesium claim 1 , and mixtures thereof.8. The process of claim 6 ...

Alkylaromatic Sulfonate Compositions From Mixed Hydrocarbons

Provided herein are various methods for forming alkylaromatic sulfonate compositions and blended alkylaromatic sulfonate compositions, and such compositions themselves. The methods of various embodiments include obtaining a C 8 -C 30 hydrocarbon mixture, optionally treating the mixture to concentrate the mixture in sulfonatable aromatics, and sulfonating the mixture to form the alkylaromatic sulfonates. The mixture or treated mixture may be blended with linear alkyl benzene (LAB) compositions and sulfonated, and/or the alkylaryl sulfonates may be blended with linear alkylbenzene sulfonate (LAS) compositions, to form the blended alkylaromatic sulfonates of some embodiments. These compositions and processes for making them may be tailored to serve a variety of end uses, such as detergents in cleaning solutions or for enhanced oil recovery operations, and/or as low foaming and/or hydrotropic additives in detergent formulations, and the like.

RECOVERY OF ETHYLENE FROM METHANOL TO OLEFINS PROCESS

Olefins may be recovered from a methanol to olefins reactor effluent by initially feeding the effluent to an absorber demethanizer to contact the effluent with an absorbent to recover an overheads including methane and ethylene and a bottoms including the absorbent, ethylene, and ethane. The bottoms are separated to recover an ethylene fraction and an ethane fraction. The overheads are cooled and partially condensed in a first heat exchanger to a temperature of −40° C. or greater. The resulting stream, or a portion thereof, may be further cooled and condensed via indirect heat exchange with a mixed refrigerant to a temperature of less than −40° C. The non-condensed vapors are separated from the condensed liquids to form a liquid fraction and a methane fraction. The liquid fraction is fed to the absorber demethanizer as reflux, and the methane and ethane fractions combined to form the mixed refrigerant. 1. A process for recovery of the olefins from a methanol to olefins reactor effluent , the process comprising:feeding an effluent from a methanol-to-olefins reactor system comprising methane, ethylene, and ethane to an absorber demethanizer;contacting at least a portion of the effluent with an absorbent in the absorber demethanizer to recover an overheads vapor fraction comprising methane and ethylene and a bottoms fraction comprising the absorbent, ethylene, and ethaneseparating the bottoms fraction via one or more extractive distillation and/or distillation stages to recover an ethylene fraction and an ethane fraction;cooling and partially condensing the overheads vapor fraction in a first heat exchanger to a temperature of about −40° C. or greater;cooling and partially condensing at least a portion of the cooled and partially condensed overhead vapor fraction, via indirect heat exchange with a mixed refrigerant comprising methane and ethane, in a second heat exchanger to a temperature of less than about −40° C.;separating non-condensed vapors from the liquids ...

Linear Alpha Olefin Process Using Temperature Control in Oligomerization Reactor

The present disclosure provides assemblies for producing linear alpha olefins and methods for producing linear alpha olefins. In at least one embodiment, a method for producing a linear alpha olefin includes providing an olefin, a catalyst, and a process solvent to a first tubular reactor; obtaining an effluent from the first tubular reactor; and transferring the effluent to a second tubular reactor. In at least one embodiment, an assembly for producing linear alpha olefins includes a first tubular reactor having a first end and a second end; an effluent line having a first end and a second end, the first end coupled with the second end of the first tubular reactor; and a second tubular reactor having a first end and a second end, the first end coupled with the second end of the effluent line. 1. A method for producing a linear alpha olefin , comprising:providing an olefin, a catalyst, and a process solvent to a first tubular reactor under oligomerization conditions;obtaining an effluent produced in the first tubular reactor;transferring the effluent to a second tubular reactor under oligomerization conditions; andobtaining an effluent produced in the second tubular reactor.2. The method of claim 1 , further comprising providing steam to a first steam jacket disposed around the first tubular reactor and providing steam to a second steam jacket disposed around the second tubular reactor.3. The method of claim 2 , further comprising controlling the pressure of steam in the first steam jacket with a valve disposed on the outlet of the steam jacket to provide a temperature (T1) within the first steam jacket.4. The method of claim 3 , further comprising controlling the pressure of steam in the second steam jacket with a valve disposed on the outlet of the steam jacket to provide a temperature (T2) within the second steam jacket.5. The method of claim 4 , wherein temperature (T1) is greater than temperature (T2).6. The method of claim 4 , wherein temperature (T1) and ...

