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 И УСТРОЙСТВО ДЛЯ РАЗДЕЛЕНИЯ СМЕСИ ВЕЩЕСТВ ПЕРЕГОНКОЙ

Группа изобретений относится к способу и устройству для разделения смеси веществ путем перегонки в системе перегонных колонн, а также к способу получения криптона и ксенона в этих колоннах. Система содержит одну первую перегонную колонну, причем смесь веществ вводится в первую перегонную колонну, головная фракция из первой перегонной колонны конденсируется частично в первом дефлегматоре в результате непрямого теплообмена с газообразной охлаждающей средой. Образованный при этом конденсат частично подается на первую перегонную колонну как флегма. При стационарной работе системы перегонных колонн в газообразную охлаждающую среду, за первым дефлегматором, добавляется жидкая фракция охлаждающей среды, образованная при этом смешанная охлаждающая среда проводится через теплообменник, в котором газообразная охлаждающая среда, выше по потоку первого дефлегматора, охлаждается в результате непрямого теплообмена. Температура охлаждающей среды при входе в первый дефлегматор, регулируется установкой ...

СПОСОБ ОБРАБОТКИ ПИТАЮЩЕГО ГАЗОВОГО ПОТОКА И УСТАНОВКА ДЛЯ ЕГО ОСУЩЕСТВЛЕНИЯ

Изобретение касается способа обработки питающего газа, в котором обеспечивают питающий газовый поток и направляют питающий газовый поток в экстракционную установку для извлечения жидкостей природного газа; в экстракционной установке охлаждают и предпочтительно по меньшей мере частично сжижают питающий газовый поток, расширяют в средстве расширения и разделяют в сепарационной колонне по меньшей мере один поток, полученный из охлажденного питающего газового потока, и после разделения извлекают обработанный газовый поток и поток жидкостей природного газа; сжимают обработанный газовый поток в по меньшей мере одном компрессоре установки сжатия для получения сжатого обработанного газового потока; в фракционной установке производят разделение потока жидкостей природного газа на множество углеводородных фракций. И из сжатого обработанного газового потока отбирают поток рецикла; и повторно вводят поток рецикла без его охлаждения в питающий газовый поток выше по ходу потока от экстракционной установки ...

СПОСОБ ОХЛАЖДЕНИЯ МНОГОКОМПОНЕНТНЫМ ХЛАДАГЕНТОМ ДЛЯ СЖИЖЕНИЯ ПРИРОДНОГО ГАЗА

Изобретение относится к сжижению богатого метаном потока сжатого газа, в котором сжижение потока газа происходит в теплообменнике, охлаждаемом холодильной машиной с многокомпонентным хладагентом с замкнутым циклом для производства богатого метаном жидкого продукта, имеющего температуру выше приблизительно -112oС и давление, достаточное для того, чтобы жидкий продукт был в точке начала кипения или ниже нее. Сжиженный газообразный продукт затем помещают в емкость для хранения при температуре выше приблизительно -112oС. Использование изобретения позволит более экономично и эффективно произвести сжижение газа. 3 с. и 18 з.п. ф-лы, 7 табл., 10 ил.

СПОСОБ И СИСТЕМА ДЛЯ ПОЛУЧЕНИЯ ПОТОКА ТОЩЕГО МЕТАНСОДЕРЖАЩЕГО ГАЗА

Изобретение относится к способу и системе получения потока тощего метансодержащего газа (22). Поток углеводородного сырья (10) подают в сепаратор (100). Отводят из сепаратора (100) нижний поток жидкости (12). Направляют нижний поток жидкости (12) в колонну стабилизации (200). Отводят из колонны стабилизации (200) поток стабилизированного конденсата (13), обогащенного пентаном. Отводят из колонны стабилизации (200) верхний поток стабилизатора (14), обогащенного этаном, пропаном и бутаном. Разделяют верхний поток стабилизатора (14) в соответствии с отношением деления потока на часть основного потока (15) и часть отводимого потока (16). Направляют часть отводимого потока (16) в установку фракционирования (300) для получения обогащенного этаном потока (17) и нижнего потока, обогащенного пропаном и бутаном (18). Техническим результатом является снижение капитальных и эксплуатационных затрат. 2 н. и 11 з.п. ф-лы, 2 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 ...

УДАЛЕНИЕ АЗОТА ИЗ ПРИРОДНОГО ГАЗА

Изобретение относится к способу разложения азотосодержащей исходной фракции с высоким содержанием углеводородов, предпочтительно природного газа, при этом: исходную фракцию частично сжижают и методом ректификации разделяют на обогащенную азотом фракцию и обедненную азотом фракцию с высоким содержанием углеводородов. В верхней зоне ректификации обогащенный азотом поток отводят, охлаждают и частично подают на ректификацию в качестве возвратного продукта и/или обогащенную азотом фракцию охлаждают и частично конденсируют, частично подают на ректификацию в качестве возвратного продукта и остаточный поток обогащенной азотом фракции подвергают процессу в двух колоннах. В средней зоне ректификации поток с низким содержанием двуокиси углерода, который используют для охлаждения обогащенного азотом частичного потока и/или охлаждения обогащенной азотом фракции, отводят. Ректификацию исходной фракции осуществляют в снабженной разделительной перегородкой разделительной колонне, при этом разделительная ...

СПОСОБ ОБРАТНОГО СЖИЖЕНИЯ БОГАТОЙ МЕТАНОМ ФРАКЦИИ

Заявлен способ обратного сжижения богатой метаном фракции, в частности испаренного газа. При этом богатую метаном фракцию сжимают до давления, которое по меньшей мере на 20% превышает критическое давление подлежащей сжатию фракции, сжижают и переохлаждают. Далее разгружают до давления между 5 и 20 бар и разделяют на газообразную богатую азотом фракцию и жидкую обедненную азотом фракцию. Обедненную азотом фракцию разгружают до давления между 1,1 и 2,0 бар, при этом получающуюся газообразную фракцию без нагревания и сжатия подмешивают в богатую метаном фракцию. Получающаяся при разгрузке бедная азотом жидкая фракция продукта имеет содержание азота ≤1,5 мол.%. 4 з.п. ф-лы, 1 ил.

СПОСОБ И УСТРОЙСТВО ДЛЯ ОБРАБОТКИ ПОТОКА УГЛЕВОДОРОДОВ

Способ обработки потока природного газа, по меньшей мере, включает стадии: подачу частично сконденсированного сырьевого потока в первый аппарат для разделения газа и жидкости при давлении выше 20 бар и ниже 40 бар, разделение сырьевого потока в первом аппарате для разделения газа и жидкости на газообразный поток и жидкостный поток, расширение жидкостного потока и подачи его во второй аппарат для разделения газа и жидкости, разделение указанного газообразного потока, по меньшей мере, на два подпотока, причем сразу после разделения подпотоки имеют одинаковый состав и фазовое состояние. Первый подпоток расширяют с получением частично сконденсированного первого подпотока, который подают во второй аппарат для разделения газа и жидкости. Второй подпоток охлаждают холодным потоком с получением частично сконденсированного второго подпотока и подают его во второй аппарат для разделения газа и жидкости. Из второго аппарата для разделения газа и жидкости отводят газообразный поток и жидкостной поток ...

СПОСОБ ОТДЕЛЕНИЯ АЗОТА ИЗ ПРИРОДНОГО ГАЗА

Изобретение относится к способу разделения азотсодержащей загрузочной фракции с высоким содержанием углеводородов, предпочтительно природного газа. Способ разделения азотсодержащей загрузочной фракции с высоким содержанием углеводородов (1, 1') включает разделение загрузочной фракции (1, 1') путем ректификации (Т1, Т2) на обогащенную азотом фракцию (5) и на фракцию, обедненную азотом, с высоким содержанием углеводородов (10), причем ректификационное разделение осуществляют в ректификационной колонне, состоящей из предварительной разделительной колонны (Т1) и главной разделительной колонны (Т2), при этом из отобранной из предварительной разделительной колонны (Т1) и подведенной в главную разделительную колонну (Т2) фракции (7, 7', 7”) на главной разделительной колонне (Т2) выше места или мест загрузки отбирают жидкую фракцию (6) и как возврат подают на предварительную разделительную колонну (Т1). При этом место отбора и/или объем используемой как возврат для предварительной разделительной ...

СПОСОБ ПОДГОТОВКИ УГЛЕВОДОРОДНОГО ГАЗА К ТРАНСПОРТУ "ОПТИМЕТ"

Изобретение относится к газонефтяной промышленности, в частности к обработке углеводородного газа с использованием низкотемпературного процесса, и может быть использовано в процессах промысловой подготовки и заводской обработки углеводородных газов. Способ подготовки газоконденсатной смеси включает в себя подачу газа с кустов скважин на трехступенчатую сепарацию, компримирование и охлаждение газового потока, введение в него водорастворимого летучего ингибитора гидратообразования, выведение из сепараторов жидкости, разделение ее на углеводородную и водную фазы, направление последней в поток газа, поступающий на одну из ступеней сепарации, и подачу водной фазы, отводимой из сепаратора третьей ступени, в теплообменный аппарат первой ступени сепарации. Водную фазу, отводимую из сепаратора второй ступени сепарации, смешивают с водной фазой, отводимой с первой ступени сепарации, и полученную смесь подают в массообменную часть десорбера-сепаратора, устанавливаемого на потоке газа после его компримирования ...

УСТАНОВКА НИЗКОТЕМПЕРАТУРНОЙ ДЕФЛЕГМАЦИИ С РЕКТИФИКАЦИЕЙ НТДР ДЛЯ КОМПЛЕКСНОЙ ПОДГОТОВКИ ГАЗА И ВЫРАБОТКИ СПГ

Предложена установка низкотемпературной дефлегмации с ректификацией НТДР для комплексной подготовки газа и выработки СПГ, включающая входной сепаратор, блок низкотемпературной конденсации с редуцирующими устройствами, содержащий первый и второй рекуперационные теплообменники, дефлегматор с теплообменной секцией, соединенный линией подачи газа дефлегмации, оснащенной редуцирующим устройством, с низкотемпературным сепаратором, оснащенным линией вывода подготовленного природного газа, а также блок стабилизации конденсата, где в качестве низкотемпературного сепаратора установлен деметанизатор с линией подачи деметанизированного конденсата и линией вывода подготовленного природного газа, оснащенной первым рекуперационным теплообменником, по меньшей мере одно из редуцирующих устройств выполнено в виде детандера, на линии подачи газа дефлегмации после редуцирующего устройства расположен сепаратор, соединенный с деметанизатором линией подачи остатка сепарации, на которой расположена теплообменная ...

СПОСОБ ОЖИЖЕНИЯ ПОТОКА ГАЗА (ВАРИАНТЫ)

Описан способ ожижения природного газа для производства сжатого жидкого продукта, имеющего температуру выше -112°С, с использованием двух смешанных холодильных агентов в двух замкнутых циклах, холодильного агента с низким уровнем температуры для охлаждения и ожижения природного газа и холодильного агента с высоким уровнем температуры для охлаждения холодильного агента с низким уровнем температуры. После использования для ожижения природного газа холодильный агент с низким уровнем температуры (а) нагревают путем теплообмена в противотоке с другим потоком холодильного агента с низким уровнем температуры и путем теплообмена с первым потоком холодильного агента с высоким уровнем температуры, (b) сжимают до повышенного давления и (с) переохлаждают внешней охлаждающей средой. Холодильный агент с низким уровнем температуры затем охлаждают путем теплообмена со вторым потоком холодильного агента с высоким уровнем температуры и путем теплообмена с холодильным агентом с низким уровнем температуры.

СПОСОБ УДАЛЕНИЯ АЗОТА

Изобретение относится к способу удаления фракции с высоким содержанием азота из исходной фракции, содержащей в основном азот и углеводороды. Исходная фракция частично конденсируется и ректификационным методом разделяется на фракцию с высоким содержанием азота и фракцию с высоким содержанием метана. В соответствии с изобретением во время прерывания подачи исходной фракции применяемая (применяемые) для ректификационного разделения разделительная колонна (разделительные колонны) (T1/T2), а также служащие для частичной конденсации (E1) исходной фракции и охлаждения и нагрева образующихся при ректификационном разделении технологических потоков теплообменники (E2) посредством одной или нескольких различных охлаждающих сред (6-11) удерживаются на уровнях температуры, которые по существу соответствуют уровням температуры во время нормального режима эксплуатации разделительной колонны (разделительных колонн) (T1/T2) и теплообменников (E1, E2). 1 з.п. ф-лы, 4 ил.

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 ...

СИСТЕМЫ ХРАНЕНИЯ И ПОДАЧИ ТОПЛИВА В ВИДЕ СЖИЖЕННОГО ПРИРОДНОГО ГАЗА (СПГ-ТОПЛИВА) ДЛЯ ТРАНСПОРТНЫХ СРЕДСТВ, РАБОТАЮЩИХ НА ПРИРОДНОМ ГАЗЕ

Изобретение относится к системам хранения сжиженного природного газа под давлением (СПГД-топлива) от примерно 1035 до примерно 7590 кПа и при температуре от примерно -123 до примерно -62oС и подачи испаряющегося СПГД-топлива для сгорания в двигателе. Системы подачи и хранения топлива имеют резервуары для хранения топлива, которые выполнены из сверхвысокопрочной низколегированной стали, содержащей менее 9 вес.% никеля и имеющей предел прочности при растяжении, превышающий 830 МПа, и температуру перехода от пластичного разрушения к хрупкому ниже, чем примерно -73oС. Изобретение особенно применимо для транспортных средств с двигателями, предназначенными для работы за счет сгорания природного газа. Использование изобретение позволит создать экономичную систему хранения и подачи топлива для сгорания в двигателе автомобиля. 6 с. и 9 з.п. ф-лы, 3 табл., 4 ил.

СПОСОБ И УСТРОЙСТВО ПРОИЗВОДСТВА ПОТОКА СЖИЖЕННОГО ПРИРОДНОГО ГАЗА

Изобретение относится к производству потока сжиженного природного газа (СПГ). Изобретение касается способа производства потока сжиженного природного газа, в котором перед сжижением природного газа из его потока удаляют тяжелые углеводородные компоненты с молекулярным весом, большим молекулярного веса бутана, включающего следующие этапы, на которых создают в основном парообразный поток (1) природного газа с давлением и температурой потока подаваемого газа; подают поток подаваемого газа (1) в дистилляционную колонну (10), имеющую две или больше ступени (11) сепарации; отбирают нижний поток (17) из нижней части дистилляционной колонны (10) и верхний поток (16) из верхней части дистилляционной колонны (10), причем верхний поток (16) содержит относительно меньшее количество компонентов тяжелых углеводородов, чем нижний поток (17); и сжижают по меньшей мере часть верхнего потока (16), в результате чего получают поток сжиженного природного газа; отличающегося тем, что перед подачей потока (1) ...

СИСТЕМА И СПОСОБ ДЛЯ ОТДЕЛЕНИЯ ГАЗОКОНДЕНСАТНОЙ ЖИДКОСТИ И АЗОТА ИЗ ПОТОКОВ ПРИРОДНОГО ГАЗА

Система и способ для удаления азота и получения потока метанового продукта высокого давления и потока NGL–продукта из сырьевых потоков природного газа, где по меньшей мере 90% этана и предпочтительно по меньшей мере 95% этана в сырьевом потоке извлекается в поток NGL–продукта. Система и способ изобретения особенно подходят для использования с потоками подачи свыше 5 млн станд. куб. фут/сут (0,1 млн м3/сут) и до 300 млн станд. куб. фут/сут (8,5 млн м3/сут) и содержащими от примерно 5% до 80% азота. Система и способ предпочтительно комбинируют использование стратегического теплообмена между различными технологическими потоками с ректификационной колонной высокого давления и способностью отклонять весь или часть потока подачи в установку удаления азота с необязательным обходом колонны фракционирования азота для снижения капитальных затрат и эксплуатационных расходов. 11 н. и 52 з.п. ф-лы, 5 ил., 2 табл.

Автономная установка очистки сжиженного природного газа (варианты)

Группа изобретений предназначена для отделения примесей от жидкости и могут быть использованы для получения СПГ повышенного качества. Установка содержит подогреватель сырьевого СПГ, компрессор, бак-сепаратор чистого СПГ с трубопроводом отвода отсепарированных паров и ректификационную колонну с патрубком слива кубовой жидкости. Трубопровод отвода греющей среды из подогревателя сырьевого СПГ соединен с подводящим трубопроводом бака-сепаратора чистого СПГ и с трубопроводом подачи флегмы в ректификационную колонну. В первом, втором и третьем варианте выполнения установка содержит испаритель, а в подогревателе сырьевого СПГ в качестве греющей среды используется частично сконденсированный сжатый пар. Охлаждающей средой испарителя ректификационной колонны является кубовая жидкость ректификационной колонны. Заявленная группа изобретений обеспечивает повышение качества очистки СПГ. 4 н.п. ф-лы, 4 ил.

СПОСОБ ДЛЯ ОБРАБОТКИ ПОТОКА УГЛЕВОДОРОДОВ И УСТРОЙСТВО ДЛЯ ЕГО ОСУЩЕСТВЛЕНИЯ

Способ обработки потока природного газа включает стадии подачи частично сконденсированного сырьевого потока (10), имеющего давление свыше 50 бар, в первый аппарат (2) для разделения газа/жидкости, разделения сырьевого потока (10) в первом аппарате (2) для разделения газа/жидкости на первый поток (20) пара и первый поток (70) жидкости, расширения первого потока (20) пара с получением частично сконденсированного первого потока (30) пара, подачи потока (30) пара во второй аппарат (4) для разделения газа/жидкости, разделения потока (30) во втором аппарате (4) для разделения газа/жидкости на второй поток (60) пара и второй поток (40) жидкости, повышения давления второго потока (40) жидкости до давления, равного по меньшей мере 50 бар, с получением в результате сжатого второго потока (50) жидкости и возврата сжатого второго потока (50) жидкости в первый аппарат (2) для разделения газа/жидкости. Первый поток (70) жидкости направляют в третий аппарат (7) для разделения газа/жидкости, который представляет ...

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 СЖИЖЕНИЯ ПРИРОДНОГО ГАЗА И УСТРОЙСТВО ДЛЯ ЕГО ОСУЩЕСТВЛЕНИЯ

Поток хладагента разделяют по меньшей мере на две части, которые пропускаются через отдельные турбодетандеры до того, как они поступят в отдельные теплообменники. При этом кривая нагревания хладагента сближается с кривой охлаждения продукта, подвергаемого сжижению. Использование изобретения позволяет снизить энергетические затраты. 2 с. и 16 з.п. ф-лы, 1 табл., 6 ил.

ДВУХСТУПЕНЧАТЫЙ ОТВОД АЗОТА ИЗ СЖИЖЕННОГО ПРИРОДНОГО ГАЗА

Азот удаляют из подачи (41) сжиженного природного газа посредством двухступенчатого разделения, в котором сжиженный природный газ (41) подвергают первому фракционированию (23), чтобы обеспечить первый поток (46) пара верхнего погона, обогащенного азотом, и поток (19) жидкого отстоя, содержащего азот, и затем, по меньшей мере, часть указанного потока (19) жидкого отстоя подвергают фракционированию (25), чтобы обеспечить второй поток (36) пара верхнего погона, обогащенного азотом, который имеет более низкую чистоту, чем указанный первый поток (46) пара верхнего погона и поток (50) очищенного сжиженного природного газа. Первое фракционирование проводят в перегонной колонне (23), орошаемой (45) верхним погоном (43) азота, сконденсированного в конденсаторе (24), размещенном в испарительном барабане (25), в котором проводят второе фракционирование. Обеспечение двух потоков (26, 36), содержащих азот с различной концентрацией, дает возможность управлять содержанием азота в топливном газе для использования ...

УСТАНОВКА ПЕРЕРАБОТКИ УГЛЕВОДОРОДНОГО ГАЗА

... 1. Установка переработки углеводородного газа, содержащая блок охлаждения газа и выделения нестабильного конденсата с выходом подготовленного газа, узел выделения широкой фракции легких углеводородов, включающий ректификационную колонну с подогревателем в нижней части, снабженную выходами широкой фракции легких углеводородов и газа, выход широкой фракции легких углеводородов из ректификационной колонны соединен с объектом потребителя и/или объектами технологического процесса, дожимную компрессорную станцию, запорную и/или запорно-регулировочную арматуру, отличающаяся тем, что установка снабжена дополнительной ректификационной колонной, обеспечивающей качество товарных продуктов - пропана автомобильного или пропан-бутана автомобильного, а также авиационного сконденсированного топлива, вход сырья которой соединен с выходом широкой фракции легких углеводородов из ректификационной колонны узла выделения широкой фракции легких углеводородов, дополнительная ректификационная колонна оснащена подогревателем ...

УСТАНОВКА ФРАКЦИОНИРОВАНИЯ ГАЗООБРАЗНЫХ И ЖИДКИХ ПОТОКОВ УГЛЕВОДОРОДОВ

Полезная модель относится к переработке газообразных и жидких углеводородов, а именно нефтяных и природных газов и газовых конденсатов для получения целевых компонентов и может быть использована на предприятиях нефтяной и газовой промышленности. Задачей заявляемой полезной модели является повышение производительности установки путем увеличения выпуска целевых продуктов за счет более полной утилизации газов стабилизации низкого давления и обеспечение экологической безопасности. Указанная задача в установке фракционирования газообразных и жидких потоков углеводородов, содержащей блок очистки природного газа с линиями подачи сырого природного газа и линиями отвода газов стабилизации низкого давления, с линиями выхода ПБФ, ПГФ и товарного газа, и блок стабилизации конденсата с линиями подачи нестабильного газового конденсата, отвода стабильного конденсата и линией отвода газов стабилизации высокого давления, которая снабжена компрессором и соединена с линиями подачи сырого природного газа, ...

ТЕРМОАКУСТИЧЕСКАЯ УСТАНОВКА ДЛЯ ПОЛУЧЕНИЯ СИНТЕТИЧЕСКОГО ПРИРОДНОГО ГАЗА ИЗ ПОПУТНОГО НЕФТЯНОГО ГАЗА

Установка для утилизации попутного нефтяного газа, имеющая узел подготовки газа, холодильники, теплообменники и узлы сжижения фракций газа, отличающаяся тем, что для более полного использования всех углеводородных фракций попутного нефтяного газа узел подготовки газа соединен с реактором конверсии фракций попутного нефтяного газа в синтез-газ; реактор конверсии соединен с реактором метанирования, превращающим синтез-газ в метан; реактор метанирования через воздушный теплообменник соединен с первым противоточным теплообменником, выход которого соединен с первым термоакустическим холодильником для сжижения углекислого газа; выход первого термоакустического холодильника через второй противоточный теплообменник соединен со вторым термоакустическим холодильником для сжижения метана с выбросом азота в атмосферу; выход второго термоакустического холодильника соединен со вторым потоком второго противоточного теплообменника, который соединен со вторым потоком первого противоточного теплообменника ...

