ОТВОД АЗОТА ИЗ КОНДЕНСИРОВАННОГО ПРИРОДНОГО ГАЗА

Изобретение может быть использовано в технологии обработки природного газа. Способ отвода азота включает введение конденсированного природного газа в первом положении дистилляционной колонны, отбор обогащенного азотом потока пара из головной части дистилляционной колонны и отбор очищенного потока сжиженного природного газа из нижней части колонны. Поток холодного орошения вводят в дистилляционную колонну во втором положении, находящемся выше первого положения. Способ также включает либо охлаждение очищенного потока сжиженного природного газа, или охлаждение потока конденсированного природного газа, либо охлаждение как очищенного потока сжиженного природного газа, так и потока конденсированного природного газа. Технический результат: удаление азота с минимальными потерями метана и обеспечение принудительного охлаждения сжиженного природного газа. 5 н. и 28 з.п. ф-лы, 8 ил.

СПОСОБ УДАЛЕНИЯ ЛЕТУЧИХ КОМПОНЕНТОВ ИЗ ПРИРОДНОГО ГАЗА

Раскрыт способ удаления, по меньшей мере, одного компонента, обладающего высокой летучестью, такого как азот, из природного газа под давлением для получения сжиженного природного газа под давлением, который имеет низкое содержание азота и температуру свыше приблизительно -112oС (-170oF). Исходный природный газ под давлением, содержащий азот, расширяют и подают во фракционирующую ректификационную колонну. Во фракционирующей ректификационной колонне образуется поток первого пара, который имеет повышенное содержание азота, и поток первой жидкости. Поток пара охлаждают для образования паровой фазы и жидкой фазы. После этого паровую и жидкую фазы подвергают разделению фаз для образования потока второго пара и потока второй жидкости. Поток второй жидкости возвращают во фракционирующую ректификационную колонну в качестве флегмы. Поток второго пара предпочтительно используют для охлаждения поступающего потока исходного сырья. Поток первой жидкости отводят из установки для фракционирования в качестве ...

СПОСОБ УДАЛЕНИЯ АЗОТА ИЗ ОБОГАЩЕННОЙ УГЛЕВОДОРОДОМ ФРАКЦИИ

Изобретение относится к способу получения сжиженного углеводородного газа с низким содержанием азота. Способ получения сжиженной обогащенной углеводородом фракции (фракции продукта) с содержанием азота ≤ 1 мол.% осуществляют следующим образом. Обогащенную углеводородом фракцию сжижают и переохлаждают с помощью холодильного контура, а затем подвергают ректификационному удалению азота. Способ отличается тем, что: а) сжиженную и переохлажденную обогащенную углеводородом фракцию (2) расширяют (V1) и подают в колонну (Т1) отгонки азота, б) фракцию (4) продукта отводят из ее нижней части, в) обогащенную азотом фракцию (5) отводят из ее верхней части, сжимают (С1), сжижают и переохлаждают (Е1-Е3) с помощью холодильного контура (К), расширяют (V2) и подают в колонну (Т2) азота высокого давления, г) часть потока обогащенной азотом фракции из колонны (Т2) азота высокого давления, который был охлажден с помощью холодильного контура (K), подают в качестве ребойлерного потока (9), д) обедненную азотом ...

Способ и устройство для очистки гелия

Изобретение относится к способу очистки гелия. Поток (1), содержащий по меньшей мере 10% гелия, по меньшей мере 10% азота в дополнение к водороду и метану, разделяют, чтобы образовать поток (3), обогащенный гелием, содержащий водород, первый поток (9), обогащенный азотом и метаном, и второй поток (11), обогащенный азотом и метаном. Поток, обогащенный гелием, обрабатывают, чтобы получить продукт (7), обогащенный гелием, и остаточный газ (15), содержащий воду. Остаточный газ обрабатывают посредством адсорбции (короткоцикловой адсорбции с колебаниями температуры (TSA)), чтобы удалить воду, и регенерационный газ (13) от адсорбции направляют в узел для сжигания (O). Техническим результатом является уменьшение количества метана, выпускемого в атмосферу. 2 н. и 7 з.п. ф-лы, 1 ил.

УСТАНОВКА ПОДГОТОВКИ УГЛЕВОДОРОДНОГО ГАЗА К ТРАНСПОРТУ

Изобретение может быть использовано в газовой, нефтехимической и других отраслях промышленности. Установка содержит последовательно соединенные по газу приемный сепаратор 1, скруббер 3, первую ступень компримирования 4, аппарат воздушного охлаждения 5, промежуточный сепаратор 6, блок глубокой осушки газа 7, вторую ступень компримирования 8, второй аппарат воздушного охлаждения 9, второй промежуточный сепаратор 10. Выход газа второго промежуточного сепаратора 10 соединен с транспортным трубопроводом газа и конденсата и с входом блока подготовки топливного газа 11 газотурбинного привода. Один выход из блока подготовки 11 соединен с входом подачи топливного газа в газотурбинные двигатели, а второй - с входом подачи регенерационного газа в блок глубокой осушки газа 7. Трубопровод выхода регенерационного газа из блока осушки газа 7 соединен с трубопроводом нагнетания первой ступени компримирования 4 перед аппаратом воздушного охлаждения 5. Изобретение позволяет повысить степень очистки газа ...

СПОСОБ КРИОГЕННОГО ФРАКЦИОНИРОВАНИЯ С САМООХЛАЖДЕНИЕМ И ОЧИСТКИ ГАЗА И ТЕПЛООБМЕННИК ДЛЯ ОСУЩЕСТВЛЕНИЯ ЭТОГО СПОСОБА

Способ предназначен для криогенного фракционирования (при самоохлаждении) и очистки и совместно с теплообменником для его осуществления относится к холодильной технике. Газовый поток обрабатывают в теплообменнике, образующем единый узел: он частично конденсируется при охлаждении в контурах С1 и С5, несконденсировавшуюся газовую фазу нагревают в контуре С2. Необходимый холод получают от конденсатов, которые после переохлаждения в контуре С3 и дросселирования через клапан V1 испаряются в контуре С4. Процесс может осуществляться в теплообменнике, состоящем из множества каналов в каждом контуре. Способ позволяет эффективно очищать газовый поток из нескольких конденсируемых компонентов при охлаждении. 2 с. и 8 з.п. ф-лы, 2 ил., 8 табл.

СПОСОБ АВТОМАТИЧЕСКОГО ПОДДЕРЖАНИЯ ПЛОТНОСТИ НЕСТАБИЛЬНОГО ГАЗОВОГО КОНДЕНСАТА НА ВЫХОДЕ УСТАНОВОК НИЗКОТЕМПЕРАТУРНОЙ СЕПАРАЦИИ ГАЗА СЕВЕРНЫХ НЕФТЕГАЗОКОНДЕНСАТНЫХ МЕСТОРОЖДЕНИЙ РФ

Изобретение относится к области добычи и подготовки газа и газового конденсата к дальнему транспорту на Крайнем Севере, в частности, к автоматическому поддержанию на установке низкотемпературной сепарации газа (далее – установка) плотности нестабильного газового конденсата (НГК), подаваемого в магистральный конденсатопровод (МКП). В способе осуществляют очистку поступающей газоконденсатной смеси от механических примесей, разделение ее на осушенный газ и смесь НГК с водным раствором ингибитора (ВРИ), и осушенный газ направляют в магистральный газопровод (МГП), а смесь в дегазатор-разделитель (ДР), из которого ВРИ отводят на регенерацию ингибитора, НГК насосом подают в МКП, а газ выветривания через клапан регулятор (КР), регулирующий давление в ДР, направляют в компрессор газов выветривания для закачки в МГП, а ведущая эти процессы автоматизированная система управления технологическими процессами (АСУ ТП) установки контролирует датчиком плотности плотность ρфакт НГК, подаваемого в МКП, и ...

СПОСОБ БЕЗОТХОДНОЙ ПОДГОТОВКИ СКВАЖИННОЙ ПРОДУКЦИИ (ВАРИАНТЫ)

Группа изобретений относится к способам подготовки газа путем низкотемпературной конденсации и может быть использована в газовой промышленности для промысловой подготовки скважинной продукции газоконденсатных месторождений. Согласно первому варианту предложенного способа сырой газ сепарируют на первой ступени с получением газа, водного и углеводородного конденсатов, последний редуцируют и стабилизируют совместно с конденсатом второй ступени с получением первого газа стабилизации и остатка. Газ первой ступени редуцируют и в смеси с первым газом стабилизации сепарируют на второй ступени путем охлаждения в условиях дефлегмации с получением конденсата и газа, который редуцируют, смешивают со вторым газом стабилизации и сепарируют на третьей ступени с получением конденсата и газа, который нагревают и выводят в качестве товарного. Остаток стабилизации редуцируют и стабилизируют совместно с конденсатом третьей ступени с получением товарного конденсата и второго газа стабилизации. Согласно второму ...

СПОСОБ ОПТИМИЗАЦИИ ПРОЦЕССА ОТМЫВКИ ИНГИБИТОРА ИЗ НЕСТАБИЛЬНОГО ГАЗОВОГО КОНДЕНСАТА НА УСТАНОВКАХ НИЗКОТЕМПЕРАТУРНОЙ СЕПАРАЦИИ ГАЗА НЕФТЕГАЗОКОНДЕНСАТНЫХ МЕСТОРОЖДЕНИЙ СЕВЕРА РФ

Изобретение относится к области подготовки природного газа и газового конденсата к дальнему транспорту, в частности к автоматическому управлению отмывкой ингибитора - метанола из нестабильного газового конденсата (НГК). Способ оптимизации процесса отмывки ингибитора включает автоматическое поддержание технологических параметров процесса подготовки газа и газового конденсата к дальнему транспорту, отделение водометанольного раствора - BMP и НТК с отмывкой ингибитора - метанола из конденсата, отвод его через клапан-регулятор и последующую регенерацию метанола из полученного BMP с возвратом его в технологический процесс. При запуске установки в эксплуатацию АСУ ТП осуществляет поиск уставки минимально возможного расхода BMP с низкой концентрацией метанола, подаваемого на вход инжекции инжектора и гарантирующего максимальную отмывку метанола из НТК с минимальными затратами энергии на его регенерацию. Технический результат изобретения: повышение точности нахождения значения уставки минимально ...

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 ...

УСТАНОВКА ФРАКЦИОНИРОВАНИЯ УГЛЕВОДОРОДНОГО ГАЗА

Установка фракционирования углеводородного газа, включающая первый, второй и третий блоки аминовой очистки от кислых компонентов с линиями подачи в них сырого газа, блок адсорбционной очистки от меркаптанов и осушки газа с линией отвода очищенного газа на блок низкотемпературной конденсации и ректификации и линией отвода газа регенерации на третий блок аминовой очистки от кислых компонентов, соединенный с блоком низкотемпературной масляной абсорбции, имеющий на выходе линии отвода товарного газа, пропан-бутановой фракции и подачи топливного газа потребителям, отличающаяся тем, что линия отвода товарного газа из блока низкотемпературной масляной абсорбции соединена с линией подачи топливного газа потребителям.

УСТАНОВКА ПО ПОДГОТОВКЕ ПОПУТНОГО НЕФТЯНОГО ГАЗА

Установка по подготовке попутного нефтяного газа, содержащая два параллельно установленных теплообменника, входы каналов для охлаждения которых соединены с компрессорной станцией (КС), а выходы каналов для охлаждения - с первым сепаратором, выход которого для нестабильного конденсата через каналы нагрева второго теплообменника соединен со вторым сепаратором, один выход которого соединен с входом в КС, а второй - с хранилищем нестабильного конденсата, газовый выход первого сепаратора соединен с входом сверхзвукового сепаратора, один выход которого через каналы нагрева первого теплообменника соединен с потребителем, а второй выход соединен с третьим сепаратором, газовый выход из которого соединен с трубопроводом подачи газа в каналы нагрева первого теплообменника, а другой выход третьего сепаратора соединен с трубопроводом подачи конденсата в каналы нагрева второго теплообменника, при этом сверхзвуковой сепаратор содержит сопло с форкамерой, с размещенным в ней средством для закрутки газового ...

УСТРОЙСТВО ДЛЯ ПОЛУЧЕНИЯ СЖИЖЕННЫХ ГАЗОВ

Полезная модель относится к устройствам получения сжиженных газов, а также к разделению на компоненты смесей газов, таких как природный, и может быть использована в газо-нефтедобывающей и перерабатывающей промышленности в металлургии, химии и других областях техники. Техническим результатом является повышение эффективности получения сжиженных газов. Устройство для сжижения газа, выполненное с возможностью его адиабатического охлаждения в сверхзвуковом сопле и отбор жидкой фазы, содержащее форкамеру, на вход которой подается поступающий под давлением газ, сверхзвуковое сопло, с дополнительным полым конусом, образующим с соплом кольцевую щель, отличается тем, что содержит пластины, формирующие постоянное электрическое поле, к которым подведен постоянный ток, причем пластины расположены по отношению к потоку таким образом, что на место конденсации жидкой фазы воздействует однородное электрическое поле.

СПОСОБ ОХЛАЖДЕНИЯ УГЛЕВОДОРОДНОГО ГАЗА ПРИ ПОДГОТОВКЕ К ТРАНСПОРТУ

В способе охлаждения углеводородного газа охлаждение проводят в аппаратах воздушного охлаждения с несколькими рядами теплообменных трубок с входным и выходным коллекторами. В процессе эксплуатации входной коллектор заполняют ингибитором гидратообразования до уровня отверстий нижнего ряда теплообменных трубок. В качестве ингибитора может использоваться метанол. Газ подают выше уровня ингибитора. В выходном коллекторе газ и ингибитор сепарируют. Использование изобретения позволит обеспечить безгидратное охлаждение углеводородного газа при максимальном снижении его температуры ниже температуры гидратообразования в процессе изменений температуры атмосферного воздуха в зимних условиях. 1 з.п. ф-лы, 1 табл., 1 ил.

УСТРОЙСТВО ДЛЯ КОМПРИМИРОВАНИЯ И ОСУШКИ ГАЗА

Изобретение относится к области теплотехники. Устройство для компримирования и осушки газа содержит многоступенчатый компрессор со ступенью низкого давления, ступенью высокого давления и нагнетательным патрубком и адсорбционный осушитель с зоной осушения и зоной регенерации, причем между ступенью низкого давления и ступенью высокого давления помещен промежуточный холодильник, и при этом устройство дополнительно снабжено теплообменником, имеющим главную камеру с входной частью и выходной частью для первой первичной текучей среды, а концы трубок теплообменника соединены с отдельной входной камерой и выходной камерой для каждого трубного пучка; и при этом первый трубный пучок образует охлаждающий контур промежуточного холодильника, служащий для разогрева газа из ступени высокого давления для регенерации адсорбционного осушителя. Технический результат - упрощение конструкции и монтажа, снижение себестоимости устройства. 13 з.п. ф-лы, 4 ил.

СПОСОБ НИЗКОТЕМПЕРАТУРНОЙ ОБРАБОТКИ ПРИРОДНОГО ГАЗА

Область использования: изобретение относится к низкотемпературной обработке природного газа преимущественно в условиях газодобывающего или газоперерабатывающего предприятия. Сущность изобретения: газовый поток подвергают предварительному охлаждению, сепарации на газовую и жидкую фазы, осуществляют отвод газа и жидкости после сепарации, при этом поток газа после сепарации подают в расширение с понижением температуры и получением энергии и направляют на нагревание в рекуперативном теплообмене с исходным газом, после нагревания поток газа делят на два потока, один из которых отводят на компримирование с подводом энергии, полученной при расширении, часть газа после компримирования отводят и подают на смешение с потоком газа, поступающим после сепарации на расширение, а предварительное охлаждение исходного газа ведут в рекуперативном теплообмене с газом, поступающим после расширения. 3 з.п. ф-лы, 1 табл. 5 ил.

СПОСОБ ПОЛУЧЕНИЯ ГАЗООБРАЗНЫХ ПРОДУКТОВ РАЗДЕЛЕНИЯ ВОЗДУХА ПОД ДАВЛЕНИЕМ И УСТРОЙСТВО ДЛЯ ПОЛУЧЕНИЯ ГАЗООБРАЗНЫХ ПРОДУКТОВ РАЗДЕЛЕНИЯ ВОЗДУХА

Использование: в криогенной технике, а именно в установках разделения воздуха и может применяться в газовой, химической и других отраслях промышленности. Сущность изобретения: необходимое давление выдачи газообразного технологического продукта получают непосредственно с помощью регенератора блока разделения воздуха, для чего попеременно из двух накопительных емкостей производят самотеком подачу жидкого продукта в змеевик регенератора под избыточным давлением 1,0 1,2 атм. обеспечиваемым с помощью регулирующих клапанов, а газификацию технологического продукта осуществляют до давления 3 32 атм. Устройство дополнительно содержит две накопительные емкости, установленные в блоке выше отметки регенератора, средство для создания избыточного давления выполнено в виде регенератора блока разделения воздуха, а средство подачи продукта в регенератор выполнено в виде упомянутых емкостей и регулирующих клапанов, установленных на трубопроводе подачи жидкого продукта из емкостей в змеевики регенератора.

Система подготовки углеводородного газа для подачи в деметанизатор (варианты)

Изобретение относится к вспомогательному оборудованию ректификационных колонн и может быть использовано в нефтегазовой промышленности. Предложено два варианта системы подготовки углеводородного газа, которая в обоих вариантах включает сепараторы 1-3, дефлегматор 4 и редуцирующие устройства 5-7. Во втором варианте система дополнительно включает четвертый сепаратор 8 и редуцирующее устройство 9. При работе первого варианта системы углеводородный газ подают в сепаратор 1, где разделяют на газ и остаток, который редуцируют в устройстве 5 и разделяют в сепараторе 2 на газ, выводимый из системы, и остаток, который подают в верхнюю часть деметанизатора 10 по первой снизу линии. Газ из сепаратора 1 направляют в дефлегматор 4, в котором в условиях дефлегмации разделяют на газ и остаток, который редуцируют в устройстве 6 и подают в верхнюю часть деметанизатора 10 по второй снизу линии. Газ из дефлегматора 4 направляют в сепаратор 3, где разделяют на газ, выводимый из системы, и остаток, который подают ...

СПОСОБ ПОДГОТОВКИ ГАЗА К ТРАНСПОРТУ

Использование: в промысловой обработке газа для его транспорта по трубопроводу, уложенному в многолетнемерзлых грунтах. Сущность изобретения: газ последовательно компримируют, подвергают низкотемпературной сепарации при температуре ниже 248 К, рекуперируют холод отсепарированного потока. Нагревая газ до 271 - 263 К, подают в трубопровод. Применение изобретения позволяет предотвратить выпадение жидкости в трубопроводах, уложенных в многолетнемерзлых грунтах.

СПОСОБ ДЕМЕТАНИЗАЦИИ ГАЗОВЫХ СМЕСЕЙ

Использование: разделение компонентов газовых смесей. Деметанизация газовых смесей осуществляется путем подачи отсепарированных потоков жидкости на ректификацию с получением деметанизированной продуктовой жидкой фазы и газообразной метановой флакции, охлаждением последней посредством внешнего холодильного цикла и сепарацией на газовую и жидкую фазу. Перед сепарацией метановую фракцию дополнительно охлаждают. После сепарации поток жидкой метановой фракции делят на два потока, первый из которых дросселируют и подают обратным потоком на регенеративный теплообмен с исходной газовой смесью. Второй поток дросселируют и направляют на испарение с подводом тепла от охлаждаемой метановой фракции. После испарения второй поток подают на смешение с первым потоком. Затем метановую фракцию компримируют и подают на рециркуляцию в исходную газовую смесь. 1 з. п. ф-лы, 2 ил.

УСТАНОВКА ДЛЯ ПОДГОТОВКИ ГАЗА С УДАЛЕННЫМ ТЕРМИНАЛОМ УПРАВЛЕНИЯ И ИСПОЛЬЗОВАНИЕМ ПРОГРАММНОГО КОМПЛЕКСА АВТОМАТИЧЕСКОГО УПРАВЛЕНИЯ ТЕХНОЛОГИЧЕСКИМ ПРОЦЕССОМ

... (57) Изобретение относится к газовой и нефтяной отраслямпромышленности и может использоваться при подготовке газа нефтяных и газоконденсатных месторождений для снижения капитальных и эксплуатационных затрат. Задачей изобретения является создание установки для первичной подготовки газа от кустов газовых скважин, работающей без обслуживающего персонала за счет использования программного комплекса автоматического регулирования подготовкой газа. Установка для подготовки газа снабжена системой автоматического управления (САУ), связанной с запорно-регулирующей арматурой, которая представляет собой первый клапан-регулятор на линии подачи газа, второй клапан-регулятор, установленный на линии, соединяющей первичный и низкотемпературный сепараторы, третий и четвертый клапаны-регуляторы, установленные на линиях, соединяющих выходы соответственно первичного и низкотемпературного сепараторов для газожидкостной смеси с дегазатором, пятый клапан-регулятор, установленный на линии сброса жидкости из дегазатора ...

СПОСОБ ПОВЫШЕНИЯ ДАВЛЕНИЯ ПОТОКА ГАЗА И ЖИДКОСТИ И УСТРОЙСТВО ДЛЯ ЕГО ОСУЩЕСТВЛЕНИЯ

Может быть использовано в нефтяной, химической, нефтехимической и газовой промышленности для повышения давления потока газа и жидкости. Прямой поток газа и жидкости охлаждают, ожижают во входном конденсаторе с образованием прямого потока жидкости, который подают в столбовую линию, поток жидкости из столбовой линии подают в виде потока жидкости низкого напора в ступень повышения давления, преобразуют в двухфазный поток, после чего его поднимают через тяговую линию в пароотделитель высокого потенциала, в котором осуществляют сепарацию газовой и жидкостной фаз, при этом газовую фазу выводят из ступени повышения давления и подают на смешение с прямым потоком газа и жидкости, а жидкостную фазу пропускают через напорную линию ступени повышения давления, затем подают в линию высокого напора ступени повышения давления, после чего поток в виде продукционного потока жидкости делят на две части в продукционной линии, одну из которых подают в линию продукционного потока жидкости высокого напора, а ...

СПОСОБ ПОЛУЧЕНИЯ ЧИСТОГО КСЕНОНА ИЗ ПЕРВИЧНОГО КРИПТОНОВОГО КОНЦЕНТРАТА

Способ получения чистого ксенона из первичного криптонового концентрата, включающий получение первичного криптонового концентрата, отличающийся тем, что первичный криптоновый концентрат при температуре выше температуры равновесной парциальному давлению в ней ксенона, вводят в вымораживатель, где его охлаждают до температуры ниже равновесной парциальному давлению ксенона в вымораживателе, при этом общее давление всех остальных компонентов первичного концентрата в вымораживателе поддерживают ниже их равновесных давлений при минимальном значении температуры в вымораживателе.

ТЕХНОЛОГИЧЕСКАЯ УСТАНОВКА

... 1. Технологическая установка (1) для переработки горючих сред, например, нефтеперерабатывающая установка, в которой из нефти извлекаются газообразные углеводороды, а бросовые или остаточные газы от неконтролируемого роста давления газа в технологическом процессе выпускаются через технологические или предохранительные клапаны в установке и отводятся в коллекторный трубопровод (9), отличающаяся тем, что бросовые или остаточные газы отводятся по коллекторному трубопроводу (9) в один или несколько накопителей (2) низкого давления, а коллекторный трубопровод или возвратный трубопровод (11, 3) проходят от накопителя(ей) (2) к технологической или другой перерабатывающей установке для обработки возвращаемой или накапливаемой среды. 2. Технологическая установка по п. 1, отличающаяся тем, что накопитель(ли) низкого давления включает(ют) накопитель (2) для хранения сырой нефти или неочищенных нефтепродуктов технологической установки выше по ходу потока от технологической установки. 3. Технологическая ...

СПОСОБ ВЫДЕЛЕНИЯ ГОРЮЧЕЙ СОСТАВЛЯЮЩЕЙ ИЗ ВОЗДУХА В ВИХРЕВОЙ УСТАНОВКЕ И ВИХРЕВАЯ УСТАНОВКА ДЛЯ ЕГО РЕАЛИЗАЦИИ

Изобретение относится к способам и установкам разделения сред с неоднородным полем плотности и с разной молекулярной массой компонентов, работа которых осуществляется в соответствии с законом свободно вращающегося вихревого потока с неоднородным полем плотностей и с разной молекулярной массой компонентов, открытым автором в 1994 году, и может быть использовано как для выделения горючей составляющей из воздуха, так и разделения других его компонентов, а также оно может быть использовано, как в целом, так и отдельные его элементы, для разделения различных сред в вихревых потоках в различных отраслях производства, в частности химической, тепловой и атомной энергетике, нефтегазодобывающей и перерабатывающей промышленности и многих других производствах. В способе выделения горючей составляющей из воздуха в вихревой установке, включающей закрутку потока, его разделение и отвод сред через центральный и периферийный каналы, а вихревая установка для его реализации содержит по меньшей мере вихревое ...

