КОНТАКТНЫЕ СТРУКТУРЫ

Изобретение относится к реакционным контактным структурам, используемым в реакторах алкилирования парафинов в качестве внутренней статической насадки системы, такой как диспергирующее устройство. Система для смешивания содержит вертикальный реактор для осуществления каталитических реакций перемешивания и расположенное в реакционной зоне диспергирующее устройство. Диспергирующее устройство выполнено в виде сетки, сплетенной с многожильным элементом, или вытянутого или раскатанного металла, переплетенного вместе с многожильным элементом, причем многожильную нить выбирают из инертных полимеров, каталитических полимеров, каталитических металлов или их смесей. Проволочная сетка обеспечивает структурную целостность системы, а также, по меньшей мере, 50 об.% открытого пространства в реакторах, необходимого, для перемещения паров и жидкостей через систему. Диспергирующее устройство может иметь форму листов, пучков или пакетов или размещаться внутри рамки. Настоящее изобретение позволяет более эффективно ...

ИСПОЛЬЗОВАНИЕ МЕДНЫХ КАТАЛИЗАТОРОВ НА МЕТАЛЛИЧЕСКИХ НОСИТЕЛЯХ ДЛЯ РИФОРМИНГА СПИРТОВ

Изобретение относится к дегидрированию или риформингу спиртов, в частности к способу дегидрирования первичного спирта, такого как метанол или этанол, для получения водорода, в частности для использования в топливном элементе с целью получения электрической энергии. В способе дегидрирования используют медьсодержащий катализатор, включающий в себя металлический носитель, при этом такой катализатор обладает повышенной активностью в газофазном риформинге первичных спиртов, также являются более устойчивыми и особенно активными для термического разложения этанола на водород, метан, монооксид углерода и диоксид углерода при умеренной температуре. Для решения поставленной задачи способ включает приведение в контакт исходной сырьевой смеси газов, содержащей спирт, с катализатором риформинга, чтобы получить смесь продуктов риформинга, содержащую водород, причем катализатор риформинга содержит металлический губчатый носитель и покрытие на меди, по меньшей мере, частично покрывающее поверхность данного ...

СПОСОБ ПОЛУЧЕНИЯ ВИНИЛАЦЕТАТА

Изобретение относится к способу получения винилацетата, где указанный способ включает: (а) взаимодействие в реакторе (i) от 65 до 80 мол.% этилена, (ii) от 10 до 25 мол.% уксусной кислоты и (iii) от 5 до 15 мол.% кислородсодержащего газа в присутствии палладиево-золотого катализатора с получением винилацетата; (b) выведение из реактора газового потока, содержащего этилен, уксусную кислоту, винилацетат, воду и диоксид углерода; (c) разделение газового потока на поток этилена, включающий этилен и диоксид углерода, и первичный поток винилацетата, включающий винилацетат, воду и уксусную кислоту; (d) разделение потока этилена на поток регенерированного этилена и поток диоксида углерода; (e) разделение первичного потока винилацетата на поток винилацетата и поток регенерированной уксусной кислоты; (f) повторную подачу в реактор на стадию (а) потока регенерированного этилена со стадии (d) и потока регенерированной уксусной кислоты со стадии (е); (g) измерение концентрации компонентов, принимающих ...

СПОСОБ И УСТАНОВКА ДЛЯ ПОЛУЧЕНИЯ МЕТАНОЛА С РЕЦИРКУЛЯЦИЕЙ УГЛЕВОДОРОДА

Настоящее изобретение относится к способу получения метанола, включающему подачу в реактор первого потока нагретого углеводородсодержащего газа, подачу в реактор кислородсодержащего газа, проведение в реакторе окисления нагретого потока углеводородсодержащего газа кислородом из кислородсодержащего газа с образованием потока продуктов, содержащего метанол и формальдегид; передачу тепла от потока продуктов первому потоку углеводородсодержащего газа, извлечение метанола из потока продуктов и извлечение СО2 и формальдегида из потока продуктов с образованием редуцированного потока продуктов, включающего углеводороды, путем их физического поглощения поглотителем, при этом первый поток включает по меньшей мере часть редуцированного потока продуктов, а также к установке (варианты) для осуществления данного способа. Предлагаемое изобретение позволяет получить целевой продукт эффективным и экономичным способом. 3 н. и 29 з.п. ф-лы, 5 ил.

СПОСОБ ПОВЫШЕНИЯ ПРОИЗВОДИТЕЛЬНОСТИ УСТАНОВКИ ДЛЯ ПОЛУЧЕНИЯ АММИАКА

Изобретение относится к области получения аммиака на основе риформинга углеводородов, в частности к способу повышения производительности установки для получения аммиака. Способ включает увеличение количества водорода, вырабатываемого секцией риформинга, посредством замены труб первичного риформера новыми трубами, имеющими меньшую толщину, для увеличения внутреннего диаметра труб, и установки источника кислорода для обогащения кислородом, поставляемым этим источником, воздуха, подаваемого на вторичный риформер, модернизацию воздушного компрессора посредством установки новых статорных и роторных частей, для увеличения расхода воздуха, подаваемого во вторичный риформер, при сохранении прежнего выходного давления, а также модернизацию секции удаления СО, компрессора синтез-газа, блока осушения синтез-газа и контура синтеза аммиака. Изобретение обеспечивает повышение производительности установки для получения аммиака. 7 з.п. ф-лы, 1 ил.

СПОСОБ И УСТРОЙСТВО ДЛЯ ОБОГАЩЕНИЯ ТЯЖЕЛОЙ НЕФТИ

Изобретение относится к способу обогащения тяжелой нефти до легкой нефти и устройству для его осуществления и их вариантам. Способ осуществляют путем обработки тяжелой нефти водородсодержащим газом, имеющим температуру выше примерно 649°С, в течение менее 10 сек. Обработанную тяжелую нефть охлаждают смешиванием обработанной тяжелой нефти с необработанной тяжелой нефтью и стабилизируют охлажденную смесь обработанной тяжелой нефти и необработанной тяжелой нефти в течение 1-60 мин. Описан также способ обогащения тяжелой нефти, содержащий стадии: а) введения окисляющего агента и водородсодержащего топлива в реакторный сосуд; b) введения тяжелой нефти в реакторный сосуд; с) воспламенения окисляющего агента и водородсодержащего топлива в присутствии тяжелой нефти с инициированием преимущественно газофазной реакции обогащения; и d) охлаждения реакции обогащения и с) стабилизацию охлажденной смеси обработанной тяжелой нефти и необработанной тяжелой нефти в течение 1-60 мин с получением обогащенной ...

УСТРОЙСТВО И СПОСОБ ИЗОМЕРИЗАЦИИ БЕНЗОЛСОДЕРЖАЩЕГО СЫРЬЯ

Изобретение относится к способу и устройству для гидрогенизации и дециклизации бензола и изомеризации С-С-парафинов в сырье, содержащем С-С-парафины и, по меньшей мере, 1 вес.% бензола. Устройство включает: (a) сырьевой трубопровод, не оборудованный конденсатором или входным отверстием для водорода, сообщающийся по жидкости с осушителем низкого давления; (b) трубопровод для потока, выходящего из осушителя, сообщающийся по жидкости с осушителем низкого давления, а также с первым трубопроводом для высушенного сырья и вторым трубопроводом для высушенного сырья; (c) трубопровод для обогащенного водородом газа, объединяющийся с первым трубопроводом для высушенного сырья с образованием трубопровода для объединенного сырья; (d) зону гидрогенизации, сообщающуюся по жидкости с трубопроводом для объединенного сырья и трубопроводом для потока из зоны гидрогенизации, причем зона гидрогенизации содержит катализатор гидрогенизации, который содержит компонент, выбранный из группы, состоящей из платины ...

УСТАНОВКА И СПОСОБ ДЛЯ ИЗОМЕРИЗАЦИИ ПОТОКА УГЛЕВОДОРОДОВ

Изобретение относится к установке для изомеризации потока углеводородов, богатого углеводородом С4 и/или по меньшей мере одним из углеводородов С5 и С6. Установка содержит: A) емкость, в которой находится текучая среда, содержащая газ, богатый водородом; B) устройство для перемещения текучей среды, принимающее из указанной емкости указанную текучую среду, содержащую газ, богатый водородом; C) по меньшей мере один осушитель, принимающий текучую среду, содержащую газ, богатый водородом, из указанного устройства для перемещения текучей среды, при этом указанный по меньшей мере один осушитель функционирует в первом режиме для осушки текучей среды, содержащей газ, богатый водородом, и во втором режиме в условиях регенерации, проводимой с помощью регенерирующего агента; D) реактор, сообщающийся, по меньшей мере, с одним осушителем для приема текучей среды, содержащей газ, богатый водородом, при этом по меньшей мере один осушитель сообщается с указанной емкостью, по меньшей мере, посредством подачи ...

СПОСОБ СИНТЕЗА МОЧЕВИНЫ С БОЛЬШИМ ВЫХОДОМ

Изобретение относится к способу синтеза мочевины из аммиака и двуокиси углерода с образованием карбамата аммония в качестве промежуточного химического соединения. Способ включает следующие стадии: a) взаимодействие аммиака и двуокиси углерода как такового или в виде карбамата аммония при молярном соотношении NH/COв диапазоне от 2,3 до 6, при температуре в диапазоне от 140 до 215°С и под давлением в диапазоне от 12 до 25 МПа с образованием первой жидкой смеси, содержащей мочевину, карбамат аммония, аммиак и воду; b) подача упомянутой первой жидкой смеси на стадию разложения-стриппинга, чтобы осуществить разложение, по крайней мере, кратного количества, в соответствии с предпочтительным примером осуществления настоящего изобретения от 50 до 99% карбамата аммония в аммиак и двуокись углерода, при работе под таким же давлением, как и на упомянутой стадии реакции (а) и при температуре в диапазоне от 160 до 240°С, одновременно подвергая упомянутую жидкую смесь стриппингу с образованием первой ...

СПОСОБ И УСТРОЙСТВО ДЛЯ ПРОИЗВОДСТВА АРОМАТИЧЕСКИХ КАРБОНОВЫХ КИСЛОТ (ВАРИАНТЫ)

Изобретение относится к усовершенствованным способам производства ароматических карбоновых кислот, включающим контактирование сырья, содержащего по меньшей мере один исходный замещенный ароматический углеводород, заместители которого способны окисляться до групп карбоновой кислоты, с газообразным кислородом в реакционной смеси жидкофазного окисления, содержащей монокарбоновую кислоту в качестве растворителя и воду, в присутствии каталитической композиции, содержащей по меньшей мере один тяжелый металл, эффективный для катализации окисления замещенного ароматического углеводорода до ароматической карбоновой кислоты, в секции реакции при повышенной температуре и давлении, эффективных для поддержания в жидком состоянии реакционной смеси жидкофазного окисления и образования ароматической карбоновой кислоты и примесей, содержащих побочные продукты окисления исходного ароматического углеводорода, растворенные или суспендированные в реакционной смеси жидкофазного окисления, и паровой фазы высокого ...

СПОСОБ МОДЕРНИЗАЦИИ УСТАНОВКИ ДЛЯ ПОЛУЧЕНИЯ МОЧЕВИНЫ

Изобретение относится к способу модернизации установки (1) для получения мочевины. Установка включает: реактор (2) для синтеза мочевины, средства (7, 8) для подачи аммиака и диоксида углерода в реактор (2) для синтеза мочевины, устройство (3) десорбции с помощью диоксида углерода для обработки реакционной смеси, выходящей из реактора (2) и содержащей мочевину, карбамат и несвязанный аммиак в водном растворе, с частичным разложением карбамата и частичным выделением несвязанного аммиака до получения таким образом, соответственно, потока, содержащего аммиак и диоксид углерода в паровой фазе, и потока, содержащего мочевину и оставшийся карбамат в водном растворе, секцию извлечения мочевины для обработки потока, выходящего из устройства (3) десорбции и содержащего мочевину и оставшийся карбамат в водном растворе, для выделения мочевины из оставшегося карбамата в водном растворе, по меньшей мере одно устройство (4) пленочной конденсации для частичной конденсации указанного потока, выходящего ...

СПОСОБ ЭКСПЛУАТАЦИИ УСТАНОВКИ ДЛЯ ПАРОВОГО РИФОРМИНГА

Изобретение касается способа эксплуатации установки (100) для парового риформинга. Способ осуществляют с помощью по меньшей мере одного реактора (2) для парового риформинга, где богатый углеводородом наполнитель (b) превращают с помощью водяного пара (с) в синтез-газ (k) с по меньшей мере одним подготовительным устройством (4-7), с помощью которого из синтез-газа (k) посредством отделения диоксида углерода (m, n) и монооксида углерода (t) получают богатую водородом фракцию (u), и с по меньшей мере одной адсорбционной установкой (9) с изменяющимся давлением, с помощью которой из богатой водородом фракции отделяют остаточный газ (h), причем используют по меньшей мере один рециркулирующий конденсатор (10), с помощью которого в первом режиме эксплуатации отделенный из синтез-газа (k) диоксид углерода (n, o) по меньшей мере частично примешивают к богатому углеводородом наполнителю (b). При этом во втором режиме эксплуатации рециркулирующий конденсатор (10) используют не для конденсации отделенного ...

УСТАНОВКА ОБЕССЕРИВАНИЯ С УЛУЧШЕННЫМ КОНТАКТОМ ЖИДКОСТЬ/ТВЕРДАЯ ФАЗА

Установка для удаления серы из углеводородсодержащего потока текучей среды, содержащая реактор с псевдоожиженным слоем, который включает ряд разнесенных по вертикали усиливающих контакт элементов, расположенных горизонтально в реакционной зоне, где обессеривание усиливается улучшением контакта между углеводородсодержащим потоком текучей среды и поглощающими серу твердыми частицами. Согласно изобретению на упомянутой установке осуществляют способ обессеривания, включающий четыре стадии: контактирование углеводородсодержащего потока текучей среды с твердыми тонкодисперсными частицами сорбента; контактирование, по меньшей мере, части углеводородсодержащего потока и частиц сорбента с рядом дефлекторов; контактирование наполненных серой частиц сорбента с кислородсодержащим регенерирующим потоком; контактирование регенерированных частиц сорбента с водородсодержащим восстанавливающим потоком; дополнительно включена стадия контактирования указанных восстановленных частиц сорбента с углеводородсодержащим ...

СПОСОБ ПОЛИМЕРИЗАЦИИ ВИНИЛСОДЕРЖАЩИХ МОНОМЕРОВ

Изобретение относится к способам полимеризации винилсодержащих мономеров, например мономерных винилгалогенидов. Полимеризацию осуществляют в реакционной смеси, представляющей собой водную суспензию. При этом из реакционной смеси выделяют по меньшей мере один продукт полимеризации, а реакционную смесь очищают и используют снова. Устройство содержит реакционный сосуд, соединенный с помощью соединительного средства для текучей среды с устройством для выделения из реакционной смеси продукта полимеризации, устройство для выделения из реакционной смеси продукта полимеризации, соединенное с помощью последующего соединительного средства для текучей среды с устройством для очистки реакционной смеси. Устройство для очистки реакционной смеси соединено с помощью соединительного средства с реакционным сосудом. Способ позволяет уменьшить количество отходов и/или сточных вод и получать полимер экологически чистым путем без ухудшения характеристик продукта полимеризации. 2 н. и 14 з.п. ф-лы, 4 ил., 10 ...

СПОСОБ ПОЛУЧЕНИЯ АММИАКА И ПРОИЗВОДНЫХ СОЕДИНЕНИЙ, В ЧАСТНОСТИ МОЧЕВИНЫ

Изобретение относится к способу и установке получения аммиака и производных соединений аммиака, такого как мочевина, из природного газового сырья, а также к способу модернизации установки для синтеза аммиака и мочевины. Способ включает конверсию природного газа в синтез-газ во входной части, синтез аммиака из синтез-газа в контуре синтеза, использование по меньшей мере части аммиака для получения производного соединения аммиака. Кроме того, способ осуществляют с энергопотребителями и потребителями тепла. При этом часть природного газового сырья используют для снабжения топливом газовой турбины, а энергию, вырабатываемую газовой турбиной, используют для обеспечения, по меньшей мере частично, потребности энергопотребителей в энергии. Далее из отходящего газа газовой турбины рекуперируют тепло и по меньшей мере часть тепла рекуперируют в виде низкотемпературного тепла для обеспечения технологическим теплом по меньшей мере одного из указанных потребителей тепла. При этом низкотемпературное ...

СПОСОБ ПОЛУЧЕНИЯ ЛЕГКИХ ОЛЕФИНОВ ИЗ КИСЛОРОДСОДЕРЖАЩИХ СОЕДИНЕНИЙ И УСТАНОВКА ДЛЯ ЕГО ОСУЩЕСТВЛЕНИЯ

Предлагаемое изобретение относится к способу получения легких олефинов, представляющих собой этилен, пропилен или их смеси из кислородсодержащих соединений в реакторе, которые содержат по меньшей мере, один атом кислорода и от 1 до 10 атомов углерода, характеризующемуся тем, что включает следующие стадии: а) подачу сырьевого потока кислородсодержащих соединений через распределитель потока в реактор с флюидизированной зоной превращения кислородсодержащих соединений с катализатором, содержащим молекулярное сито ELAPO, контактирование кислородсодержащих соединений с катализатором с целью получения смеси, содержащей легкие олефины, диолефины, непрореагировавшие кислородсодержащие соединения и другие побочные продукты; b) отделение непрореагировавших кислородсодержащих соединений и диолефинов от легких олефинов и побочных продуктов и с) возврат непрореагировавших кислородсодержащих соединений и диолефинов на вход в реактор, отдельно от сырьевого потока кислородсодержащих соединений. Также изобретение ...

ГИДРОИЗОМЕРИЗАЦИЯ ДВОЙНЫХ СВЯЗЕЙ БУТЕНОВ

Изобретение относится к способу для превращения С4 потока, содержащего 1-бутен и 2-бутен, предпочтительно в 2-бутен, включающему: смешивание указанного С4 потока с первым потоком водорода для образования вводимого потока, гидроизомеризацию указанного вводимого потока в присутствии первого катализатора гидроизомеризации, чтобы превратить по меньшей мере часть указанного 1-бутена в 2-бутен и получить выводимый продукт гидроизомеризации, отделение указанного выводимого продукта гидроизомеризации в колонне для каталитической дистилляции, имеющей верхний конец и нижний конец, для получения смеси 1-бутена у указанного верхнего конца, верхнего выводимого потока, включающего в себя изобутан и изобутилен, и нижнего потока, включающего 2-бутен, и гидроизомеризацию указанной смеси 1-бутена у указанного верхнего конца указанной колонны для каталитической дистилляции с использованием второго катализатора гидроизомеризации для получения добавочного 2-бутена в указанном нижнем потоке; где расположение ...

СПОСОБ ПРЕВРАЩЕНИЯ КИСЛОРОДСОДЕРЖАЩИХ СОЕДИНЕНИЙ В ОЛЕФИНЫ И УСТРОЙСТВО ДЛЯ ЕГО ОСУЩЕСТВЛЕНИЯ

Изобретение относится к способу превращения кислородсодержащих соединений, имеющих по меньшей мере от 1 до 10 атомов углерода в олефины, характеризующемуся тем, что включает следующие стадии: а) контактирование в реакторе кислородсодержащих соединений с флюидизированным катализатором, содержащим ELAPO, с превращением указанных соединений в углеводороды, причем в реакторе имеются, по меньшей мере две зоны: первая зона, в которой газ движется с большей скоростью, чем во второй зоне, в которой газ движется с меньшей скоростью, и b) введение продувочного газа, содержащего некоторое количество инертного газа, во вторую зону отдельно от сырьевого потока. Также изобретение относится к устройству для осуществления настоящего способа. Применение настоящего изобретения позволяет предотвратить накопление нежелательных побочных продуктов в застойных зонах внутри реактора и уменьшает количество кокса, осажденного на катализаторе в застойных зонах или на поверхности внутри этих зон. 2 н. и 6 з.п. ф-лы ...

СПОСОБ ПОЛУЧЕНИЯ МОЧЕВИНЫ И УСТАНОВКА ДЛЯ ЕГО ОСУЩЕСТВЛЕНИЯ

Изобретение относится к получению мочевины из аммиака и диоксида углерода. В реакторе (112) синтеза при заданном высоком давлении в результате реакции между NH3 и CO2 получают реакционную смесь, содержащую мочевину, карбамат аммония и несвязанный аммиак в водном растворе, из которой извлекают карбамат аммония и аммиак с их последующей рециркуляцией в реактор (112) синтеза. Карбамат аммония и аммиак извлекают из реакционной смеси на технологических стадиях разложения карбамата аммония на NH3 и СО2 и их отпарки и на последующей технологической стадии их повторной конденсации с получением карбамата аммония, который рециркулирует в реактор синтеза. Реакционная смесь, полученная в результате реакции между аммиаком и диоксидом углерода, подается на технологические стадии разложения и отпарки посредством насоса. Обеспечивается изменение производственной мощности путем изменения параметров насоса, возможность горизонтальной компоновки, снижение затрат на обслуживание и увеличение безопасности.

МНОГОРЕАКТОРНАЯ ХИМИЧЕСКАЯ ПРОИЗВОДСТВЕННАЯ СИСТЕМА

Изобретение относится к многореакторной системе и способу для производства продукта, получаемого по ограничиваемой равновесием реакции. Система содержит реакторную емкость, выполненную с возможностью выдерживания рабочих температур и давлений реакции получения продукта, причем реакторная емкость содержит множество реакционных зон, образованных в реакторной емкости с помощью разделительных стенок, емкость сепарации, выполненную с возможностью выдерживания рабочих температур и давлений реакции получения продукта, причем емкость сепарации содержит множество зон сепарации, образованных в емкости сепарации с помощью разделительных стенок, и реакторные комплекты, содержащие множество теплообменников подаваемый поток/отходящий поток. Причем теплообменник первого реакторного комплекта функционально соединен с реакционной зоной подаваемым потоком, а теплообменники остальных реакторных комплектов функционально соединены с реакционной зоной возвращаемым потоком. Изобретение обеспечивает экономику ...

СПОСОБ И УСТРОЙСТВО ДЛЯ ПОЛУЧЕНИЯ МОЧЕВИНОВОЙ КОНСИСТЕНТНОЙ СМАЗКИ

Изобретение относится к способу получения мочевиновой консистентной смазки, который осуществляют в устройстве, использующем экструдер и содержащем несколько реакционных зон, смонтированных в ряд и связанных по текучей среде. При этом устройство включает в себя: (а) первую зону подачи; (b) вторую зону подачи; (с) первую зону реакции-смешивания и (d) зону охлаждения-смешивания, причем указанные зоны расположены в устройстве в порядке (а), (b), (с), (d), и способ включает введение первого исходного компонента в первую зону подачи (а); введение второго исходного компонента во вторую зону подачи (b); реакцию первого и второго компонентов в первой зоне реакции-смешивания (с) и охлаждение и смешивание продукта первой зоны реакции-смешивания в зоне охлаждения-смешивания (d) с получением мочевиновой консистентной смазки. Также изобретение относится к устройству для осуществления данного способа. Настоящее изобретение обладает такими преимуществами, как технологическая стабильность, обладает трансформируемостью ...