УСТАНОВКА НИЗКОТЕМПЕРАТУРНОГО РАЗДЕЛЕНИЯ УГЛЕВОДОРОДНОГО ГАЗА

Установка низкотемпературного разделения углеводородного газа, содержащая блок предварительного охлаждения газа, включающий последовательно установленные теплообменник, пропановый холодильник и сепаратор первой ступени, блок конденсации и охлаждения газа, включающий теплообменники, отпарные колонны, турбодетандерный агрегат, состоящий из турбодетандера и турбокомпрессора, сепараторы второй ступени и сепаратор третьей ступени с линией отвода метановой фракции высокого давления, блок выделения этана и широкой фракции легких углеводородов, включающий теплообменники, деэтанизатор, деметанизатор, состоящий из отпарной секции, снабженной выносным насосом для подачи кубовой жидкости в деэтанизатор, и укрепляющей секции с линией отвода метановой фракции среднего давления и установленным на ней клапаном, блок получения гелиевого концентрата, и соединительные трубопроводы, отличающаяся тем, что линия отвода метановой фракции среднего давления на выходе из укрепляющей секции деметанизатора соединена ...

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.

МНОГОСТУПЕНЧАТЫЙ ЦИКЛОННЫЙ СЕПАРАТОР ДЛЯ ТЕКУЧЕЙ СРЕДЫ

Изобретение относится к циклонному сепаратору для текучей среды, содержащему горловинную часть (4), которая размещается между секцией впуска сходящейся текучей среды и секцией выпуска расходящейся текучей среды. Циклонный сепаратор для текучей среды выполнен с возможностью продвигать циклонный поток через секцию впуска сходящейся текучей среды и горловинную часть к секции выпуска расходящейся текучей среды в направлении вниз по потоку. Секция выпуска расходящейся текучей среды содержит внутреннюю первичную выпускную трубу (7) для текучих компонентов, обедненных конденсирующимися парами, и внешнюю вторичную выпускную трубу (6) для текучих компонентов, обогащенных конденсирующимися парами. Циклонный сепаратор для текучей среды содержит дополнительную внешнюю вторичную выпускную трубу (16). Внешняя вторичная выпускная труба (6) размещается в первой позиции вдоль центральной оси (I) циклонного сепаратора для текучей среды, и дополнительная внешняя вторичная выпускная труба (16) размещается ...

СПОСОБ СЖИЖЕНИЯ ГАЗА С ФРАКЦИОНИРОВАНИЕМ ПРИ ВЫСОКОМ ДАВЛЕНИИ

Способ предлагает сжижать природный газ, осуществляя следующие стадии: охлаждают природный газ, вводят охлажденный природный газ в колонну для фракционирования таким образом, чтобы разделить газовую фазу, обогащенную метаном, и жидкую фазу, обогащенную соединениями, более тяжелыми, чем этан, извлекают вышеупомянутую жидкую фазу из нижней части колонны для фракционирования и удаляют вышеупомянутую газовую фазу из верхней части колонны разделения, частично сжижают вышеупомянутую газовую фазу таким образом, чтобы получить конденсат и газообразный поток, при этом конденсат возвращают в верхнюю часть колонны для фракционирования в качестве флегмы, сжижают вышеупомянутый газообразный поток, за счет теплообмена при давлении выше 50 бар. Рабочие условия колонны для фракционирования, функционирующей при давлении, находящемся в диапазоне от 40 до 60 бар, выбирают таким образом, чтобы вышеупомянутая жидкая фаза содержала молярное количество метана в интервале от 10% до 150% молярного количества этана ...

СПОСОБ И УСТРОЙСТВО ДЛЯ ОТДЕЛЕНИЯ ОДНОГО ИЛИ БОЛЕЕ C+УГЛЕВОДОРОДОВ ИЗ УГЛЕВОДОРОДНОГО ПОТОКА СО СМЕШАННЫМИ ФАЗАМИ

Способ отделения одного или более С+углеводородов из жидкого углеводородного потока включает подачу потока углеводородного сырья со смешанными фазами в виде потока частично испарившегося углеводородного сырья в первый газожидкостной сепаратор. Поток углеводородного сырья со смешанными фазами получают из одного или более резервуаров-хранилищ посредством пропускания через теплообменник жидкого углеводородного потока из одного или более резервуаров-хранилищ. Далее разделяют поток углеводородного сырья со смешанными фазами в первом газожидкостном сепараторе на первый газообразный поток, выходящий из первого выхода, и, по меньшей мере, один жидкий поток C+. Первый газообразный поток пропускают через компрессор, в результате чего получают компримированный поток, который охлаждают в одном или более теплообменниках, в результате чего получают поток, по крайней мере, частично сконденсированного углеводородного продукта. Второй газообразный поток добавляют к потоку после первого выхода. Второй газообразный ...

ОБЪЕДИНЕННЫЕ ИЗВЛЕЧЕНИЕ ПГК И ПРОИЗВОДСТВО СЖИЖЕННОГО ПРИРОДНОГО ГАЗА

Объединенный способ производства природного газоконденсата и сжиженного природного газа включает подачу газа в колонну-скруббер в первом местоположении, отвод из колонны-скруббера первого потока пара верхнего погона, обедненного компонентами, более тяжелыми, чем метан, и потока отстоя, обогащенного компонентами, более тяжелыми, чем метан. Далее охлаждают и частично конденсируют первый поток пара верхнего погона, чтобы образовать первый двухфазный поток. Разделяют первый двухфазный поток, чтобы обеспечить второй поток пара верхнего погона и богатый метаном первый поток орошения. Вводят обогащенный метаном первый поток орошения во второе местоположение в колонну-скруббер выше первого местоположения. Сжижают второй поток пара верхнего погона в основном теплообменнике, чтобы обеспечить продукт СПГ. Разделяют поток отстоя, чтобы обеспечить обогащенный этаном поток и поток продукта ПГК, обогащенный компонентами, более тяжелыми, чем этан. Полностью конденсируют обогащенный этаном поток при температуре ...

СПОСОБ ПОДГОТОВКИ НЕСТАБИЛЬНОГО УГЛЕВОДОРОДНОГО КОНДЕНСАТА К ТРАНСПОРТИРОВАНИЮ ПО ТРУБОПРОВОДУ В ОДНОФАЗНОМ СОСТОЯНИИ

Способ предназначен для извлечения нестабильного конденсата на промысловых установках подготовки конденсатосодержащих природных газов. Достижение кондиции продуктового конденсата по давлению и обеспечение совместного транспортирования газа дегазации и продуктового газа осуществляется в абсорбционно-отпарной колонне под давлением, близким к давлению в концевой ступени разделения исходного газа, но не выше 7,0 МПа. При этом достижение кондиции продуктового конденсата по температуре осуществляют путем рекуперативного теплообмена с конденсатными потоками, выделенными при ступенчатом разделении исходного газа, и потоком продуктового газа, что обеспечивает снижение эксплуатационных затрат при осуществлении подготовки конденсата к транспортированию по трубопроводу в однофазном состоянии. 1 табл.,3 ил.

СПОСОБ ПЕРЕРАБОТКИ ПОПУТНОГО НЕФТЯНОГО ГАЗА

Изобретение относится к нефтяной промышленности. Способ переработки попутного нефтяного газа включает компримирование газа путем сжатия и охлаждения компрессата в условиях дефлегмации и стабилизации флегмы с получением сжатого газа и жидкого продукта. Газ смешивают с газами сепарации и компримируют в две ступени с редуцированием и сепарацией жидких продуктов с получением газов сепарации и стабильных жидких продуктов. Сжатый газ второй ступени подвергают низкотемпературной сепарации с получением конденсата и газа, который подают на вторую ступень в качестве хладоагента и выводят в качестве подготовленного газа. Сепарацию редуцированного жидкого продукта на второй ступени осуществляют совместно с конденсатом низкотемпературной сепарации. В качестве стабильного жидкого продукта на первой ступени получают газовый бензин, а на второй - пропан-бутановую фракцию. При необходимости перед одной из ступеней компримирования газ очищают от сероводорода и меркаптанов и/или осушают. Техническим результатом ...

ТЕПЛООБМЕННИК СО СТРУЙНЫМ ИСТЕЧЕНИЕМ ЖИДКОСТИ И УСТАНОВКА ДЛЯ РАЗДЕЛЕНИЯ ВОЗДУХА ДИСТИЛЛЯЦИЕЙ

Использование: в теплотехнике. Сущность изобретения: каналы 19 конденсации азота образованы с помощью заслонки 22, над которой размещен отсек 23 для распределения жидкого кислорода, закрытый в его верхнем конце. Этот отсек 23 содержит на середине высоты перфорированную горизонтальную заслонку 27 и под ней футеровку 28 с вырезами с горизонтальными образующими. Жидкий кислород вводят сбоку в эти отсеки, предварительно распределяя его через отверстия 33 заслонки 27 при помощи футеровки 28, и он проходит в смежные каналы 18 испарения кислорода, открытые сверху и снизу, через горизонтальную прорезь 34, расположенную как раз над заслонкой 22. Теплообменник применен в главных испарителях-конденсаторах установок дистилляции воздуха с двумя колоннами. 2 с. и 10 з.п. ф-лы, 5 ил.

СПОСОБ АВТОМАТИЧЕСКОГО УПРАВЛЕНИЯ ПРОЦЕССОМ ОЧИСТКИ АРГОНА

Использование: в криогенной технике, в частности в воздухоразделительных установках при получении чистого аргона из сырого с использованием метода каталитического гидрирования. Сущность изобретения: в установку вводят схему автоматического регулирования, с помощью которой управляют процессом очистки путем управляющих воздействий на расход потока газообразного водорода в первый и второй реакторы. При этом информацию о содержании кислорода в сыром аргоне, давлении сырого аргона и водорода, о расходе сырого аргона, температуре реакции и избытке водорода используют для формирования электрических сигналов управляющих воздействий y1 и y2 по расчетным формулам. 1 ил.

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 ...

Газоперерабатывающий завод

Настоящее изобретение относится к криогенной технике и может быть использовано в газовой промышленности для переработки углеводородных газов. Предложен газоперерабатывающий завод, включающий установку выделения фракции углеводородов С2+, которая включает расположенные на линии очищенного и осушенного газа компрессорную секцию первого детандер-компрессорного агрегата, основной многопоточный теплообменник, сепаратор, оснащенный линиями вывода газа сепарации и остатка сепарации. Причем линия вывода газа сепарации разделена на линии подачи первого и второго газов сепарации, линия вывода остатка сепарации разделена на линии подачи первого и второго остатков сепарации, при этом линия подачи первого остатка сепарации соединена с линией подачи первого газа сепарации, оснащенной верхним многопоточным теплообменником, редуцирующим вентилем и соединенной с верхней частью ректификационной колонны, линия подачи второго остатка сепарации оснащена редуцирующим вентилем и соединена со средней частью ректификационной ...

СПОСОБ КРИОГЕННОГО РАЗДЕЛЕНИЯ ГАЗОВЫХ СМЕСЕЙ И УСТРОЙСТВО ДЛЯ ЕГО ОСУЩЕСТВЛЕНИЯ

СПОСОБ И УСТРОЙСТВО ДЛЯ ЕГО ОСУЩЕСТВЛЕНИЯ (ВАРИАНТЫ)

Использование: для улавливания и извлечения этана и более тяжелых углеводородных компонентов из потока углеводородного газа. Сущность изобретения: поток подразделяется на первый и второй потоки. Первый поток охлаждается с последующим конденсированием всего этого потока и расширением до давления, которое ниже давления дистилляционной колонны. После расширения охлажденный первый поток направляется в теплообменник, где он вступает в теплообменную связь с более теплым дистилляционным потоком, поднимающимся из секций фракционирования дистилляционной колонны. После этого происходит разделение нагретого первого потока с целью образования холодного пара и потока жидкости. Жидкость подается в колонну в первой позиции подачи по центру колонны, а холодный пар подается в колонну во второй позиции подачи по центру колонны. Второй поток расширяется до давления колонны, а затем подается в колонну в третьей позиции подачи по центру колонны. Дистилляционный поток охлаждается первым потоком в достаточной ...

СПОСОБ РАЗДЕЛЕНИЯ ГАЗОВОГО ПОТОКА И УСТРОЙСТВО ДЛЯ ЕГО ОСУЩЕСТВЛЕНИЯ (ВАРИАНТЫ)

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

СПОСОБ УПРАВЛЕНИЯ РЕКТИФИКАЦИОННОЙ УСТАНОВКОЙ

Изобретение относится к криогенной технике, в частности к управлению установок по очистке и разделению криптоно-ксенонового концентрата, получаемого на воздухоразделительных установках. Способ управления ректификационной установкой для переработки сжатых смесей включает регулирование расходов исходной смеси в установку и питания ректификационных колонн, давлений и количества выводимых из колонн верхнего и нижнего продуктов. Ректификационные колонны оборудованы пробоотборниками в концентрационной части и конденсаторами-испарителями с промежуточным теплоносителем в замкнутой полости. Смесь на входе в установку стабилизируют по температуре и давлению, расход смеси в установку устанавливают дроссельным клапаном, обеспечивая перепад давления на дроссельном клапане для критического истечения смеси. Дополнительно осуществляют анализ из паровой зоны куба, при этом для каждой колонны определяют ключевые компоненты и их содержание в упреждающем анализе и анализе из паровой зоны куба. Концентрации ...

Способ получения концентрата ксенона из природного газа

Изобретение относится к области неорганической химии, а именно к разделению компонентов природного газа методами газогидратной кристаллизации и мембранного газоразделения, объединенных в едином массообменном аппарате, и может быть использовано для получения концентрата ксенона. Способ включает образование газовых гидратов ксенона при давлении от 2.4 до 8.0 МПа и температуре от 273 до 283 K и последующее их разложение с образованием концентрата ксенона. Причем в мембранно-газогидратном кристаллизаторе создают области низкого давления от 0.01 до 0.1 МПа и высокого давления от 2.4 до 8.0 МПа, разделенные непористой полимерной газоразделительной мембраной. Далее поток природного газа подают в область высокого давления с находящимся в ней 6-10-кратным избытком воды относительно объемной концентрации гидратообразующих газов в природном газе при указанных условиях для образования газовых гидратов ксенона. Затем компоненты природного газа с высокой газовой проницаемостью после прохождения через ...

УСТАНОВКА ДЛЯ ВЫДЕЛЕНИЯ УГЛЕВОДОРОДОВ CИЗ ПРИРОДНОГО ГАЗА (ВАРИАНТЫ)

Изобретение относится к установкам низкотемпературной сепарации и может быть использовано в газовой промышленности для выделения углеводородов Сиз природного газа. Предложена установка, включающая в варианте 1 блок осушки, внешний контур охлаждения в составе испарителя, компрессора, конденсатора и редуцирующего устройства, два рекуперационных теплообменника, два детандера, насос, дефлегматор и деметанизатор. Вариант 2 взамен внешнего контура охлаждения включает компрессор, холодильник и третий детандер. При работе варианта 1 газ высокого давления осушают и разделяют на два потока, первый охлаждают в первом рекуперационном теплообменнике, а второй - в испарителе и во втором рекуперационном теплообменнике, затем потоки объединяют, редуцируют в первом детандере и направляют в дефлегматор, охлаждаемый газом низкого давления, который затем нагревают в первом рекуперационном теплообменнике и выводят. При циркуляции хладагент внешнего контура после нагрева в испарителе сжимают компрессором, приводимым ...

СПОСОБ ПОДГОТОВКИ УГЛЕВОДОРОДНОГО ГАЗА К ТРАНСПОРТУ

... 1. Способ подготовки углеводородного газа к транспорту, включающий подачу газа с кустов скважин на трехступенчатую сепарацию, компримирование и охлаждение газового потока, введение в него водорастворимого летучего ингибитора гидратообразования, выведение из сепараторов жидкости, разделение ее на углеводородную и водную фазы, направление последней в поток газа, поступающий на одну из предыдущих ступеней сепарации, отличающийся тем, что водную фазу, отводимую из сепаратора третьей ступени, подают в теплообменный аппарат первой ступени сепарации, водную фазу, отводимую из сепаратора второй ступени, смешивают с водной фазой, отводимой с первой ступени сепарации, и полученную смесь подают в массообменную часть десорбера-сепаратора, устанавливаемого на потоке газа после его компримирования, а водную фазу, выделяющуюся в десорбере-сепараторе направляют на утилизацию. 2. Способ по п. 1, отличающийся тем, что водную фазу, выделившуюся в сепараторе третьей ступени делят на две части: одну из которых ...

КОНСТРУКЦИЯ РЕБОЙЛЕРА КОЛОННЫ ДЕАЗОТИРОВАНИЯ

... 1. Способ деазотирования поступающего потока сжиженного природного газа (СПГ), включающий: ! (а) увеличение объема поступающего потока (102) СПГ и охлаждение поступающего потока СПГ перед увеличением или после в теплообменнике (106) с образованием охлажденного и увеличенного в объеме потока (108) СПГ; ! (b) введение указанного охлажденного и увеличенного в объеме потока (108) СПГ в колонну деазотирования (150); ! (c) отвод обогащенного азотом верхнего потока пара (130) из указанной колонны (150); ! (d) отвод очищенного от азота потока донной жидкости (110) из указанной колонны (150); ! (e) подачу донного потока (110) со стадии (d) через насос (112) для увеличения его давления; ! (f) разделение донного потока (110) на первый поток (114) и второй поток (116); ! (g) по меньшей мере, частичное испарение указанного второго потока (116) путем снижения давления и затем подачу через указанный теплообменник (106); ! (h) впрыскивание указанного частично испаренного второго потока (120) в указанную ...

СПОСОБ КРИОГЕННОГО ВЫДЕЛЕНИЯ МЕТАНА ИЗ СИНТЕЗ-ГАЗА, В ЧАСТНОСТИ ОКСО-ГАЗА

... 1. Способ отделения метана от синтез-газа, в частности оксо-газа, включающий стадии:конденсация потока (21) синтез-газа таким образом, что образуются обедненная метаном фракция (22) синтез-газа и обогащенный метаном богатый СО конденсат (23),отделение конденсата (23),разделение конденсата (23) в колонне (35) на богатый CH, жидкий поток (24) и обедненный метаном богатый СО газообразный поток (25),выведение богатого СО потока (25) из верхней части колонны (35),сжатие богатого СО потока (25) исмешивание богатого СО потока (25) с обедненной метаном фракцией (26) синтез-газа (26) для получения конечного потока (27) синтез-газа.2. Способ по п. 1, отличающийся тем, что конденсат (23) в сепараторе (34) отделяют от фракции синтез-газа (22), в частности, при температуре в области от -150°C до -170°C, в частности при -165°C.3. Способ по п. 1, отличающийся тем, что поток синтез-газа (21) для конденсации в по меньшей мере первом и, в частности, также в последующем втором теплообменнике (32, 33) охлаждают ...

УСТАНОВКА И СПОСОБ ПОЛУЧЕНИЯ СИНТЕЗ-ГАЗА ИЗ ПРИРОДНОГО ГАЗА

... 1. Установка для одновременного получения из природного газа метанольного синтез-газа, аммиачного синтез-газа, монооксида углерода и диоксида углерода, отличающаяся тем, что отдельная производственная линия, состоящая из последовательно соединенных друг с другом узлов, включает: первый реактор А, в котором при подаче кислорода осуществляют превращение природного газа в синтез-газовую смесь, состоящую из монооксида углерода, диоксида углерода, водорода и воды; второй реактор В, в котором осуществляют регулируемое превращение монооксида углерода в диоксид углерода; абсорбер D, который служит для поглощения диоксида углерода и получения смеси монооксида с водородом, используемой для синтеза метанола; холодильный сепаратор Е, в котором при подаче жидкого азота получают аммиачный синтез-газ и одновременно выделяют монооксид углерода, аргон и метан. 2. Установка по п.1, отличающаяся тем, что предусмотрен компрессор С, посредством которого могут быть сжаты образующиеся в реакторах А и В газы.

УСТАНОВКА СИСТЕМЫ И СИСТЕМА СЖИЖЕНИЯ УГЛЕВОДОРОДНОЙ ТЕКУЧЕЙ СРЕДЫ

СПОСОБ И УСТРОЙСТВО ДЛЯ ОБРАБОТКИ ПОТОКА УГЛЕВОДОРОДОВ И УСТРОЙСТВО ДЛЯ ЕГО ОСУЩЕСТВЛЕНИЯ

... 1. Способ обработки потока углеводородов, например потока природного газа, включающий, по меньшей мере, стадии: ! (a) подачи частично сконденсированного сырьевого потока (10), имеющего давление свыше 50 бар, в первый аппарат (2) для разделения газа/жидкости; ! (b) разделения сырьевого потока (10) в первом аппарате (2) для разделения газа/жидкости на первый поток (20) пара и первый поток (70) жидкости; ! (c) расширения первого потока (20) пара, полученного на стадии (b), с получением в результате, по меньшей мере, частично сконденсированного первого потока (30) пара; ! (d) подачи, по меньшей мере, частичного сконденсированного первого потока (30) пара, полученного на стадии (с), во второй аппарат (4) для разделения газа/жидкости; ! (e) разделения потока (30), полученного на стадии (d), во втором аппарате (4) для разделения газа/жидкости на второй поток (60) пара и второй поток (40) жидкости; ! (f) повышения давления второго потока (40) жидкости, полученного на стадии (е), до давления, равного ...

СПОСОБ КРИОГЕННОЙ ОБРАБОТКИ СЫРЬЯ, СОДЕРЖАЩЕГО АЗОТ И МЕТАН, И УСТРОЙСТВО ДЛЯ ЕГО ОСУЩЕСТВЛЕНИЯ

Использование: изобретение относится к криогенной технике и используется в основном для разделения азота и метана методом криогенной ректификации. Сущность изобретения: устройство содержит два сепаратора 2 и 11 фаз, отгоночную колонну 3 и устройство для удаления азота. В сепараторе 2 сырье разделяют на первый пар и первую жидкость, разделяют последнюю в отгоночной колонне 3 на обогащенную азотом и обогащенную метаном фракции, причем фракцию обогащенную азотом, подают на ректификацию в устройство для удаления азота, а фракцию, обогащенную метаном, выделяют в качестве готового продукта. Первый пар после частичной конденсации подают в сепаратор 11, где его разделяют на второй пар и вторую жидкость. Второй пар подают на ректификацию, а вторую жидкость - на разделение в отгоночную колонну. 2 с. и 6 з.п. ф-лы, 1 ил.