Linear Alpha Olefin Process Using Solvent Flash Drum for Olefin Separation

The present disclosure provides assemblies for producing linear alpha olefins and methods for producing linear alpha olefins. In at least one embodiment, a method for producing a linear alpha olefin includes providing an olefin, a catalyst, and a process solvent to a reactor under oligomerization conditions; obtaining an effluent produced in the reactor; and transferring the effluent to a solvent-containing portion of a flash drum via a first effluent line coupled with the flash drum. In at least one embodiment, an assembly for producing linear alpha olefins includes a configuration to provide olefin, catalyst and process solvent coupled with a reactor; a flash drum; a first effluent line coupled with the reactor at a first end and coupled with the flash drum at a second end; and a second effluent line coupled with the flash drum at a first end and coupled with the first effluent line at a second end. 1. A method for producing a linear alpha olefin , comprising:providing an olefin, a catalyst, and a process solvent to a reactor;obtaining an effluent produced in the reactor; andtransferring the effluent to a solvent-containing portion of a flash drum via a first effluent line coupled with the flash drum.2. The method of claim 1 , further comprising controlling the flow rate of effluent transferred to the flash drum with a V-Ball valve.3. The method of claim 1 , further comprising providing heat to the effluent line using one or more heaters coupled with the effluent line.4. The method of claim 1 , wherein the temperature in the flash drum is 130° C. or greater.5. The method of claim 4 , further comprising transferring an effluent from the flash drum to a knockout drum via an effluent line and cooling the effluent using a chiller coupled with the effluent line.6. The method of claim 5 , further comprising transferring a first effluent from the knockout drum to the reactor and transferring a second effluent from the knockout drum to the flash drum.7. The method of ...

Catalytic Alkane Conversion and Olefin Separation

Disclosed is a hydrocarbon conversion process that is less energy intensive than comparable processes. The hydrocarbon conversion process is particularly desirable for converting alkanes, such as methane into C 2+ olefins, such as ethylene and propylene, particularly with increasing selectivity to ethylene production. It is also desirable for effectively removing a C 2 composition (i.e., ethane, ethylene and/or acetylene) produced from the catalytic conversion of hydrocarbon comprised of C 2+ olefins. In addition, the hydrocarbon process is desirable for providing a substantially non-cryogenic separation of the desired C 2 compositions from the hydrocarbons (e.g., methane) present in the reaction mixture.

Catalytic Alkane Conversion

Disclosed is a hydrocarbon conversion process in which an alkane component is catalytically converted in the presence of an oxygen or oxidizing component (i.e., oxidant). The hydrocarbon conversion process can be an oxidative coupling reaction, which refers to the catalytic conversion of alkane in the presence of oxidant to produce an olefin product, i.e., a composition containing Colefin. Reverse-flow reactors can be used to carry out the oxidative coupling reaction. 1. An alkane conversion process , comprising:(a) providing a first flow, the first flow comprising alkane and oxidant and having an alkane : oxidant molar ratio ≧2.0;(b) providing a catalytic flow-through reactor configured to accept the first flow, the catalytic flow-through reactor comprising at least one hydrocarbon conversion catalyst and at least one thermal mass, wherein (i) the hydrocarbon conversion catalyst has an initial average temperature in the range of 550° C. to 1100° C., (ii) at least a first portion of the thermal mass is located downstream of the hydroconversion catalyst with respect to the first flow's flow direction, and (iii) the first portion of the thermal mass has an initial average temperature such that the hydroconversion catalyst's initial average temperature minus the first portion of the thermal mass's initial average temperature is ≧50° C.; the catalytic conversion includes catalytically transferring hydrogen from the alkane to the oxidant and', 'the reaction mixture comprises (i) olefin produced by the catalytic transfer and (ii) any unreacted alkane and/or any unreacted oxidant;, '(c) catalytically converting at least a portion of the alkane in the presence of the hydrocarbon conversion catalyst to produce a reaction mixture, wherein'}(d) quenching the reaction mixture in the flow-through reactor by transferring heat from the reaction mixture to the thermal mass at a location downstream of the hydroconversion catalyst, downstream being with respect to the first flow's ...

