ГЕНЕРИРОВАНИЕ ВОДЯНОГО ПАРА В ПРОЦЕССАХ РЕФОРМИНГА С ВОДЯНЫМ ПАРОМ

FIELD: machine building. SUBSTANCE: invention refers to procedure for generation of steam of at least two kinds with different purity at process of reforming with steam and to device for implementation of this procedure. At least two installations for reforming with steam operate parallel; also, steam of the first kind possesses higher purity, than steam of the second kind. Installations for reforming with steam operating parallel are united into groups of at least two installations for reforming with steam. Inside the groups all generated amount of pure steam is generated in one of the installations exclusively by evaporation of degassed and demineralised water, while all generated amount of impure steam is generated in another installation by evaporation of degassed water containing water impurities. Also, this muddy water at least partially is produced of condensate inside the group containing mainly water. EFFECT: generation of steam of high purity at reduced expenditures for maintenance and operation. 10 cl, 2 dwg, 2 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2 425 796 (13) C2 (51) МПК C01B 3/32 (2006.01) B01J 7/00 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ, ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (21)(22) Заявка: 2007115798/05, 26.04.2007 (24) Дата начала отсчета срока действия патента: 26.04.2007 2 4 2 5 7 9 6 R U Адрес для переписки: 101000, Москва, М. Златоустинский пер., 10, кв. 15, "ЕВРОМАРКПАТ", пат.пов. Р.А. Каксис (54) ГЕНЕРИРОВАНИЕ ВОДЯНОГО ПАРА В ПРОЦЕССАХ РЕФОРМИНГА С ВОДЯНЫМ ПАРОМ (57) Реферат: Изобретение относится к способу генерирования водяного пара по меньшей мере двух типов, обладающих разной чистотой, в процессах реформинга с водяным паром и к устройству для осуществления этого способа. По меньшей мере две установки для реформинга с водяным паром работают параллельно, причем водяной пар первого типа обладает более высокой чистотой, чем водяной пар второго типа. Установки для реформинга с водяным паром, ...

ПОЛУЧЕНИЕ МЕТАНОЛА С ИСПОЛЬЗОВАНИЕМ СВЕРХЧИСТОГО ВОДОРОДА ВЫСОКОГО ДАВЛЕНИЯ

Изобретение относится к способу получения метанола. Способ включает получение кислорода на установке разделения воздуха с воздушными компрессорами, приводимыми в действие газовой турбиной, нагревание потока углеводородного сырья с использованием отработанного в газовой турбине газа, экзотермическое взаимодействие первой части потока нагретого углеводородного сырья с паром или газообразным окислителем, включающим молекулярный кислород, с получением сингаза с экзотермическим выделением тепла, эндотермический риформинг второй части потока углеводородного сырья паром над катализатором в риформинг-установке с теплообменником с получением сингаза эндотермического риформинга, причем часть тепла, использованного при получении сингаза эндотермического риформинга, образуется при извлечении экзотермического тепла от образовавшегося сингаза и образовавшегося сингаза эндотермического риформинга, объединение образовавшегося с экзотермическим выделением тепла сингаза и образовавшегося сингаза эндотермического ...

СПОСОБ ПОЛУЧЕНИЯ АЦЕТИЛЕНА И СИНТЕЗ-ГАЗА

FIELD: technological processes; gas industry. SUBSTANCE: invention relates to a process for the production of acetylene and synthesis gas. Process is carried out by partial oxidation of hydrocarbons by oxygen, wherein the first feed stream containing one or more hydrocarbons, and the second feed stream containing oxygen are separately heated from each other, mixed in a mass flow ratio from the second feed stream and the first feed stream corresponding to an oxygen number less than or equal to 0.31, wherein the oxygen number is the ratio of the actually present amount of oxygen in the second feed stream and the stoichiometrically necessary amount of oxygen, which is required for the complete combustion of one or more hydrocarbons contained in the first feed stream, is supplied to a combustion chamber where occurs partial oxidation of these hydrocarbons to obtain the first cracked gas stream, wherein the first cracked gas stream in the prequenching as the result of injection of aqueous medium for quenching is cooled to a temperature in the range of from 100 to 1,000 °C, to obtain the second cracked gas stream, from 50 to 90 % of the solids contained therein is separated from the second cracked gas stream to obtain a stream of solids, as well as the third cracked gas stream, the third cracked gas stream during the final quenching as a result of water injection is cooled to a temperature from 80 to 90 °C to obtain the fourth cracked gas stream, as well as the first stream of process water , the fourth cracked gas stream is subjected to final separation of the solids to obtain one or more process water streams, as well as a gaseous product stream, process water streams are collected into one combined stream which is partially fed back to the final quenching process, but otherwise subjected to purification by partial evaporation,wherein the stream being evaporated in an amount from 0.01 to 10 % by weight, based on the total mass of the stream, to obtain a purified stream ...

Способ получения синтез-газа

FIELD: chemical or physical processes. SUBSTANCE: invention relates to a method of producing hydrocarbons. Method is realized by producing first (3) and second (4) partial feed streams from hydrocarbon-containing feed stream (1). At that, first partial feed stream (3) is converted by partial oxidation or autothermal reforming (R) into first stream of synthesis gas (8), and second partial feed stream (4) is converted by steam reforming (D) to second stream of synthesis gas (10). Then combined with first stream of synthesis gas (8) to form third stream of synthesis gas (5), at least first part (11) of which by Fischer—Tropsch synthesis (F) is converted into crude product stream (16) containing hydrocarbons with different chain lengths, from which light hydrocarbons are separated into residual gas (17) to return them to the process and used in partial oxidation or autothermal reforming (R). At least one part (19) of residual gas (17) is used to extract unsaturated hydrocarbons (21) using cryogenic separation methods, to obtain stream (20) which does not contain unsaturated hydrocarbons for use as feedstock for partial oxidation or autothermal reforming (R). EFFECT: technical result of the invention is higher efficiency of the process. 10 cl, 1 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 734 821 C2 (51) МПК C10G 2/00 (2006.01) C01B 3/24 (2006.01) C01B 3/36 (2006.01) C10G 45/02 (2006.01) C01B 3/48 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК C10G 2/00 (2020.08); C01B 3/24 (2020.08); C01B 3/36 (2020.08); C10G 45/02 (2020.08); C01B 3/48 (2020.08) (21)(22) Заявка: 2017107429, 07.03.2017 (24) Дата начала отсчета срока действия патента: (73) Патентообладатель(и): ЛИНДЕ АКЦИЕНГЕЗЕЛЛЬШАФТ (DE) Дата регистрации: 23.10.2020 08.03.2016 DE 102016002728.2 (43) Дата публикации заявки: 10.09.2018 Бюл. № 25 (56) Список документов, цитированных в отчете о поиске: US 20140326639 A1, 06.11.2014. US 20080312347 A1, 18.12.2008. ...

СПОСОБ ПРОИЗВОДСТВА СИНТЕЗ-ГАЗА

Изобретение относится к газовой и химической промышленности. Твердые или жидкие углеродсодержащие топлива газифицируют с кислородсодержащим окислительным средством в реакторе (1). Синтез-газ выводят из реактора (1) через верхнюю часть, а образовавшиеся во время реакции минеральные капли шлака - в направлении силы тяготения вниз. Газификацию проводят в реакторе (1) при температуре от 800 до 1800°С. Синтез-газ без охлаждения направляют через фильтр горячего газа (2) и затем для охлаждения через газотрубный котел (3). Отделяющиеся на фильтре горячего газа частицы шлака (13) направляют назад в реактор (1) газификации в направлении силы тяготения. Изобретение позволяет использовать для отвода тепла дешевые газотрубные котлы вместо котлов с радиационными поверхностями нагрева. 2 н. и 23 з.п. ф-лы, 3 ил.

ТЕПЛООБМЕННЫЙ РЕАКТОР ДЛЯ ПРОИЗВОДСТВА ВОДОРОДА С ПОМОЩЬЮ ВСТРОЕННОГО ПУЧКА ПАРОГЕНЕРАТОРА

Изобретение предназначено для осуществления реакций парового риформинга и может быть использовано в химической промышленности. Теплообменный реактор содержит множество байонетных труб (4), подвешенных к верхнему своду (2), простирающихся до уровня нижнего дна (3) и заключенных в кожух (1), содержащий впускной (Е) и выпускной (S) патрубки для дымовых газов. Теплообменный реактор содержит пучок труб парогенератора, образованный множеством вертикальных труб (5), подвешенных к верхнему своду (2) и заключенных в периферийное пространство между внутренней перегородкой (Bi) и вертикальной стенкой кожуха (1). Внутренняя перегородка (Bi) содержит отверстие (Oi) для прохода дымовых газов из середины реактора к периферийному пространству. Вертикальные трубы (5) питаются водой из нижнего распределителя (9). Пароводяная смесь, выходящая из вертикальных труб (5), собирается в верхнем коллекторе (7), расположенном над верхним сводом (2). Нижняя линия (14) связывает жидкую фазу сепараторного резервуара ...

SOFC-система и способ эксплуатации SOFC-системы

Изобретение относится к системе твердооксидного топливного элемента, а также к способу эксплуатации такой системы и может быть применено в энергетике. Система твердооксидного топливного элемента содержит установку реформинга, батарею твердооксидного топливного элемента, топку для получения тепла для установки реформинга. В установку реформинга подается поток газообразного углеводорода и пар. Установка реформинга и топка встроены в один блок для компактности и уменьшения тепловых потерь. В системе предусмотрен блок управления расходом свежего воздуха с помощью нагнетателя. За топкой расположен один или несколько испарителей для охлаждения выхлопного потока топки и выработки пара, который затем подается в установку реформинга. В системе предусмотрен датчик температуры газа, обогащенного водородом, на основании которого блок управления регулирует работу нагнетателя для поддержания содержания кислорода в выхлопном потоке топки в пределах заданного диапазона. Обеспечивается повышение надежности ...

СПОСОБ ПОЛУЧЕНИЯ АММИАКА И ПРОИЗВОДНЫХ СОЕДИНЕНИЙ, В ЧАСТНОСТИ МОЧЕВИНЫ

Изобретение относится к способу и установке для получения аммиака и производного соединения 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. Способ осуществляют с энергопотребителями (2) и потребителями (3) тепла. При этом часть (15) природного газового сырья используют для снабжения топливом поршневого газового двигателя (6), а энергию (7), вырабатываемую газовым двигателем (6), используют для обеспечения, по меньшей мере частично, потребности энергопотребителей (2) в энергии. Далее рекуперируют тепло из отходящего газа газового двигателя и по меньшей мере часть тепла рекуперируют для обеспечения им по меньшей мере одного из указанных потребителей (3) тепла. При этом тепло, рекуперированное из ...