БЛОЧНАЯ УСТАНОВКА ПОДГОТОВКИ УГЛЕВОДОРОДНОГО ГАЗА

Изобретение относится к газовой промышленности, а именно к установкам подготовки природного газа к транспорту адсорбционным способом, и может быть использовано в нефтяной и других отраслях промышленности. Установка содержит регулирующий клапан, входной сепаратор, адсорберы, верх которых соединен с линией подачи исходного газа, линией подачи газа охлаждения и линией отвода насыщенного газа регенерации, а низ соединен с линией отвода подготовленного газа, линией отвода газа охлаждения и линией подачи газа регенерации, фильтрующее устройство, печь, сепаратор высокого давления, подпиточную емкость и блок регенерации метанола. Ректификационная колонна блока регенерации метанола оснащена ребойлером с использованием в качестве теплоносителя части насыщенного газа регенерации. Вход ребойлера сообщен через линию отвода части насыщенного газа регенерации с линией отвода насыщенного газа регенерации перед вторым рекуперативным теплообменником, а выход соединен через линию отвода охлажденной части ...

СПОСОБ АБСОРБЦИОННОЙ ПОДГОТОВКИ ПРИРОДНОГО ГАЗА

Изобретение относится к газовой промышленности, в частности к подготовке природного газа и извлечению нестабильного углеводородного конденсата из пластового газа, и может быть использовано на газоконденсатных месторождениях, расположенных в зоне многолетнемерзлых грунтов. В способе абсорбционной подготовки природного газа природный газ подвергают первичной сепарации, после чего его охлаждают и подают на вторичную сепарацию. Отсепарированный при вторичной сепарации газ охлаждают и подают на вход абсорбера, в котором газ подвергают абсорбции жидким углеводородным абсорбентом. Его получают из отсепарированного после первичного сепаратора жидкого углеводородного потока путем его последовательного трехступенчатого трехфазного разделения, а затем его сепарации от остаточных газов и охлаждения. После второй и третьей ступени трехфазного разделения производят нагрев жидкого углеводородного потока. Газ, отводимый из абсорбера, нагревают и отводят потребителю. Поток жидких углеводородов после вторичной ...

Установка извлеченияHe из товарного жидкого гелия методом ректификации

Изобретение относится к области получения гелия из природного газа. Установка извлеченияНе из товарного жидкого гелия содержит внешний ожижитель гелия, блок ректификации, включающий ректификационную колонну с конденсаторами, трубопроводы, соединяющие ожижитель гелия и блок ректификации, и один или более отводящих тепло от конденсаторов рефрижераторов с избыточным обратным потоком, создаваемым за счет добавления жидкого гелия из внешнего ожижителя. Изобретение обеспечивает снижение стоимости установки и эксплуатационных затрат, а также упрощение управления производительностью установки. 2 з.п. ф-лы, 1 ил.

ПАРЦИАЛЬНЫЙ КОНДЕНСАТОР

... 1. Парциальный конденсатор, имеющий по меньшей мере один теплообменный блок (1) с конденсационными каналами и каналами для прохода хладоносителя, рассчитанный на работу под давлением корпус (2), охватывающий теплообменный блок (1) сверху и с боков, средства (14, 15, 16, 17) для подачи пара в нижнюю часть конденсационных каналов, средства (19) для отвода жидкого конденсата из нижней части конденсационных каналов, средства (29, 30) для отвода пара из верхней части конденсационных каналов и средства для подачи хладоносителя в предназначенные для его прохода каналы, отличающийся тем, что конденсационные каналы на их нижнем конце сообщаются с коллектором, который расположен под теплообменным блоком (1) и имеет фазоразделительное устройство. 2. Парциальный конденсатор по п.1, отличающийся тем, что фазоразделительное устройство имеет днище (13) с по меньшей мере одним отверстием (14, 15, 16, 17) для прохода газа, которое со своей верхней стороны окружено круговым бортиком (18), обеспечивающим ...

СПОСОБ ОБРАБОТКИ ЖИДКОГО ПРИРОДНОГО ГАЗА

... 1. Способ выделения углеводородов, являющихся более тяжелыми, чем метан, из сжиженного природного газа (LNG), включающий: ! а) закачивание насосом жидкого LNG низкого давления в зону с давлением, превышающим 100 ф/дюйм2; ! б) направление сжатого жидкого LNG со стадии а) в холодильный резервуар, где происходит его теплообмен с целью повышения его температуры; ! в) направление нагретого жидкого LNG под давлением со стадии б) в сепаратор, где в комбинации с первой и второй флегмой получается отгоняемый продукт разделения вместе с нижним отстоем; ! г) сжатие нижнего отстоя из сепаратора и затем разделение этого сжатого продукта на первую и вторую части; ! д) направление первой части нижнего отстоя в этаноотгонную колонну в виде потока флегмы; ! е) нагревание второй части сжатого нижнего отстоя из сепаратора путем направления этой второй части в холодильный резервуар; ! ж) направление нагретой второй части сжатого нижнего отстоя из сепаратора в этаноотгонную колонну; ! з) удаление углеводородов ...

Установка дл производства изотопов 18О, 17О и 15N

... 1. Установка для производства изотопов18O,17О и15 N, включающая последовательно установленные, по крайней мере, один водяной абсорбер с патрубками ввода и вывода оксидов азота, подачи воды и отвода азотной кислоты, по крайней мере, одну силикагелевую колонну с патрубками ввода и вывода оксидов азота, по крайней мере, один силикагелевый адсорбер, по крайней мере, одну низкотемпературную ректификационную очистительную колонну и блок получения указанных изотопов с выходами оксидов азота и указанных изотопов, отличающаяся тем, что она снабжена, по крайней мере, одной колонной нормализации потока питания с патрубками ввода оксидов азота и азотной кислоты и патрубком вывода оксидов азота, соединенным с патрубком ввода оксидов азота водяного абсорбера, и, по крайней мере, одним сернокислотным абсорбером с патрубками ввода и вывода оксидов азота, ввода и вывода серной кислоты и подачи диоксида серы, причем, патрубки ввода и вывода оксидов азота сернокислотного абсорбера соединены, соответственно ...

УСОВЕРШЕНСТВОВАННЫЙ СПОСОБ СЖИЖЕНИЯ ПРИРОДНОГО ГАЗА

... 1. Способ сжижения газового потока с высоким содержанием метана, который включает следующие этапы: (a) создание газового потока под давлением, превышающим, примерно, 3103 кПа (450 фн-с/кв.д абс); (b) расширение газового потока до более низкого давления для создания газовой фазы и жидкого продукта, температура которого превышает, примерно, -112oС (-170oF), а давление достаточно для того, чтобы жидкий продукт находился в точке начала кипения или ниже; (c) фазовое разделение газовой фазы и жидкого продукта; (d) введение жидкого продукта в средство хранения для хранения при температуре, превышающей, примерно, -112oС (-170o F). 2. Способ по п.1, дополнительно включающий охлаждение газового потока до осуществления этапа (b). 3. Способ по п.2, дополнительно включающий охлаждение газового потока в теплообменнике, охлаждаемом системой охлаждения с замкнутым циклом. 4. Способ по п. 3, в котором система охлаждения с замкнутым циклом в качестве основного хладагента использует пропан. 5. Способ по п ...

ОБРАБОТКА ГАЗООБРАЗНЫХ УГЛЕВОДОРОДОВ

СПОСОБ И СИСТЕМА ДЛЯ ПОЛУЧЕНИЯ ПОТОКА ТОЩЕГО МЕТАНСОДЕРЖАЩЕГО ГАЗА

СПОСОБ И СИСТЕМА ДЛЯ УПЛОТНЕНИЯ КРИОГЕННОГО РАКЕТНОГО ТОПЛИВА

... 1. Система уплотнения жидкого кислорода, которая включает в себя трубопровод, приспособленный для транспортировки потока жидкого кислорода, потока жидкого азота и потока жидкого водорода, первый теплообменник, приспособленный для обеспечения возможности теплового взаимодействия жидкого кислорода с жидким азотом, причем жидкий кислород и жидкий азот протекают через первый теплообменник в противоположных направлениях, при этом первый теплообменник выполнен таким образом, что поток жидкого кислорода охлаждается и за счет этого уплотняется, и башню с насадкой, которая приспособлена для обеспечения возможности теплового взаимодействия жидкого азота с жидким водородом, причем жидкий азот и водород протекают через башню с насадкой в противоположных направлениях, при этом башня с насадкой приспособлена для охлаждения жидкого азота за счет теплового взаимодействия ранее его выпуска из башни с насадкой, причем башня с насадкой приспособлена также для выпуска из указанной системы любого парообразного ...

СПОСОБ НИЗКОТЕМПЕРАТУРНОЙ СЕПАРАЦИИ КОМПОНЕНТОВ ГАЗА

... 1. Способ низкотемпературной сепарации, включающий охлаждение смеси, частичную конденсацию компонентов смеси при расширении смеси в закрученном потоке в сопле, разделении потока смеси на поток, обогащенный компонентами тяжелее метана, и поток, обедненный этими компонентами, разделение потока смеси или ее части в ректификационной колонне, отличающийся тем, что обедненный поток или его часть дополнительно охлаждают, расширяют в дроссельном клапане и направляют в ректификационную колонну.2. Способ низкотемпературной сепарации, включающий охлаждение смеси, частичную конденсацию компонентов смеси при расширении смеси в закрученном потоке в сопле, разделении потока смеси на поток, обогащенный компонентами тяжелее метана, и поток, обедненный этими компонентами, разделение потока смеси или ее части в ректификационной колонне, отличающийся тем, что обедненный поток или его часть дополнительно охлаждают, расширяют в турбине детандера и направляют в ректификационную колонну.

СИСТЕМА ДЛЯ ПЕРЕРАБОТКИ ГАЗОВ

... 1. Система для переработки топочных газов из работающей на ископаемом топливе электростанции для производства электрической энергии, содержащая:адиабатический компрессор для первого сжатия указанного топочного газа до низкого давления;вторая система сжатия низкого давления, имеющая одну или более ступеней и один или более охладителей; исистема сжатия высокого давления, содержащая несколько ступеней и один или более охладителей, причем вторая система сжатия низкого давления и система сжатия высокого давления объединены в одном устройстве и установлены на один общий вал и приводятся в действие одним общим приводом.2. Система по п. 1, дополнительно включающая блок для криогенной очистки топочного газа путем удаления инертных газов из топочного газа, причем блок для криогенной очистки расположен после второй системы сжатия низкого давления и перед системой сжатия высокого давления.3. Система по п. 1, дополнительно включающая блок для дегидратации, расположенную после второй системы сжатия низкого ...

СПОСОБ СЖИЖЕНИЯ БОГАТОГО УГЛЕВОДОРОДАМИ ПОТОКА С ОДНОВРЕМЕННЫМ ИЗВЛЕЧЕНИЕМ С3/С4 -БОГАТОЙ ФРАКЦИИ

... 1. Способ сжижения богатого углеводородами потока, прежде всего потока природного газа, с одновременным извлечением С3/С4-богатой фракции за счет теплообмена богатого углеводородами потока по меньшей мере с одним хладагентом и/или одной смесью хладагентов и подачи сжижаемого богатого углеводородами потока после его предварительного охлаждения в разделительную колонну, в которой от сжижаемого богатого углеводородами потока отделяют высшие углеводороды, с последующим его охлаждением и сжижением, при этом в разделительную колонну в качестве флегмы подают С2+-богатую фракцию, извлеченную из богатого углеводородами потока при его последующем охлаждении, отличающийся тем, что в разделительную колонну (Т1) подают в качестве дополнительной флегмы С4/С5-богатую фракцию (20, 35), располагая при этом точку подачи С4/С5-богатой фракции (20, 35) над точкой подачи С2+-богатой фракции (5) и предусматривая между точкой подачи С4/С5-богатой фракции (20, 35) и точкой подачи С2+-богатой фракции (5) зону массообмена ...

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

Газовый поток обрабатывают в теплообменнике, образующем единый узел: он частично конденсируется при охлаждении в контурах , а несконденсировавшуюся газовую фазу нагревают в другом контуре. Необходимый холод получают от конденсатов, которые после переохлаждения и дросселирования испаряются. Процесс может осуществляться в теплообменнике, состоящем из множества каналов в каждом контуре.

ОЧИСТКА СЖИЖЕННОГО ПРИРОДНОГО ГАЗА

... 1. Способ очистки сжиженного природного газа, подводимого под давлением сжижения, содержащего компоненты с низкими точками кипения, для получения потока жидкого продукта с пониженным содержанием компонентов, имеющих низкие точки кипения, который включает (a) расширение сжиженного газа до давления разделения с получением расширенной двухфазной текучей среды; (b) ввод расширенной двухфазной текучей среды в колонну, содержащую единственную секцию контактирования газа и жидкости, при этом расширенную двухфазную текучую среду вводят ниже единственной секции контактирования газа и жидкости, размещенной в этой колонне; (c) накопление в нижней части колонны жидкости из двухфазной текучей среды и отвод из нижней части колонны потока жидкости, имеющей пониженное содержание компонентов с низкими точками кипения с получением потока жидкого продукта; (d) обеспечение протекания пара двухфазной текучей среды через единственную секцию контактирования; (e) отвод из верхней части колонны потока газообразной ...

ОЧИСТКА СЖИЖЕННОГО ПРИРОДНОГО ГАЗА

... 1. Способ очистки сжиженного природного газа, подводимого под давлением сжижения, содержащего компоненты с низкими точками кипения, для получения потока жидкого продукта с пониженным содержанием компонентов, имеющих низкие точки кипения, который включает (a) расширение сжиженного газа до давления разделения на фазы с получением расширенной двухфазной текучей среды; (b) введение расширенной двухфазной текучей среды в колонну ниже секции контактирования газа и жидкости, размещенной в колонне; (c) накопление в нижней части колонны жидкости из двухфазной текучей среды и отвод из нижней части колонны потока жидкости, имеющей пониженное содержание компонентов с низкими точками кипения; ввод потока жидкости в испарительную камеру при низком давлении; удаление второго газового потока через верх испарительной камеры; удаление из нижней части испарительной камеры потока жидкости для получения потока жидкого продукта; (d) обеспечение протекания пара двухфазной текучей среды через секцию контактирования ...

СПОСОБ РАЗДЕЛЕНИЯ СМЕСИ, СОДЕРЖАЩЕЙ ПО МЕНЬШЕЙ МЕРЕ АЗОТ И МЕТАН

Установка деэтанизации попутного нефтяного газа высокого давления

АВАРИЙНАЯ ДИСТИЛЛЯЦИОННАЯ КОЛОННА И ЕЕ ПРИМЕНЕНИЕ

Настоящее изобретение относится к аварийной дистилляционной колонне и к ее применению, в частности, для регенерации отработанных масел. Установка для регенерации отработанных масел состоит из двух отдельных фракционирующих сегментов, один из которых состоит из основной дистилляционной колонны (1), а другой состоит из аварийной дистилляционной колонны (2), предпочтительно под вакуумом. Указанные два сегмента действуют взаимодополняющим образом, и один поддерживает другой. Аварийная дистилляционная колонна (2) соединена с основной дистилляционной колонной (1) посредством отвода от трубопроводов, которые питают указанную основную дистилляционную колонну (1). Упомянутый отвод имеет устройства перекрывания жидкости, которые позволяют снабжать указанную аварийную дистилляционную колонну (2), когда падения давления ниже по потоку относительно основной дистилляционной колонны (1) превышают предварительно заданное пороговое значение. Техническим результатом является отсутствие засорения и периодов ...

Пленочная парциально-конденсационная колонна

Установка для стабилизации газового конденсата

УСТАНОВКА ДЛЯ СТАБИЛИЗАЦИИ ГАЗОВОГО КОНДЕНСАТА, содержадая последовательно установленные колонны деэ.танизации-депропанизации и стабилизации с теплообменниками нестабильного газового конденсата, подогревателями и конденсаторами колонн , о т л и-ча.ю ща я Ся тем, что, с целью повьппения степени извлечения целевых углеводородных газов, она снабжена дополнительной ректификационной колонной с. подогревателем, конденсатором и холодильником, нижняя часть которой через холодильник, а средняя часть через совденсатор соединены соответственно с вводом и вьшодом верхней части колонны деэтанизацни-дёпропанизации ..

Способ выделения гелия

Воздухоразделительная установка

Способ одновременного получения гелия, этана и более тяжелых углеводородов

Изобретение относится к газовой промышленности . Целью изобретения является повышение экономичности. Перерабатываемый газ разделяют на потоки, которые раздельно охлаждают и частично конденсируют за счет холода обратных потоков. Затем потоки смешивают и сепарируют, при этом жидкость дросселируют и направляют на сепарацию, откуда испаренные гелий и легкие углеводороды подают в нижнюю часть гелиевой ректификационной колонны. Жидкую фазу колонны делят на два потока, один из которых дросселируют, частично испаряют и разделяют в сепараторе. Выделившуюся жидкость дросселируют, смешивают с жидкостью, выделившейся при охлаждении и сепарации подаваемого на переработку газа, и подают в качестве питания в колонну-деметанизатор. Пар. выделившийся при охлаждении и сепарации первой части жидкой фазы гелиевой колонны, расширяют, объединяют с остальной частью жидкой фазы гелиевой колонны, сепарируют и жидкость направляют в качестве холодного орошения в колонну-деметанизатор. 1 ил. (А С ...

Способ автоматического регулирования процесса разделения воздуха в криогенной установке

Изобретение относится к способу автоматического регулирования процесса разделения воздуха в ректификационных колоннах криогенной установки , может быть использовано в химической промьшшенности и позволяет увеличить выход чистого азота. Способ реализуется САР, включающей контур регулирования соотношения между концентрацией азотной флегмы (датчик 8) и концентрацией отбросного азота (датчик 7) изменением расхода азотной флегмы (исполнительный механизм 13, связанный с выходом регулятора 12 соотношения). Камера задания регулятора 12 соотношения соединена с регулятором 10 концентрации чистого азота . 1 ил. (Л г , чистый СО ( со to Kucfopod ...

Устройство для стабилизации теплового режима групп регенераторов

Способ охлаждения воздуха

Способ обогащения криптонового концентрата

Способ разделения сжатых газовых смесей

Способ получения криптоно-ксеноновой смеси

СПОСОБ ПОЛУЧЕНИЯ КРИПТОНО-КСЕНОНОВОЙ СМЕСИ из метановой фракции продувочных газов синтеза аммиака методом низкотемпературной ректификации , включающий сжатие выходящих паров, охлаждение и конденсацию с образованием флегмы, отличающийся тем, что, с целью снижения энергозатрат процесс ректификации проводят при давлении в колонне 0,4-1,2 МПа.

Способ получения водорода из углеводородной газовой смеси

Способ низкотемпературной цеметанизации углеводородных газов

Колонна для разделения газовых смесей

Способ разделения содержащей двуокись углерода и легкие углеводороды газовой смеси

Изобретение относится к технологии разделения газовых смесей, в частности к способу разделения содержащей двуокись углерода и легкие углеводороды газовой смеси, и позволяет снизить энергозатраты. Способ включает в себя ступенчатую ректификацию смеси, отвод из первой ступени ректификации головного продукта, содержащего углеводороды Ci и С2 и часть двуокиси углерода, и кубового продукта, подачу кубового продукта на вторую ступень ректиИзобретение относится к технологии разделения газовых смесей, в частности к способу разделения содержащей двуокись углерода и легкие углеводороды газовой смеси, Цель изобретения - снижение энергозатрат . На чертеже изображена технологическая схема выполнения способа. фикации.отвод из второй ступени головного продукта, содержащего фракцию двуокиси углерода, и кубового продукта, содержащего фракции углеводородов Сз+, при этом разделение газовой смеси в первой ступени осуществляют при давлении 30-45 бар с получением кубового продукта, содержащего 95,7-96,6 мол.

Kapazitätsregelverfahren für ein kryogenisches Rektifikationssystem

Verfahren und Vorrichtung für die Herstellung von Kohlenoxid und Wasserstoff.

Verfahren und Vorrichtung zur Reinigung von Gasen

Verfahren und Vorrichtung zur Zerlegung eines Gasgemisches

VERFAHREN ZUR REINIGUNG VON STICKSTOFF-FLUORID.

Verfahren und Vorrichtung zur Entfernung von Spurenverunreinigungen aus Kohlendioxyd

Kryogenisches Destillationsverfahren zur Herstellung von Sauerstoff und Stickstoff

Kühlverfahren, der angewandte Kühlkreislauf und seine Anwendung in der Lufttrennung.

KRYOGENE RUECKGEWINNUNG VON HOCHREINEM WASSERSTOFF.

Separation of lower hydrocarbons comprises operating de-ethanizer at no less than de-methanizer pressure and combines head fractions for at least an interval

A de-ethanizer (E) is operated at the same, or a higher pressure than the de-methanizer (M). At least some of the 2C-rich fraction (9) withdrawn at the head of the de-ethanizer is supplied for at least an interval to the 1C-rich fraction (11, 11') withdrawn at the head of the de-methanizer. Preferred Features: The fluid fraction (5) withdrawn from the sump of the de-methanizer, which is supplied to the de-ethanizer, is made available at least at a pressure permitting admixture of the head product (8, 9) of the de-ethanizer to the head product (11, 11') of the de-methanizer, without an additional compression of the former. For an interval , especially when recovered 2C-rich fraction is not extracted, one or more of the following measures is adopted. The temperature of the recycle stream (2, 3''') supplied to the demethanizer (M) is increased by up to 20 K, preferably by 10-15 K. The quantity of this recycle is reduced, or supply is interrupted. The temperature of the hydrocarbon-rich fraction ...

Verfahren zum Verdichten von Boil-off-Gas

Es wird Verfahren zum Verdichten von bei der Lagerung von verflüssigtem Erdgas (LNG) anfallendem Boil-off-Gas beschrieben, wobei dieses ein- oder mehrstufig verdichtet und anschließend einer weiteren Verwendung zugeführt wird. Erfindungsgemäß erfährt das zu verdichtende Boil-off-Gas (1) mittels wenigstens eines Ejektors (Y) eine Druckerhöhung, wird angewärmt (E2) und ein- oder mehrstufig verdichtet (V), wobei als Treibgas (2) für den Ejektor (Y) ein Teilstrom des verdichteten Boil-off-Gases und/oder ein Gas verwendet wird, dessen Zusammensetzung im Wesentlichen identisch oder ähnlich derjenigen des Boil-off-Gases (1) ist und/oder dessen Vermischung mit dem Boil-off-Gas die beabsichtigte Verwendung des verdichteten Boil-off-Gases nicht beeinträchtigt.

Liquefaction of hydrocarbon stream, such as natural gas, with simultaneous recovery of liquid natural gas fraction comprises rectification and absorption process

A C2-rich stream (4) from the top of a column T1 is cooled before feeding (5) to a second column T2 for the removal of residual higher hydrocarbons, and the bottom C2 stream (6) from this column then recycled to the head of column T1. Stream (7) is methane rich ; a C3-C4 fraction is obtained from further rectification of stream (3). Preferred Features: A C4-C5 rich stream (8) is fed to the head of column T2. The rectification and absorption functions of columns T1 and T2 may be combined into a single column.