MEMBRANE SEPARATION PROCESS USING MIXED VAPOR-LIQUID FEED

The present invention pertains to a pervaporation membrane process for the separation of high octane fuel components from a gasoline feed stream comprising feeding a mixed phase vapor-liquid feed to a cyclone separation means to separate the liquid from the vapor, then sending the saturated vapor to the membrane, thereby extending the useful life of the membrane. 1. An apparatus for the separation of high octane components from a feed stream , said feed stream including aromatic and non-aromatic hydrocarbons and having a boiling range of at least 50° C. , said apparatus comprising:means for heating the feed stream to produce a combination vapor and liquid feed stream;means for separating the liquid feed stream from the vapor feed stream, a pervaporation membrane that selectively permeates high octane aromatics and oxygenates from the vapor feed stream;means for collecting the permeate of the pervaporation membrane;means for collecting the retentate of the pervaporation membrane and the liquid from the separating means.2. The apparatus of claim 1 , wherein the separation means is a cyclone and said feed stream is gasoline.3. The apparatus of claim 2 , further including pressure control means claim 2 , wherein feed pressure Pand feed temperature Tto the pervaporation membrane are selectively controlled to condense a liquid layer upon the membrane.4. The apparatus of claim 3 , wherein said feed stream is a gasoline containing oxygenates that comprise methanol claim 3 , ethanol claim 3 , propanol claim 3 , and butanol.5. A process for extending the life of a pervaporation membrane for separating high octane components from a gasoline feed stream claim 3 , including aromatics and non-aromatics and having a boiling point of at least 50° C. comprising:{'sub': f', 'f, 'heating the gasoline at a temperature Tunder pressure Pto partially vaporize the gasoline to produce a saturated vapor and a liquid from the gasoline;'}separating the vapor from the liquid;directing the vapor ...

AROMATIC HYDROCARBON PRODUCTION APPARATUS

An apparatus includes a first distillation apparatus for obtaining a fraction enriched in C8+ aromatics; a second distillation apparatus for obtaining a fraction enriched in C8 aromatics; an adsorption separation apparatus for obtaining an extract containing para-xylene and a raffinate containing xylene isomers; a third distillation apparatus for obtaining a fraction enriched in para-xylene; and a fourth distillation apparatus for obtaining a fraction enriched in xylene isomers. The second distillation apparatus includes a high-pressure part including a rectifying section; a low-pressure part including a stripping section; a line for directing overhead vapor of the low-pressure part to a column bottom of the high-pressure part; a line for directing a column bottom liquid of the high-pressure part to a column top of the low-pressure part; and a heat exchange structure for transferring heat from the rectifying section to the stripping section. 1. An aromatic hydrocarbon production apparatus , comprising:a first distillation apparatus configured to obtain, by distillation, from a feedstock, a fraction enriched in aromatic hydrocarbons having 8 or more carbon atoms and a fraction enriched in a component lighter than the aromatic hydrocarbons having 8 or more carbon atoms;a second distillation apparatus configured to obtain, by distillation, from the fraction enriched in aromatic hydrocarbons having 8 or more carbon atoms obtained from the first distillation apparatus, a fraction enriched in aromatic hydrocarbons having 8 carbon atoms and a fraction enriched in an aromatic hydrocarbon having 9 or more carbon atoms;an adsorption separation apparatus configured to separate para-xylene, by adsorption separation, from the fraction enriched in aromatic hydrocarbons having 8 carbon atoms obtained from the second distillation apparatus, and to obtain an extract and a raffinate, the extract being a stream containing a desorbent and para-xylene, and the raffinate being a stream ...

Process for recovering benzene and fuel gas in an aromatics complex

A process for separating xylene from a feedstock in which the feedstock is separated into a xylene stream, a benzene rich stream and a light ends stream. Two separation zones may be utilized in which liquid from both is sent to a compression zone and the vapor from the compression zone is combined with a stream prior to the stream entering the second separation zone.

PROCESS FOR RECOVERING BENZENE AND FUEL GAS IN AN AROMATICS COMPLEX

A process for separating xylenes from a feedstock in which the feedstock is separated into a xylene stream, a benzene rich stream and a light ends stream. Two separation zones may be utilized in which liquid from the first zone sent to a toluene recovery zone and vapor from the first zone is sent to a compression zone. The compressed vapor from the compression zone is sent to the second separation zone. 1. A process for the recovery of a benzene rich liquid stream and a light ends vapor stream in a xylene isomerization process from a feedstock , the process comprising:passing a feedstock into a deheptanizer in which the feedstock is separated into a deheptanizer vapor phase and a deheptanizer liquid phase, the deheptanizer vapor phase containing hydrocarbons with seven carbon atoms or less, and the deheptanizer liquid phase containing hydrocarbons with eight carbon atoms or more;passing the deheptanizer vapor phase from the deheptanizer to a first separation zone;separating the deheptanizer vapor phase in the first separation zone into a first liquid phase and a first vapor phase;passing the first liquid phase from the first separation zone to a toluene recovery comprising an overhead stream and a bottoms stream;passing the first vapor phase from the first separation zone to a compression zone in which the first vapor phase is compressed and partially condensed to provide a compressed and partially condensed vapor phase;passing the compressed and partially condensed vapor phase from the compression zone to the toluene recovery zone to be combined with the toluene recovery zone overhead stream, which is passed to a second separation zone;separating the compressed and partially condensed vapor phase into a second liquid phase and a second vapor phase in the second separation zone, the second vapor phase being a light ends vapor stream;recovering the light ends vapor stream;passing the second liquid phase back to the toluene recovery zone; andrecovering the benzene ...