СПОСОБ ОБРАЗОВАНИЯ И ВЫДЕЛЕНИЯ КОНДЕНСАТА ИЗ ГАЗОВОЙ СМЕСИ И УСТРОЙСТВО ДЛЯ ЕГО ОСУЩЕСТВЛЕНИЯ

... 1. Способ образования конденсата из низкокипящих компонент газовой смеси, включающий охлаждение газовой смеси до температуры насыщения ее низкокипящих компонент при разгоне газовой смеси в конфузорном канале, отличающийся тем, что, с целью более эффективного охлаждения газовой смеси, проведения гетерогенной конденсации при относительно небольших перепадах давления, дозвуковых скоростях потока и с малыми энергетическими потерями газовую смесь разгоняют в конфузоре совместно с каплями жидкости конденсируемой компоненты, которую предварительно подают на вход в конфузор. 2. Устройство для образования и выделения конденсата низкокипящих компонент газовой смеси, включающее сепаратор с конфузорно-диффузорной проточной частью и подвижным в осевом направлении центральным телом, с щелевыми отверстиями для отбора выпадающей на стенки сепаратора и центральное тело жидкости, включающее также накопительную емкость для слива конденсата и подводящую к ней магистраль, отличающееся тем, что, с целью более ...

СПОСОБ ОБОГАЩЕНИЯ ГЕЛИЕМ ГЕЛИЙСОДЕРЖАЩЕГО ПРИРОДНОГО ГАЗА

Изобретение относится к нефтегазовой и химической промышленности и касается способа обогащения гелием гелийсодержащего природного газа. Способ содержит этапы, на которых обеспечивают канал, выполненный в виде, по меньшей мере, одной винтообразной однообъёмной спирали, состоящей из, по меньшей мере, одного витка, вводят в канал в качестве основного потока гелийсодержащий природный газ, обеспечивают ламинарность основного потока, обеспечивают перераспределение гелия, содержащегося в основном потоке, посредством центробежной силы с насыщением гелием той части основного потока, которая расположена ближе к центру вращения потока, полностью отделяют часть основного потока, насыщенного гелием, от остального потока, содержащего тяжелые компоненты основного потока, с помощью перегородки такой формы и установленной в канале таким образом, что обеспечивается минимальное сопротивление движению потоков, обеспечивают ламинарность насыщенного гелием потока, обеспечивают перераспределение гелия, содержащегося ...

СПОСОБ УПРАВЛЕНИЯ ПРОЦЕССОМ НЕПРЕРЫВНОЙ РЕГЕНЕРАЦИИ ВОДОРОДА ИЗ ПАРОГАЗОВОЙ СМЕСИ, ОТХОДЯЩЕЙ ОТ ПЕЧЕЙ ВОДОРОДНОГО ВОССТАНОВЛЕНИЯ В ПРОИЗВОДСТВЕ ПОЛУПРОВОДНИКОВОГО КРЕМНИЯ

Способ управления процессом непрерывной регенерации водорода из парогазовой смеси, отходящей от печей водородного восстановления в производстве полупроводникового кремния, заключающийся в ступенчатом низкотемпературном охлаждении парогазовой смеси и регулировании расхода исходного хладагента, отличающийся тем, что, с целью увеличения выхода регенерированного водорода, увеличения извлечения трихлорсилана в основной конденсируемый продукт и уменьшения энергозатрат, испаренный азот, выходящий из теплообменника-вымораживателя и направляемый последовательно по теплообменникам процесса регенерации навстречу парогазовой смеси, перед вводом его в очередной теплообменник распределяют в зависимости от температуры конденсации компонентов регенерируемой парогазовой смеси на два потока, один из которых пропускают через теплообменник, а другой направляют по обводному каналу, по отношению их расходов корректируют расход исходного хладагента, например жидкого азота, подаваемого на конденсацию хлорсиланов ...

СПОСОБ НИЗКОТЕМПЕРАТУРНОЙ ОБРАБОТКИ ПРИРОДНОГО ГАЗА

Изобретение относится к низкотемпературной обработке природного газа преимущественно при его заводской и промысловой обработке. Цель изобретения - повышение степени сжатия компримируемого газа. Это достигается тем, что газовой поток предварительно охлаждают в рекуперативном теплообмене, сепарируют от сконденсировавшейся жидкости, расширяют с понижением температуры в режиме генерации волн сжатия, нагревают при рекуперации холода и частично отводят за пределы процесса, а энергию волн сжатия подводят к потоку, оставшемуся в процессе и подлежащему компримированию и составляющему не менее 10% от массы расширенного потока.

СПОСОБ ДЕМЕТАНИЗАЦИИ ГАЗОВЫХ СМЕСЕЙ

Способ деметанизации газовых смесей может найти применение в нефтехимической, нефтеперерабатывающей и газовой промышленности, преимущественно в производстве этилена. Цель изобретения - снижение потерь целевого продукта (этилена) и энергозатрат при деметанизации газовых смесей. Способ деметанизации газовых смесей включает последовательное охлаждение сжатой исходной газовой смеси посредством внешнего и внутреннего холодильных циклов с образованием промежуточных частичных конденсатов компонентов смеси, ректификацию этих конденсатов с получением деметанизированной жидкой фазы и газообразной метановой фракции, охлаждение последней внешним холодильным циклом с образованием частичного конденсата, сепарацию и использование этого конденсата в качестве хладоагента упомянутого внутреннего холодильного цикла путем дросселирования конденсата, его испарения охлаждаемой смесью и рециркуляции в исходную газовую смесь, при этом после охлаждения внешним холодильным циклом перед сепарацией метановую фракцию ...

СПОСОБ ЭФФЕКТИВНОЙ РАБОТЫ КОМБИНИРОВАННОЙ ВОЗДУХОРАЗДЕЛЯЮЩЕЙ УСТАНОВКИ ГЛУБОКОГО ОХЛАЖДЕНИЯ

Изобретение относится к способам разделения воздуха в воздухоразделяющих установках глубокого охлаждения для получения технологического, технического, медицинского кислорода, чистого азота и редких газов и может быть использовано на заводах для производства товарного газообразного и жидкого кислорода и других газов, на кислородных станциях металлургических, химических и машиностроительных предприятий. В способе повышения эффективности работы воздухоразделяющей установки глубокого охлаждения в комбинированной установке, включающем, по крайней мере очистку воздуха от пыли и механических примесей, сжатие воздуха в компрессорах, очистку сжатого воздуха от углекислого газа, его осушку и очистку от углеродов, сжижение и ректификацию воздуха для разделения и накопление разделенных газов, комбинированная установка содержит воздухоразделяющую установку глубокого охлаждения, по меньшей мере часть воздуха до разделения в вышеуказанной воздухоразделяющей установке подвергается предварительному разделению ...

УСТАНОВКА ПОДГОТОВКИ УГЛЕВОДОРОДНОГО ГАЗА

... 1. Установка подготовки углеводородного газа, содержащая компрессор, холодильник газа, скруббер, сепаратор для отделения газа от жидкости, соединенный с выходом газа из скруббера и емкость для рециркуляции воды, соединенную со скруббером, отличающаяся тем, что она дополнительно снабжена рекуперативным теплообменником, промежуточным сепаратором и воздушным холодильником, причем вход газа в рекуперативный теплообменник соединен с выходом газа из компрессора, а выход газа из рекуперативного теплообменника соединен со входом газа в холодильник газа, при этом выход воды из емкости рециркуляции воды дополнительно соединен со входом воды в рекуперативный теплообменник, выход воды из которого соединен через промежуточный сепаратор и воздушный холодильник с емкостью рециркуляции воды. 2. Установка по п.1, отличающаяся тем, что она дополнительно снабжена сепаратором, установленным на выходе газа из холодильника газа и соединенным со входом газа в скруббер.

СПОСОБ ПЕРЕРАБОТКИ НИЗКОНАПОРНЫХ УГЛЕВОДОРОДНЫХ ГАЗОВ И ЖИДКИХ УГЛЕВОДОРОДОВ

СПОСОБ ОЧИСТКИ КРИОАГЕНТА

Изобретение относится к криогенной технике, в частности к способам очистки криоагентов от примесей, и может быть использовано в криогенных гелиевых и воздухоразделительных установках, а также в установках по переработке природного газа. Основная задача изобретения - стабилизация работы адсорбера, увеличение времени его непрерывной работы и уменьшение габаритов, а также очистка криоагента с возможностью выделения содержащихся в нем примесей для дальнейшего их использования как выходного продукта. Для этого в способе очистки криоагента, включающем последовательное охлаждение криоагента, конденсацию примеси и отделение жидкой фракции примеси, нагревание криоагента и последующее адсорбирование оставшейся в нем примеси, криостатирование процесса адсорбции ведут охлаждением адсорбента отделенной жидкой фракцией примеси. Для уменьшения концентрации примеси в газовой фракции перед адсорбером криоагент охлаждают до температуры 1,02-1,5 Тпл (температуры плавления примеси) и вторично отделяют жидкую ...

Способ очистки аргона

Способ очистки природного газа от кислых компонентов

Изобретение относится к технологии переработки газа, в частности к очистке газа от кислых компонентов. Для осуществления очистки природного газа от кислых компонентов путем ступенчатого охлаждения с одновременной конденсацией кислых компонентов с получением жидкой фазы, для повьше- ния степени извлечения кислых компонентов и удешевления процесса охлаждения ведут в три ступени, причем на первой ступени - воздухом, а на последующих ступенях - испаряющейся жидкой фазой, полученной на предыдущей CTjraeHH охлаждения. 1 табл. (Л с ...

Способ разделения воздуха

CПOCOБ PAЗДEЛEHИЯ BOЗДУXA

Способ обогащения неоно-гелиевой смеси

Способ переработки нефтяных газов

Способ выделения тяжелых углеводородов C4 и выше из газовых смесей

Способ получения загрязненного, приблизительно 70%-ного кислорода

Установка для очистки аргона

Способ очистки сырого аргона от кислорода

Verfahren und Vorrichtung für die Herstellung von Kohlenoxid und Wasserstoff.

VERFAHREN ZUR REINIGUNG VON STICKSTOFF-FLUORID.

Process for purifying a crude gas for the ammonia synthesis by means of a nitrogen scrub

The process serves for purifying a crude gas for the ammonia synthesis by means of a nitrogen scrub. For this purpose, the crude gas is cooled down in a first stage, partly condensed and subjected to a separation. The liquid fraction arising, which mainly contains CH4 and CO, is taken off, while the gaseous fraction alone is subjected to the nitrogen scrub. Due to the low methane concentration in the gaseous fraction, the nitrogen scrub can be run at a temperature below the solidification point of methane. ...

Verfahren und Vorrichtung zur Entfernung von Spurenverunreinigungen aus Kohlendioxyd

Verfahren zum Reinigen zu zerlegender Gasgemische

KRYOGENE RUECKGEWINNUNG VON HOCHREINEM WASSERSTOFF.

Process for recovering highly pure oxygen from less pure oxygen in a distillation system comprises cooling the heat exchange fluid downstream of the high pressure column sump vaporizer and upstream of a pressure relieving device

Process for recovering highly pure oxygen from less pure oxygen in a distillation system consisting of a high pressure column (2) and a low pressure column (3) comprises cooling the heat exchange fluid (107) downstream of the high pressure column sump vaporizer (4) and upstream of a pressure relieving device (109) in a sub-cooling heat exchanger (105) by indirect heat exchange. An Independent claim is also included for a device for recovering highly pure oxygen from less pure oxygen in a distillation system. Preferred Features: Gaseous heat exchange fluid (111) removed from the low pressure column head condenser (6) is heated in the sub-cooling heat exchanger. The heat exchange fluid is cooled upstream of the high pressure column sump vaporizer in a main heat exchanger (104) and the main heat exchanger and the sub-cooling heat exchanger are formed by an integrated heat exchanger block (103).

WIEDERGEWINNUNG VON HELIUM ZUR HERSTELLUNG VON OPTISCHEN FASERN

LUFTTROCKNER

GASADSORBER

Verfahren zur Vermeidung der Explosionsgefahr im Verdampferraum von Luftzerlegungsanlagen

Low boiling gases purification - by condensation, reheating and adsorption

Low-boiling gases (helium, hydrogen, neon) are purified by removal of higher boiling impurities. The greater part of the latter is separated by condensation. The gas is reheated after the condensation cycle and the remaining impurities are removed at room temp. by adsorption.

Reinigungsfluessigkeit fuer Tieftemperatur-Apparate

Verfahren und Vorrichtung zur Herstellung eines flüssigen Druckstromes von hochreinem Kohlendioxid

Verfahren und Vorrichtung zur Verbesserung von Rückgewinnung von Kohlendioxyd

Methane - free synthesis gas - from dip-flame process

Cracked gas from dip-flame process, after separation of CO2, H2S, steam and C2+ hydrocarbons, is cooled in one or more stages to liquefaction temp. of CO at 8 atmos and condensate so produced is then used as the washing agent in a counter-current column.

Method and apparatus for controlling condensation of gaseous hydrocarbon stream

Process for the production of hydrogen or hydrogen-nitrogen mixtures from hydrocarbons

H2 or H2/N2 mixture is produced by reacting a hydrocarbon material with water-vapour using external heating, and fractionating and/or scrubbing with liquid N2 the cracked gas to give a crude H2 or H2N2 fraction, and a fraction containing CO and CH4 which is used to heat the reaction, the reaction conditions and reactant ratios being such that the heating fraction produced is sufficient to supply all the external heat required. Specified hydrocarbon materials are light petroleum and natural gas. The cracked gas may be separated in cyclically operable regenerators to form a condensed heating fraction and a crude H2 fraction, the H2 may then be purified, e.g. by partial condensation and the impurities added to the evaporated heating fraction. The product H2 or H2/N2 mixture may be used in NH3 synthesis, in which case, an O2-free "stack gas" (gaseous combustion products of carbonaceous material), containing N2 and CO2 may be added before, during or after the reaction. CO2 may be removed before ...

Process for liquefying a natural gas stream containing at least one freezable component

Improvements in or relating to the precooling and purification of gaseous mixtures prior to liquefaction

... 615,683. Liquefaction of gases. BRITISH OXYGEN CO., Ltd., and SCHUFTAN, P. M. June 25, 1946, No. 18965. [Class 8 (ii)] Prior to liquefaction a gas mixture is precooled and its impurities removed by being brought into direct countercurrent contact with a cold liquid, e.g. a glycol-water mixture in a unit 10, and the liquid is afterwards regenerated by means of heat transfer in an exchanger 17 with a gaseous coolant derived from the sequential liquefaction of the gas mixture. Impurity-laden glycol-water mixture leaving the unit 10 has its water content reduced in a purifier 15 from which the mixture then passes in direct or indirect contact with liquefied gases entering and leaving the exchanger 17 by ducts 18, 19 respectively. A pump 21 then delivers the regenerated liquid through a second exchanger 23, where it is cooled by indirect contact with boiling ammonia, before passing to the exchanger 10.

Improvements in the purification of hydrogen for destructive hydrogenation

For the hydrogenation of carbonaceous materials hydrogen is scrubbed with liquefied hydrocarbons which are gaseous at ordinary temperatures, and is subsequently washed with oils to remove traces of the said scrubbing agents. Liquefied methane, ethane, p propane, butane, ethylene, or a mixture of these is suitable. The scrubbing may be performed under pressure. The hydrogen is preferably subjected to a preliminary purification to remove the greater part of the impurities such as hydrocarbons, carbon dioxide, ammonia, &c.

SIMPLIFIED APPARATUS FOR PRODUCING LIQUID NITROGEN

REMOVAL AND RECOVERY OF SULPHUR DIOXIDE FROM STACK GASES

"improvements in and relating to low-temperature gas absorption"

Apparatus for carrying out a process of separating one component of mixed gases, such as CO2 or H2S from a hydrogen-containing gas, by absorption in and desorption from absorber liquid comprising an absorption tower having an upper lean absorption section and a lower rich absorption section and a stripping tower having an upper rich stripping section and a lower lean stripping section, characterized by a cooler to cool the absorber liquid leaving said lower rich absorption section, a pump to pressurize absorber liquid leaving said upper rich stripping section and to introduce the pressurized absorber liquid into said lower rich absorption section, and a pump to pressurize absorber liquid leaving said lower lean stripping section and to introduce the pressurized absorber liquid into said upper lean absorption section. The stripping of said component is effected by passing a stripping gas in countercurrent contact first with the enriched lean absorber liquid and then with the cooled rich ...

Improvements in or relating to methods and devices for separating components from a gas and/or vapour mixture

... 885,482. Cold separation of gas mixtures. PHILIPS' GLOEILAMPENFABRIEKEN N. V. July 23, 1958 [July 26, 1957], No. 23701/58 Class 8(2). Readily condensible impurities e.g. water carbon dioxide and acetylene are separated from a gas mixture e.g. air to be rectified or merely liquefied by passing the mixture through a layer of snow formed on a gauze 2, Fig. 1, supported by vertical radially extending copper strips 1 and horizontal radial strips 4 ; the lower ends of the strips 1 and gauze 2 dipping into a liquid air gutter 3. As shown in Fig. 3 water is trapped by snow formed on an outer gauze 2a and carbon dioxide on snow formed on an inner gauze 2; the copper strips 1, 4 being carried by the cold head 9 of a gas refrigerator of the reversed hot gas engine type.

Improvements in the cold separation of gas-mixtures

... 746,436. Cold separation of gas mixtures. NAAMLOOZE VENNOOTSCHAP PHILLIP'S GLOEILAMPENFABRIEKEN. April 15, 1954 [April 22, 1953], No. 11161/54. Class 8(2). In the separation of one or more condensible components of a gas mixture e.g., the water and carbon dioxide content of air by cooling in a heat exchanger the latter comprises a plurality of fins or vanes 16, Fig. 1, projecting laterally from a carrier 15 connected at one end 14 to a thermal sink e.g., a known gas refrigerator, the mean temperature of the vane or vanes on which deposition of a component begins being maintained at not more than 20‹C. below the highest temperature at which deposition can occur and also the temperature difference between successive vanes in the direction of gas flow being not greater than 20‹C. In operation air enters an aperture 23 of an insulating screen 22 and traverses staggered apertures 17 of a group 18 of vanes 16 which serve to freeze the water vapour content. Dry air at 60‹C. then traverses a second ...

METHOD OF LIQUEFYING A CONTAMINATED HYDROCARBON-CONTAINING GAS STREAM

Device separating, with létat solid, of the components of a gas mixture.

METHOD OF LIQUEFYING A CONTAMINATED HYDROCARBON-CONTAINING GAS STREAM

METHOD OF LIQUEFYING A CONTAMINATED HYDROCARBON-CONTAINING GAS STREAM

Process for liquefying a natural gas stream containing at least one freezable component

Method and apparatus for controlling condensation of gaseous hydrocarbon stream

Aromatics and/or heavies removal from a methane-based feed by condensation and stripping

Removing contaminants from natural gas.

Installation of gas fractionation.

Device allowing separation by cooling, at the solid state, of the components of a gas mixture.

A refrigeration process and the production of liquefied natural gas.

PROCEDURE AND DEVICE FOR THE PRODUCTION OF A LIQUID PRINTING ROME OF HIGHLY PURE CARBON DIOXIDE

VERFAHREN UND VORRICHTUNG ZUM VERFLUSSIGEN VON KOHLENSAURE

PROCEDURE FOR REKTIFIKATIVEN CLEANING OF AT LEAST 85 VOL % CARBON DIOXIDE CONTAINING GAS MIXTURES

PROCEDURE FOR REKTIFIKATIVEN CLEANING OF AT LEAST 85 VOL % CARBON DIOXIDE CONTAINING GAS MIXTURES

DISTILLATIVE SEPARATION OF CARBON DIOXIDE FROM A CARBON DIOXIDE/CHYDROGEN SULFIDE MIXTURE.

Verfahren und System zur Verarbeitung von Verbrennungsgasen einer Wärmequelle

Die Erfindung betrifft ein Verfahren und eine Verarbeitungsvorrichtung für Verbrennungsstoffe einer Wärmequelle (2). Die durch Verbrennung von wasserstoffhaltigem Gasbrennstoff (19) entstehenden Verbrennungsstoffe werden nach dem Verlassen einer Wärmequelle in einem Thermokondensator (1) auf eine Temperatur abgekühlt, die niedriger als der Taupunkt der Verbrennungsstoffe liegt und parallel dazu niedriger ist als die Temperatur des Rücklaufzweigs (4) des Heizmediums. Bei der Abkühlung kommt es zur Kondensation des Wasserdampfs und zur Abtrocknung der Verbrennungsstoffe. Die Verbrennungsstoffe werden bis unter die Temperatur der Verflüssigung abgekühlt, wobei aus dem Verbrennungsstoff CO2 abgeschieden wird. Die Wärme aus dem Thermokondensator (1) wird in die Wärmepumpe (9) abgeleitet, die an ihrem Ausgang das Heizmedium erwärmt, vorrangig im Rücklaufzweig (4). Wenigstens ein Teil der Wärmequelle (2) weist die Form der Kogenerationseinheit auf, welche elektrische Energie produziert. Dabei ...

CRYOGENIC PROCEDURE FOR REMOVING FROM SOUR GASES FROM A GAS MIXTURE BY SOLVENTS.

PROCEDURE AND DEVICE FOR THE VERFLUSSIGEN OF COAL-SOUR

PROCEDURE FOR THE TREATMENT OF GAS FLOWS

Adsorption filter for the removal of smell materials from liquid gases

Process and apparatus for heavy hydrocarbon removal from lean natural gas before liquefaction

Documen4-24/0D/2020 A process is described herein for removing high freeze point hydrocarbons, including benzene compounds, from a mixed feed gas stream. The process involves cooling process streams in one or more heat exchangers and separating condensed compounds in multiple separators to form a methane-rich product gas stream. Select solvent streams from a fractionation train and/or separate solvent streams are employed to lower the freeze point of one or more streams that contain high freeze point hydrocarbons. A corresponding system also is disclosed.

INDUSTRIAL PROCESS FOR THE REMOVAL OF CHLORINE

METHOD AND APPARATUS OF PRODUCING CARBON DIOXIDE IN HIGH YIELDS FROM LOW CONCENTRATION CARBON DIOXIDE FEEDS

Process and apparatus for the purification of methane rich gas streams

Process and apparatus for removal of sour species from a natural gas stream

A process for removal of sour species from a dehydrated natural gas feed stream is provided. The dehydrated natural gas feed stream is cooled to conditions where a slurry of solid sour species and hydrocarbon liquids is formed together with a gaseous stream containing gaseous sour species. The gaseous stream containing gaseous sour species is then separated from the slurry and treated with a liquid solvent, thereby forming a liquid solution of the sour species and a dehydrated sweetened natural gas product stream. An apparatus for removing sour species from a dehydrated natural gas feed stream is also provided. The apparatus has a vessel with a solids formation zone in fluid communication with a gas solvation zone. The solids formation zone is configured to facilitate formation of a slurry of solid sour species and hydrocarbon liquids and a gaseous stream containing gaseous sour species. The gas solvation zone is configured to facilitate formation of a liquid solution of sour species. The ...

Process for obtaining helium

Apparatus for the liquefaction of natural gas and methods relating to same

ARGON AND NITROGEN COPRODUCTION PROCESS

Mixed refrigerant liquefaction system and method

A system for liquefying a gas includes a liquefaction heat exchanger having a feed gas inlet adapted to receive a feed gas and a liquefied gas outlet through which the liquefied gas exits after the gas is liquefied in the liquefying passage of the heat exchanger by heat exchange with a primary refrigeration passage. A mixed refrigerant compressor system is configured to provide refrigerant to the primary refrigeration passage. An expander separator is in communication with the liquefied gas outlet of the liquefaction heat exchanger, and a cold gas line is in fluid communication with the expander separator. A cold recovery heat exchanger receives cold vapor from the cold gas line and liquid refrigerant from the mixed refrigerant compressor system so that the refrigerant is cooled using the cold vapor.

Sublimation systems and associated methods

A system for vaporizing and sublimating a slurry comprising a fluid including solid particles therein. The system includes a first heat exchanger configured to receive the fluid including solid particles and vaporize the fluid and a second heat exchanger configured to receive the vaporized fluid and solid particles and sublimate the solid particles. A method for vaporizing and sublimating a fluid including solid particles therein is also disclosed. The method includes feeding the fluid including solid particles to a first heat exchanger, vaporizing the fluid, feeding the vaporized fluid and solid particles to a second heat exchanger and sublimating the solid particles. In some embodiments the fluid including solid particles is liquid natural gas or methane including solid carbon dioxide particles.