УСТРОЙСТВА И СПОСОБЫ ОБРАБОТКИ ВОДОРОДА И МОНООКСИДА УГЛЕРОДА

FIELD: chemistry. SUBSTANCE: invention relates to hydrocarbon chemistry and an apparatus and a method of processing hydrogen and carbon monoxide. A stream of starting gas can be processed via a Fischer-Tropsch process. Unreacted hydrogen and carbon monoxide can be recycled, wherein a reactor for catalytic reforming of exhaust gas and a heat exchanger for spent gas of a gas turbine, which carries the pre-heating thermal load, are used. EFFECT: invention increases technological effectiveness of the process by increasing efficiency of the process of converting raw material to end products. 18 cl, 1 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2 495 914 (13) C2 (51) МПК C10K C10K 3/02 3/06 (2006.01) (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (21)(22) Заявка: 2011101927/05, 19.06.2009 (24) Дата начала отсчета срока действия патента: 19.06.2009 (73) Патентообладатель(и): ДжиТиЭлПЕТРОЛ ЭлЭлСи (US) R U Приоритет(ы): (30) Конвенционный приоритет: 20.06.2008 US 61/074,571 (72) Автор(ы): АЛЛАМ Родни Дж. (GB) (43) Дата публикации заявки: 27.07.2012 Бюл. № 21 2 4 9 5 9 1 4 (45) Опубликовано: 20.10.2013 Бюл. № 29 (56) Список документов, цитированных в отчете о поиске: RU 2137702 С1, 20.09.1999. US 6669744 В2, 30.12.2003. WO 2007114250 А1, 11.10.2007. WO 2005082776 А2, 09.09.2005. US 6159395 А, 12.12.2000. 2 4 9 5 9 1 4 R U (86) Заявка PCT: US 2009/048021 (19.06.2009) C 2 C 2 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 20.01.2011 (87) Публикация заявки РСТ: WO 2009/155554 (23.12.2009) Адрес для переписки: 129090, Москва, ул. Б. Спасская, 25, стр.3, ООО "Юридическая фирма Городисский и Партнеры" (54) УСТРОЙСТВА И СПОСОБЫ ОБРАБОТКИ ВОДОРОДА И МОНООКСИДА УГЛЕРОДА (57) Реферат: Изобретение относится к химии углеводородов и касается устройства и способа обработки водорода и монооксида углерода. Поток исходного газа может быть обработан посредством осуществления процесса ФишераТропша. Непрореагировавшие водород и ...

СПОСОБ ПОЛУЧЕНИЯ МЕТАНОВОДОРОДНОЙ СМЕСИ

Изобретение относится к области химии. Способ получения метановодородной смеси осуществляют путем подачи природного газа по трубопроводу 1 в сатуратор 2, заполняемый циркулирующим конденсатом водяного пара 3, для получения смешанного газового потока 4, в который на выходе из сатуратора 2 вводится перегретый водяной пар 5. Теплообменник 6 служит для нагревания потока 4 до 350-530° и соединен с первым адиабатическим реактором 7. Второй теплообменник 8, используемый для нагрева потока до 620-680°С, соединен со вторым адиабатическим реактором 9, в котором осуществляется конверсия углеводородов. В третьем теплообменнике 10 смешанный поток 4 разогревается до температуры 600-680°С и проходит через третий адиабатический реактор 11, в котором происходит более глубокая конверсия метана. Пароперегреватель 12 используют для перегрева потока водяного пара, производимого в парогенераторе 13 из питательной воды 14. В подогревателе 15 циркулирующего конденсата производится нагрев охлажденного потока 4, ...

СПОСОБ КОНВЕРСИИ УГЛЕВОДОРОДОВ (ВАРИАНТЫ), КАТАЛИЗАТОР (ВАРИАНТЫ) И СПОСОБ ПОЛУЧЕНИЯ КАТАЛИЗАТОРА НА ПОДЛОЖКЕ

ÐÎÑÑÈÉÑÊÀß ÔÅÄÅÐÀÖÈß (19) RU (11) 2005 139 412 (13) A (51) ÌÏÊ B01J 19/00 (2006.01) ÔÅÄÅÐÀËÜÍÀß ÑËÓÆÁÀ ÏÎ ÈÍÒÅËËÅÊÒÓÀËÜÍÎÉ ÑÎÁÑÒÂÅÍÍÎÑÒÈ, ÏÀÒÅÍÒÀÌ È ÒÎÂÀÐÍÛÌ ÇÍÀÊÀÌ (12) ÇÀßÂÊÀ ÍÀ ÈÇÎÁÐÅÒÅÍÈÅ (21), (22) Çà âêà: 2005139412/15, 08.04.2004 (71) Çà âèòåëü(è): ÂÈËÎÑÈÑ ÈÍÊ. (US) (30) Êîíâåíöèîííûé ïðèîðèòåò: 16.05.2003 US 10/440,053 30.05.2003 US 10/449,913 (85) Äàòà ïåðåâîäà çà âêè PCT íà íàöèîíàëüíóþ ôàçó: 16.12.2005 (74) Ïàòåíòíûé ïîâåðåííûé: Ïîïåëåíñêèé Íèêîëàé Êîíñòàíòèíîâè÷ (87) Ïóáëèêàöè PCT: WO 2004/103549 (02.12.2004) Àäðåñ äë ïåðåïèñêè: 127055, Ìîñêâà, à/ 11, ïàò.ïîâ. Í.Ê.Ïîïåëåíñêîìó R U ÑÏÎÑÎÁ ÏÎËÓ×ÅÍÈß ÊÀÒÀËÈÇÀÒÎÐÀ ÍÀ ÏÎÄËÎÆÊÅ (57) Ôîðìóëà èçîáðåòåíè 1. Ñïîñîá êîíâåðñèè óãëåâîäîðîäîâ, â ÷àñòíîñòè ïðåâðàùåíè óãëåâîäîðîäíîãî ðåàãåíòà â ïðîäóêò, ñîäåðæàùèé ÑÎ è H2, îòëè÷àþùèéñ òåì, ÷òî ïðîïóñêàþò ÷åðåç ìèêðîêàíàëüíûé ðåàêòîð ïîòîê êîìïîçèöèè ðåàãåíòîâ, ñîäåðæàùåé óãëåâîäîðîäíûé ðåàãåíò è êèñëîðîä èëè èñòî÷íèê êèñëîðîäà, ïðè êîíòàêòèðîâàíèè ñ êàòàëèçàòîðîì ÷àñòè÷íîãî îêèñëåíè â óñëîâè õ ðåàêöèè ÷àñòè÷íîãî îêèñëåíè ñ îáðàçîâàíèåì ïðîäóêòà, ïðè ýòîì ìèêðîêàíàëüíûé ðåàêòîð âêëþ÷àåò ãðóïïó ðàáî÷èõ ìèêðîêàíàëîâ, ñîäåðæàùèõ êàòàëèçàòîð, âõîäíîé êîëëåêòîð, ÷åðåç êîòîðûé ïîäàþò ïîòîê òåêó÷åé ñðåäû â ðàáî÷èå êàíàëû, è âûõîäíîé êîëëåêòîð, ÷åðåç êîòîðûé âûâîä ò ïîòîê òåêó÷åé ñðåäû èç ðàáî÷èõ ìèêðîêàíàëîâ, à óãëåâîäîðîäíûé ðåàãåíò ñîäåðæèò ìåòàí, ïðè÷åì îáåñïå÷èâàþò âðåì êîíòàêòèðîâàíè êîìïîçèöèè ðåàãåíòîâ âíóòðè ðàáî÷åãî ìèêðîêàíàëà â ïðåäåëàõ ïðèáëèçèòåëüíî 500 ìñ, òåìïåðàòóðó êîìïîçèöèè ðåàãåíòîâ è ïðîäóêòà âíóòðè ðàáî÷åãî ìèêðîêàíàëà â ïðåäåëàõ ïðèáëèçèòåëüíî 1150°Ñ, è âåëè÷èíó êîíâåðñèè óãëåâîäîðîäíîãî ðåàãåíòà ïî ìåíüøåé ìåðå ïðèáëèçèòåëüíî 50%. 2. Ñïîñîá ïî ï.1, îòëè÷àþùèéñ òåì, ÷òî óêàçàííûé ïðîäóêò âë åòñ ïðîìåæóòî÷íûì ïðîäóêòîì, è äîïîëíèòåëüíî îñóùåñòâë þò ïðîïóñê ýòîãî ïîëó÷åííîãî ïðîìåæóòî÷íîãî ïðîäóêòà ÷åðåç ìèêðîêàíàëüíûé ðåàêòîð ïðè êîíòàêòèðîâàíèè ñ êàòàëèçàòîðîì ñãîðàíè â óñëîâè õ ðåàêöèè îáðàçîâàíè êîíå÷íîãî ïðîäóêòà, ñîäåðæàùåãî CO2 è H2O. 3. Ñïîñîá ïî ...

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 ...

СИСТЕМЫ И СПОСОБЫ ИСПОЛЬЗОВАНИЯ ОСТАТОЧНОГО ГАЗА СИНТЕЗА ФИШЕРА-ТРОПША В ТЕХНОЛОГИЧЕСКОМ ПРОЦЕССЕ ПОЛУЧЕНИЯ СИНТЕТИЧЕСКОГО ЖИДКОГО ТОПЛИВА ИЗ ПРИРОДНОГО ГАЗА

FIELD: oil and gas industry. SUBSTANCE: one of alternatives includes: reactor of Fischer-Tropsch synthesis that ensures availability of residue gas source; the first heater for preheating of residue gas; hydrogenation unit for hydrogenising of preheated residue gas; expansion device to reduce pressure of preheated and hydrogenated residue gas; the second heater for preheating of preheated, hydrated and expanded residue gas with receipt of initial gas consisting of residue gas and steam; and reactor of catalytic reforming for performance of initial gas reforming in presence of catalyst. At that the first preheater preheats residue gas up to temperature within the approximate range of 200 - 300°C, expansion device reduces pressure of preheated and hydrogenated residue gas up to the value from approximately 250,000 up to 500,000Pa (from 2.5 up to 5 bar), while the second heater heats preheated, hydrated and expanded residue gas up to temperature within the range of 500-600°C. The invention is also referred to recycling of residue gas from Fischer-Tropsch synthesis. EFFECT: reduced losses of methane and bringing carbon soot content in the reforming reactor to zero value. 25 cl, 1 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 560 874 C1 (51) МПК C07C 27/00 (2006.01) C07C 1/04 (2006.01) C10G 2/00 (2006.01) C10G 35/00 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ (21)(22) Заявка: ИЗОБРЕТЕНИЯ К ПАТЕНТУ 2014123008/04, 08.11.2012 (24) Дата начала отсчета срока действия патента: 08.11.2012 Приоритет(ы): (30) Конвенционный приоритет: (72) Автор(ы): ЧИЛИ Роберт Б. (US), МЕТЬЮС Гэри Е. (US), МЕЙССНЕР Дэвид К. (US) 08.11.2011 US 61/556,933 (45) Опубликовано: 20.08.2015 Бюл. № 23 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 09.06.2014 (86) Заявка PCT: US 2012/064026 (08.11.2012) 2 5 6 0 8 7 4 (56) Список документов, цитированных в отчете о поиске: US 2003134911 A1, 17.07.2003. US 6114400 A, 05.09.2000. EA 199800445 A1, 25.02.1999 R U ...