INTEGRATED OXIDATIVE ALKANE DEHYDROGENATION AND HYDROGEN GENERATION PROCESS

As part of an integrated oxidative alkane dehydrogenation and hydrogen generation process, carbon dioxide from Pressure Swing Adsorption (PSA) off gas stream of Hydrogen Generation Unit (HGU), and alkane from any known source are sent to oxidative dehydrogenation (ODH) unit for producing high value olefins, such as ethylene, propylene and butenes. Products formed from ODH reactor are separated and the stream comprising of hydrogen, carbon monoxide and methane are recycled to Shift reactor of HGU unit for enhanced production of hydrogen at PSA. 1. An integrated process for catalytic oxidative dehydrogenation (ODH) of alkane(s) and for generation of hydrogen , the process comprising:a) feeding a fresh hydrocarbon alkane feed along with a carbon dioxide rich stream to an ODH reactor comprising of dehydrogenation catalyst, where the alkane feed gets converted into alkenes and producing an effluent gas comprising of hydrogen, methane, carbon monoxide, carbon dioxide, water and unreacted alkanes;{'sub': 4', '3', '2, 'b) separating ODH effluent gas from the ODH reactor in a Gas Separation system, wherein the Gas Separation system consists of a De-Propanizer section, a De-Butanizer and CSplitter section, a CSplitter section, a De-Methanizer section and a CSplitter section;'} [{'sub': 4+', '4', '4, '(i) a C stream consisting of Calkanes, Colefins and higher hydrocarbons;'}, {'sub': '3', '(ii) a Cstream consisting of propane and propylene; and'}, '(iii) an Off gas stream consisting of hydrogen, methane, ethane, ethylene, carbon monoxide and carbon dioxide in the De-Propanizer section;, 'c) separating the ODH effluent gases into{'sub': 4', '4, 'd) separating butanes, butene and heavy hydrocarbons from the C+ stream in the De-Butanizer and the CSplitter section and recycling back the butane to the ODH reactor for further conversion;'}{'sub': 3', '3, 'e) separating the Cstream into petrochemical grade propylene and a propane rich stream in a CSplitter and recycling back the ...

Linear Alpha Olefin Process Using Catalyst Deactivation with High Product Purity

The present disclosure provides assemblies for producing linear alpha olefins and methods for producing linear alpha olefins. In at least one embodiment, a method for producing a linear alpha olefin includes providing an olefin, a catalyst, and a process solvent to a reactor under oligomerization conditions; obtaining an effluent produced in the reactor; transferring the effluent through an effluent line; and providing a quench agent to the effluent line via a quench agent line coupled with the effluent line. In at least one embodiment, an assembly for producing linear alpha olefins includes a configuration to provide olefin, catalyst and process solvent coupled with a reactor; an effluent line coupled with the reactor at a first end and coupled with a mixer or a flash drum at a second end; and a quench agent line coupled with the effluent line at a first end. 1. A method for producing a linear alpha olefin , comprising:providing an olefin, a catalyst, and a process solvent to a reactor under oligomerization conditions; 'transferring the effluent through an effluent line; and', 'obtaining an effluent produced in the reactor;'}providing a quench agent to the effluent line via a quench agent line coupled with the effluent line.2. The method of claim 1 , further comprising controlling the flow rate of effluent transferred through the effluent line using a V-Ball valve coupled with the effluent line.3. The method of claim 1 , wherein transferring the effluent comprises transferring the effluent through the effluent line to a mixer.4. The method of claim 1 , wherein transferring the effluent comprises transferring the effluent through the effluent line to a flash drum.5. The method of claim 4 , wherein the flash drum has a pressure from 300 psi to 400 psi and a temperature from 100° C. to 150° C.6. The method of claim 1 , wherein the quench agent is provided to the effluent line via a dip tube coupled with a first end of the quench agent line and disposed within the ...

Process for the production of high purity isobutylene

Processes for the production of high purity isobutylene are disclosed. The processes may include supplying a mixed C4 feed stream to a catalytic distillation column, which may contain a butene isomerization catalyst. 1-butene is isomerized to 2-butene and concurrently in the catalytic distillation column the 2-butene is separated from the isobutane and isobutylene. The overheads fraction comprising the isobutane and isobutylene is then condensed in an overheads system and fed to a splitter, where the isobutane is separated from the isobutylene. The process further includes operating the catalytic distillation column at an overheads temperature greater than a bottoms temperature of the splitter, and heating a portion of the splitter bottoms stream via indirect heat exchange with at least a portion of the catalytic distillation column overheads fraction, thereby producing a heated bottoms stream (reboil vapor) fed to the splitter and a cooled overheads fraction.