HELIUM-RECOVERY PLANT

A helium recovery plant adapted to filter, compress, and purify helium gas collected from one or more helium-using instruments, as well as to liquefy and redistribute the purified gas within a closed system. The recovery plant is adapted to match the purification and liquefaction rate of the system with the consumption rate of the coupled instruments. Additionally, the recovery plant is adapted to match the liquefaction rate of a liquefaction module with a boil-off rate of liquid helium within a Dewar thereof. The recovery plant is further adapted to recycle helium therein in an effort to achieve zero loss. 1. A helium recovery plant for recovering helium from helium-using equipment , the recovery plant comprising:a recovery module coupled to the helium gas using equipment, said recovery module being adapted to recover gas-phase helium from the helium-using equipment;a pressurized storage module coupled to said recovery module, said storage module being adapted to filter, compress, and store the recovered gas-phase helium of said recovery module;a purification module coupled to said storage module, said purification module comprising one or more refrigerators adapted to remove impurities from the recovered gas-phase helium to form an amount of purified gas-phase helium;a first distribution management module comprising a first distribution means, said first distribution management module being disposed between said storage module and said purification module and adapted to regulate a flow of the gas-phase helium therebetween;a liquefaction module comprising one or more liquefiers, said liquefaction module being adapted to liquefy the purified gas-phase helium into liquid-phase helium using said one or more liquefiers;a second distribution management module comprising a second distribution means, said second distribution management module being disposed between said purification module and said liquefaction module and adapted to regulate a flow of gas therebetween; ...

SEPARATION OF A GAS MIXTURE

A method is described for use in the separation of carbon dioxide from a gas mixture comprising carbon dioxide. The method includes the steps of: (i) compressing and cooling the gas mixture using a compressor to form a two-phase mixture including liquid carbon dioxide (ii) separating a liquid carbon dioxide stream from the two-phase mixture; and (iii) recirculating at least a part of the liquid carbon dioxide stream and introducing the recirculated liquid stream into a process stream by recirculating separated liquid COinto an upstream process stream, cooling of the process stream can be obtained. By using the liquid stream, additional cooling is possible as cooling is affected by the evaporation of the liquid CO. Thus the recirculated liquid can be used to reduce the temperature of the process stream. 1. A method for use in the separation of carbon dioxide from a gas mixture comprising carbon dioxide , the method comprising the steps of:(i) compressing and cooling the gas mixture using a compressor to form a two-phase mixture including liquid carbon dioxide(ii) separating a liquid carbon dioxide stream from the two-phase mixture; and(iii) recirculating at least a part of the liquid carbon dioxide stream and introducing the recirculated liquid stream into a process stream.2. A method according to claim 1 , wherein the recirculated COliquid stream is introduced upstream of the compressor.3. A method according to claim 1 , wherein a gaseous stream is fed to the compressor and at least a part of the recirculated liquid carbon dioxide stream is introduced into the gaseous stream claim 1 , such that the liquid carbon dioxide evaporates before entering the compressor.4. A method according to wherein the gas mixture further includes hydrogen claim 1 , the two phase mixture comprising liquid carbon dioxide and a hydrogen rich gas claim 1 , wherein the hydrogen rich gas is separated from the two-phase mixture and at least a part of the separated hydrogen rich gas stream is ...

Ethylene Expansion for Low Temperature Refrigeration in Polyethylene Vent Recovery

Provided are processes and systems for recovering hydrocarbons in a vent stream from a polymerization process. The methods and systems may include the recovery of an olefin monomer from a polymerization vent gas using ethylene refrigeration to condense and recover the olefin monomers from the vent gas. In some embodiments, the methods and systems may also include compression and condensation of polymerization vent gas, recompression of ethylene refrigerant, and use of an expander compressor turbine device for ethylene refrigeration. 1. A process for recovery of hydrocarbons from a polymerization vent gas , the process comprising:(a) reducing a pressure of an ethylene stream from a pressure of greater than or equal to 3.4 MPa to a pressure of less than or equal to about 1.4 MPa to form a reduced pressure ethylene stream;(b) cooling a vent gas comprising a monomer via heat exchange with the reduced pressure ethylene stream to form a first condensate comprising at least a portion of the monomer entrained in a first light gas;(c) recovering the first condensate and the first light gas;(d) separating the first condensate from the first light gas;(e) compressing the reduced pressure ethylene stream to a pressure of greater than or equal to 2.4 MPa;(f) passing the compressed ethylene stream to a polymerization reactor.2. The process according to claim 1 , wherein the pressure of the ethylene stream is reduced to about 0.9 MPa or less.3. The process according to claim 1 , wherein the pressure of the ethylene stream is reduced to about 0.2 MPa or less.4. The process according to claim 1 , further comprising cooling the ethylene stream to a temperature of about 10° C. or less before step (a).5. The process according to claim 1 , further comprising cooling the compressed ethylene stream a temperature of about 10° C. or less.6. The process according to claim 1 , further comprising cooling the polymerization vent gas via heat exchange with the reduced pressure ethylene stream ...

HIGH PRESSURE RECOVERY OF CARBON DIOXIDE FROM A FERMENTATION PROCESS

The present invention relates to a method for recovering carbon dioxide from a gaseous stream originating from a fermentation process by compression, absorption, condensation and distillation, wherein at least the absorption and condensation is performed under a high pressure of at least 30 bar. 117-. (canceled)18. A method for recovering carbon dioxide from a gaseous carbon dioxide stream originating from a fermentation process or a bottling line , the method comprises the steps of:a) providing the carbon dioxide stream originating from the fermentation process or bottling line;b) compressing the provided carbon dioxide stream by at least one compression step providing a compressed gaseous stream;c) subjecting the compressed gaseous stream to an absorption step providing at least a carbon dioxide rich gaseous stream;d) condensing the carbon dioxide rich gaseous stream in a condenser providing at least a condensate and a purge gas;e) distilling the liquid carbon dioxide stream to provide purified carbon dioxide. wherein the pressure of the compressed gaseous stream obtained in step b) is at least 30 bar, the temperature is within a range where there is substantially no condensation of carbon dioxide and that said pressure is maintained to at least step d) andwherein the condensation of step d) is performed by a coolant present in the brewery, or bottlery for example brine.19. A method according to claim 18 , wherein the absorbent of step c) is water or liquid carbon dioxide claim 18 , preferably liquid carbon dioxide.20. A method according to further comprising the step of transferring the condensed claim 18 , distilled carbon dioxide to a storage tank having a pressure that is lower than the condensation pressure of step d) claim 18 , whereby in addition to the liquid carbon dioxide is formed a gaseous stream and wherein said gaseous stream is further processed.21. A method according to claim 20 , wherein the further processing is selected from: transferring as a ...

APPARATUS AND PROCESS FOR WORKING UP A HYDROGEN- AND METHANE-COMPRISING STREAM

The invention relates to an apparatus () for working up a hydrogen- and methane-comprising stream (), which comprises the following components: 110011. An apparatus () for working up a hydrogen- and methane-comprising stream (.) , which comprises the following components:{'b': 1', '1', '1, '(i) at least one heat exchanger (KS) for cooling a stream (.) to be worked up;'}{'b': 1', '2', '2', '3', '5, '(ii) at least one separation unit (A, A, A, A′) for purifying the stream () to be worked up to give a stream () rich in hydrogen and methane;'}{'b': 2', '5, '(iii) at least one cooling unit (KS) for cooling the stream () rich in hydrogen and methane; and'}{'b': 3', '6', '7', '8', '9, '(iv) at least one cryogenic gas separation unit (KS) for separating the stream () rich in hydrogen and methane into at least one hydrogen-rich stream () and at least one methane-rich stream (, ).'}210011123. The apparatus () according to claim 1 , wherein the stream (. claim 1 , . claim 1 , ) to be worked up comprises at least 40% by volume of hydrogen and at least 15% by volume of methane.31001. The apparatus () according to claim 1 , wherein the at least one heat exchanger (KS) is configured as a plate claim 1 , helical or shell-and-tube heat exchanger.41001. The apparatus () according to claim 1 , wherein the heat exchanger (KS) is made of steel claim 1 , copper claim 1 , aluminum claim 1 , glass claim 1 , plastic claim 1 , enamel and/or silicon carbide.5100122122. The apparatus () according to claim 1 , wherein the separation unit (A claim 1 , A claim 1 , A claim 1 , A′) comprises at least one phase separator (A) and/or at least one gas purification unit (A claim 1 , A′).610022. The apparatus () according to claim 5 , wherein the gas purification unit (A claim 5 , A′) is configured as an adsorptive gas purification unit.710022. The apparatus () according to claim 5 , wherein the gas purification unit (A claim 5 , A′) is configured as a continuously operated temperature-swing adsorption. ...

PROCESSES AND SYSTEMS FOR PURIFYING SILANE

Processes and systems for purifying silane-containing streams and, in particular, for purifying silane-containing streams that also contain ethylene are disclosed. The processes and systems may be arranged such that one or more ethylene reactors are downstream of light-end distillation operations. 1. A process for purifying a silane-containing stream , the stream comprising silane , ethylene and one or more compounds having a boiling point less than silane , the process comprising:introducing the silane-containing stream into a reactor to convert ethylene to at least one of ethylsilane and ethane and to produce an ethylene-depleted stream relative to the silane-containing stream; andintroducing the ethylene-depleted stream into a light-ends distillation column to produce a silane-depleted overhead fraction and a silane-enriched bottoms fraction relative to the ethylene-depleted stream, the silane-enriched bottoms fraction comprising silane and at least one of ethylsilane and ethane.2. The process as set forth in wherein the silane-enriched bottoms fraction produced from the light-ends distillation column is introduced into a heavy-ends distillation column to produce a silane-enriched overhead fraction and a silane-depleted bottoms fraction relative to the silane-enriched bottoms fraction produced from the light-ends distillation column claim 1 , the silane-depleted bottoms fraction being enriched in at least one of ethylsilane and ethane.3. The process as set forth in wherein the silane-containing stream comprises compounds having a boiling point greater than silane other than ethylsilane and ethane claim 2 , wherein the silane-depleted bottoms fraction produced from the heavy-ends distillation column is enriched in such compounds.4. The process as set forth in wherein the one or more compounds having a boiling point greater than silane are selected from the group consisting of diethyl silane claim 3 , toluene claim 3 , dimethoxyethane and mixtures thereof.5. The ...

System and Method of Capturing, Processing and Utilizing Stranded Natural Gas

A system and method for utilizing stranded natural gas produced by one wellsite or facility site at a second wellsite or facility site as natural gas in a fuel supply system to reduce the dependency of diesel fuel in operating equipment at the second wellsite or facility site. The system and method includes transporting the gas collected at the first wellsite or facility site to the second wellsite or facility site as a gas mixture of natural gas and hydrocarbon liquids in vapor form at a pressure and temperature to prevent drop out of the hydrocarbon liquids during transport. At the second wellsite or facility site, the gas mixture is processed to recover the hydrocarbon liquids and to provide a compressed natural gas free of the hydrocarbon liquids to a fuel system for combustion by wellsite or facility site equipment. 1. A method of transporting , processing , and utilizing stranded natural gas , comprising the steps of:transporting compressed natural gas containing hydrocarbon liquids in vapor form captured from a natural gas producing well at a gas well location in pressure containers from said gas well location to a gas consuming location; andprocessing said compressed natural gas containing hydrocarbon liquids in vapor form at said gas consuming location to provide a compressed natural gas separate of said hydrocarbon liquids to a fuel system for consumption.2. A method of capturing , transporting , processing , and utilizing stranded natural gas , comprising the steps of:capturing natural gas from a natural gas producing well at a gas well location to provide raw natural gas;conditioning said raw natural gas to sweeten and dehydrate said raw natural gas to provide a sweet dry natural gas;compressing and cooling said dry natural gas to a pressure and temperature to provide a compressed natural gas containing hydrocarbon liquids in vapor form;transporting said compressed natural gas containing hydrocarbon liquids in vapor form in pressure containers from said ...

Natural Gas Processing Plant

The invention provides systems and methods for separating ethane and heavier hydrocarbons from a natural gas stream. In aspects of the invention, an adsorption unit is integrated with a cryogenic gas processing plant in order to overcome methane recovery limitations by sending the tail gas from the adsorption unit to the cryogenic gas processing plant to recover methane that would otherwise be lost. 2. The system of claim 1 , further comprising a heat exchanger configured to receive and cool the first stream.3. The system of claim 1 , wherein the raw natural gas stream comprises at least 60% methane by volume.4. The system of claim 1 , wherein the raw natural gas stream comprises less than 2% carbon dioxide by volume.5. The system of claim 1 , wherein the raw natural gas stream comprises less than 100 ppm water vapor by volume.6. The system of claim 1 , wherein the pressure of the raw natural gas stream is greater than 700 psia.7. The system of claim 1 , wherein the adsorption unit is a pressure swing adsorption unit.8. The system of claim 6 , wherein the lowest pressure in the pressure swing adsorption unit during any single cycle is 1 atm.9. The system of claim 1 , wherein the adsorption unit is a vacuum swing adsorption unit.10. The system of claim 9 , wherein the lowest pressure in the vacuum swing adsorption unit during any single cycle is 0.05 atm.11. The system of claim 1 , wherein the beds of the adsorption unit have a length to diameter ratio less than 1.5.12. The system of claim 1 , wherein a portion of the compressed first stream is compressed to the pressure of the raw natural gas stream claim 1 , recycled claim 1 , and fed to the adsorption unit.13. The system of claim 1 , wherein the adsorption unit is portable.14. A system for treating raw natural gas comprising:(i) an adsorption unit configured to receive a raw natural gas stream and produce a first stream comprising methane and enriched in natural gas liquids and a second stream comprising methane ...

PROCESS AND DEVICE FOR TREATING FLUE GASES

A process and a device for treating a carbon dioxide-containing flue gas stream are described. At least a part of the carbon dioxide present is removed from the flue gas stream by means of a scrubber, forming a low carbon dioxide gas stream and a high carbon dioxide gas stream. The high carbon dioxide and water-saturated gas stream formed from the flue gas stream after removal of the carbon dioxide is cooled by means of a refrigeration system in a heat exchanger below the dew point temperature of the water contained in the gas stream and dried by condensing and separating out the water in a condensate separator . The dried gas stream meets the requirements of carbon dioxide products intended for further use. 14. Process for treating a carbon dioxide-containing flue gas stream , wherein at least a part of the carbon dioxide present is removed from the flue gas stream by means of a scrubber , forming a low carbon dioxide gas stream and a high carbon dioxide gas stream , characterized in that the high carbon dioxide and water-saturated gas stream formed from the flue gas stream after removal of the carbon dioxide is cooled by means of a refrigeration system () below the dew point temperature of the water contained in the gas stream and dried by condensing and separating out the water.24. Process according to claim 1 , characterized in that claim 1 , as a refrigeration system () claim 1 , an absorption refrigeration system is used.3. Process according to claim 2 , characterized in that the absorption refrigeration system is driven by means of thermal energy claim 2 , in particular in the form of steam and/or remote heat and/or direct firing.4. Process according to claim 3 , characterized in that claim 3 , in the case of treatment of a flue gas stream from a coal-fired combustion and/or gasification plant claim 3 , the thermal energy is obtained from vapours (BD) and/or vapour condensate of a coal drying stage connected upstream of the combustion and/or gasification ...

CARBON DIOXIDE RECOVERY APPARATUS AND CARBON DIOXIDE RECOVERY METHOD

In one embodiment, a carbon dioxide recovery apparatus includes a heat exchanger which heats a first rich liquid, a flow divider which divides the first rich liquid heated by the heat exchanger into a second rich liquid and a third rich liquid, a first release device which heats the second rich liquid and discharges a first semi-lean liquid, a second release device which heats the third rich liquid and discharges a second semi-lean liquid, and a regeneration tower which heats the first and second semi-lean liquids to generate a lean liquid. The first release device heats the second rich liquid, using the lean liquid. The second release device heats the third rich liquid, using a carbon dioxide-containing steam discharged at the regeneration tower. The heat exchanger heats the first rich liquid, using the lean liquid which has passed through the first release device. 1. A carbon dioxide recovery apparatus comprising:an absorption tower which introduces therein carbon dioxide-containing gas and brings the carbon dioxide-containing gas into contact with an absorbing liquid for absorbing carbon dioxide to generate a first rich liquid having absorbed the carbon dioxide, and, thus, to discharge the first rich liquid;a heat exchanger which heats the first rich liquid;a flow divider which divides the first rich liquid heated by the heat exchanger into a second rich liquid and a third rich liquid;a first carbon dioxide release device which heats the second rich liquid and thereby discharges a first semi-lean liquid in which carbon dioxide-containing steam is released;a second carbon dioxide release device which heats the third rich liquid and thereby discharges a second semi-lean liquid in which carbon dioxide-containing steam is released; anda regeneration tower which heats the first semi-lean liquid and the second semi-lean liquid to release remaining carbon dioxide-containing steam, and, thus, to generate a lean liquid and thereby returns the lean liquid to the absorption ...

Method and apparatus for separating air by cryogenic distillation

A method and apparatus for the cryogenic distillation of air to produce gaseous oxygen with a purity between 75 and 95 mol % and a pressure lower than 5.5 bar abs using a triple column having a high-pressure column, a low-pressure column, and a medium-pressure column, wherein the medium-pressure column is at least partially thermally coupled with the low-pressure column and the high-pressure column is also at least partially thermally coupled with the low-pressure column.

Adsorbed Natural Gas Storage Facility

A method of using the natural gas storage facility to reduce the effect of diurnal demand on a natural gas source includes introducing natural gas into the natural gas storage facility, separating the natural gas into a heavy natural gas component and a light natural gas component, and retaining the components during a non-peak period of demand. The natural gas storage facility includes a guard bed system and an adsorption bed system. The method also includes releasing the heavy and light natural gas components, mixing them into a released natural gas component product and introducing it to the natural gas source during a peak period of demand. 2. The method of where the guard bed system includes a heavy natural gas adsorbent and is operable to retain the heavy natural gas component by adsorption.3. The method of where the heavy natural gas adsorbent is a microporous material.4. The method of where the light natural gas component is substantially free of propane.5. The method of where the light natural gas component is substantially free of ethane.6. The method of where the released natural gas product has a similar thermal value to the thermal value of the introduced natural gas.9. The method of further comprising the step of operating a storage facility compressor during the introduction of the natural gas into the natural gas storage facility claim 1 , where the natural gas storage facility further comprises the storage facility compressor that is coupled to the guard bed system.10. The method of further comprising the step of operating a storage facility compressor during the period of peak demand such that a less than atmospheric condition forms in the guard bed system claim 1 , where the natural gas storage facility further comprises the storage facility compressor that is coupled to the guard bed system.11. The method of further comprising the step of operating a storage compressor during the period of peak demand such that a less than atmospheric pressure ...

Systems and Methods for Recovering Hydrocarbons From a Polyolefin Purge Gas Product

Provided are systems and methods for separating a purge gas recovered from a polyethylene product. The method includes recovering a polyethylene product containing one or more volatile hydrocarbons from a polymerization reactor and contacting the polyethylene product with a purge gas to remove at least a portion of the volatile hydrocarbons to produce a polymer product having a reduced concentration of volatile hydrocarbons and a purge gas product enriched in volatile hydrocarbons. The purge gas product is compressed to a pressure of 2,500 kPaa to 10,000 kPaa, and is then cooled and separated into at least a first product, a second product, and a third product. A portion of one or more of the first, second, or third products is then recycled as a purge gas, to the polymerization reactor, or to the purge gas product enriched in volatile hydrocarbons prior to compression, respectively. 1. A method for recovering hydrocarbons from a polyolefin purge gas product , comprising:recovering a polyolefin product comprising one or more volatile hydrocarbons from a polymerization reactor;{'sub': 2', '12, 'contacting the polyolefin product with a purge gas to remove at least a portion of the volatile hydrocarbons to produce a polymer product having a reduced concentration of volatile hydrocarbons and a purge gas product enriched in volatile hydrocarbons, wherein the volatile hydrocarbons comprise hydrogen, methane, one or more C-Chydrocarbons, or any combination thereof, and wherein the purge gas product is at a pressure of about 50 kPaa to about 250 kPaa;'}compressing the purge gas product to a pressure of about 2,500 kPaa to about 10,000 kPaa;cooling the compressed purge gas product;separating the cooled purge gas product into at least a first product, a second product, and a third product; andrecycling at least a portion of at least one of the first product as the purge gas, the second product to the polymerization reactor, or the third product to the purge gas product ...

PROCESS AND APPARATUS FOR PRODUCTION OF AMMONIA SYNTHESIS GAS AND PURE METHANE BY CRYOGENIC SEPARATION

A process for the production of ammonia synthesis gas and pure methane by cryogenic separation of a feed gas containing at least 75% hydrogen as well as methane and nitrogen, the feed gas is cooled in a heat exchanger and partially condensed, the partially condensed feed is sent to a phase separator, the gas from the phase separator is sent to a nitrogen wash column, liquid nitrogen is sent to the top of the nitrogen wash column and ammonia synthesis gas is removed from the top of the nitrogen wash column, the liquid from the phase separator is expanded and sent to a separation column, a nitrogen enriched gas stream is removed from the top of the column and a nitrogen depleted liquid stream rich in methane is removed from the bottom of the column and the nitrogen depleted liquid stream rich in methane is vaporized to form a pure methane product. 115-. (canceled)16. A process for the production of ammonia synthesis gas and pure methane by cryogenic separation of a feed gas containing at least 75% hydrogen as well as methane and nitrogen , the process comprising the steps of:cooling and partially condensing the feed gas in a heat exchanger to form a partially condensed feed;introducing the partially condensed feed to a phase separator;introducing gas from the phase separator to a nitrogen wash column;introducing liquid nitrogen to the top of the nitrogen wash column;withdrawing ammonia synthesis gas from the top of the nitrogen wash column;withdrawing liquid from the phase separator and expanding the liquid before sending the liquid to a separation column;withdrawing a nitrogen enriched gas stream from the top of the separation column;withdrawing a nitrogen depleted liquid stream rich in methane from the bottom of the separation column; andvaporizing the nitrogen depleted liquid stream rich in methane to form a pure methane product.17. The process according to claim 16 , wherein the feed gas comprises at least 5% nitrogen.18. The process according to claim 16 , ...

Method and arrangement for expanding a gas stream comprising carbon dioxide

The present disclosure relates to a method and an arrangement for expanding a gas stream comprising carbon dioxide, CO 2 . The method includes: removing CO 2 from a process gas to produce a CO 2 lean gas stream comprising residual CO 2 ; monitoring a temperature of the gas stream downstream of an expander; controlling a pressure of the gas stream downstream of the expander by means of a pressure controller; and overriding the pressure controller when the temperature downstream of the expander is below a predefined minimum temperature; whereby deposition of solid CO 2 from the residual CO 2 in the gas stream is avoided. The disclosure also relates to a gas cleaning system and a power plant, such as an oxy-combustion power plant, associated with the arrangement.

Method of recovering ammonia and method of recycling ammonia by using the same

There are provided methods capable of easily and efficiently recovering and recycling ammonia from exhaust gas containing a small amount of ammonia, the exhaust gas being exhausted from a production process of a gallium nitride compound semiconductor. The method of recovering ammonia includes filtering exhaust gas containing ammonia, hydrogen, nitrogen, and a solid compound with a filter to remove the solid compound from the exhaust gas; pressurizing and cooling the filtered exhaust gas with a heat pump to liquefy ammonia contained in the filtered exhaust gas; and separating liquefied ammonia from hydrogen and nitrogen to recover liquefied ammonia. The method of recycling ammonia includes evaporating recovered liquid ammonia; mixing the evaporated ammonia with another crude ammonia to obtain mixed gas; purifying the mixed gas; and supplying the purified gas to the production process of a gallium nitride compound semiconductor.

METHOD FOR CONTROLLING ACIDIC COMPOUNDS PRODUCED FOR OXY-COMBUSTION PROCESSES

The present invention relates generally to the field of emissions control and, in particular to a new and useful method and/or system by which to control, treat and/or mitigate various liquid-based acidic compounds that are produced during oxy-combustion (e.g., during a compression step and/or cooling step) from various gaseous acid compounds and/or gaseous acid precursor compounds (e.g., SO, NO, etc.). In one embodiment, the present invention relates to a method and/or system by which such one or more liquid-based acid compounds are recycled into the flue gases and/or into one or more of the emissions control and/or flue gas treatment equipment of an oxy-combustion power generation system. 1. A method for treating one or more acidic compounds generated during an oxy-combustion process , the method comprising the steps of:(i) generating a flue gas stream as a result of the oxy-combustion of at least one carbonaceous fuel, wherein the flue gas stream contains at least one type of gaseous acid compound and/or gaseous acid precursor compound;(ii) treating the flue gas stream to remove at least a portion of at least one gaseous acid compound and/or gaseous acid precursor compound present therein via the use of at least one flue gas treatment device;(iii) subjecting at least a portion of the flue gas stream from Step (ii) to at least one compression step and/or cooling step so as to remove at least one additional gaseous acid compound and/or gaseous acid precursor compound present therein, wherein the compression step and/or cooling step yields a liquid-based acidic waste stream generated as a result of the removal of the at least one additional gaseous acid compound and/or gaseous acid precursor compound and an acid-depleted, or acid-lean, flue gas stream;(iv) recycling at least a portion of the liquid-based acidic waste stream to the at least one flue gas treatment device of Step (ii) for treatment, or neutralization, therein; and(v) subjecting the acid-depleted, or ...