РЕАКТОР ДЛЯ ПАРЦИАЛЬНОГО ОКИСЛЕНИЯ УГЛЕВОДОРОДНЫХ ГАЗОВ

FIELD: power industry. SUBSTANCE: reactor includes an external housing with a reactor reaction products removal device and at least with one device for supply of raw material or components of raw material to a catalyst sleeve arranged inside the reactor with a gap with the external housing, filled with a catalyst and including devices for removal of products from its lower part. The catalyst sleeve is provided with a jacket adjacent at least to some part of the cylindrical wall of the catalyst sleeve, which in the adjoining area of the jacket has through openings; the reactor is provided with a device for supply to the jacket of a cooling agent cooling down the catalyst sleeve and supplied to the catalyst sleeve through the openings in its cylindrical wall. EFFECT: reduction of wall temperature of a catalyst sleeve; reduction of metal corrosion of the catalyst sleeve. 6 cl, 2 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 554 008 C1 (51) МПК C01B 3/38 (2006.01) B01J 8/04 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ (21)(22) Заявка: ИЗОБРЕТЕНИЯ К ПАТЕНТУ 2014100683/04, 13.01.2014 (24) Дата начала отсчета срока действия патента: 13.01.2014 (72) Автор(ы): Долинский Сергей Эрикович (RU), Дергачев Александр Александрович (RU) (45) Опубликовано: 20.06.2015 Бюл. № 17 R U (73) Патентообладатель(и): Общество с ограниченной ответственностью "Газохим Техно" (RU) Приоритет(ы): (22) Дата подачи заявки: 13.01.2014 (56) Список документов, цитированных в отчете о поиске: WO2011088982 A1, 28.07.2011 . 2 5 5 4 0 0 8 R U (54) РЕАКТОР ДЛЯ ПАРЦИАЛЬНОГО ОКИСЛЕНИЯ УГЛЕВОДОРОДНЫХ ГАЗОВ (57) Реферат: Изобретение относится к реактору для стенки катализаторной гильзы, которая в области парциального окисления углеводородного сырья. примыкания рубашки выполнена со сквозными Реактор включает внешний корпус со средством отверстиями, реактор снабжен средством ввода вывода продуктов реакции из реактора и с хотя в рубашку хладоагента, охлаждающего бы одним средством ...

SOFC-система и способ эксплуатации SOFC-системы

СПОСОБ ПОЛУЧЕНИЯ АММИАКА И ПРОИЗВОДНЫХ СОЕДИНЕНИЙ, В ЧАСТНОСТИ МОЧЕВИНЫ

СИСТЕМА ПОЛУЧЕНИЯ ЭЛЕКТРОЭНЕРГИИ ПРИ ФЕРМЕНТАЦИИ СИНТЕЗ-ГАЗА

... 1. Способ получения пара высокого давления в процессе ферментации синтез-газа, включающий: приведение в контакт горячего синтез-газа, имеющего температуру, превышающую примерно 1400°F, с охлажденным синтез-газом с получением во входном отверстии котла-утилизатора отходящего тепла предварительно охлажденного синтез-газа с температурой, не превышающей 1400°F, и подачу предварительно охлажденного синтез-газа в котел-утилизатор отходящего тепла, обеспечивающего получение пара высокого давления и охлажденного синтез-газа.2. Способ по 1, дополнительно включающий подачу низкокалорийного синтез-газа в горелку для отходящих газов, обеспечивающую получение горячего газа горелки; подачу горячего газа из горелки в пароперегреватель котла-утилизатора отходящих газов, обеспечивающего получение пара высокого давления; исоединение пара высокого давления котла-утилизатора отходящего тепла и пара высокого давления котла-утилизатора отходящих газов для получения смешанного пара высокого давления.3. Способ ...

Verfahren zur Herstellung von Synthesegas fuer die Ammoniaksynthese

Autothermer Reformer mit mehreren Durchlässen

Autothermer Reformer zum Reformieren eines Kohlenwasserstoff-Brennstoffes, mit: einem Gehäuse, das eine Reformierkammer definiert; einem Brennstoffeinlass in Verbindung mit der Reformierkammer; einem Wasserdampfeinlass in Verbindung mit der Reformierkammer; und einer Vielzahl von Lufteinlässen in Fluidverbindung mit der Reformierkammer, wobei einer der Vielzahl von Lufteinlässen in der Startbetriebsart ein Luftvolumen an die Reformierkammer liefert, und ein zweiter der Vielzahl von Lufteinlässen in einer Normalbetriebsart ein Luftvolumen an die Reformierkammer liefert.

Vorrichtung zur Herstellung von Wasserstoff

PROCESS FOR PRODUCING AMMONIA

... 1331661 Ammonia synthesis W R GRACE & CO 11 June 1971 [12 June 1970] 27530/71 Heading C1A [Also in Division C5] In the synthesis of ammonia comprising primary reforming of hydrocarbons (e.g. CH 4 ) with steam, secondary reforming with air and treatment of the effluent so produced in a water gas shift reaction to form a crude ammonia synthesis gas, purification of the latter to remove CO 2 and conversion of the purified synthesis gas to NH 3 under pressure, heat energy is recovered from the formation of the synthesis gas and is converted to mechanical energy, e.g. via electrical energy, which is used to compress the synthesis gas, before the conversion to ammonia operation, to such a pressure that the ammonia obtained is condensed without recourse to refrigeration, e.g. by heat exchange with water. The conversion of the synthesis gas to NH 3 is preferably carried out at 700-1200‹ F. and 5000-15000 p.s.i.a.

Process for the preparation of a hydrogen-containing gas mixture

A high temperature gas made by a partial combustion process with steam at 1 is brought to a lower temperature and pressure by passage through at least one gas turbine 22, subjected to a catalytic shift conversion at 24, and is brought to a high pressure, e.g. 150 to 300 atmos. in one or more compressors 29 driven by the turbines. The apparatus shown in Fig. 1 is adapted for making synthesis gas using heavy oils as feedstock, and includes soot and sulphur removal plant 9, 13, and CO2 removal plant 26. The cooled, purified gas at 15 is reheated to 800 DEG C. in a combustion chamber 17 where light hydrocarbon or purified gas delivered at 19 is completely burnt. Catalytic afterburners supplied with light hydrocarbon, air, oxygen and steam may be inserted in the line 21, see Fig. 2 (not shown), to suppress CH4 and carbon in the final gas. In the modification of Fig. 3 (not shown), intended for a light distillate feedstock, the parts 9, 13 are omitted, and catalytic afterburners ...

A method of disposing a water gas shift catalyst on a metal substrate

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).

Gas-to-liquid technology

Process and Apparatus for Reforming Hydrocarbons.

... 1,156,002. Catalytic apparatus. C. F. BRAUN & CO. 14 June, 1966 [22 Oct., 1965], No. 26552/66. Heading B1F. [Also in Division Cl] Apparatus used in the autothermal conversion of hydrocarbons comprises an outer shell 410 having an inlet 412 and an outlet 414, the outer shell enclosing an inner shell 416 separated from the outer shell along a major portion of its length by a fluid conducting space 420 and being connected to the outer shell at a point proximate to the outlet of the outer shell e.g. gas tight seal 418, the inner shell having a plurality of openings 422 in the wall thereof, and .a plurality of gas conducting fuses 424 having one end in communication with the outlet, a chamber for containing catalyst 444 and means for introducing air into the chamber e.g. spanger 434, the gas conducting tubes having an opposite end in communication with the chamber, the walls of the chamber being spaced from the walls of the inner shell to provide fluid communication between the chamber and the ...

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.

PRODUCTION OF SYNTHESIS GAS

Improvements in or relating to a reaction process and apparatus therefor

Process for production of hydrogen

... In the production of hydrogen from hydrocarbons by the steps of reforming with steam and shift conversion, an improvement is effected by maintaining a steam-to-carbon ratio of 3 to 7 and a pressure of 300 to 700 p.s.i.a. in the reformer, converting 50 to 85% of the hydrocarbons to hydrogen in the reforming step, removing carbon oxides and steam from the process stream and cryogenically separating unconverted hydrocarbons from hydrogen to give 96% to 99.5% pure hydrogen. Contaminated process condensate (principally dissolved CO2, H2 and hydrocarbons), obtained after shift conversion, may be vaporized and recycled to the reformer. Low-purity hydrogen from an extraneous source may be purified by addition to the process stream prior to cryogenic separation. As shown, hydrocarbon and steam are preheated, e.g. to 750 DEG F., and fed to reformer R-1, inlet pressure being e.g. 500 p.s.i.g. and outlet temperature being e.g. 1480 DEG F. R-1 exit gases are cooled to e.g. 700 DEG ...

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

Method and apparatus for sequestering carbon from a spent gas

METHOD OF SUPPRESSING METAL CONTAMINATION OF SYNTHESIS GAS PRODUCTION

HEAT EXCHANGE SYSTEM

Method of suppressing metal contamination of synthesis gas production apparatus

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

Heat exchange system

Process of production of hydrogen.