PROCESS AND SYSTEM FOR EXTRACTION OF A FEEDSTOCK

The present invention relates to a method and system for recovering aromatics from a naphtha feedstock obtained from a crude petroleum, natural gas condensate, or petrochemical feedstock. The method and system comprise the steps of recovering an aromatics fraction from the feedstock prior to reforming. 127.-. (canceled)28. A method of recovering aromatics comprising the steps of:{'sub': 6', '11, '(a) providing a Cto Chydrocarbon fraction;'}{'sub': 6', '11, '(b) recovering from the Cto Chydrocarbon fraction an aromatics fraction, an aromatics precursors fraction and a raffinate fraction in an aromatics extraction unit;'}(c) converting aromatics precursors in the aromatics precursors fraction to aromatics; and(d) recovering aromatics from step (c) in an aromatics extraction unit;{'sub': 6', '11, 'wherein the Cto Chydrocarbon fraction provided in step (a) is subjected to step (b) without having been subjected to a reforming or a dehydrogenation process.'}29. The method according to claim 28 , wherein the Cto Chydrocarbon fraction is obtained by separation from a naphtha feedstock.30. The method according to claim 28 , wherein the Cto Chydrocarbon fraction is obtained by separation from a Cfraction of a naphtha feedstock.31. The method according to claim 28 , further comprising recovering from step (d) any unreacted aromatics precursors and returning them to step (c) for conversion to aromatics.32. The method according to claim 28 , wherein benzene claim 28 , toluene claim 28 , xylenes claim 28 , or a combination thereof claim 28 , are recovered claim 28 , and the aromatics precursors fraction comprises Cto Cnaphthenes and paraffins.33. The method according to claim 32 , wherein the aromatics precursors fraction is further fractionated by fractional distillation to selectively concentrate C claim 32 , C claim 32 , or Cnaphthenes claim 32 , or a combination thereof claim 32 , in the aromatics precursors fraction claim 32 , with C claim 32 , Cor Cnormal paraffins claim 32 ...

PROCESS FOR RECOVERY OF PROPYLENE FROM A PROPANE DEHYDROGENATION PROCESS

In a propane dehydrogenation (PDH) process, the purpose of the deethanizer and chilling train systems is to separate the cracked gas into a methane-rich tail gas product, a C2, and a C3 process stream. By the use of staged cooling, process-to-process inter-change against propane feed to the reactor and use of high efficiency heat exchangers and distributed distillation techniques, refrigeration power requirements are reduced and a simple and reliable design is provided by the process described herein. 1. A process for recovering propylene from a propane dehydrogenation (PDH) process comprising a PDH Reactor , the process comprising:feeding dried process gas from a Process Gas Dryer to a First Deethanizer Feed Chiller and chilling it against propane;sending the chilled dried process gas to a First Deethanizer Feed Drum;feeding liquid from First Deethanizer Feed Drum to a Deethanizer;sending the overhead vapors from the First Deethanizer Feed Drum to a Process Gas Compressor (PGC);cooling the discharge from the PGC against propane in a Second Deethanizer Feed Chiller, followed by propylene refrigerant in a Third Deethanizer Feed Chiller, and sending the discharge to a Second Deethanizer Feed Drum;feeding liquid from Second Deethanizer Feed Drum to the Deethanizer;chilling and partially condensing the vapor from the Second Deethanizer Feed Drum in a Cold Box;separating process effluent from the Cold Box into vapor and liquid phases in a First Cold Drum;vaporizing liquid from the First Cold Drum in the Cold Box and recycling it to a first stage of the PGC;reheating the vapor from First Cold Drum to become a methane-rich tail gas product;separating ethane and lighter components from C3 and heavier components in the Deethanizer;partially condensing overhead vapor against Propylene refrigerant in an overhead Deethanizer Condenser;separating process effluent from the overhead Deethanizer Condenser into vapor and liquid phases in a Deethanizer Reflux Drum and sending a vapor ...

REFRIGERATION RECOVERY FROM REACTOR FEED IN A PROPANE DEHYDROGENATION SYSTEM

A method to recover refrigeration credit from propane feed to a propane dehydrogenation reactor by fully condensing a Depropanizer overhead stream, letting the condensed stream down in pressure, and vaporizing the stream at lower pressure against process streams to recover refrigeration credit. 1. A process for recovering propylene from a propane dehydrogenation process , the process comprising:partially or fully condensing a depropanizer overhead stream against a relatively warm cooling medium at relatively high pressure;letting down the liquid overhead stream in pressure; andpartially or fully vaporizing the liquid overhead stream against at least one process stream to provide refrigeration.2. The process of where the letting down the liquid overhead stream in pressure is based on the back-pressure from a reactor.3. The process of where in vaporizing the liquid overhead stream against at least one process stream to provide refrigeration claim 1 , the refrigeration is in the range of about −10 to about 30° C.4. The process of where in vaporizing the liquid overhead stream against at least one process stream to provide refrigeration offsets the requirement for refrigeration provided by a propylene or propane refrigeration system in the same temperature range.5. The process of where the relatively warm cooling medium is at a temperature between about 20° C. and about 50° C. and where the relatively high pressure is between about 10 and about 20 barg.6. A system for recovering propylene from a propane dehydrogenation process claim 1 , the system comprising:a depropanizer column generating a depropanizer overhead stream;at least one condenser for partially or fully condensing the depropanizer overhead stream;at least one device for letting down the pressure of the depropanizer overhead stream as determined by back-pressure of a reactor; andat least one chiller for partially or fully vaporizing the depropanizer overhead stream.7. The system of where the device is a ...