METHOD FOR SEPARATING C2+-HYDROCARBONS FROM A HYDROCARBON-RICH FRACTION

Described herein is a method for separating C-hydrocarbons from a hydrocarbon-rich fraction comprising partially condensing a hydrocarbon-rich fraction, and separating the hydrocarbon-rich fraction into a gaseous fraction and a liquid fraction. These fractions are subjected to a rectification fractionation to obtain a methane-rich fraction and a C-hydrocarbon-rich fraction. The methane-rich fraction is compressed, and a partial stream of the compressed methane-rich fraction is condensed is fed as reflux to rectification fractionation. In addition, before rectification fractionation, the liquid fraction is separated into two partial streams. The first partial stream is partially evaporated and then is fed to rectification fractionation. The second partial stream is undercooled and then is fed as additional reflux to rectification fractionation. 2. The method according to claim 1 , wherein said hydrocarbon-rich fraction is from natural gas.3211. The method according to claim 1 , wherein said first partial stream (′) is partially evaporated (E) against the hydrocarbon-rich fraction () that is to be partially condensed.42312. The method according to claim 1 , wherein the evaporation pressure of the first partial stream (′ claim 1 , ) is variable (V claim 1 , V).54210. The method according to claim 1 , wherein said second partial stream () is sub-cooled (E) against the methane-rich fraction () obtained from the rectification fractionation (T).6416. The method according to claim 5 , wherein the sub-cooled second partial stream (′) is fed as reflux to the rectification fractionation (T) at a feed point below the feedpoint of the condensed partial stream of the compressed methane-rich fraction used as reflux ().7. The method according to claim 1 , whereinthree heating circuits—via which intermediate fractions are drawn off from the rectification fractionation, partially evaporated and fed again to the rectification fractionation—are assigned to the rectification ...

Cryocooler-based gas scrubber

A cryocooler-based gas scrubber, or cryocooler-based gas purifier, utilizes the cooling power of a cryocooler to cool and condense cryogen gas forming coalesced impurities which are then filtered through a filter matrix, such as for example a fiberglass filter matrix. The scrubber may further comprise a counter-flow heat exchanger for warming the purified gas prior to dispensing at an outlet for storage or consumption.

Cryogenic Separation of Synthesis Gas

A process and apparatus for separating a feed containing hydrogen, carbon monoxide, methane, and optionally nitrogen to form a product gas having a desired H:CO molar ratio and optionally a hydrogen product gas and a carbon monoxide product gas. The feed is partially condensed to form a hydrogen-enriched vapor fraction and a carbon monoxide-enriched liquid fraction. The hydrogen-enriched vapor fraction and carbon monoxide-enriched liquid fraction are combined in a regulated manner to form an admixture, which is cryogenically separated to form the product mixture having the desired H:CO molar ratio. 112-. (canceled)13. An apparatus for separating a feed comprising hydrogen , carbon monoxide , methane , and optionally nitrogen , comprising:a first heat exchanger for partially condensing the feed to form a partially condensed feed;a phase separator for separating the partially condensed feed into a hydrogen-enriched vapor fraction and a carbon monoxide-enriched liquid fraction;a means for feeding the partially condensed feed to the phase separator from the first heat exchanger, the means for feeding the partially condensed feed configured so that no portion of the partially condensed feed passes through an expander when feeding the partially condensed feed to the phase separator from the first heat exchanger;a means for combining a portion or all of the carbon monoxide-enriched liquid fraction with a regulated portion of the hydrogen-enriched vapor fraction to form a two-phase admixture, the means for combining operatively disposed to receive the hydrogen-enriched vapor fraction from the phase separator without any other phase separator operatively disposed between the means for combining and the phase separator;a means for feeding at least one of the portion or all of the carbon monoxide-enriched liquid fraction and at least a portion of the two-phase admixture to the first heat exchanger;a first fractionator for cryogenically separating the at least a portion of the ...

METHOD AND DEVICE FOR GENERATING GASEOUS COMPRESSED NITROGEN

Method and device for generating gaseous compressed nitrogen by the low-temperature separation of air in a distillation column system, having a pre-column, a high-pressure column and a low-pressure column. The feed air is compressed, purified in a purification apparatus and cooled. A first sub-flow of the cooled feed air is introduced in a predominantly liquid state into the distillation column system. A gaseous fraction from the pre-column in introduced into the liquefaction chamber of a pre-column head condenser with liquid formed therein fed as reflux into the pre-column. A first gaseous nitrogen product fraction is drawn from the high-pressure column, heated, and obtained as first gaseous compressed nitrogen product. At least a part of the second sub-flow is introduced into the evaporation chamber of the pre-column head condenser. A third sub-flow of the cooled feed air is expanded to perform work and subsequently introduced into the liquefaction chamber. 2. The method as claimed in claim 1 , characterized in that a second gaseous nitrogen product fraction is drawn off from the pre-column in gaseous form claim 1 , warmed in the main heat exchanger and obtained as to second gaseous compressed product.3. The method as claimed in claim 1 , characterized in that less than 30 mol % of the input air quantity is fed in the liquid state into the distillation column system.4. The method as claimed in claim 1 , characterized in that the total quantity of oxygen-enriched currents that are fed in the liquid state from the pre-column and the evaporation chamber of the pre-column head condenser into the high-pressure column and the low-pressure column is less 14% than the input air quantity.5. The method as claimed in claim 1 , characterized in thatthe second partial current is compressed before being cooled in the main heat exchanger to a high pressure that is higher than the operating pressure of the pre-column, and is liquefied or pseudo-liquefied in the main heat ...

SYSTEMS AND METHODS FOR RECOVERING CARBON DIOXIDE FROM INDUSTRIALLY RELEVANT WASTE STREAMS, ESPECIALLY ETHANOL FERMENTATION PROCESSES, FOR APPLICATION IN FOOD AND BEVERAGE PRODUCTION

A system for recovering CO2 via liquefaction and purification from a vented CO2 gas stream comprising a compressor; a dehydrator; a scrubber; a refrigerator having one or more stages; and a separation subsystem adapted to ensure non-condensable gas content in the final product meets industry standards. The liquid CO2 product is of sufficient purity to be used in applications requiring beverage-grade CO2. The system can be utilized as a single-brewery installation to reduce venting from ethanol fermenters to an absolute minimum, produce a high purity liquid CO2 product for use in-process or external sales, and offset the purchasing of expensive, industrial CO2 of inferior purity. 1. An apparatus for recovering via purification and liquefaction of carbon dioxide gas from a vented CO2 waste gas stream , comprising:a chassis adapted for installation inside a space-limited production facility;one or more compressors for compressing the raw CO2 gas stream;one or more dehydrators for removing water from the compressed CO2 gas stream;one or more scrubbers containing solid-state adsorbent for deodorizing and purifying the inlet CO2 gas stream;a refrigerator having one or more stages for lowering a temperature of the dehydrated, deodorized, compressed CO2 stream; anda separation subsystem system adapted to separate the liquefied CO2 product from any remaining contamination by non-condensable gases, especially oxygen.2. The apparatus of claim 1 , wherein the final oxygen content is less than 30 parts per million.3. The apparatus of claim 1 , wherein the final water content is less than 20 parts per million.4. The apparatus of claim 1 , wherein the liquid CO2 product has no foreign color claim 1 , taste claim 1 , or odor.5. The apparatus of claim 1 , wherein the liquid CO2 product meets a beverage-grade standard.6. The apparatus of claim 1 , wherein the one or more compressors compress the raw natural gas stream to a pressure range of 75 psia to 300 psia.7. The apparatus of ...

SYSTEM AND METHOD FOR RARE GAS RECOVERY

A system and method for argon and nitrogen extraction and liquefaction from a low-pressure tail gas of an ammonia production plant is provided. The preferred tail gas of the ammonia production plant comprises methane, nitrogen, argon, and hydrogen. The disclosed system and method provides for the methane rejection via rectification and hydrogen rejection by way of a side stripper column or phase separator. The resulting nitrogen and argon containing stream is separated and liquefied in a double column distillation system. 1. A method for recovering a rare gas from a pre-purified feed gas comprising hydrogen , nitrogen , methane , argon , and one or more rare gases , the method comprising the steps of:directing the pre-purified feed gas to a rectification column;separating the pre-purified feed gas in a rectification column to produce a methane-rich liquid column bottoms containing the one or more rare gases and an hydrogen-nitrogen rich gas overhead;conditioning the methane-rich liquid column bottoms containing rare gases to produce a stream having a vapor fraction greater than 90% and at or near saturation;directing the methane rich stream and a rare gas lean stream to an auxiliary wash/rectifying column, wherein the rare gas lean stream is a liquid stream extracted from the rectification column or a liquid nitrogen stream;rectifying the two phase methane rich stream and the rare gas lean stream to produce a liquid bottoms rare gas concentrate and a methane-rich overhead; andseparating one or more rare gases from the liquid bottoms rare gas concentrate to produce a rare gas product stream.2. The method of claim 1 , wherein the feed gas is a tail gas from an ammonia plant.3. The method of wherein the rare gas is krypton or xenon.4. The method of claim 1 , wherein the feed gas contains greater than about 50% nitrogen by mole fraction.5. The method of wherein the feed gas is a high pressure feed gas having a pressure of between about 300 psia to 500 psia.6. The method ...

AIR SEPARATION METHOD AND APPARATUS

A method and apparatus for separating air in which an oxygen-rich liquid stream is pumped and then heated within a heat exchanger to produce an oxygen product through indirect heat exchange with first and second boosted pressure air streams. The first boosted pressure air stream is cold compressed at an intermediate temperature of the heat exchanger, reintroduced into the heat exchanger at a warmer temperature and then fully cooled and liquefied. The second boosted pressure air stream, after having been partially cooled, is expanded to produce an exhaust stream that is in turn introduced into a lower pressure column producing the oxygen-rich liquid. The second boosted pressure air stream is partially cooled to a temperature no greater than the intermediate temperature at which the cold compression occurs so that both the first and second boosted pressure air streams are able to take part in the heating of the oxygen-rich stream. 1. (canceled)2. (canceled)3. (canceled)4. (canceled)5. (canceled)6. (canceled)7. (canceled)8. (canceled)9. (canceled)10. (canceled)11. (canceled)12. (canceled)13. (canceled)14. (canceled)15. (canceled)16. (canceled)17. (canceled)18. (canceled)19. (canceled)20. (canceled)21. (canceled)22. (canceled)23. (canceled)24. (canceled)25. (canceled)26. (canceled)27. (canceled)28. (canceled)29. An apparatus for separating air comprising:one or more main air compressors configured for producing a stream of compressed and purified air, wherein the stream of compressed and purified air is split into a first part of the stream of compressed and purified air, a second part of the stream of compressed and purified air that is further compressed in a first booster compressor to produce a first boosted pressure air stream, and a third part of the stream of compressed and purified air that is further compressed in a second booster compressor to produce a second boosted pressure air stream;a main heat exchange system configured to cool the first part of the ...

Sales Gas Enrichment with Propane and Butanes By IDS Process

The present invention is a separation unit process in which a high pressure section of a separation unit operates at a relatively high pressure to initially process and separate a high pressure feed stream and a low pressure section of the separation unit to initially process and separate a low pressure feed stream, where the high pressure section and the low pressure section are integral with and exchange streams to accomplish a desired separation of a wellhead fluid feed which typically includes a heavier portion of pentanes and heavier components 1. A separation unit process for a hydrocarbon fluid feed from a wellhead source comprising:(a) separating the fluid feed in a high pressure drum to form an HP gas and an HP liquid;(b) reducing the pressure of the HP liquid to a low pressure and separating the low pressure HP liquid in a stabilizer column to form a sales oil product as a bottoms liquid product and a stabilizer overhead stream, which has hydrocarbon components that consist essentially of butanes and lighter components;(c) combining a compressed stabilizer overhead stream with the HP gas to be fed to a high pressure column operating at about the pressure of the natural HP gas feed, where a portion of a liquid bottoms stream of the high pressure column consists of a sales condensate stream recovering a portion of all hydrocarbon components of pentanes and heavier components in the fluid feed and a high pressure column overhead stream is compressed in a first compressor, where a portion of the compressed high pressure column overhead is further compressed to form a sale gas stream;(d) the balance of the compressed high pressure column overhead stream being cooled and fed to the bottom stage of an fuel gas absorber column operating at a substantially higher pressure than the high pressure column, where the fuel gas absorber column overhead stream is mixed with the balance of the liquid bottom stream of the high pressure column (pentanes plus), cooled and ...

Liquefied Natural Gas Production System and Method With Greenhouse Gas Removal

Described herein are systems and processes to produce liquefied natural gas (LNG) using liquefied nitrogen (LIN) as the refrigerant. Greenhouse gas contaminants are removed from the LIN using a greenhouse gas removal unit.

Increasing Efficiency In An LNG Production System By Pre-Cooling A Natural Gas Feed Stream

Described herein are systems and processes to produce liquefied natural gas (LNG) using liquefied nitrogen (LIN) as the refrigerant. Greenhouse gas contaminants are removed from the LIN using a greenhouse gas removal unit. The LNG is compressed prior to being cooled by the LIN. 1. A liquefied natural gas production system , the system comprising:a natural gas stream from a supply of natural gas;a refrigerant stream from a refrigerant supply;at least one heat exchanger that exchanges heat between the refrigerant stream and the natural gas stream to at least partially vaporize the refrigerant stream and at least partially condense the natural gas stream;a natural gas compressor that compresses the natural gas stream to a pressure of at least to 135 bara to form a compressed natural gas stream;a natural gas cooler that cools the compressed natural gas stream after being compressed by the natural gas compressor; anda natural gas expander that expands the compressed natural gas to a pressure less than 200 bara, but no greater than the pressure to which the natural gas compressor compresses the natural gas stream, after being cooled by the natural gas cooler;wherein the natural gas expander is connected to the at least one heat exchanger to supply natural gas thereto.2. The liquefied natural gas production system of claim 1 , wherein the natural gas compressor compresses the natural gas stream to a pressure greater than 200 bara.3. The liquefied natural gas production system of claim 1 , wherein the natural gas expander expands the compressed natural gas stream to a pressure less than 135 bara.4. The liquefied natural gas production system of claim 1 , wherein the at least one heat exchanger comprises a first heat exchanger claim 1 , and further comprising a second heat exchanger that cools the natural gas stream prior to the natural gas stream being compressed in the natural gas compressor.5. The liquefied natural gas production system of claim 4 , wherein the ...

METHODS AND SYSTEMS FOR TREATING FUEL GAS

Methods and systems for treating a compressed gas stream. The compressed gas stream is cooled and liquids are removed therefrom to form a dry gas stream, which is chilled in a first heat exchanger. Liquids are separated therefrom, thereby producing a cold vapor stream and a liquids stream. A first part of the cold vapor stream is expanded to produce a cold two-phase fluid stream, and a second part of the cold vapor stream is cooled to form a cooled reflux stream. Various streams are fed into a separation column to produce a cold fuel gas stream and a low temperature liquids stream. The second part of the cold vapor stream is cooled by the cold fuel gas stream, which becomes a warmed fuel gas stream that is compressed and used with the low-temperature liquids stream to chill the dry gas stream and to cool the compressed gas stream. 1. A method for treating a compressed gas stream , comprising:cooling the compressed gas stream to form a cool compressed gas stream;removing liquids from the cool compressed gas stream to form an overhead vapor stream;dehydrating the overhead vapor stream to form a dry gas stream;chilling the dry gas stream in a first heat exchanger to produce a dry cold fluid stream;separating liquids from the dry cold fluid stream, thereby producing a cold vapor stream and a liquids stream;expanding a first part of the cold vapor stream in a turbo-expander to produce a cold two-phase fluid stream;cooling a second part of the cold vapor stream in a reflux heat exchanger to form a cooled reflux stream;feeding the liquids stream, the cold two-phase fluid stream, and the cooled reflux stream into a separation column to produce a cold fuel gas stream and a low temperature liquids stream;using the cold fuel gas stream to cool the second part of the cold vapor stream in the reflux heat exchanger, the cold fuel gas stream becoming a warmed fuel gas stream;compressing the warmed fuel gas stream in a compressor to form a compressed cold fuel gas stream;using the ...

ALKALINITY CONTROL AGENT SUPPLY METHOD AND APPARATUS FOR COMPRESSOR IMPURITY SEPARATION MECHANISM

Exhaust gas from which impurities have been removed through pressurization and cooling by a compressor-based impurity separation mechanism is further cooled by a refrigerator-type heat exchanger. Drain produced from the cooling by the refrigerator-type heat exchanger is discharged and supplied as an alkalinity control agent to at least upstream of an aftercooler in a first impurity separator.

METHOD OF SEPARATING COMPONENTS OF A GAS

The disclosure provides a method for separating components of a gas. A feed gas stream is cooled in a first vessel. The feed gas stream includes methane, water, carbon dioxide, and Natural Gas Liquids. The feed gas stream is cooled in a first vessel. A portion of the water condenses to form a primary liquid stream, resulting in a first depleted gas stream, which is cooled in a second vessel. A portion of the NGLs condense to form a secondary liquid stream, resulting in a second depleted gas stream, which is cooled in a condensing exchanger. A first portion of the methane condenses to form a liquid methane stream, resulting in a third depleted gas stream, which is cooled in a third vessel. A portion of the carbon dioxide condenses, desublimates, or condenses and desublimates as a final product stream, also resulting in a fourth depleted gas stream. 1. A method for separating components of a gas comprising:cooling a feed gas stream in a first vessel, wherein the feed gas stream comprises methane, water, carbon dioxide, and NGLs, such that a portion of the water condenses to form a primary liquid stream, resulting in a first depleted gas stream;cooling the first depleted gas stream in a second vessel such that a first portion of the NGLs condense to form a secondary liquid stream, resulting in a second depleted gas stream;cooling the second depleted gas stream in a condensing exchanger such that a first portion of the methane condenses to form a liquid methane stream, resulting in a third depleted gas stream; andcooling the third depleted gas stream in a third vessel such that a first portion of the carbon dioxide condenses, desublimates, or condenses and desublimates as a final product stream, resulting in a fourth depleted gas stream.2. The method of claim 1 , wherein cooling the second depleted gas stream condenses a second portion of the carbon dioxide into the first liquid methane stream.3. The method of claim 1 , wherein the NGLs comprise compounds selected from ...

Method for separating components of a gas

A method is disclosed for separating components of a gas. A feed gas stream is cooled in the first vessel. The feed gas stream comprises methane, carbon dioxide, and a secondary component. A first portion of the secondary component condenses, desublimates, or a combination thereof to form a primary stream, resulting in a first depleted gas stream. The first depleted gas stream is cooled in a condensing exchanger such that a first portion of the methane condenses as a first liquid methane stream, resulting in a second depleted gas stream. The second depleted gas stream is cooled in the second vessel such that a first portion of the carbon dioxide desublimates to form a solid product stream, resulting in a third depleted gas stream.

Method of separating components of a gas

A method is disclosed for separating components of a gas. A feed gas stream is passed into a vessel. The feed gas stream includes methane, carbon dioxide, and water. The feed gas stream is cooled in the vessel such that a portion of the methane and a portion of the carbon dioxide condense and a portion of the water desublimates, resulting in a product stream and a depleted gas stream exiting the vessel.

METHOD FOR RECOVERING HELIUM

A method for recovering a helium product fraction () from a nitrogen- and helium-containing feed fraction () is described, wherein the nitrogen- and helium-containing feed fraction () is partially condensed (E), separated into a first helium-enriched fraction () and a first nitrogen-enriched fraction () and the former is cleaned again in an adsorptive manner. 2. The method according to claim 1 , characterized in that the third nitrogen-enriched fraction is at least partially work-performing expanded.3. The method according to claim 1 , characterized in that the separation column is operated under a pressure of 7 to 20 bar.4. The method according to claim 1 , characterized in that the third nitrogen-enriched fraction contains at least 50% of the nitrogen contained in the first nitrogen-enriched fraction.5. The method according to claim 1 , characterized in that at least a sub-flow of the second nitrogen-enriched fraction is evaporated against the nitrogen- and helium-containing feed fraction to be partially condensed under a pressure of less than 3 bar.6. The method according to claim 1 , characterized in that the adsorptive cleaning process is a (V)PSA and/or TSA process.7. The method according to claim 3 , characterized in that the separation column is operated under a pressure of 10 to 15 bar. The invention relates to a method for recovering a helium product fraction from a nitrogen- and helium-containing feed fraction, whereinThe term “helium product fraction” be comprised of highly purified helium, the concentration and contamination of which do not exceed a value of 100 vppm, preferably of 10 vppm.The term “nitrogen- and helium-containing feed fraction” be understood as a fraction, which contains 1 to 20 mol-% helium and 80 to 99 mol-% nitrogen. Further, this feed fraction can contain 0.1 to 2 mol-% methane and traces of hydrogen, argon and/or other noble gases.Currently, helium is obtained almost exclusively from a mixture of volatile natural gas components, ...

Heavy Hydrocarbon Removal System for Lean Natural Gas Liquefaction

A system and method for integrated heavy hydrocarbon removal in a liquefaction system having a lean natural gas source. An economizer located between a main cryogenic heat exchanger and a reflux drum is provided to cool an overhead vapor stream against a partially condensed stream. In addition, pressure of the natural gas feed stream is maintained into a scrub column. A pressure drop is provided by a valve located between the economizer and the reflux drum on a partially condensed stream withdrawn from the cold end of the warm section of the main cryogenic heat exchanger.

Cryogenic System for Removing Acid Gases from a Hydrocarbon Gas Stream

A system for removing acid gases from a raw gas stream is provided. The system includes a cryogenic distillation tower. The cryogenic distillation tower has a controlled freezing zone that receives a cold liquid spray comprised primarily of methane. The tower receives and then separates the raw gas stream into an overhead methane gas stream and a substantially solid material comprised on carbon dioxide. The system includes a collector tray below the controlled freezing zone. The collector tray receives the substantially solid material as it is precipitated in the controlled freezing zone. The system also has a filter. The filter receives the substantially solid material and then separates it into a solid material comprised primarily of carbon dioxide, and a liquid material comprising methane. The solid material may be warmed as a liquid and sold, while the liquid material is returned to the cryogenic distillation tower. 1. A system for removing acid gases from a raw gas stream , comprising:a cryogenic distillation tower, the tower having a controlled freezing zone that receives a cold liquid spray comprised primarily of methane, the tower receiving and then separating the raw gas stream into an overhead methane gas stream and a substantially solid material comprised of precipitated carbon dioxide;refrigeration equipment downstream of the cryogenic distillation tower for cooling the overhead methane stream and returning a portion of the overhead methane stream to the cryogenic distillation tower as the cold liquid spray;a collector tray below the controlled freezing zone for receiving the substantially solid material as it is precipitated in the controlled freezing zone and directing the substantially solid material out of the cryogenic distillation tower;a first filter for receiving the substantially solid material from the cryogenic distillation tower and separating the substantially solid material into a solid component comprised primarily of carbon dioxide, and a ...

Recovery Of Helium From Nitrogen-Rich Streams

Overall power consumption in a cryogenic distillation process for recovering helium from nitrogen-rich gases comprising helium may be reduced if the feed to the distillation column system is at least substantially condensed by indirect heat exchange against a first bottoms liquid at first pressure, and a second bottoms liquid at a second pressure that is different from the first pressure. 1. Apparatus for recovering helium from a nitrogen-rich feed gas comprising helium , said apparatus comprising:a distillation column system for operation at an elevated operating pressure to separate at least partially condensed feed gas into helium-enriched overhead vapor and nitrogen-enriched bottoms liquid(s);an overhead condenser for partially condensing helium-enriched overhead vapor by indirect heat exchange to produce helium-enriched vapor as product and liquid for reflux in the column system;a first heat exchange system for cooling feed gas by indirect heat exchange with a first nitrogen-enriched bottoms liquid to produce cooled feed gas and vapor for the column system;a first pressure reduction device for reducing the pressure of a second nitrogen-enriched bottoms liquid to produce reduced pressure bottoms liquid;a second heat exchange system for cooling said cooled feed gas by indirect heat exchange against said reduced pressure bottoms liquid to produce at least partially condensed feed gas and vaporized bottoms liquid; anda second pressure reduction device for reducing the pressure of said at least partially condensed feed gas to produce at least partially condensed feed gas at reduced pressure for use as said feed to the distillation column system.2. The apparatus of comprising a third pressure reduction device for reducing the pressure of a third nitrogen-enriched bottoms liquid to produce reduced pressure bottoms liquid for vaporization by indirect heat exchange in said overhead condenser to produce nitrogen-enriched vapor.3. The apparatus of comprising an expander ...