Heat exchange system

Method of suppressing metal contamination of synthesis gas production apparatus

Heat exchange system

Method of suppressing metal contamination of synthesis gas production apparatus

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

DISK ARCHITECTURE FOR CHEMICAL PROCESS ON BASIS OF MICRO COMPONENTS

PROCEDURE FOR THE PRODUCTION OF LANGKETTIGEN

CATALYTIC SULFUR RECUPERATION SYSTEM WITH SHORT RETENTION TIME FOR THE DISTANCE OF H2S FROM AN EXHAUST GAS STREAM

COMPACT FUEL PROCESSING CONVERTING TO THE PRODUCTION OF A HYDROGEN-RICH GAS

SPOX SUPPORTED PROCEDURE FOR THE PRODUCTION OF SYNTHESIS GAS

BRENNKRAFTMASCHINE, INSBESONDERE STATIONÄRER GASMOTOR, UMFASSEND EINEN BRENNRAUM

Brennkraftmaschine (1), insbesondere stationärer Gasmotor, umfassend einen Brennraum (2), dem über eine Brennraumleitung (3) ein Treibstoff (B1) aus einer ersten Treibstoffquelle (4) zuführbar ist, eine Vorkammer (5), der über eine Spülgasleitung (6) ein Spülgas (S) zuführbar ist, wobei ein Spülgasmischer (7) vorgesehen ist, in dem ein über eine Treibstoffleitung (8) zuführbarer Treibstoff (B2) aus der ersten Treibstoffquelle (4) oder aus einer zweiten Treibstoffquelle (4') und ein über eine Synthesegasleitung (9) zuführbares Synthesegas (R) mischbar sind und wobei ein Mischerausgang (10) in die Spülgasleitung (6) mündet, wobei das Synthesegas (R) durch einen Reformer (11) erzeugbar ist, dem über eine Reformerzuleitung (12) ein Brennstoff (B3) aus einer Brennstoffquelle (4, 4') zuführbar ist und dessen Reformerausgang (14) in die Synthesegasleitung (9) mündet, wobei eine Kühlvorrichtung (13, 15) zum Kühlen des Synthesegases (R) vorgesehen ist.

BRENNKRAFTMASCHINE, INSBESONDERE STATIONÄRER GASMOTOR, UMFASSEND EINEN BRENNRAUM

Brennkraftmaschine (1), insbesondere stationärer Gasmotor, umfassend einen Brennraum (2), dem über eine Brennraumleitung (3) ein Treibstoff (B-i) aus einer ersten Treibstoffquelle (4) zuführbar ist, eine Vorkammer (5), der über eine Spülgasleitung (6) ein Spülgas (S) zuführbar ist, wobei ein Spülgasmischer (7) vorgesehen ist, in dem ein über eine Treibstoffleitung (8) zuführbarer Treibstoff (B2) aus der ersten Treibstoffquelle (4) oder aus einer zweiten Treibstoffquelle (4') und ein über eine Synthesegasleitung (9) zuführbares Synthesegas (R) mischbar sind und wobei ein Mischerausgang (10) in die Spülgasleitung (6) mündet, wobei das Synthesegas (R) durch einen Reformer (11) erzeugbar ist, dem über eine Reformerzuleitung (12) ein Brennstoff (B3) aus einer Brennstoffquelle (4, 4') zuführbar ist und dessen Reformerausgang (14) in die Synthesegasleitung (9)mündet, wobei eine Kühlvorrichtung (13, 15) zum Kühlen des Synthesegases (R) vorgesehen ist.

PRODUCTION OF LIQUID HYDROCARBON PARLIAMENTARY GROUPS BY HYDROGENATION OF FOSSIL REPLACEMENT MATERIAL.

PRODUCTION A HYDROGEN OF A CONTAINING GAS.

MICRO COMPONENT DEVICE FOR EFFICIENT CONTACTING OF A FLUID

DISK ARCHITECTURE FOR CHEMICAL PROCESS ON BASIS OF MICRO COMPONENTS

SYNTHESIS GAS PRODUCTION

PROCEDURE FOR EXECUTION OF CATALYTIC OR NICHTKATALYTI PROCEDURES, REACTANT ENRICHED WITH A WITH OXYGEN

CYLINDRICAL EINROHR REFORMER

PROCESS AND APPARATUS FOR THE PRODUCTION OF SYNTHESIS GAS

Steam pyrolysis as a process to enhance the hydro-gasification of carbonaceous materials

Supply of steam and hydrogen to a process or plant producing synthesis gas

Combined synthesis gas generator

In various systems and processes, synthesis gas generation may be combined. A partial oxidation reactor (POX) and a gas convectively heated steam/hydrocarbon catalytic reformer (GHR) may be combined to produce synthesis gas. In some implementations, a partial oxidation reactor, a gas convectively heated steam/catalytic reformer, and a waste hat boiler may be combined to produce synthesis gas.

Heat transfer optimization in multishell reformer

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 engine; power produced by said gas engine; is transferred to at least one power user of the process, such as a compressor; heat is recovered from exhaust gas of said gas engine;, and at least part of said heat may be 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.

Production of H2-rich gas

Background of the invention

Fuel processor for producing a hydrogen rich gas

Reactor module for use in a compact fuel processor

HYDROGEN GENERATION PROCESSES AND APPARATUS AND CONTROL SYSTEM

Hydrogen generators and processes for operating hydrogen generators using partial oxidation/steam reforming of fuel are provided that can achieve desirable Net Hydrogen Efficiencies over a range of fuels and hydrogen product production rates and purities. Superheated steam for the reformer feed is provided through indirect heat exchange with the reformate and through indirect heat exchange with a flue gas. The relative portions of superheated steam from each heat exchange is adjusted to enhance Net Hydrogen Efficiency as a demand condition such as hydrogen product production rate or purity changes, and cooler oxygen--containing gas is used to avoid precombustion temperatures in the reformer feed.

STEAM-HYDROCARBON PROCESS AND APPARATUS

In a process of reacting a hydrocarbon with steam and/or carbon dioxide in a reaction zone heated by a combustion furnace to give olefins or process gas containing carbon oxides and hydrogen high grade heat is recovered from furnace flue gasses and/or process gas whereby to cool such gases to 150-300.degree.C. When the process gas is used in a synthesis of for example methanol or ammonia, gases at 150-300.degree.C are also produced. Previously the recovery of heat fro such low grade heat sources has been inefficient or inconvenient. According to the invention the best is recovered by means of an intermediary liquid coolant, which is brought into direct heat exchange with streams to be used in the process. Preferably the liquid is water under pressure and is brought into direct heat exchange with a gas to be fed to the process; by this means 10-30% of the stream used can be provided from low grade waste heat.

RECOVERY OF SULFUR FROM H2S AND CONCURRENT PRODUCTION OF H2 USING SHORT CONTACT TIME CPOX

A method, apparatus and system for treating a stream containing H2S are disclosed. A preferred method comprises mixing the stream containing H2S with a light hydrocarbon stream and an oxygen containing stream to form a feed stream, contacting the feed stream with a catalyst for less than about 10000 microseconds while simultaneously raising the temperature of the stream sufficiently to allow oxidation of the H2S and partial oxidation of the light hydrocarbon to produce a product stream containing elemental sulfur, CO and hydrogen, and cooling the product stream sufficiently to condense at least a portion of the elemental sulfur and produce a tail gas. A preferred method further includes the step of processing the tail gas so as to react CO in the tail gas with water to produce CO2 and hydrogen and so as to convert elemental sulfur, SO2, COS, and CS2 in the tail gas into H2S, the step of contacting the tail gas with an alkanolamine absorber to produce a treated tail gas, and the step of ...

MICROCOMPONENT ASSEMBLY FOR EFFICIENT CONTACTING OF FLUID

The present invention is a fundamental method and apparatus of a microcomponent assembly that overcomes the inherent limitations of state of the art chemical separations. The fundamental element enabling miniaturization is the porous contactor (200) contained within a microcomponent assembly for mass transfer of a working compound from a first medium to a second medium. The porous contactor (200) has a thickness, and a plurality of pores extending through the thickness. The pores are of a geometry cooperating with a boundary tension of one or the other or both of the media thereby preventing migration of one, other or both through the microporous contactor while permitting passage of the working compound. In the microcomponent assembly, the porous contactor (200) is placed between a first laminate (208) such that a first space or first microplenum is formed between the microporous contactor (200) and the first laminate (208). Additionally, a cover sheet (206) provides a second space or ...

PRODUCTION OF SYNTHETIC TRANSPORTATION FUELS FROM CARBONACEOUS MATERIALS USING SELF-SUSTAINED HYDRO-GASIFICATION

A process and apparatus for producing a synthesis gas for use as a gaseous fuel or as feed into a Fischer-Tropsch reactor to produce a liquid fuel in a substantially self-sustaining process. A slurry of particles of carbonaceous material in water, and hydrogen from an internal source, are fed into a hydro- gasification reactor under conditions whereby methane rich producer gases are generated and fed into a steam pyrolytic reformer under conditions whereby synthesis gas comprising hydrogen and carbon monoxide are generated. A portion of the hydrogen generated by the steam pyrolytic reformer is fed through a hydrogen purification filter into the hydro-gasification reactor, the hydrogen therefrom constituting the hydrogen from an internal source. The remaining synthesis gas generated by the steam pyrolytic reformer is either used as fuel for a gaseous fueled engine to produce electricity and/or process heat or is fed into a Fischer-Tropsch reactor under conditions whereby a liquid fuel is ...

HEAT TRANSFER OPTIMIZATION IN MULTISHELL REFORMER

A hydrocarbon fuel processing reactor for generating a hydrogen-enriched reformate from hydrocarbons is disclosed. A plurality of shells (36,46,56,66,76) are arranged coaxially having a gap defined between each of the successive shells, thereby forming a plurality of coaxial zones. The shells are configured to permit heat transfer from one zone to another. Fluid streams for reactions within the reactor are preheated by heat transfer from adjacent zones.

STEAM-PRODUCING PROCESS AND SYSTEM

System and process for producing steam in a steam-hydrocarbon reforming facility where oxygen is removed from demineralized water using a membrane degasifier. The membrane degasifier operates at a lower temperature compared to a deaerator, which is the conventional technology for removing oxygen.

TAIL GAS HEATING WITHIN PSA SURGE TANK

A method for operating a hydrogen generation system comprising: producing a synthesis gas stream in a steam reformer which has a combustion zone; introducing at least a portion of the synthesis gas stream to a water gas shift reactor; cooling the shifted synthesis gas stream to produce a cooled shifted synthesis gas stream; introducing the cooled shifted synthesis gas stream into a pressure swing adsorption unit, thereby producing a stream of predominantly hydrogen and a tail gas comprising predominantly byproducts; routing said tail gas to one or more surge tank(s) having a heat exchange device disposed therein and indirectly heating said tail gas by passing it over a surface of said heat exchange device inside which a hot fluid is cooled, thereby obtaining a heated tail gas; and routing said heated tail gas to the combustion zone of the reformer.