Process for Nitrile Removal from Hydrocarbon Feeds

A process is described, such process comprising i) contacting a hydrocarbon feed with a heterogeneous catalyst under conditions suitable to hydrolyze nitriles present in the feed to form a nitrile hydrolysis product comprising ammonia, carboxylic acid and carboxylate salts or a mixture thereof; and ii) removing the nitrile hydrolysis product from the feed. In an embodiment, the hydrocarbon feed comprises olefins and is intended for use in an olefin oligomerization process.

Process for Recovering Olefins from Manufacturing Operations

A process for treating an effluent gas stream arising from a manufacturing operation that produces an olefin or an olefin derivative. The process involves compressing the feed gas stream, which comprises an olefin, a paraffin, and a third gas, to produce a compressed stream, then cooling and condensing the compressed stream. The condensation step produces a liquid condensate and an uncondensed gas stream. The liquid condensate is then passed through a membrane separation step. The membrane separation of the condensate results in an olefin-enriched stream, which may be recycled for use within the manufacturing operation, and an olefin-depleted stream, which may be purged from the process. 1. A process for treating an effluent gas stream arising from an operation that manufactures an olefin or an olefin derivative , said effluent gas stream comprising an olefin , a paraffin and a third gas , the process comprising the steps of:(a) passing said effluent gas stream to a compressor to produce a compressed stream;(b) partially condensing the compressed stream, including cooling and separating the compressed stream into an uncondensed gas stream depleted in olefin and paraffin and a condensed liquid condensate enriched in olefin and paraffin; and(c) separating the condensed liquid condensate using a first membrane to produce a first olefin-enriched permeate stream and a first olefin-depleted residue stream.2. The process of claim 1 , wherein the olefin is selected from the group consisting of ethylene claim 1 , propylene and butylene.3. The process of claim 1 , wherein the operation is selected from the group consisting of steam cracking claim 1 , fluid catalytic cracking claim 1 , propane dehydrogenation claim 1 , olefin metathesis claim 1 , a methanol-to-olefin process claim 1 , a methanol-to-propylene process claim 1 , and polyolefin manufacturing.4. The process of claim 1 , wherein the first membrane is an inorganic membrane.5. The process of claim 1 , wherein the ...

Process for Recovering Olefins from Manufacturing Operations

A process for treating an effluent gas stream arising from a manufacturing operation that produces an olefin or a non-polymeric olefin derivative. The process involves cooling and condensing the effluent gas stream, which comprises an olefin, a paraffin, and a third gas, to produce a liquid condensate and an uncondensed (residual) gas stream. Both streams are then passed through membrane separation steps. The membrane separation of the uncondensed gas stream results in an olefin-enriched stream and an olefin-depleted stream. The olefin-enriched stream is recirculated within the process prior to the condensation step. The membrane separation of the condensate also results in an olefin-enriched stream, which may be recycled for use within the manufacturing operation, and an olefin-depleted stream, which may be purged from the process. 1. A process for treating an effluent gas stream arising from an operation that manufactures an olefin , said effluent gas stream comprising an olefin , a paraffin and a third gas , the process comprising the steps of:(a) passing the effluent gas stream to a compressor to produce a compressed stream;(b) partially condensing the compressed stream, including cooling and separating the compressed stream into a condensed liquid condensate enriched in olefin and paraffin and an uncondensed gas stream depleted in olefin and paraffin;(c) separating the condensed liquid condensate from step (b) using a first membrane to produce a first olefin-enriched permeate stream and a first olefin-depleted residue stream;(d) separating the uncondensed gas stream from step (b) using a second membrane to produce a second olefin-enriched permeate stream and a second olefin-depleted residue stream; and(e) returning the second olefin-enriched permeate stream upstream of the compressor.2. The process of claim 1 , wherein the olefin is selected from the group consisting of ethylene claim 1 , propylene and butylene.3. The process of claim 1 , wherein the operation ...