Verfahren zur Zerleggung unterhalb des Umgebungsdrucks mit Kühlvorrichtung mit einem Mehrkomponenten-Kühlmittel

RÜCKGEWINNUNG EINES SEKUNDÄREN ÄTHYLENSTROMES AUS EINEM ÄTHYLENREINIGUNGSVERFAHREN

TIEFTEMPERATURREKTIFIKATIONSVERFAHREN ZUM TRENNEN VON GASGEMISCHEN AUS BESTANDTEILEN, DEREN SIEDETEMPERATUREN WEIT AUSEINANDERLIEGEN

Lng facility with integrated ngl recovery for enhanced liquid recovery and product flexibility

Process for efficiently operating a natural gas liquefaction system with integrated heavies removal/natural gas liquids recovery to produce liquefied natural gas (LNG) and/or natural gas liquids (NGL) products with varying characteristics, such as, for example higher heating value (HHV) and/or propane content. Resulting LNG and/or NGL products are capable of meeting the significantly different specifications of two or more markets.

Method for separating off nitrogen and hydrogen from natural gas

The invention relates to a method for separating off nitrogen and lighter components, in particular hydrogen, carbon monoxide, neon and argon, from a feed fraction (e.g., natural gas) that is to be liquefied containing at least methane, nitrogen and hydrogen. The cooling and liquefaction of the feed fraction proceeds against the refrigerant or mixed refrigerant of at least one refrigeration cycle. In the inventive method, the feed fraction ( 1 ) is partially condensed (E 1 ), and separated in at least one rectification column (T) into a methane-rich fraction ( 6 ) and a fraction ( 4 ) containing nitrogen and lighter components. The methane-rich fraction ( 6 ) is subcooled. Additionally, cooling of the top condenser (E 2 ) of the rectification column (T) proceeds via a refrigerant or mixed refrigerant or a substream of the refrigerant or mixed refrigerant of at least one, refrigeration cycle ( 20 - 24 ).

Configurations and Methods of Heating Value Control in LNG Liquefaction Plant

NGL recovery from natural gas is achieved by processing the natural gas in a scrub column that operates at high pressure. A C3+ depleted vapor stream is generated from the vapor portion of partially condensed scrub column overhead and expanded to provide refrigeration for the vapor portion to so form a second reflux stream and the C3+ depleted vapor stream. The C3+ depleted vapor stream is then combined with another vapor portion of partially condensed column overhead to produce a lean liquefaction feed stream.

Process for separating and recovering NGLs from hydrocarbon streams

This process comprises using unconventional processing of hydrocarbons, e.g. natural gas, for recovering C2+ and NGL hydrocarbons that meet pipeline specifications, without the core high capital cost requirement of a demethanizer column, which is central to and required by almost 100% of the world's current NGL recovery technologies. It can operate in Ethane Extraction or Ethane Rejection modes. The process uses only heat exchangers, compression and simple separation vessels to achieve specification ready NGL. The process utilizes cooling the natural gas, expansion cooling, separating the gas and liquid streams, recycling the cooled streams to exchange heat and recycling selective composition bearing streams to achieve selective extraction of hydrocarbons, in this instance being NGLs. The compactness and utility of this process makes it feasible in offshore applications as well as to implementation to retrofit/revamp or unload existing NGL facilities. Many disparate processes and derivatives are anticipated for its use.

Cryogenic system for removing acid gases from a hydrocarbon gas stream, with removal of hydrogen sulfide

A system for removing acid gases from a raw gas stream includes an acid gas removal system (AGRS) and a sulfurous components removal system (SCRS). The acid gas removal system receives a sour gas stream and separates it into an overhead gas stream comprised primarily of methane, and a bottom acid gas stream comprised primarily of carbon dioxide. The sulfurous components removal system is placed either upstream or downstream of the acid gas removal system. The SCRS receives a gas stream and generally separates the gas stream into a first fluid stream comprising hydrogen sulfide, and a second fluid stream comprising carbon dioxide. Where the SCRS is upstream of the AGRS, the second fluid stream also includes primarily methane. Where the SCRS is downstream of the AGRS, the second fluid stream is principally carbon dioxide. Various types of sulfurous components removal systems may be utilized.

Methanol to olefins process

A process for chilling ethylene to required storage temperatures is disclosed, the process including: cooling an ethylene product from at least one of an ethylene production process and an ethylene recovery process via indirect heat exchange with a coolant at a temperature less than about −100° C. to decrease the temperature of the ethylene product; mixing a portion of the cooled ethylene product with methane to form the coolant; expanding at least one of the coolant, the methane, and the portion of the cooled ethylene to reduce a temperature of the coolant to less than −100° C. prior to the cooling; and feeding the heat exchanged coolant to at least one of the ethylene production process, the ethylene recovery process, and an open-loop refrigeration system.

Single-Unit Gas Separation Process Having Expanded, Post-Separation Vent Stream

A process comprising separating a hydrocarbon feed stream into a natural gas-rich stream and a liquefied petroleum gas (LPG)-rich stream using process equipment comprising only one multi-stage separation column, wherein the natural gas-rich stream has an energy content of less than or equal to about 1,300 British thermal units per cubic foot (Btu/ft 3 ), and wherein the LPG-rich stream has a vapor pressure less than or equal to about 350 pounds per square inch gauge (psig). A process comprising separating a hydrocarbon feed stream into a top effluent stream and a LPG-rich stream, and subsequently expanding the top effluent stream to produce a natural gas-rich stream. An apparatus comprising a multi-stage separation column configured to separate a hydrocarbon feed stream into a top effluent stream and a LPG-rich stream, and an expander configured to expand the top effluent stream and produce a natural gas-rich stream.

Method for fractionating a stream of cracked gas to obtain an ethylene-rich cut and a stream of fuel, and related installation

This method includes introducing a downstream stream ( 140 ) of cracked gas from a downstream heat exchanger ( 58 ) in a downstream separator ( 60 ) and recovering, at the head of the downstream separator ( 60 ), a high-pressure fuel gas stream ( 144 ). The method includes the passage of the stream ( 144 ) of fuel through the downstream exchanger ( 58 ) and an intermediate exchanger ( 50, 54 ) to form a reheated high-pressure fuel stream ( 146 ), the expansion of the reheated high-pressure fuel stream ( 146 ) in at least a first dynamic expander ( 68 ) and the passage of the partially expanded fuel stream ( 148 ) from the intermediate exchanger ( 50, 54 ) in a second dynamic expander ( 70 ) to form an expanded fuel stream ( 152 ). The expanded fuel stream ( 152 ) from the second dynamic expander ( 70 ) is reheated in the downstream heat exchanger ( 58 ) and in the intermediate heat exchanger ( 50, 54 ).

Method To Produce Liquefied Natural Gas (LNG) At Midstream Natural Gas Liquids (NGLs) Recovery Plants

A method to recover natural gas liquids (NGLs) from natural gas streams at NGL recovery plants. The present disclosure relates to methods using liquid natural gas (LNG) as an external source of stored cold energy to reduce the energy and improve the operation of NGL distillation columns. More particularly, the present disclosure provides methods to efficiently and economically achieve higher recoveries of natural gas liquids at NGL recovery plants.

Power and regasification system for lng

The present invention provides a power and regasification system based on liquefied natural gas (LNG), comprising a vaporizer by which liquid motive fluid is vaporized, said liquid motive fluid being LNG or a motive fluid liquefied by means of LNG; a turbine for expanding the vaporized motive fluid and producing power; heat exchanger means to which expanded motive fluid vapor is supplied, said heat exchanger means also being supplied with LNG for receiving heat from said expanded fluid vapor, whereby the temperature of the LNG increases as it flows through the heat exchanger means; a conduit through which said motive fluid is supplied from at least the outlet of said heat exchanger to the inlet of said; and a line for transmitting regasified LNG.

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 ...

SIMPLIFIED METHOD FOR PRODUCING A METHANE-RICH STREAM AND A C2+ HYDROCARBON-RICH FRACTION FROM A FEED NATURAL-GAS STREAM, AND ASSOCIATED FACILITY

A method comprising the cooling of the feed natural-gas () in a first heat exchanger () and the introduction of the cooled feed natural-gas () in separator flask (). The method further comprising dynamic expansion of a turbine input flow () in a first expansion turbine () and the introduction of the expanded flow () into a splitter column (). This method includes sampling at the head of the splitter column () a methane-rich head stream () and sampling in the compressed methane-rich head stream () a first recirculation stream (). The method comprises the formation of at least one second recirculation stream () obtained from the methane-rich head stream () downstream from the splitter column () and the formation of a dynamic expansion stream () from the second recirculation stream (). 1. A method for producing a methane-rich stream and a C hydrocarbon-rich fraction from a dehydrated feed natural-gas stream , consisting of hydrocarbons , nitrogen and of CO , advantageously having a C hydrocarbon molar content of more than 10% , the method being of the type comprising the following steps:cooling the feed natural-gas stream advantageously at a pressure of more than 40 bars in a first heat exchanger, and introducing the cooled feed natural-gas stream into a separator flask;separating the cooled natural gas stream in the separator flask and recovering an essentially gaseous light fraction and an essentially liquid heavy fraction;forming a turbine input flow from the light fraction;dynamically expanding the turbine input flow in a first expansion turbine, and introducing the expanded flow into an intermediate portion of a splitter column;expanding the heavy fraction and introducing the heavy fraction into the splitter column, the heavy fraction recovered in the separator flask being introduced into the splitter column without passing through the first heat exchanger;{'sub': 2', '2, 'sup': +', '+, 'recovering, at the foot of the splitter column, a C hydrocarbon-rich bottom ...

Methods for separating hydrocarbon gases

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

System and Method for Removing Excess Nitrogen from Gas Subcooled Expander Operations

A system and method for removing nitrogen from an intermediate stream in a gas subcooled process operation that processes natural gas into a sales gas stream and a natural gas liquids stream. The system and method of the invention are particularly suitable for use with gas subcooled process operations where the sales gas stream exceeds pipeline nitrogen specifications by up to about 3%, such as for reducing the nitrogen content of sales gas streams to levels permissible for pipeline transport.

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 ...

CONFIGURATIONS AND METHODS FOR OFFSHORE NGL RECOVERY

A natural gas two-column processing plant allows for recovery of at least 95% of C4 and heavier hydrocarbons, and about 60 to 80% of C3 hydrocarbons from a rich feed gas stream in which the first column (absorber) operates at a higher pressure than the second column, with the absorber receiving a compressed gas from the second column, and a turboexpander discharging a two-phase stream to the top of the absorber. Most typically, contemplated configurations and methods operate without the use of external refrigeration. 1. A method of processing a natural gas stream , comprising:cooling the natural gas stream and separating the cooled natural gas stream into a vapor portion and a liquid portion;using a turboexpander to reduce pressure of the vapor portion to thereby generate a two-phase stream having a liquid phase and a vapor phase;feeding the two phase stream to an absorber such that the liquid phase is a reflux in an absorber that produces an absorber overhead product and an absorber bottom product;reducing the bottom product in pressure and feeding the bottom product after pressure reduction into a fractionator that produces a fractionator bottom product and a fractionator overhead product; andcompressing the fractionator overhead product and using the compressed fractionator overhead product as a stripping gas in the absorber.2. The method of claim 1 , further comprising a step of using refrigeration content of the absorber overhead product for the step of cooling the natural gas stream.3. The method of or claim 1 , further comprising a step of using refrigeration content of the liquid portion and the bottom product after pressure reduction for the step of cooling the natural gas stream.4. The method of further comprising a step of compressing the absorber overhead product claim 1 , and using heat content of the compressed absorber overhead for reboiling the fractionator.5. A natural gas processing plant claim 1 , comprising:a heat exchanger configured to cool a ...

Mixing and Heat Integration of Melt Tray Liquids in a Cryogenic Distillation Tower

A cryogenic distillation tower for separating a feed stream. The tower includes a distillation section. A controlled freeze zone section is situated above the distillation section and forms a solid from the feed stream. The controlled freeze zone section includes a spray assembly in an upper section and a melt tray assembly in a lower section. The melt tray assembly includes at least one vapor stream riser that directs the vapor from the distillation section into liquid retained by the melt tray assembly, and one or more draw-off openings positioned to permit a portion of the liquid to exit the controlled freeze zone section. The portion of the liquid indirectly exchanges heat with a heating fluid. One or more return inlets return the portion of the liquid to the melt tray assembly after it has been heated in the heat exchanger. 1. A cryogenic distillation tower for separating a feed stream , the distillation tower comprising:a distillation section permitting vapor to rise upwardly therefrom;one or more lines for directing the feed stream into the distillation tower; a spray assembly in an upper section of the controlled freeze zone, and', at least one vapor stream riser that directs the vapor from the distillation section into liquid retained by the melt tray assembly, and', 'one or more draw-off openings positioned to permit a portion of the liquid retained by the melt tray assembly to exit the controlled freeze zone section;, 'a melt tray assembly in a lower section of the controlled freeze zone, wherein the melt tray assembly includes'}], 'a controlled freeze zone section situated above the distillation section, the controlled freeze zone constructed and arranged to form a solid from the feed stream, the controlled freeze zone section including'}a heat exchanger arranged to heat the portion of the liquid through indirect heat exchange with a heating fluid; andone or more return inlets that return the portion of the liquid to the melt tray assembly after the ...

METHOD FOR TREATING A FEED GAS STREAM AND ASSOCIATED INSTALLATION

The method includes cooling and liquefying a feed gas stream, separating a stream obtained from the feed gas stream, and recovering a treated gas stream and a natural gas liquid stream. The method further includes compressing the treated gas stream in order to form a compressed treated gas stream, and fractionating the natural gas liquid stream into a plurality of hydrocarbon fractions (). The method additionally includes withdrawing from the compressed treated gas stream, of a recycle stream, and reintroducing the recycle stream without cooling into the feed gas stream, into the cooled feed gas stream, or into a stream obtained from the cooled feed gas stream upstream of an expander. 1. A feed gas treating method comprising:supplying a feed gas stream and conveying the feed gas stream into a natural gas liquids extractor; cooling the feed gas stream,', 'expanding in an expander the cooled feed gas stream,', 'separating, in a separation column, at least one stream obtained from the cooled feed gas stream, and', 'recovering after separation, a treated gas stream and a natural gas liquid stream;, 'within the extractor'}compressing the treated gas stream in at least one compressor to form a compressed treated gas stream;fractionating, in a fractionator, the natural gas liquid stream into a plurality of hydrocarbon cuts;withdrawing a recycle stream in the compressed treated gas stream; the feed gas stream upstream of the extraction unit,', 'the cooled feed gas stream, or', 'a stream obtained from the cooled feed gas stream, upstream of the expander., 'reintroducing without cooling the recycle stream into at least one of2. The method according to claim 1 , comprising adjusting a flow rate of the reintroduced recycle stream as a function of the natural gas liquid content in the feed gas stream.3. The method according to claim 1 , wherein the molar flow rate of the reintroduced recycle stream is greater than 10% of the molar flow rate of the feed gas stream prior to the ...

Methanol to olefins process

A process for chilling ethylene to required storage temperatures is disclosed, the process including: cooling an ethylene product from at least one of an ethylene production process and an ethylene recovery process via indirect heat exchange with a coolant at a temperature less than about −100° C. to decrease the temperature of the ethylene product; mixing a portion of the cooled ethylene product with methane to form the coolant; expanding at least one of the coolant, the methane, and the portion of the cooled ethylene to reduce a temperature of the coolant to less than −100° C. prior to the cooling; and feeding the heat exchanged coolant to at least one of the ethylene production process, the ethylene recovery process, and an open-loop refrigeration system.

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 ...

CONFIGURATIONS AND METHODS FOR NITROGEN REJECTION, LNG AND NGL PRODUCTION FROM HIGH NITROGEN FEED GASES

Variable N2 content in feed gas ranging from 3 mol % to 50 mol % can be rejected from the process using a feed exchanger that is fluidly coupled with a cold separator and a single fractionation column to produce a nitrogen vent stream and streams that are suitable to be further processed for NGL recovery and LNG production. 1. A plant with a nitrogen removal unit and a natural gas liquids recovery unit , comprising:a feed gas source configured to provide a hydrocarbonaceous feed gas having a CO2 content of equal or less than 50 ppmv, a water content of equal or less than 0.1 ppmv, and a nitrogen content of at least 3 mol %;a heat exchanger configured to receive and cool the hydrocarbonaceous feed gas to a temperature that condenses C3+ components in the hydrocarbonaceous feed gas;a phase separator configured to receive the cooled hydrocarbonaceous feed gas and to separate the condensed C3+ components as a liquid stream from a vapor stream comprising C1, C2, and nitrogen;a conduit fluidly coupled to the phase separator and configured to transport the liquid stream to a natural gas liquids recovery unit;a refluxed fractionation column configured to receive the vapor stream and to produce a nitrogen-enriched overhead product and a nitrogen-depleted bottom product;a reflux condenser configured to partially condense the nitrogen-enriched overhead product using refrigeration of a pressure-reduced first portion of the nitrogen-depleted bottom product to thereby produce a liquid reflux to the fractionation column and a gaseous nitrogen vent stream; anda natural gas liquefaction unit fluidly coupled to the refluxed fractionation column and configured to receive the first portion of the nitrogen-depleted bottom product and a second portion of the nitrogen-depleted bottom product.2. The plant of claim 1 , wherein the heat exchanger is further configured to receive and cool the vapor stream to at least partially condense the vapor stream.3. The plant of claim 1 , wherein the ...

System and Method for Separating Wide Variations in Methane and Nitrogen

A system and method for removing nitrogen and producing a high pressure methane product stream from natural gas feed streams having wide variations in nitrogen and methane content are disclosed. Optional add-on systems may be incorporated into the nitrogen and methane separation to produce an NGL sales stream to reduce excess hydrocarbons in the nitrogen vent stream, or to recover helium. The system and method of the invention are particularly suitable for use with feed streams in excess of 50 MMSCFD and up to 300 MMSCFD and containing up to 100 ppm carbon dioxide. Typical power requirements for compressing the methane product stream to produce a suitably high pressure stream for sale are reduced according to the systems and methods of the invention. 1. A system for removing nitrogen and for producing a high pressure methane product stream from a first feed stream comprising nitrogen , methane , and other components , the system comprising:a first splitter wherein the first feed stream is divided into a second feed stream and a third feed stream;a first fractionating column wherein the second feed stream and the third feed stream are separated into a first overhead stream and a first bottoms stream;a second fractionating column comprising a condenser and a reboiler, wherein first overhead stream is separated into a second overhead stream and a second bottoms stream;a first heat exchanger for cooling the first feed stream upstream of the first splitter and for cooling the second feed stream upstream of the first fractionating column through heat exchange with the first bottoms stream and the first overhead stream;an external reboiler for cooling the third feed stream upstream of the first fractionating column through heat exchange with the first bottoms stream;wherein the methane product stream comprises the first bottoms stream and second bottoms stream;wherein the second overhead stream is a nitrogen vent stream; andwherein a duty for the condenser and a duty for ...

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.

SYSTEM AND METHOD FOR LIQUEFACATION OF NATURAL GAS

By using the power generated by an expander by an expansion of material gas, the outlet pressure of a compressor is increased, and a requirement on the cooling capacity of a cooler is reduced. The liquefaction system () for natural gas comprises a first expander () for generating power by expanding natural gas under pressure as material gas; a first cooling unit () for cooling the material gas depressurized by expansion in the first expander; a distillation unit () for reducing or eliminating a heavy component in the material gas by distilling the material gas cooled by the first cooling unit; a first compressor () for compressing the material gas from which the heavy component was reduced or eliminated by the distillation unit by using the power generated in the first expander; a second heat exchanger for exchanging heat between the material gas introduced into the first compressor and the material gas compressed by the first compressor; and a liquefaction unit () for liquefying the material gas compressed by the first compressor by exchanging heat with a refrigerant. 1. A method for cooling a natural gas feed comprising:a) reducing the pressure of the natural gas feed to produce a reduced pressure material gas;b) removing heavy components from the reduced pressure material gas to produce a top fraction and a bottom fraction;c) cooling the top fraction to produce a cooled top fraction;d) separating the cooled top fraction into a gas phase component and a liquid phase component;e) increasing the pressure of the gas phase component to produce a compressed material gas; andf) exchanging heat between the gas phase component and the compressed material gas to produce at least a cooled compressed material gas.2. The method of further comprising cooling the reduced pressure material gas of step (a) prior to removing heavy components in step (b).3. The method of further comprising at least partially liquefying the cooled compressed material gas of step (f).4. The method of ...

USING METHANE REJECTION TO PROCESS A NATURAL GAS STREAM

A process that is configured for treating natural gas mixed with carbon dioxide (CO) in high concentrations of 30% mole by volume or more. In one embodiment, the process comprises contacting a first feedstream comprising liquid natural gas (LNG) with a feedstock comprising methane to form an overhead product comprising methane vapor and a bottom product comprising carbon dioxide (CO). The embodiment can also comprise liquefying the methane vapor to form a LNG product and using the LNG product as the liquid natural gas (LNG) in the first feedstream. 1. A process for treating natural gas , said process comprising contacting a first feedstream comprising liquid natural gas (LNG) with a feedstock comprising methane to form an overhead product comprising methane and a bottom product comprising carbon dioxide (CO).2. The process of claim 1 , further comprising liquefying the overhead product to form a liquefied product.3. The process of claim 2 , further comprising directing a portion of the liquefied product as the first feedstream comprising liquid natural gas (LNG).4. The process of claim 1 , wherein the feedstock further comprises carbon dioxide (CO) in a concentration of 30% mole by volume or more.5. The process of claim 4 , wherein the methane in the overhead product has a concentration of 97% mole by volume or more.6. The process of claim 4 , wherein the carbon dioxide (CO) in the bottom product has a concentration of 80% mole by volume or more.7. The process of claim 1 , further comprising:{'sub': '2', 'distilling the bottom product to generate a vapor comprising methane and a liquid comprising carbon dioxide (CO).'}8. The process of claim 7 , further comprising:increasing the pressure of the vapor from a first pressure to a second pressure that is different from the first pressure.9. The process of claim 8 , further comprising:mixing the vapor at the second pressure into the feedstock.10. The process of claim 7 , further comprising:{'sub': '2', 'boiling the ...