METHOD AND APPARATUS FOR IMPROVING THE EFFICIENCY OF REFORMING PROCESS FOR PRODUCING SYNGAS AND METHANOL WHILE REDUCING THE CO2 IN A GASEOUS STREAM

A method for the co-production of hydrogen and methanol including a hydrocarbon reforming or gasification device producing a syngas stream comprising hydrogen, carbon monoxide and carbon dioxide; introducing the syngas stream to a water gas shift reaction thereby converting at least a portion of the CO and H2O into H2 and CO2 contained in a shifted gas stream; cooling the shifted gas stream and condensing and removing the condensed fraction of H2O; then dividing the shifted syngas stream into a first stream and a second stream; introducing the first stream into a first hydrogen separation device, thereby producing a hydrogen stream, and introducing the second stream into a methanol synthesis reactor, thereby producing a crude methanol stream and a methanol synthesis off gas; introducing at least a portion of the methanol synthesis off gas into a second hydrogen separation device.

CYLINDRICAL STEAM REFORMING UNIT

A cylindrical steam reforming unit comprising a plurality of cylindrical bodies consisting of a first cylindrical body, a second cylindrical body and a third cylindrical body of successively increasing diameters disposed in a concentric spaced relation, a radiation cylinder disposed within and concentrically with the first cylindrical body, a burner disposed in the radial central portion of the radiation cylinder, and a reforming catalyst layer with a reforming catalyst filled in a gap between the first and second cylindrical bodies, wherein a CO shift catalyst layer and a CO removal catalyst layer are disposed in a gap between the second and third cylindrical bodies, the CO shift catalyst layer being formed in a gap with the direction of flow reversed at one axial end of the reform ing catalyst layer and through a heat recovery layer of predetermined length. According to this reforming unit, without internally disposing a heat insulation layer, a cooling mechanism or the like, the reforming ...

HYDROGEN MANUFACTURE WITH INTEGRATED STEAM USAGE

PROCESS FOR PRODUCING SYNTHESIS GAS

The invention relates to a process for producing hydrocarbons (23), in which a first feed substream (3) and a second feed substream (4) are obtained from a hydrocarbonaceous feed stream (1), of which the first feed substream (3) is converted by means of partial oxidation or autothermal reforming (R) to a first synthesis gas stream (8) and the second feed substream (4) is converted by means of steam reforming (D) to a second synthesis gas stream (10) and subsequently combined with the first synthesis gas stream (8) to give a third synthesis gas stream (5), of which at least a first portion (11) is converted by Fischer-Tropsch synthesis (F) to a crude product stream (16) comprising hydrocarbons of different chain lengths, from which light hydrocarbons are separated in a tail gas (17), in order to recycle them and use them in the partial oxidation or autothermal reforming (R). The characteristic feature here is that unsaturated hydrocarbons (21) are separated from at least a portion (19) of ...

HYDROGEN PRODUCTION PROCESS FOR COLD CLIMATES

Process for producing a hydrogen-containing product gas suited for operating in regions where the ambient conditions are below freezing for extended periods of time during the winter and warm or hot during the summer months. Hot makeup water is provided to the process to avoid freezing. A portion of the hot makeup water stream is heated in a steam generator to make steam where the steam is used to heat incoming hydrocarbon feed for the process. Another portion of the hot makeup water stream may be heated by combustion product gases where the heated water stream is used to heat incoming combustion oxidant.

SYNTHETIC GAS GENERATOR

The invention relates to an apparatus for generating synthetic gas, comprising a POX reactor with a first reaction chamber, into which a carbon-containing gaseous feedstock, as well as an oxidizing agent, can be introduced via a feeding system, and a discharge system, whereby a gasification product can be withdrawn from the reaction chamber. The apparatus further contains at least one further, i.e., a second, reaction chamber with a second feeding system, which is connected to the first reaction chamber via the discharge system.

HYDROGEN PRODUCTION SYSTEM AND POWER GENERATION SYSTEM

The amount of high-temperature steam to be supplied from outside equipment is reduced. A hydrogen production system (1) is provided which is equipped with: a reactor (3) in which a humidified process fluid sent from a humidifier (2) is reacted in the presence of a catalyst to convert the carbon monoxide contained in the process fluid into carbon dioxide; a second passage (B) through which the high-temperature process fluid that has been reacted in the reactor (3) flows; a circulation passage (C) through which excess water in the humidifier (2) is circulated; and a first heat exchanger (7) which is disposed in a position where the circulation passage (C) and the second passage (B) cross and in which heat exchange is conducted between the high-temperature process fluid that has been reacted in the reactor (3) and the fluid circulating through the circulation passage (C).

PROCESS AND APPARATUS FOR THE GENERATION OF PROCESS STEAM AND BOILER FEED WATER STEAM IN A HEATABLE REFORMING REACTOR FOR THE PRODUCTION OF SYNGAS

A process is described for the generation of process steam and boiler feed water steam in a heatable reforming reactor for the production of syngas. The process serves to exploit the sensible heat of a syngas produced from hydrocarbons and steam to obtain two types of steam, each being generated when heating and evaporating boiler feed water and process condensate, with the process also including a conversion of the carbon monoxide contained in the syngas, and with the process including optional heating of the boiler feed water by means of the flue gas obtained from the heating of the reforming reactor. The process allows exploiting the sensible heat of the syngas and the flue gas from the heating more efficiently, while avoiding the disadvantages of the flue gas heating on account of the varying amounts of heat available in the flue gas duct. An apparatus for carrying out this process is described.

HEAT EXCHANGE SYSTEM

The present invention relates to a heat exchange system comprising: - a single apparatus (N) having an area immersed in a fluid bath (N2) and a free space (N1) at the head in which a vapour phase is accumulated, - at least one interspace (P) open at both ends, situated inside said apparatus and completely immersed in the fluid bath, - one or more heat exchange surface (s) (6, 7, 8, 9, 10, 11), said system characterized in that it contains all the heat exchange surfaces in a single apparatus and said surfaces are completely immersed in the fluid bath and are fluidly connected to the hot and cold sources, external to said system, through flows of matter. At least one of the heat exchange surfaces (6, 7, 8) is situated inside the interspace and at least another surface (9, 10, 11) is situated in the space between said interspace and the walls of the apparatus.

OXIDATION PROCESS USING MICROCHANNEL TECHNOLOGY AND NOVEL CATALYST USEFUL IN SAME

A process is disclosed for converting a hydrocarbon reactant to CO and H2. The process comprises: (A) flowing a reactant composition comprising the hydrocarbon reactant and oxygen or a source of oxygen through a microchannel reactor in contact with a catalyst under reaction conditions to form the product. The product formed in step (A) may be converted to a product comprising CO2 and H2O in a microchannel reactor. A catalyst is disclosed which comprises a composition represented by the formula M1a M2b M3c Al d O x wherein: M1 is Rh, Ni, Pd, Pt, Ru, Co or a mixture of two or more thereof; M2 is Ce, Pr, Tb or a mixture of two or more thereof.

METHOD OF OPERATION OF PROCESS TO PRODUCE SYNGAS FROM CARBONACEOUS MATERIAL

A process is provided for producing syngas that is effective for use in downstream processes. The process for producing syngas includes operating a gasification apparatus in a start-up mode until the gasification apparatus and equipment downstream of the gasification apparatus are adequately warmed up to a first target temperature. Upon reaching a first target temperature, the process is then operated in a production mode to produce a second syngas with a higher CO/CO2 molar ratio. Operation in a start-up mode until reaching a first target temperature, provides a process that is effective for reducing fouling in downstream equipment and for providing a second syngas can be more effectively cooled and cleaned.

SYNGAS COOLER SYSTEM AND METHOD OF OPERATION

A process and system for cooling syngas provides effective syngas cooling and results in reduced levels of fouling in syngas cooling equipment. A process for cooling syngas includes blending syngas with cooled recycled syngas in an amount effective for providing a blended syngas with a temperature at an inlet of a syngas cooler of about 600°F to about 1400°F. The blended syngas changes direction of flow at least once prior to the inlet of the syngas cooler.

A SYSTEM AND A METHOD OF RECOVERING AND PROCESSING A HYDROCARBON MIXTURE FROM A SUBTERRANEAN FORMATION

The present invention relates to a method and system for recovering and processing a hydrocarbon mixture from a subterranean formation. The method comprises: (i) mobilising said hydrocarbon mixture; (ii) recovering said mobilised hydrocarbon mixture; (iii) deasphalting said recovered hydrocarbon mixture to produce deasphalted hydrocarbon and asphaltenes; (iv) gasifying said asphaltenes in a gasifier to generate hydrogen, steam and/or energy and CO2; (v) upgrading said deasphalted hydrocarbon by hydrogen addition to produce upgraded hydrocarbon; and (vi) adding a diluent to said upgraded hydrocarbon, wherein said method is at least partially self- sufficient in terms of hydrogen and diluent.

CONVERSION OF LIQUID HEAVY HYDROCARBON FEEDSTOCKS TO GASEOUS PRODUCTS

The present invention relates to processes and apparatuses for generating light olefins, methane and other higher-value gaseous hydrocarbons from "liquid" heavy hydrocarbon feedstocks.

HYDROGEN/SYNGAS GENERATOR

The present invention relates to a compact, concentric auto thermal hydrogen/ syngas generator for production of hydrogen/ syngas without any external heating. Further, the auto thermal hydrogen/ syngas generator of the present invention involves combination of reactions such as partial oxidation, steam reforming, dry reforming, auto thermal reforming, dry autothermal reforming, water gas shift, preferential oxidation or methanation that takes place without external heating, for converting air, steam and fuel into a reformate mainly containing CO, CO2, N2, CH4 and H2O which is subsequently converted to hydro gen/syn gas as a feed for fuel cell or syngas applications.

MICROCOMPONENT CHEMICAL PROCESS SHEET ARCHITECTURE

The invention is a microcomponent chemical process assembly wherein macroscale unit processes are performed by microscale components. The sheet architecture may be a single laminate with a plurality of separate microcomponent sections or the sheet architecture may be a plurality of laminates with one or more microcomponent sections on each laminate. Each microcomponent or plurality of like microcomponents perform at least one chemical process unit operation. A first laminate having a plurality of like first microcomponents is combined with at least a second laminate having a plurality of like second microcomponents thereby combining at least two unit operations to achieve a system operation.

MICROCHANNEL LAMINATED MASS EXCHANGER AND METHOD OF MAKING

The present invention is a microchannel mass exchanger (100) having a first plurality of inner thin sheets (106, 116, 200, 300) and a second plurality of outer thin sheets (110, 118, 204, 302, 504, 510). The inner thin sheets (106, 118, 200, 300) each have a solid margin (108) around a circumference, the solid margin (108) defining a slot (104, 508) through the inner thin sheet (106, 116, 200, 300) thickness. The outer thin sheets (110, 118, 204, 302, 504, 510) each have at least two header holes (112, 202) on opposite ends and when sandwiching an inner thin sheet (106, 116, 200, 300). The outer thin sheets (110, 118, 204, 302, 504, 510) further have a mass exchange medium (400, 500). The assembly forms a closed flow channel assembly wherein fluid enters through one of the header holes into the slot and exits through another of the header holes after contacting the mass exchange medium.