Process for preparing 1,3-butadiene from n-butenes by oxidative dehydrogenation

The invention relates to a process for producing butadiene from n-butenes, comprising the steps of: A) providing an n-butenes-comprising input gas stream a 1, B) feeding the n-butenes-comprising input gas stream al, an oxygenous gas and an oxygenous cycle gas stream a 2 into at least one oxidative dehydrogenation zone and oxidatively dehydrogenating n-butenes to butadiene to obtain a product gas stream b comprising butadiene, unconverted n-butenes, steam, oxygen, low-boiling hydrocarbons, high-boiling secondary components, possibly carbon oxides and possibly inert gases, Ca) cooling down the product gas stream b and optionally at least partially removing high-boiling secondary components and steam to obtain a product gas stream b′, Cb) compressing and cooling the product gas stream b′ in at least one compression and cooling stage to obtain at least one aqueous condensate stream c 1 and one gas stream c 2 comprising butadiene, n-butenes, steam, oxygen, low-boiling hydrocarbons, possibly carbon oxides and possibly inert gases, Da) absorbing the C 4 hydrocarbons comprising butadiene and n-butenes into an aromatic hydrocarbon solvent absorption medium stream A 1 in an absorption column K 1 and removing noncondensable and low-boiling gas constituents comprising steam, oxygen, low-boiling hydrocarbons, possibly carbon oxides, aromatic hydrocarbon solvent and possibly inert gases as gas stream d 2 from the gas stream c 2 to obtain a C 4 hydrocarbons-laden absorption medium stream A 1 ′ and the gas stream d 2 and subsequently desorbing the C 4 hydrocarbons from the laden absorption medium stream A 1 ′ to obtain a C 4 product gas stream d 1, Db) at least partially recycling the gas stream d 2 into the oxidative dehydrogenation zone as cycle gas stream a 2, wherein said process comprises limiting the content of aromatic hydrocarbon solvent in the cycle gas stream a 2 to less than 1 vol % by contacting in a further column K 2 the gas stream d 2 exiting the removal stage Da) ...

ETHANE RECOVERY PROCESS AND ALKYLATION PROCESS WITH ETHANE RECOVERY

Processes and systems for the production of ethylbenzene using a dilute ethylene feed and subsequent recovery of ethane in the alkylation vent gas. 1. A process for the recovery of ethane , comprising:feeding a first stream comprising methane, ethane, and ethylene to a reboiled absorber column;contacting the first stream with an absorbent-reactant in the reboiled absorber column to absorb essentially all of the ethane and ethylene, producing a rich oil bottoms stream comprising the absorbent-reactant, ethylene, and ethane, and a vapor stream comprising methane;reacting the ethylene and the absorbent-reactant in a reaction zone, producing a reaction zone effluent comprising ethane and a reaction product;stripping the effluent in a stripper to produce a lean oil bottoms stream and an overhead vapor stream comprising ethane.2. The process of claim 1 , wherein the first stream and the vapor stream each further comprise one or more of nitrogen claim 1 , hydrogen claim 1 , carbon monoxide claim 1 , and carbon dioxide.3. The process of claim 1 , further comprising:operating the reboiled absorber column at a bottoms temperature in the range from about 150° C. to about 220° C.;operating the stripper at a bottoms temperature in the range from about 200° C. to about 280° C.4. The process of claim 1 , further comprising recycling at least a portion of the lean oil bottoms steam from the stripper to the reboiled absorber column as the absorbent-reactant.5. The process of claim 4 , further comprising introducing the absorbent-reactant proximate an upper end of the reboiled absorber column at a temperature in the range from about −20° C. to about 50° C.6. The process of claim 1 , wherein the reboiled absorber column comprises multiple reboilers configured to sequentially extract heat from the lean oil bottoms stream from the stripper.7. The process of claim 6 , wherein the multiple reboilers comprise one or more side reboilers.8. The process of claim 6 , further comprising ...

SYSTEM AND METHOD FOR REMOVING SULFUR FROM HYDROCARBON FLUIDS

An apparatus for removing sulfur from a hydrocarbon liquid may comprise a tank with a chamber, a barrier in the chamber forming at least a partial barrier to liquid flow with a gap defined therein, a gas distribution manifold for introducing the gas into the liquid, and a gas conversion structure defining an interior in fluid communication with the chamber. The gas conversion structure may include a conversion tube defining a tube interior in fluid communication with the chamber, an air injection device configured to inject air into the tube interior and draw gas from the chamber, a water injection device configured to inject water into the tube interior to create a mist of water in the tube interior to contact the gas from the chamber of the tank, and a fluid drain configured to drain fluid from the tube interior. 1. An apparatus for removing sulfur from a hydrocarbon liquid , comprising:a tank having an interior defining a chamber configured to hold a liquid, the tank including an upper wall and a lower wall;a barrier in the chamber forming at least a partial barrier to liquid flow in the chamber, at least a portion of the barrier extending substantially vertically in the chamber, a gap being defined between the lower wall of the tank and a lower portion of the barrier;a gas distribution manifold for introducing the gas into the liquid, the gas distribution manifold being positioned in the chamber for being submerged in liquid positioned in the chamber, at least a portion of the gas distribution manifold being perforated with holes to permit gas in an interior of the manifold to exit the manifold; a conversion tube defining a tube interior and having an inlet end and an outlet end, the tube interior being in fluid communication with the chamber of the tank;', 'an air injection device configured to inject air into the tube interior of the conversion tube and draw gas from the chamber of the tank;', 'a water injection device configured to inject water into the tube ...