РЕГУЛИРОВАНИЕ В СПОСОБЕ ПОЛУЧЕНИЯ АБСОРБИРУЮЩИХ ВОДУ ПОЛИМЕРНЫХ ЧАСТИЦ В НАГРЕТОЙ ГАЗОВОЙ ФАЗЕ

Настоящее изобретение относится к способу получения абсорбирующих воду полимерных частиц. Описан способ получения абсорбирующих воду полимерных частиц, когда образуются содержащие мономеры капли, которые содержат не менее чем один этиленовый ненасыщенный мономер, содержащий по крайней мере одну кислотную группу, не менее чем одно средство для образования сетчатой структуры, по крайней мере один инициатор и воду, мономеры полимеризуются в окружающей капли нагретой газовой фазе и газ проходит через реактор полимеризации, при этом температуру выходящего из реактора полимеризации газа регулируют, отличающийся тем, что регулирование осуществляется посредством предварительного нагрева проходящего через реактор газа перед входом в реактор с помощью соответствующего теплообменника. Технический результат - способ, позволяющий получать абсорбирующие воду полимерные частицы постоянного высокого качества. 7 з.п. ф-лы, 1 табл., 6 пр.

СПОСОБ И УСТРОЙСТВО ДЛЯ ДЕПОЛИМЕРИЗАЦИИ

... 1. Способ регенерации мономерных сложных эфиров замещенной или незамещенной акриловой кислоты, мономерного стирола и/или мономерных производных стирола из содержащего соответствующие структурные единицы полимерного материала, причем осуществляют контакт полимерного материала с теплоносителем в обогреваемом реакторе (1; 51), теплоноситель и полимерный материал в реакторе (1; 51) приводят в движение и образующийся в реакторе (1; 51), содержащий мономер газ выводят из реактора (1; 51), причем теплоноситель состоит из множества сферических частиц (67), прежде всего обладающих диаметром от 0,075 до 0,25 мм. 2. Способ по п.1, причем полимерный материал содержит акриловые соединения и средняя температура частиц (67) теплоносителя в реакторе (1; 51) составляет от 250 до 600°С. 3. Способ по п.1, причем реактор (1; 51) имеет электрообогрев. 4. Способ по одному из пп.1-3, причем сферические частицы (67) выполнены из материала, не участвующего в протекающих при регенерации мономера реакциях. 5. Способ ...

СПОСОБ И УСТАНОВКА ДЛЯ ПОЛУЧЕНИЯ МЕТАНОЛА

... 1. Способ синтеза метанола, при осуществлении которого природный газ и водяной пар подают в секцию первичной конверсии, в секции первичной конверсии в результате взаимодействия природного газа и водяного пара получают газообразную смесь, содержащую СО, СО2, Н2 в стехиометрическом избытке и СН4, эту содержащую СО, СО2, Н2 в стехиометрическом избытке и СН4 газообразную смесь подают в секцию синтеза метанола, в которой в результате протекающей в ней реакции получают метанол, и из секции синтеза метанола путем продувки отбирают содержащий СО, СО2, H2 и СН4 газовый поток, отличающийся тем, что из отбираемого продувкой из секции синтеза метанола газового потока выделяют Н2 с получением первой газообразной фазы, по существу состоящей из Н2, и второй газообразной фазы, содержащей СО, СО2 и СН4 и по существу не содержащей Н2, и рекуперируют вторую газообразную фазу, содержащую СО, СО2 и СН4 и по существу не содержащую Н2, для ее использования в процессе конверсии в секции первичной конверсии. 2.

СПОСОБ И УСТРОЙСТВО ДЛЯ ОБОГАЩЕНИЯ ТЯЖЕЛОЙ НЕФТИ

... 1. Способ обогащения тяжелой нефти, в котором, по меньшей мере, часть тяжелой нефти обрабатывают водородсодержащим газом, имеющим температуру выше примерно 649°C, в течение менее 10 с и обработанную тяжелую нефть охлаждают смешиванием обработанной тяжелой нефти с необработанной тяжелой нефтью. 2. Способ по п.1, в котором газ является экзотермическим продуктом воспламенения окисляющего агента и водородсодержащего топлива. 3. Способ по п.1, в котором обработка включает испарение части тяжелой нефти. 4. Способ по п.1, в котором обработка включает преимущественно газофазную реакцию обогащения тяжелой нефти. 5. Способ по п.1, дополнительно предусматривающий стабилизацию охлажденной смеси обработанной тяжелой нефти и необработанной тяжелой нефти в течение 1-60 мин. 6. Способ по п.1, дополнительно предусматривающий время пребывания 1-60 мин для погашенной смеси обработанной тяжелой нефти и необработанной тяжелой нефти. 7. Способ по п.1, в котором указанная необработанная тяжелая нефть, используемая ...

СПОСОБ ПРОИЗВОДСТВА ВОДОРОДА И/ИЛИ ОКИСИ УГЛЕРОДА

... 1. Способ производства газа, обогащенного водородом и/или окисью углерода, из газообразного или жидкого углеводородного сырья, предусматривающий следующие стадии:(a) десульфирования углеводородного исходного материала, смешения исходного материала с водяным паром, произведенным от отходящего тепла в этом процессе, подачи смеси в секцию реформинга с водяным паром для превращения углеводородного исходного материала посредством реакции с паром с образованием технологического газа, содержащего смесь из водорода, окиси углерода, двуокиси углерода, остаточного метана и избыточного водяного пара,(b) охлаждения технологического газа путем производства водяного пара,(c) отделения водорода и/или окиси углерода путем пропускания технологического газа через секцию очистки водорода и/или окиси углерода,(d) добавления по существу всего газа, выходящего из секции очистки, в качестве топлива в секцию реформинга, чтобы обеспечить тепло для реакции реформинга,(e) преобразования горячего дымового газа от ...

СПОСОБ И УСТАНОВКА ДЛЯ ПОЛУЧЕНИЯ МОЧЕВИНЫ

... 1. Способ получения мочевины, при осуществлении которого жидкий аммиак и диоксид углерода подают в секцию (100) синтеза и подвергают в ней реакции для получения мочевины, отличающийся тем, что секция синтеза включает по меньшей мере реактор, отпарной аппарат и конденсатор, образующие контур высокого давления, и по меньшей мере часть диоксида углерода подают в секцию (100) синтеза в жидкой фазе. ! 2. Способ по п.1, в котором часть диоксида углерода подают в секцию (100) синтеза в жидкой фазе, а остальную часть подают в секцию (100) синтеза в газовой фазе. ! 3. Способ по п.1, в котором весь диоксид углерода подают в секцию (100) синтеза в жидком состоянии. ! 4. Способ по одному из предшествующих пунктов, в котором секция (100) синтеза включает реактор (110, 130), отпарной аппарат (112, 132) и конденсатор (114, 134), а жидкий диоксид углерода подают или в реактор, или в конденсатор. ! 5. Способ по одному из пп.1-3, в котором секция (100) синтеза включает реактор (110, 130), отпарной аппарат ...

ТРУБЧАТЫЙ РЕАКТОР ДЛЯ ПОЛУЧЕНИЯ СЕРОСОДЕРЖАЩИХ АЗОТНЫХ УДОБРЕНИЙ

... 1. Способ получения серосодержащих азотных удобрений в трубчатом реакторе (1), содержащем, по меньшей мере, одну входную зону (2) и, по меньшей мере, один смесительный тракт (3), причем трубчатый реактор (1) содержит, по меньшей мере, одно первое средство (6) для загрузки первого реагента и, по меньшей мере, одно второе средство (7) для загрузки второго реагента, расположенные, по меньшей мере, в одной входной зоне (2), и, по меньшей мере, одно третье средство (8, 9) для загрузки, по меньшей мере, одного третьего реагента, причем третье средство (8, 9) расположено, по меньшей мере, в одной входной зоне (2), на и/или после, по меньшей мере, одного смесительного тракта (3), причем раствор нитрата кальция превращают в трубчатом реакторе (1) серной кислотой в присутствии аммиака и за счет гранулирования возникающей гипсосодержащей суспензии получают удобрение, при котором на первом этапе а) реагенты раствор нитрата кальция и NH3 загружают во входную зону (2) трубчатого реактора (1) и смешивают ...

ПСЕВДОИЗОТЕРМИЧЕСКИЙ СПОСОБ ПОЛУЧЕНИЯ АММИАКА

... 1. Способ превращения исходного потока азота и водорода в аммиак, включающий подачу исходного потока на вход псевдоизотермического реактора синтеза аммиака, имеющего реакционную зону, включающую множество трубок катализатора, расположенных в косвенной теплообменной взаимосвязи с газовым потоком в канале горячего газа установки сжигания, чтобы поддерживать температуру реакционной зоны от 300 до 650°C; взаимодействие азота и водорода в реакционной зоне с получением потока продукта, имеющего повышенное содержание аммиака относительно исходного потока; удаление потока продукта с выхода реактора. 2. Способ по п.1, включающий повышение температуры между входом и выходом менее 80°C. 3. Способ по п.2, в котором температура повышается менее чем на 55°C. 4. Способ по п.3, в котором температуру реакционной зоны поддерживают равной от 370 до 480°C. 5. Способ по п.1, в котором трубки катализатора имеют ребристую поверхность. 6. Способ по п.1, в котором исходный поток включает от 50 до 75 об.% водорода ...

СПОСОБ ПОЛУЧЕНИЯ ГОМОПОЛИМЕРОВ ИЛИ СОПОЛИМЕРОВ ЭТИЛЕНА

Изобретение относится к способу получения гомополимеров или сополимеров этилена. Описан способ получения гомополимеров или сополимеров этилена в установке, содержащей трубчатый реактор высокого давления и предварительный нагреватель. Реакционная текучая среда, введенная в реактор, на входе в реактор нагревается в предварительном нагревателе, а средняя скорость реакционной текучей среды в предварительном нагревателе ниже, чем средняя скорость реакционной текучей среды в трубчатом реакторе на входе в реактор. Соотношение средней скорости реакционной текучей среды в трубчатом реакторе к средней скорости реакционной текучей среды в предварительном нагревателе составляет от 1,5:1 до 5:1. Технический результат - получение ПЭНП с более высокой глубиной превращения этилена за реакторный цикл и лучшими оптическими свойствами. 13 з.п. ф-лы, 1 табл., 3 пр., 3 ил.

СПОСОБ И УСТРОЙСТВА ДЛЯ ПОЛУЧЕНИЯ БИУРЕТА И ЦИАНУРОВОЙ КИСЛОТЫ

... 1. Способ получения биурета, включающий (a) плавление мочевины; (b) осуществление термического разложения расплавленной мочевины при нагревании; (c) добавление воды к полученному продукту термического разложения для осаждения и фильтрования неочищенных кристаллов биурета; (d) растворение неочищенных кристаллов биурета в водном растворе щелочи; (e) охлаждение растворенного продукта для осаждения кристаллов биурета; и (f) фильтрование охлажденного продукта, чтобы получить кристаллы биурета и маточный раствор, и промывание кристаллов биурета. 2. Способ по п.1, в котором на стадии (а) мочевину нагревают в плавителе до температуры от 130°С до 160°С. 3. Способ по п.1, в котором на стадии (b) температура нагрева находится в диапазоне от 130°С до 200°С. 4. Способ по п.1, в котором газообразный аммиак и газообразную изоциановую кислоту, полученные на стадии (b), направляют на стадию (а). 5. Способ по п.1, в котором стадию (b) осуществляют при подаче воздуха или инертного газа в нижнюю часть реактора ...

СПОСОБ И УСТАНОВКА ДЛЯ ПОЛУЧЕНИЯ ПОЛИМЕРОВ И СОПОЛИМЕРОВ НА ОСНОВЕ ЭТИЛЕНА

... 1. Способ получения полимеров и сополимеров этилена, включающий следующие стадии: сжатие этилена в первичном компрессоре, имеющем производительность по крайней мере 55 т/ч, за которым следует смешивание этого этилена с возвратным этиленом, дополнительное сжатие смешанного этилена до давления, составляющего по крайней мере 2300 бар, при производительности по крайней мере 120 т/ч во вторичном компрессоре; нагревание по крайней мере части сжатого этилена до температуры, составляющей, по крайней мере, 95°С, и введение этого нагретого этилена в переднюю часть трубчатого реактора, имеющего максимальный внутренний диаметр по крайней мере 65 мм и длину по крайней мере 1500 м, введение инициатора в трубчатый реактор по крайней мере в трех отдельных местах, что определяет по крайней мере три реакционные зоны; полимеризацию этилена, охлаждение реакционной смеси по крайней мере в первых двух реакционных зонах, так, что по крайней мере 28% мономера превращается в полимер; поддержание падения давления ...

СПОСОБ ОБЛАГОРАЖИВАНИЯ АТМОСФЕРНЫХ ОСТАТКОВ

... 1. Способ переработки одного или нескольких углеводородов, включающий ! селективное отделение легкого деасфальтированного масла от одной или нескольких разновидностей углеводородного сырья; и ! гидрокрекинг по меньшей мере части отделенных легких деасфальтированных масел для получения одного или нескольких легких углеводородных продуктов. ! 2. Способ по п.1, где легкие углеводородные продукты включают керосин, дизельное топливо, газойль, бензин, их комбинации, их производные или их смеси. ! 3. Способ по п.1, где одна или несколько разновидностей исходного сырья включают атмосферные остатки со дна колонны, кубовые остатки вакуумной перегонки нефти, сырую нефть, нефтяные сланцы, нефтеносные пески, гудроны, битумы, их смеси или любую их комбинацию. ! 4. Способ по п.1, где легкое деасфальтированное масло селективно отделяют при использовании способа экстрагирования растворителем, включающий ! объединение исходного сырья, содержащего одно или несколько тяжелых масел, одно или несколько легких ...

СПОСОБ СУШКИ ВЛАЖНОГО ПОЛИМЕРНОГО ПОРОШКА И ПРИГОДНОЕ ДЛЯ ЭТОГО УСТРОЙСТВО

... 1. Способ сушки полимерного порошка в сушильном устройстве (1), включающий стадии:i) обработка полимерного порошка нагретым газом (6a) в сушильном устройстве (1), оснащенном входным отверстием (2) и выходным отверстием (3) для полимерного порошка и установленным во внутреннем пространстве (4) нагревательным элементом (5);ii) подача нагретого газа (6a) через трубопровод (7) во внутреннее пространство (4) сушильного устройства (1);iii) нагревание газа (6) в теплообменнике (9) для получения нагретого газа (6a); причемiv) обогрев теплообменника (9) проводят с помощью горячего текучего вещества (5a, 10, 19), которое было нагрето тепловой энергией, которая образовалась в устройстве для получения 1,2-дихлорэтана (15) и/или для получения винилхлорида из 1,2-дихлорэтана; иv) подача через нагревательный элемент (5) горячей воды в качестве горячего текучего вещества (5а), которую нагревают тепловой энергией, которая образовалась в устройстве для получения 1,2-дихлорэтана (15) и/или для получения винилхлорида ...

СПОСОБ КОНТРОЛЯ ТЕХНОЛОГИЧЕСКОГО ПРОЦЕССА НА ПРОИЗВОДСТВЕННОЙ УСТАНОВКЕ (ВАРИАНТЫ), И УСТАНОВКА ДЛЯ ПРОИЗВОДСТВА ИЗОЦИАНАТОВ

... 1. Способ контроля технологического процесса на производственной установке, включающей ! a) по меньшей мере, два входящих потока ! b) по меньшей мере, один выходящий поток и ! c) по меньшей мере, один внутренний рециркулирующий поток, включающий регулирование объема, по меньшей мере, одного входящего потока посредством регулирующего контроля, чтобы контролировать концентрацию и/или объем выходящего потока. ! 2. Способ контроля процесса производства изоцианата, проводимого на производственной установке, содержащей ! a) по меньшей мере, два входящих потока, содержащих: ! (1) поток фосгена, содержащий фосген и ! (2) поток растворителя, содержащий растворитель. ! b) по меньшей мере, один выходящий поток и ! c) по меньшей мере, один внутренний рециркулирующий поток, включающий регулирование объема потока фосгена и/или объема потока растворителя посредством регулирующего контроля, чтобы контролировать концентрацию и/или количество выходящего потока. ! 3. Способ по п.2, в котором поток фосгена ...

СПОСОБ И УСТРОЙСТВО ДЛЯ ПРЕВРАЩЕНИЯ ЦЕЛЛЮЛОЗНОГО МАТЕРИАЛА В ЭТАНОЛ

... 1. Способ превращения целлюлозного материала в этанол и другие продукты, причем целлюлозный материал содержит по меньшей мере целлюлозу, лигнин, гемицеллюлозу и золу, в котором целлюлозный материал очищают и подвергают непрерывной гидротермической предварительной обработке без добавления кислот или оснований, или других химических реактивов, которые требуется извлекать, причем получают жидкость и фракцию волокон, фракцию волокон подвергают ферментативному размягчению и осахариванию, причем способ включает ферментацию с получением этанола и извлечение продукта, где способ включает: ! осуществление гидротермической предварительной обработки, подвергая целлюлозный материал по меньшей мере одной операции вымачивания, и проведение целлюлозного материала через по меньшей мере один реактор высокого давления, задающий зону высокого давления реактора, работающую при повышенном давлении; целлюлозный материал нагревают до температуры от 170 до 230°С, и проводят по меньшей мере одну операцию отжима ...

СПОСОБ И АППАРАТ ДЛЯ ПРОИЗВОДСТВА АРОМАТИЧЕСКИХ КАРБОНОВЫХ КИСЛОТ

... 1. Способ производства ароматических карбоновых кислот, включающий: ! контактирование сырья, содержащего по меньшей мере один предшественник кислоты - ароматический углеводород, с газообразным кислородом в реакционной смеси жидкофазного окисления, содержащей монокарбоновую кислоту в качестве растворителя и воду, в присутствии каталитической композиции, содержащей по меньшей мере один тяжелый металл, в секции реакции при повышенной температуре и давлении, эффективных для сохранения реакционной смеси жидкофазного окисления и образования ароматической карбоновой кислоты и примесей, содержащих побочные продукты реакции, растворенные или суспендированные в реакционной смеси жидкофазного окисления и в паровой фазе высокого давления, содержащей растворитель - монокарбоновую кислоту, воду и небольшие количества исходного ароматического углеводорода и побочных продуктов окисления исходного ароматического углеводорода и растворителя - монокарбоновой кислоты; ! перенос паровой фазы высокого давления ...

СПОСОБ И УСТРОЙСТВО ПЕРЕРАБОТКИ ТЯЖЕЛОГО НЕФТЯНОГО СЫРЬЯ

... 1. Способ переработки углеводородного сырья, заключающийся в том, чтонагревают перерабатываемое сырье и параллельно готовят перегретый водяной пар,нагретое перерабатываемое сырье и перегретый водяной пар подают в первую реакционную камеру реактора, имеющего две последовательно расположенные и сообщающиеся между собой реакционные камеры, при этом объем первой реакционной камеры меньше объема второй реакционной камеры, и диаметр и объем второй реакционной камеры обеспечивают снижение давления и температуры реакционной смеси,температуру перерабатываемого сырья устанавливают меньше температуры в первой реакционной камере, а температуру водяного пара устанавливают выше температуры в первой реакционной камере, температура и давление перерабатываемого сырья, температура и давление перегретого водяного пара устанавливаются на значения достаточные для осуществления термического крекинга, по меньшей мере, части углеводородного сырья в первой реакционной камере, при этомдавление и температуру перерабатываемого ...

ПОЛУЧЕНИЕ ДИКАРБОНОВЫХ КИСЛОТ С ПОВЫШЕННОЙ РЕГЕНЕРАЦИЕЙ ЭНЕРГИИ

... 1. Способ получения ароматической дикарбоновой кислоты, причем указанный способ включает стадии:(а) окисления ароматического соединения по меньшей мере в одном окислительном устройстве с получением, тем самым, отходящих газов окислительного устройства и суспензии окислительного устройства, включающей ароматическую дикарбоновую кислоту, причем указанные отходящие газы окислительного устройства содержат по меньшей мере 12,4 кг пара на кг указанного ароматического соединения, подводимого в указанное окислительное устройство;(b) извлечения углеводородных соединений из указанных отходящих газов окислительного устройства в системе регенерации растворителя с получением, тем самым, обедненных углеводородами отходящих газов, содержащих по меньшей мере 3 кг водяного пара на килограмм указанного ароматического соединения, подводимого в указанное окислительное устройство; и(с) пропускания по меньшей мере части указанных обедненных углеводородами отходящих газов по меньшей мере через один турбодетандер ...

ОКИСЛИТЕЛЬНАЯ СИСТЕМА С ВТОРИЧНЫМ РЕАКТОРОМ ДЛЯ БОКОВОЙ ФРАКЦИИ

... 1. Система для производства поликарбоновой кислоты путем контакта суспензии с газофазным окислителем, причем указанная система включает:первичный окислительный реактор, включающий первый суспензионный выпуск; ивторичный окислительный реактор, включающий впуск суспензии и второй суспензионный выпуск,в которой указанный впуск суспензии находится ниже по потоку в гидравлическом соединении с указанным первым выпуском суспензии;в которой указанный вторичный окислительный реактор представляет собой вторичную реакционную зону, имеющую максимальную длину Ls и максимальный диаметр Ds,в которой расстояние до указанного впуска от дна указанной вторичной реакционной зоны находится в интервале от приблизительно 0,3 Ls до приблизительно 0,9 Ls.2. Система по п.1, в которой указанный вторичный окислительный реактор включает нормально верхний впуск окислителя, в которой расстояние от указанного нормально верхнего впуска окислителя составляет менее чем 0,4 Ls от указанного впуска суспензии, в которой расстояние ...

СПОСОБ КОНТРОЛЯ СПОСОБА ПОЛУЧЕНИЯ ИЗОЦИАНАТОВ

КРИСТАЛЛИЗУЮЩИЙ КОНВЕЙЕР

... 1. Способ кристаллизации множества полимерных гранул, включающий ! а) подачу множества полимерных гранул на вход пневматической конвейерной системы, при этом множество полимерных гранул содержит кристаллизуемый полимер, имеющий температуру кристаллизации и температуру плавления, и ! b) пневматический перенос множества полимерных гранул от входа к выходу транспортным газом, при этом транспортный газ имеет температуру, достаточную для поддержания температуры множества полимерных гранул в таком диапазоне, чтобы кристаллизация множества полимерных гранул по существу была инициирована или завершена до извлечения гранул из выхода пневматической конвейерной системы. ! 2. Способ по п.1, где часть множества гранул имеет сферическую форму или цилиндрическую форму. ! 3. Способ по п.1, где множество полимерных гранул содержат компонент, выбранный из группы, включающей сложный полиэфир, полиолефины, полистиролы, нейлоны и поликетоны. ! 4. Способ по п.3, где сложным полиэфиром является полимер или сополимер ...