Procédé et dispositif pour le craquage thermique d'hydrocarbures

Verfahren zur Herstellung von Synthesegas für die Ammoniaksynthese

Procédé et dispositif pour la fabrication de gaz combustible

Procédé pour la fabrication de gaz combustible et appareillage pour la mise en oeuvre de ce procédé

PRODUCTION OF TECHNOLOGICAL OF GAS BY MEANS OF SECONDARY USE LOW TEMPERATURE OF REJECTED HEAT

METHOD OF SUPPRESSING CONTAMINATION METALS DEVICE FOR PRODUCTION OF SYNTHESIS GAS-

Method and System for Synthesizing Liquid Hydrocarbon Compounds

Provided is a method for synthesizing liquid hydrocarbon compounds wherein synthesizing liquid hydrocarbon compounds from a synthesis gas by a Fisher-Tropsch synthesis reaction. The method includes a first absorption step of absorbing a carbon dioxide gas, which is contained in gaseous by-products generated in the Fisher-Tropsch synthesis reaction, with an absorbent, and a second absorption step of absorbing a carbon dioxide gas, which is contained in the synthesis gas, with the absorbent which is passed through the first absorption step.

Co-production of fuels, chemicals and electric power using turbochargers

A method and system for co-production of electric power, fuel, and chemicals in which a synthesis gas at a first pressure is expanded using a turbo-expander, simultaneously producing electric power and an expanded synthesis gas at a second pressure after which the expanded synthesis gas is converted to a fuel and/or a chemical.

Hydrogen production by an autothermal heat exchanger packed-bed membrane gas reformer

A process for producing hydrogen from natural gas, said process comprises the steps of: (i) providing an autothermal heat exchanger packed-bed membrane reformer (APBMR) comprising: (a) an elongated external gas oxidation compartment comprising an inlet, an outlet and packed oxidation catalyst particles, said inlet and outlet being located each at one extremity of said external gas oxidation compartment; (b) an elongated internal gas steam-reforming compartment comprising an inlet, an outlet and packed steam-reforming catalyst particles, said inlet and outlet being located each at one extremity of said internal gas steam-reforming compartment; (c) one or more hydrogen-separating membrane(s) positioned in said steam-reforming compartment substantially parallel to the longitudinal axis of said steam-reforming compartment; (d) one insulation layer surrounding said external compartment; and, optionally, (e) one or more elongated internal gas oxidation compartment(s) positioned in said steamreforming compartment substantially parallel to the longitudinal axis of said gas steam-reforming internal compartment, and comprising an inlet, an outlet and packed oxidation catalyst particles, said inlet and outlet being located each at an extremity of said internal gas oxidation compartment(s); (ii) supplying a mixture comprising said natural gas and air to said gas oxidation compartment(s) of said reformer; and (iii) supplying a mixture comprising said natural gas and water to said gas steam-reforming compartment, wherein the water-to-gas molar ratio

Conversion of hydrocarbons to carbon dioxide and electrical power

A process for reducing CO 2 emissions from combined cycle power generation processes utilizing a gaseous hydrocarbon feed, which includes splitting the hydrocarbon feed into two portions; a first portion≦45% by volume of the feed and a larger portion≧55% by volume of the feed, feeding the first portion to an autothermal reforming process to generate a hydrogen-containing gas and a carbon dioxide stream, combining the hydrogen-containing stream with the second portion, combusting the resulting hydrogen-containing fuel stream with oxygen containing gas in a gas turbine to generate electrical power and passing the exhaust gas mixture from the gas turbine to a heat recovery steam generation system that feeds one or more steam turbines to generate additional electrical power. The captured carbon dioxide stream may be fed to storage or enhanced oil recovery processes. The process may be retrofitted into existing combined cycle processes.

Hydrogen/syngas generator

The present invention relates to a compact, concentric auto thermal hydrogen/syngas generator for production of hydrogen/syngas without any external heating. Further, the auto thermal hydrogen/syngas generator of the present invention involves combination of reactions such as partial oxidation, steam reforming, dry reforming, auto thermal reforming, dry autothermal reforming, water gas shift, preferential oxidation or methanation that takes place without external heating, for converting air, steam and fuel into a reformate mainly containing CO, CO 2 , N 2 , CH 4 and H 2 O which is subsequently converted to hydrogen/syngas as a feed for fuel cell or syngas applications.

Method and device for producing process vapor and boiler feed steam in a heatable reforming reactor for producing synthesis gas

A method for producing process vapor and boiler feed steam in a heatable reforming reactor for producing synthesis gas. The sensible heat of a synthesis gas produced from hydrocarbons and steam can be used so that two types of vapor are produced during the heating and evaporation of boiler feed water and process condensate. The method also includes a conversion of the carbon monoxide contained in the synthesis gas. The method includes an optional heating of the boiler feed water using the flue gas from the heating of the reforming reactor. The sensible heat of the synthesis gas and of the flue gas originating from the heating can be used more efficiently. The disadvantages from the flue gas heating, which are caused by the fluctuating heat supply in the flue gas duct, are avoided. A system for practicing the method is also disclosed.

HYDROGEN AUTOTHERMAL REFORMING PROCESS

A process for on-site hydrogen reforming is disclosed. The process includes providing a combined reformer heat exchanger component in which heated air, steam, and hydrocarbon fuel react to form process gas containing hydrogen, and the process gas is cooled via the heat exchanger. The combined components enable reductions in size, materials, costs, and heat loss. Additionally, as the heat exchanger side of the component operates at a cooler temperature, an uninsulated flange for access to the catalyst chamber can be used. A combined combustion heat exchanger component is also provided with similar advantages. Process gas is processed, and hydrogen gas is produced via a purification process. 1. A hydrogen reforming process comprising the steps of:providing a combined reformer heat exchanger component having a first chamber adapted to enable a reforming reaction and a second chamber adapted to house a first heat exchanger,inputting fuel into said first chamber of said reformer heat exchanger component,inputting heated air and steam into said first chamber of said reformer heat exchanger component,enabling a reforming reaction to produce a process gas containing hydrogen in said first chamber of said reformer heat exchanger component,feeding said process gas into said second chamber of said reformer heat exchanger component,cooling said process gas in said second chamber of said reformer heat exchanger component and allowing said process gas to leave said reformer heat exchanger component at a heat exchanger exit,further cooling said process gas after it leaves said reformer heat exchanger component, andpurifying said process gas and producing a hydrogen product.2. The method according to claim 1 , further comprising the step of:providing a catalyst section having at least one catalyst element within said first chamber of said reformer heat exchanger component to assist in the reforming reaction.3. The method according to claim 2 , further comprising the step of: ...

Steam methane reformer system and method of performing a steam methane reforming process

An apparatus includes a furnace having at least one bayonet reforming tube. The furnace is adapted to receive a gas including a hydrocarbon and at least one of steam and carbon dioxide via the bayonet reforming tube, heat and catalytically react the gas to form syngas at a first temperature, cool the syngas to a second temperature lower than the first temperature, and eject the syngas from the tube. The furnace has a first effluent stream including flue gas and a second effluent stream including syngas. The apparatus also includes a first heat recovery section adapted to transfer heat from the first effluent stream to a first heat load including one of air, water, and steam, and a second heat recovery section adapted to transfer heat from the second effluent stream to a second heat load.

PRODUCTION OF HYDROCARBON LIQUIDS

A process to efficiently convert organic feedstock material into liquid non-oxygenated hydrocarbons in the Cto Ccarbon skeleton range is disclosed. The process can utilize gaseous, liquid or solid organic feedstocks containing carbon, hydrogen and, optionally, oxygen. The feedstock may require preparation of the organic feedstock for the process and is converted first into a synthesis gas containing carbon monoxide and hydrogen. The synthesis gas is then cleaned and conditioned and extraneous components removed, leaving substantially only the carbon monoxide and hydrogen. It is then converted via a series of chemical reactions into the desired liquid hydrocarbons. The hydrocarbons are suitable for combustion in a vehicle engine and may be regarded a replacement for petrol made from fossil fuels in the Cto Ccarbon backbone range. The process also recycles gaseous by-products back through the various reactors of the process to maximize the liquid hydrocarbon in the Cto Ccarbon skeleton range yield. 1. A process for producing a Cto Chydrocarbon fuel from organic material , comprising:a) applying a heat source to heat an organic feedstock and oxygen at substoichiometric conditions to a temperature sufficient for partial combustion of said organic feedstock to occur and then ceasing application of said heat source once partial combustion has commenced;b) partially combusting said organic feedstock so as to produce a synthesis gas stream, said synthesis gas stream containing at least carbon monoxide, carbon dioxide and hydrogen;{'sub': '10', 'c) substantially removing unwanted solid and liquid matter comprising oxides, ash and hydrocarbons having a carbon skeleton of greater than Cfrom said synthesis gas stream to produce a first cleaned synthesis gas stream containing at least carbon monoxide, carbon dioxide and hydrogen;'}d) compressing said first cleaned synthesis gas stream and substantially removing water;e) conditioning and further cleaning the first cleaned ...

System for generating power from a syngas fermentation process

A system and process is provided for generating power from a syngas fermentation process. The process includes contacting hot syngas having a temperature above about 1400° F. with cooled syngas to produce a pre-cooled syngas having a temperature of 1400° F. or less at an inlet of a waste heat boiler. A waste heat boiler receives the pre-cooled syngas and is effective for producing waste heat boiler high pressure steam and a cooled syngas.

METHOD AND ARRANGEMENT FOR HEAT ENERGY RECOVERY IN SYSTEMS COMPRISING AT LEAST ONE REFORMER

A method of heat energy recovery in installations including at least one reformer, wherein, for the purpose of heat energy recovery, process condensate is preheated and/or evaporated on a cooling section of the installation by heat exchange with gas generated in the installation, in particular synthesis gas, wherein, prior to being preheated in a flue gas duct of the installation, combustion air is preheated by heat exchange by means of boiler feed water. The invention also relates to a heat energy recovery system for the implementation of the method. 115-. (canceled)16. A method for heat energy recovery in an installation , comprising:at least one reformer in a synthesis gas installation having steam reforming means, combustion air for the reformer,', 'boiler feed water for steam generation,', 'process condensate on a cooling section of the installation, and', 'flue gas from the reformer;, 'wherein at least the following process streams of the installation are interconnectedthe method comprising:a) at least partially evaporating the process condensate on the cooling section;b) recovering heat energy from the flue gas discharged through a flue gas duct;c) conducting the combustion air through the flue gas duct prior to being supplied to the reformer for recovery of the heat energy;d) one or both of preheating and evaporating the process condensate on the cooling section for the purpose of heat energy recovery by heat exchange with synthesis gas generated in the installation, ande) preheating the combustion air by heat exchange by means of the boiler feed water prior to being preheated in the flue gas duct.17. The method of claim 16 , wherein heat transfer from the boiler feed water to the combustion air is realized in that the boiler feed water and the combustion air are conducted through at least one external air preheater arranged externally with respect to the flue gas duct claim 16 , before the boiler feed water is conducted to the flue gas duct.18. The method ...