OLIGOMER PREPARATION METHOD AND OLIGOMER PREPARATION APPARATUS

Provided are a method for preparing an oligomer and an apparatus for preparing an oligomer. The method for preparing an oligomer includes performing an oligomerization reaction by feeding a feed stream containing a monomer to a reactor; feeding a first discharge stream of the reactor to a first separation device, and feeding a second discharge stream of the reactor to a second separation device; feeding a lower discharge stream of the second separation device to a third separation device; feeding an upper discharge stream containing the monomer of the third separation device to a monomer dissolution device and dissolving the upper discharge stream in a solvent fed to the monomer dissolution device; and feeding a discharge stream of the monomer dissolution device to the reactor. 1. A method for preparing an oligomer , the method comprising:performing an oligomerization reaction by feeding a feed stream containing a monomer to a reactor;feeding a first discharge stream of the reactor to a first separation device and feeding a second discharge stream of the reactor to a second separation device;feeding a lower discharge stream of the second separation device to a third separation device;feeding an upper discharge stream containing the monomer of the third separation device to a monomer dissolution device and dissolving the upper discharge stream in a solvent fed to the monomer dissolution device; andfeeding a discharge stream of the monomer dissolution device to the reactor.2. The method of claim 1 , wherein the second separation device is operated at a higher pressure than the third separation device.3. The method of claim 2 , wherein a pressure in the second separation device is 10 bar to 50 bar claim 2 , and a pressure in the third separation device is 0.5 bar to 15 bar.4. The method of claim 1 , wherein the lower discharge stream of the second separation device contains the monomer.5. The method of claim 1 , wherein a pressure of the upper discharge stream of the ...

OLIGOMER PREPARATION METHOD AND OLIGOMER PREPARATION DEVICE

Provided are a method for preparing an oligomer and an apparatus for preparing the same. The method for preparing an oligomer including: supplying a feed stream including a monomer to a reactor to perform an oligomerization reaction; supplying a first discharge stream from the reactor to a first separation device and supplying a second discharge stream from the reactor to a second separation device; recovering the monomer as an upper discharge stream from the second separation device and supplying a lower discharge stream from the second separation device to a third separation device; and supplying an upper discharge stream from the third separation device to the second separation device. 1. A method for preparing an oligomer , the method comprising:supplying a feed stream including a monomer to a reactor to perform an oligomerization reaction;supplying a first discharge stream from the reactor to a first separation device and supplying a second discharge stream from the reactor to a second separation device;recovering the monomer as an upper discharge stream from the second separation device and supplying a lower discharge stream from the second separation device to a third separation device; andsupplying an upper discharge stream from the third separation device to the second separation device.2. The method for preparing an oligomer of claim 1 , wherein the upper discharge stream from the third separation device is a liquid stream including a C4 compound.3. The method for preparing an oligomer of claim 2 , wherein a part of the upper discharge stream from the third separation device is not supplied to the second separation device but recovered.4. The method for preparing an oligomer of claim 3 , wherein a content of the C4 compound included in the part of the upper discharge stream from the third separation device is 70 wt % or more.5. The method for preparing an oligomer of claim 3 , wherein a content of the monomer included in the part of the upper discharge ...

Methods and systems for separating c4 crude streams

The present invention provides, among other things, new processes for separating and purifying C4 fractions from a crude C4 stream. Compared to prior methods, the processes of the present invention simplify the C4 separation processes, afford more possible configurations for separation and purification, and are more cost effective. The processes and systems provided herein can be used as part of a cost-effective and efficient method for synthesizing methyl tertiary-butyl ether.

Low Emissions Oxidative Dehydrogenation Process for Producing Butadiene

Butadiene is formed by dehydrogenation of butenes which are mixed with steam and oxygen then converted to butadiene by oxidative dehydrogenation over a ferritic oxide catalyst, wherein the sensible heat in the oxidative dehydrogenation reaction product is utilized along with heat produced by thermal oxidation of low value volatile products formed to reduce energy requirements and CO 2 emissions. Sensible heat is utilized at high temperature for purposes of superheating feed and at somewhat lower temperatures for purposes of vaporizing feed at sequential locations in the process.