СПОСОБ И УСТРОЙСТВО ДЛЯ ПОЛИМЕРИЗАЦИИ ПРОПИЛЕНА

... 1. Способ получения гетерофазных пропиленовых сополимеров путем полимеризации пропилена в присутствии катализатора полимеризации и водорода в качестве регулятора молекулярного веса, включающий следующие стадии: а) полимеризация пропилена в газовой или жидкой фазе, необязательно совместно с одним или более α-олефиновыми сомономерами, с получением фракции кристаллического полимера; b) сополимеризация этилена с пропиленом и/или 1-бутеном и необязательно одним или более альфа-олефиновыми сомономерами С5-С12 в газофазном реакторе с соединенными друг с другом зонами полимеризации, где растущие полимерные частицы перетекают снизу вверх через первую зону полимеризации (устройство с восходящим потоком) в условиях быстрого псевдоожижения или транспортирования, покидают упомянутое устройство с восходящим потоком и поступают во вторую зону полимеризации (устройство с нисходящим потоком), через которую они перетекают сверху вниз под действием силы тяжести, покидают упомянутое устройство с нисходящим ...

УСТРОЙСТВО И СПОСОБ ИЗОМЕРИЗАЦИИ БЕНЗОЛСОДЕРЖАЩЕГО СЫРЬЯ

... 1. Устройство для гидрогенизации и дециклизации бензола и изомеризации С5-С6-парафинов в сырье, содержащем C5-С6-парафины и, по меньшей мере, 1 вес.% бензола, которое включает: ! (a) сырьевой трубопровод (10), не оборудованный конденсатором или вентиляционным отверстием для водорода, сообщающийся по жидкости с осушителем (11) низкого давления; ! (b) трубопровод для потока, выходящего из осушителя, сообщающийся по жидкости с осушителем (11) низкого давления, а также с первым трубопроводом (15) для высушенного сырья и вторым трубопроводом (15') для высушенного сырья; ! (c) трубопровод для обогащенного водородом газа, объединяющийся с первым трубопроводом (15) для высушенного сырья с образованием трубопровода (18) для объединенного сырья; ! (d) зону (32) гидрогенизации, сообщающуюся по жидкости с трубопроводом (18) для объединенного сырья и трубопроводом (34) для потока из зоны гидрогенизации, причем зона (32) гидрогенизации содержит катализатор гидрогенизации; ! (e) трубопровод (34') для ...

СИСТЕМА ИЗВЛЕЧЕНИЯ КАТАЛИЗАТОРА КОНВЕРСИИ ОКСИГЕНАТОВ В ОЛЕФИНЫ С БАШНЕЙ ГАШЕНИЙ РЕАКЦИИ, ИСПОЛЬЗУЮЩАЯ НИЗКОТЕМПЕРАТУРНУЮ СУШИЛЬНУЮ КАМЕРУ С ПСЕВДООЖИЖЕННЫМ СЛОЕМ

... 1. Способ извлечения катализатора в процессе конверсии оксигенатов в олефины, при этом способ включает: удаление нижнего потока башни гашения реакции, содержащего катализатор, из башни гашения реакции; разделение нижнего потока башни гашения реакции для получения по существу осветленной жидкости и потока, содержащего катализатор; перепускание потока, содержащего катализатор, в сушильную камеру; и высушивание потока, содержащего катализатор, в сушильной камере для получения по существу высушенного катализатора. ! 2. Способ по п.1, который дополнительно включает хранение потока, содержащего катализатор, в резервуаре для хранения извлеченного катализатора перед перепусканием потока, содержащего катализатор, в сушильную камеру. ! 3. Способ по п.1, который дополнительно включает перепускание высушенного катализатора в регенератор катализатора и регенерацию высушенного катализатора. ! 4. Способ по п.1, в котором стадию разделения проводят, по меньшей мере, в одном гидроциклоне. ! 5. Способ по ...

СПОСОБ СИНТЕЗА МОЧЕВИНЫ С БОЛЬШИМ ВЫХОДОМ

... 1. Способ синтеза мочевины из аммиака и двуокиси углерода с образованием карбамата аммония в качестве промежуточного химического соединения, который состоит из таких стадий, как:a. взаимодействие аммиака и двуокиси углерода как такового или в виде карбамата аммония при молярном соотношении NH/COв диапазоне от 2,3 до 6, при температуре в диапазоне от 140 до 215°C и под давлением в диапазоне от 12 до 25 МПа с образованием первой жидкой смеси, содержащей мочевину, карбамат аммония, аммиак и воду;b. подача упомянутой первой жидкой смеси на стадию разложения-стриппинга, чтобы осуществить разложение, по крайней мере, кратного количества, в соответствии с предпочтительным примером осуществления настоящего изобретения от 50 до 99% карбамата аммония в аммиак и двуокись углерода, при работе под таким же давлением, как и на упомянутой стадии реакции (а) и при температуре в диапазоне от 160 до 240°C, одновременно подвергая упомянутую жидкую смесь стриппингу с образованием первой газообразной смеси, ...

ОПТИМИЗИРОВАННОЕ ЖИДКОФАЗНОЕ ОКИСЛЕНИЕ

... 1. Способ, включающий окисление окисляемого соединения в жидкой фазе многофазной реакционной среды, содержащейся в зоне реакции барботажной колонны реакторного типа, где упомянутая реакционная среда включает нижнюю часть, имеющую максимальную площадь горизонтального поперечного сечения, и верхнюю часть, имеющую минимальную площадь горизонтального поперечного сечения, где упомянутая максимальная площадь поперечного сечения, по меньшей мере, приблизительно на 10% превышает упомянутую минимальную площадь поперечного сечения. 2. Способ по п.1, где упомянутая максимальная площадь поперечного сечения, по меньшей мере, приблизительно на 20% превышает упомянутую минимальную площадь поперечного сечения. 3. Способ по п.1, где упомянутая зона реакции включает нижнюю секцию, содержащую упомянутую нижнюю часть, и верхнюю секцию, содержащую упомянутую верхнюю часть, где упомянутая нижняя секция характеризуется максимальной высотой (Ll), максимальным диаметром (Dl) и соотношением Ll:Dl, равным, по меньшей ...

ГАЗОВЫЙ СКРУББЕР И СООТВЕТСТВУЮЩИЕ СПОСОБЫ

... 1. Способ удаления примесей из технологического газа, включающий следующие этапы:подачу входящего потока технологического газа, содержащего первую концентрацию ацетальдегида, в газоочистную установку;подачу входящего потока жидкого этиленгликоля в газоочистную установку;приведение в контакт входящего потока технологического газа с входящим потоком жидкого этиленгликоля в присутствии одного или более кислотных катализаторов в газоочистной установке, при этом ацетальдегид вступает в реакцию с этиленгликолем с образованием 2-метил-1,3-диоксолана на указанном этапе приведения в контакт, а результатом этапа приведения в контакт является образование потока очищенного технологического газа, содержащего вторую концентрацию ацетальдегида, более низкую, чем первая концентрация, и выходящего потока жидкого этиленгликоля, содержащего 2-метил-1,3-диоксолан; иудаление потока очищенного технологического газа и выходящего потока этиленгликоля из газоочистной установки.2. Способ по п. 1, отличающийся тем ...

СПОСОБ И УСТРОЙСТВО ДЛЯ ОБРАБОТКИ РАСТВОРОВ, СОДЕРЖАЩИХ ЦИАНИД И/ИЛИ КОМПЛЕКСООБРАЗУЮЩИЕ АГЕНТЫ

... 1. Способ обработки водного раствора, содержащего цианиды и/или комплексообразующие агенты, возможно содержащего тяжелые и/или драгоценные металлы, включающий высокотемпературную обработку раствора в закрытом реакционном сосуде, где после высокотемпературной обработки некоторую часть обработанного раствора выгружают из реакционного сосуда, указанную выгружаемую часть раствора по меньшей мере частично заменяют необработанным раствором, который подвергают высокотемпературной обработке вместе с частью обработанного раствора, оставшейся в реакционном сосуде. ! 2. Способ по п.1, где после высокотемпературной обработки обработанный раствор или выгружаемую часть обработанного раствора переносят в резервуар для хранения, расположенный ниже по потоку от реакционного сосуда, и охлаждают в нем, при этом паро- и газообразные реакционные продукты выпускают из резервуара для хранения. ! 3. Способ по п.2, где паро- и газообразные реакционные продукты и/или охлажденный раствор подают по меньшей мере в ...

СПОСОБ И АППАРАТ ДЛЯ УТИЛИЗАЦИИ ТЕПЛА В УСТАНОВКАХ ДЛЯ ПОЛУЧЕНИЯ МОНОМЕРА ВИНИЛХЛОРИДА ИЛИ В ИНТЕГРИРОВАННЫХ УСТАНОВКАХ ДЛЯ ПОЛУЧЕНИЯ МОНОМЕРА ВИНИЛХЛОРИДА/ПОЛИВИНИЛХЛОРИДА

... 1. Способ получения винилхлорида термическим расщеплением 1,2-дихлорэтана в комплексе для получения винилхлорида посредством дистилляционной очистки 1,2-дихлорэтана с применением по меньшей мере одной колонны высококипящих соединений, в которой удаляют вещества с более высокой температурой кипения, чем у 1,2-дихлорэтана, а также посредством необязательно присоединенной установки для получения поливинилхлорида, при этом указанный способ включает операцииa) эксплуатации колонны высококипящих соединений при температурах наверху колонны 120-150°С иb) применения по меньшей мере части верхнего потока из колонны высококипящих соединений с получением тепловой энергии, применяемой в теплоотводах компонента установки, предназначенного для получения 1,2-дихлорэтана, и/или в теплоотводах компонента установки ниже по потоку, предназначенного для получения винилхлорида, и/или в теплоотводах компонента установки ниже по потоку, предназначенного для получения поливинилхлорида, сc) применением верхнего ...

Способ получения полиолефинов

Lowering the temperature prevailing in a reaction zone of a trichlorosilane-synthesis reactor, comprises introducing a liquid chlorosilane into the reaction zone

Lowering the temperature prevailing in a reaction zone (9) of a trichlorosilane-synthesis reactor (10), comprises introducing at least one liquid chlorosilane (62) into the reaction zone. An independent claim is also included for a device for carrying out the above mentioned method, comprising the trichlorosilane-synthesis reactor, a condensing device for condensing at least one product gas (60) into its liquid phase, which is synthesized in the reactor, and a recirculation device (20, 46), through which at least one condensed product gas is recycled into the reactor.

VERFAHREN, REAKTOR UND SYSTEM ZUR HERSTELLUNG EINES BISPHENOLS

Anlage für exotherme nasschemische Hochdruck-Reaktionen

Die Erfindung betrifft eine Anlage (2) insbesondere zur hydrothermalen Karbonisierung von Reaktionsgut in Form von Biomasse (4). Die Anlage (2) hat einen Reaktionsbehälter (8) mit einem Reaktionsraum (6) für exotherme nasschemische Hochdruck-Reaktionen, in welchen das Reaktionsgut (4) zuführbar ist. Erfindungsgemäß enthält die Anlage (2) eine Einrichtung (22, 42, 76, 114, 130) für das Rückgewinnen und Übertragen von bei einer exothermen nasschemischen Reaktion in dem Reaktionsbehälter (6) freigesetzter Wärme zum Aufheizen von Reaktionsgut (4).

VORRICHTUNG ZUR BEHANDLUNG VON FLÜSSIGKEITEN

Verfahren und Vorrichtung zur Behandlung von Perfluorkohlenstoff

VERFAHREN ZUR HERSTELLUNG VON VINYLCHLORID DURCH THERMISCHE SPALTUNG VON 1,2-DICHLORETHAN

Verfahren zum Anfahren eines Reaktors und Reaktorsystem

VERFAHREN UND GERÄT ZUM VORHERSAGEN VON POLYMER-LATEX EIGENSHAFTEN IN EINEM EMULSIONSPOLYMERISATIONPROZESS ZUR QUALITÄT UND PRODUKTIVITÄTVERBESSERUNG DER POLYMERLATEX

Verfahren zur katalytischen Durchführung von Mehrphasenreaktionen, insbesondere Vinylierungen von Carbonsäuren

Die Erfindung betrifft ein Verfahren zur katalytischen Durchführung von Mehrphasenreaktionen in einem Rohrreaktor, wobei der Katalysator in der kontinuierlichen Phase und mindestens ein Edukt in einer dispergierten Phase enthalten ist und der Belastungsfaktor B des Rohrreaktors gleich oder größer 0,8 ist. DOLLAR A Das Verfahren ist besonders zur Herstellung von Vinylestern durch Reaktion von Carbonsäuren mit Acetylen geeignet. DOLLAR A Die Vinylester finden zur Herstellung von Homo- oder Copolymerisaten Verwendung.

Verfahren und Vorrichtung zur parallelen Erzeugung unterschiedlicher Synthesegase

Die Erfindung betrifft ein Verfahren sowie eine Vorrichtung zur parallelen Erzeugung von wenigstens zwei Synthesegasen (10, 11) unterschiedlicher Zusammensetzung aus einem kohlenwasserstoffhaltigen Ausgangsstoff (1), der nach Zumischung von Wasserdampf (2) und/oder Kohlendioxid (3) einem Dampfreformer (R) zugeführt und dort in zumindest zweit parallel betriebenen Katalysatorrohren (K1, K2, K3) durch Dampfreformierung zu Synthesegas umgesetzt wird. Für die Erfindung ist kennzeichnend, dass aus dem Kohlenwasserstoffe enthaltenden Ausgangsstoff (1) durch Teilung und der Zumischung von Wasserdampf (2) und/oder Kohlendioxid (3) wenigstens zwei Stoffgemische (6, 9) unterschiedlicher Zusammensetzung gebildet werden, wobei jedes der unterschiedlichen Stoffgemische (6, 9) einem Katalysatorrohr oder einer Gruppe von Katalysatorrohren (K1, K2, K3) des Dampfreformers (R) als ausschließlicher Einsatz zugeführt und zu Synthesegas (10, 11) umgesetzt wird.

Vorrichtung zur Herstellung von Harnstoff

Verfahren und Vorrichtung zur Herstellung von H¶2¶ und CO enthaltendem Synthesegas

Bei einem Verfahren zur Herstellung von Synthesegas durch katalytische Konvertierung von in einem entschwefelten Einsatzgasstrom enthaltenen Kohlenwasserstoffen mit Dampf wird das Einsatzgas-Dampf-Gemisch bei einem Druck von 10 bis 45 bar durch Wärmeaustausch auf eine Temperatur von 300 bis 700 DEG C vorgewärmt und anschließend über einem Katalysator bei einem Druck von 10 bis 45 bar durch Wärmeaustausch auf eine Temperatur von 650 bis 950 DEG C aufgeheizt. Um den apparativen Aufwand niedrig zu halten, ist vorgesehen, dass das Einsatzgas-Dampf-Gemisch eine in einem Reaktionsbehälter befindliche Katalysatorschicht durchströmt und die Katalysatorschicht durch thermische Strahlung und Konvektion aufgeheizt wird.

VERFAHREN UND VORRICHTUNG ZUR POLYMERISATION VON ETHYLEN

Vorrichtung und Verfahren zur Behandlung von Fest-Flüssig-Gemischen

Ein Laminarstromreaktor zur Herstellung von Werk- oder Brennstoffen, Humus, Maillard- oder ähnlichen Reaktionsprodukten aus einem Fest-Flüssig-Gemisch aus Wasser und einer kohlenstoffhaltigen Komponente, wobei das Fest-Flüssig-Gemisch bei einer Temperatur von über 100°C und einem Druck von über 5 bar behandelt wird, besteht aus Rohrreaktoreinheiten aus weitgehend senkrechten Haltestrecken (1, 3) und richtungsändernden Umlenkern (2, 4). Dabei werden die Haltestrecken von dem Fest-Flüssig-Gemisch langsamer durchströmt als die restlichen Rohrstrecken, weil sie größere Durchmesser aufweisen.

Continuous production of silane, useful in production of silicon for semiconductors, involves catalytic disproportionation of trichlorosilane over solid catalyst in 2 or more zones with intermediate condensation

Silane is produced in a continuous process by the disproportionation of trichlorosilane in at least 2 reaction areas through which vapour and liquid flow in counter-current, by means of reaction/distillation on catalytically active solid matter under a pressure which ranges between 500 mbar and 50 bar.

Verfahren und Vorrichtung zur Behandlung von cyanid- und/oder komplexbildnerhaltigen Lösungen

Beschrieben wird ein Verfahren zur Behandlung einer wässrigen, gegebenenfalls Schwer- und/oder Edelmetalle enthaltenden, cyanid- und/oder komplexbildnerhaltigen Lösung, umfassend eine Hochtemperaturbehandlung der Lösung in einem geschlossenen Reaktionsbehälter, dadurch gekennzeichnet, dass nach der Hochtemperaturbehandlung ein Teil der behandelten Lösung aus dem Reaktionsbehälter abgelassen wird, der abgelassene Teil mindestens teilweise durch unbehandelte Lösung ersetzt wird und diese mit dem im Reaktionsbehälter verbliebenen Teil der behandelten Lösung hochtemperaturbehandelt wird. Darüber hinaus wird eine Vorrichtung zur Durchführung eines solchen Verfahrens beschrieben.

Kohlenwasserstoff-Reformer

Verfahren zur Reformierung von Kohlenwasserstoffen, ausgewählt aus Mineralöl, Dieselöl, Benzin, Bio-Diesel und Pflanzenöle, in überkritischem Wasser mit den Schritten a) Kompression von Wasser auf einen Druck p1 und Einspeisung in eine Aufheizzone; b) Aufheizen des komprimierten Wassers in einem Kapillarrohrreaktor auf eine Temperatur T1, wobei das Wasser bei dem Druck p1 und der Temperatur T1 im überkritischen Zustand vorliegt; c) Kompression der Kohlenwasserstoffe auf den Druck p1 und Einspeisung in das überkritische Wasser, wobei ein überkritisches Wasser/Kohlenwasserstoff-Gemisch erhalten wird; d) Reagierenlassen des überkritischen Wasser/Kohlenwasserstoff-Gemischs in einem Kapillarrohrreaktor unter überkritischen Bedingungen, wobei die Kohlenwasserstoffe zumindest teilweise mit Wasser zu Kohlenmonoxid, Kohlendioxid und Wasserstoff reagieren; e) Abkühlen des in Schritt d) erhaltenen Produktgemischs auf eine Temperatur T2 und Entspannen auf einen Druck p2, wobei das Produktgasgemisch ...

Verfahren und Vorrichtung zur Herstellung von Biodiesel

Die vorliegende Erfindung betrifft ein Verfahren zur kontinuierlichen Herstellung von Biodiesel aus biogenen fett- oder öl-haltigen Ausgangsgemischen mit einem hohen Anteil freier Fettsäuren sowie eine Vorrichtung zur Herstellung von Biodiesel.

Hydrocarbon based fuel reforming device vaporizes either hydrocarbon fuel or water to produce vapor gas which is mixed with non-vaporized gas portion to produce vapor mixture

A vaporizing device (30) vaporizes a portion of either of a hydrocarbon fuel or water, to produce a vapor gas containing vapor and air. A vapor mixing device (50) creates a vapor mixture by spraying a portion of non-vaporized fuel or water, towards the vapor gas. A reforming device (60) reforms the fuel in the vapor mixture to reformate gas containing hydrogen. The vapor mixing device has a spray nozzle (52) to spray a portion of either the hydrocarbon fuel or the water, towards the vapor gas. The hydrocarbon fuel is either in liquid state or in gaseous state. A return pipe (48) is attached to the spray nozzle to return a portion of hydrocarbon fuel which is not vaporized, to a fuel tank (42). A vapor gas supply quantity adjusting valve (49) for adjusting the quantity of vapor gas supplied by the vaporizing device to the vapor mixing device, is provided in the return pipe. An air supply quantity adjusting valve (28) adjusts the quantity of the air supplied to the vapor mixing device. The ...

Control of gas composition

Process

Primary steam reforming plant

A plant for the synthesis of a product from a synthesis gas includes a synthesis gas generation stage including a high pressure reforming stage using tubes heated externally by means of pressurised combustion products; a synthesis stage wherein the product is synthesised from the synthesis gas; a combustion stage wherein part of the synthesis gas, or waste gas remaining after synthesis of the product, is combusted with compressed air to form the pressurised combustion products at a pressure similar to the reforming pressure; a trip system responsive to a plant malfunction including means to shut off the supply of feedstock to the reformer tubes, but not to isolate the synthesis stage and combustion stage from the reforming stage, and means to depressurise the combustion stage.

Systems and methods for carbon monoxide clean-up

Integrated Fuel Processor For Distributed Hydrogen Production

A fuel processing system is provided wherein heat is transferred from a reformate flow (32) downstream from a water-gas shift (38) to both a) a combustor feed flow (40) that is supplied to a combustor (25); and b) a water flow (26) that is supplied to a reformer feed mix (34) for a steam reformer (28).

Integrated fuel processor for distributed hydrogen production

An integrated steam reformer/combustor assembly (42) is provided for use in a fuel processor (20) that supplies a steam/fuel feed mix (34) to be reformed in the assembly and a combustor feed (40) to be combusted in the assembly (42). The assembly (42) includes a housing (44,58) defining first and second axially extending, concentric annular passages in heat transfer relation to each other; a first convoluted fin (46) located in the first passage to direct the feed mix therethrough, the first convoluted fin coated with a catalyst that induces a desired reaction in the feed mix; and a second convoluted fin (50) located in the second passage to direct the combustor feed therethrough, the second convoluted fin coated with a catalyst that induces a desired reaction in the combustor feed.

Process for production of DME from crude methanol

Process for the recovery of metals and hydrochloric acid

HYDROCARBON SYNTHESIS REACTION APPARATUS

Method and apparatus for sequestering carbon dioxide from a spent gas.

Deep conversion combining the demetallization and the conversion of crudes, residues or heavy oils into light liquids with pure or impure oxygenated compounds.

A process for the conversion of hydrocarbons that are solid or have a high boiling temperature and may be laden with metals, sulfur or sediments, into liquids (gasolines, gas oil, fuels) with the help of a jet of gas properly superheated betwwen 600 and 800c. The process comprises preheating a feed (5) in a heater (8) to a temperature below the selected temperature of a reactor (10). This feed injected by injectors (4) into the empty reactor (10) (i.e. without catalyst.) the feed is treated with a jet of gas or superheated steam from superheater (2) to activate the feed. The activated products in the feed are well allowed to stabilize at the selected temperature and at a selected pressure in the reactor and are then run through a series of extractors (13) to separate heavy and light hydrocarbons and to demetallize the feed. Useful products appearing in the form of water/hydrocarbon emulsions are generally demulsified in emulsion breaker (16) to form water laden with different impurities ...

Method, apparatus and system for manufacture of a cyanide

Method of producing hydrocarbons

Method and apparatus for sequestering carbon from a spent gas

PROCESS FOR PRODUCTION OF DME FROM CRUDE METHANOL

HYDROCARBON SYNTHESIS REACTION APPARATUS

Process for production of DME from crude methanol

Process for the recovery of metals and hydrochloric acid

Method and apparatus for sequestering carbon dioxide from a spent gas.

Method of producing hydrocarbons

Reactor apparatus and methods

Method, apparatus and system for manufacture of a cyanide.

HYDROCARBON SYNTHESIS REACTION APPARATUS

Method, apparatus and system for manufacture of a cyanide.

Deep conversion combinig the demetallization and the conversion of crudes, residues or heavy oils into light liquids with pure or impure oxygenated compounds.

Fischer-Tropsch synthesis process carried out on a floatable structure.

Reactor apparatus and methods

Method of producing hydrocarbons

Method, apparatus and system for manufacture of a cyanide.