Method for hydrogen production

The present invention relates to a method for hydrogen production and to a method of hydrogen and/or carbon dioxide production from syngas. The method comprises the steps of: (i) providing a gas stream comprising hydrogen and carbon monoxide, (ii) separating at least part of hydrogen from the stream yielding a hydrogen-depleted stream, (iii) subjecting the hydrogen-depleted stream to a water-gas shift reaction, and (iv) separating hydrogen from the stream resulting from step (iii). The method according to the invention improves the conversion of carbon monoxide in the water gas shift reaction and allows to increase the hydrogen production by 10-15% and to increase the overall energy efficiency of the system by 5-7%. The invention further relates to a plant for hydrogen and/or carbon dioxide production suitable for the method of the invention.

Systems And Methods For Producing Substitute Natural Gas

Systems and methods for producing synthetic gas are provided. The method can include gasifying a carbonaceous feedstock in the presence of an oxidant within a gasifier to provide a raw syngas. The raw syngas can be cooled within a cooler to provide a cooled syngas. The cooled syngas can be processed within a purification system to provide a treated syngas. The purification system can include a saturator adapted to increase a moisture content of the cooled syngas. The treated syngas and a first heat transfer medium can be introduced to a methanator to provide a synthetic gas, a second heat transfer medium, and a methanation condensate. At least a portion of the methanation condensate can be recycled from the methanator to the saturator.

PROCESS COMPRISING EXOTHERMAL CATALYTIC REACTION OF A SYNTHESIS GAS AND RELATED PLANT

A synthesis process comprising steam reforming a gaseous hydrocarbon feedstock (); exothermically reacting the resulting synthesis gas; removing heat from said exothermal reaction by producing steam (); using said steam as heat input to the steam reforming, wherein the steam reforming comprises: a) forming a mixture () containing steam and hydrocarbons by at least the step of adding a first stream of water () to the hydrocarbon feedstock (); b) heating said mixture () by indirect heat exchange with synthesis gas; c) reforming said mixture after said heating step b). 115-. (canceled)16. A synthesis process , comprising:steam reforming a gaseous hydrocarbon feedstock, thereby obtaining a synthesis gas;exothermically reacting said synthesis gas in the presence of a catalyst, thereby obtaining a synthesis product;removing heat from said exothermal reaction by producing steam, wherein at least part of said steam provides a heat input to the reforming of said hydrocarbon feedstock; a) forming a mixture containing steam and hydrocarbons by at least a step of adding a first stream of water to the hydrocarbon feedstock in a saturating tower, said stream of water being pre-heated by indirect heat exchange, prior to admission into said tower, with at least a portion of the steam produced by removing heat from the exothermal synthesis reaction;', 'b) heating said mixture by indirect heat exchange with at least part of said synthesis gas; and', 'c) reforming said mixture after said heating step b)., 'wherein the steam reforming of the hydrocarbon feedstock includes17. The synthesis process of claim 16 , wherein the formation of said mixture further includes mixing an effluent of said tower with a second stream of water claim 16 , and said second stream is pre-heated by indirect heat exchange with said synthesis gas.18. The synthesis process of claim 17 , wherein a stream of synthesis gas transfers heat to said mixture during the heating step b) claim 17 , and the synthesis gas ...

GENERATING METHANOL USING ULTRAPURE, HIGH PRESSURE HYDROGEN

In various implementations, methanol is produced using a (CO+H) containing synthesis gas produced from a combined PDX plus EHTR or a combined ATR plus EHTR at a pressure of 70 bar to 100 bar at the correct stoichiometric composition for methanol synthesis so that no feed gas compressor is required for the feed to the methanol synthesis reactor loop. 1. A method for producing methanol , comprising;producing oxygen in an air separation plant with air compressors driven by a gas turbine;heating a hydrocarbon feed stream using exhaust from the gas turbine;exothermically reacting a first portion of the heated hydrocarbon feed stream with at least one of steam or an oxidant gas comprising molecular oxygen to produce an exothermically generated syngas product;endothermically reforming a second portion of the hydrocarbon feed stream with steam over a catalyst in a heat exchange reformer to produce an endothermically-reformed syngas product, wherein at least a portion of heat used in generation of the endothermically-reformed syngas product is obtained by recovering heat from the exothermically-generated syngas product and the endothermically reformed syngas product;combining the exothermically generated syngas product and the endothermically-reformed syngas product to produce a combined syngas stream;producing steam in a waste heat boiler by cooling the combined syngas stream;separating water from the cooled combined syngas to produce a methanol plant feed at substantially reaction loop pressure;after separating water, passing the cooled combined syngas to a methanol plant; andcombining methanol plant combustible effluent with methane fuel to the gas turbine.2. The method of claim 1 , wherein the exothermically-generated syngas product is generated using a partial oxidation burner followed by a catalytic reforming section in a convectively heated steam plus hydrocarbon reformer.3. The method of claim 1 , wherein the hydrocarbon feed stream includes methane.4. The method of ...

Method and system for producing hydrogen using an oxygen transport membrane based reforming system

The synthesis gas product is further treated in a separate high temperature water gas shift reactor and optionally in a separate low temperature water gas shift reactor. Hydrogen is produced from the resulting hydrogen-enriched gas using hydrogen PSA. A distinctive feature of this OTM configuration is that no portion of the syngas is fed to the OTM reactor, which allows reforming to be conducted in the reforming reactors at much higher pressures. The synthesis gas stream is directed to the water gas shift (WGS) reactor where H2/CO ratio increases from about 4.7 to about 21. Since the WGS reaction is exothermic, the shifted syngas leaves the reactor at a higher temperature, typically about 410° C. This shifted syngas is used to heat the NG feedstock in the NG heater to about 370° C., and then used to preheat boiler feed water (BFW). Syngas leaving the BFW heater is at about 175° C. It is cooled down to about 40° C. in a syngas cooler fed by cooling water. The cooled syngas then enters a knock-out drum where water is removed from the bottoms as process condensate and recycled for use within the process.

Rsc external downcomer tube arrangement

A system includes a radiant syngas cooler which receives and cools syngas generated in a gasifier. The radiant syngas cooler includes an outer shell of the radiant syngas cooler defining an annular space of the radiant syngas cooler and a heat exchange tube of the radiant syngas cooler positioned within the annular space and configured to flow a cooling medium. The heat exchange tube is configured to enable heat exchange between the syngas and the cooling medium to cool the syngas. The radiant syngas cooler includes a downcomer tube of the radiant syngas cooler which supplies the cooling medium to the heat exchange tube, where the downcomer tube includes a downflow portion positioned outside of the annular space of the radiant syngas cooler. The downflow portion is fluidly coupled to a header, and the header fluidly couples the downcomer tube to the heat exchange tube.

Process and plant for producing hydrogen by steam reforming and high-temperature electrolysis

The invention relates to a process and a plant for producing hydrogen by steam reforming and high-temperature electrolysis. Steam reforming produces a synthesis gas from a carbon-containing starting material and steam. Process heat generated in the context of the steam reforming is utilized for producing steam from water. Thus-produced steam is utilized as reactant for producing an electrolysis product in a high-temperature electrolysis step, wherein the electrolysis product includes at least hydrogen and oxygen. Hydrogen is separated from the synthesis gas produced by steam reforming and from the electrolysis product produced by high-temperature electrolysis.

Steam-Producing Process and System

System and process for producing steam in a steam-hydrocarbon reforming facility where oxygen is removed from demineralized water using a membrane degasifier. The membrane degasifier operates at a lower temperature compared to a deaerator, which is the conventional technology for removing oxygen. 1. A process for producing steam in a steam-hydrocarbon reforming facility , the process comprising:cooling a reformate containing water in an amount effective to condense at least a portion of the water in the reformate and thereby forming condensed water and water-depleted reformate;separating the condensed water from the water-depleted reformate in a separator thereby forming a water-depleted reformate gas and a process condensate, the process condensate formed from the condensed water;{'sub': 2', '2, 'passing the process condensate to a steam stripping unit, stripping at least COfrom the process condensate, and withdrawing a CO-depleted process condensate from the steam stripping unit;'}{'sub': '2', 'passing the CO-depleted process condensate to a steam drum to produce a product steam;'}{'sub': 2', '2, 'passing demineralized make-up water to a membrane separation unit to remove at least Ofrom the demineralized make-up water to form an O-depleted demineralized make-up water; and'}{'sub': '2', 'passing a first portion or all of the O-depleted demineralized make-up water to the steam drum to produce the product steam;'}{'sub': 2', '2, 'wherein the CO-depleted process condensate and the O-depleted demineralized make-up water are each heated by indirect heat exchange with reformate prior to being introduced into the steam drum.'}2. The process as claimed in wherein not all of the O-depleted demineralized make-up water is passed to the steam drum claim 1 , the process further comprising:{'sub': '2', 'passing a second portion of the O-depleted demineralized make-up water to a second steam drum to produce a second product steam.'}3. The process as claimed in wherein at least a ...

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.

PROCESS AND PLANT FOR THE PRODUCTION OF SYNTHESIS GAS BY MEANS OF CATALYTIC STEAM REFORMATION OF A HYDROCARBONACEOUS FEED GAS

A plant for producing a synthesis gas chiefly consisting of hydrogen and carbon monoxide by catalytic steam reformation of a hydrocarbonaceous feed gas, wherein the heat of burners required for the chemical reforming reactions to take place is generated by producing a flue gas and wherein, by utilizing the heat contained in the synthesis gas and in the flue gas, a pure steam is generated from boiler feed water and a process steam is generated from process condensate, wherein for the generation of the pure steam synthesis gas and flue gas are used and for the generation of the process steam a part of the pure steam is used as heat-transfer medium and the remaining part of the pure steam is discharged from the process as export steam. 1. A plant for producing a synthesis gas consisting essentially of hydrogen and carbon monoxide by catalytic steam reformation of a hydrocarbonaceous feed gas , the plant comprising:at least one tubular furnace configured to carry out the catalytic steam reformation, wherein the at least one tubular furnace comprises burners that are configured to provide heat for the catalytic steam reformation;a degassing boiler configured for the thermal degasification of boiler feed water;a steam boiler configured to generate pure steam from boiler feed water, wherein the steam boiler comprises a first heat exchanger and a second heat exchanger, wherein the first heat exchanger is configured to heat and evaporate the boiler feed water using heat from the syntheses gas, wherein the second heat exchanger is configured to heat and evaporate the boiler feed water using heat from the flue gas;a splitter in fluid communication with the steam boiler and configured to receive the pure steam from the steam boiler;a first steam line in fluid communication with the splitter configured to receive a first pure steam;an export steam line in fluid communication with the splitter that is configured to receive a second pure steam;a condensate separator configured for ...