Method for purifying, cooling and separating a gaseous mixture and associated apparatus

The invention relates to a method for cooling, purifying and separating a gaseous mixture containing at least one impurity, in which the gaseous mixture is cooled to a temperature no higher than the temperature at which the at least one impurity solidifies in a heat exchanger having cooling passages, the cooling passages being at least partially covered with a coating and/or physically treated and/or chemically treated, the coating and/or the treatment serving to limit or even prevent the solidified impurity from forming and/or adhering to a surface of the passages; at least one portion of the solidified impurity exiting the cooling passages of the heat exchanger is collected; and the gaseous mixture is withdrawn from the heat exchanger.

PROCESS FOR OPTIMIZING REMOVAL OF CONDENSABLE COMPONENTS FROM A FLUID

A method for removing condensable components from a fluid containing condensable components. The method involves optimizing the temperature of an initial feed stream including the condensable components through heat exchange and cooling to condense liquids there from. The liquids are removed to form a gas stream which is then compressed and after-cooled to form a high pressure stream. A portion of the high pressure stream is expanded to form a cooled low pressure stream which is mixed with the initial feed stream to augment cooling and condensation of condensable components in the initial feed stream. 1. A method for removing condensable components from a fluid containing said condensable components , comprising:cooling an initial feed stream including said condensable components by heat exchange to condense liquids there from and removing said liquids to form a gas stream;compressing and after-cooling the gas stream to form a high pressure stream;expanding at least a portion of the high pressure stream to form a cooled low pressure stream;mixing with said cooled low pressure stream and said initial feed stream to augment cooling and condensation of condensable components to form a mixture;separating said mixture into a liquid stream and a gas stream;contacting the separated liquid stream and the separated gas stream with said initial feed stream for heat exchange through a gas-liquid heat exchange operation in sequence with a gas-gas heat exchange operation or absent gas-liquid heat exchange where hydrocarbon recovery is unfeasible;manipulating the composition of all streams during said method to prevent hydrate formation; andrecovering any hydrocarbons.2. The method as set forth in claim 1 , including the step of determining the hydrocarbon and water content of said initial fuel stream.3. The method as set forth in or claim 1 , further including the step of operating the method at a temperature range outside that where hydrates form.4. The method as set forth in ...

LIQUID NATURAL GAS PROCESSING WITH HYDROGEN PRODUCTION

Devices, systems, and methods for liquefied natural gas production facilities are disclosed herein. A liquefied natural gas (LNG) production facility includes a liquefaction unit that condenses natural gas vapor into liquefied natural gas; an electric-driven compression system for the refrigerant(s) in power to the liquefaction unit; and a sequestration compression unit configured to compress and convey at least one CO2-rich stream towards a sequestration site, thereby reducing the overall emissions from the LNG facility. 1. A liquefied natural gas (LNG) facility comprising:an acid gas removal unit configured to process a feed natural gas and generate an acid gas stream, a flash gas stream, and a purified natural gas stream, the LNG facility being configured to direct the acid gas stream to a sequestration compression unit;a liquefaction unit configured to condense a natural gas stream into an LNG; andthe sequestration compression unit configured to compress a CO2-rich stream and convey the compressed CO2-rich stream towards a sequestration site, the CO2-rich stream comprising the acid gas stream.2. The LNG facility of claim 1 , wherein the CO2-rich stream further comprises the flash gas stream.3. The LNG facility of claim 1 , wherein the sequestration compression unit comprises a compressor selected from the group consisting of an electric-driven compressor claim 1 , and electrically driven refrigerant compressor claim 1 , and combinations thereof.4. The LNG facility of claim 1 , wherein the sequestration site is selected from the group consisting ofan underground geological formation comprising an at least partially depleted hydrocarbon reservoir,a region on top of a seabed and located at a depth greater than about 3.0 kilometers below a sea level,a region below a seabed, andcombinations thereof.5. The LNG facility of claim 1 , wherein the acid gas removal unit comprises at least one of (i) an amine absorber and a liquid amine absorbent for absorbing CO2 from the ...

FRACTIONATION SYSTEM AND METHOD INCLUDING DEPROPANIZER COLUMN AND BOTTOMS STRIPPING COLUMN

Fractionation systems utilizing a rectifying column with a stripping column are described. The liquid from the rectifying column bottoms is sent to the first tray of the stripping column, while the overhead stream from the stripping column is sent to the bottom of the rectifying column. Processes for separating feed streams are also described. 1. A fractionation system comprising:a rectifying column having a feed inlet between a top and a bottom tray, a reflux inlet at the top tray, a fluid inlet at the bottom tray, an overhead product outlet at the first tray, and a bottoms outlet at the bottom tray;a rectifying column reboiler in communication with the rectifying column;a stripping column having a fluid inlet at a top tray, an overhead outlet at the top tray, and a bottoms outlet at a bottom tray, the bottoms outlet of the rectifying column being in fluid communication with the fluid inlet of the stripping column, the overhead outlet of the stripping column being in fluid communication with the fluid inlet of the rectifying column; anda stripping column reboiler in communication with the stripping column.2. The fractionation system of wherein the rectifying column and the stripping column are in separate vessels.3. The fractionation system of wherein the rectifying column and the stripping column are in a single vessel claim 1 , the rectifying column being positioned above the stripping column claim 1 , the rectifying column having a diameter claim 1 , and the stripping column having a diameter less than the diameter of the rectifying column.4. The fractionation system of wherein the rectifying column is separated from the stripping column by a liquid accumulator tray.5. The fractionation system of further comprising a condenser having an inlet in fluid communication with the product overhead outlet of the rectifying column claim 1 , and an outlet in fluid communication with the reflux inlet of the rectifying column.6. The fractionation system of wherein at least ...

FRACTIONATION SYSTEM HAVING RECTIFYING AND STRIPPING COLUMNS IN A SINGLE VESSEL WITH A UNIFORM DIAMETER

Fractionation systems utilizing a single rectifying column with a stripping column housed in the same vessel and having a uniform diameter are described. Methods of separating feed streams using the fractionation systems are also described. 1. A fractionation system comprising:a rectifying column having a feed inlet between a top and a bottom plate, a reflux inlet at the top plate, a fluid inlet at the bottom plate, an overhead product outlet at the first plate, and a bottoms outlet at the bottom plate;a rectifying column side reboiler in communication with the rectifying column;a stripping column having a fluid inlet at a top plate, an overhead outlet at the top plate, and a bottoms outlet at the bottom plate, the bottoms outlet of the rectifying column being in fluid communication with the fluid inlet of the stripping column, the overhead outlet of the stripping column being in fluid communication with the fluid inlet of the rectifying column;a stripping column reboiler in communication with the stripping column; andthe rectifying column and the stripping column being in a single vessel having a uniform diameter, the rectifying column being positioned above the stripping column.2. The fractionation system of wherein the rectifying column includes a plurality of high performance trays.3. The fractionation system of wherein the stripping column comprises a side-by-side stacked arrangement of fractionation trays claim 1 , wherein the bottom of the first stack is in liquid communication with the top of the second stack and wherein the top of the second stack is in vapor communication with the bottom of the first stack.4. The fractionation system of wherein there is a blind tray at the top of the second stack to prevent direct liquid and vapor communication between the second stack and the rectifying column.5. The fractionation system of wherein the vapor communication is provided by a vapor channel from the top of the second stack to the bottom of the first stack.6. ...

PROCESS AND APPARATUS FOR SEPARATION OF HYDROCARBONS AND NITROGEN

There is provided a process for the separation of a gaseous feed comprising a mixture of nitrogen, hydrocarbons and at least 0.005 mol % carbon dioxide, the process comprising: (i) cooling and at least partially condensing the gaseous feed, and (ii) separating in one or more stages the cooled and at least partially condensed gaseous feed into a hydrocarbon rich product stream low in nitrogen and a nitrogen rich reject stream low in hydrocarbons, and wherein refrigeration is provided to one or more stages of the separation process by a heat pump system in which a heat pump refrigerant fluid is compressed and subsequently expanded at one or more pressure levels below the condensing pressure, and subsequently heated in heat exchange with the gaseous feed and/or one or more streams generated by the separation process to provide refrigeration thereto; and further wherein at least part of the heated refrigerant is recycled through the heat pump system. There is also provided an apparatus for the separation of a gaseous feed comprising a mixture of nitrogen, hydrocarbons and at least 0.005 mol % carbon dioxide. 2. A process according to claim 1 , wherein the hydrocarbons in the gaseous feed comprise or consist of methane.3. A process according to claim 1 , wherein the gaseous feed comprises or consists of natural gas.4. A process according to any preceding claim claim 1 , wherein the gaseous feed comprises less than 35 mol % nitrogen gas.5. A process according to any preceding claim claim 1 , wherein the gaseous feed comprises from 5 mol % to 25 mol % nitrogen gas.6. A process according to any preceding claim claim 1 , wherein the gaseous feed comprises from 0.01 mol % to 4.0 mol % carbon dioxide.7. A process according to any preceding claim claim 1 , wherein the heat pump refrigerant fluid comprises less than 0.02 mol % carbon dioxide.8. A process according to any preceding claim claim 1 , wherein claim 1 , after expansion claim 1 , the heat pump refrigerant is at a ...

Facility For Producing Gaseous Methane By Purifying Biogas From Landfill, Combining Membranes And Cryogenic Distillation For Landfill Biogas Upgrading

A process and facility for producing gaseous methane by purifying biogas from landfill, can include a VOC purification unit, at least one membrane, a booster, a COpurification unit, a cryodistillation unit comprising a heat exchanger, a distillation column, and a subcooler, a deoxo, and a dryer. 1a compression unit for compressing an initial gas flow of the biogas to be purified,a VOC purification unit arranged downstream of the compression unit to receive the compressed initial flow of the biogas and comprising at least one adsorber loaded with adsorbents capable of reversibly adsorbing VOCs to thereby produce a VOC-depleted gas flow;at least one membrane arranged downstream of the VOC purification unit to receive the VOC-depleted gas flow and subject the VOC-depleted gas flow to at least one membrane separation to thereby produce a retentate;a booster arranged downstream of the membrane unit to receive the retentate from the membrane capable of increasing the pressure of the retentate to produce a pressurized retentate;{'sub': 2', '2', '2', '2, 'a COpurification unit arranged downstream of the booster to receive the pressurized retentate, wherein the COpurification unit comprises at least one adsorber loaded with adsorbents capable of reversibly adsorbing the majority of remaining COfrom the pressurized retentate to produce a CO-depleted gas flow;'}{'sub': 2', '2', '2', '2', '2', '2, 'a cryodistillation unit comprising a heat exchanger, a distillation column, and a subcooler, the cryodistillation unit arranged downstream of the COpurification unit to receive the CO-depleted gas flow and subject the CO-depleted gas flow to a cryogenic separation to separate Oand Nfrom the CO-depleted gas flow capable and to produce 2 methane enriched flows respectively a low pressure (LP) and a medium pressure (MP) methane enriched flows;'}a compressor compressing the low pressure methane enriched flow, in order to mix it with the medium pressure methane enriched flow, to produce a ...

PROCESS AND APPARATUS FOR PRODUCING CARBON MONOXIDE

The present invention relates to a cold box cycle which allows for independent control of the heat supplied for reboilers associated with the separation columns. More specifically, the invention relates to the tight control of the hydrogen removal separation, thus avoiding the possibility of excess reboiling in this separation. Optimal reboiling also results in a lower temperature of the hydrogen depleted liquid from this separation. As this stream is used to provide a portion of the cooling at the cold end of the primary heat exchanger, lower temperatures facilitate cooling of the incoming syngas feed, reducing carbon monoxide (CO) losses into the crude hydrogen stream from the high pressure separator. Lower CO in the crude hydrogen allows for smaller hydrogen purification equipment. 1. A method for the separation of carbon monoxide and hydrogen from a syngas feedstock , comprising:cooling and partially condensing the syngas feedstock containing carbon monoxide and hydrogen in a primary heat exchanger to produce a cooled and partially condensed syngas feed stream;separating the cooled and partially condensed syngas feed stream in a first hydrogen rich vapor stream and a first carbon monoxide rich liquid stream in a high pressure separator;feeding the first carbon monoxide rich liquid stream to a hydrogen removal column operating at a pressure lower than the high pressure separator, wherein a second hydrogen rich vapor stream is separated from a second carbon monoxide rich stream;splitting said second carbon monoxide rich stream into two portions wherein a first portion of the second carbon monoxide rich stream is at least partially vaporized in the primary heat exchanger and providing a second portion of the second carbon monoxide rich stream wherein both portions are introduced into a carbon monoxide/methane column for separating purified carbon monoxide vapor stream from a methane rich liquid stream;separating a portion of the cooled syngas feedstock to provide ...

Scrubber System With Moving Adsorbent Bed

A regenerative carbon dioxide removal system () is provided onboard the container () through which air from within the cargo box () may be circulated for removing at least a portion of the carbon dioxide present in the air. The regenerative carbon dioxide removal system () includes a scrubber module () containing a carbon dioxide absorbent material (), and an actuator () for moving the scrubber module () to pass the carbon dioxide absorbent material () alternately between a first flow of air () to be cleaned drawn by the evaporator fan () from within the cargo box (), and a second flow of air () drawn from an environment outside the cargo box for regenerating the carbon dioxide adsorbent material () by removing collected carbon dioxide from the carbon dioxide adsorbent material (). 1. A regenerative scrubber system for removing carbon dioxide from the atmosphere within a cargo box of a refrigerated transport container equipped with a refrigeration unit having an evaporator heat exchanger and an associated fan disposed in air flow communication with the cargo box , the regenerative scrubber system comprising:a scrubber module containing a carbon dioxide adsorbent material; andan actuator for moving the scrubber module to pass the carbon dioxide adsorbent material alternately between a first flow of air drawn by the evaporator fan from within the cargo box and a second flow of air from an environment outside the cargo box.2. The regenerative scrubber system as set forth in wherein the actuator comprises a rotary actuator for rotating the scrubber module about an axis of rotation through the first flow of air and the second flow of air in sequence.3. The regenerative scrubber system as set forth in wherein the scrubber module is mounted in a partition panel separating a condenser module of the refrigeration unit from an evaporator module of the refrigeration unit; and the actuator rotates the scrubber module through the evaporator module and the condenser module.4. The ...

Flare Recovery with Carbon Capture

A flare recovery method includes receiving a flare gas inlet stream that has C-Chydrocarbons. The flare gas inlet stream is separated in a recovery column to produce a C-Chydrocarbon stream and a C-Chydrocarbon stream. The C-Chydrocarbon stream is separated in a separation column to produce a Chydrocarbon stream and a C-Chydrocarbon stream. The C-Chydrocarbon stream is transported to a location for blending with crude oil. The Chydrocarbon stream is optionally recovered as a saleable product or is combined with the C-Chydrocarbon stream to produce a flare gas stream. 157-. (canceled)58. A method for flare recovery , comprising:{'sub': 1', '8, 'receiving a gas inlet stream, the gas inlet stream comprising C-Chydrocarbons;'}{'sub': 1', '2', '3', '8, 'separating the gas inlet stream in a recovery column to produce a C-Chydrocarbon stream and a C-Chydrocarbon stream;'}{'sub': 3', '8', '3', '4', '8, 'separating the C-Chydrocarbon stream in a separation column to produce a Chydrocarbon stream and a C-Chydrocarbon stream;'}{'sub': '3', 'recovering the Chydrocarbon stream; and'}{'sub': 4', '8', '9+, 'combining the C-Chydrocarbon stream with a C hydrocarbon stream.'}59. The method of claim 58 , wherein the gas inlet stream comprises 96-100 mole % C-Chydrocarbons claim 58 , 0-2 mole % carbon dioxide claim 58 , and 0-2 mole % nitrogen claim 58 , the C-Chydrocarbon stream comprises 80 mole % C-Chydrocarbons claim 58 , 10-20 mole % Chydrocarbons claim 58 , 0-2 mole % C-Chydrocarbons claim 58 , 0-2 mole % carbon dioxide claim 58 , and 0-2 mole % nitrogen claim 58 , the C-Chydrocarbon stream comprises 5-15 mole % C-Chydrocarbons claim 58 , 85-95 mole % C-Chydrocarbons claim 58 , and 0-2 mole % carbon dioxide claim 58 , the Chydrocarbon stream comprises 30-40 mole % C-Chydrocarbons claim 58 , 60-70 mole % Chydrocarbons claim 58 , 0-2 mole % C-Chydrocarbons claim 58 , and 0-2 mole % carbon dioxide claim 58 , and the C-Chydrocarbon stream comprises 0 mole % C-Chydrocarbons claim 58 , ...

Separation of Components from a Fluid by Solids Production

A method for separating components from a fluid is disclosed. A cooling element is provided and is disposed in contact with a distal side of one or more thermally-conductive surfaces. One or more resistive heating elements are provided and are disposed in contact with or embedded in a proximal side of the one or more thermally-conductive surfaces. A fluid comprising one or more secondary components is provided. The fluid is passed across the one or more thermally conductive surfaces, the one or more secondary components freezing, crystallizing, desublimating, depositing, condensing, or combinations thereof, out of the fluid. The one or more resistive heating elements engage such that the one or more solid secondary components detach and pass out the solids outlet. The one or more resistive heating elements disengage, restarting production of the one or more solid secondary components. 1. A method for separating components from a fluid comprising:providing a cooling element, one or more resistive heating elements, a fluid inlet, one or more thermally-conductive surfaces, a fluid outlet, and a solids outlet;providing the cooling element disposed in contact with a distal side of the one or more thermally-conductive surfaces, the cooling element cooling the one or more thermally-conductive surfaces;providing the one or more resistive heating elements disposed in contact with or embedded in a proximal side of the one or more thermally-conductive surfaces;providing a fluid comprising one or more secondary components dissolved, entrained, suspended, absorbed, condensed, or combinations thereof, wherein the fluid freezes at a lower temperature than the one or more secondary components, wherein the fluid is passed across the one or more thermally conductive surfaces, at least a portion of the one or more secondary components freezing, crystalizing, desublimating, depositing, condensing, or combinations thereof, out of the fluid as one or more solid secondary components, ...

METHOD OF LIQUEFYING A CONTAMINATED HYDROCARBON-CONTAINING GAS STREAM

A method of liquefying a contaminated hydrocarbon-containing gas stream includes cooling the stream in a first heat exchanger and cooling the cooled stream in an expander to obtain a partially liquefied stream. The method further includes separating the partially liquefied stream in a separator to obtain a gaseous stream and a liquid stream. The liquid stream is expanded to obtain a multiphase stream containing at least a vapour phase, a liquid phase and a solid phase. The multiphase stream is separated in a separator to obtain a gaseous stream and a slurry stream. The slurry stream is separated in a solid/liquid separator to obtain a liquid hydrocarbon stream and a concentrated slurry stream. The gaseous stream is passed through the first heat exchanger to obtain a heated gaseous stream. The heated gaseous stream is compressed and combined with the contaminated hydrocarbon-containing gas stream. 1. A method of liquefying a contaminated hydrocarbon-containing gas stream , the method comprising at least the steps of:(a) providing a contaminated hydrocarbon-containing gas stream;(b) cooling the contaminated hydrocarbon-containing gas stream in a first heat exchanger thereby obtaining a cooled contaminated hydrocarbon-containing stream;(c) cooling the cooled contaminated hydrocarbon-containing stream in an expander thereby obtaining a partially liquefied stream;(d) separating the partially liquefied stream in a separator thereby obtaining a gaseous stream and a liquid stream;(e) expanding the liquid steam obtained in step thereby obtaining a multiphase stream, the multiphase stream containing at least a vapour phase, a liquid phase and a solid phase;(f) separating the multiphase stream in a separator thereby obtaining a gaseous stream and a slurry stream;(g) separating the slurry stream in a solid/liquid separator thereby obtaining a liquid hydrocarbon stream and a concentrated slurry stream;(h) passing the gaseous stream obtained in step (d) through the first heat ...

Onsite Ultra High Purity Chemicals or Gas Purification

An onsite purification plant/system to delivery high and ultra high purity product, such as, process chemicals, industrial and specialty gases to manufacturing processes within the onsite plant turndown ratio from 0% to 100% while preserving the predetermined purity of the supplied substances within a predefined specification range is provided. Preserving liquid/vapor ratio in at least one of the purification means/units ensuring that product purity range stays unchanged is achieved by redirecting the product back into the onsite purification plant/system. 1. An onsite purification system comprising:1) a feed stream comprising of a chemical or gas being purified;2) at least two purification units for receiving and purifying the feed stream;3) at least one purified stream out from the at least two purification units;4) an automatic stream control system for receiving the at least one purified stream; wherein the at least one automatic stream control system comprising:an output product junction and a feedback junction;5) at least one product stream out from the output product junction; and6) at least one feedback stream out from the feedback junction and back into the at least two purification units.2. The onsite purification system of claim 1 , wherein the feed stream is an industrial grade purity product having a purity of <98%; and the at least one product stream is an industrial grade purity product having a purity of >99.5%.3. The onsite purification system of claim 1 , wherein the chemical or gas being purified is selected from the group consisting of NH claim 1 , HCl claim 1 , Cl claim 1 , NF claim 1 , O claim 1 , N claim 1 , CO claim 1 , and combinations thereof.4. The onsite purification system of claim 1 , wherein the chemical or gas being purified is NH.5. The onsite purification system of claim 1 , wherein each of the at least two purification units is independently selected from the group consisting of filter claim 1 , absorption bed claim 1 , ...

PRETREATMENT OF NATURAL GAS PRIOR TO LIQUEFACTION

Method and system for removing high freeze point components from natural gas. Feed gas is cooled in a heat exchanger and separated into a first vapor portion and a first liquid portion. The first liquid portion is reheated using the heat exchanger and separated into a high freeze point components stream and a non-freezing components stream. A portion of the non-freezing components stream may be at least partially liquefied and received by an absorber tower. The first vapor portion may be cooled and received by the absorber tower. An overhead vapor product which is substantially free of high freeze point freeze components and a bottoms product liquid stream including freeze components and non-freeze components are produced using the absorber tower. 1. A method for removing high freeze point components from natural gas , comprising:cooling a feed gas in a heat exchanger;separating the feed gas into a first vapor portion and a first liquid portion in a separation vessel;reheating the first liquid portion using the heat exchanger;separating the reheated first liquid portion into a high freeze point components stream and a non-freezing components stream;at least partially liquefying the non-freezing components stream;receiving, at an upper feed point of an absorber tower, the at least partially liquefied non-freezing component stream;receiving, at a lower feed point of the absorber tower, the first vapor portion of the separated feed gas that has been cooled;producing, using the absorber tower, an overhead vapor product which is substantially free of high freeze point freeze components and a bottoms product liquid stream including freeze components and non-freeze components; andreheating the overhead vapor product from the absorber tower using the heat exchanger.2. The method of claim 1 , wherein the absorber tower includes one or more mass transfer stages.3. The method of claim 1 , further comprising compressing the reheated overhead vapor product using an expander- ...

PROCESS AND APPARATUS FOR REMOVING HEAT AND WATER FROM FLUE GAS

Disclosed is a process for use with flue gas having a moisture content M. The flue gas is introduced to strong brine adapted to exothermically absorb moisture. Simultaneously, heat is withdrawn. This produces heat, water-enriched brine and a gas having a moisture concentration less than M. The strong brine can be recovered by distillation from enriched brine to produce water. The brine temperature throughout absorption can remain within 2° F. of a temperature T in the range 220° F.-300° F. The heat withdrawal can be associated with gas-liquid phase change of a working fluid. The terminus of the heat flow can be associated with gas-liquid phase change of the working fluid. The working fluid can: as liquid, flow only by gravity, convection or wicking; and, as gas, flow only by diffusion or convection. The heat flow can drive a boiler producing steam. M can be greater than 15 wt. % water. 1. A process for use with a flue gas having a moisture content M , the process comprising the steps of: introducing said flue gas to a flow of strong brine adapted to exothermically absorb moisture from the flue gas to produce heat; and', 'withdrawing heat,, 'i. simultaneously'}thereby to produce a flow of heat, a flow of water-enriched brine and a gas having a moisture concentration less than M; andii. recovering the strong brine from the water-enriched brine to produce a flow of water,characterized in thata. the temperature of the brine throughout the absorption step remains within 2° F. of a temperature T that lies in the range 220° F.-300° F.; and/orb. the withdrawal of heat is associated with the phase change of a working fluid from the liquid state to a gaseous state; the terminus of the heat flow is associated with the phase change of the working fluid from the gaseous state to the liquid state; in the liquid state, the working fluid flows only by one or more of gravity, convection and wicking; and in the gaseous state, the working fluid flows only by one or more of diffusion ...