Method and apparatus for preparing hydroxymethylfurfural

In an embodiment of the invention, an apparatus for preparing hydroxymethylfurfural (HMF) is provided. The apparatus includes a reaction area including a first organic layer including sugar and a solvent and a second organic layer including a solvent mixture with azeotropy and extractability, a boiling area including a mixing solution formed by the hydroxymethylfurfural and the solvent mixture, connected with the reaction area, and a distilling area including water and a liquid layer including the solvent mixture, connected to the reaction area. In another embodiment of the invention, a method for preparing hydroxymethylfurfural (HMF) is provided.

Method and apparatus for manufacturing trichlorosilane

An apparatus 1 for manufacturing trichlorosilane includes a decomposition furnace 2 into which polymers and hydrogen chloride are introduced, the decomposition furnace 2 includes: a heating device 11 which heats an interior of the decomposition furnace 2; a reaction chamber 4 which is formed in the decomposition furnace; a center tube 3 which is inserted in the reaction chamber 4 along a longitudinal direction of the reaction chamber and has a lower-end opening portion 3 a; raw-material-supply pipes 5 and 6 which supplies the polymer and the hydrogen chloride to the reaction chamber 4 at an exterior of the center tube 3; and a gas-discharge pipe 7 which leads out reacted gas from the center tube 3, the apparatus 1 further includes a fin 14 that leads the polymer and the hydrogen chloride to the lower-end opening portion 3 a of the center tube 3 so as to stir the polymer and the hydrogen chloride.

Removal of light fluoroalkanes from hydrocarbon streams

The removal of fluoroalkanes from fluoroalkane-containing hydrocarbon streams, preferably C 3 to C 5 hydrocarbon streams. The fluoroalkane-containing hydrocarbon stream is contacted with an adsorbent containing a strong acid function, preferably a silica gel or a strong cation ion-exchange resin having sulfonic acid functionality.

Method and Apparatus for Obtaining Aromatics from Diverse Feedstock

The process relates to the use of any naphtha-range stream containing a portion of C8+ aromatics combined with benzene, toluene, and other non-aromatics in the same boiling range to produce toluene. By feeding the A8+ containing stream to a dealkylation/transalkylation/cracking reactor to increase the concentration of toluene in the stream, a more suitable feedstock for the methylation reaction can be produced. This stream can be obtained from a variety of sources, including the pygas stream from a steam cracker, “cat naphtha” from a fluid catalytic cracker, or the heavier portion of reformate.

Method of making a catalyst

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

Methods of deoxygenation and systems for fuel production

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

Process for preparing n,n-dimethylaminoethoxyethanol

A process for preparing N,N-dimethylaminoethoxyethanol (DMAEE), wherein a) dimethylamine and ethylene oxide are reacted, b) the resulting product mixture of N,N-dimethylethanolamine and DMAEE is separated by distillation to obtain a DMAEE-containing fraction as the bottom stream, and c) DMAEE from the fraction obtained in (b) is removed by distillation.

Process for the preparation of a multimodal polyolefin polymer with improved hydrogen removal

Process for the preparation of a multimodal polyolefin polymer at temperatures of from 40 to 150° C. and pressures of from 0.1 to 20 MPa in the presence of a polymerization catalyst in a first and a second polymerization reactor connected in series, wherein further polymerization reactors can be connected to said reactors upstream or downstream of said reactors, in which in the first polymerization reactor a first polyolefin polymer is prepared in suspension in the presence of hydrogen and in the second polymerization reactor a second polyolefin polymer is prepared in the presence of a lower concentration of hydrogen than in the first polymerization reactor, comprising a) withdrawing from the first polymerization reactor a suspension of solid polyolefin particles in a suspension medium comprising hydrogen; b) feeding the suspension to a flash drum of a lower pressure than that of the first polymerization reactor; c) vaporizing a part of the suspension medium; d) withdrawing a hydrogen-depleted suspension from the flash drum and feeding it to the second polymerization reactor; e) withdrawing gas from the gas-phase of the flash drum and feeding it to a heat exchanger; f) condensing a part of the gas withdrawn from the flash drum; and g) returning the liquid obtained in the heat exchanger to the polymerization process at a point where suspension is present, and apparatus for preparing a multimodal polyolefin polymer according to the process.

Process for alkylation of toluene to form styrene and ethylbenzene

A process is disclosed for making styrene and/or ethylbenzene by reacting toluene with a C 1 source over a catalyst in at least one radial reactor to form a product stream comprising styrene and/or ethylbenzene.

Flashline heater system and method

The present embodiments provide a system and method for separation within a polymer production process. Specifically, a flashline heater configured according to present embodiments may provide more time than is required for complete vaporization of liquid hydrocarbons that are not entrained within a polymer fluff produced within a polymerization reactor. Such extra time may allow for liquid hydrocarbons that are entrained within the polymer fluff to be vaporized.

Hydrogen generation assemblies and hydrogen purification devices

Hydrogen generation assemblies, hydrogen purification devices, and their components, and methods of manufacturing those assemblies, devices, and components are disclosed. In some embodiments, the assemblies may include a vaporization region with packing material configured to transfer heat from a heated exhaust stream to a liquid-containing feed stream, and/or an insulation base adjacent a combustion region and configured to reduce external temperature of an enclosure. In some embodiments, the assemblies may include a cooling block configured to maintain an igniter assembly in thermal communication with a feed stream conduit, an igniter assembly including a catalytic coating, and/or a fuel stream distribution assembly. In some embodiments, the assemblies may include a heat conducting assembly configured to conduct heat from external heaters to an enclosure portion. In some embodiments, the devices may include frames with membrane support structures and/or may include a microscreen structure configured to prevent intermetallic diffusion.

Methods and Systems for Upgrading Hydrocarbon

Methods and systems for upgrading hydrocarbon are described. The system can include a combustor and a nozzle reactor. The combustor can be used to produce a motive fluid suitable for use in the nozzle reactor. The motive fluid produced by the combustor and a hydrocarbon stream can be injected into the nozzle reactor to upgrade the hydrocarbon material. The systems and methods can also be integrated with a steam assisted gravity drainage system.

Processes and systems for converting synthesis gas to liquid hydrocarbon product

Processes and systems are provided for converting synthesis gas containing a mixture of H 2 and CO to liquid hydrocarbon products having a cloud point less than about 15° C. The systems utilize at least one Fischer-Tropsch reactor containing hybrid Fischer-Tropsch catalyst with cooling and separation of reactor effluent following each reactor. The low cloud point indicates that the amount of wax in the hydrocarbon products is minimized relative to conventional Fischer-Tropsch conversion. Accordingly, more economical systems can be built and operated because equipment associated with wax removal or wax treatment can be reduced or eliminated.

Process unit for flexible production of alkylate gasoline and distillate

A process unit, comprising: a) an alkylation reactor; and b) a control system that enables the alkylation reactor to be operated in an alkylate mode and in a distillate mode; wherein the alkylation reactor can switch back and forth from operating in the alkylate mode to the distillate mode.

Method of and device for optimizing a hydrogen generating system

A method of and apparatus for optimizing a hydrogen producing system is provided. The method of optimizing the hydrogen producing system comprises producing hydrogen gas using a hydrogen producing formulation and removing a chemical substance that reduces the hydrogen gas producing efficiency. Further, the hydrogen producing system comprises a hydrogen producing catalyst, a hydrogen generating voltage applied to the hydrogen producing catalyst to generate hydrogen gas, and a catalyst regenerating device to regenerate the hydrogen producing catalyst to a chemical state capable of generating the hydrogen gas when a hydrogen generating voltage is applied.

Gas scrubber and related processes

The invention relates to a method for producing a high molecular weight polyethylene terephthalate (PET) via a solid state polymerization system. The method comprises using an acid catalyst to effectuate the conversion of acetaldehyde present within the system to 2-methyl-1,3-dioxolane, which can be readily removed. The invention also relates to PET prepared via this process, which can advantageously exhibit low levels of acetaldehyde.

Process for the production of hexamethlenediamine

It is described a process for the production of hexamethylenediamine by hydrogenation of adiponitrile, comprising an improved step of regeneration of the catalyst. Also described are an equipment for the production of hexamethylenediamine, and a washing apparatus ( 14 ) for implementing the catalyst regeneration step.

Production of aromatics from a methane conversion process

Methods and systems are provided for converting methane in a feed stream to acetylene. The hydrocarbon stream is introduced into a supersonic reactor and pyrolyzed to convert at least a portion of the methane to acetylene. The reactor effluent stream may be treated to convert acetylene to a process stream having aromatic compounds. The acetylene stream can be reacted to generate larger hydrocarbon compounds, which are passed to a cyclization and aromatization reactor to generate aromatics. The method according to certain aspects includes controlling the level of carbon oxides in the hydrocarbon stream.

High-yield process for the synthesis of urea

A process for the direct synthesis of urea from ammonia and carbon dioxide at high pressures and temperatures, with the formation of ammonium carbamate as intermediate, comprising a decomposition step of the ammonium carbamate and stripping of the gases formed, operating substantially at the same pressure as the synthesis step, wherein the recycled liquid streams are fed, at least partially, to the same decomposition and stripping step after being preheated by heat exchange with a stream included in the high-pressure synthesis cycle.

METHOD OF AND DEVICE FOR OPTIMIZING A HYDROGEN GENERATING SYSTEM

A method of and apparatus for optimizing a hydrogen producing system is provided. The method of optimizing the hydrogen producing system comprises producing hydrogen gas using a hydrogen producing formulation and removing a chemical substance that reduces the hydrogen gas producing efficiency. Further, the hydrogen producing system comprises a hydrogen producing catalyst, a hydrogen generating voltage applied to the hydrogen producing catalyst to generate hydrogen gas, and a catalyst regenerating device to regenerate the hydrogen producing catalyst to a chemical state capable of generating the hydrogen gas when a hydrogen generating voltage is applied. 113-. (canceled)14. A method of generating hydrogen gas comprising:a. preparing a hydrogen generating catalyst containing aluminum, copper, and silver; andb. applying a pulsed voltage to the hydrogen generating catalyst.15. The method of claim 14 , further comprising applying a voltage incrementally until a drop of a current.16. The method of claim 14 , further comprising increasing a density of the hydrogen generating catalyst on an electrode.17. The method of claim 14 , further comprising applying a voltage to the aluminum claim 14 , wherein the aluminum comprises an aluminum metal.18. The method of claim 14 , further comprising applying a voltage to the copper claim 14 , wherein the aluminum comprises a copper metal.19. The method of claim 14 , further comprising adding aluminum metal to increase a rate of hydrogen gas production until an applied current drops.20. The method of claim 14 , further comprising adding AgCl.21. The method of claim 14 , further comprising adding HCl.2229-. (canceled)30. A method of forming a hydrogen gas generating system:a. preparing a hydrogen generating catalyst containing aluminum, copper, and silver in a first reactor by applying a base voltage a pulsed voltage to the hydrogen generating catalyst in the first reactor at a pre-hydrogen gas generation phase;b. generating hydrogen gas ...

EFFICIENT OXIDATIVE COUPLING OF METHANE PROCESSES AND SYSTEMS

The present disclosure provides oxidative coupling of methane (OCM) systems for small scale and world scale production of olefins. An OCM system may comprise an OCM subsystem that generates a product stream comprising C compounds and non-C impurities from methane and an oxidizing agent. At least one separations subsystem downstream of, and fluidically coupled to, the OCM subsystem can be used to separate the non-C impurities from the C compounds. A methanation subsystem downstream and fluidically coupled to the OCM subsystem can be used to react Hwith CO and/or COin the non-C impurities to generate methane, which can be recycled to the OCM subsystem. The OCM system can be integrated in a non-OCM system, such as a natural gas liquids system or an existing ethylene cracker. 1. A method for producing hydrocarbon compounds including two or more carbon atoms (C compounds) , the method comprising:{'sub': 2', '2', '2+', '2', '6', '2', '4', '4, '(a) performing an oxidative coupling of methane (OCM) reaction in an OCM reactor to produce an OCM effluent stream comprising carbon monoxide (CO), carbon dioxide (CO), hydrogen (H), one or more C compounds including ethane (CH) and ethylene (CH), and methane (CH);'}(b) directing the OCM effluent stream to a heat recovery steam generator (HRSG) system;(c) with the HRSG system, transferring heat from the OCM effluent stream to a water stream to produce steam;{'sub': 2+', '2', '2', '4, '(d) separating the OCM effluent stream into a first stream comprising at least some of the one or more C compounds and a second stream comprising CO, CO, H, and CH,'}wherein the method has a carbon efficiency of at least about 50%.2. The method of claim 1 , further comprising directing the OCM effluent stream to a cracking unit prior to step (b).3. The method of claim 2 , further comprising directing a stream comprising CHto the cracking unit claim 2 , wherein the stream comprising CHis external to the OCM reactor.4. The method of claim 2 , wherein the ...

METHOD AND APPARATUS FOR EFFICIENT ON-DEMAND PRODUCTION OF H2 AND O2 FROM WATER USING WASTE HEAT AND ENVIRONMENTALLY SAFE METALS

A method of and apparatus for efficient on-demand production of Hand 0from water and heat using environmentally safe metals are disclosed. In one aspect, the apparatus for the hydrogen generation through water decomposition reaction includes a main reactor, an oxidizer reactor, and a computer controlling system. The main reactor contains a hydrogen generating substance, such as aluminium hydroxide. In some embodiments, the main reactor includes hydroxide shuttles, such as Cu ion and Ag ion. In another aspect, the system for hydrogen generation through water decomposition includes the steps of (1) REDOX reaction, (2) pre-generation reaction, (3) generation reaction, (4) regeneration reaction, (5) second hydrogen reaction, and (6) oxygen reaction. 127-. (canceled)28. A method of hydrogen production comprising:a. preparing a solution containing an ionic compound, wherein the solution contains some amount of aluminium, copper, and silver;b. ionizing aluminum, copper, and silver into the solution by an applied voltage; andc. applying a voltage to the solution causing an electric hydrolysis reaction, thereby generating hydrogen gas.29. The method of claim 28 , wherein the voltage magnitude is smaller than 1.0V.30. (canceled)31. The method of claim 28 , wherein the applied voltage used to ionize the aluminum claim 28 , copper claim 28 , and silver is greater than the voltage causing the electric hydrolysis reaction.32. The method of further comprising forming some amount of white precipitate by applying the voltage.33. The method of further comprising heating the solution.34. The method of further comprising passing the solution through some amount of light.35. The method of further comprising an automatic controlling system.36. The method of claim 35 , wherein the automatic controlling system controls a transportation of the solution from a location having electric hydrolysis reactions to a location having photolysis reactions.37. An electric hydrolysis catalyst ...

PRODUCING C5 OLEFINS FROM STEAM CRACKER C5 FEEDS

Producing C5 olefins from steam cracker C5 feeds may include reacting a mixed hydrocarbon stream comprising cyclopentadiene, C5 olefins, and C6+ hydrocarbons in a dimerization reactor where cyclopentadiene is dimerized to dicyclopentadiene. The dimerization reactor effluent may be separated into a fraction comprising the C6+ hydrocarbons and dicyclopentadiene and a second fraction comprising C5 olefins and C5 dienes. The second fraction, a saturated hydrocarbon diluent stream, and hydrogen may be fed to a catalytic distillation reactor system for concurrently separating linear C5 olefins from saturated hydrocarbon diluent, cyclic C5 olefins, and C5 dienes contained in the second fraction and selectively hydrogenating C5 dienes. An overhead distillate including the linear C5 olefins and a bottoms product including cyclic C5 olefins are recovered from the catalytic distillation reactor system. Other aspects of the C5 olefin systems and processes, including catalyst configurations and control schemes, are also described. 1. A process for producing C5 olefins from a C5 feed , comprising linear C5 olefins , branched C5 olefins , C5 dienes , including cyclopentadiene , and one or more C5 paraffins , the process comprising:feeding the C5 feed, a saturated hydrocarbon diluent stream, and hydrogen to a fixed bed selective hydrogenation unit to selectively hydrogenate the C5 dienes, including cyclopentadiene, producing a partially hydrogenated stream comprising linear C5 olefins, branched C5 olefins, and remaining C5 dienes;feeding the partially hydrogenated stream to a catalytic distillation reactor system, wherein the partially hydrogenated stream is introduced below a first catalyst zone; separating the C5 olefins from the saturated hydrocarbon diluent; and', 'selectively hydrogenating at least a portion of the remaining C5 dienes to form additional linear C5 olefins and branched C5 olefins; and, 'concurrently in the catalytic distillation reactor systemrecovering linear ...

SYSTEMS AND METHODS RELATED TO THE PRODUCTION OF METHYL TERT-BUTYL ETHER

Disclosed herein is a system comprising: a) a Fischer-Tropsch reactor comprising a first inlet and a first outlet; b) an olefin separator comprising a second inlet and a second outlet; c) a deisobutanizer comprising a third inlet and a third outlet; d) an iso-butane to isobutylene reactor comprising a fourth inlet and a fourth outlet; and e) a MTBE reactor comprising a fifth inlet, the recited structures are in fluid communication. 1. A method comprising the steps of:a) providing a first product gas stream comprising at least about 1 wt % of a first C4 hydrocarbon product, wherein the first C4 hydrocarbon product comprises a C4 olefin hydrocarbon product comprising isobutylene and a C4 paraffin hydrocarbon product, wherein the C4 paraffin hydrocarbon product comprises n-butane and i-butane;b) separating at least a portion of the C4 olefin hydrocarbon product from the first C4 hydrocarbon product, thereby producing a second C4 hydrocarbon product;c) separating at least a portion of the n-butane from the second C4 hydrocarbon product, thereby producing a third C4 hydrocarbon product;d) isomerizing at least a portion of the separated n-butane into i-butane;e) combining at least a portion of the i-butane produced in step d) with the third C4 hydrocarbon product, thereby producing a fourth C4 hydrocarbon product;producing isobutylene from at least a portion of the fourth C4 hydrocarbon product;g) combining at least a portion of the separated C4 olefin hydrocarbon product and at least a portion of the isobutylene produced in step f), thereby producing a fifth C4 hydrocarbon product; andh) producing methyl tertiary butyl ether (MTBE) from at least a portion of the fifth C4 hydrocarbon product.2. The method of claim 1 , wherein the first product gas stream comprises at least about 5 wt % of the first C4 hydrocarbon product.3. The method of claim 1 , wherein the first product gas stream comprises at least about 10 wt % of the first C4 hydrocarbon product.4. The method of ...

DESALINATION METHODS AND DEVICES USING GEOTHERMAL ENERGY

A method of and apparatus for desalinating sea water using geothermal energy. A low voltage (such as less than 0.9V) is applied to a hydrogen generating catalysts to generate hydrogen and oxygen, wherein geothermal heat is used as a heat source. The hydrogen and oxygen are used to drive a gas turbine to generate electricity. The oxygen and hydrogen are transported away and combusted to generate heat and pure water, as such salt are separated from the pure water. 1. A method of desalination using geothermal heat comprising:a. performing a catalytic electrolysis reaction in a reaction vessel by applying a voltage to a solution containing sea water and a hydrogen generating catalyst, wherein the sea water contains amount of sea salt, and wherein the hydrogen generating catalyst contains aluminium, copper, and silver;b. applying an electric voltage to the hydrogen generating catalyst between 0.4V to 0.9V for generating an amount of oxygen and an amount of hydrogen; andc. generating an amount of pure water by combusting the amount of oxygen and the amount of hydrogen.2. The method of claim 1 , further comprising providing an amount of geothermal heat to the reaction vessel.3. The method of claim 1 , further comprising leaving the salt in the solution.4. The method of claim 1 , wherein the electric voltage is 0.85V.5. The method of claim 1 , further comprising driving an electricity generating turbine using the hydrogen claim 1 , the oxygen claim 1 , or both.6. The method of claim 1 , further comprising separating the pure water generated and an amount of heat generated claim 1 , wherein the pure ware and the heat are generated through a combustion reaction of the hydrogen and the oxygen.7. The method of claim 6 , wherein the water is condensed using a condenser.8. The method of claim 6 , wherein the heat is collected using a heat exchanger.9. The method of claim 6 , further comprising separately recycling back the heat and the water to the reaction vessel.10. The method ...

PROCESS AND PLANT FOR PRODUCING METHANOL FROM SYNTHESIS GASES HAVING A HIGH PROPORTION OF CARBON DIOXIDE

The invention relates to a process for producing methanol and to a plant for producing methanol. A first fresh gas suitable for production of methanol and having a high carbon dioxide content is pre-compressed by a first compressor stage to obtain a second fresh gas. The second fresh gas is merged with a recycle gas stream and further compressed to synthesis pressure in a second compressor stage. Catalytic conversion of the thus obtained synthesis gas stream in a plurality of serially arranged reactor stages with intermediate condensation and separation of the crude methanol reduces the recycle gas amount in the synthesis circuit to such an extent that recycle gas may be directly recycled to the second fresh gas stream, thus ensuring that no recycle gas compressor stage is required and that the total compressor power may be reduced. 1. A process for producing methanol , comprising:a) providing an input gas comprising carbon oxides and hydrogen, wherein the proportion of carbon dioxide in the input gas, based on the total amount of the carbon oxides, is at least 80% by volume;b) introducing the input gas as a first fresh gas stream into a first compressor stage for precompression of the first fresh gas stream to obtain a second fresh gas stream;c) introducing a recycle gas stream and the second fresh gas stream into a second compressor stage for compression of the recycle gas stream and the second fresh gas stream to synthesis pressure to obtain a synthesis gas stream;d) catalytically converting the synthesis gas of the synthesis gas stream in a plurality of serially arranged reactor stages at synthesis pressure to obtain a product stream comprising methanol and unreacted synthesis gas per reactor stage;e) cooling the product stream obtained per reactor stage for condensation and separation of methanol from unreacted synthesis gas and introducing unreacted synthesis gas into a respective subsequent stage of the serially arranged reactor stages;f) withdrawing ...

CONTINUOUS GAS FLUIDIZED BED POLYMERIZATION PROCESS

The invention relates to a process for the preparation of a polyolefin in a reaction system from one or more α-olefin monomers of which at least one is ethylene or propylene, 5 wherein the reaction system comprises a reactor, a product purge bin, a granular feed bin, wherein the granular feed bin is located downstream of the product purge bin, a recovery unit and an extrusion unit directly coupled to the granular fed bin, wherein the reactor comprises a fluidized bed, an expanded section located at or near the top of the reactor, a distribution plate located at the lower part of the reactor and an 10 inlet for a recycle stream located under the distribution plate, wherein the process comprises a) feeding a polymerization catalyst to the fluidized bed in the area above the distribution plate, b) feeding the one or more α-olefin monomers to the reactor, 15 c) circulating fluids from the top of the reactor to the bottom of the reactor, wherein the circulating fluids are cooled using a heat exchanger, resulting in a cooled recycle stream comprising liquid, and wherein the cooled recycle stream is introduced into the reactor using the inlet for the recycle stream, d) withdrawing a stream comprising the polyolefin and fluids from the reactor and 20 passing said stream into the product purge bin, e) purging the product purge bin with a purge stream comprising a first inert gas, preferably nitrogen and steam such that a stream comprising a purged polyolefin and a stream comprising fluids, wherein the stream comprising the fluids is substantially free of steam, is obtained, 25 f) introducing at least part of the stream comprising the fluids back into the reactor via the recovery unit, g) introducing the stream comprising the purged polyolefin into the granular feed bin and h) contacting a deactivating stream comprising steam with the purged polyolefin in the 30 granular feed bin to obtain a polyolefin that is substantially free of active polymerization catalyst. 1. A process ...