System and Method for Separating Wide Variations in Methane and Nitrogen

A system and method for removing nitrogen and producing a high pressure methane product stream from natural gas feed streams having wide variations in nitrogen and methane content are disclosed. Optional add-on systems may be incorporated into the nitrogen and methane separation to produce an NGL sales stream to reduce excess hydrocarbons in the nitrogen vent stream, or to recover helium. The system and method of the invention are particularly suitable for use with feed streams in excess of 50 MMSCFD and up to 300 MMSCFD and containing up to 100 ppm carbon dioxide. Typical power requirements for compressing the methane product stream to produce a suitably high pressure stream for sale are reduced according to the systems and methods of the invention. 1. A system for removing nitrogen and for producing a methane product stream from a first feed stream comprising nitrogen and methane , the system comprising:a first splitter wherein the first feed stream is divided into a second feed stream and a third feed stream;a first fractionating column wherein the second feed stream and the third feed stream are separated into a first overhead stream and a first bottoms stream;a second fractionating column comprising a condenser and a second external reboiler, wherein the first overhead stream is separated into a second overhead stream and a second bottoms stream;a third fractionating column wherein the second overhead stream is separated into a third overhead stream and a third bottoms stream;a first heat exchanger for cooling the first feed stream upstream of the first splitter and for cooling the second feed stream upstream of the first fractionating column through heat exchange with the first bottoms stream and the first overhead stream, whereby the first bottoms stream and first overhead stream are heated in the first heat exchanger;a first external reboiler for cooling the third feed stream upstream of the first fractionating column through heat exchange with the first ...

Process for liquefaction of natural gas

A process and system for production of liquefied natural gas (LNG) from natural gas. The natural gas is first partially purified by removal of water and other contaminants, followed by partial chilling to freeze some contaminants and to allow for production of a purge stream to remove other contaminants. These contaminants may be removed from the stream. The process has advantages of low cost and improved removal of contaminants.

NATURAL GAS LIQUID FRACTIONATION PLANT WASTE HEAT CONVERSION TO POTABLE WATER USING MODIFIED MULTI-EFFECT DISTILLATION SYSTEM

A method of recovering heat from a Natural Gas Liquid (NGL) fractionation plant for production of potable water. The method includes heating a buffer fluid via a heat exchanger in to transfer heat from the NGL fractionation plant to the buffer fluid. The method includes heating water with the buffer fluid discharged from the heat exchanger to produce potable water via train distillation effects. 1. A method of recovering heat , via a waste heat recovery heat exchanger network having heat exchangers , from a Natural Gas Liquid (NGL) fractionation plant for producing potable water , the method comprising:heating a buffer fluid via a heat exchanger in the waste heat recovery network with a stream in the NGL fractionation plant, the NGL fractionation plant comprising a dehydrator, a distillation column, and a compressor; andproducing potable water via train distillation effects with heat from the buffer fluid.2. The method of claim 1 , wherein producing potable water with heat from the buffer fluid comprises heating brackish water with heat carried by the buffer fluid claim 1 , wherein a multi-effect-distillation (MED) system comprises the train distillation effects.3. The method of claim 2 , wherein the buffer fluid comprises water or oil claim 2 , and wherein the MED system comprises a modified MED system.4. The method of claim 1 , wherein the distillation column comprises a de-propanizer distillation column the stream comprises an overhead outlet stream from the de-propanizer distillation column claim 1 , or wherein the distillation column comprises a de-butanizer distillation column and the stream comprises an overhead outlet stream from the de-butanizer distillation column.5. The method of claim 1 , wherein the distillation column comprises a de-butanizer distillation column claim 1 , and wherein the stream comprises an overhead outlet stream from the de-butanizer distillation column or a bottoms outlet stream from the de-butanizer distillation column.6. The method ...

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 ...

Natural Gas Liquid Fractionation Plants Low Grade Waste Heat Conversion to Cooling, Power and Water

A method of recovering heat from a Natural Gas Liquid (NGL) fractionation plant for production of potable water. The method includes heating a buffer fluid via a heat exchanger in the NGL fractionation plant to transfer heat from the NGL fractionation plant to the buffer fluid. The method includes heating feed water with the buffer fluid discharged from the heat exchanger for production of potable water via a multi-effect-distillation (MED) system. The method may include producing potable water with heat from the buffer fluid in the MED system. 1. A method of recovering heat from a Natural Gas Liquid (NGL) fractionation plant for production of potable water , the method comprising:heating a buffer fluid via a heat exchanger in a NGL fractionation plant to transfer heat from the NGL fractionation plant to the buffer fluid, the NGL fractionation plant comprising a dehydrator column and a distillation column; andproducing potable water with heat from the buffer fluid in a multi-effect distillation (MED) system comprising train distillation effects.2. The method of claim 1 , comprising:storing the buffer fluid in a storage tank;flowing the buffer fluid from the storage tank to the heat exchanger; andflowing the buffer fluid from the MED system to the storage tank.3. The method of claim 1 , wherein producing potable water with heat from the buffer fluid comprises heating brackish water with heat from the buffer fluid claim 1 , wherein the MED system is a modified MED system claim 1 , and wherein the buffer fluid comprises water or oil.4. The method of claim 1 , wherein the NGL fractionation plant comprises a natural gas de-colorizing section comprising the distillation column as a natural gas de-colorizer distillation column claim 1 , and wherein heating the buffer fluid comprises heating the buffer fluid via the heat exchanger with heat from a pre-flash drum overhead outlet stream in the natural gas de-colorizing section.5. The method of claim 1 , wherein the NGL ...

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. ...

METHODS FOR PROVIDING REFRIGERATION IN NATURAL GAS LIQUIDS RECOVERY PLANTS

A process and plant for natural gas liquids (NGL) recovery includes a main heat exchanger, a cold gas/liquid separator, a separation or distillation column, and an overhead gas heat exchanger. A pressurized residue gas generated from an overhead gas stream removed the top of the separation or distillation column is expanded and used as a cooling medium in the overhead gas heat exchanger and the main heat exchanger. The expanded residue gas, used as a cooling medium, is then compressed up to a pressure to be combined with the overhead stream from the separation or distillation column. 1. A process for natural gas liquids (NGL) recovery comprising:introducing a natural gas feed stream into a main heat exchanger wherein the feed stream is cooled and partially condensed,introducing the partially condensed feed stream into a cold gas/liquid separator wherein the partially condensed feed stream is separated into a liquid fraction and a gaseous fraction,introducing the liquid fraction into a separation or distillation column,separating the gaseous fraction into a first portion and a second portion,cooling the first portion of the gaseous fraction in an overhead heat exchanger by indirect heat exchange with an overhead gaseous stream removed from the top of the separation or distillation column, and introducing the cooled and partially condensed first portion of the gaseous fraction into the separation or distillation column at a point above the introduction point of the liquid fraction into the separation or distillation column,expanding the second portion of the gaseous fraction and introducing the expanded second portion of the gaseous fraction into the separation or distillation column at a point above the introduction point of the liquid fraction into the separation or distillation column,removing a C2+ or C3+ liquid product stream (NGL) from the bottom of the separation or distillation column,removing the overhead gaseous stream from the top of the separation or ...

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 PRODUCTION OF CARBON MONOXIDE BY PARTIAL CONDENSATION

A process for separating a mixture of hydrogen, methane and carbon monoxide by cryogenic distillation. The mixture is cooled in a first heat exchanger and is partially condensed in at least one second heat exchanger which is a bottom reboiler of a first or second column of the column system and at least one portion of the liquid produced by the partial condensation is sent to an intermediate level of the first column. 1. A process for separating a mixture of hydrogen , methane and carbon monoxide by cryogenic distillation in a column system comprising a first column and a second column , comprising:i. cooling the mixture in a first heat exchanger and partially condensing at least one portion thereof in at least one second heat exchanger which is a bottom reboiler of the second column of the column system and at least one portion of the liquid produced by the partial condensation, or a liquid derived therefrom, by at least one step of partial condensation is sent to an intermediate level of the first column, only the at least one portion of the mixture and bottom liquid from the second column exchanging heat in the second heat exchanger, the vaporized bottom liquid being sent back to the column from which it originates,ii. withdrawing a hydrogen-enriched overhead gas from the first column and reheating the hydrogen-enriched overhead gas in the first heat exchanger,iii. withdrawing a liquid enriched in carbon monoxide and in methane from the bottom of the first column and sending it to at least one intermediate level of the second column,iv. withdrawing a methane-rich liquid from the bottom of the second column and withdrawing a fluid rich in carbon monoxide from the top of the second column, andv. producing refrigeration to keep the process cold by means of a refrigeration cycle.2. The process according to claim 1 , in which a portion of the cooled mixture is sent to the second heat exchanger which is a reboiler of the first column.3. The process according to claim 1 ...

Ethane recovery and ethane rejection methods and configurations

Contemplated plants for flexible ethane recovery and rejection by allowing to switch the top reflux to the demethanizer from residue gas to the deethanizer overhead product and by controlling the flow ratio of feed gas to two different feed gas exchangers. Moreover, the pressure of the demethanizer is adjusted relative to the deethanizer pressure for control of the ethane recovery and rejection.

Method of natural gas pretreatment

A method of natural gas treatment including introducing a natural gas containing stream into a dryer unit, thereby producing a treated natural gas containing stream. Introducing the treated natural gas containing stream into a nitrogen rejection unit, thereby producing a further treated natural gas stream as a nitrogen rejection unit product. Splitting the nitrogen rejection unit product into at least two portions, introducing the first portion of the further treated natural gas stream into a reformer unit as first part of feed, and introducing a second portion of the further treated natural gas stream into the dryer unit as a regeneration stream, thereby producing a regeneration waste stream. Introducing at least a portion of the regeneration waste stream into the reformer unit as second part of feed.

Facility For Producing Gaseous Biomethane By Purifying Biogas From Landfill Combining Membranes, Cryodistillation And Deoxo

A process and facility for producing gaseous methane by purifying biogas from landfill can include a VOC purification unit, at least one membrane, a CO2 purification unit, a cryodistillation unit comprising a heat exchanger and a distillation column, a deoxo, and a dryer.

PROCESS AND DEVICE FOR THE CRYOGENIC SEPARATION OF SYNTHESIS GAS

The invention relates to a process and device for the cryogenic separation of a methane-containing feed gas predominantly consisting of hydrogen and carbon monoxide, that is partially condensed in this case by cooling, in order to obtain a hydrogen-containing first liquid phase predominantly consisting of carbon monoxide and methane, from which first liquid phase, in an Hseparation column that is heated via a circulation heater, a second liquid phase is generated by separating off hydrogen, from which second liquid phase, in a CO/CHseparation column, a carbon monoxide-rich gas phase is obtained having a purity that permits release thereof as carbon monoxide product. It is characteristic in this case that a low-methane material stream is withdrawn from the Hseparation column and is then applied to the CO/CHseparation column as reflux. 1151811922829263412. Process for the cryogenic separation of a methane-containing feed gas () predominantly consisting of hydrogen and carbon monoxide , that is partially condensed in this case by cooling , in order to obtain a hydrogen-containing first liquid phase () predominantly consisting of carbon monoxide and methane , from which first liquid phase , in an Hseparation column (T) that is heated via a circulation heater () , a second liquid phase () is generated by separating off hydrogen () , from which second liquid phase , in a CO/CHseparation column (T) , a carbon monoxide-rich gas phase () is obtained having a purity that permits release thereof as carbon monoxide product () , characterized in that a low-methane material stream ( , ) is withdrawn from the Hseparation column (T) and is then applied to the CO/CHseparation column (T) as reflux.22612. Process according to claim 1 , characterized in that the low-methane material stream () is withdrawn in the gaseous state from the Hseparation column (T) and liquefied by cooling before introduction thereof into CO/CHseparation column (T).3261. Process according to claim 1 , ...

Refrigerant Recovery in Natural Gas Liquefaction Processes

Described herein is a method of removing refrigerant from a natural gas liquefaction system in which vaporized mixed refrigerant is withdrawn from the closed-loop refrigeration circuit and introduced into a distillation column so as to be separated into an overhead vapor enriched in methane and a bottoms liquid enriched in heavier components. Overhead vapor is withdrawn from the distillation column to form a methane enriched stream that is removed from the liquefaction system, and bottoms liquid is reintroduced from the distillation column into the closed-loop refrigeration circuit. Also described are methods of altering the rate of production in a natural gas liquefaction system in which refrigerant is removed as described above, and a natural gas liquefaction systems in which such methods can be carried out. 1. A method of removing refrigerant from a natural gas liquefaction system during shutdown , turndown , or other occurrences or upset situations , that uses a mixed refrigerant to liquefy and/or subcool natural gas , the mixed refrigerant comprising a mixture of methane and one or more heavier components , and the liquefaction system comprising a closed-loop refrigeration circuit in which the mixed refrigerant is circulated when the liquefaction system is in use , the closed-loop refrigeration circuit including a main heat exchanger through which natural gas is fed to be liquefied and/or subcooled by indirect heat exchange with the circulating mixed refrigerant , the method comprising:(a) withdrawing vaporized mixed refrigerant from the closed-loop refrigeration circuit; wherein the vaporized mixed refrigerant is withdrawn from a shell side of the main heat exchanger;(b) introducing the vaporized mixed refrigerant into a distillation column and providing reflux to the distillation column so as to separate the vaporized mixed refrigerant into an overhead vapor enriched in methane and a bottoms liquid enriched in heavier components;(c) withdrawing overhead vapor ...

Hydrocarbon Gas Processing

A process and an apparatus are disclosed for a compact processing assembly to improve the recovery of C(or C) and heavier hydrocarbon components from a hydrocarbon gas stream. The preferred method of separating a hydrocarbon gas stream generally includes producing at least a substantially condensed first stream and a cooled second stream, expanding both streams to lower pressure, and supplying the streams to a fractionation tower. In the process and apparatus disclosed, the tower overhead vapor is directed to an absorbing means and a heat and mass transfer means inside a processing assembly. A portion of the outlet vapor from the processing assembly is compressed to higher pressure, cooled and substantially condensed in a heat exchange means inside the processing assembly, then expanded to lower pressure and supplied, to the heat and mass transfer means to provide cooling. Condensed liquid from the absorbing means is fed to the tower. 1. In a process for the separation of a gas stream containing methane , Ccomponents , Ccomponents , and heavier hydrocarbon components into a volatile residue gas fraction and a relatively less volatile traction containing a major portion of said Ccomponents , Ccomponents , and heavier hydrocarbon components or said Ccomponents and heavier hydrocarbon components , in which process '(b) said substantially condensed first stream is expanded to a lower pressure whereby it is further cooled, and thereafter supplied at a top feed position on a distillation column that produces at least an overhead vapor stream and a bottom liquid stream;', '(a) said gas stream is treated in one or more heat exchange steps and at least one division step to produce at least a first stream that has been cooled under pressure to condense substantially all of it, and at least a second stream that has been cooled under pressure;'}(c) said cooled second stream is expanded to said lower pressure, and thereafter supplied to said distillation column at a mid-column ...

Hydrocarbon Gas Processing

A process and an apparatus are disclosed for a compact processing assembly to improve the recovery of C(or C) and heavier hydrocarbon components from a hydrocarbon gas stream. The preferred method of separating a hydrocarbon gas stream generally includes producing at least a substantially condensed first stream and a cooled second stream, expanding both streams to lower pressure, and supplying the streams to a fractionation tower. In the process and apparatus disclosed, the tower overhead vapor is directed to an absorbing means and a heat and mass transfer means inside a processing assembly. A portion of the outlet vapor from the processing assembly is compressed to higher pressure, cooled and substantially condensed in a heat exchange means inside the processing assembly, then expanded to lower pressure and supplied to the heat and mass transfer means to provide cooling. Condensed liquid from the absorbing means is fed to the tower. 1. In a process for the separation of a gas stream containing methane , Ccomponents , Ccomponents , and heavier hydrocarbon components into a volatile residue gas fraction and a relatively less volatile fraction containing a major portion of said Ccomponents , Ccomponents , and heavier hydrocarbon components or said Ccomponents and heavier hydrocarbon components , in which process(a) said gas stream is treated in one or more heat exchange steps and at least one division step to produce at least a first stream that has been cooled under pressure to condense substantially all of it, and at least a second stream that has been cooled under pressure;(b) said substantially condensed first stream is expanded to a lower pressure whereby it is further cooled, and thereafter supplied at a top feed position on a distillation column that produces at least an overhead vapor stream and a bottom liquid stream;(c) said cooled second stream is expanded to said lower pressure, and thereafter supplied to said distillation column at a mid-column feed ...

Hydrocarbon Gas Processing

A process and an apparatus are disclosed for a compact processing assembly to improve the recovery of C(or C) and heavier hydrocarbon components from a hydrocarbon gas stream. The preferred method of separating a hydrocarbon gas stream generally includes producing at least a substantially condensed first stream and a cooled second stream, expanding both streams to lower pressure, and supplying the streams to a fractionation tower. In the process and apparatus disclosed, the tower overhead vapor is directed to an absorbing means and a heat and mass transfer means inside a processing assembly. A portion of the outlet vapor from the processing assembly is compressed to higher pressure, cooled and substantially condensed in a heat exchange means inside the processing assembly, then expanded to lower pressure and supplied to the heat and mass transfer means to provide cooling. Condensed liquid from the absorbing means is fed to the tower. 1. In a process for the separation of a gas stream containing methane , Ccomponents , Ccomponents , and heavier hydrocarbon components into a volatile residue gas fraction and a relatively less volatile fraction containing a major portion of said Ccomponents , Ccomponents , and heavier hydrocarbon components or said Ccomponents and heavier hydrocarbon components , in which process(a) said gas stream is treated in one or more heat exchange steps and at least one division step to produce at least a first stream that has been cooled under pressure to condense substantially all of it, and at least a second stream that has been cooled under pressure;(b) said substantially condensed first stream is expanded to a lower pressure whereby it is further cooled, and thereafter supplied at a top feed position on a distillation column that produces at least an overhead vapor stream and a bottom liquid stream;(c) said cooled second stream is expanded to said lower pressure, and thereafter supplied to said distillation column at a mid-column feed ...

NATURAL GAS LIQUEFACTION WITH INTEGRATED NITROGEN REMOVAL

A natural gas liquefaction method and system having integrated nitrogen removal. Recycled LNG gas is cooled in a separate and parallel circuit from the natural gas stream in the main heat exchanger. Cooled recycled gas and natural gas streams are directed to a nitrogen rectifier column after the warm bundle. The recycle stream is introduced to the rectifier column above the natural gas stream and at least one separation stage is located in the rectifier column between the recycle stream inlet and the natural gas inlet. The bottom stream from the rectifier column is directed to a cold bundle of the main heat exchanger where it is subcooled. 1. A method for producing a nitrogen-depleted LNG product , the method comprising:(a) passing a natural gas feed stream through a first circuit of a main heat exchanger to cool the natural gas feed stream and liquefy at least a portion of the natural gas stream against a first refrigerant, thereby producing a first cooled LNG stream;(b) withdrawing the first cooled LNG stream from the main heat exchanger;(c) expanding the first cooled LNG stream to form a first reduced pressure LNG stream;(d) introducing the first reduced pressure LNG stream into a nitrogen rectifier column at a first location, the first location being located at a bottom end of the nitrogen rectifier column;(e) withdrawing a first LNG bottoms stream from the bottom end of the nitrogen rectifier column;(f) withdrawing an overhead stream from the nitrogen rectifier column;(g) cooling the first LNG bottoms stream to create a subcooled LNG stream;(h) directing at least a portion of the subcooled LNG stream to a flash drum or an LNG storage tank;(i) collecting at least one selected from the group of: a flash gas stream from the flash drum and a boil-off gas stream from the LNG storage tank to form a recycle stream;(j) passing the recycle stream through a second circuit of the main heat exchanger to cool the recycle stream and liquefy at least a portion of the recycle ...

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 , ...

HYDROCARBON GAS PROCESSING

A process and an apparatus are disclosed for the recovery of ethane, ethylene, propane, propylene, and heavier hydrocarbon components from a hydrocarbon gas stream. The stream is divided into first and second streams. The first stream is cooled to condense substantially all of it, expanded to lower pressure, and supplied to a fractionation tower at an upper mid-column feed position. The second stream is cooled sufficiently to partially condense it and separated into vapor and liquid streams. The vapor stream is divided into first and second portions. The first portion is cooled to condense substantially all of it, expanded to the tower pressure, and supplied to the tower at the top feed position. The second portion is expanded to the tower pressure and supplied to the fractionation tower at an intermediate mid-column feed position. The liquid stream is expanded to the tower pressure and supplied to the column at a lower mid-column feed position. The quantities and temperatures of the feeds to the fractionation tower are effective to maintain the overhead temperature of the fractionation tower at a temperature whereby the major portion of the desired components is recovered. 1. In a process for the separation of a gas stream containing methane , Ccomponents , Ccomponents , and heavier hydrocarbon components into a volatile residue gas fraction and a relatively less volatile fraction containing a major portion of said Ccomponents , Ccomponents , and heavier hydrocarbon components or said Ccomponents and heavier hydrocarbon components , in which process(a) said gas stream is cooled under pressure to provide a cooled stream;(b) said cooled stream is expanded to a lower pressure whereby it is further cooled; and(c) said further cooled stream is directed into a distillation column and fractionated at said lower pressure whereby the components of said relatively less volatile fraction are recovered;the improvement wherein prior to cooling, said gas stream is divided into ...

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- ...

System and Method for Natural Gas Liquid Production with Flexible Ethane Recovery or Rejection

A system and method for producing an NGL product stream in either an ethane retention or rejection mode. Rejection modes include (a) two heat exchange stages between a feed stream and first separator bottoms stream and cooling a side stream withdrawn from a fractionation tower through heat exchange with both the fractionation tower and second separator overhead streams; or (b) warming the first separator bottoms stream and fractionation overhead stream through heat exchange with the side stream prior to heat exchange with the feed stream, to achieve 4-15% ethane recovery and 97%+ propane recovery. In ethane retention mode, a portion of the feed stream and portions of a first separator overhead and bottoms streams are separately cooled through heat exchange with other process streams, including the entireties of a recycled residue gas and fractionation column overhead streams, resulting in around 99% ethane and around 100% propane recovery. 1. A system for processing a feed stream comprising methane , ethane , propane , and other components in an ethane rejection mode to produce an NGL product stream and a residue gas stream , system comprising:a first separator wherein the feed stream is separated into a first overhead stream and a first bottoms stream;a fractionation column wherein one or more fractionating column feed streams are separated into a second overhead stream and a second bottoms stream;a first heat exchanger and a second heat exchanger, wherein (1) at least a first portion of the feed stream is cooled in the first heat exchanger upstream of the first separator through heat exchange with (a) the first bottoms stream downstream from the second heat exchanger, (b) the second overhead stream downstream from the second heat exchanger, (c) a third overhead stream downstream from the second heat exchanger, and (d) a first side stream withdrawn from a mid-portion of the fractionation column and (2) the second overhead stream is warmed in the second heat ...