METHOD OF COOLING A NATURAL GAS FEED STREAM AND RECOVERING A NATURAL GAS LIQUID STREAM FROM THE NATURAL GAS FEED STREAM

The invention relates to a method and system for cooling a natural gas feed stream and recovering a natural gas liquid stream from the natural gas feed stream using an expansion-based cooling unit and a natural gas liquid removal unit which are integrated. The integration is done by using (part of) a cooling stream from the expansion-based cooling unit to provide cooling duty to the natural gas liquid removal unit. 1. A method of cooling a natural gas feed stream and recovering a natural gas liquid stream from the natural gas feed stream , the method comprising:a) operating an expansion based cooling unit, comprising obtaining a cooling stream being derived from the natural gas feed stream,{'sub': '5', 'sup': '+', 'claim-text': {'sub': '5', 'sup': '+', 'wherein the method comprises cooling the C depleted top stream in an overhead condenser against at least part of the cooling stream.'}, 'b) operating a natural gas liquid removal unit, comprising passing a feed stream being derived from the natural gas feed stream to a separation unit and obtaining a C depleted top stream from the separation unit,'}2. The method according to comprising: a1) obtaining a compressed process stream and a cooling stream from a pressure unit, both the compressed process stream and the cooling stream being derived from the natural gas feed stream,', 'a2) passing the compressed process stream and at least part of the cooling stream to an indirect heat exchanger to cool the compressed process stream against the at least part of the cooling stream to obtain a cooled compressed process stream and a warmed cooling stream,', 'a3) recycling the warmed cooling stream to the pressure unit to be comprised in the compressed process stream and/or the cooling stream,, 'a) operating an expansion based cooling unit, comprising'} [{'sub': '5', 'sup': '+', 'b1) passing a feed stream being derived from the natural gas feed stream to a separation unit and obtaining the natural gas liquid stream from a lower ...

PURIFICATION OF ARGON THROUGH LIQUID PHASE CRYOGENIC ADSORPTION

The invention relates to a process for removing oxygen from liquid argon using a TSA (temperature swing adsorption) cyclical process that includes cooling an adsorbent bed to sustain argon in a liquid phase; supplying the adsorbent bed with a liquid argon feed that is contaminated with oxygen and purifying the liquid argon thereby producing an argon product with less oxygen contaminant than is in the initial liquid argon feed; draining the purified residual liquid argon product and sending purified argon out of the adsorbent bed. Regeneration of specially prepared adsorbent allows the adsorbent bed to warm up to temperatures that preclude the use of requiring either vacuum or evacuation of adsorbent from the bed. 1. An adsorption process for purifying a feed stream containing primarily liquid argon and oxygen , comprising the following cycle of process steps:a) supplying from the inlet of an adsorbent bed said liquid argon feed that contains oxygen, adsorbing at least part of the oxygen on the adsorbent thereby producing a purified liquid argon product leaving said adsorbent bed from the outlet with less oxygen than present in said liquid argon feed at the inlet;b) draining from said adsorbent bed purified residual liquid argon by introducing a displacement purge gas;c) allowing said adsorbent bed containing said adsorbent to warm to a temperature, desorbing at least part of the adsorbed oxygen and removing said adsorbed oxygen from the adsorbent bed such that the liquid argon feed may be supplied for purposes of repeating the cycle;d) cooling said adsorbent bed having an inlet and an outlet and containing an adsorbent such that said adsorbent bed is cooled to a temperature below the boiling point of argon;e) wherein said process steps (a)-(d) are repeated in a cyclical manner.2. The process of claim 1 , wherein the liquid argon feed for step (a) contains more than 10 parts per million of oxygen and less or equal to 10 claim 1 ,000 parts per million of oxygen and ...

APPARATUS AND METHOD FOR PURIFYING GASES AND METHOD OF REGENERATING THE SAME

A method and device for purifying a process gas mixture, such as a cryogen gas, in which impurity components of the mixture are removed by de-sublimation via cryo-condensation. The gas mixture is cooled to a temperature well below the condensation temperature of the impurities, by direct exchange of the gas mixture with a cooling source disposed in a first region of the device. The de-sublimated or frozen impurities collect about the cooling region surfaces, and ultimately transferred to a portion of the device defining an impurities storage region. The output-purified gas is transferred from the impurities storage region, is optionally passed through a first micrometer sized filter, through a counter-flow heat exchanger, and ultimately up to an output port at room temperature. A method of purging the collected impurities and regenerating the device is also disclosed. 1. A gas purifier for removing gaseous impurities from a cryogen gas comprising:a housing having an inlet for receiving a cryogen gas to be purified and a purified gas outlet, said housing defining a hollow interior which defines a first region in an uppermost interior portion thereof and a second region in a lower interior portion thereof;a coldhead disposed in the first region and operative to contact a flow of the cryogen gas sought to be purified received through the inlet, the coldhead being operative to cool the cryogen gas to a temperature sufficient to de-sublimate at least one gaseous impurity present in the cryogen gas; anda collection mechanism coupled to the purified gas outlet, the collection mechanism being disposed within the second region and selectively positioned therein such that the cryogen gas passes therethrough and through the outlet while retaining the at least de-sublimated impurity within the interior of said housing.2. The gas purifier of wherein the second region of the interior of the housing is configured to retain the at least one de-sublimated impurity formed in the ...

Helium Extraction from Natural Gas

A crude helium stream is recovered from a natural gas feed by distillation. Refrigeration from expanding a portion of the bottoms liquid is used to partially condense the helium-enriched overhead vapor and generate a crude helium vapor and a helium-containing liquid stream that is recycled to the distillation column to maximize helium recovery. The helium-depleted natural gas stream can be returned at pressure for utilization or transportation. 1. A process for recovering helium from a natural gas feed comprising methane , nitrogen , and helium , said process comprising:cooling said natural gas feed to produce a cooled natural gas feed which is at least partially condensed;separating the cooled natural gas feed in a distillation column system to produce a helium-enriched overhead vapor and a helium-depleted bottoms liquid;cooling said helium-enriched overhead vapor to produce a partially condensed overhead stream;separating said partially condensed overhead stream in an overhead separator to produce a crude helium vapor and a recycle liquid;expanding at least a portion of the helium-depleted bottoms liquid to produce a first helium-depleted bottoms fraction;wherein cooling duty for cooling said helium-enriched overhead vapor is provided at least in part by indirect heat exchange with said first helium-depleted bottoms fraction.2. Process of wherein the pressure of said cooled natural gas feed is reduced to achieve a ratio of liquid to vapor density in the distillation column greater than 4.3. Process of wherein the pressure of said cooled natural gas feed is reduced to achieve a liquid phase surface tension in the distillation column greater than 0.5 dyne/cm.4. Process of wherein the difference between the pressure of the top of the distillation column system and the pressure of said overhead separator is no more than 1 bar.5. Process of wherein the re-boiling duty for said distillation column system is provided at least in part by indirect heat exchange with the ...

Helium Extraction from Natural Gas

A helium-containing stream is recovered from a natural gas feed using a membrane followed by multiple distillation steps. Refrigeration is provided by expanding a bottoms liquid with a higher nitrogen content than the feed, achieving a lower temperature in the process. The helium-enriched vapor is then purified and the helium-containing waste stream is recycled to maximize recovery and reduce the number of compressors needed. The helium-depleted natural gas stream can be returned at pressure for utilization or transportation.

SYSTEM AND METHOD FOR SUBSEA COOLING A WELLHEAD GAS TO PRODUCE A SINGLE PHASE DEW-POINTED GAS

A system and method for subsea cooling a wellhead gas containing components separable by dewpoint condensation to produce a single phase dew-pointed gas for pipeline transport is disclosed. The system includes a first cooling apparatus configured in use to cool the wellhead gas in direct or indirect heat exchange relation with ambient seawater to a first temperature marginally above ambient seawater temperature to condense liquids comprising one or more hydrocarbons other than methane and at least partially condense water in the wellhead gas. The system also includes a first separator to separate the condensed liquids and water from the cooled gas and a means to add a hydrate inhibitor into the separated cooled gas. The system further includes a second cooling apparatus configured to cool the separated cooled gas to a second temperature below the first temperature, wherein the second temperature is below the ambient seawater temperature to condense the remaining water and produce a single phase dew-pointed gas; and a second separator to separate the condensed remaining water from the single phase dew-pointed gas. 1. A system for subsea cooling a wellhead gas containing components separable by dewpoint condensation to produce a single phase dew-pointed gas for pipeline transport , said system comprising:a first cooling apparatus configured in use to cool the wellhead gas in direct or indirect heat exchange relation with ambient seawater to a first temperature marginally above ambient seawater temperature to condense liquids comprising one or more hydrocarbons other than methane and at least partially condense water in the wellhead gas;a first separator to separate the condensed liquids and water from the cooled gas;a means to add a hydrate inhibitor into the separated cooled gas;a second cooling apparatus configured to further cool the separated cooled gas to a second temperature below the first temperature, wherein the second temperature is below the ambient ...

Purification of Carbon Dioxide

In a process for separating at least one “heavy” impurity such as hydrogen sulfide from crude carbon dioxide comprising significant quantities of at least one “light” impurity such as non-condensable gases, involving at least one heat pump cycle using carbon dioxide-containing fluid from the process as the working fluid, the “light” impurity is removed from the crude carbon dioxide and carbon dioxide is subsequently recovered from the removed “light” impurity, thereby improving overall carbon dioxide recovery and efficiency in terms of energy consumption. 2. The process of claim 1 , wherein said recovered carbon dioxide is fed to said second column system for mass transfer separation.3. The process of claim 1 , wherein said cooled crude carbon dioxide fluid is expanded prior to being fed to said first column system.4. The process of claim 3 , wherein said cooled crude carbon dioxide fluid is below the critical pressure of carbon dioxide prior to expansion.5. The process of claim 3 , wherein said cooled crude carbon dioxide fluid is above the critical pressure of carbon dioxide prior to expansion.6. The process of claim 1 , wherein said overhead vapor from said first column system is cooled prior to carbon dioxide recovery.7. The process of claim 6 , wherein said overhead vapor is cooled by indirect heat exchange to condense carbon dioxide in the vapor which is recovered by phase separation.8. The process of claim 1 , wherein carbon dioxide and said at least one “heavy” impurity are washed out of said overhead vapor from said first column system in a wash column using as washing liquid carbon dioxide-enriched liquid from said second column system.9. The process of claim 8 , wherein said overhead vapor from said first column system is cooled but not condensed prior to being fed as cooled vapor to said wash column.10. The process of claim 8 , wherein said overhead vapor from said first column system is cooled by direct heat exchange with said washing liquid in said ...

Purification of Carbon Dioxide

In a process for separating “heavy” impurities such as hydrogen sulfide from crude carbon dioxide comprising significant quantities of “light” impurities such as non-condensable gases, involving at least one heat pump cycle using as working fluid a fluid from the “heavy” impurity separation, the “light” impurities are removed from carbon dioxide-enriched gas generated in the “heavy” impurity separation. The carbon dioxide-enriched gas, or a compressed carbon dioxide-enriched gas produced therefrom, is at least partially condensed by indirect heat exchange against intermediate liquid also generated in the “heavy” impurity separation. Total and specific energy consumption is reduced compared to conventional processes in which “light” impurities are removed from carbon dioxide product gas. 2. The process of claim 1 , wherein said at least partially condensed carbon dioxide-enriched gas is expanded prior to said separation to produce said “light” impurity-enriched gas and said carbon dioxide-enriched liquid.3. The process of claim 1 , wherein said carbon dioxide-enriched overhead vapor claim 1 , or said compressed carbon dioxide-enriched gas produced therefrom claim 1 , is partially condensed by said indirect heat exchange to produce partially condensed carbon dioxide-enriched gas.4. The process of claim 1 , wherein said carbon dioxide-enriched liquid is separated from said “light” impurity-enriched gas by phase separation.5. The process of claim 1 , wherein said carbon dioxide-enriched liquid is separated from said “light” impurity-enriched gas by mass transfer separation in a second column system.6. The process of claim 1 , wherein at least part of the vaporization duty required for re-boiling said first column system is provided by at least one stream selected from the group consisting of at least one recycle stream in said heat pump cycle(s); and said crude carbon dioxide fluid.7. The process of claim 1 , wherein said “heavy” impurity-enriched liquid(s) providing ...

AIR SEPARATION METHOD AND APPARATUS

A method and apparatus for separating air in which an oxygen-rich liquid stream is pumped and then heated within a heat exchanger to produce an oxygen product through indirect heat exchange with first and second boosted pressure air streams. The first boosted pressure air stream is cold compressed at an intermediate temperature of the heat exchanger, reintroduced into the heat exchanger at a warmer temperature and then fully cooled and liquefied. The second boosted pressure air stream, after having been partially cooled, is expanded to produce an exhaust stream that is in turn introduced into a lower pressure column producing the oxygen-rich liquid. The second boosted pressure air stream is partially cooled to a temperature no greater than the intermediate temperature at which the cold compression occurs so that both the first and second boosted pressure air streams are able to take part in the heating of the oxygen-rich stream. 1. A method of separating air comprising:separating compressed and purified air in a cryogenic rectification process such that an oxygen-rich liquid column bottoms is produced in a lower pressure column linked in a heat transfer relationship to a higher pressure column by a condenser reboiler, an oxygen-rich liquid stream is pumped to produce a pumped oxygen stream and at least part of the pumped oxygen stream is heated in a main heat exchange system to produce an oxygen product stream;heating the at least part of the pumped oxygen stream within the main heat exchange system by further compressing part of the compressed and purified air stream to produce a first boosted pressure air stream and a second boosted pressure air stream, respectively, partially cooling the first boosted pressure air stream and the second boosted pressure air stream within the main heat exchange system, cold compressing the first boosted pressure air stream, after having been partially cooled, at an intermediate temperature to produce a cold compressed air stream, ...

METHOD FOR PURIFICATION OF CARBON DIOXIDE USING LIQUID CARBON DIOXIDE

The present invention relates to a method for removing at least one contaminant from a gaseous stream substantially comprising carbon dioxide. More specifically said method includes the step of subjecting the gaseous stream to an absorption step in which the absorbent is liquid carbon dioxide. 1. A method for removing a plurality of contaminants from a gaseous feed stream substantially comprising carbon dioxide , said method comprising:subjecting the gaseous feed stream to an absorption step in an absorption column having a top, bottom and an intermediate section, wherein an absorbent is liquid carbon dioxide and wherein the plurality of contaminants are selected from the group consisting of non-polar organic compounds and compounds having a boiling point higher than the boiling point of carbon dioxide; andobtaining a carbon dioxide enriched gaseous stream and a contaminant rich liquid stream containing at least 95% (w/w) of the plurality of contaminants from the gaseous feed stream,wherein the temperature of the gaseous feed stream entering the column is higher than a dew point temperature of carbon dioxide at the prevailing absorption condition and the ratio of absorbent to gaseous feed stream is at least 1/11.2. The method according to claim 1 , wherein the plurality of contaminants are selected from the group consisting of NOx's claim 1 , oxygenates claim 1 , esters claim 1 , aromatic compounds claim 1 , alcohols and combinations thereof.3. The method according to claim 1 , wherein the ratio of absorbent to gaseous feed stream is in the range 1/11 to 1/2 claim 1 , and wherein the plurality of contaminants are selected from the group consisting of NOx's claim 1 , oxygenates claim 1 , esters aromatic compounds claim 1 , alcohols and combinations thereof.4. The method according to claim 1 , wherein the absorbent is an externally supplied source of pure liquid carbon dioxide.5. The method according to claim 1 , wherein the absorption step further comprises an ...

Method and System of Controlling A Temperature Within A Melt Tray Assembly Of A Distillation Tower

A method and system of controlling a temperature within a melt tray assembly of a distillation tower. The method may include determining a melt tray fluid composition of a melt tray fluid, determining a melt tray fluid temperature of the melt tray fluid, determining if the melt tray fluid temperature is within an expected melt tray fluid temperature range for the melt tray fluid composition, decreasing the melt tray fluid temperature if the melt tray fluid temperature is greater than an expected melt tray fluid temperature range upper limit, increasing the melt tray fluid temperature if the melt tray fluid temperature is less than an expected melt tray fluid temperature range lower limit, and maintaining the melt tray fluid temperature if the melt tray fluid temperature is within the expected melt tray fluid temperature range. 1. A method of controlling a temperature within a melt tray assembly of a distillation tower , comprising:maintaining a melt tray assembly, within a controlled freeze zone section of a distillation tower that forms a solid and a vapor from a stream that enters the distillation tower, that comprises a melt tray fluid and a melt tray heat exchanging device within the melt tray fluid;providing a phase changing fluid, to the melt tray heat exchanging device, that is configured to be a dual-phase heat transfer fluid;determining a melt tray fluid composition of the melt tray fluid;determining a melt tray fluid pressure of the melt tray fluid;determining a melt tray fluid temperature of the melt tray fluid;determining if the melt tray fluid temperature is within an expected melt tray fluid temperature range for the melt tray fluid composition and pressure, wherein the expected temperature has an expected melt tray fluid temperature range upper limit and an expected melt tray fluid temperature range lower limit;decreasing the melt tray fluid temperature if the melt tray fluid temperature is greater than the expected melt tray fluid temperature range ...

AIR SEPARATION SYSTEM AND METHOD

A system and method for separating air in an air separation plant is provided. The disclosed systems and methods divert a portion of the compressed, purified air stream to a bypass system configured to selectively produce a higher pressure compressed output stream or a lower pressure compressed output stream. The higher pressure and/or lower pressure compressed output streams are cooled in a main heat exchanger by indirect heat transfer with a plurality of product streams from the air separation plant and then rectified in the distillation column system. A second portion of the compressed, purified air stream is partially cooled in the main heat exchanger and expanding in a turbo-expander to produce power and an exhaust stream which is directed to the distillation column system of the air separation plant where it imparts additional refrigeration generated by the expansion of the compressed air stream in the turbo-expander. 1. (canceled)2. (canceled)3. (canceled)4. (canceled)5. (canceled)6. (canceled)7. (canceled)8. (canceled)9. (canceled)10. (canceled)11. (canceled)12. (canceled)13. An air separation system comprising:an air intake system comprising a main air compressor, a purification unit connected to the main air compressor, the air intake system configured to produce a stream of compressed, purified air;a bypass system in flow communication with the air intake system and configured to receive a first portion of the compressed, purified air stream and condition the first portion of the compressed, purified air stream into a compressed output stream; the bypass system comprising a booster compressor circuit having one or more booster compressors, a bypass circuit, and a plurality of control valves to control the flows through the booster compressor circuit and the bypass circuit;a main heat exchanger in flow communication with the air intake system and the bypass system, the main heat exchanger configured to receive the conditioned compressed output stream from ...

METHODS AND SYSTEMS FOR REMOVING NITROGEN FROM NATURAL GAS

Methods and systems for producing a product natural gas employing a natural gas liquids (NGL) recovery unit followed by removing nitrogen in a nitrogen rejection unit (NRU) operatively connected with the NGL recovery unit by a pressure management sub-system (PMSS). In one embodiment, the PMSS includes a first conduit fluidly connecting the top of a demethanizer column (or an existing conduit connected to the top of the demethanizer) to a separator, a second conduit fluidly connecting the separator to a pump, the pump connected to a distillation column in the NRU by a third conduit, in another embodiment, the PMSS includes a first conduit fluidly connecting an NGL expander to a separator, allowing natural gas vapors and nitrogen to be fed to the NRU column through a second conduit. Alternatively, the PMSS allows mixture from the NGL recovery unit expander to be fed directly via the first conduit to the NRU distillation column. 1. A system comprising:(a) a natural gas liquids (NGL) recovery unit;(b) a nitrogen rejection unit (NRU); and (i) a demethanizer column overhead to one or more heat exchangers and then to a separator,', '(ii) the separator to a pump, the pump having a pump outlet;', '(iii) the pump outlet with a lower section of an NRU distillation column;', '(iv) the NRU distillation column bottoms to an expansion valve;', '(v) the expansion valve with the one or more heat exchangers;', '(vi) the separator overhead to a point of the fifth conduit downstream of the expansion valve and upstream of the one or more heat exchangers; and', '(vii) the point of the fifth conduit to the one or more heat exchangers and then to an NGL recovery unit heat exchanger network., '(c) a pressure management sub-system (PMSS) operatively and fluidly connecting the NGL recovery unit and the NRU, the PMSS comprising a set of conduits, individual members of the set of conduits fluidly connecting2. The system of wherein the separator and the pump are configured so that the ...

Vapor Stripping by Desublimation and Dissolution

Devices, methods, and systems for stripping a vapor from a gas are disclosed. A carrier gas is bubbled through a liquid coolant in a vessel. The vessel contains a mesh screen, packing materials, or combinations thereof. The carrier gas has a vapor component. The vapor component condenses, freezes, deposits, desublimates, or a combination thereof out of the carrier gas onto the mesh screen, the packing material, or combinations thereof, as a solid component. The solid component dissolves into the coolant as the coolant passes through the mesh screen, the packing material, or combinations thereof. 1. A method for stripping a vapor from a gas comprising:passing a carrier gas through a liquid coolant in a vessel, wherein the vessel comprises a mesh screen, packing material, or combinations thereof, and wherein the carrier gas comprises a vapor component;condensing, freezing, depositing, desublimating, or a combination thereof, the vapor component out of the carrier gas onto the mesh screen, the packing material, or combinations thereof, as a solid component; anddissolving the solid component into the coolant as the coolant passes through the mesh screen, the packing, or a combination thereof.2. The method of claim 1 , wherein the liquid coolant comprises water claim 1 , hydrocarbons claim 1 , liquid ammonia claim 1 , liquid carbon dioxide claim 1 , cryogenic liquids claim 1 , or combinations thereof.3. The method of claim 2 , wherein the hydrocarbons comprise 1 claim 2 ,1 claim 2 ,3-trimethylcyclopentane claim 2 , 1 claim 2 ,4-pentadiene claim 2 , 1 claim 2 ,5-hexadiene claim 2 , 1-butene claim 2 , 1-methyl-1-ethyl cyclopentane claim 2 , 1-pentene claim 2 , 5 claim 2 ,3 claim 2 ,3 claim 2 ,3-tetrafluoropropene claim 2 , 5 claim 2 ,3-dimethyl-1-butene claim 2 , 5-chloro-1 claim 2 ,1 claim 2 ,1 claim 2 ,2-tetrafluoroethane claim 2 , 5-methylpentane claim 2 , 3-methyl-1 claim 2 ,4-pentadiene claim 2 , 3-methyl-1-butene claim 2 , 3-methyl-1-pentene claim 2 , 3-methylpentane ...

Recuperative Heat Exchange for Desiccation of Cold Fluids

Devices, systems, and methods for removing a component from a fluid are disclosed. A feed fluid is heated by passing the feed fluid through a heating path of a first indirect-contact heat exchanger (ICHE). The feed fluid contains a first component. The fluid is heated from a first temperature to a second temperature, resulting in a heated feed fluid. The heated feed fluid is passed through a desiccator, containing a desiccant. The first component is bound up to the desiccant, resulting in a stripped-heated feed fluid. The stripped-heated feed fluid is cooled by passing the stripped-heated feed fluid through a cooling path of the first indirect-contact heat exchanger (ICHE). The stripped-heated feed fluid is cooled from a second temperature to a third temperature, the third temperature being greater than the first temperature, producing a product fluid. 1. A method for removing a component from a fluid comprising:heating a feed fluid, the feed fluid comprising a first component, by passing the feed fluid through a heating path of a first indirect-contact heat exchanger (ICHE), wherein the fluid is heated from a first temperature to a second temperature, resulting in a heated feed fluid;passing the heated feed fluid through a desiccator, containing a desiccant, wherein the first component is bound up to the desiccant, resulting in a stripped-heated feed fluid;cooling the stripped-heated feed fluid by passing the stripped-heated feed fluid through a cooling path of the first ICHE, wherein the stripped-heated feed fluid is cooled from the second temperature to a third temperature, the third temperature being greater than the first temperature, producing a product fluid.2. The method of claim 1 , wherein the second temperature is maintained substantially at an ambient temperature.3. The method of claim 2 , wherein passing the feed fluid at a feed rate provides a first sensible heat transfer from the desiccant to the feed fluid claim 2 , and wherein the feed rate is ...

Cryogenic purification device and method and machine comprising a purification device

Device and method for the cryogenic purification of a stream of gas, comprising a purification circuit comprising a first inlet and a first set of filters arranged in series, the first set of filters comprising a terminal heat exchanger in a heat-exchange relationship with a cold source, the purification circuit comprising, downstream of the terminal exchanger, a first outlet, the device comprising at least one drive member intended to set the stream of gas in motion in the circuit, the purification circuit further comprising, between the terminal exchanger and the first outlet, a second set of filter(s), and the at least one drive member being configured to set two successive volumes of gas for purification in motion in opposite directions of circulation in the circuit. The invention also relates to a machine including such a device.