OLEFIN CONVERSION PROCESS

Processes for the production of olefins are disclosed, which may include: contacting a hydrocarbon mixture comprising linear butenes with an isomerization catalyst to form an isomerization product comprising 2-butenes and 1-butenes; contacting the isomerization product with a first metathesis catalyst to form a first metathesis product comprising 2-pentene and propylene, as well as any unreacted Colefins, and byproducts ethylene and 3-hexene; and fractionating the first metathesis product to form a C3-fraction and a C5 fraction comprising 2-pentene. The 2-pentene may then be advantageously used to produce high purity 1-butene, 3-hexene, 1-hexene, propylene, or other desired products. 1. A system for the production of olefins , the system comprising: contacting a hydrocarbon mixture comprising linear butenes with an isomerization catalyst to form an isomerization product comprising 2-butenes and 1-butenes; and', {'sub': '4', 'contacting the isomerization product with a first metathesis catalyst to form a first metathesis product comprising 2-pentene and propylene, as well as any unreacted Colefins, and byproducts ethylene and 3-hexene;'}], 'an isomerization/metathesis reaction system fora fractionation system for fractionating the first metathesis product to form a C3-fraction and a C5 fraction comprising 2-pentene as essentially the only C5 olefin; anda flow conduit for feeding at least a portion of the C3-fraction to the isomerization/metathesis reaction system.2. The system of claim 1 , wherein the flow conduit for recycling the C3-fraction is configured to introduce the C3-fraction upstream of the isomerization catalyst claim 1 , upstream of the metathesis catalyst claim 1 , or both.3. The system of claim 1 , further comprising a metathesis reactor for contacting ethylene and the C5 fraction with a second metathesis catalyst claim 1 , which may be the same or different than the first metathesis catalyst claim 1 , to convert at least a portion of the 2-pentene and ...

ETHYLENE-TO-LIQUIDS SYSTEMS AND METHODS

Integrated systems are provided for the production of higher hydrocarbon compositions, for example liquid hydrocarbon compositions, from methane using an oxidative coupling of methane system to convert methane to ethylene, followed by conversion of ethylene to selectable higher hydrocarbon products. Integrated systems and processes are provided that process methane through to these higher hydrocarbon products. 1. A system , comprising:{'sub': 2', '4', '2', '4', '3', '6', '2', '2', '4, 'an ethylene-to-liquids (ETL) reactor that (i) receives an olefin feed stream at a first temperature, said olefin feed stream comprising (1) ethylene (CH) at a concentration of at least about 0.5 mole percent (mol %), (2) CHand propylene (CH) at a combined concentration of at most about 10 mol %, and (3) carbon monoxide (CO) or carbon dioxide (CO), and (ii) as part of an ETL process, facilitates conversion of CHto higher hydrocarbon products with the aid of an ETL catalyst to yield a product stream comprising said higher hydrocarbon products that is at a second temperature which is higher than said first temperature, wherein said ETL process liberates heat, wherein said higher hydrocarbon products comprise an olefin compound and an aromatic compound; and'}a separations module in fluid communication with said ETL reactor that recovers from said product stream a liquid stream comprising said higher hydrocarbon products, wherein said higher hydrocarbon products include (i) at least 5 compounds having 5 different carbon numbers, said 5 different carbon numbers selected from 4 through 20, wherein each of said at least 5 compounds is at a concentration of at least 5 weight percent (wt %) of said liquid stream, and (ii) a paraffin compound, an isoparaffin compound, and a naphthene compound,wherein at least about 80% of said heat liberated in said ETL process provides a difference between said first temperature and said second temperature of between about 50° C. and about 150° C.2. The system ...

METHOD AND APPARATUS FOR CARBONYLATING METHANOL WITH ACETIC ACID ENRICHED FLASH STREAM

A carbonylation process for producing acetic acid including: (a) carbonylating methanol or its reactive derivatives in the presence of a Group VIII metal catalyst and methyl iodide promoter to produce a liquid reaction mixture including acetic acid, water, methyl acetate and methyl iodide; (b) feeding the liquid reaction mixture at a feed temperature to a flash vessel which is maintained at a reduced pressure; (c) heating the flash vessel while concurrently flashing the reaction mixture to produce a crude product vapor stream, wherein the reaction mixture is selected and the flow rate of the reaction mixture fed to the flash vessel as well as the amount of heat supplied to the flash vessel is controlled such that the temperature of the crude product vapor stream is maintained at a temperature less than 90° F. cooler than the feed temperature of the liquid reaction mixture to the flasher and the concentration of acetic acid in the crude product vapor stream is greater than 70% by weight of the crude product vapor stream. 125.-. (canceled)26. A carbonylation process for producing acetic acid comprising:(a) carbonylating methanol or its reactive derivatives in a reactor in the presence of a rhodium metal catalyst and methyl iodide promoter to produce a liquid reaction mixture including acetic acid, water, methyl acetate and methyl iodide;(b) feeding the liquid reaction mixture to a flash vessel and heating the liquid reaction mixture in the flash vessel to separate the liquid reaction mixture into a crude product vapor stream and a catalyst solution;(c) recycling the catalyst solution to the reactor;(d) separating the crude product vapor stream in a first distillation column into an overhead stream comprising methyl iodide, methyl acetate and water and process stream comprising acetic acid; and(e) condensing the overhead stream and separating the condensed overhead stream into an aqueous stream and an organic stream,wherein the ratio of the crude product vapor stream ...

PROCESSES FOR REFORMING AND TRANSALKYLATING HYDROCARBONS

Processes for reforming and transalkylating hydrocarbons are disclosed. A method for processing a hydrocarbon stream includes the steps of separating para-xylene from a first mixed-xylene and ethylbenzene-containing stream to produce a first non-equilibrium xylene and ethylbenzene stream and isomerizing the first non-equilibrium xylene and ethylbenzene stream to produce additional para-xylene. The method further includes transalkylating a toluene stream to produce a second mixed-xylene and ethylbenzene-containing stream, separating para-xylene from the second mixed-xylene and ethylbenzene-containing stream to produce a second non-equilibrium xylene and ethylbenzene stream, and isomerizing the second non-equilibrium xylene and ethylbenzene stream using a liquid phase isomerization process to produce additional para-xylene. 1. A process for processing a hydrocarbon stream comprising the steps of:separating para-xylene from the first mixed-xylene and ethylbenzene-containing stream to produce a first non-equilibrium xylene and ethylbenzene stream;isomerizing the first non-equilibrium xylene and ethylbenzene stream to produce additional para-xylene;transalkylating a toluene stream to produce a second mixed-xylene and ethylbenzene-containing stream;separating para-xylene from the second mixed-xylene and ethylbenzene-containing stream to produce a second non-equilibrium xylene and ethylbenzene stream; andisomerizing the second non-equilibrium xylene and ethylbenzene stream using a liquid phase isomerization process to produce additional para-xylene.2. The process of claim 1 , wherein the first mixed-xylene and ethylbenzene-containing stream comprises a greater proportion of ethylbenzene than does the second mixed-xylene and ethylbenzene-containing stream.3. The process of claim 1 , further comprising reforming a naphtha-containing hydrocarbon stream to produce the first mixed-xylene and ethylbenzene-containing stream and the toluene stream.4. The process of claim 3 , ...

METHOD AND APPARATUS FOR CARBONYLATING METHANOL WITH ACETIC ACID ENRICHED FLASH STREAM

A carbonylation process for producing acetic acid including: (a) carbonylating methanol or its reactive derivatives in the presence of a Group VIII metal catalyst and methyl iodide promoter to produce a liquid reaction mixture including acetic acid, water, methyl acetate and methyl iodide; (b) feeding the liquid reaction mixture at a feed temperature to a flash vessel which is maintained at a reduced pressure; (c) heating the flash vessel while concurrently flashing the reaction mixture to produce a crude product vapor stream, wherein the reaction mixture is selected and the flow rate of the reaction mixture fed to the flash vessel as well as the amount of heat supplied to the flash vessel is controlled such that the temperature of the crude product vapor stream is maintained at a temperature less than 90° F. cooler than the feed temperature of the liquid reaction mixture to the flasher and the concentration of acetic acid in the crude product vapor stream is greater than 70% by weight of the crude product vapor stream. 125-. (canceled)26. A carbonylation process for producing acetic acid comprising:carbonylating methanol or its reactive derivatives in the presence of a rhodium catalyst in a reactor to produce a liquid reaction mixture comprising acetic acid, the rhodium metal catalyst, water, iodide catalyst stabilizer, methyl acetate and methyl iodide;flashing the liquid reaction mixture in a flash vessel to form a crude product vapor stream comprising acetic acid, methyl iodide, and methyl acetate, and a catalyst solution comprising the rhodium metal catalyst, iodide catalyst stabilizer, methyl acetate, and water; and distilling the crude product vapor stream to form a first overhead, and a side stream comprising acetic acid; and', 'distilling the side stream into a second overhead, and a purified acetic acid stream,, 'an acetic acid collection step comprisingwherein the catalyst solution comprises methyl acetate in an amount less than or equal to 1.9% by weight ...

ETHYLENE-TO-LIQUIDS SYSTEMS AND METHODS

Integrated systems are provided for the production of higher hydrocarbon compositions, for example liquid hydrocarbon compositions, from methane using an oxidative coupling of methane system to convert methane to ethylene, followed by conversion of ethylene to selectable higher hydrocarbon products. Integrated systems and processes are provided that process methane through to these higher hydrocarbon products. 1111.-. (canceled)112. A method , comprising:(a) directing an olefin-containing stream comprising an olefin into an ethylene-to-liquids (ETL) reactor comprising an ETL catalyst that facilitates conversion of at least a portion of said olefin to higher hydrocarbon compounds to yield an ETL product stream comprising said higher hydrocarbon compounds;{'sub': 4+', '3, '(b) directing at least a portion of said ETL product stream into a de-propanizer that separates said higher hydrocarbon compounds into a bottom stream comprising hydrocarbon compounds with four or more carbon atoms (C compounds) and an overhead stream comprising hydrocarbon compounds with three carbon atoms (Ccompounds); and'}{'sub': '3', '(c) directing at least a portion of said Ccompounds into said ETL reactor.'}113. The method of wherein said olefin comprises ethylene claim 112 , propylene claim 112 , or a combination thereof.114. The method of claim 112 , further comprising claim 112 , prior to (a) claim 112 , directing a hydrocarbon feedstream comprising feedstream hydrocarbons into a cracking reactor comprising a cracking catalyst that facilitates a cracking of said feedstream hydrocarbons to produce a cracked stream comprising cracked hydrocarbons claim 112 , wherein said cracked hydrocarbons have a lower molecular weight than said feedstream hydrocarbons claim 112 , and using at least a subset of said cracked hydrocarbons to generate said olefin-containing stream.115. The method of claim 114 , further comprising directing said cracked stream into a separations unit that separates said ...

Apparatus and process for the controlled reduction of organic material via microwave radiation

A controllable, continuous-feed system and process for the reduction or depolymerization of organic materials using microwave energy in a reducing, substantially oxygen-reduced atmosphere. The microwave energy is generated by a plurality of magnetrons in a microwave tunnel. Gaseous products may be extracted from the microwave tunnel for recycling and/or analysis. A collector such as a liquid trap may be used to separately collect floating and sinking constituents of the solid products while preventing the escape of the reducing atmosphere from the system.

Methods and apparatus for producing jet-range hydrocarbons

Methods and apparatus are provided for producing jet-range hydrocarbons from biorenewable sources, such as oligomerizing C 3 -C 8 biorenewable olefins, for example, derived from C 3 -C 8 alkanol products of fermentation of biomass. Production of jet-range hydrocarbons is increased by employing an additional oligomerization zone for oligomerizing naphtha separated from the effluent of a primary oligomerization zone wherein the C 3 -C 8 biorenewable olefins were first subjected to oligomerization.

Processing biomass

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

Ceramic oxygen transport membrane array reactor and reforming method

A commercially viable modular ceramic oxygen transport membrane reforming reactor for producing a synthesis gas that improves the thermal coupling of reactively-driven oxygen transport membrane tubes and catalyst reforming tubes required to efficiently and effectively produce synthesis gas.

OXIDATIVE COUPLING OF METHANE IMPLEMENTATIONS FOR OLEFIN PRODUCTION

The present disclosure provides oxidative coupling of methane (OCM) systems for small scale and world scale production of olefins. An OCM system may comprise an OCM subsystem that generates a product stream comprising C compounds and non-C impurities from methane and an oxidizing agent. At least one separations subsystem downstream of, and fluidically coupled to, the OCM subsystem can be used to separate the non-C impurities from the C compounds. A methanation subsystem downstream and fluidically coupled to the OCM subsystem can be used to react Hwith CO and/or COin the non-C impurities to generate methane, which can be recycled to the OCM subsystem. The OCM system can be integrated in a non-OCM system, such as a natural gas liquids system or an existing ethylene cracker. 1. A method for producing hydrocarbon compounds including two or more carbon atoms (C compounds) , the method comprising:{'sub': 2', '2', '2+', '4, '(a) performing an oxidative coupling of methane (OCM) reaction in an OCM reactor to produce an OCM effluent stream comprising carbon dioxide (CO), carbon monoxide (CO), hydrogen (H), one or more C compounds, and methane (CH);'}{'sub': 2+', '2', '2', '4, '(b) separating the OCM effluent stream into a first stream comprising at least some of the one or more C compounds and a second stream comprising CO, CO, H, and CH;'}{'sub': 4', '2', '2, '(c) separating the second stream in a pressure swing adsorption (PSA) unit to produce an OCM reactor feed comprising CHand a third stream comprising Hand CO and/or CO; and'}(d) directing the OCM reactor feed to the OCM reactor.2. The method of claim 1 , further comprising claim 1 , prior to step (b) claim 1 , directing the OCM effluent stream to a post-bed cracking unit to generate olefins from alkanes in the OCM effluent.3. The method of claim 2 , further comprising directing a fourth stream comprising ethane to the post-bed cracking unit.4. The method of claim 1 , further comprising directing the third stream to a ...

Reactor Systems and Processes Related Thereto

A process for separating components of a reactor off gas is provided. A related reactor system is also provided. The reactor system may include a high pressure tubular reactor and/or an autoclave reactor and may be used for the production polyolefin polymers.

INTEGRATED INSTALLATION AND METHOD FOR FLEXIBLY USING ELECTRICITY

The present invention relates to an integrated plant which comprises a plant for the electrothermic production of hydrogen cyanide and a plant for electricity generation, the plant for the electrothermic production of hydrogen cyanide being connected to the plant for electricity generation via a conduit and electricity being generated in the plant for electricity generation from a product gas obtained in the plant for the electrothermic production of hydrogen cyanide. This integrated plant affords flexible use of electricity by a method in which, at times of a high electricity supply, the plant for the electrothermic production of hydrogen cyanide is operated and at least some of the hydrogen and/or gaseous hydrocarbons obtained in addition to hydrogen cyanide is stored and, at times of a low electricity supply, stored hydrogen and/or gaseous hydrocarbons are fed to the plant for electricity generation. 123-. (canceled)24. An integrated plant , comprising an electrothermic hydrogen cyanide production plant and an electrical power plant , wherein the electrothermic hydrogen cyanide production plant is connected to the electrical power plant via a conduit feeding a product gas obtained in the electrothermic hydrogen cyanide production plant to the electrical power plant.25. The integrated plant of claim 24 , wherein the electrical power plant comprises a fuel cell.26. The integrated plant of claim 24 , wherein the electrical power plant comprises a power generating plant with a turbine.27. The integrated plant of claim 26 , wherein the power generating plant with a turbine comprises a gas turbine that can be operated with hydrogen claim 26 , a hydrocarbon-containing gas claim 26 , or both.28. The integrated plant of claim 26 , wherein the power generating plant with a turbine is a gas-and-steam turbine power plant.29. The integrated plant of claim 24 , wherein the electrothermic hydrogen cyanide production plant comprises an arc reactor.30. The integrated plant of ...

DESALINATION METHODS AND DEVICES USING GEOTHERMAL ENERGY

A method of and apparatus for desalinating sea water using geothermal energy. A low voltage (such as less than 0.9V) is applied to a hydrogen generating catalysts to generate hydrogen and oxygen, wherein geothermal heat is used as a heat source. The hydrogen and oxygen are used to drive a gas turbine to generate electricity. The oxygen and hydrogen are transported away and combusted to generate heat and pure water, as such salt are separated from the pure water. 120-. (canceled)21. A method of desalination of sea water using geothermal heat comprising:a. providing an amount of sea water with sea salt and an amount of geothermal heat as a heat source to a reaction vessel;b. generating an amount of oxygen and an amount of hydrogen by performing a catalytic electrolysis reaction by applying an electric voltage between 0.4V to 0.9V to a hydrogen generating catalyst having aluminum, copper, and silver in the sea water in the reaction vessel;c. driving a turbine to generate an amount of generated electricity by using a gas pressure generated by the amount of hydrogen, the amount of oxygen, or both;d. combusting the amount of hydrogen and the amount of oxygen generating an amount of desalinated water and generated heat; ande. providing the amount of generated electricity or the amount of generated heat in assisting the catalytic electrolysis reaction in the reaction vessel.22. The method of claim 21 , further comprising leaving the sea salt in the reaction vessel.23. The method of claim 21 , wherein the electric voltage is 0.85V.24. The method of claim 21 , further comprising separating the desalinated water and the amount of generated heat.25. The method of claim 24 , further comprising collecting the generated heat using a heat exchanger.26. The method of claim 21 , further comprising condensing the desalinated water using a condenser.27. The method of claim 21 , wherein the solution is a non-acidic solution.28. A sea water desalination method comprising:a. providing an ...

PRODUCING C5 OLEFINS FROM STEAM CRACKER C5 FEEDS

Producing C5 olefins from steam cracker C5 feeds may include reacting a mixed hydrocarbon stream comprising cyclopentadiene, C5 olefins, and C6+ hydrocarbons in a dimerization reactor where cyclopentadiene is dimerized to dicyclopentadiene. The dimerization reactor effluent may be separated into a fraction comprising the C6+ hydrocarbons and dicyclopentadiene and a second fraction comprising C5 olefins and C5 dienes. The second fraction, a saturated hydrocarbon diluent stream, and hydrogen may be fed to a catalytic distillation reactor system for concurrently separating linear C5 olefins from saturated hydrocarbon diluent, cyclic C5 olefins, and C5 dienes contained in the second fraction and selectively hydrogenating C5 dienes. An overhead distillate including the linear C5 olefins and a bottoms product including cyclic C5 olefins are recovered from the catalytic distillation reactor system. Other aspects of the C5 olefin systems and processes, including catalyst configurations and control schemes, are also described. 1. (canceled)2. (canceled)3. (canceled)4. (canceled)5. (canceled)6. (canceled)7. (canceled)8. (canceled)9. (canceled)10. (canceled)11. (canceled)12. (canceled)13. (canceled)14. (canceled)15. (canceled)16. (canceled)17. (canceled)18. (canceled)19. (canceled)20. (canceled)21. (canceled)22. (canceled)23. (canceled)24. (canceled)25. (canceled)26. (canceled)27. (canceled)28. (canceled)29. A process for the selective hydrogenation of C5 dienes in a mixed C5 hydrocarbon stream , comprising:feeding hydrogen and a C5-olefin containing stream comprising linear pentenes, dienes, acetylenes, and a diluent compound to a catalytic distillation reactor system; hydrogenating the acetylenes and dienes; and', 'fractionating the C5-olefin containing stream;, 'concurrently in the catalytic distillation reactor systemrecovering an overheads fraction comprising the pentenes;recovering a bottoms fraction; a first reaction zone disposed below a C5-olefin containing stream ...

PROCESSING BIOMASS

Biomass (e.g., plant biomass, animal biomass, and municipal waste biomass) is processed to produce useful products, such as fuels. For example, systems can use feedstock materials, such as cellulosic and/or lignocellulosic materials and/or starchy or sugary materials, to produce ethanol and/or butanol, e.g., by fermentation. 1. A method comprising:{'sup': '3', 'densifying a biomass material comprising starch, the biomass material having a starting bulk density of less than 0.25 g/m, to produce a densified biomass material;'}irradiating the densified biomass material; andsaccharifying the irradiated material.2. The method of wherein the densified biomass material is irradiated with ionizing radiation.3. The method of wherein the ionizing radiation is delivered using an electron beam.4. The method of wherein the densified biomass material has a bulk density of greater than 0.3 g/cm.5. The method of wherein the densified biomass material has a bulk density of greater than 0.6 g/cm.6. The method of wherein densifying comprises sealing the material in a bag and then evacuating the bag.7. The method of wherein densifying is performed at a first location and the method further comprises transporting the densified material to a second location prior to saccharifying.8. The method of wherein irradiating is performed at the second location.9. The method of wherein the bag is formed of a material that dissolves in water.10. The method of wherein densifying comprises adding a binder to the biomass material to form a mixture and applying pressure to the mixture.11. The method of wherein the binder is water-soluble.12. The method of wherein densifying comprises processing the lignocellulosic material in a pellet mill.13. The method of wherein the densified biomass material is in the form of a mat claim 1 , roll or bale.14. The method of wherein claim 1 , prior to densifying claim 1 , the biomass material is in the form of particles.15. The method of wherein the biomass material ...

Liquid fuel cpox reformers and methods of cpox reforming

A liquid fuel catalytic partial oxidation (CPOX) reformer can include a plurality or an array of spaced-apart CPOX reactor units, each reactor unit including an elongate tube having a gas-permeable wall with internal and external surfaces, the wall enclosing an open gaseous flow passageway with at least a portion of the wall having CPOX catalyst disposed therein and/or comprising its structure. The catalyst-containing wall structure and open gaseous flow passageway enclosed thereby define a gaseous phase CPOX reaction zone, the catalyst-containing wall section being gas-permeable to allow gaseous CPOX reaction mixture to diffuse therein and hydrogen rich product reformate to diffuse therefrom. At least the exterior surface of the CPOX reaction zone can include a hydrogen barrier. The liquid fuel CPOX reformer can include a vaporizer, one or more igniters, and a source of liquid reformable fuel.

A METHANOL SYNTHESIS PROCESS LAYOUT FOR LARGE PRODUCTION CAPACITY

A process layout for large scale methanol synthesis comprises one or more boiling water reactors and one or more radial flow reactors in series, the boiling water reactor(s) being fed with approximately fresh make-up syngas. The methanol synthesis loop comprises a make-up gas compressor K a recycle gas compressor K two or more boiling water converters for methanol synthesis (A A . . . ), a radial flow converter (B) for methanol synthesis, a steam drum (V), a high pressure separator (V), a low pressure separator (V), feed effluent heat exchangers (E and E), a wash column (C), an air cooler (E) and a water cooler (E). 1. A process layout for methanol synthesis , comprising one or more boiling water reactors and one or more radial flow reactors in series , wherein the boiling water reactor(s) is/are fed with approximately fresh make-up syngas.212. A process layout for a methanol synthesis loop comprising a make-up gas compressor K , a recycle gas compressor K , two or more boiling water converters for methanol synthesis , a radial flow converter for methanol synthesis , a steam drum , a high pressure separator , a low pressure separator , feed effluent heat exchangers , a wash column , an air cooler and a water cooler.3. A process layout for a methanol synthesis loop according to claim 2 , wherein the purge gas is split from the effluent product gas as wet gas (including methanol) and washed with water to recover methanol at approximately the synthesis loop pressure.4. A process layout for a methanol synthesis loop according to claim 2 , wherein the radial flow reactor temperature is controlled by adjusting the purge gas and hence the level of inert gas in the reactor inlet.5. A process layout for a methanol synthesis loop according to claim 2 , wherein the radial flow reactor has a structure claim 2 , which requires no cooling device.6. A process layout for a methanol synthesis loop according to claim 2 , wherein only one train of cooling equipment is used. The ...