System and Method for Natural Gas Liquid Production with Flexible Ethane Recovery or Rejection

A system and method for processing an NGL product stream from a natural gas feed stream in either an ethane retention or ethane rejection mode utilizing heat exchange of particular process streams. In ethane rejection mode, there are preferably two stages of heat exchange between the feed stream and a first separator bottoms stream and a side stream withdrawn from a fractionation tower is cooled through heat exchange with both the fractionation tower and second separator overhead streams, and optionally with an external refrigerant, resulting in 5-15% ethane and at least 97% propane recovery. In ethane retention mode, a portion of the feed stream and portions of a first separator overhead and bottoms streams are preferably separately cooled through heat exchange with other process streams, including the entireties of a recycled residue gas and fractionation column overhead streams, resulting in around 99% ethane and around 100% propane recovery. 1. A system for processing a feed stream comprising methane , ethane , propane , and other components in either an ethane rejection mode or ethane retention mode to produce an NGL product stream and a residue gas stream , system comprising:a first separator wherein the feed stream is separated into a first overhead stream and a first bottoms stream;a fractionation column wherein the first overhead stream and first bottoms stream are separated into a second overhead stream and a second bottoms stream, wherein the residue gas stream comprises the second overhead stream and the NGL product stream comprises the second bottoms stream;a first heat exchanger for cooling at least a first portion of the feed stream prior to the first separator through heat exchange with a first set of other streams;a second heat exchanger for warming the second overhead stream prior to the first heat exchanger through heat exchange with a second set of other streams;wherein the first set of other streams comprises (1) the first bottoms stream, the ...

METHOD AND APPARATUS FOR AN IMPROVED CARBON MONOXIDE COLD BOX OPERATION

The present invention is directed to a method and system of separating carbon monoxide from syngas mixtures with low methane content by cryogenic means where a partial condensation cycle is generally employed, and more specifically towards providing a methane slip stream to the feed in order to reduce the potential for any carbon dioxide entering the cold box to freeze, thereby preventing plugging of the cold box heat exchanger. 1. A method for reducing carbon dioxide freezing in a partial condensation carbon monoxide cold box that separates a combined cold box syngas feed stream , comprising:cooling and partially condensing the combined cold box syngas feed stream in a process heat exchanger to produce a cooled and partially condensed syngas feed stream;separating the cooled and partially condensed syngas feed stream into a hydrogen rich vapor stream and a carbon monoxide rich liquid stream in a single-stage high-pressure separator;routing the carbon monoxide rich liquid stream to a downstream separation train to separate and form at least a CO-rich stream, a methane-rich liquid stream, and a flash gas vapor stream;{'sub': '2', 'wherein a methane-rich stream is added to the syngas feed upstream of a COfreeze zone in the process heat exchanger to increase the concentration of methane in the mixture thereby reducing carbon dioxide freezing in the partial condensation carbon monoxide cold box.'}2. The method of in which a methane-rich liquid stream is vaporized in the process heat exchanger to form a methane-rich gas stream.3. The method of in which at least a portion of the methane-rich gas stream is introduced into the combined cold box syngas feed before it enters the freeze zone in the process heat exchanger.4. The method of claim 1 , wherein the dew point temperature of the syngas feed is raised to about 103-113° K in the combined cold box feed stream.5. The method of claim 1 , wherein the methane-rich recycle stream contains 10-98% methane by volume.6. The ...

PROCESS FOR THE PRODUCTION OF DILUTE ETHYLENE

Processes and systems for recovery of a dilute ethylene stream are illustrated and described. More specifically, embodiments disclosed herein relate to processes and systems for separation of a dilute ethylene stream from an offgas or other vapor streams, where the ultra-low temperature refrigeration for the desired separations is provided by the offgas itself, and only moderately-low temperature externally supplied propylene refrigerants (for example, at −40° C. to 15° C.) are necessary. 1. A process for producing a dilute ethylene stream , the process comprising:{'sub': '3+', 'cooling and partially condensing a feedstock comprising hydrogen, methane, ethane, ethylene, and C hydrocarbons;'}separating the cooled and partially condensed feedstock into a vapor feed stream and a liquid feed stream, wherein the liquid feed stream comprises a portion of the ethylene contained in the feedstock;{'sub': '3+', 'separating the vapor feed stream in a deethanizer to recover an overhead stream and a bottoms product stream comprising the Chydrocarbons;'}separating the liquid feed stream into a first vapor fraction and a first liquid fraction;cooling and partially condensing the overhead stream via indirect heat exchange with a refrigerant comprising at least a portion of the first liquid fraction.2. The process of claim 1 , further comprising separating the cooled and partially condensed overhead stream into a liquid reflux stream and an overhead vapor dilute ethylene product stream.3. The process of claim 1 , further comprising separating the first liquid fraction claim 1 , after the indirect heat exchange claim 1 , into a second vapor fraction and a second liquid fraction.4. The process of claim 3 , further comprising compressing the first vapor fraction and the second vapor fraction to form a compressed refrigerant stream.5. The process of claim 4 , further comprising cooling the compressed refrigerant stream via indirect heat exchange with the second liquid fraction and ...

GAS SUBCOOLED PROCESS CONVERSION TO RECYCLE SPLIT VAPOR FOR RECOVERY OF ETHANE AND PROPANE

A design is provided to convert a gas subcooled process plant to a recycle split vapor process for recovering ethane and propane from natural gas. When in operation, the recovery of ethane and propane can exceed 97 to 99 wt. % of the stream being processed. A second smaller demethanizer column is added to the gas subcooled process plant as well as the addition of several cryogenic pumps. 1. A process for the separation of a gas stream containing methane , C2 components , C3 components , and heavier hydrocarbon components into a volatile residue gas fraction and a relatively less volatile fraction containing said C2. components , C3 components and heavier hydrocarbon components or said C3 components and heavier hydrocarbon components in a fractionation tower , comprising the steps of:dividing said gas stream into a gaseous first stream and a gaseous second stream;cooling said gaseous second stream under pressure sufficiently to partially condense;separating said partially condensed second stream to thereby provide a vapor stream and a condensed stream;expanding said vapor stream to a lower pressure and supplying it at a first mid-column feed position within a lower region of the fractionation tower;expanding at least a portion of the condensed stream to said lower pressure and supplying it to said fractionation tower at a second mid-column feed position;withdrawing a distillation stream from an upper region of the fractionation tower;sending said distillation stream to a lower region of a second fractionation tower that smaller than said first fractionation tower;removing a more volatile stream from said second fractionation tower to be sent to a residue gas stream; andremoving a less volatile stream from said second fractionation tower and sending at least a portion of said less volatile stream to said first fractionation tower,2. The process of wherein said second fractionation tower is about 10 to 50% of the height of said fractionation tower.3. The process of ...

System and Method for Separating Natural Gas Liquid and Nitrogen from Natural Gas Streams

A system and method for removing nitrogen and producing a high pressure methane product stream and an NGL product stream from natural gas feed streams where at least 90%, and preferably at least 95%, of the ethane in the feed stream is recovered in the NGL product stream. The system and method of the invention are particularly suitable for use with feed streams in excess of 5 MMSCFD and up to 300 MMSCFD and containing around 5% to 80% nitrogen. The system and method preferably combine use of strategic heat exchange between various process streams with a high pressure rectifier tower and the ability to divert all or a portion of a nitrogen rejection unit feed stream to optionally bypass a nitrogen fractionation column to reduce capital costs and operating expenses. 1. A system for removing nitrogen from a feed stream comprising nitrogen , methane , ethane , and other components to produce a methane product stream , an NGL product stream , and a nitrogen vent stream the system comprising:a first separator wherein the feed stream is separated into a first overhead stream and a first bottoms stream;a first fractionating column wherein the first overhead stream is separated into a second overhead stream and a second bottoms stream;an expander for expanding the first overhead stream prior to the first fractionating column;a second fractionating column wherein the first bottoms stream and second bottoms stream are separated into a third overhead stream and a third bottoms stream;a third fractionating column wherein at least a first NRU feed stream separated into a fourth overhead stream and a fourth bottoms stream;a first heat exchanger for cooling a first portion of the feed stream prior to the first separator and cooling a first portion of the second overhead stream prior to the third fractionating column through heat exchange with the fourth bottoms stream and a recycle refrigerant stream;a second heat exchanger for cooling the first portion of the second overhead ...

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 ...

UNSATURATED HYDROCARBON PRODUCTION APPARATUS

An unsaturated hydrocarbon production apparatus includes: a light collecting device configured to collect sunlight, and to convert the sunlight into solar heat; and a heating furnace configured to heat a raw material gas containing at least any one selected from the group consisting of methane and hydrogen, methane and oxygen, and ethane with the solar heat generated by the light collecting device to 700° C. or more and 2,000° C. or less. 1. An unsaturated hydrocarbon production apparatus , comprising:a light collecting device configured to collect sunlight, and to convert the sunlight into solar heat; anda heating furnace configured to heat a raw material gas containing at least any one selected from the group consisting of methane and hydrogen, methane and oxygen, and ethane with the solar heat generated by the light collecting device to 700° C. or more and 2,000° C. or less.2. The unsaturated hydrocarbon production apparatus according to claim 1 , further comprising a cooling unit configured to rapidly cool a generated gas generated in the heating furnace to 600° C. or less.3. The unsaturated hydrocarbon production apparatus according to claim 1 , wherein the heating furnace accommodates a catalyst for accelerating a reaction of the raw material gas to any one or both of ethylene and acetylene.4. The unsaturated hydrocarbon production apparatus according to claim 1 , further comprising a preheating unit configured to preheat the raw material gas with heat released from the heating furnace.5. The unsaturated hydrocarbon production apparatus according to claim 4 , further comprising a first heat exchange unit configured to subject the generated gas generated in the heating furnace and the raw material gas to heat exchange claim 4 ,wherein the raw material gas subjected to heat exchange in the first heat exchange unit is introduced into the preheating unit.6. The unsaturated hydrocarbon production apparatus according to claim 4 , further comprising a second heat ...

SYSTEM AND METHOD FOR CRYOGENIC PURIFICATION OF A FEED STREAM COMPRISING HYDROGEN, METHANE, NITROGEN AND ARGON

A system and method for cryogenic purification of a hydrogen, nitrogen, methane and argon containing feed stream to produce a methane free, hydrogen and nitrogen containing synthesis gas and a methane rich fuel gas, as well as to recover an argon product stream, excess hydrogen, and excess nitrogen is provided. The disclosed system and method are particularly useful as an integrated cryogenic purifier in an ammonia synthesis process in an ammonia plant. The excess nitrogen is a nitrogen stream substantially free of methane and hydrogen that can be used in other parts of the plant, recovered as a gaseous nitrogen product and/or liquefied to produce a liquid nitrogen product. 1. A method for purifying a hydrogen , nitrogen , methane and argon containing feed stream to produce a hydrogen and nitrogen containing synthesis gas and a methane fuel gas , the method comprising the steps of:conditioning the feed stream to a temperature near saturation at a pressure greater than about 300 psia;directing the conditioned feed stream to a synthesis gas rectification column configured to produce an hydrogen and nitrogen enriched overhead vapor stream and a methane-rich condensed phase stream proximate the bottom of the synthesis gas rectification column;directing the methane-rich condensed phase stream to a hydrogen stripping column configured to strip hydrogen from the methane-rich condensed phase stream and produce a hydrogen free methane bottom stream and a hydrogen enriched gaseous overhead;vaporizing the hydrogen free methane bottom stream to produce a vaporized or partially vaporized hydrogen free methane-rich stream;warming the hydrogen and nitrogen enriched overhead vapor stream via indirect heat exchange with the feed stream to produce the hydrogen and nitrogen containing synthesis gas; andwarming the vaporized or partially vaporized hydrogen free methane-rich stream via indirect heat exchange with the feed stream to produce the methane fuel gas.2. The method of claim 1 , ...

SYSTEM AND METHOD FOR CRYOGENIC PURIFICATION OF A FEED STREAM COMPRISING HYDROGEN, METHANE, NITROGEN AND ARGON

A system and method for cryogenic purification of a hydrogen, nitrogen, methane and argon containing feed stream to produce a methane free, hydrogen and nitrogen containing synthesis gas and a methane rich fuel gas, as well as to recover an argon product stream, excess hydrogen, and excess nitrogen is provided. The disclosed system and method are particularly useful as an integrated cryogenic purifier in an ammonia synthesis process in an ammonia plant. The excess nitrogen is a nitrogen stream substantially free of methane and hydrogen that can be used in other parts of the plant, recovered as a gaseous nitrogen product and/or liquefied to produce a liquid nitrogen product. 1. A method for purifying a stream comprising hydrogen , nitrogen , methane and argon to produce a hydrogen and nitrogen containing synthesis gas , a methane rich fuel gas , and at least one nitrogen product , the method comprising the steps of:conditioning the pre-purified feed stream to a temperature near saturation at a pressure greater than about 300 psia;directing the conditioned feed stream to a synthesis gas rectification column configured to produce an hydrogen and nitrogen enriched overhead vapor stream and a methane-rich condensed phase stream proximate the bottom of the synthesis gas rectification column;vaporizing the methane-rich condensed phase stream to produce a vaporized or partially vaporized methane-rich stream;directing the vaporized or partially vaporized methane-rich stream and a nitrogen reflux stream to a nitrogen rectification column configured to produce a nitrogen containing overhead vapor stream substantially free of methane, and a methane enriched liquid bottoms stream;warming at least a portion of the nitrogen containing overhead vapor stream via indirect heat exchange with the feed stream to produce a warm gaseous nitrogen stream and directing the warm gaseous nitrogen stream to a nitrogen recovery system to produce the at least one nitrogen product;warming the ...

SYSTEM AND METHOD FOR CRYOGENIC PURIFICATION OF A FEED STREAM COMPRISING HYDROGEN, METHANE, NITROGEN AND ARGON

A system and method for cryogenic purification of a hydrogen, nitrogen, methane and argon containing feed stream to produce a methane free, hydrogen and nitrogen containing synthesis gas and a methane rich fuel gas, as well as to recover an argon product stream, excess hydrogen, and excess nitrogen is provided. The disclosed system and method are particularly useful as an integrated cryogenic purifier in an ammonia synthesis process in an ammonia plant. The excess nitrogen is a nitrogen stream substantially free of methane and hydrogen that can be used in other parts of the plant, recovered as a gaseous nitrogen product and/or liquefied to produce a liquid nitrogen product. 1. A cryogenic purification system configured for purifying a hydrogen , nitrogen , methane and argon containing feed stream , the system comprising:a synthesis gas rectification column configured to receive the feed stream and produce a hydrogen and nitrogen enriched overhead vapor stream and a methane-rich condensed phase stream proximate the bottom of the synthesis gas rectification column;a hydrogen stripping column configured to receive the methane-rich condensed phase stream from the synthesis gas rectification column, strip hydrogen from the methane-rich condensed phase stream and produce a hydrogen free methane bottom stream and a hydrogen enriched gaseous overhead;a condenser configured to receive the hydrogen free methane bottom stream and a working fluid and to produce a vaporized or partially vaporized hydrogen free methane-rich stream; anda heat exchanger configured to (a) warm the hydrogen and nitrogen enriched overhead vapor stream via indirect heat exchange with the feed stream to produce a hydrogen and nitrogen containing synthesis gas; and (b) to warm the vaporized or partially vaporized hydrogen free methane-rich stream via indirect heat exchange with the feed stream to produce a methane fuel gas.2. The system of claim 1 , further comprising a compressor disposed upstream of ...

Heating Component to Reduce Solidification in a Cryogenic Distillation System

A method and a system for feeding a feed gas including methane (CH) and carbon dioxide (CO) to a cryogenic distillation column are provided herein. The method includes flowing a freeze zone COvapor stream into a freezing section of the column to produce an overhead stream that exits the column. The method includes heating the overhead stream via a heating component to reduce or prevent solidification of the COin the overhead stream. 1. A method comprising:{'sub': 4', '2, 'feeding a feed gas comprising methane (CH) and carbon dioxide (CO) to a cryogenic distillation column during start-up of the cryogenic distillation column;'}producing an acid gas rich bottom stream and a freeze zone vapor stream;flowing the freeze zone vapor stream into a freezing section of the cryogenic distillation column, wherein the freeze zone vapor stream exits the cryogenic distillation column as an overhead stream;{'sub': '2', 'heating the overhead stream via a heating component to form a heated overhead stream to reduce or prevent solidification of the COin the overhead stream;'}flowing the heated overhead stream into a heat exchanger to substantially reduce or prevent solidification in the heat exchanger;compressing the heated overhead stream via an overhead compressor to produce a high-pressure vapor; andreducing pressure of the high-pressure vapor to produce a liquid-vapor stream at an inlet of the cryogenic distillation column, wherein the liquid-vapor stream is introduced into the cryogenic distillation column as a refluxing spray.2. The method of claim 1 , wherein the heating of the overhead stream comprises raising a temperature of the overhead stream by about 0.5° F. to about 10° F.3. The method of claim 1 , comprising measuring a temperature of the heated overhead stream at an inlet of the heat exchanger.4. The method of claim 1 , comprising regulating an amount of heat emitted by the heating component via a control system claim 1 , wherein the control system maintains a ...

METHOD FOR DISTILLING A GAS STREAM CONTAINING OXYGEN

A process for producing biomethane by scrubbing a biogas feed stream includes introducing the feed gas stream into a pretreatment unit wherein a CO-depleted gas stream is partially separated from a COstream and an oxygen stream and is compressed to a pressure P1 above 25 bar abs. Subjecting the CO-depleted gas stream to cryogenic separation in a distillation column to separate a nitrogen stream and produce a CH-enriched stream, the distillation column comprising n plates, n being an integer between 8 and 100. Recovering a pressurized CH-enriched stream by pumping the CO-depleted gas stream to a pressure P2 above 25 bar absolute. 110-. (canceled)12. The process of claim 11 , wherein when C1 is greater than 0.5 mol % and less than or equal to 1 mol % claim 11 , the CO-depleted gas stream is introduced into the distillation column at the level of plate n claim 11 , plate n being the plate that is positioned the highest in said column.13. The process of claim 11 , wherein n is between 15 and 100 and wherein when C1 is less than or equal to 0.1 mol % claim 11 , the CO-depleted gas stream is introduced into the distillation column at a level between plate n-10 and plate n-5 claim 11 , platen being the plate that is positioned the highest in said column.14. The process of claim 11 , wherein P1 is greater than 50 bar absolute.15. The process of claim 11 , wherein step a) further comprises scrubbing the water from the gas stream compressed to the pressure P1.16. The process of claim 11 , wherein the separation of the COand of the oxygen from the feed gas stream is performed by a unit comprising at least two separating membrane stages.17. The process of claim 11 , wherein the pressure P2 is greater than 40 bar abs.18. The process of claim 11 , wherein claim 11 , during step b) claim 11 , the CO-depleted gas stream undergoes an expansion to a pressure P3 of between 15 bar abs and 40 bar abs prior to being introduced into said distillation column.19. The process of claim 11 , ...

NATURAL GAS LIQUID FRACTIONATION PLANT WASTE HEAT CONVERSION TO SIMULTANEOUS POWER AND POTABLE WATER USING KALINA CYCLE AND MODIFIED MULTI-EFFECT-DISTILLATION SYSTEM

Flowing a first buffer fluid and a second buffer fluid through a heat exchanger network thermally coupled to heat sources of a Natural Gas Liquid (NGL) fractionation plant, and transferring heat from the heat sources to the first buffer fluid and the second buffer fluid. Generating power via a first sub-system thermally coupled to the heat exchanger network and generating potable water from brackish water via a second sub-system thermally coupled to the heat exchanger network. 1. A method comprising:flowing a first buffer fluid and a second buffer fluid through a heat exchanger network thermally coupled to a plurality of heat sources of a Natural Gas Liquid (NGL) fractionation plant, wherein the heat exchanger network is a waste heat recovery heat exchanger network comprising heat exchangers;transferring heat, via the heat exchanger network, from the plurality of heat sources to the first buffer fluid and the second buffer fluid;generating power via a first sub-system thermally coupled to the heat exchanger network; andgenerating potable water from brackish water via a second sub-system thermally coupled to the heat exchanger network.2. The method of claim 1 , wherein the plurality of heat sources comprise:a first plurality of sub-units of the NGL fractionation plant, the first plurality of sub-units comprising a de-ethanizer section, a propane dehydration section, a de-propanizer section, a butane de-hydrator section, and a de-butanizer section;a second plurality of sub-units of the NGL fractionation plant, the second plurality of sub-units comprising a de-pentanizer section, an Amine-Di-Iso-Propanol (ADIP) regeneration section, a natural gas de-colorizing section, a propane vapor recovery section, and a propane product refrigeration section; anda third plurality of sub-units of the NGL fractionation a propane product sub-cooling section, a butane product refrigeration section, an ethane production section, and a Reid Vapor Pressure (RVP) control section.3. The ...

METHOD FOR PRODUCING PURE NITROGEN FROM A NATURAL GAS STREAM CONTAINING NITROGEN

A process for liquefying a natural gas feed stream including cooling a feed gas stream to obtain a liquefied natural gas stream; introducing the liquefied natural gas stream into a deazotization column to produce a liquefied natural gas stream and a nitrogen-enriched vapor stream; at least partially condensing at least part of the nitrogen-enriched vapor stream to produce a two-phase stream; introducing the two-phase stream into a phase-separating vessel to produce a first liquid stream and a first nitrogen-enriched gas stream; introducing at least part of the nitrogen-enriched gas stream into a distillation column thereby producing a second nitrogen-enriched stream containing less than 1 mol % of methane and a second liquid stream containing less than 10 mol % of nitrogen; wherein at least part of the liquefied natural gas stream is used to cool the at least part of the nitrogen-enriched vapor stream in said heat exchanger. 113.-. (canceled)15. The process of claim 14 , wherein the natural gas feed stream and a second coolant mixture are cooled by indirect heat exchange with at least one first coolant mixture to obtain a cooled natural gas and a second cooled coolant mixture claim 14 , and the cooled natural gas is then condensed and cooled by indirect heat exchange with at least the second cooled coolant mixture to obtain a liquefied natural gas.16. The process of claim 14 , wherein the second nitrogen-enriched stream contains less than 100 molar ppm of methane and the second liquid stream contains less than 4 mol % of nitrogen.172. The process of claim 14 , wherein the liquefied natural gas stream is cooled in a reboiling means of said deazotization column down to the temperature T.182. The process of claim 14 , wherein the stream cooled to the temperature T is expanded in an expansion means before being introduced into the deazotization column.19. The process of claim 14 , wherein at least part of the first liquid stream is used as reflux at the top of the ...