METHOD AND DEVICE FOR DEHYDRATING A CO2 CONTAINING GAS

Proposed is a method for dehydrating a COcontaining gas () by cooling the gas () and separating the condensed water from the gas (), wherein the gas is contacted with liquid COto condense water contained in the gas () and the condensate is separated from the remaining gas. Further, a device for dehydrating a COcontaining gas is proposed, comprising a gas feeding system for feeding the gas which has to be dehydrated, wherein the device comprises a COfeeding system for feeding liquid CO, a contacting device (C) for contacting the gas and the liquid CO for cooling the gas () to condense the water contained in the gas (), and which comprises a first separator () for separating the condensate from the remaining gas. 1. A method for dehydrating a COcontaining gas by{'b': 1', '1, 'cooling the gas () and separating the condensed water from the gas (),'}{'b': 1', '1', '1, 'sub': '2', 'wherein the gas () is contacted with liquid COfor cooling the gas () to condense water contained in the gas () and the condensate is separated from the remaining gas, and'}{'sub': 2', '2, 'b': '10', 'wherein the remaining gas which comprises gaseous COis expanded to condense water contained in the gas, and the thus obtained liquid phase comprising liquid COwater () and, optionally, hydrates is separated from the dehydrated gas.'}2. (canceled)310. The method according to claim 1 , characterized in that the obtained liquid phase () is at least partially used for contacting with the gas to be dehydrated.4. The method according to claim 1 , wherein the liquid COto be mixed with the gas has a temperature within a range of −60° C. to 20° C.5. The method according to claim 1 , wherein the gas to be mixed with the liquid COhas a temperature within a range of −40° C. to 50° C.6. The method according to claim 1 , wherein the temperature of the gas is lowered by expansion below 0° C.7. The method according to claim 1 , wherein the pressure of the gas is lowered by expansion below 7000 kPa.810. The method ...

Heat Exchange Mechanism For Removing Contaminants From A Hydrocarbon Vapor Stream

A system for melting contaminant-laden solids that have been separated from a hydrocarbon-containing vapor stream in a hydrocarbon distillation tower, comprising at least one plate positioned where the solids form within the hydrocarbon distillation tower, hollow tubing forming an integral part of each of the at least one plate, and a heating medium disposed to flow through the hollow tubing at a higher temperature than a temperature of the solids to at least partially melt the solids. 1. A system for melting contaminant-laden solids that have been separated from a hydrocarbon-containing vapor stream in a hydrocarbon distillation tower , comprising:at least one plate positioned where the solids form within the hydrocarbon distillation tower;hollow tubing forming an integral part of each of the at least one plate; anda heating medium disposed to flow through the hollow tubing at a higher temperature than a temperature of the solids to at least partially melt the solids.2. The heat exchange mechanism of claim 1 , wherein the at least one plate is substantially rectangular in shape.3. The heat exchange mechanism of claim 1 , wherein the at least one plate is conical in shape.4. The heat exchange mechanism of claim 1 , wherein the at least one plate is frusto-conical in shape.5. The heat exchange mechanism of claim 1 , wherein the at least one plate comprises a plurality of plates concentrically arranged claim 1 , with each of the plurality having a different radius of curvature.6. The heat exchange mechanism of claim 1 , wherein the at least one plate is formed in a spiral.7. The heat exchange mechanism of claim 1 , wherein the at least one plate comprises a plurality of interconnected sets of plates.8. The heat exchange mechanism of claim 1 , wherein the at least one plate is disposed to accommodate passage of at least one vapor riser adjacent thereto.9. The heat exchange mechanism of claim 8 , wherein the at least one vapor riser comprises a plurality of vapor risers ...

Integrated Gas Separation-Turbine CO2 Capture Processes

Sweep-based gas separation processes for reducing carbon dioxide emissions from gas-fired power plants. The invention involves at least two compression steps, a combustion step, a carbon dioxide capture step, a power generate step, and a sweep-based membrane separation step. One of the compression steps is used to produce a low-pressure, low-temperature compressed stream that is sent for treatment in the carbon dioxide capture step, thereby avoiding the need to expend large amounts of energy to cool an otherwise hot compressed stream from a typical compressor that produces a high-pressure stream, usually at 20-30 bar or more. 1. A process for controlling carbon dioxide exhaust from a combustion process , comprising:(a) compressing an oxygen-containing stream in a first compression apparatus, thereby producing a first compressed gas stream;(b) compressing a carbon dioxide-containing stream in a second compression apparatus, thereby producing a second compressed gas stream;(c) combusting the first compressed gas stream with a gaseous fuel in a combustion apparatus, thereby producing a combusted gas stream;(d) routing at least a portion of the second compressed gas stream to a gas separation apparatus adapted to selectively remove carbon dioxide, thereby producing a carbon dioxide-enriched stream and a carbon dioxide-depleted stream;(e) compressing the carbon dioxide-depleted stream in a third compression apparatus, thereby producing a third compressed gas stream;(f) routing the combusted gas stream and the third compressed gas stream as part of a working gas stream to a gas turbine apparatus mechanically coupled to an electricity generator, and operating the gas turbine apparatus, thereby generating electric power and producing a turbine exhaust stream;(g) passing a first portion of the turbine exhaust stream back to the second compressor as at least a portion of the carbon dioxide-containing stream; (i) providing a membrane having a feed side and a permeate side, and ...

PROCESS FOR PURIFICATION OF A SYNTHESIS GAS CONTAINING HYDROGEN AND IMPURITIES

A process for purification of a current of hydrogen synthesis gas (), particularly in the front-end of an ammonia plant, wherein said gas contains hydrogen and minor amounts of carbon monoxide, carbon dioxide, water and impurities, said process including steps of methanation () of said current (), converting residual amounts of carbon monoxide and carbon dioxide to methane and water, dehydration () of the gas to remove water, and then a cryogenic purification () such as liquid nitrogen wash, to remove methane and Argon; a corresponding plant and method for revamping an ammonia plant are also disclosed. 1100151413100. A process for purification of a current of hydrogen synthesis gas () , said current being composed of hydrogen and minor amounts of carbon monoxide , carbon dioxide , water and impurities , said process including a step of cryogenic purification () , and dehydration () of syngas prior to said cryogenic purification , characterized by a step of methanation () of said current () , converting carbon monoxide and carbon dioxide to methane and water , prior to said steps of dehydration and cryogenic purification.2. A process according to claim 1 , wherein prior to said step of methanation claim 1 , the synthesis gas is subject to shift conversion of carbon monoxide to carbon dioxide claim 1 , and removal of carbon dioxide.3100106107. A process according to or claim 1 , said hydrogen synthesis gas () being obtained by reforming of a hydrocarbon source () with oxygen ().4. A process according to any of the previous claims claim 1 , wherein a portion of the gas claim 1 , after said step of methanation and dehydration claim 1 , bypasses said cryogenic purification.5. A process according to any of to claim 1 , said step of cryogenic purification comprising a liquid nitrogen wash.6. A process according to any of to claim 1 , for obtaining a make-up synthesis gas for the synthesis of ammonia.7. A process according to any of to claim 1 , said current of hydrogen ...

METHOD FOR PRODUCING HIGH PURITY GERMANE BY A CONTINUOUS OR SEMI-CONTINUOUS PROCESS

A continuous or semi-continuous process for producing a high purity germane includes (a) preparing a reaction mixture containing hydrogen and crude germane and (b) separating the hydrogen from the crude germane by a pressure swing adsorption process. The pressure swing adsorption process results in a hydrogen-rich product stream and a germane-rich product stream. 1. A continuous or semi-continuous process for producing a high purity germane containing less than 0.1 volume percent of impurities , the method comprising:(a) preparing a reaction mixture containing hydrogen and crude germane;(b) separating the hydrogen from the crude germane by a pressure swing adsorption process, the pressure swing adsorption process resulting in a hydrogen-rich product stream and a germane-rich product stream; and(c) purifying the germane-rich product stream by continuous distillation thereof to remove impurities therefrom and to produce a high purity germane containing less than 0.1 volume percent of impurities.2. The method of claim 1 , wherein the reaction mixture is prepared by contacting a germanium-containing compound with a hydrogen-containing reducing agent.3. The method of claim 2 , wherein the reducing agent is a borohydride.4. The method of claim 3 , wherein the germanium-containing compound is germanium dioxide.5. The method of claim 1 , wherein the pressure swing adsorption process takes place in a vessel including an adsorbent material having a form of a zeolite molecular sieve.65. The method of claim 5 , wherein the zeolite molecular sieve is a A zeolite molecular sieve.7. The method of claim 5 , wherein during the pressure swing adsorption process claim 5 , germane is adsorbed by and desorbed from the zeolite molecular sieve in respective adsorption and desorption stages.8. The method of claim 7 , wherein the reaction mixture further contains digermane and the digermane is adsorbed by and desorbed from the zeolite molecular sieve in the respective adsorption and ...

METHOD AND SYSTEM FOR SEPARATING A FEED STREAM WITH A FEED STREAM DISTRIBUTION MECHANISM

The present disclosure provides a distillation tower for separating a feed stream. The distillation tower includes a controlled freeze zone section having a controlled freeze zone upper section and a controlled freeze zone lower section below the controlled freeze zone upper section. The controlled freeze zone section includes: (a) a spray assembly in the controlled freeze zone upper section; (b) a melt tray assembly in the controlled freeze zone lower section; (c) a feed stream distribution mechanism between the spray assembly and the melt tray assembly. The feed stream distribution mechanism is constructed and arranged to uniformly distribute the feed stream in the controlled freeze zone section. 1. A distillation tower for separating a feed stream , the distillation tower comprising: (a) a spray assembly in the controlled freeze zone upper section;', '(b) a melt tray assembly in the controlled freeze zone lower section;', '(c) a feed stream distribution mechanism between the spray assembly and the melt tray assembly,, 'a controlled freeze zone section having a controlled freeze zone upper section and a controlled freeze zone lower section below the controlled freeze zone upper section, wherein the controlled freeze zone section is constructed and arranged to form a solid from a feed stream and the controlled freeze zone section compriseswherein the feed stream distribution mechanism is constructed and arranged to uniformly distribute at least a portion of the feed stream in the controlled freeze zone section.2. The distillation tower of claim 1 , wherein the feed stream distribution mechanism is separate and distinct from the spray assembly and the melt tray assembly.3. The distillation tower of claim 1 , wherein the feed stream distribution mechanism comprises a pipe header having orifices that are closer to the melt tray assembly than the spray assembly.4. The distillation tower of claim 3 , wherein the orifices are oriented towards a controlled freeze zone ...

System and Method for Separating Methane and Nitrogen with Reduced Horsepower Demands

A system and method for removing nitrogen from natural gas using two fractionating columns, that may be stacked, and a plurality of separators and heat exchangers, with horsepower requirements that are 50-80% of requirements for prior art systems. The fractionating columns operate at different pressures. A feed stream is separated with a vapor portion feeding the first column to produce a first column bottoms stream that is split into multiple portions at different pressures and first column overhead stream that is split or separated into two portions at least one of which is subcooled prior to feeding the top of the second column. Optional heat exchange between first column and second column streams provides first column reflux and reboil heat for a second column ascending vapor stream. Three sales gas streams are produced, each at a different pressure. 1. A system for removing nitrogen and for producing a methane product stream from a feed stream comprising nitrogen , methane , and other components , the system comprising:a first separator wherein the feed stream is separated into a first separator overhead stream and a first separator bottoms stream;a first splitter for splitting the first separator overhead stream into a first portion and a second portion;a first fractionating column wherein the first and second portions of the first separator overhead stream are separated into a first column overhead stream and a first column bottoms stream;a second splitter for splitting the first column bottoms stream into three portions;a second fractionating column wherein the first column overhead stream is separated into a second column overhead stream and a second column bottoms stream;a second separator wherein the second column bottoms stream is separated into a second separator overhead stream and a second separator bottoms stream;a first mixer to mix the second separator bottoms stream and a third portion of the first column bottoms stream to form a first mixed ...

Method and system of dehydrating a feed stream processed in a distillation tower

The present disclosure provides a method of dehydrating a feed stream processed in a distillation tower. The method may include (a) introducing a feed stream comprising a first contaminant stream into a distillation tower; (b) forming a solid from the feed stream in a controlled freeze zone section of the distillation tower; (c) feeding a second contaminant stream into the feed stream outside the distillation tower; and (d) removing water from the feed stream with a second contaminant stream by feeding the second contaminant stream.

METHOD AND SYSTEM FOR PREVENTING ACCUMULATION OF SOLIDS IN A DISTILLATION TOWER

The present disclosure provides a method for preventing accumulation of solids in a distillation tower. The method includes introducing a feed stream into a controlled freeze zone section of a distillation tower; forming solids in the controlled freeze zone section from the feed stream; discontinuously injecting a first freeze-inhibitor solution into the controlled freeze zone section toward a location in the controlled freeze zone section that accumulates the solids; and destabilizing accumulation of the solids from the location with the first freeze-inhibitor solution. 1. A method for preventing accumulation of solids in a distillation tower , the method comprising:introducing a feed stream into a controlled freeze zone section of a distillation tower;forming solids in the controlled freeze zone section from the feed stream;discontinuously injecting a first freeze-inhibitor solution into the controlled freeze zone section toward a location in the controlled freeze zone section that accumulates the solids; anddestabilizing accumulation of the solids from the location with the first freeze-inhibitor solution.2. The method of claim 1 , wherein the first freeze-inhibitor solution comprises any carbon dioxide solubilizing solvent that remains unfrozen in the controlled freeze zone section.3. The method of claim 1 , wherein the first freeze-inhibitor solution comprises at least one of light hydrocarbons and light alcohols.4. The method of claim 1 , wherein the first freeze-inhibitor solution comprises at least one of ethane claim 1 , methanol claim 1 , propane and butane.5. The method of claim 1 , wherein discontinuously injecting the first freeze-inhibitor solution comprises releasing the first freeze-inhibitor solution from the location.6. The method of claim 1 , wherein the location comprises at least one of a spray assembly of the controlled freeze zone section and a first freeze-inhibitor injection piping arrangement adjacent to a controlled freeze zone wall of the ...

METHOD AND DEVICE FOR SEPARATING HYDROCARBONS AND CONTAMINANTS WITH A SURFACE TREATMENT MECHANISM

The disclosure includes a method for separating a feed stream in a distillation tower may comprise maintaining a controlled freeze zone section in the distillation tower that forms solids from a feed stream, wherein the controlled freeze zone section includes one or more internally disposed elements and a controlled freeze zone wall having an internal wall surface inside of the distillation tower, modifying at least one of the internally disposed elements, the internal wall surface, or both with a treatment mechanism that includes at least one of (a) removing portions of the internal wall surface and (b) applying a coating surface, introducing the feed stream into the controlled freeze zone section, forming the solids from the feed stream in the controlled freeze zone section, and at least one of preventing and destabilizing adhesion of the solids to the internal wall surface with the treatment mechanism. 1. A method for separating a feed stream in a distillation tower comprising:maintaining a controlled freeze zone section in the distillation tower that forms solids from a feed stream, wherein the controlled freeze zone section includes one or more internally disposed elements and a controlled freeze zone wall having an internal wall surface inside of the distillation tower;modifying at least one of the internally disposed elements, the internal wall surface, or both with a treatment mechanism that includes at least one of (a) removing portions of the internal wall surface and (b) applying a coating surface;introducing the feed stream into the controlled freeze zone section;forming the solids from the feed stream in the controlled freeze zone section; andat least one of preventing and destabilizing adhesion of the solids to the internal wall surface with the treatment mechanism.2. The method of claim 1 , wherein removing portions of the internal wall surface comprises one of mechanically and electrochemically removing material from the internal wall surface.3. The ...

METHOD AND DEVICE FOR SEPARATING HYDROCARBONS AND CONTAMINANTS WITH A SPRAY ASSEMBLY

A method for separating a feed stream in a distillation tower comprising maintaining a controlled freeze zone (CFZ) section in the distillation tower, receiving a freezing zone liquid stream in a spray nozzle assembly in the CFZ section, wherein the spray nozzle assembly comprises a plurality of outer spray nozzles on an outer periphery of the spray nozzle assembly and at least one inner spray nozzle interior to the outer spray nozzles, wherein each outer spray nozzle is configured to spray the freezing zone liquid stream along a central spray axis, and wherein the central spray axis of at least one of the outer spray nozzles is not parallel to a CFZ wall, and spraying the freezing zone liquid stream through the spray nozzle assembly into the CFZ section to keep a temperature and pressure at which the solid and the hydrocarbon-enriched vapor stream form. 1. A method for separating a feed stream in a distillation tower comprising:maintaining a controlled freeze zone section in the distillation tower;receiving a freezing zone liquid stream in a spray nozzle assembly in the controlled freeze zone section, wherein the spray nozzle assembly comprises a plurality of outer spray nozzles on an outer periphery of the spray nozzle assembly and at least one inner spray nozzle interior to the plurality of outer spray nozzles, wherein each outer spray nozzle is configured to spray the freezing zone liquid stream along a central spray axis, and wherein the central spray axis of at least one of the plurality of outer spray nozzles is not parallel to a controlled freeze zone wall; andspraying the freezing zone liquid stream through the spray nozzle assembly into the controlled freeze zone section to keep the controlled freeze zone section at a temperature and pressure at which the solid and the hydrocarbon-enriched vapor stream form.2. The method of claim 1 , wherein an angle of the central spray axis of at least one of the plurality of outer spray nozzles is achieved by angling ...

METHOD AND DEVICE FOR SEPARATING A FEED STREAM USING RADIATION DETECTORS

The present disclosure provides a method for separating a feed stream in a distillation tower. The method may include forming solids in a controlled freeze zone section of the distillation tower; emitting radiation from a first radiation source in the controlled freeze zone section while the controlled freeze zone section forms no solids; detecting radiation emitted by the first radiation source as a first radiation level; detecting radiation emitted by the first radiation source as a second radiation level after detecting the first radiation level; and determining whether the solids adhered to at least one of on and around a first mechanical component included in the controlled freeze zone section based on the first radiation level and the second radiation level. 1. A method for separating a feed stream in a distillation tower comprising:forming solids in a controlled freeze zone section of the distillation tower;emitting radiation from a first radiation source in the controlled freeze zone section while the controlled freeze zone section forms no solids;detecting radiation emitted by the first radiation source as a first radiation level;detecting radiation emitted by the first radiation source as a second radiation level after detecting the first radiation level; anddetermining whether the solids adhered to at least one of on and around a first mechanical component included in the controlled freeze zone section based on the first radiation level and the second radiation level.2. The method of claim 1 , wherein the first mechanical component comprises one of: (a) a wall of the controlled freeze zone section and (b) a channel of the controlled freeze zone section.3. The method of claim 1 , wherein determining whether the solids adhered comprises:using the first radiation level to generate a baseline radiation level in the controlled freeze zone section and comparing the second radiation level to a radiation deviation range, the radiation deviation range dependent on ...

METHOD OF REMOVING SOLIDS BY MODIFYING A LIQUID LEVEL IN A DISTILLATION TOWER

The present disclosure provides a method of separating a feed stream in a distillation tower. The method includes maintaining a controlled freeze zone section in a distillation tower; maintaining a melt tray assembly within the controlled freeze zone section that operates at a temperature and pressure at which solid melts; forming solids in a controlled freeze zone section; raising a liquid level of a liquid in the melt tray assembly when the solids accumulate on a mechanical component in the controlled freeze zone section; raising a liquid temperature of the liquid while raising the liquid level; and lowering the liquid level after at least one of (a) a predetermined time period has passed and (b) an alternative temperature of the mechanical component is within an expected temperature range of a baseline temperature of the mechanical component. 1. A method of separating a feed stream in a distillation tower comprising:maintaining a controlled freeze zone section in a distillation tower that operates at a temperature and pressure at which a solid forms;maintaining a melt tray assembly within the controlled freeze zone section that operates at a temperature and pressure at which the solid melts;forming solids in the controlled freeze zone section;raising a liquid level of a liquid in the melt tray assembly when the solids accumulate on a mechanical component in the controlled freeze zone section;raising a liquid temperature of the liquid while raising the liquid level; andlowering the liquid level after at least one of (a) a predetermined time period has passed and (b) an alternative temperature of the mechanical component is within an expected temperature range of a baseline temperature of the mechanical component.2. The method of claim 1 , wherein raising the liquid level comprises determining whether the solids have accumulated on the mechanical component.3. The method of claim 1 , wherein the mechanical component comprises a controlled freeze zone wall.4. The ...

METHOD AND SYSTEM OF MODIFYING A LIQUID LEVEL DURING START-UP OPERATIONS

The present disclosure provides a method for separating a feed stream in a distillation tower. The method includes operating a controlled freeze zone section in a distillation tower that separates a feed stream at a temperature and pressure at which the feed stream forms a solid in the controlled freeze zone section, wherein the feed stream includes a first contaminant; maintaining a melt tray assembly in the controlled freeze zone section; introducing the feed stream to the controlled freeze zone section; and accumulating a liquid in the melt tray assembly until the liquid is at a predetermined liquid level in the controlled freeze zone section, by: feeding a second contaminant to the controlled freeze zone section; and adding the second contaminant to the melt tray assembly, wherein the liquid comprises the second contaminant. 1. A method for separating a feed stream in a distillation tower , the method comprising:operating a controlled freeze zone section in a distillation tower that separates a feed stream at a temperature and pressure at which the feed stream forms a solid in the controlled freeze zone section, wherein the feed stream includes a first contaminant;maintaining a melt tray assembly in the controlled freeze zone section;introducing the feed stream to the controlled freeze zone section; and feeding a second contaminant to the controlled freeze zone section; and', 'adding the second contaminant to the melt tray assembly, wherein the liquid comprises the second contaminant., 'accumulating a liquid in the melt tray assembly until the liquid is at a predetermined liquid level in the controlled freeze zone section, by2. The method of claim 1 , wherein feeding the second contaminant occurs at least one of before and after introducing the feed stream.3. The method of claim 1 , wherein feeding the second contaminant comprises at least one of directly feeding the second contaminant to the controlled freeze zone section and indirectly feeding the second ...

METHOD AND DEVICE FOR SEPARATING HYDROCARBONS AND CONTAMINANTS WITH A HEATING MECHANISM TO DESTABILIZE AND/OR PREVENT ADHESION OF SOLIDS

The present disclosure provides a method for separating a feed stream in a distillation tower which includes separating a feed stream in a stripper section into an enriched contaminant bottom liquid stream and a freezing zone vapor stream; contacting the freezing zone vapor stream in the controlled freeze zone section with a freezing zone liquid stream at a temperature and pressure at which a solid and a hydrocarbon-enriched vapor stream form; directly applying heat to a controlled freeze zone wall of the controlled freeze zone section with a heating mechanism coupled to at least one of a controlled freeze zone internal surface of the controlled freeze zone wall and a controlled freeze zone external surface of the controlled freeze zone wall; and at least one of destabilizing and preventing adhesion of the solid to the controlled freeze zone wall with the heating mechanism. 1. A method for separating a feed stream in a distillation tower comprising:introducing a feed stream into one of a stripper section and a controlled freeze zone section of a distillation tower, the feed stream comprising a hydrocarbon and a contaminant;separating the feed stream in the stripper section into an enriched contaminant bottom liquid stream, comprising the contaminant, and a freezing zone vapor stream, comprising the hydrocarbon, at a temperature and pressure at which no solid forms;contacting the freezing zone vapor stream in the controlled freeze zone section with a freezing zone liquid stream, comprising the hydrocarbon, at a temperature and pressure at which a solid, comprising the contaminant, and a hydrocarbon-enriched vapor stream, comprising the hydrocarbon, form;directly applying heat to a controlled freeze zone wall of the controlled freeze zone section with a heating mechanism coupled to at least one of a controlled freeze zone internal surface of the controlled freeze zone wall and a controlled freeze zone external surface of the controlled freeze zone wall; andat least ...

METHOD FOR PRODUCING A FLOW WHICH IS RICH IN METHANE AND A CUT WHICH IS RICH IN C2+ HYDROCARBONS FROM A FLOW OF FEED NATURAL GAS AND AN ASSOCIATED INSTALLATION

This method comprises cooling the feed natural gas in a first heat exchanger and introducing the cooled, feed natural gas into a first separation flask. 2. The method according to claim 1 , wherein the second recirculation flow is introduced into a flow downstream of the first heat exchanger and upstream of the first expansion turbine in order to form the dynamic expansion flow.3. The method according to claim 2 , wherein the second recirculation flow is mixed with the turbine supply flow from the first separation flask in order to form the dynamic expansion flow claim 2 , the dynamic expansion turbine receiving the dynamic expansion flow being formed by the first expansion turbine.4. Method according to claim 2 , wherein the second recirculation flow is mixed with the cooled natural gas flow before it is introduced into the first separation flask claim 2 , the dynamic expansion flow being formed by the turbine supply flow from the first separation flask.5. The method according to claim 2 , wherein the second recirculation flow is removed from the first recirculation flow.6. Method according to claim 2 , wherein it comprises the following steps of:removing a removal flow from the head flow rich in methane, before it is introduced into the first compressor and the second compressor;compressing the removal flow in a third compressor;forming the second recirculation flow from the compressed removal flow from the third compressor, after cooling.7. Method according to claim 6 , wherein it comprises passing the removal flow into a third heat exchanger and into a fourth heat exchanger before it is introduced into the third compressor claim 6 , then passing the compressed removal flow into the fourth heat exchanger claim 6 , then into the third heat exchanger in order to supply the head of the separation column claim 6 , the second recirculation flow being removed from the cooled claim 6 , compressed removal flow claim 6 , between the fourth heat exchanger and the third ...