Olefin conversion process

Processes for the production of olefins are disclosed, which may include: contacting a hydrocarbon mixture comprising linear butenes with an isomerization catalyst to form an isomerization product comprising 2-butenes and 1-butenes; contacting the isomerization product with a first metathesis catalyst to form a first metathesis product comprising 2-pentene and propylene, as well as any unreacted C 4 olefins, and byproducts ethylene and 3-hexene; and fractionating the first metathesis product to form a C3− fraction and a C5 fraction comprising 2-pentene. The 2-pentene may then be advantageously used to produce high purity 1-butene, 3-hexene, 1-hexene, propylene, or other desired products.

LIQUID FUEL REFORMER INCLUDING A VAPORIZER AND METHOD OF REFORMING LIQUID REFORMABLE FUEL

A liquid fuel reformer includes a fuel vaporizer which utilizes heat from an upstream source of heat, specifically, an electric heater, operable in the start-up mode of the reformer, and therefore independent of the reforming reaction zone of the reformer, to vaporize fuel in a downstream vaporization zone. 118-. (canceled)19. A method of reforming a liquid reformable fuel , the method comprising:introducing an oxygen-containing gas into a conduit for routing fluids toward an inlet of a reformer;heating a stream of the oxygen-containing gas with at least one of a first source of heat comprising an electric heater disposed in the conduit and a second source of heat disposed in the conduit comprising heat of exotherm from the liquid fuel reformer and/or a hydrogen reformate-consuming device external to the liquid fuel reformer to provide a stream of heated oxygen-containing gas;introducing into the stream of heated oxygen-containing gas through or proximate to a vaporizer a liquid reformable fuel to provide a heated gaseous reforming reaction mixture; andreforming the heated gaseous reforming reaction mixture to produce a hydrogen-rich reformate.20. The method of claim 19 , comprising:heating the stream of the oxygen-containing gas and/or the stream of heated oxygen-containing gas with a third source of heat comprising an electric heater disposed in the conduit downstream from the first and second sources of heat and upstream from the vaporizer.21. The method of claim 20 , comprising:discontinuing heating the stream of oxygen-containing gas with the first source of heat; andheating the stream of oxygen-containing gas with the second and third sources of heat.22. The method of comprising adjusting the heat supplied by the second source and/or third source of heat.23. The method of claim 19 , comprising heating the liquid reformable fuel using the second source of heat and/or the third source of heat claim 19 , when present claim 19 , prior to introducing the liquid ...

PROCESS FOR PRODUCTION OF AMMONIA AND DERIVATIVES, IN PARTICULAR UREA

A process for producing ammonia and a derivative of ammonia from a natural gas feed comprising conversion of natural gas into a make-up synthesis gas; synthesis of ammonia; use of said ammonia to produce said derivative of ammonia, wherein a portion of the natural gas feed is used to fuel a gas turbine; power produced by said gas turbine is transferred to at least one power user of the process, such as a compressor; heat is recovered from exhaust gas of said gas turbine, and at least part of said heat is recovered as low-grade heat available at a temperature not greater than 200° C., to provide process heating to at least one thermal user of the process, such as CO2 removal unit or absorption chiller; a corresponding plant and method of modernization are also disclosed. 1. A process for producing ammonia and a derivative of ammonia from a natural gas feed comprising:conversion of natural gas into synthesis gas in a front-end section;synthesis of ammonia from said synthesis gas in a synthesis loop;use of at least part of said ammonia to produce said derivative of ammonia,said process being carried out with power users requiring a mechanical power for operation, and thermal users requiring a heat input for operation;wherein:a portion of said natural gas feed is used to fuel a gas turbine;power produced by said gas turbine is used to cover at least partially the power demand of said power users;heat is recovered from exhaust gas of said gas turbine, and at least part of said heat is recovered as low-grade heat, to provide process heating to at least one of said thermal users,said low-grade heat being transferred from said exhaust gas to said at least one of said thermal users via a heat exchange medium, said medium being heated by indirect heat exchange with the exhaust gas to a temperature which is not greater than 200° C.2. The process according to claim 1 , said power being transferred from said gas turbine to at least one of said power users in a mechanical or ...

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 ...

PROCESS FOR PRODUCTION OF AMMONIA AND DERIVATIVES, IN PARTICULAR UREA

A process for producing ammonia and a derivative of ammonia from a natural gas feed comprising conversion of natural gas into a make-up synthesis gas; synthesis of ammonia; use of said ammonia to produce said derivative of ammonia, wherein a portion of the natural gas feed is used to fuel a gas turbine; power produced by said gas turbine is transferred to at least one power user of the process, such as a compressor; heat is recovered from exhaust gas of said gas turbine, and at least part of said heat is recovered as low-grade heat available at a temperature not greater than 200° C., to provide process heating to at least one thermal user of the process, such as COremoval unit or absorption chiller; a corresponding plant and method of modernization are also disclosed. 1. A method of modernizing a plant for producing ammonia and a derivative of ammonia , particularly urea , wherein:said plant comprises a front-end section for generation of ammonia make-up synthesis gas; a synthesis loop for synthesis of ammonia from said make-up synthesis gas;a section for the conversion of at least part of the synthesized ammonia into said derivative;the plant also comprising power users and thermal users;wherein:the provision of at least one gas turbine, and the provision of suitable power transfer means to transfer the power produced by said turbine to at least one of said power users,the provision of heat recovery means for recovering a low-grade heat from exhaust gas of said gas turbine, by indirect heat exchange with a medium, said medium being heated by the exhaust gas to a temperature not greater than 200° C.,the provision of the so recovered low-grade heat to at least one of said thermal users of the plant, or to at least one newly-installed thermal user.2. The method according to claim 1 , wherein the provision of said power transfer means includes: the provision of an electrical motor and the provision of an electrical generator coupled to said gas turbine.3. The method ...

HYDROGEN SULFIDE GAS PRODUCTION PLANT SYSTEM AND METHOD FOR RECOVERING AND USING HYDROGEN SULFIDE GAS

The present invention allows low-concentration hydrogen sulfide gas to be recovered and supplied to a processing plant that uses hydrogen sulfide gas. The hydrogen sulfide gas production plant is provided with a first supply pipe that supplies hydrogen sulfide gas obtained from a sulfur recovery facility to a processing plant, and a second supply pipe that is branched at a predetermined point in the first supply pipe and supplies the hydrogen sulfide gas from the sulfur recovery facility to the processing plant. The first supply pipe has a concentration meter that is provided on the upstream side than the branch point and measures the concentration of the hydrogen sulfide gas. The first supply pipe and the second supply pipe have ON/OFF valves that are provided on the downstream side of the branch point and perform ON/OFF control of the supply to the processing plant through the supply pipe. 1. A hydrogen sulfide gas production plant system , comprising:a plurality of systems of hydrogen sulfide gas production plants provided with at least a reaction facility that generates hydrogen sulfide gas from sulfur and hydrogen gas, a plurality of cooling facilities that cool the generated hydrogen sulfide gas, and a sulfur recovery facility that recovers sulfur contained in the hydrogen sulfide gas,the hydrogen sulfide gas production plant system that:the hydrogen sulfide gas production plant of each system is provided witha first supply pipe that supplies the hydrogen sulfide gas from which sulfur has been recovered in the sulfur recovery facility to a processing plant that uses hydrogen sulfide gas, anda second supply pipe that is branched at a predetermined point in the first supply pipe and supplies the hydrogen sulfide gas from the sulfur recovery facility to the processing plant;the first supply pipe has a concentration meter that is provided on the sulfur recovery facility side than the predetermined branch point and measures the concentration of the hydrogen sulfide ...

USE OF UREA SYNTHESIS PURGE GAS IN AN INTEGRATED AMMONIA-UREA PROCESS AND RELATED PLANT

An ammonia-urea plant where purge gas stream () generated in the urea section is used as ammonia source for selective catalytic reduction of nitrogen oxides in combustion fumes () which are emitted by the ammonia section; a related process and a method for modification of an ammonia-urea plant are also disclosed. 1. A process where:ammonia is synthesized in an ammonia section (AM) of an ammonia-urea integrated plant by reacting hydrogen and nitrogen, said hydrogen being produced by reforming of a hydrocarbon source;at least part of said ammonia is reacted in a urea section (UR) of said plant for the synthesis of urea (U), and a purge gas stream containing some ammonia is generated by said urea section, wherein said purge gas stream is used as an ammonia source for selective catalytic reduction of nitrogen oxides contained in combustion fumes produced in the ammonia-urea plant.2. The process according to claim 1 , where said combustion fumes are emitted by the ammonia section (AM) of said ammonia-urea plant.3. The process according to claim 1 , wherein said purge gas stream claim 1 , or at least a portion thereof claim 1 , is fed to a selective catalytic reduction unit (SCR) or is mixed with said combustion fumes before entering said reduction unit.4. An ammonia-urea plant including an ammonia section (AM) and a urea section (UR) claim 1 , wherein ammonia is synthesized in the ammonia section from hydrogen and nitrogen claim 1 , said hydrogen being obtained via reforming of a hydrocarbon source claim 1 , and at least part of said ammonia is passed to the urea section for the synthesis of urea claim 1 , said plant being characterized by comprising a selective catalytic reduction unit (SCR) for removal of nitrogen oxides from combustion fumes produced in the plant claim 1 , and by comprising a line arranged to feed a purge gas stream generated by the urea section to said selective catalytic reduction unit (SCR) claim 1 , for use of said purge gas stream as an ammonia ...

Energy efficient polyolefin process

A manufacturing system for producing polyolefin includes a polymerization reactor, a flash chamber, and a purge column. In certain embodiments, the purge column may receive a solids stream directly from the flash chamber. Further, the purge column may function as a feed tank for an extruder within an extrusion/loadout system. According to certain embodiments, the manufacturing system may be configured to consume less than 445 kilowatt-hours of energy per metric ton of polyolefin produced based on consumption of electricity, steam, and fuel gas.

APPARATUS AND PROCESS FOR THE PREPARATION OF ACETYLENE AND SYNTHESIS GAS

An apparatus () for the preparation of acetylene and synthesis gas by partial oxidation of hydrocarbons with oxygen is proposed. The apparatus () comprises a reactor (), wherein the reactor () comprises a burner block () with a furnace chamber for the preparation of a composition C comprising at least acetylene and substituted acetylene, a first scrubber () which is constructed for adding a solvent to the composition C to obtain a composition C, a second scrubber () which is constructed for adding the solvent to the composition C to obtain a composition C, a first stripper () which is constructed for stripping the composition C to obtain a composition C comprising the substituted acetylene, acetylene and the solvent and for separating off the acetylene, a first column () which is constructed for partial degassing of the composition C under a pressure of from 1.0 bar to 1.5 bar to obtain a composition C and a first amount A of the solvent, a second stripper () to which the composition C can be fed for stripping a composition C to obtain a second amount A of the solvent and a composition C, a third stripper () which is constructed for stripping the solvent from the first scrubber () to obtain a composition C, wherein the third striper () is connected to the second stripper () for feeding the composition C to the second stripper (), an apparatus () for adding a diluting gas to the composition C, which is arranged between the first column () and the second stripper (), a second column () which is constructed for adding water to the composition C to obtain a composition C comprising a third amount A of the solvent and water and to obtain a composition C comprising the substituted acetylene, and a mixing condenser () which is constructed for adding water to the composition C to obtain a composition C comprising the substituted acetylene. 1: An apparatus for preparation of acetylene and synthesis gas by partial oxidation of hydrocarbons with oxygen , comprising:{'b': '1', ...

Process for producing nitrobenzene

The present invention relates to a process for the continuous production of nitrobenzene by the nitration of benzene with nitric acid and sulphuric acid under adiabatic conditions, not the entire production plant being shut down during a production stop, but the production plant being entirely or at least partly operated in recirculation mode. The invention further relates to a plant for producing nitrobenzene and to a method for operating a plant for producing nitrobenzene.

REACTOR SYSTEM

A reactor tank is provided having an enzyme inlet, a heating jacket positioned around the exterior center of the tank, a gas outlet for communicating with a vacuum apparatus to create a vacuum within the reactor tank and for communicating with a condensing unit, a first gas inlet for receiving gas from a feed tank and a first liquid outlet for recirculating the liquid from the first liquid outlet back to the feed tank. The reactor tank further includes a sparged unit and a screen positioned within the tank between the sparged unit and the first liquid outlet, where the sparged unit is connected to the first gas inlet for receiving gas from the feed tank. The reactor tank is utilized in a reactor system further including a condensing unit, vacuum pump or venturi valve, a first feed tank connected to the first gas inlet, a coalescer having at least one circulation pipe and a first circulation pump connected to the first liquid outlet for circulating a portion of the liquid dispelled from the liquid outlet to the coalescer, which after being filtered through coalescer is recirculated through circulation pipe back to the first feed tank. 1. A reactor comprising:a tank having a catalyst inlet;a heating jacket positioned around the exterior center of the tank;a gas outlet for communicating with a contact condenser unit for the continuous removed of water from the tank during use;a first gas inlet for receiving gas from a feed tank;a first liquid outlet for recirculating the liquid from the first liquid outlet back to the feed tank;a sparged unit positioned within the tank and in communication with the first gas inlet to sparge the gas received through the first gas inlet; anda screen positioned within the tank between the sparged unit and the first liquid outlet.2. The reactor of further includes a second gas outlet on the second end of the vessel to vent air from the reactor.3. The reactor of further including an agitator mount.4. The reactor of further including a raw ...

PRODUCING C5 OLEFINS FROM STEAM CRACKER C5 FEEDS

Producing C5 olefins from steam cracker C5 feeds may include reacting a mixed hydrocarbon stream comprising cyclopentadiene, C5 olefins, and C6+ hydrocarbons in a dimerization reactor where cyclopentadiene is dimerized to dicyclopentadiene. The dimerization reactor effluent may be separated into a fraction comprising the C6+ hydrocarbons and dicyclopentadiene and a second fraction comprising C5 olefins and C5 dienes. The second fraction, a saturated hydrocarbon diluent stream, and hydrogen may be fed to a catalytic distillation reactor system for concurrently separating linear C5 olefins from saturated hydrocarbon diluent, cyclic C5 olefins, and C5 dienes contained in the second fraction and selectively hydrogenating C5 dienes. An overhead distillate including the linear C5 olefins and a bottoms product including cyclic C5 olefins are recovered from the catalytic distillation reactor system. Other aspects of the C5 olefin systems and processes, including catalyst configurations and control schemes, are also described. 1. (canceled)2. (canceled)3. (canceled)4. (canceled)5. (canceled)6. (canceled)7. (canceled)8. (canceled)9. (canceled)10. (canceled)11. (canceled)12. (canceled)13. (canceled)14. (canceled)15. (canceled)16. (canceled)17. (canceled)18. (canceled)19. (canceled)20. (canceled)21. (canceled)22. A process for producing C5 olefins from a steam cracker C5 feed , the process comprising:reacting a mixed hydrocarbon stream comprising cyclopentadiene, linear C5 olefins, cyclic C5 olefins, and C6+ hydrocarbons in a dimerization reactor wherein cyclopentadiene is dimerized to form dicyclopentadiene, producing a dimerization reactor effluent;separating the dimerization reactor effluent in a fraetionator to form a first fraction comprising the C6+ hydrocarbons and dicyclopentadiene and a second fraction comprising the linear and cyclic C5 olefins and linear C5 dienes;feeding the second fraction, a saturated hydrocarbon diluent stream, and hydrogen to a catalytic ...

PRODUCING C5 OLEFINS FROM STEAM CRACKER C5 FEEDS

Producing C5 olefins from steam cracker C5 reeds may include reacting a mixed hydrocarbon stream comprising cyclopentadiene, C5 olefins, and C6+ hydrocarbons in a dimerization reactor where cyclopentadiene is dimerized to dicyclopentadiene. The dimerization reactor effluent may be separated into a traction comprising the C6+ hydrocarbons and dicyclopentadiene and a second fraction comprising C5 olefins and C5 dienes. The second fraction, a saturated hydrocarbon diluent stream, and hydrogen may be fed to a catalytic distillation reactor system for concurrently separating linear C5 olefins from saturated hydrocarbon diluent, cyclic C5 olefins, and C5 dienes contained in the second fraction and selectively hydrogenating C5 dienes. An overhead distillate including the linear C5 olefins and a bottoms product including cyclic C5 olefins are recovered from the catalytic distillation reactor system. Other aspects of the C5 olefin systems and processes, including catalyst configurations and control schemes, are also described. 1. (canceled)2. (canceled)3. (canceled)4. (canceled)5. (canceled)6. (canceled)7. (canceled)8. (canceled)9. (canceled)10. (canceled)11. (canceled)12. (canceled)13. (canceled)14. (canceled)15. (canceled)16. (canceled)17. (canceled)18. (canceled)19. (canceled)20. (canceled)21. (canceled)22. (canceled)23. (canceled)24. (canceled)25. (canceled)26. (canceled)27. (canceled)28. (canceled)29. (canceled)3231. The system of claim , further comprising a fractionator configured to concurrently (a) convert cyclopentadiene in a mixed hydrocarbon to dicyclopentadiene and produce a dimerization reactor effluent , and (b) separate the mixed hydrocarbon to form a bottoms fraction including the dicyclopentadiene and an overheads fraction comprising the mixed C5 hydrocarbon feedstock.3331. The system of claim , further comprising:a dimerization reactor for converting cyclopentadiene in a mixed hydrocarbon to dicyclopentadiene and producing a dimerization reactor effluent; ...

High Value Organic-Enhanced Inorganic Fertilizers

The invention is directed to manufacture of fertilizer having commercial levels of nitrogen supplemented with organic substances. The process treats organic matter with acid causing hydrolysis of organic polymers after which the mix is injected with nitrogen. The resultant sterilized and liquefied organic matter is disbursed over recycled material for the production of granules. Because the process allows for the controlled addition of acids and ammonia, desired levels of components can be achieved. The process is scalable, odor controlled and safe thereby allowing for the location of biosolid processing facilities in most any location. Further, the fertilizer of the invention provides a dual nitrogen-release profile when applied to crops. After application to soil, fertilizer of the invention releases an immediate bolus of nitrogen, similar to traditional ammonium sulfate, followed by continued slow release of nitrogen typically over a season.

Method for processing viscous oil or oil products and a plant for their refining.

The invention describes and claims a processing plant and a method for processing viscous oil and oil products. The processing is effectuated with a plant, which comprises a plurality of reaction modules, a plurality of rectifying chambers and pipelines. Each reaction module and each rectifying chamber comprises a tank, a pump, a hydrocavitation generator. Each reaction module comprises a plurality of intermediate reaction stages. Each rectifying chamber comprises a plurality of intermediate rectifying stages. The reaction module and the rectifying chamber are interconnected. Intermediate reaction stages are connected by pipelines, with the last one connected to a rectifying chamber.

Method and System for Performing Gasification of Carbonaceous Feedstock

The gasification of a carbonaceous material includes receiving a volume of feedstock, supplying thermal energy to the volume of feedstock to convert at least a portion of the volume of feedstock to at least one pyrolysis reaction product via at least one pyrolysis reaction, super-heating the at least one pyrolysis reaction product, providing a volume of super-heated steam, mixing the volume of super-heated steam with the super-heated at least one pyrolysis reaction product and converting at least a portion of at least one reformed product to at least one synthesis gas product via at least one water-gas-shift reaction.

PROCESS FOR THE LARGE-SCALE MANUFACTURE OF ZEOLITE-TEMPLATED CARBON

A method for the large-scale synthesis of a zeolite-templated carbon (ZTC). The method includes the steps of: introducing a bed material comprising a zeolite to a fluidized bed reactor and heating the bed material to a temperature between 550° C. and 800° C.; fluidizing the bed material with a fluidizing gas and maintaining the temperature of the bed material between 550° C. and 800° C.; introducing an organic carbon precursor while fluidizing the zeolite for a period of time such that carbon is deposited on the zeolite by chemical vapor deposition to produce a zeolite-carbon composite; and treating the zeolite-carbon composite with an acid solution such that the zeolite template is dissolved and the ZTC is obtained. 1. A method for large-scale synthesis of a zeolite-templated carbon (ZTC) , the method comprising the steps of:introducing a bed material comprising a zeolite to a fluidized bed reactor and heating the bed material to a first temperature between 550 degrees Celsius (° C.) and 800° C.;fluidizing the bed material with a fluidizing gas and maintaining the temperature of the bed material between 550° C. and 800° C.;introducing an organic carbon precursor while fluidizing the zeolite for a first period of time such that carbon is deposited on the zeolite by chemical vapor deposition to produce a zeolite-carbon composite;treating the zeolite-carbon composite with an acid solution such that the zeolite is dissolved and the ZTC is obtained.2. The method of claim 1 , wherein at least 100 grams of the ZTC is obtained.3. The method of claim 1 , wherein the fluidizing gas has an average gas velocity in the fluidized bed reactor that is between 5 centimeters per second (cm/s) and 25 cm/s.4. The method of claim 1 , wherein the step of fluidizing the bed material further comprises introducing the fluidizing gas such that the bed material is fluidized in a bubbling fluidization regime.5. The method of claim 1 , wherein the zeolite is a bead-type zeolite having a ...

Flashline heater system and method

The present embodiments provide a system and method for separation within a polymer production process. Specifically, a flashline heater configured according to present embodiments may provide more time than is required for complete vaporization of liquid hydrocarbons that are not entrained within a polymer fluff produced within a polymerization reactor. Such extra time may allow for liquid hydrocarbons that are entrained within the polymer fluff to be vaporized.

Method and Device for Lightening Heavy Oil by Utilizing A Suspension-Bed Hydrogenation Process

A method and device for lightening heavy oil by utilizing a suspension-bed hydrogenation process are provided. In the process, a part of a raw oil is mixed with a suspension-bed hydrocracking catalyst to form a first mixture, then the first mixture is subjected to first shear and second shear in sequence so as to realize high dispersion and mixing of the catalyst and the raw oil; through pretreatment of the raw oil, the device can prevent the raw oil from coking in the hydrogenation process; through the adoption of a suspension-bed reactor with a liquid phase self-circulation function or a cold-wall function; and light and heavy components are separated from the suspension-bed hydrogenated product in advance and only medium component is subjected to fixed-bed hydrogenation, thereby reducing the load of the fixed-bed hydrogenation, prolonging the service life of the fixed-bed catalyst, improving the yield and quality of gasoline and diesel, and being beneficial for energy conservation and emission reduction of the whole system.