Process for Separating Hydrogen from an Olefin Hydrocarbon Effluent Vapor Stream

One or more specific embodiments disclosed herein includes a method for separating hydrogen from an olefin hydrocarbon rich compressed effluent vapor stream, employing a single heat exchanger, multiple gas-liquid separators, multiple expander/compressor sets, and a rectifier attached to a liquid product drum. 1. A process for the separation of hydrogen from an olefin hydrocarbon rich compressed effluent vapor stream from a dehydrogenation unit , which process comprises:a. cooling a compressed effluent vapor stream in a heat exchanger, wherein the heat exchanger comprises a warm section and a cold section;b. separating hydrogen from olefin and heavy paraffinic components in the cooled compressed effluent vapor stream in a first separator to provide a first vapor stream and a first liquid stream;c. cooling the first vapor stream in the heat exchanger;d. separating hydrogen from olefin and heavy paraffinic components in the cooled first vapor stream in a second separator to provide a second vapor stream and a second liquid stream;e. warming the second vapor stream in the heat exchanger;f. isentropically expanding, in a high-pressure expander, the second vapor stream, wherein the pressure and temperature of the second vapor stream are lowered;g. warming the second vapor stream in the heat exchanger;h. compressing, in a high-pressure compressor, the second vapor stream;i. cooling the second vapor stream in a first discharge cooler;j. dividing the second vapor stream into a gas product and a split stream;k. withdrawing a gas product;l. compressing, in a low-pressure compressor, the split stream;m. cooling the split stream in a second discharge cooler and further cooling the split stream in the heat exchanger;n. isentropically expanding, in a low-pressure expander, the split stream, wherein the pressure and temperature of the split stream are lowered;o. cooling a liquid paraffinic stream in the heat exchanger;p. combining the cooled liquid paraffinic stream with the ...

PROCESS FOR REMOVING NITROGEN FROM HIGH-FLOW NATURAL GAS

A process for separating the components of a gas mixture comprising methane, nitrogen, and at least one hydrocarbon having at least two carbon atoms, or a mixture of these hydrocarbons, including the following steps: a) introduction of a stream of the mixture to be treated into a demethanization of the gas mixture with at least N demethenization column; b) partial condensation of a gas mixture, comprising less than 1 mol % of hydrocarbons having at least two carbon atoms, extracted from the demethanization unit to obtain a liquid, at least a portion of which is treated in order to be extracted as denitrogenated natural gas and a second gas, c) introduction of the second gas into a nitrogen removal unit having N nitrogen removal columns. 16-. (canceled)8. The process as claimed in claim 7 , further comprising the additional step:d) treating said gas from step c) in a second nitrogen removal unit in order to produce a gaseous nitrogen stream comprising at most 2 mol % of methane and a gaseous methane stream comprising at most 5 mol % of nitrogen.9. The process as claimed in claim 8 , wherein the second nitrogen removal unit (B) comprises at most N−1 nitrogen removal columns.10. The process as claimed in claim 7 , wherein N is greater than or equal to 6.11. The process as claimed in claim 10 , wherein the second nitrogen removal unit comprises between N−5 nitrogen removal columns and N−1 nitrogen removal columns.12. The process as claimed in claim 7 , wherein the steps b) and c) are carried out at a temperature below −50° C. and the fluid is not reheated above −50° C. between step b) and step c). This application is a 371 of International PCT Application PCT/FR2015/052632, filed Oct. 1, 2015, which claims priority to French Patent Application No. 1552781, filed Apr. 1, 2015, the entire contents of which are incorporated herein by reference.The present invention relates to a process for separating the components of a gas mixture containing methane, nitrogen and ...

METHODS AND APPARATUS FOR GENERATING A MIXED REFRIGERANT FOR USE IN NATURAL GAS PROCESSING AND PRODUCTION OF HIGH PURITY LIQUEFIED NATURAL GAS

A novel method and system for liquefying and distilling raw natural gas into NGL and liquid methane (LNG) product streams, with at least one novel feature including the use of a mixed refrigerant comprising naturally occurring natural gas liquids that were recovered from the inlet gas stream being processed. Heat exchangers and distillation towers are configured to produce high purity liquefied natural gas (LNG) and NGL product streams, utilizing liquid NGL as the process refrigerant for both systems. 1. A method of operating a gas processing plant by using an NGL product from the gas processing plant as a mixed refrigerant for liquefying an inlet hydrocarbon gas being introduced to said gas processing plant , wherein said liquefied inlet hydrocarbon gas is further processed into the NGL product and a methane rich residue gas the method comprising:introducing the inlet hydrocarbon gas to a first heat exchange unit utilizing a mixed refrigerant to produce a cooled hydrocarbon gas having a liquid portion and a vapor portion;flowing the liquid and vapor portions to a first pressurized distillation tower;flowing a vapor product of hydrocarbons comprising methane rich residue gas from the first pressurized distillation tower;flowing NGL product from the first pressurized distillation tower;flowing said NGL product to at least the first heat exchange unit said NGL product to be used as the mixed refrigerant to aid in cooling of the hydrocarbon gas.2. The method of claim 1 , further comprising vaporizing at least a portion of the mixed refrigerant forming a mixed refrigerant vapor portion and a mixed refrigerant liquid portion claim 1 , separating the mixed refrigerant vapor portion from the mixed refrigerant liquid portion claim 1 , recompressing and condensing that vapor portion and recombining with the liquid portion to form a final NGL product.3. The method of claim 1 , wherein the NGL product contains a percentage of ethane and methane claim 1 , the method further ...

Treatment Plant for Hydrocarbon Gas Having Variable Contaminant Levels

A method of designing, constructing, and operating a hydrocarbon gas treatment plant is disclosed. A target hydrocarbon production range for a hydrocarbon gas meeting a required product specification is established. A cryogenic distillation column is designed and constructed with a vapor capacity to meet the target hydrocarbon production range. A variable feed refrigeration system is incorporated to cool an inlet feed of the hydrocarbon gas. The variable feed refrigeration system is designed to handle the target hydrocarbon production range and a wide range of contaminant concentrations in the inlet feed. A variable bottoms heating system is incorporated to handle heating duties associated with the wide range of contaminant concentrations in the inlet feed. A variable bottoms pumping system is incorporated to handle liquid flows associated with the wide range of contaminant concentrations in the inlet feed. 1. A method of treating , in a gas treatment plant , a feed gas stream comprising hydrocarbon gas and acid gas , the method comprising:(a) measuring the acid gas concentration in the feed gas stream at a first time to determine a first acid gas fraction;(b) cooling and liquefying at least a first portion of the feed gas stream in a first feed refrigeration unit;(c) separating the liquefied acid gas from the first portion of the feed gas stream to create a first vapor stream having a first composition;(d) separating, primarily by freezing, from the first vapor stream substantially all of the acid gas remaining in the first vapor stream to create a hydrocarbon gas stream;(e) melting the frozen acid gas;(f) removing the melted acid gas and the liquefied acid gas, which together form a bottoms stream;(g) removing the hydrocarbon gas stream; cooling and liquefying at least a first portion of the feed gas stream using the first feed refrigeration unit and cooling and liquefying at least a second portion of the acid gas stream using at least one additional feed ...

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.

LEAN GAS LNG HEAVIES REMOVAL PROCESS USING NGL

Disclosed herein are systems and processes for removing heavies during the liquefaction of a natural gas. The processes include dissolving the heavies in the natural gas by adding external natural gas liquid (NGL), followed by a staged removal of the natural gas liquid (NGL) and dissolved heavies. 1. A process for removing heavies from natural gas , the process comprising:combining a natural gas feed stream having a plurality of hydrocarbons including a quantity of heavies with an external natural gas liquid (NGL), in a vessel to form a mixture;cooling the mixture in a first chiller to generate a liquid portion and a gas portion;introducing the liquid portion and the gas portion into a first stripping column, wherein the gas portion is introduced towards a top of the first stripping column and the liquid portion is introduced below the gas;removing a liquid bottoms from the first stripping column, wherein the liquid bottoms comprises the external NGL and the quantity of heavies dissolved therein;introducing the liquid bottoms into a second stripping column and separating a recyclable NGL from the heavies dissolved therein; andrecycling the recyclable NGL to the vessel.2. The process in accordance with claim 1 , wherein the plurality of hydrocarbons of the natural gas feed stream further includes methane and nitrogen.3. The process in accordance with claim 2 , wherein the natural gas feed stream is a rich natural gas.4. The process in accordance with claim 2 , wherein the natural gas feed stream includes a lean natural gas.5. The process in accordance with claim 2 , wherein the natural gas feed stream includes a very lean natural gas.6. The process in accordance with claim 1 , wherein the external NGL comprises a Cand/or Chydrocarbon.7. The process in accordance with claim 1 , wherein the external NGL comprises a C-Calkane.8. The process in accordance with claim 1 , further comprising:determining the composition of the natural gas feed stream including the quantity ...

METHOD FOR VAPORIZING LIQUID PROPANE AND VAPORIZING APPARATUS USED THEREFOR

A method for vaporizing liquid propane to be supplied as a raw material to a naphtha cracking ractor. The method comprises: decompressing liquid propane to lower a vaporization point and vaporize at least a portion of the liquid propane; utilizing vaporization heat, generated during vaporization of the portion of liquid propane, as a refrigerant; compressing the vaporized propane gas to increase pressure of the propane gas and produce compressed propane gas; and preheating the compressed propane gas. By using this method, it is possible to reduce pressure of liquid propane to a significantly lower pressure than the related art method so that all the vaporization latent heat or vaporization heat included in liquid propane may be utilized as a refrigerant, while also reducing heat energy consumed in a preheat process before it is supplied to the naphtha cracking reactor. 1. A method for vaporizing liquid propane which is to be injected as a raw material into a naphatha cracking reactor , the method for vaporizing liquid propane comprising:S1) decompressing liquid propane to lower an initial vaporization point and vaporize at least a portion of the liquid propane;S2) utilizing vaporization heat, generated during vaporization of the portion of liquid propane, as a refrigerant;S3) compressing the vaporized propane gas to increase pressure of the propane gas and produce compressed propane gas; andS4) preheating the compressed propane gas.2. The method of claim 1 , wherein claim 1 ,{'sup': '2', 'in the decompression step S1), the pressure of the liquid propane is reduced to 7 kg/cmgauge or less, and in step S2), the vaporization heat generated during vaporization of the portion of the liquid propane is used as a refrigerant having a temperature less than 20° C.'}3. The method of claim 1 , wherein claim 1 ,{'sup': '2', 'in the decompression step S1), the pressure of the liquid propane is reduced to 1 kg/cmgauge or less, and in step S2), the vaporization heat generated ...

INTEGRATED METHODS AND CONFIGURATIONS FOR PROPANE RECOVERY IN BOTH ETHANE RECOVERY AND ETHANE REJECTION

A natural gas liquids (NGL) plant, the NGL plant comprising an absorber configured to provide an absorber overhead and an absorber bottoms, a stripper configured to produce a stripper overhead and a stripper bottoms, wherein the stripper is positioned downstream from the absorber and fluidly connected therewith such that the absorber bottoms can be introduced into the stripper, and a multi-pass heat exchanger configured to provide at least one reflux stream to the absorber, wherein the absorber and stripper are configured, in an ethane rejection arrangement, to provide the stripper overhead to a top of the absorber, and wherein the absorber and stripper are configured, in an ethane recovery arrangement, to provide the stripper overhead to a bottom of the absorber. 1. A natural gas liquids (NGL) plant , the NGL plant comprising:an absorber configured to provide an absorber overhead and an absorber bottoms;a stripper configured to produce a stripper overhead and a stripper bottoms, wherein the stripper is positioned downstream from the absorber and fluidly connected therewith such that the absorber bottoms can be introduced into the stripper; anda multi-pass heat exchanger configured to provide at least one reflux stream to the absorber wherein the multi-pass heat exchanger is configured, in the ethane recovery arrangement, to provide at least two reflux streams to the absorber,wherein the absorber and stripper are configured, in an ethane rejection arrangement, to provide the stripper overhead to a top of the absorber, and wherein the absorber and stripper are configured, in an ethane recovery arrangement, to provide the stripper overhead to a bottom of the absorber.2. (canceled)3. The NGL plant of claim 1 , wherein the stripper is configured claim 1 , in the ethane recovery arrangement claim 1 , as a demethanizer to provide a stripper bottoms comprising less than 1 vol % methane claim 1 , and the stripper is configured claim 1 , in the ethane rejection arrangement ...

METHOD AND SYSTEM FOR PROCESSING NATURAL GAS

Methods and systems for processing natural gas to meet gas pipeline specifications and/or recovering natural gas liquids (NGL). The natural gas is cooled and distilled such that propane and heavier components are produced as a bottoms NGL product, and inerts, methane, ethane, and other lighter portions are produced as a fuel gas grade/quality residue gas product stream. The gas can optionally be treated to remove hydrogen-sulfide and/or carbon dioxide. The NGL product can be split into a marketable propane and butane liquefied petroleum gas (LPG) liquid product and a natural gas condensate product. 1. A system for processing natural gas , the system comprising:a compressor for compressing the natural gas into a compressed gas;a cooling unit for cooling the compressed gas, a three-way valve downstream of the cooling unit;an ethylene glycol regeneration unit for injecting ethylene glycol into the cooling unit; 'a deethanizer comprising a top section and a bottom section; the top section configured to separate the heated hydrocarbon liquid into a top section gas and a top section liquid, the top section liquid sent to the bottom section; and the bottom section configured to separate the top section liquid into a bottom section gas and a bottom section liquid, the bottom section gas sent to the top section and the bottom section liquid sent to a natural gas liquids cooler, resulting in a natural gas liquids product for discharge to a natural gas liquids line;', 'a low-temperature gas-liquid phase separator for: separating the cooled compressed gas into a separator gas, a hydrocarbon liquid and a liquid water/ethylene glycol; directing the separator gas to the cooling unit before filtering and discharge to a natural gas product line as a natural gas product or after compression in a compressed natural gas compressor to a compressed natural gas line as a compressed natural gas product; directing the hydrocarbon liquid to at least one condenser for heating to form a heated ...

METHOD AND ARRANGEMENT FOR PRODUCING LIQUEFIED METHANE GAS (LMG) FROM VARIOUS GAS SOURCES

The method is carried out for continuously producing a liquefied methane gas (LMG) from a pressurized mixed methane gas feed stream. It is particularly well adapted for use in relatively small LMG distributed production plant, for instance those ranging from 400 to 15,000 MT per year, and/or when the mixed methane gas feed stream has a wide range of nitrogen-content proportions, including nitrogen being substantially absent. The proposed concept can also be very useful in the design of medium-scale and/or large-size plants, including ones where the nitrogen content always remains above a certain threshold. The methods and arrangements proposed herein can mitigate losses of methane gas when venting nitrogen, for instance in the atmosphere. 1. A method of continuously producing a liquefied methane gas (LMG) from a pressurized mixed methane gas feed stream , the mixed methane gas feed stream containing methane and a variable concentration of nitrogen within a range that includes nitrogen being substantially absent from the mixed methane gas feed stream , the method including the simultaneous steps of:(A) passing the mixed methane gas feed stream through a first heat exchanger and then through a second heat exchanger to condense at least a portion of the mixed methane gas feed stream, the first heat exchanger using a first cryogenic refrigerant and the second heat exchanger using a second cryogenic refrigerant;(B) sending the mixed methane gas feed stream coming out of the second heat exchanger though a mid-level inlet of a fractional distillation column;(C) when nitrogen is present in the mixed methane gas feed stream, separating the mixed methane gas feed stream inside the fractional distillation column into a methane-rich liquid fraction and a nitrogen-rich gas fraction;(D) withdrawing the methane-rich liquid fraction accumulating at a bottom of the fractional distillation column through a bottom outlet, the methane-rich liquid fraction constituting the LMG;(E) ...

NITROGEN RECOVERY APPARATUS AND METHOD OF RECOVERING NITROGEN

A nitrogen recovery apparatus for recovering nitrogen from natural gas comprises a separator having a liquid fraction port and a vapour fraction port in fluid communication with a split flow arrangement, the split flow arrangement having a sub-cooled fluid path and an expanded fluid path. A fractionating column has a reflux inlet port in fluid communication with the subcooled fluid path above a middle feed port thereof, the middle feed port being in fluid communication with the expanded fluid path. A bottom feed port of the fractionating column is in fluid communication with the liquid fraction port of the separator. A side reboiler circuit and a reboiler circuit are operably coupled to the fractionating column below the bottom feed port. A bottom hydrocarbon product stream path is in fluid communication with a bottom hydrocarbon port of the fractionating column. 1100100. A nitrogen recovery apparatus () for recovering nitrogen from natural gas , the apparatus () comprising:{'b': 110', '112', '112', '118', '120, 'a separator () having a liquid fraction port and a vapour fraction port in fluid communication with a split flow arrangement (), the split flow arrangement () having a sub-cooled fluid path () and an expanded fluid path ();'}{'b': 116', '124', '118', '130', '130', '120, 'a fractionating column () having a reflux inlet port () in fluid communication with the subcooled fluid path () above a middle feed port () thereof, the middle feed port () being in fluid communication with the expanded fluid path ();'}{'b': 114', '116', '110, 'a bottom feed port () of the fractionating column () in fluid communication with the liquid fraction port of the separator ();'}{'b': 132', '116', '114, 'a side reboiler circuit () operably coupled to the fractionating column () below the bottom feed port ();'}{'b': 140', '116', '132, 'a reboiler circuit () operably coupled to the fractionating column () below the side boiler circuit (); and'}{'b': 160', '162', '116, 'a bottom ...

Process for separating a component mixture and separation apparatus

A process for separating a component mixture comprising essentially hydrocarbons having two or two or more carbon atoms, methane and hydrogen using a distillation apparatus () is proposed. Fluid (a, c, e, g, i) from the component mixture is cooled stepwise to a first pressure level, with separation of first condensates (b, d, f, h, j) out of the fluid (a, c, e, g, i) in each case. Fluid (k) from the component mixture that remains in gaseous form thereafter is expanded to a second pressure level in an expander, giving a second condensate (I). Fluid from the first condensates (b, d, f, h, j) is expanded from the first pressure level to the second pressure level and fed together with the fluid from the second condensates into the distillation apparatus (10) which is being operated at the second pressure level. The present invention likewise provides a corresponding separation apparatus. 21013. Process according to claim 1 , wherein the distillation apparatus () has a condenser () which is operated at the temperature level above the second temperature level.31110. Process according to claim 2 , wherein the fluid from the condensates (b claim 2 , d claim 2 , f claim 2 , h claim 2 , j) is fed at least partly into the first and second distillation units () of the distillation apparatus ().412101312. Process according to claim 2 , wherein a gaseous stream of matter (m) is drawn off from the second distillation unit () of the distillation apparatus () claim 2 , cooled down in the condenser () and used to provide a liquid return stream to the second distillation unit ().5. Process according to claim 1 , wherein the liquid stream of matter (o) is expanded from the second pressure level to a pressure level below the second pressure level.6. Process according to claim 1 , wherein the fluid (a claim 1 , c claim 1 , e claim 1 , g claim 1 , i) from the component mixture (C2minus) is cooled down using an ethane and/or ethylene coolant at different pressure levels from the first ...

PROCESS AND APPARATUS FOR SWEETENING AND LIQUEFYING A GAS STREAM

A process and apparatus for liquefying a gas stream comprising hydrocarbons and sour species is provided in which the sour species are removed in liquefied form as the sweetened gas stream is progressively cooled to liquefaction temperatures. The process involves cooling the gas stream in a manner to produce a cooled gas stream comprising gaseous hydrocarbons and residual sour species. The cooled gas stream is then treated with a cold solvent to deplete the cooled gas stream of residual sour species. The resulting cooled sweetened gas stream is then further cooled to produce liquid hydrocarbons. 1. A process for liquefying a gas stream comprising hydrocarbons and sour species , the process comprising the steps of:a) cooling the gas stream by heat exchange with a first refrigerant stream to a temperature marginally greater than at which solidification of the sour species occurs;b) further cooling the gas stream to a first temperature between about −80° C. to −95° C. at a pressure between about 15 to 25 bar by expanding the gas stream as it is introduced into a vessel to produce a mixture of solid and/or liquid sour species and a cooled gas stream comprising gaseous hydrocarbons and residual sour species;c) separating the solid and/or liquid sour species from the cooled gas stream in the vessel;d) contacting the cooled gas stream with a solvent under temperature conditions close to or at the first temperature to deplete the cooled gas stream of residual sour species, thereby producing a cooled sweetened gas stream; ande) cooling the cooled sweetened gas stream to a second temperature below the methane boiling point by heat exchange with a second refrigerant stream to produce liquid hydrocarbons.2. The process according to claim 1 , wherein the first temperature is at or just below the temperature at which the sour species solidifies and/or condenses.3. The process according to claim 1 , wherein the first temperature is a temperature at which freezable hydrocarbon ...

SYSTEM AND METHOD FOR ARGON RECOVERY FROM THE TAIL GAS OF AN AMMONIA PRODUCTION PLANT

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 separating a feed gas comprising hydrogen , nitrogen methane and argon , the method comprising the steps of:conditioning the feed gas to a near saturated vapor state at a pressure of less than or equal to about 150 psia and a temperature near saturation;providing the conditioned feed gas to a rectification column;separating the conditioned feed gas in a rectification column to produce a methane-rich liquid column bottoms; an argon-depleted, hydrogen-nitrogen gas overhead; and an argon-rich side draw, the argon-rich side draw comprising trace amounts of hydrogen;removing the argon-rich side draw with trace amounts of hydrogen from an intermediate location of the rectification column as an argon-rich stream;directing the argon-rich stream to a hydrogen rejection arrangement;stripping the trace amounts of hydrogen from the argon-rich stream in the hydrogen stripping arrangement to produce an argon depleted stream and a hydrogen-free, nitrogen and argon containing stream; andseparating the argon from the hydrogen-free, nitrogen and argon containing stream in at least one distillation column to produce an argon product.2. The method of claim 1 , wherein the feed gas is a tail gas from an ammonia plant.3. The method of claim 1 , wherein the feed gas contains greater than about 50% nitrogen by mole fraction.4. The method of wherein the conditioned feed gas is at a pressure of less than or equal to about 50 psia.5. The method of claim 1 , ...

PHASE IMPLEMENTATION OF NATURAL GAS LIQUID RECOVERY PLANTS

Embodiments relate generally to systems and methods for operating a natural gas liquids plant in ethane rejection and in ethane recovery. A natural gas liquid plant may comprise an absorber configured to produce an ethane rich bottom stream and an ethane depleted vapor stream; a stripper fluidly coupled to the absorber configured to, during ethane rejection, fractionate the ethane rich bottom stream from the absorber into an ethane overhead product and a propane plus hydrocarbons product, and configured to, during ethane recovery, fractionate the ethane rich bottom stream into an ethane plus NGL stream and an overhead vapor stream; and an exchanger configured to, during ethane recovery, counter-currently contact the ethane rich bottom stream from the absorber with the ethane depleted vapor stream from the absorber, thereby heating the vapor stream and chilling the ethane rich bottom stream before the ethane rich bottom stream is fed to the stripper. 1. A natural gas liquid plant configured to operate in either ethane rejection or ethane recovery , the plant comprising:an absorber configured to produce an ethane rich bottom stream and an ethane depleted vapor stream;a stripper fluidly coupled to the absorber configured to, during ethane rejection, fractionate the ethane rich bottom stream from the absorber into an ethane overhead product and a propane plus hydrocarbons product, and configured to, during ethane recovery, fractionate the ethane rich bottom stream into an ethane plus NGL stream and an overhead vapor stream; andan expander configured to, during ethane recovery, expand a vapor portion of a feed gas to the plant, and feed the expanded stream to the absorber.2. The plant of claim 1 , further comprising an exchanger configured to claim 1 , during ethane recovery claim 1 , counter-currently contact the ethane rich bottom stream from the absorber with the ethane depleted vapor stream from the absorber claim 1 , thereby heating the vapor stream and chilling the ...