AIR SEPARATION METHOD AND APPARATUS

A method and apparatus for separating air in which an oxygen-rich liquid stream is pumped and then heated within a heat exchanger to produce an oxygen product through indirect heat exchange with first and second boosted pressure air streams. The first boosted pressure air stream is cold compressed at an intermediate temperature of the heat exchanger, reintroduced into the heat exchanger at a warmer temperature and then fully cooled and liquefied. The second boosted pressure air stream, after having been partially cooled, is expanded to produce an exhaust stream that is in turn introduced into a lower pressure column producing the oxygen-rich liquid. The second boosted pressure air stream is partially cooled to a temperature no greater than the intermediate temperature at which the cold compression occurs so that both the first and second boosted pressure air streams are able to take part in the heating of the oxygen-rich stream. 128-. (canceled)29. An apparatus for separating air comprising:one or more main air compressors configured for producing a stream of compressed and purified air, wherein the stream of compressed and purified air is split into a first part of the stream of compressed and purified air, a second part of the stream of compressed and purified air that is further compressed in a first booster compressor to produce a first boosted pressure air stream, and a third part of the stream of compressed and purified air that is further compressed in a second booster compressor to produce a second boosted pressure air stream;a main heat exchange system configured to cool the first part of the stream of compressed and purified air, to partially cool the first boosted pressure air stream, and to partially cool the second boosted pressure air stream;a cold compressor configured to further compress the partially cooled first boosted pressure air stream and form a cold compressed stream, wherein the cold compressed stream is further cooled in the main heat ...

Use of Eductor for Liquid Disposal from Vessel

A system for the processing of a hydrocarbon flare gas. An input gas stream contains a gas component and a liquid component. A knock-out drum separates the gas component from the liquid component. An eductor has a motive inlet, a suction inlet, and a discharge outlet. The separated liquid component is introduced into the suction inlet of the eductor. A high-pressure gas stream is introduced into the motive inlet of the eductor. The high-pressure gas stream has a pressure sufficient to draw the separated liquid component from the knock-out drum and through the discharge outlet. 1. A system for the processing of a hydrocarbon flare gas , comprising:an input gas stream containing a gas component and a liquid component;a knock-out drum that separates the gas component from the liquid component;an eductor having a motive inlet, a suction inlet, and a discharge outlet;wherein the separated liquid component is introduced into the suction inlet of the eductor; anda high-pressure gas stream introduced into the motive inlet of the eductor, the high-pressure gas stream having a pressure sufficient to draw the separated liquid component from the knock-out drum and through the discharge outlet.2. The system of claim 1 , wherein the knock-out drum has a boot or sump claim 1 , and wherein the separated liquid component is drawn from the boot or sump to the suction inlet of the eductor.3. The system of claim 1 , wherein the high-pressure gas stream is a defrost gas stream.4. The system of claim 1 , wherein the high-pressure gas stream has a pressure of about 100 psig and the input gas stream has a pressure between 1-2 psig.5. The system of claim 1 , further comprising a dry flare that flares the gas component of the input gas stream after the liquid component has been separated therefrom in the knock-out drum.6. A cryogenic or cold gas processing system claim 1 , comprising:an input gas stream containing a gas component and a liquid component;a knock-out drum that separates the gas ...

Method For Producing Pressurized Gaseous Oxygen Through The Cryogenic Separation Of Air

A method is provided for production of gaseous oxygen at moderate pressures by splitting a main air feed into at least three separate streams, with the first stream being fed to a heat exchanger and then a column system for rectification; the second stream being further compressed in a warm booster, partially cooled in the heat exchanger, expanded in a turbine coupled to the warm booster and then fed to the column system; the third stream being expanded in a warm expander before being introduced to the heat exchanger and introduced to the column system. In certain embodiments, substantially all of the main air feed is eventually introduced to the column system for rectification, resulting in reduced sizing of a main air compressor and improved product recoveries. 1. A method for producing pressurized gaseous oxygen through the cryogenic separation of air , the method comprising the steps of:obtaining a main air feed comprising filtered and compressed air;splitting the main air feed into at least a first air fraction, a second air fraction, and a third air fraction;fully cooling the first air fraction in a heat exchanger to a temperature suitable for rectification of the first air fraction to form a cooled air feed;withdrawing the cooled air feed from the heat exchanger and introducing the cooled air feed to a column system under conditions effective for rectification of the cooled air feed into low pressure gaseous nitrogen (LP GAN), liquid oxygen (LOX), liquid nitrogen (LIN), and high pressure gaseous nitrogen (HP GAN), wherein the column system comprises a double column having a higher pressure column and a lower pressure column;warming the LP GAN, LOX, and HP GAN in the heat exchanger;boosting the second air fraction in a warm booster to form a boosted second air fraction;partially cooling the boosted second air fraction in the heat exchanger and then expanding the boosted second air fraction in a turbine to form an expanded second air fraction;introducing the ...

Process for producing liquid nitrogen

A process for producing a liquid nitrogen product through the cryogenic separation of air in a nitrogen production plant is provided. The nitrogen production plant can include a main air compressor; a heat exchanger; an air separation unit having a single column, a top condenser, and a bottom reboiler; a recycle compressor; at least one turbine-booster having a booster and a turbine; a liquid/gas separator; and a subcooler. The reboiler can be driven by gaseous nitrogen withdrawn from the recycle compressor, preferably at a first stage discharge of the recycle compressor. Additionally, the single column can be partly refluxed with liquid nitrogen split-off from a Joule-Thompson stream.

APPARATUS FOR PRODUCING LIQUID NITROGEN

An apparatus for producing liquid nitrogen is provided. The apparatus includes a heat exchanger, a pair of turbine-boosters, a warm compressor, an air separation unit having a single column, a top condenser and a bottom reboiler, a liquid/gas separator, and an optional subcooler. The apparatus is configured to produce merchant or non-merchant grade liquid nitrogen using the pair of turbine-boosters to provide refrigeration and energy for the process. 1. An apparatus for producing nitrogen through the cryogenic separation of air , the apparatus comprising:a heat exchanger configured to receive a main air feed comprising purified and compressed air at a pressure of at least 5 bar;an air separation unit in fluid communication with a cool side of the heat exchanger, the air separation unit configured to receive cooled air from the heat exchanger and produce gaseous nitrogen and waste oxygen, wherein the air separation unit comprises a single column having a bottom reboiler and a top condenser;a recycle compressor in fluid communication with a warm side of the heat exchanger such that the recycle compressor is configured to receive a nitrogen recycle from the heat exchanger, wherein at least a portion of the nitrogen recycle is made up of gaseous nitrogen from the air separation unit;a first turbine-booster having a first booster and a first turbine, the first booster in fluid communication with the recycle compressor such that the first booster is configured to receive a compressed nitrogen recycle from the recycle compressor;a second turbine-booster having a second booster and a second turbine, the second booster in fluid communication with the first booster such that the second booster is configured to receive a boosted nitrogen from the first booster, wherein an outlet of the second booster is in fluid communication with the heat exchanger such that the boosted nitrogen from the second booster is cooled within the heat exchanger, wherein the second turbine is in ...

PURIFICATION OF ARGON THROUGH LIQUID PHASE CRYOGENIC ADSORPTION

The invention relates to a process for removing oxygen from liquid argon using a TSA (temperature swing adsorption) cyclical process that includes cooling an adsorbent bed to sustain argon in a liquid phase; supplying the adsorbent bed with a liquid argon feed that is contaminated with oxygen and purifying the liquid argon thereby producing an argon product with less oxygen contaminant than is in the initial liquid argon feed; draining the purified residual liquid argon product and sending purified argon out of the adsorbent bed. Regeneration of specially prepared adsorbent allows the adsorbent bed to warm up to temperatures that preclude the use of requiring either vacuum or evacuation of adsorbent from the bed. 1. An adsorption process for purifying a feed stream containing primarily liquid argon and oxygen , comprising the following cycle of process steps:a) supplying from the inlet of an adsorbent bed said liquid argon feed that contains oxygen, adsorbing at least part of the oxygen on the adsorbent thereby producing a purified liquid argon product leaving said adsorbent bed from the outlet with less oxygen than present in said liquid argon feed at the inlet;b) draining from said adsorbent bed purified residual liquid argon by introducing a displacement purge gas;c) allowing said adsorbent bed containing said adsorbent to warm to a temperature, desorbing at least part of the adsorbed oxygen and removing said adsorbed oxygen from the adsorbent bed such that the liquid argon feed may be supplied for purposes of repeating the cycle;d) cooling said adsorbent bed having an inlet and an outlet and containing an adsorbent such that said adsorbent bed is cooled to a temperature below the boiling point of argon;e) wherein said process steps (a)-(d) are repeated in a cyclical manner.2. The process of claim 1 , wherein the liquid argon feed for step (a) contains more than 10 parts per million of oxygen and less or equal to 10 claim 1 ,000 parts per million of oxygen and ...

METHOD FOR RECOVERING HYDROCARBON COMPOUNDS AND A HYDROCARBON RECOVERY APPARATUS FROM A GASEOUS BY-PRODUCT

There is provided a method for recovering hydrocarbon compounds from a gaseous by-products generated in the Fisher-Tropsch synthesis reaction, the method comprising a pressurizing step in which the gaseous by-products are pressurized, a cooling step in which the pressurized gaseous by-products are pressurized to liquefy hydrocarbon compounds in the gaseous by-products, and a separating step in which the hydrocarbon compounds liquefied in the cooling step are separated from the remaining gaseous by-products.

Systems and Methods for Enhanced Recovery of NGL Hydrocarbons

Systems and methods for the enhanced recovery of ethane and heavier hydrocarbons using an absorbing agent. Typical absorbing agents include one or more C3+ alkanes. The systems and methods separate components of a feed gas containing methane and heavier hydrocarbons, which maximizes ethane recovery, without requiring appreciable increases in capital and operating costs, and improves the safety margin with respect to the risk of COfreeze-out. 1. A method for recovering ethane and heavier hydrocarbons from a hydrocarbon feed gas , which comprises:cooling an absorbing agent and an inlet stream comprising the feed gas in a heat exchanger to produce a cooled absorbing agent and a chilled inlet stream;separating the chilled inlet stream in a separator to produce a liquid hydrocarbon stream and an overhead vapor stream;combining the cooled absorbing agent with a portion of the overhead vapor stream to form a combined stream;cooling the combined stream into a reflux exchanger to produce a subcooled liquid stream;expanding another portion of the overhead vapor stream in an expander to produce a demethanizer feed stream; andintroducing the liquid hydrocarbon stream, the subcooled liquid stream and the demethanizer feed stream into a demethanizer column, wherein the ethane and heavier hydrocarbons are recovered as a bottom product in the demethanizer column and methane and lighter hydrocarbons are recovered as a top product in the demethanizer column.2. The method of claim 1 , wherein the absorbing agent comprises one or more C3+ alkanes.3. The method of claim 1 , wherein the hydrocarbon feed gas comprises methane and heavier hydrocarbons.4. The method of claim 1 , wherein the absorbing agent and the inlet stream are cooled in the heat exchanger by indirect heat exchange with a residue stream claim 1 , a side reboiling stream and a demethanizer reboiling stream.5. The method of claim 1 , further comprising processing the methane and lighter hydrocarbons in the reflux exchanger ...

FLOW MANAGEMENT AND CO2-RECOVERY APPARATUS AND METHOD OF USE

An apparatus and method for flow management and CO-recovery from a COcontaining hydrocarbon flow stream, such as a post CO-stimulation flowback stream. The apparatus including a flow control zone, a gas separation zone, a pretreatment zone, and a CO-capture zone. The CO-capture zone is in fluid communication with the pretreatment zone to provide CO-capture from a pretreated flowback gas stream and output a captured CO-flow stream. The CO-capture zone includes a flow splitter to direct a first portion of the pretreated flowback gas stream to a CO-enricher to provide an enriched CO-stream for mixing with a second portion of the pretreated flowback gas to form a mixed stream. The CO-capture zone further includes at least one condenser to output the captured CO-flow stream. 1. An apparatus for flow management and CO-recovery from a COcontaining hydrocarbon flow stream comprising:{'sub': 2', '2', '2, 'a flow control zone in fluid communication with the COcontaining hydrocarbon flow stream to provide control of a flowrate of the COcontaining hydrocarbon flow stream and output a modified COcontaining hydrocarbon flow stream;'}{'sub': 2', '2', '2, 'a gas separation zone in fluid communication with the modified COcontaining hydrocarbon flow stream to provide separation of a gas from the modified COcontaining hydrocarbon flow stream and output a COcontaining hydrocarbon process stream;'}{'sub': '2', 'a pretreatment zone in fluid communication with the gas separation zone to provide removal of one or more of trace solids, aerogels, oil, hydrogen sulfides, water and non-gas liquids from the COcontaining hydrocarbon process stream and output a pretreated gas stream; and'}{'sub': 2', '2', '2', '2', '2', '2', '2', '2, 'a CO-capture zone in fluid communication with the pretreatment zone to provide CO-capture from the pretreated flowback gas stream and output a captured CO-flow stream, the CO-capture zone including a flow splitter to direct a second portion of the pretreated ...

Solids-Producing Siphoning Exchanger

Devices, systems, and methods for siphoning heat exchange or reaction for solids production are disclosed. Passing a contact fluid through a siphoning device, wherein the siphoning device is made of a contact fluid inlet, a carrier fluid inlet, and an outlet, and wherein the contact fluid passes through the contact fluid inlet, inducing a siphon in the carrier fluid inlet. This siphon then siphons a carrier fluid through the carrier fluid inlet and into the contact fluid. The carrier fluid is, in part, made of a first component. The carrier fluid and the contact fluid mix. This mixing produces a product solid, wherein the product solid is produced from the first component by desublimation, condensation, solidification, crystallization, precipitation, reaction with the contact fluid, or a combination thereof of at least a portion of the first component. The product solid passes through the outlet. 1. A method for removing a vapor from a gas comprising:passing a contact fluid through a siphoning device, wherein the siphoning device comprises a contact fluid inlet, a carrier fluid inlet, and an outlet, and wherein the contact fluid passes through the contact fluid inlet, inducing a siphon in the carrier fluid inlet;siphoning a carrier fluid through the carrier fluid inlet and into the contact fluid, the carrier fluid comprising a first component;mixing the carrier fluid and the contact fluid, wherein mixing produces a product solid, wherein the product solid is produced from the first component by desublimation, condensation, solidification, crystallization, precipitation, reaction with the contact fluid, or a combination thereof of at least a portion of the first component; andpassing the product solid through the outlet.2. The process of claim 1 , wherein mixing further produces a warm contact fluid and a component-depleted carrier fluid claim 1 , wherein the warm contact fluid is produced by the carrier fluid transferring heat to the contact fluid claim 1 , and ...

Filtering Coil for Screw Press

Devices, systems, and methods for concentrating a slurry are disclosed. A concentrator is utilized, including a cylindrical vessel containing a cylindrical filter and a screw. The cylindrical filter consists of a flat coil compression spring. The screw passes through the cylindrical filter. A slurry passed through the cylindrical vessel is concentrated. The slurry is conveyed by the screw along an interior of the cylindrical filter. Any two concentric coils of the spring are spaced such that the solid is prevented from passing between them. The slurry is concentrated to produce a concentrated slurry by restricting the product outlet such that a back pressure is created in the cylindrical vessel. The back pressure causes a portion of the liquid to pass between the concentric coils of the spring and out a fluid outlet. The concentrated slurry passes out a product outlet. 1. A concentrator device comprising:a cylindrical vessel comprising a fluid inlet, a fluid outlet, and a product outlet, and wherein the cylindrical vessel has a first inner diameter and a longitudinal axis;a cylindrical filter comprising a flat coil compression spring having a geometric center located on the longitudinal axis and a second outer diameter and a second inner diameter, wherein the second outer diameter is smaller than the first inner diameter such that a space between an outer side wall of the flat coil compression spring and an inner wall of the cylindrical vessel forms a fluid plenum, the fluid outlet being adjacent to the fluid plenum;a screw passing through the cylindrical filter along the longitudinal axis, an outer edge of the screw having a first outer diameter, wherein the first outer diameter is substantially the same as the second inner diameter such that the outer edge of the screw is adjacent to an inner side wall of the flat coil compression spring without contact.2. The concentrator device of claim 1 , wherein any two concentric coils of the flat coil compression spring are ...

FLOW MANAGEMENT AND CO2-RECOVERY APPARATUS AND METHOD OF USE

An apparatus and method for flow management and CO-recovery from a COcontaining hydrocarbon flow stream, such as a post CO-stimulation flowback stream. The apparatus including a flow control zone, a gas separation zone, a pretreatment zone, and a CO-capture zone. The CO-capture zone is in fluid communication with the pretreatment zone to provide CO-capture from a pretreated flowback gas stream and output a captured CO-flow stream. The CO-capture zone includes a first CO-enricher and at least one additional COenricher disposed downstream of the first COenricher and in cascading relationship to provide a CO-rich permeate stream, the CO-capture zone further including at least one condenser to condense the enriched CO-stream and output the captured CO-flow stream. 1. An apparatus for flow management and CO-recovery from a COcontaining hydrocarbon flow stream comprising:{'sub': 2', '2', '2, 'a flow control zone in fluid communication with the COcontaining hydrocarbon flow stream to provide control of a flowrate of the COcontaining hydrocarbon flow stream and output a modified COcontaining hydrocarbon flow stream;'}{'sub': 2', '2', '2, 'a gas separation zone in fluid communication with the modified COcontaining hydrocarbon flow stream to provide separation of a gas from the modified COcontaining hydrocarbon flow stream and output a COcontaining hydrocarbon process stream;'}{'sub': '2', 'a pretreatment zone in fluid communication with the gas separation zone to provide removal of one or more of trace solids, aerogels, oil, hydrogen sulfides, water and non-gas liquids from the COcontaining hydrocarbon process stream and output a pretreated gas stream; and'}{'sub': 2', '2', '2', '2', '2', '2', '2', '2', '2', '2', '2, 'a CO-capture zone in fluid communication with the pretreatment zone to provide CO-capture from the pretreated gas stream and output a captured CO-flow stream, the CO-capture zone including a first CO-enricher and at least one additional CO-enricher disposed ...

Process For Recovering Hydrocarbons From Crude Carbon Dioxide Fluid

The power required to recover C hydrocarbons from crude carbon dioxide comprising C hydrocarbons and hydrogen sulfide may be reduced by distilling the crude carbon dioxide to produce carbon dioxide-enriched overhead vapor and C hydrocarbon-enriched bottoms liquid such that the hydrogen sulfide is rejected with the overhead vapor. Power consumption reductions may be achieved by incorporating a heat pump cycle using carbon dioxide vapor as working fluid to provide at least a part of the refrigeration duty and using a side reboiler to reduce the bottom reboiler duty. Where the bottoms liquid is further processed to produce “lighter” and “heavier” hydrocarbon fractions, the process enables optimization of upgrading crude oil on the basis of API gravity, Reid Vapor pressure and/or viscosity. 1. A process for recovering C hydrocarbon compounds from crude carbon dioxide fluid comprising C hydrocarbon compounds and at least one non-hydrocarbon “heavy” impurity , said process comprising:{'sub': 1', '3', '3+, 'feeding crude carbon dioxide fluid to a distillation column system for distillation to produce carbon dioxide-enriched overhead vapor comprising C-Chydrocarbon compounds and said non-hydrocarbon “heavy” impurity, and C hydrocarbon-enriched bottoms liquid;'}{'sub': '3+', 're-boiling said distillation column system by at least partially vaporizing by indirect heat exchange at least a portion of said C hydrocarbon-enriched bottoms liquid and at least one intermediate liquid in or taken from said distillation column system to provide vapor for said distillation column system;'}cooling and at least partially condensing carbon dioxide-enriched overhead vapor and/or a compressed carbon dioxide-enriched recycle gas produced therefrom, by indirect heat exchange to produce at least partially condensed carbon dioxide-enriched gas; andproviding at least a portion of said at least partially condensed carbon dioxide-enriched gas as reflux for said distillation column system.2. The ...

LIQUEFIED NATURAL GAS FROM RICH NATURAL GAS

Rich natural gas is dried in a water scavenger unit, and then purified in a refluxed absorber. The refluxed stream for the absorber is a stream of predominantly methane condensed by cryogenic refrigeration. The refluxed absorber is operated below the critical point of methane, to allow condensation to occur. Liquefied natural gas is condensed in a cryogenic box, and then further cooled. Natural gas liquid from the refluxed absorber is stabilized for storage and transport. 1. A liquefied natural gas (LNG) system comprising:a water scavenger unit fluidly connected to a rich natural gas source conduit and adapted to produce a dry natural gas;a refluxed absorber disposed downstream of said water scavenger unit to receive the dry natural gas and form a purified natural gas and a natural gas liquid (NGL);a refrigeration unit disposed downstream of said refluxed absorber configured to receive the purified natural gas from said refluxed absorber;a first separator disposed downstream of said refrigeration unit configured to receive a first liquid/gas mixture from the refrigeration unit and separate liquid and gas phases into a first separator liquid outlet and a first separator gas outlet, wherein the first separator liquid outlet is fluidly connected to the refluxed absorber and the first separator gas outlet is fluidly connected to the refrigeration unit;a pressure reduction valve disposed downstream of said refrigeration unit configured to receive liquid from said refrigeration unit;a second separator disposed downstream of said pressure reduction valve configured to receive a second liquid/gas mixture from said pressure reduction valve and separate the liquid and gas phases into a second separator liquid outlet and a second separator gas outlet; andan NGL upgrader disposed downstream of said refluxed absorber receiving the NGL, configured to remove a stabilizer gas from a top of said NGL upgrader and a hydrocarbon liquid from a bottom of said NGL upgrader.2. The system ...

METHOD AND DEVICE FOR DISCHARGING COMPONENTS THAT ARE LESS VOLATILE THAN OXYGEN FROM AN AIR SEPARATION PLANT

A method and plant for discharging components that are less volatile than oxygen from an air separation plant that contains a main heat exchanger a side condenser and a two-column distillation column system for nitrogen-oxygen separation. The side condenser is constructed as a condenser-evaporator and is arranged in a vessel. A part of the feed air is cooled in the main heat exchanger and liquefied at least in part in the side condenser. A first oxygen fraction is withdrawn in the liquid state from the low-pressure column, introduced into the vessel of the side condenser and in part vaporized. A purge stream is taken off from the bottom of the vessel in the liquid state and discharged or withdrawn as end product. The vessel has a mass transfer section above the side condenser, which mass transfer section corresponds to more than one theoretical plate and fewer than 10 theoretical plates. 2. The method according to claim 1 , characterized in that the third oxygen fraction is brought to an elevated pressure in the liquid state by a pump and at this elevated pressure is vaporized in an external evaporator claim 1 , wherein the vaporizing proceeds in the external evaporator.3. The method according to claim 2 , characterized in that the vaporizing proceeds in indirect heat exchange with air or with a water bath.4. The method according to claim 1 , characterized in that the third oxygen fraction is let out into the atmosphere in a gaseous state or withdrawn as gaseous product.5. The method according to claim 1 , characterized in that at least a part of the first oxygen fraction is introduced into the vessel of the side condenser above the mass transfer section.6. The method according to claim 1 , characterized in that a part of the first oxygen fraction is introduced into the vessel of the side condenser below the mass transfer section.7. The method according to claim 1 , characterized in that the first oxygen fraction has an oxygen content of more than 89.0 mol %.8. The ...

Accumulation and Melt Tray Assembly for a Distillation Tower

The disclosure includes techniques associated with a collector tray assembly for a cryogenic distillation tower disposed below a slurry mix zone and above a lower distillation zone, wherein the collector tray assembly comprises a deck at a lower end of the slurry mix zone, and wherein the deck comprises at least one vapor riser configured to pass the vapor from the lower distillation zone into the slurry mix zone, wherein the vapor riser comprises a substantially vertical heat transfer section configured to pass the vapor substantially upwards through the slurry mix zone, and a vapor outlet section comprising at least one vapor outlet, wherein the vapor outlet section is below the heat transfer section. 1. A cryogenic distillation tower system for separating acid gases from hydrocarbons in a raw gas stream , comprising:a controlled freezing zone configured to separate the raw gas stream into an overhead methane gas stream and a substantially solid material comprised of precipitated carbon dioxide;a lower distillation zone configured to receive a bottoms stream comprising acid gases in liquid phase from the controlled freezing zone, and further configured to pass a vapor separated from the acid gases, wherein the acid gas comprises carbon dioxide, hydrogen sulfide, ethane, propane, butane, hydrogen sulfide, aromatic hydrocarbons, or combinations thereof, in substantially liquid phase;a slurry mix zone below the controlled freezing zone configured to house a liquid bath, and wherein the slurry mix zone is configured to receive the substantially solid material from the controlled freezing zone; and a substantially vertical heat transfer section configured to pass the vapor substantially upwards through the slurry mix zone; and', 'a vapor outlet section comprising at least one vapor outlet, wherein the vapor outlet section is below the heat transfer section., 'at least one vapor riser configured to pass the vapor from the lower distillation zone into the slurry mix zone ...