Dual riser fluid bed process and reactor

Processes and systems for cracking feeds to produce olefins are provided. The process for cracking feeds can include converting a first feed containing at least about 50 wt % methanol in a first riser under a first set of process conditions to produce a first effluent enriched in ethylene, propylene, or a mixture thereof, wherein the first effluent contains at least about 25 wt % dry basis propylene and converting a second feed containing C 4 -C 10 light hydrocarbons in a second riser under a second set of process conditions to produce a second effluent enriched in ethylene, propylene, or a mixture thereof. The process can also include combining the first effluent with the second effluent to produce a mixed effluent, separating the mixed effluent to produce a coked-catalyst and a gaseous product, regenerating the coked-catalyst, and recycling the regenerated catalyst to the first and second risers.

CONVERSION OF HEAVY FUEL OIL TO CHEMICALS

Processes and systems for converting high sulfur fuel oils to petrochemicals including hydrocracking the high sulfur fuel oil in a fuel oil hydrocracker to form a cracked fuel oil effluent, which may be separated into a light fraction and a heavy fraction. The heavy fraction may be gasified to produce a syngas, and the syngas or hydrogen recovered from the syngas may be fed to the fuel oil hydrocracker. The light fraction may be hydrocracked in a distillate hydrocracker to form a cracked effluent, which may be separated into a hydrogen fraction, a light hydrocarbon fraction, a light naphtha fraction, and a heavy naphtha fraction. The heavy naphtha fraction may be reformed to produce hydrogen and at least one of benzene, toluene, and xylenes. The light hydrocarbon fraction and/or the light naphtha fraction may be steam cracked to produce at least one of ethylene, propylene, benzene, toluene, and xylenes. 1. A process for converting high sulfur fuel oils to petrochemicals , the process comprising:hydrocracking a high sulfur fuel oil in an ebullated bed or slurry bed fuel oil hydrocracker to form a cracked fuel oil effluent;separating the cracked fuel oil effluent into a light fraction and a heavy fraction;hydrocracking the light fraction in a distillate hydrocracker to form a cracked effluent;separating the cracked effluent into a hydrogen fraction, a light hydrocarbon fraction, a light naphtha fraction, and a heavy naphtha fraction;reforming the heavy naphtha fraction to produce a reformer effluent comprising hydrogen and at least one of benzene, toluene, and xylenes;steam cracking the light hydrocarbon fraction and/or the light naphtha fraction to produce a steam cracker effluent comprising at least one of ethylene, propylene, benzene, toluene, and xylenes.2. The process of claim 1 , further comprising:gasifying the heavy fraction to produce a syngas comprising carbon monoxide and hydrogen; andfeeding the syngas or hydrogen recovered from the syngas to the fuel oil ...

Integrated process and methods of producing (e) 1-chloro-3,3,3-trifluoropropene

The present invention relates to methods, process, and integrated systems for economically producing (E)-1-chloro-3,3,3-trifluoropropene via vapor phase and/or liquid processes.

Synthesis of Methyl Carbamate and Dimethyl Carbonate (DMC) in Presence of Stripping with Inert Gas or Superheated Vapours and a Reactor for the Same

The invention relates to synthesis of methyl carbamate (MC) and dimethyl carbonate (DMC) in presence of stripping inert gas or superheated methanol vapors using packed column reactor and bubble column reactor. 1. A horizontal sectionalized bubble column reactor for synthesis of methyl carbamate and dimethyl carbonate (DMC) comprising:a. a cylindrical bubble column reactor with single or multiple compartments to receive liquid reactant feed comprising of urea and methanol or methyl carbamate and methanol through inlet ports for a reaction to occur;b. a gas distributor chamber located within the cylindrical bubble column reactor comprising a plate intersecting a cylinder of the cylindrical bubble column reactor with or without an angle to an axis of the cylinder;c. single or multiple inlet ports fitted to the gas distributor chamber for distributing gas;d. single or multiple inlet ports fitted with a constant pressure regulator, single or multiple gas/vapor outlet ports fitted with a back pressure regulator for gaseous phase, wherein, a pressure difference of 10 psi is maintained to ensure positive flow of inert gas into the cylindrical bubble column reactor;e. single or multiple liquid outlet ports with an in-line filter fitted to the cylindrical bubble column reactor for liquid phase withdrawal;f. a heat transfer device fitted to the cylindrical bubble column reactor for maintaining temperature of the reaction;g. a condenser and a gas-liquid separator fitted to the outlet port(s) wherein a product in vapor form is condensed and separated from liquid components;h. an outlet for condensate and an outlet for non-condensate connected to the gas-liquid separator.2. The horizontal sectionalized bubble column reactor as claimed in claim 1 , wherein the cylindrical bubble column reactor further comprises an expanded slurry bed of solid catalyst particles suspended in a suspension liquid or in a packed bed of solid catalyst.3. The horizontal sectionalized bubble column ...

OXIDATIVE COUPLING OF METHANE IMPLEMENTATIONS FOR OLEFIN PRODUCTION

The present disclosure provides oxidative coupling of methane (OCM) systems for small scale and world scale production of olefins. An OCM system may comprise an OCM subsystem that generates a product stream comprising C compounds and non-C impurities from methane and an oxidizing agent. At least one separations subsystem downstream of, and fluidically coupled to, the OCM subsystem can be used to separate the non-C impurities from the C compounds. A methanation subsystem downstream and fluidically coupled to the OCM subsystem can be used to react Hwith CO and/or COin the non-C impurities to generate methane, which can be recycled to the OCM subsystem. The OCM system can be integrated in a non-OCM system, such as a natural gas liquids system or an existing ethylene cracker. 123.-. (canceled)24. A method for producing hydrocarbon compounds including two or more carbon atoms (C compounds) , the method comprising:{'sub': 2', '2', '2+', '4, '(a) performing an oxidative coupling of methane (OCM) reaction in an OCM reactor to produce an OCM effluent stream comprising carbon dioxide (CO), hydrogen (H), one or more C compounds, and methane (CH);'}{'sub': 2+', '2', '2', '4, '(b) separating the OCM effluent stream into a first stream comprising at least some of the one or more C compounds and a second stream comprising carbon monoxide (CO), CO, H, and CH;'}(c) directing a first portion of the second stream and an air stream to a gas compressor, and burning the first portion of the second stream to compress the air stream to produce a compressed air stream;{'sub': 2', '2, '(d) separating the compressed air stream in an air separation unit (ASU) into a third stream comprising Oand a fourth stream comprising N; and'}(e) feeding the third stream to the OCM reactor.25. The method according to claim 24 , further comprising:{'sub': 4', '2', '2, 'methanating a second portion of the second stream to produce a methanated stream comprising CHformed from the Hand CO and/or COin the second ...

High Value Organic-Enhanced Inorganic Fertilizers

The invention is directed to manufacture of fertilizer having commercial levels of nitrogen supplemented with organic substances. The process treats organic matter with acid causing hydrolysis of organic polymers after which the mix is injected with nitrogen. The resultant sterilized and liquefied organic matter is disbursed over recycled material for the production of granules. Because the process allows for the controlled addition of acids and ammonia, desired levels of components can be achieved. The process is scalable, odor controlled and safe thereby allowing for the location of biosolid processing facilities in most any location. Further, the fertilizer of the invention provides a dual nitrogen-release profile when applied to crops. After application to soil, fertilizer of the invention releases an immediate bolus of nitrogen, similar to traditional ammonium sulfate, followed by continued slow release of nitrogen typically over a season. 1. A system for the manufacture of a fertilizer comprising:a mixer configured to blend organic material with an odor control agent forming blended organic material;a first reaction or pressure vessel containing one or more inlets configured for the blended organic material and an acid, wherein the blended organic material is mixed with the acid and heated to a first predetermined temperature and pressurized to a first predetermined pressure for a period of time forming a liquid;a second reaction or pressure vessel containing one or more inlets configured for the liquid and an ammonia source, wherein the liquid is mixed with ammonia from the ammonia source and heated to a second predetermined temperature and pressurized to a second predetermined pressure for a second period of time; anda granulator wherein the ammoniated liquid is mixed with preformed granules and heated to form dried granules of the fertilizer.2. The system of claim 1 , wherein the ammonia source is liquefied or gaseous ammonia under pressure.3. The system of ...

Systems and methods for the manufacture of high melting hydrocarbons from coal

A method and apparatus are provided for processing hydrocarbon coal slurry feeds. The method and apparatus enhance the conversion of the coal feeds into useful conversion products, such as high melting and high carbon containing pitch products. In particular, the present techniques utilize a specially designed “self-cleaning” and “wall-catalyzed” preheater-reactor systems.

PROCESSING BIOMASS

Biomass (e.g., plant biomass, animal biomass, and municipal waste biomass) is processed to produce useful products, such as fuels. For example, systems can use feedstock materials, such as cellulosic and/or lignocellulosic materials and/or starchy or sugary materials, to produce ethanol and/or butanol, e.g., by fermentation. 1. A method of converting an intermediate to a product , the method comprising treating an irradiated intermediate product with a microorganism , the intermediate having been prepared by irradiating a starchy material and treating the starchy material with an enzyme.2. The method of wherein the product comprises a combustible fuel.3. The method of wherein the starchy material is selected from the group consisting of corn starch claim 1 , wheat starch claim 1 , potato starch claim 1 , rice starch claim 1 , derivatives thereof claim 1 , and mixtures thereof.4. The method of claim 3 , wherein the starchy material consists essentially of corn starch.5. The method of wherein the starchy material is selected from the group consisting of arracacha claim 1 , buckwheat claim 1 , banana claim 1 , rice claim 1 , arrowroot claim 1 , barley claim 1 , cassava claim 1 , kudzu claim 1 , oca claim 1 , sago claim 1 , sorghum claim 1 , potatoes claim 1 , sweet potato claim 1 , taro claim 1 , yams claim 1 , beans claim 1 , lentils claim 1 , peas and mixtures thereof.6. The method of wherein the starchy material comprises corn.7. The method of claim 1 , wherein when irradiating the starchy material claim 1 , the radiation is applied at a total dosage of between about 10 MRad and about 50 MRad.8. The method of claim 1 , wherein treating the intermediate product with the microorganism comprises fermentation.9. The method of claim 1 , wherein the intermediate product comprises one or more sugars selected from the group consisting of cellobiose claim 1 , lactose claim 1 , sucrose claim 1 , glucose and xylose.10. The method of claim 1 , wherein irradiating is performed ...

PRODUCING C5 OLEFINS FROM STEAM CRACKER C5 FEEDS

Producing C5 olefins from steam cracker C5 feeds may include reacting a mixed hydrocarbon stream comprising cyclopentadiene, C5 olefins, and C6+ hydrocarbons in a dimerization reactor where cyclopentadiene is dimerized to dicyclopentadiene. The dimerization reactor effluent may be separated into a fraction comprising the C6+ hydrocarbons and dicyclopentadiene and a second fraction comprising C5 olefins and C5 dienes. The second fraction, a saturated hydrocarbon diluent stream, and hydrogen may be fed to a catalytic distillation reactor system for concurrently separating linear C5 olefins from saturated hydrocarbon diluent, cyclic C5 olefins, and C5 dienes contained in the second fraction and selectively hydrogenating C5 dienes. An overhead distillate including the linear C5 olefins and a bottoms product including cyclic C5 olefins are recovered from the catalytic distillation reactor system. Other aspects of the C5 olefin systems and processes, including catalyst configurations and control schemes, are also described. 1. (canceled)2. (canceled)3. (canceled)4. (canceled)5. (canceled)6. (canceled)7. (canceled)8. (canceled)9. (canceled)10. (canceled)11. (canceled)12. (canceled)13. (canceled)14. (canceled)15. (canceled)16. (canceled)17. (canceled)18. (canceled)19. (canceled)20. (canceled)21. (canceled)22. (canceled)23. (canceled)24. (canceled)25. (canceled)26. (canceled)27. A process for producing C5 olefins from a mixed C5 feed , the process comprising:feeding hydrogen and a mixed hydrocarbon stream comprising cyclopentadiene, linear C5 olefins, cyclic C5 olefins, and C6+ hydrocarbons to a catalytic distillation reactor system; [{'sub': '+', 'separating the linear C5 olefins from the cyclic C5 olefins, C5 dienes, and C6 hydrocarbons; and'}, 'selectively hydrogenating at least a portion of the C5 dienes to form additional linear C5 olefins;, 'concurrently in the catalytic distillation reactor systemwithdrawing a liquid side draw from a stage below a mixed hydrocarbon ...

PROCESS AND APPARATUS FOR HEAT RECOVERY IN VINYL CHLORIDE MONOMER PLANTS OR IN INTEGRATED VINYL CHLORIDE MONOMER OR POLYVINYL CHLORIDE PLANTS

Disclosed is a process and apparatus for heat recovery in vinyl chloride monomer manufacturing plants or in integrated vinyl chloride monomer/polyvinyl chloride manufacturing plants. A process for capture and use of excess heat recovered in the production of vinyl chloride includes distillatively purifying DCE in a high-boilers column, using a heat exchanger to capture thermal energy from a purified DCE vapor stream from the high-boilers column, generating low pressure steam from the captured thermal energy, returning condensed DCE vapors to the high-boilers column, and heating parts of the plant with the generated low pressure steam. 112.-. (canceled)13. A process for the capture and use of excess heat recovered during the production of vinyl chloride by the thermal cleavage of 1 ,2-dichloroethane in a vinyl chloride manufacturing complex that incorporates distillative purification of 1 ,2-dichloroethane using at least one high-boilers column in which substances boiling at temperatures higher than the boiling point of 1 ,2-dichloroethane are removed , the process comprising:distillatively purifying 1,2-dichloroethane by boiling 1,2-dichloroethane at temperatures between 120-150° C. in a high-boilers column of the vinyl chloride manufacturing complex to create a 1,2-dichloroethane vapor stream;capturing thermal energy from at least a portion of a distillatively purified 1,2-dichloroethane vapor stream, by at least one heat exchanger associated with at least one of a plant component dedicated to producing 1,2-dichloroethane, a downstream plant component dedicated to producing vinyl chloride, or a downstream plant component dedicated to producing polyvinyl chloride;generating low-pressure steam from the thermal energy captured by the heat exchanger;returning the 1,2-dichloroethane vapor into the high-boilers column following a condensation thereof; andheating selected parts of the plant with the generated low pressure steam.14. The process of claim 13 , wherein the at ...

Apparatus and Process for the Hydroconversion of Heavy Oil Products

The present invention relates to an apparatus for the hydroconversion of heavy oil products (the fresh load). Said apparatus comprises: a slurry bubble column hydroconversion reactor, which comprises a feed line in which the fresh load and the recirculated slurry phase are conveyed, an inlet line for a hydrogenating stream and an outlet for a reaction effluent through an outlet nozzle; a stripping column at high pressure and high temperature placed downstream of the reactor and directly connected to the reactor head through a pipeline in which the reaction effluent flows; said column having an inlet line for a stripping gas, an inlet for the reactor effluent, a head outlet for steam and an outlet for the slurry phase; lines and means for recirculating the slurry leaving the stripping column; lines and means for taking a drain stream, which has the function of preventing the accumulation of solids in the reactor. The stripping column is characterized in that it contains one or more contact devices that allow physical contact to be created between different phases. 1. Apparatus for the hydroconversion of heavy oil products which constitute the fresh load , said apparatus comprising:a slurry bubble column hydroconversion reactor, which comprises a feed line in which the fresh load and the recirculated slurry phase are conveyed, an inlet line for a hydrogenating stream and an outlet for a reaction effluent through an outlet nozzle;a high pressure and high temperature stripping column placed downstream of the reactor and directly connected to the reactor head through a pipeline in which the reaction effluent flows; said column having an inlet line for a stripping gas, an inlet for the reactor effluent, a head outlet for steam and an outlet for the slurry phase;lines and means for recirculating the slurry leaving the stripping column;lines and means for taking a drain stream, which has the function of preventing the accumulation of solids in the reactor;said stripping ...

REACTOR SYSTEM

A reactor tank is provided having an enzyme inlet, a heating jacket positioned around the exterior center of the tank, a gas outlet for communicating with a vacuum apparatus to create a vacuum within the reactor tank and for communicating with a condensing unit, a first gas inlet for receiving gas from a feed tank and a first liquid outlet for recirculating the liquid from the first liquid outlet back to the feed tank. The reactor tank further includes a sparged unit and a screen positioned within the tank between the sparged unit and the first liquid outlet, where the sparged unit is connected to the first gas inlet for receiving gas from the feed tank. The reactor tank is utilized in a reactor system further including a condensing unit, vacuum pump or venturi valve, a first feed tank connected to the first gas inlet, a coalescer having at least one circulation pipe and a first circulation pump connected to the first liquid outlet for circulating a portion of the liquid dispelled from the liquid outlet to the coalescer, which after being filtered through coalescer is recirculated through circulation pipe back to the first feed tank. 1. A reactor comprising:a tank having a catalyst inlet;a heating jacket positioned around the exterior center of the tank;a gas outlet for communicating with a contact condenser unit for the continuous removed of water from the tank during use;a first gas inlet for receiving gas from a feed tank;a first liquid outlet for recirculating the liquid from the first liquid outlet back to the feed tank;a sparged unit positioned within the tank and in communication with the first gas inlet to sparge the gas received through the first gas inlet; anda screen positioned within the tank between the sparged unit and the first liquid outlet.2. The reactor of further includes a second gas outlet on the second end of the vessel to vent air from the reactor.3. The reactor of further including an agitator mount.4. The reactor of further including a raw ...

Metallocene Catalyst Feed System for Solution Polymerization Process

Methods and systems for solution polymerization. The method can include forming a first mixture stream consisting essentially of at least one catalyst and a process solvent, and forming a second mixture stream consisting essentially of at least one activator and the process solvent. The first mixture stream and the second mixture stream can be fed separately to at least one reaction zone comprising one or more monomers dissolved in the process solvent where the at least one monomers can be polymerized within the at least one reaction zone in the presence of the catalyst, activator and process solvent to produce a polymer product.

METHOD AND SYSTEM FOR PRODUCING A SYNTHESIS GAS IN AN OXYGEN TRANSPORT MEMBRANE BASED REFORMING SYSTEM USING A COMBINED FEED STREAM

A method and system for producing a synthesis gas in an oxygen transport membrane based reforming system that utilizes a combined feed stream having a steam to carbon ratio between about 1.6 and 3.0 and a temperature between about 500° C. and 750° C. The combined feed stream is comprised a pre-reformed hydrocarbon feed, superheated steam, and a reaction product stream created by the reaction of a hydrogen containing stream reacted with the permeated oxygen at the permeate side of the oxygen transport membrane elements. 1. A method for producing a synthesis gas in an oxygen transport membrane based reforming system , wherein said system comprises two distinct reactors: i.) at least one catalyst containing reforming reactor configured to produce a synthesis gas stream by reacting a combined feed stream in the presence of the catalyst and heat; andii.) a reactively driven oxygen transport membrane reactor proximate the at least one catalyst containing reforming reactor, the reactively driven oxygen transport membrane reactor comprising a plurality of oxygen transport membrane elements configured to separate oxygen from an oxygen containing feed stream and produce an oxygen permeate at a permeate side of the oxygen transport membrane elements and an oxygen depleted retentate stream at a retentate side of the oxygen transport membrane elements, the method comprising the steps of:separating an oxygen containing stream into an oxygen permeate and an oxygen depleted retentate stream using a plurality of oxygen transport membrane elements disposed in the oxygen transport membrane based reforming system;reacting a hydrogen containing stream fed to a permeate side of the oxygen transport membrane elements with the oxygen permeate to generate a reaction product stream and heat;transferring the heat via convection to the oxygen depleted retentate stream and via radiation to at least one catalyst containing reforming reactor configured to produce a synthesis gas stream;pre- ...

Rapid Depressurization of a Reactor System

Systems and processes for rapidly depressurizing a reactor system are disclosed. The systems and processes are particularly useful in the high pressure polymerization of ethylene. 1. A reactor system comprising:a. a compressor in fluid connection with a reactor, the reactor comprising at least one reaction zone and at least one cooling zone;b. a first pressure relief valve located downstream of the reactor; andc. a second pressure relief valve located along the reactor in the cooling zone.2. A reactor system comprising:{'sup': '3', 'd. a compressor in fluid connection with a reactor, the reactor comprising at least one reaction zone and at least one cooling zone, wherein the total inner volume of the reactor is less than about 6 m; and'}e. a first pressure relief valve located downstream of the reactor.3. The system of claim 1 , wherein the reactor comprises at least three cooling zones claim 1 , and a second pressure relief valve is located along the reactor in cooling zone three or a cooling zone further downstream.4. The system of claim 1 , wherein the reactor comprises at least four cooling zones claim 1 , and a second pressure relief valve is located along the reactor in cooling zone four or a cooling zone further downstream.5. The system of claim 1 , further comprising a preheater upstream of the reactor claim 1 , wherein the system does not have a pressure relief valve upstream of the preheater or between the preheater and the reactor.6. The system of claim 1 , further comprising a preheater upstream of the reactor claim 1 , wherein the system is capable of reducing the operating pressure at the inlet of the preheater from above about 2000 bar to below about 1000 bar in less than 10 seconds.7. The system of claim 1 , wherein the reactor further comprises at least one rupture disk.8. The system of claim 1 , further comprising a stagnant zone within the reactor during a pressure dump event claim 1 , wherein the stagnant zone is located entirely within a cooling ...

Gasoline production device

Provided is a gasoline production device capable of effectively using heat of reaction generated in the synthesis of gasoline and also capable of readily cooling heat generated by synthesizing gasoline. A device 30 for producing gasoline from methanol includes a plurality of reaction tubes 34 configured to synthesize gasoline from methanol and a duct 36 configured to allow air to flow outside the reaction tubes, and heat exchange is carried out between synthesis heat generated within the reaction tubes 34 and the air which flows through the duct 36.

Efficient oxidative coupling of methane processes and systems

The present disclosure provides oxidative coupling of methane (OCM) systems for small scale and world scale production of olefins. An OCM system may comprise an OCM subsystem that generates a product stream comprising C 2+ compounds and non-C 2+ impurities from methane and an oxidizing agent. At least one separations subsystem downstream of, and fluidically coupled to, the OCM subsystem can be used to separate the non-C 2+ impurities from the C 2+ compounds. A methanation subsystem downstream and fluidically coupled to the OCM subsystem can be used to react H 2 with CO and/or CO 2 in the non-C 2+ impurities to generate methane, which can be recycled to the OCM subsystem. The OCM system can be integrated in a non-OCM system, such as a natural gas liquids system or an existing ethylene cracker.

Method and Device for Treating Solid-Fluid Mixtures

A laminar stream reactor for the production of hydrochar of a solid-fluid mixture of water and a carbon-containing component, wherein the solid-fluid mixture is treated at a temperature of 100-300 degree ° C. and a pressure of 5-70 bar, consists of tubular reactor units of largely vertical holding sections () and direction-changing diverters (). The holding sections are thereby flown through slower by the solid-fluid mixture than the remaining tube distances, as they have larger diameters. 1. Method for the production of hydrochar of a solid-fluid mixture of water and a carbon-containing component , wherein the solid-fluid mixture is treated at a temperature of 100-300° C. and a pressure of 5-70 bar in a laminar stream reactor with at least two holding sections and at least one diverter arranged below it , and whereina. the average flow velocity of the solid-fluid mixture in the lower diverter is 10-500 or 20-200 m/min than in the holding sections,b. the average flow direction of the solid-fluid mixture in the holding section is inclined to the horizontal from the vertical andc. a total residence time in the pressurized heat exchangers and reactor is more than 2 hours.2. Method according to claim 1 , wherein the average flow velocity in the lower diverter is 1-1 claim 1 ,000 m/min and/or 1.5-1000 claim 1 , 5-300 or 20-100 times larger than in the holding section.3. Method according to or claim 1 , wherein the sold-fluid mixture flows through an upwardly-directed holding section and thereafter an upper diverter after the lower diverter claim 1 , wherein in particular the average flow velocity in the lower diverter is 1.1-2 claim 1 , 2-5 or 4-40 times faster than in the upper diverter and/or the flow velocity in an ascender directly following the lower diverter is 1.1-40 or 2-5 times faster than in the descender directly preceding the lower diverter.4. Method according to one of to claim 1 , wherein the average flow velocity in the descending holding section is 0.01- ...