OVERHEAD RECYCLE PROCESS APPARATUS AND METHOD OF OVERHEAD RECYCLE PROCESSING OF HYDROCARBONS

An overhead recycle process apparatus () comprises a heat exchange arrangement () and a separator () in fluid communication with an absorber () and a de-ethaniser (), the absorber () having a reflux inlet port (). An ethane rectifier () in fluid communication with the de-ethaniser () is also provided, the de-ethaniser () being arranged to provide cooling by heat exchange to an overhead stream path () of the ethane rectifier (). The ethane rectifier () comprises a reflux drum () having an ethane outlet port () and a vapour phase outlet port () in fluid communication with the reflux inlet port () of the absorber (). 1100. An overhead recycle process apparatus () comprising:{'b': 116', '118', '120', '146', '150', '198, 'a heat exchange arrangement (, , , , , );'}{'b': 110', '104', '106', '104', '164, 'a separator () in fluid communication with an absorber () and a de-ethaniser (), the absorber () having a reflux inlet port (); and'}{'b': 170', '106', '106', '194', '170, 'an ethane rectifier () in fluid communication with the de-ethaniser (), the de-ethaniser () being arranged to provide cooling by heat exchange to an overhead stream path () of the ethane rectifier (); and'}{'b': 170', '182', '184', '185', '164', '104, 'the ethane rectifier () comprises a reflux drum () having an ethane outlet port () and a vapour outlet port () in fluid communication with the reflux inlet port () of the absorber ().'}2106197. An apparatus as claimed in claim 1 , wherein the de-ethaniser () comprises a bottom product outlet port () arranged to provide hydrocarbon fractions having a molecular weight heavier than a molecular weight of ethane.3. An apparatus as claimed in claim 1 , further comprising:{'b': 172', '174', '176', '178', '180, 'a side stream circuit (, , , , ); wherein'}{'b': 106', '172', '174', '174', '172', '106, 'the de-ethaniser () comprises a side stream inlet port () and a side stream outlet port (), the side stream outlet port () being disposed above the side stream ...

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 ...

REFINING ASSEMBLIES AND REFINING METHODS FOR RICH NATURAL GAS

Refining assemblies and methods for refining rich natural gas containing a first methane gas and other hydrocarbons that are heavier than methane gas are disclosed. In some embodiments, the assemblies may include a methane-producing assembly configured to receive at least one liquid-containing feed stream that includes water and rich natural gas and to produce an output stream therefrom by (a) converting at least a substantial portion of the other hydrocarbons of the rich natural gas with the water to a second methane gas, a lesser portion of the water, and other gases, and (b) allowing at least a substantial portion of the first methane gas from the rich natural gas to pass through the methane-producing assembly unconverted. The assemblies may additionally include a purification assembly configured to receive the output stream and to produce a methane-rich stream therefrom having a greater methane concentration than the output stream. 1. A refining assembly for rich natural gas containing a first methane gas and other hydrocarbons that are heavier than methane gas , comprising:a methane-producing assembly configured to receive at least one liquid-containing feed stream that includes water and rich natural gas and to produce an output stream therefrom by (a) converting at least a substantial portion of the other hydrocarbons of the rich natural gas with the water to a second methane gas, a lesser portion of the water, and other gases, and (b) allowing at least a substantial portion of the first methane gas from the rich natural gas to pass through the methane-producing assembly unconverted; anda purification assembly configured to receive the output stream and to produce a methane-rich stream therefrom having a greater methane concentration than the output stream.2. The refining assembly of claim 1 , wherein the methane-producing assembly includes:a vaporizer configured to receive and vaporize at least a portion of the at least one liquid-containing feedstream that ...

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 ...

Process for Separating Hydrogen from an Olefin Hydrocarbon Effluent Vapor Stream

One or more specific embodiments disclosed herein includes a method for separating hydrogen from an olefin hydrocarbon rich compressed effluent vapor stream, employing a single heat exchanger, multiple gas-liquid separators, multiple expander/compressor sets, and a rectifier attached to a liquid product drum. 1. A process for the separation of hydrogen from an olefin hydrocarbon rich compressed effluent vapor stream from a dehydrogenation unit , which process comprises:a. cooling a compressed effluent vapor stream in a heat exchanger;b. separating hydrogen from olefin and heavy paraffinic components in the cooled compressed effluent vapor stream in a first separator to provide a first vapor stream and a first liquid stream;c. cooling the first vapor stream in the heat exchanger;d. separating hydrogen from olefin and heavy paraffinic components in the cooled first vapor stream in a second separator to provide a second vapor stream and a second liquid stream;e. warming the second vapor stream in the heat exchanger;f. isentropically expanding the second vapor stream, wherein the pressure and temperature of the second vapor stream is lowered;g. dividing the second vapor stream into a first split stream and a second split stream;h. warming the first split stream in the heat exchanger;i. compressing the first split stream;j. cooling the first split stream in a first discharge cooler;k. withdrawing a gas product;l. cooling a liquid paraffinic stream in the heat exchanger;m. combining the cooled liquid paraffinic stream with the second split stream to provide a combined feed;n. vaporizing the combined feed in the heat exchanger;o. withdrawing the vaporized combined feed;p. lowering the pressure of the first liquid stream in a control valve;q. partially vaporizing the first liquid stream in the heat exchanger;r. flashing the partially vaporized first liquid stream in a liquid product drum to provide a hydrogen-rich gas, which travels to a rectifier connected to the liquid ...

PREPARING HYDROCARBON STREAMS FOR STORAGE

A system and process that are configured to prepare incoming hydrocarbon feedstocks for storage. For incoming ethane gas, the embodiments can utilize a plurality of vessels to distill the incoming feedstock to vapor and liquid ethane that is suitable for storage. The embodiments can direct the vapor to a demethanizer column that is downstream of the vessels and other components. The process can include stages for distilling an incoming feedstock at a plurality of vessels to form a vapor and a liquid for storage; directing the vapor to a demethanizer column; and circulating liquid from the demethanizer column back to the plurality of vessels. 1. A gas processing system , comprising: a distillation unit comprising a plurality of vessels, the plurality of vessels configured to form an incoming feedstock into a vapor and a liquid that meets specification for liquid ethane; and', 'a demethanizer column coupled with the plurality of vessels, the demethanizer column configured to form liquid from the vapor,, 'a fluid circuit configured to process an incoming feedstock comprising predominantly ethane liquid into a liquid that meets specification for liquid ethane, the fluid circuit comprisingwherein the fluid circuit is configured to direct the liquid from the demethanizer column to one of the plurality of vessels.2. The gas processing system of claim 11 , wherein the fluid circuit comprises:a mixing unit configured to form a mixture of the vapor with boil-off gas from a storage facility, wherein the fluid circuit is configured to direct the mixture to the demethanizer column.3. The gas processing system of claim 11 , wherein the plurality of vessels comprises:a first vessel configured to receive the incoming feedstock;a second vessel coupled with the first vessel and with the demethanizer column; anda third vessel coupled with the first vessel and the second vessel.4. The gas processing system of claim 1 , wherein the plurality of vessels comprises:a flash drum coupled ...

CRYOGENIC PROCESS FOR REMOVING NITROGEN FROM A DISCHARGE GAS

A process for producing biomethane by scrubbing a biogas feed stream including introducing a feed gas stream into a pretreatment unit wherein the gas stream is partially separated from a COstream and an oxygen stream, thereby producing a CO-depleted gas stream, which is compressed, thereby producing a pressurized CO-depleted gas stream; separating the pressurized CO-depleted gas stream by cryogenic separation by introducing the pressurized CO-depleted gas stream into a distillation column thereby producing a nitrogen stream and a CH-enriched stream, recovering a pressurized CH-enriched stream by pumping the CH-enriched stream; wherein the separation of the COstream and the oxygen stream from the feed gas stream is performed by a unit comprising at least two separating membrane stages in order that the CO-depleted gas stream comprises between 0.3 mol % and 2 mol % of CO. 18.-. (canceled)10. The process of claim 9 , further comprising scrubbing water from the pressurized CO-depleted gas stream.11. The process of claim 9 , wherein P1 is greater than 50 bar absolute.12. The process of claim 9 , wherein the pressure P2 is greater than 40 bar abs.13. The process of claim 9 , wherein the CO-depleted gas stream undergoes an expansion to a pressure P3 of between 15 bar abs and 40 bar abs prior to being introduced into said distillation column.14. The process of claim 13 , wherein prior to the expansion claim 13 , the CO-depleted gas stream is at least partially condensed in a heat exchanger.15. The process of claim 14 , wherein the CO-depleted gas stream is at least partially condensed in a heat exchanger counter-currentwise relative to the CH-enriched stream and to at least part of the nitrogen stream. This application is a 371 of International Application No. PCT/FR2018/053338, filed Dec. 17, 2018, which claims priority to French Patent Application No. 1762858, filed Dec. 21, 2017, the entire contents of which are incorporated herein by reference.The invention relates to a ...

PROCESSES FOR PRODUCING A NATURAL GAS STREAM

Processes for separating a natural gas stream from a liquid hydrocarbon stream. After being cooled, a feed stream may be separated in a first separation zone, into a gaseous stream and a liquid stream. A portion of each stream may be passed to a heat transfer zone to sub cool and then passed to a second separation zone having a distillation or fractionation column. An intermediate separation zone may be used to flash a gaseous stream from the sub-cooled liquid stream. The fractionation column may be operated to include ethane in either a residue gas stream rich in methane, or in the liquid hydrocarbon stream. 1. A process for separating a stream comprising hydrocarbons into at least two streams , the process comprising:cooling a hydrocarbon stream comprising mostly methane to provide a chilled hydrocarbon stream;separating the chilled hydrocarbon stream in a first separation zone into a gaseous stream and a liquid stream;separating a first portion of the liquid stream in a second separation zone into a residue gas stream and a liquid hydrocarbon stream;cooling a second portion of the liquid stream in a heat transfer zone to provide a cooled liquid stream;separating the cooled liquid stream in the second separation zone; and,separating one or more streams comprising the gaseous stream in the second separation zone.2. The process of wherein the second separation zone has an operating pressure at least 689 kPa less than an operating pressure of the first separation zone.3. The process of further comprising:separating a flashed gaseous stream from the cooled liquid stream in an intermediate separation zone; and,separating the flashed gaseous stream in the second separation zone.4. The process of wherein the intermediate separation zone has an operating pressure at least 1 claim 3 ,724 kPa psi less than an operating pressure of the first separation zone.5. The process of wherein the second separation zone has an operating pressure at least 2 claim 4 ,758 kPa lower than ...

Carbon Dioxide Recycle Stream Processing in an Enhanced Oil Recovery Process

A method for recovering natural gas liquids from a recycle stream having natural gas liquids includes receiving a carbon dioxide recycle stream that comprises carbon dioxide, natural gas, and the natural gas liquids. The carbon dioxide recycle stream is separated into a purified carbon dioxide recycle stream and a natural gas liquids stream. The purified carbon dioxide recycle stream comprises the carbon dioxide and the natural gas, and the natural gas liquids stream comprises the natural gas liquids. In another embodiment, a system comprises piping and a separator. The piping is configured to receive a recycle stream, and the separator is coupled to the piping and is configured to separate the recycle stream into a purified recycle stream and a natural gas liquids stream. 1. A set of process equipment for use in an enhanced oil recovery (EOR) process , the set of process equipment comprising:{'sub': 1', '8, 'a heat exchanger configured to receive a carbon dioxide recycle stream and cool the carbon dioxide recycle stream to produce a cooled carbon dioxide recycle stream, wherein the cooled carbon dioxide recycle stream comprises carbon dioxide, C-Chydrocarbons, and is substantially free of water;'}a multi-stage column configured to receive the cooled carbon dioxide recycle stream and produce a top effluent stream and a bottom effluent stream;{'sub': 1', '4, 'a single stage separator configured to receive the top effluent stream and produce a vapor stream and a liquid stream, wherein the vapor stream is transferred to the heat exchanger to produce a heated vapor stream, wherein the heated vapor stream comprises carbon dioxide and C-Chydrocarbons; and'}{'sub': 3', '8, 'an expander configured to receive the bottom effluent stream and produce an expanded bottom effluent stream, wherein the expanded bottom effluent stream comprises C-Chydrocarbons.'}2. The set of process equipment of claim 1 , further comprising a molecular sieve dehydrator configured to receive a feed ...

METHODS AND CONFIGURATION FOR RETROFITTING NGL PLANT FOR HIGH ETHANE RECOVERY

A natural gas liquid plant is retrofitted with a bolt-on unit that includes an absorber that is coupled to an existing demethanizer by refrigeration produced at least in part by compression and expansion of the residue gas, wherein ethane recovery can be increased to at least 99% and propane recovery is at least 99%, and where a lower ethane recovery of 96% is required, the bolt-on unit does not require the absorber, which could be optimum solution for revamping an existing facility. Contemplated configurations are especially advantageous to be used as bolt-on upgrades to existing plants. 1. A natural gas liquid plant bolt-on unit , comprising:an absorber configured to condense an ethane content from an overhead gas stream from a demethanizer using a cold lean residue gas to produce a liquid portion and a vapor portion, wherein the demethanizer is configured to receive the liquid portion as a first reflux;a reflux exchanger and a subcooler, wherein the reflux exchanger and the subcooler are configured to receive the vapor portion and use the vapor portion to provide cooling within the reflux exchanger and the subcooler; anda flow control valve configured to direct between about 70% to 90% of the vapor portion to: 1) reflux cooling, and 2) a second reflux of the demethanizer in the subcooler.2. The natural gas liquid plant bolt-on unit of claim 1 , wherein the overhead gas is at a pressure between about 250 psig to about 350 psig.3. The natural gas liquid plant bolt-on unit of claim 1 , wherein the absorber and the reflux exchanger are fluidly coupled to a residue gas compressor and the demethanizer claim 1 , and wherein the natural gas liquid plant is configured to provide at least a 99% ethane recovery.4. The natural gas liquid plant bolt-on unit of claim 1 , further comprising a reduction device comprising a Joule-Thompson valve claim 1 , wherein the reduction device is configured to receive the liquid portion and expand the liquid portion prior to the liquid ...

CRACKER MODULAR PROCESSING FACILITY

The various processes of an ethane cracker plant may be segmented into separate process blocks, which may be interconnected using fluid conduits and/or electrical connections. These process blocks may be directly connected, for example without an external piperack or other external piping interconnecting process blocks. Each process block may be formed of one or more modules The process blocks can include an ethane cracking furnace, a steam generation process, a water stripper, a water quench, a compression, a caustic scrubber, a drier, a deethanizer, an acetylene conversion, a demethanizer, a refrigerator, or a splitter. 1. A modular processing facility , comprising:at least 3 process blocks;wherein the at least 3 process blocks are non-identical process blocks;wherein the at least 3 process blocks each comprise one or more modules;wherein each process block of the at least 3 process blocks is interconnected to one or more of the other at least 3 process blocks; andwherein the at least 3 process blocks comprise the following: an ethane cracking furnace, a steam generation process, a water stripper, a water quench, a compression, a caustic scrubber, a drier, a deethanizer, an acetylene conversion, a demethanizer, a refrigerator, or a splitter,wherein the at least 3 process blocks comprise a compression process block, a caustic treatment process block, a drier process block, an acetylene conversion process block, and a deethanizer process block;wherein the compression process block abuts at least the caustic treatment process block;wherein the drier process block abuts at least the caustic treatment process block; andwherein the acetylene conversion process block abuts at least the deethanizer process block.2. The modular processing facility of claim 1 , wherein each of the at least 3 process blocks comprises its own integral E+I Distribution/System claim 1 , and wherein each of the at least 3 process blocks is configured to allow for independent pre-commissioning ...

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 cooled and separated into vapor and liquid portions to control subcooling of the vapor portion prior to feeding the second column. 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 four 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 and a fourth portion of the first column bottoms stream are 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 ...

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 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 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 ...

CONFIGURATIONS AND METHODS FOR NGL RECOVERY FOR HIGH NITROGEN CONTENT FEED GASES

A low cost and efficient design is used to convert a propane recovery process based on low nitrogen content feed gas to an ethane recovery process based on a high nitrogen feed gas while achieving over 95 mole % ethane recovery while maintaining a 99% propane recovery, and achieved without additional equipment. 1. A NGL plant configured to convert from a propane recovery configuration to an ethane recovery configuration , the NGL plant comprising:an absorber; anda fractionator,wherein the absorber is configured to produce an absorber overhead product and an absorber bottom product, wherein the fractionator is configured to produce a fractionator overhead product and a fractionator bottom product,wherein the absorber is configured to receive a vapor portion of the fractionator overhead product as a top reflux in the propane recovery configuration and to receive a stream comprising a first portion of a feed gas and a first portion of the absorber overhead product as the top reflux in the ethane recovery configuration;wherein the fractionator overhead product is configured to flow to a chiller in the propane recovery configuration and to a bottom of the absorber in the ethane recovery configuration; andwherein the absorber bottom product is configured to flow to a mid-section of the fractionator in the propane recovery configuration and to a top tray of the fractionator in the ethane recovery configuration.2. The NGL plant of claim 1 , wherein the fractionator overhead product is further configured to flow to a separator after flowing to the chiller in the propane recovery configuration.3. The NGL plant of claim 2 , wherein the separator is configured to separate the fractionator overhead into the vapor portion and a liquid portion in the propane recovery configuration.4. The NGL plant of claim 3 , wherein the fractionator is configured to receive a first portion of the liquid portion of the fractionator overhead product at the top tray of the fractionator in the ...

SYSTEM AND METHOD FOR LIQUEFACTION OF NATURAL GAS

By using the power generated by an expander by an expansion of material gas, the outlet pressure of a compressor is increased, and a requirement on the cooling capacity of a cooler is reduced. The liquefaction system () for natural gas comprises a first expander () for generating power by using natural gas under pressure as material gas; a first cooling unit () for cooling the material gas depressurized by expansion in the first expander; a distillation unit () for reducing or eliminating a heavy component in the material gas by distilling the material gas cooled by the first cooling unit; a first compressor () for compressing the material gas from which the heavy component was reduced or eliminated by the distillation unit by using power generated in the first expander; and a liquefaction unit () for liquefying the material gas compressed by the first compressor by exchanging heat with a refrigerant. 1. A system for the liquefaction of natural gas that cools the natural gas to produce liquefied natural gas , comprising:a first expander for generating power by expanding natural gas under pressure as material gas;a first cooling unit for cooling the material gas depressurized by expansion in the first expander;a distillation unit for reducing or eliminating a heavy component in the material gas by distilling the material gas cooled by the first cooling unit;a first compressor for compressing the material gas from which the heavy component was reduced or eliminated by the distillation unit by using the power generated in the first expander; anda liquefaction unit for liquefying the material gas compressed by the first compressor by exchanging heat with a refrigerant.2. The system for the liquefaction of natural gas according to claim 1 , further comprising a second cooling unit placed between the first compressor and the liquefaction unit to cool the material gas compressed by the first compressor.3. The system for the liquefaction of natural gas according to claim 1 ...

Process for Separating Hydrogen from an Olefin Hydrocarbon Effluent Vapor Stream

One or more specific embodiments disclosed herein includes a method for separating hydrogen from an olefin hydrocarbon rich compressed effluent vapor stream, employing a integrated heat exchanger, multiple gas-liquid separators, external refrigeration systems, and a rectifier attached to a liquid product drum. 1. A process for the separation of hydrogen from an olefin hydrocarbon rich compressed effluent vapor stream from a dehydrogenation unit , which process comprises:a. introducing a compressed effluent vapor stream into a processing unit;b. cooling the compressed effluent vapor stream in a heat exchanger;c. separating hydrogen from olefin and heavy paraffinic components in the cooled compressed effluent vapor stream in a first separator to provide a first vapor stream and a first liquid stream;d. cooling a first vapor stream in the heat exchanger;e. separating hydrogen from olefin and heavy paraffinic components in the cooled first vapor stream in a second separator to provide a second vapor stream and a second liquid stream;f. dividing the second vapor stream into a first split stream and a second split stream;g. warming the first split stream in the heat exchanger to produce a gas product;h. withdrawing the gas product from the processing unit;i. lowering the pressure of the second split stream in a control valve, wherein the temperature of the second spilt stream is reduced;j. cooling a liquid paraffinic stream in the heat exchanger;k. combining the cooled liquid paraffinic stream with the cooled second split stream to provide a combined feed;l. vaporizing the combined feed in the heat exchanger;m. withdrawing the vaporized combined feed;n. lowering the pressure of the first liquid stream in a control valve;o. partially vaporizing the first liquid stream in the heat exchanger;p. flashing the partially vaporized first liquid stream in a liquid product drum to provide a hydrogen-rich gas, which travels to a rectifier connected to the liquid product drum;q. ...

PROCESS AND APPARATUS FOR HEAVY HYDROCARBON REMOVAL FROM LEAN NATURAL GAS BEFORE LIQUEFACTION

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. 1. A process for removing high freeze point hydrocarbons , including benzene compounds , from a mixed feed gas stream , comprising:cooling the mixed feed gas stream in a first heat exchanger to condense at least a portion of the C3, C4 and C5 components and high freeze point hydrocarbons,separating the condensed C3, C4, C5 components and high freeze point hydrocarbons in a first separator to form a first liquid stream and a first gas stream,cooling the first gas stream in a second heat exchanger to condense at least a portion of the first gas stream,separating the condensed portion of the first gas stream in a second separator to form a methane-rich second gas stream as a top stream and a second liquid stream,feeding the first and second liquid streams to a first fractionator, and removing methane gas in a top stream and a third liquid stream as a bottom stream,removing a methane-rich product gas stream downstream from the top of the second separator,fractionating the third liquid stream in a fractionation train to obtain a recycle stream comprising at least one of C3 and components and C4 components, and a high freeze point hydrocarbon stream, andfeeding the recycle stream comprising at least one of C3 components and C4 components to the process at a location upstream from the first fractionator to lower the freeze point of the stream at the location where the recycle stream is introduced.2. The process of claim 1 , wherein the ...