Reformer with perovskite as structural component thereof

A reformer includes at least one reformer reactor unit ( 300 ) having a space-confining wall with external ( 307 ) and internal surfaces ( 306 ), at least a section of the wall and space confined thereby defining a reforming reaction zone ( 311 ), an inlet end ( 301 ) and associated inlet ( 302 ) for admission of flow of gaseous reforming reactant to the reforming reaction zone ( 311 ), an outlet end ( 303 ) and associated outlet ( 304 ) for outflow of hydrogen-rich reformate produced in the reforming reaction zone ( 311 ), at least that section of the wall ( 305 ) corresponding to the reforming reaction zone comprising perovskite as a structural component thereof such wall section being gas-permeable to allow gaseous reforming reactant to diffuse therein and hydrogen-rich reformate to diffuse therefrom.

Process and apparatus for preparation of a crystallizable polylactic acid mixture, and polylactic acid mixture

In a practicable continuous or batchwise process for the preparation of a crystallizable polylactic acid mixture, lactic acid may be polycondensed to yield an oligomer, which may then be depolymerized to yield a crude lactide. The crude lactide may be purified to yield a pure lactide, wherein fractionation may be carried out in the purification into an L- or D-lactide-rich fraction and also a meso-lactide-rich fraction. Subsequently a separate ring-opening polymerization of the resulting lactide fractions can be carried out. The individual polylactic acid batches or streams generated by the ring-opening polymerization may then be mixed. The present disclosure further relates to apparatuses for carrying out such processes and polylactic acid mixtures.

CONTINUOUS PROCESS FOR MAKING POLYBUTYLENE TEREPHTHALATE USING PURIFIED TEREPHTHALIC ACID AND 1,4-BUTANE DIOL

Disclosed is a continuous process and device for making polybutylene terephthalate (PBT) resin, particularly high molecular weight PBT resin. Also disclosed are a device for conducting the process, and a monitoring process for determining the carboxylic acid end group concentration of the resulting PBT. 1(a) combining 1,4-butane diol (BDO) and purified terephthalic acid (PTA) in a slurry paste vessel to form a mixture; (b1) the mixture from step (a) is subjected to the esterification section with a treatment temperature in the range of 170 to 270° C. and a treatment pressure in the range of 0.5 to 1 bar; a first quantity of catalyst is supplied;', '(b2) the product of step (b1) is transferred continuously into a pipe stretch while optionally a quantity of BDO is supplied;', '(b3) the product of step (b2) is transferred continuously to a cascade postesterification part of the tower reactor, comprising multiple cascades in series, preferably four cascades in series, wherein the pressure of each cascade is subsequently reduced to ultimately ≤1.25 bar, preferably 0.20 bar and optionally a second quantity of catalyst is supplied into the last cascade zone of the post-esterification part of the tower reactor;, '(b) continuously supplying the mixture from step (a) to a tower reactor having a plurality of reactor zones for at least one of esterification or transesterification; wherein the following conditions are maintained(c) the product obtained from step (b3) is continuously supplied to a first continuously stirred tank reactor, wherein the product of step (b3) is subjected to a melt temperature of 225 to 250° C., a pressure of 5 to 40 mbar, and a residence time between 10 and 60 minutes;(d) optionally, the product obtained from step (c) is continuously supplied to a second continuously stirred tank reactor, wherein the product of step (c) is subjected to a melt temperature of 230 to 260° C., a pressure of 0.1 to 35 mbar, and a residence time between 10 and 60 minutes; ...

Integrated Chilling of Process Air Compression in Ammonia Plants Utilizing Direct and Indirect Chilling from the Ammonia Compression Train of the Plant Followed by Air Flow Split and Multistage Air Preheating to the Secondary Ammonia Reformer

An improved performance ammonia plant system utilizing both a direct and indirect chilling of the compressed process air train using a single or multistage chilling system integrated with the ammonia plant ammonia compression train to increase process air flow to the secondary ammonia reformer of the ammonia plant. 1. A method for improving the performance of an ammonia plant utilizing a direct integrated chilling system in an ammonia plant air compression train to increase process air flow to a secondary reformer of the ammonia plant , the method comprising:providing a single integrated suction air chiller in the ammonia plant air compression train for chilling incoming air by heat exchange with compressed liquid ammonia;supplying the compressed liquid ammonia from the ammonia plant ammonia compression train to the single integrated suction air chiller;expanding the compressed liquid ammonia to an expanded ammonia vapor in the single integrated suction air chiller to provide chilling of the air; andreturning all of the expanded ammonia vapor to the ammonia plant compression train to be integrated for recompression and cooling back to liquid ammonia.2. The method of claim 1 , wherein providing the single integrated suction air chiller in the air compression train provides a single integrated suction air chiller in which all of the ammonia flows through and is expanded to the expanded ammonia vapor in only one section in the single integrated suction air chiller claim 1 , and wherein returning all of the expanded ammonia vapor to the ammonia plant compression train returns all of the expanded ammonia vapor to a single medium pressure stage of the ammonia compression train.3. The method of claim 1 , wherein providing the single integrated suction air chiller in the air compression train provides a single integrated suction air chiller in which the entering liquid ammonia is separated and flows through two separate sections of the single integrated suction air chiller ...

Process and Apparatus for Continuous Solution Polymerization

Provided are processes and apparatuses for continuous solution polymerization which can mitigate fouling during the production of propylene-based polymers.

Treatment of Heavy Crude Oil and Diluent

An integrated process simultaneously removes the diluent and reduces the TAN, resulting in cost savings from the diluent recovery and increasing the value of the produced heavy crude stream by removing the acids and other contaminants, while reducing the overall energy requirements when compared to performing the two processes separately. 1. An apparatus comprising:one or more heaters to heat a blend of bituminous crude oil and diluent to degradation of naphthenic acids in the crude oil;one or more reactors to provide sufficient residence time at elevated temperatures for the decomposition reactions to reduce the acid concentrations to reduce total acid number by at least 75% and to simultaneously remove the diluent; anda distillation column to remove diluent by distillation.2. The apparatus of including: ["each reactor's vapor flow is individually controlled to maintain a constant rate over the required residence time; and", 'both liquid and vapor flow concurrently upwards in the reactor so that as more degradation products are formed, vapor flow is also increasing, while vapor and liquid are separated at the top of each reactor; and, 'multiple reactors, arranged such thatheaters between the reactors to compensate for the heat required for the vaporization of the light hydrocarbons.3. The apparatus of including a vertical concurrent upward flow path for both the bituminous oil blend and the evaporated diluents and a flow path for hydrocarbon vapor stream through the liquid to remove decomposition products and drive the reaction to completion.4. The apparatus of including a condenser to recover the light hydrocarbons from the vented vapors by cooling and condensing said vapors while venting the non-condensable contaminants and residual hydrocarbon vapors to a vapor destruction device.5. The apparatus of including said distillation column to recover from said light hydrocarbons the fractions in the distillate boiling range claim 1 , that were stripped with the ...

UREA SYNTHESIS REACTOR AND PROCESS

A urea synthesis reactor is provided that comprises a casing extending along an axis and a first and a second inlet tube inserted through respective through openings of the casing and respectively connected, inside the casing, to a light phase distributor and to a heavy phase distributor configured to feed the reactor with a light phase containing carbon dioxide and a heavy phase containing ammonia, respectively; the light phase distributor comprises one or more tubular elements extending and/or distributed over the cross-section of the reactor and about the axis and provided with intake holes spaced apart from one another, so as to distribute said light phase in a plurality of intake points distributed transversely in the reactor and about the axis. 117-. (canceled)18. A urea synthesis reactor comprising:a casing extending along an axis and having a main portion closed at opposite axial ends by two end caps; anda first inlet tube inserted through a first opening defined by the casing and connected, inside the casing, to a light phase distributor including at least one tubular element extending, about the axis, into a cross-section of the casing, said at least one tubular element defining a plurality of spaced apart intake holes, the light phase distributor being configured to distribute a light phase containing carbon dioxide to a plurality of intake points distributed transversely in the casing about the axis, said first opening being formed through a side wall of the main portion of the casing above a peripheral edge joining said main portion with a dome-shaped bottom portion of the casing; anda second inlet tube inserted through a second opening defined by the casing and connected, inside the casing, to a heavy phase distributor configured to distribute a heavy phase containing ammonia, said second opening being formed through the side wall of the main portion of the casing above the peripheral edge joining said main portion with the dome-shaped bottom portion ...

Integrated process and plant for production of urea and uas (urea-ammonium sulphate) mixtures

An integrated process for production of urea and urea-ammonium sulphate (“UAS”) comprises: a urea synthesis step carried out in a urea synthesis reactor; a recovery and concentration step, wherein a urea solution produced in the urea synthesis step is progressively concentrated in at least one recovery section and in a concentration section, recovering unreacted ammonia and carbon dioxide and water from said urea solution; a step of producing ammonium sulphate by reaction of sulphuric acid and ammonia in an ammonium sulphate production apparatus; a step of mixing said ammonium sulphate with concentrated urea coming from the concentration section to produce a UAS mixture; in the ammonium sulphate production step, at least a part of the ammonia is provided by at least one off-gas containing ammonia and recovered from the recovery and concentration step.

PROCESS AND APPARATUS FOR THE PRODUCTION OF SYNTHESIS GAS

Reactive diluent fluid () is introduced into a stream of synthesis gas (or “syngas”) produced in a heat-generating unit such as a partial oxidation (“POX”) reactor () to cool the syngas and form a mixture of cooled syngas and reactive diluent fluid. Carbon dioxide and/or carbon components and/or hydrogen in the mixture of cooled syngas and reactive diluent fluid is reacted () with at least a portion of the reactive diluent fluid in the mixture to produce carbon monoxide-enriched and/or solid carbon depleted syngas which is fed into a secondary reformer unit () such as an enhanced heat transfer reformer in a heat exchange reformer process. An advantage of the invention is that problems with the mechanical integrity of the secondary unit arising from the high temperature of the syngas from the heat-generating unit are avoided. 1. A process for the production of syngas comprising carbon monoxide and molecular hydrogen , said process comprising: exothermically reacting hydrocarbon-containing fuel with an oxidant gas comprising molecular oxygen in a first reactor to produce an exothermically-generated syngas product , the exothermically-generated syngas product having a first concentration of carbon monoxide; combining an effluent stream of the exothermically-generated syngas product with reactive diluent fluid with to produce a mixture comprising cooled exothermically-generated syngas product and reactive diluent fluid , the mixture including carbon dioxide , molecular hydrogen and solid carbon particles; reacting the carbon dioxide and the molecular hydrogen in the mixture over a catalyst in a second reactor to produce reacted syngas product having a second concentration of carbon monoxide greater than the first concentration; and gasifying solid carbon particles in the mixture with at least one other component in the mixture to produce reacted syngas product.2. The process of claim 1 , further comprising endothermically reforming hydrocarbon-containing fuel gas with ...

METAL CHLORIDES AND METALS OBTAINED FROM METAL OXIDE CONTAINING MATERIALS

Method and apparatus for preparing at least one metal chloride from metal oxide containing material comprising calcining the metal oxide containing material under temperature conditions sufficient to obtain a calcined product comprising at least one metal oxide; and selectively chlorinating the calcined product to form at least one metal chloride. 120.-. (canceled)21. A method for preparing at least one metal chloride from at least one of coal mine waste and coal fired power plant ash , the at least one of coal mine waste and coal fired power plant ash comprising non-combustible material and combustible material , comprising:(a) introducing particles of the at least one of coal mine waste and coal fired power plant ash into a calciner, combusting the combustible material in the calciner in an oxidizing atmosphere to provide heat content and calcining the non-combustible material under temperature conditions sufficient to cause decomposition to obtain a resulting calcined product comprising metal oxides; and(b) selectively chlorinating the resulting calcined product of (a) in a fluidized bed chlorinator by carbochlorination in the absence of a catalyst, including introducing (i) the resulting calcined product of (a), (ii) a chlorinating agent, and (iii) a reducing agent comprising particles of coal into the fluidized bed chlorinator including an inert gas as a fluidizing media to obtain mixing of the resulting calcined product, the chlorinating agent and the particles of coal after introduction into the fluidized bed chlorinator; the selectively chlorinating including determining a content of metal oxides in the resulting calcined product and using an amount of the chlorinating agent and an amount of coal based upon the determining to thereby form at least one metal chloride from the resulting calcined product without substantial formation of non-metal chloride, the without substantial formation of non-metal chloride including formation of less than about 5 wt. % non ...

SYSTEM AND PROCESS FOR CUMENE HYDROPEROXIDE CLEAVAGE WITH IMPROVED ONLINE INSTRUMENTATION CONFIGURATION

Disclosed herein are a method and systems for cumene hydroperoxide cleavage with an improved configuration for online instrumentation. The systems comprise a first fluid loop comprising one or more reactors and a fluid pump and a second fluid loop in fluid communication with the first fluid loop. This second fluid loop comprises an instrument configured to measure a characteristic of a fluid flowing through the second loop, wherein an input of the second fluid loop is disposed downstream of said fluid pump and an output of the second fluid loop is disposed upstream of said fluid pump. The method comprises causing fluid to flow within a first stage comprising one or more reactors and a fluid pump, wherein the first stage is configured to decompose a cumene hydroperoxide in the presence of a catalyst mixture to form a dicumyl peroxide mixture. The method also comprises causing at least a portion of the fluid to flow through a instrumentation line in open fluid communication with the first stage. This instrumentation line comprises an instrument configured to measure a characteristic of the fluid flowing through the instrumentation line and an input of the instrument line is disposed downstream of said fluid pump. 1. A system comprising:a first fluid loop comprising one or more reactors and a fluid pump configured in fluid communication with each other, wherein the fluid pump is configured to cause an output of the one or more reactors to flow as an input to the one or more reactors; anda second fluid loop in fluid communication with the first fluid loop, the second fluid loop comprising an instrument configured to measure a characteristic of a fluid flowing through the second loop, wherein an input of the second fluid loop is disposed downstream of the fluid pump and an output of the second fluid loop is disposed upstream of the fluid pump.2. The system of claim 1 , wherein the one or more reactors of the first fluid loop comprise tubing claim 1 , a pre-heater claim 1 ...

Synthesis of methyl carbamate and dimethyl carbonate (dmc) in presence of stripping with inert gas or superheated vapours and a reactor for the same

The invention relates to synthesis of methyl carbamate (MC) and dimethyl carabonate (DMC) in presence of stripping inert gas or superheated methanol vapors using packed column reactor and bubble column reactor.

Process for degassing and buffering polyolefin particles obtained by olefin polymerization

Process for preparing a polyolefin polymer comprising the steps of a) forming a particulate polyolefin polymer by polymerizing one or more olefins in the presence of a polymerization catalyst system in a polymerization reactor; b) discharging the formed polyolefin particles from the polymerization reactor; c) degassing the polyolefin particles by a process comprising at least a final step of contacting the polyolefin particles with a nitrogen stream in a degassing vessel; and d) transferring the polyolefin particles from the vessel, in which the contacting of the polyolefin particles with the nitrogen stream is carried out, to a melt mixing device, in which the polyolefin particles are melted, mixed and thereafter pelletized, without passing the particles through a buffering device, wherein the degassing vessel is only partly filled with polyolefin particles and the empty volume within the degassing vessel is sufficient to take up additional polyolefin particles for at least 3 hours if the transfer of polyolefin particles of step d) from the degassing vessel to the melt mixing device is discontinued and the discharge of polyolefin particles from the polymerization reactor according to step b) is continued with unchanged rate.

MACHINE AND METHODS FOR TRANSFORMING BIOMASS AND/OR WASTE PLASTICS VIA SUPERCRITICAL WATER REACTION

The machinery and methods disclosed herein are based on the use of a specialized extruder configured to continuously convey and plasticize/moltenize selected lignocellulosic biomass and/or waste plastic materials into a novel variable volume tubular reactor, wherein the plasticized/moltenized material undergoes reaction with circumferentially injected supercritical water—thereby yielding valuable simple sugar solutions and/or liquid hydrocarbon mixtures (e.g., “neodiesel”), both of which are key chemical commodity products. The reaction time may be adjusted by changing the reactor volume. The machinery includes four zones: (1) a feedstock conveyance and plasticization/moltenization zone; (2) a steam generation and manifold distribution zone; (3) a central supercritical water reaction zone; and (4) a pressure let-down and reaction product separation zone. The machinery and methods minimize water usage—thereby enabling the economic utilization of abundant biomass and waste plastics as viable renewable feedstocks for subsequent conversion into alternative liquid transportation fuels and valuable green-chemical products. 1. A machine for transforming a selected polymeric material into a plurality of reaction products via supercritical water reaction , comprising:an extruder having an inlet and a downstream outlet, wherein the downstream outlet is coincident with the longitudinal axis of the extruder;a steam generator fluidically connected to a downstream inlet manifold, wherein the inlet manifold forms a ring having a plurality of inwardly facing exit portals, wherein the plurality of exit portals is circumferentially positioned about the inner surface of the ring;a tubular reactor having an interior space fluidically connected to an inlet end and an outlet end, wherein the inlet end of the tubular reactor is adjacent and fluidically connected to both (i) the outlet of the extruder, and (ii) the plurality of circumferentially positioned exit portals of the inlet ...

ETHYLENE-TO-LIQUIDS SYSTEMS AND METHODS

Integrated systems are provided for the production of higher hydrocarbon compositions, for example liquid hydrocarbon compositions, from methane using an oxidative coupling of methane system to convert methane to ethylene, followed by conversion of ethylene to selectable higher hydrocarbon products. Integrated systems and processes are provided that process methane through to these higher hydrocarbon products. 1111.-. (canceled)112. A method , comprising:(a) directing an olefin-containing stream comprising an olefin into an ethylene-to-liquids (ETL) reactor comprising an ETL catalyst that facilitates conversion of at least a portion of said olefin to higher hydrocarbon compounds to yield an ETL product stream comprising said higher hydrocarbon compounds;{'sub': 4+', '3, '(b) directing at least a portion of said ETL product stream into a de-propanizer that separates said higher hydrocarbon compounds into a bottom stream comprising hydrocarbon compounds with four or more carbon atoms (C compounds) and an overhead stream comprising hydrocarbon compounds with three carbon atoms (Ccompounds); and'}{'sub': '3', '(c) directing at least a portion of said Ccompounds into said ETL reactor.'}113. The method of claim 112 , wherein said olefin comprises ethylene claim 112 , propylene or a combination thereof.114. The method of claim 112 , further comprising claim 112 , prior to (a) claim 112 , directing a hydrocarbon feedstream comprising feedstream hydrocarbons into a cracking reactor comprising a cracking catalyst that facilitates cracking of said feedstream hydrocarbons to produce a cracked stream comprising cracked hydrocarbons claim 112 , wherein said cracked hydrocarbons have a lower molecular weight than said feedstream hydrocarbons claim 112 , and using at least a subset of said cracked hydrocarbons to generate said olefin-containing stream.115. The method of claim 114 , further comprising directing said cracked stream into a separations unit that separates said cracked ...

LIQUID FUEL CPOX REFORMER AND FUEL CELL SYSTEMS, AND METHODS OF PRODUCING ELECTRICITY

Integrated liquid fuel catalytic partial oxidation (CPOX) reformer and fuel cell systems can include a plurality or an array of spaced-apart CPOX reactor units, each reactor unit including an elongated tube having a gas-permeable wall with internal and external surfaces. The wall encloses an unobstructed gaseous flow passageway. At least a portion of the wall has CPOX catalyst disposed therein and/or comprising its structure. The catalyst-containing wall structure and open gaseous flow passageway enclosed thereby define a gaseous phase CPOX reaction zone, the catalyst-containing wall section being gas-permeable to allow gaseous CPOX reaction mixture to diffuse therein and hydrogen rich product reformate to diffuse therefrom. The liquid fuel CPOX reformer also can include a vaporizer, one or more igniters, and a source of liquid reformable fuel. The hydrogen-rich reformate can be converted to electricity within a fuel cell unit integrated with the CPOX reactor unit. 1. A reformer for the gaseous phase catalytic partial oxidation of a gaseous CPOX reaction mixture of an oxygen-containing gas and a gaseous and/or vaporized liquid CPOX fuel reaction mixture to provide a hydrogen gas product , the reformer comprising:a generally U-shaped open conduit configured to convey a gaseous CPOX reaction mixture of an oxygen-containing gas and a gaseous and/or vaporized liquid CPOX fuel to an inlet of at least one elongate tubular gaseous phase CPOX reactor unit, the reactor unit having a gas permeable wall with an internal surface and an external surface defining a wall thickness therebetween and having at least one CPOX catalyst disposed (i) on at least a portion of an internal surface of the CPOX reactor unit and/or (ii) within the wall thickness thereof, the CPOX-containing portion of the CPOX reactor unit defining a gaseous phase CPOX reaction zone, the CPOX reaction zone adapted to emit a heat of exotherm during a CPOX reaction therein;the U-shaped open conduit comprising a ...

Plant and process for producing fatty alcohol

A plant and a process for carrying out the continuous production of fatty alcohol from fatty acid ester by catalytic trickle-bed hydrogenation, comprising shaft reactors each containing at least one catalyst fixed bed, which are connected with each other via pipe conduits such that they can be traversed by the educt/product mixture one after the other, in freely selectable order.

Method for producing a gaseous fuel comprising hydrogen from kinetic and/or potential energy recovered from a vehicle powered by a four stroke diesel engine fitted with an engine braking mechanism and system useful to implement such method

A method for producing a hydrogen gaseous fuel from kinetic and/or potential energy recovered from a vehicle powered by a four stroke Diesel engine fitted with a Jacobs engine brake during a deceleration stage. Such a method comprises the following steps: a) providing a preheated steam flow; b) providing a gas flow from at least one chemical species used as preheated carbon and hydrogen source; c) mixing the gas flow from at least one chemical species used as carbon and hydrogen source from step a) with the steam flow from step b); d) reacting the mixture from step c) in the catalytic bed of a reforming reactor, heated by high temperature air from the compression stage of the Diesel engine acting as engine brake upon deceleration, producing an outlet synthesis gas flow which contains hydrogen; e) causing water to condense in the outlet synthesis gas flow which contains hydrogen, producing a water-free synthesis gas flow, and f) storing the synthesis gas flow obtained at step e) in a reservoir for its subsequent use during an acceleration stage of the vehicle. A system useful to implement the method for recovering kinetic and/or potential energy from a vehicle powered by a four stroke Diesel engine fitted with a Jacobs engine brake during a deceleration stage.