PROCESS AND PLANT FOR THE PRODUCTION OF SYNTHESIS GAS BY MEANS OF CATALYTIC STEAM REFORMATION OF A HYDROCARBONACEOUS FEED GAS

A process and plant for producing a synthesis gas chiefly consisting of hydrogen and carbon monoxide by catalytic steam reformation of a hydrocarbonaceous feed gas, wherein the heat of burners required for the chemical reforming reactions to take place is generated by producing a flue gas and wherein, by utilizing the heat contained in the synthesis gas and in the flue gas, a pure steam is generated from boiler feed water and a process steam is generated from process condensate, wherein for the generation of the pure steam synthesis gas and flue gas are used and for the generation of the process steam a part of the pure steam is used as heat-transfer medium and the remaining part of the pure steam is discharged from the process as export steam. 16-. (canceled)7. A process for producing a synthesis gas consisting essentially of hydrogen and carbon monoxide by catalytic steam reformation of a hydrocarbonaceous feed gas , wherein the heat of burners required for the chemical reforming reactions to take place is generated by producing a flue gas and wherein , by utilizing the heat contained in the synthesis gas and in the flue gas , a pure steam is generated from boiler feed water and a process steam is generated from process condensate , wherein for the generation of the pure steam synthesis gas and flue gas are used and for the generation of the process steam a part of the pure steam is used as heat-transfer medium and the remaining part of the pure steam is discharged from the process as export steam.8. The process according to claim 7 , wherein the respective pressures of that part of the pure steam which is used as heat-transfer medium for the generation of process steam and that part which is discharged from the process as export steam are adjusted independent of each other.9. A plant for carrying out the process according to claim 7 , the plant comprising:at least one tubular furnace for carrying out the catalytic steam reformation;a boiler for the thermal ...

PROCESS AND PLANT FOR PRODUCING HYDROGEN BY MEANS OF CATALYTIC STEAM REFORMATION OF A HYDROCARBONACEOUS FEED GAS

Plant and process for the generation of hydrogen from a hydrocarbonaceous feed gas and steam by means of catalytic steam reformation, wherein the heat of the synthesis gas and the flue gas is utilized for generating export steam from boiler feed water and process steam from the condensate separated from the synthesis gas, and wherein the gases expelled from the boiler feed water during its degasification and the vapors obtained during the depressurization of the elutriation waters of the steam boilers for the generation of export and process steam are used for preheating the fuel gas for operation of the burners of the steam reformer. 112-. (canceled)13. A process for producing hydrogen from a hydrocarbonaceous feed gas and steam , the process comprising the following process steps:a) conversion of a hydrocarbonaceous feed gas by steam reformation into a synthesis gas chiefly consisting of hydrogen and carbon monoxide, wherein process steam is used for the steam reformation and wherein the reformation is carried out in a reformer furnace which is equipped with reformer tubes filled with catalyst and burners heating the same, which are operated with process-internally produced fuel gas and/or hydrocarbonaceous feed gas and with an oxygen-containing feed gas, wherein a flue gas is produced;b) cooling of the synthesis gas produced in part a) to a temperature which is suitable for the treatment of the synthesis gas for the separation of hydrogen by the PSA (pressure swing adsorption) process, wherein cooling of the synthesis gas comprises its use as heat-transfer medium for generating export steam and/or process steam and/or for the thermal degasification of boiler feed water by forming aqueous condensate in the synthesis gas, wherein the generation of export steam and/or process steam and/or the thermal degasification of boiler feed water is carried out in containers from which vent streams and/or elutriation streams are discharged; andc) separation of the hydrogen ...

Process and system for converting waste to energy without burning

This invention relates to a power recovery process in waste steam/CO 2 reformers whereby a waste stream can be made to release energy without having to burn the waste or the syngas. This invention does not make use of fuel cells as its critical component but makes use of highly exothermic chemical reactors using syngas to produce large amounts of heat, such as Fischer-Tropsch. It also relates to control or elimination of the emissions of greenhouse gases in the power recovery process of this invention with the goal of producing energy in the future carbonless world economy. A New Concept for a duplex kiln was developed that has the combined functionality of steam/CO 2 reforming, heat transfer, solids removal, filtration, and heat recovery. New methods of carbon-sequestering where the syngas produced by steam/CO 2 reforming can be used in Fischer-Tropsch processes that make high-carbon content compounds while recycling the methane and lighter hydrocarbons back to the reformer to further produce syngas at a higher H 2 /CO ratio.

Method for producing acetylene and syngas

A process for producing acetylene and syngas by partial oxidation of hydrocarbons with oxygen, involving: separately preheating a hydrocarbon and a oxygen-comprising input stream; mixing in a mass flow ratio of the oxygen-comprising to hydrocarbon stream at an oxygen number no more than 0.31; feeding the streams via a burner block to a combustion chamber and therein partially oxidizing the hydrocarbon(s) to a cracking gas; quenching the cracking gas to 80 to 90° C. downstream by injecting an aqueous quench medium to obtain a process water stream-1 and a product gas stream-2; cooling the product gas stream-2 in a cooling column by direct heat exchange with cooling water to obtain a process water stream-2 as bottoms, a product gas stream-2 as uppers, and a sidestream; and depleting the sidestream of soot in an electrofilter to generate therein a process water stream-3 combined with water streams-1/2 to afford the process water stream-4.

REACTOR FOR PARTIAL OXIDATION OF HYDROCARBON GASES

This disclosure is related to reactor for partial oxidation of hydrocarbonaceous feedstock. The reactor comprises outer shell with reaction products outlet device with at least one device for inlet of feedstock or feedstock components into the catalyst sleeve placed within the reactor with a gap between the outer shell filled with a catalyst and comprising means of product outlet from its lower part. This catalyst sleeve is furnished with a jacket in contact with at least a part of the cylindrical wall of the catalyst sleeve having open-end holes in the point of contact with jacket, and the reactor is equipped with a means of inlet of a cooling agent into the jacket that cools the catalyst sleeve. Technical result of claimed invention is reduction of catalyst sleeve wall temperature to 1000° C. or lower and reduction of catalyst sleeve material corrosion. 1. A reactor for partial oxidation of hydrocarbonaceous feedstock comprising a pressure vessel with a means of outlet of reaction products and at least one means of inlet of feedstock , or feedstock components , into the placed within the reactor with a gap catalyst sleeve filled in with a catalyst and comprising means of product outlet in its lower part and differing in that the catalyst sleeve is furnished with a jacket adjacent to at least a part of the cylindrical wall of the catalyst sleeve , which is made with open-end holes in the adjacency zone of the jacket , and the reactor is equipped with a means of inlet into the jacket of a cooling agent that cools the catalyst sleeve and then enters into the catalyst sleeve through the holes in its wall.2. The reactor according to claim 1 , wherein the cooling agent comprises water steam claim 1 , synthesis gas or their admixture.3. The reactor according to claim 1 , wherein a gap between the catalyst sleeve jacket and the reactor pressure vessel is filled in with a heat-insulating material.4. The reactor according to claim 1 , further comprising a cooling chamber ...

Method and system for producing methanol using partial oxidation

A method and system for producing methanol that employs steam methane reforming (SMR) and/or autothermal (ATR) synthesis gas production system, together with a partial oxidation system, is disclosed. The dual mode system and method for producing the synthesis gas in a methanol production process optimizes the efficiency and productivity of the methanol plant by using the partial oxidation based reforming system as an independent source of synthesis gas. The disclosed methods and systems are configurable either as a retrofit to existing methanol production facilities or as an integrated package into newly constructed methanol production facilities.

Natural Gas Reactors and Methods

A method of producing heat for industrial purposes such as power generation can use at least one, if not two exothermic reactions. First, methane may be produced from carbon dioxide and hydrogen in a reactor. This reaction produces heat. The methane may be burned, or oxidized (which is also an exothermic reaction) to produce carbon dioxide and hydrogen. Oxygen and/or hydrogen may supplement the process as could be produced from the electrolysis of water. Carbon dioxide may be obtained from a variety of sources. 1. A method of heat generation and producing methane comprising the steps of:(a) providing hydrogen and carbon dioxide to a reactor;(b) exothermically reacting the hydrogen and carbon dioxide in the reactor to form methane, water and heat;(c) separating the methane from the water; and (i) using the heat from the reactor for an industrial process selected from the group of generating power in a turbine and heating;', '(ii) burning the methane for an industrial process selected from the group of generating power in a turbine and heating; and', '(iii) oxidizing the methane of step (b) in an exothermic reaction to produce at least carbon dioxide and hydrogen, at least one of which is used to repeat step (a) above, and heat, said heat used for an industrial process selected from the group of generating power in a turbine and heating., '(d) at least one of the following steps2. The method of wherein step (d)(iii) is performed and the oxidation step further produces carbon monoxide and water claim 1 , with at least one of the carbon dioxide and hydrogen separated from the carbon monoxide.3. The method of wherein step (d)(iii) is performed and both the carbon dioxide and hydrogen are used to repeat step (a).4. The method of wherein step (d)(iii) is performed and both the carbon dioxide and hydrogen are used to repeat step (a).5. The method of further comprising a heat exchanger receiving output of the reactor claim 3 , said heat exchanger used for an industrial ...

PROCESSES FOR PRODUCING HYDROGEN GAS STREAM FROM AN OFFGAS STREAM

Processes for producing a recycle hydrogen gas stream from an offgas separated from a reaction zone effluent. The reaction zone may receive a renewable feedstock and produce an effluent with gaseous components of hydrogen and light hydrocarbons. The offgas may be compressed, pass through hydrogen sulfide removal and then be sent to a reforming unit, such as a steam reformer. The steam reformer will generate additional hydrogen which can be recycled back to the reaction zone. 1. A process for producing a hydrogen rich gas stream , the process comprising:compressing a hydrogen containing gas separated from a reaction zone in a two stage compressor system, the hydrogen containing gas including light hydrocarbons and carbon oxides;removing hydrogen sulfide from the compressed gas in a hydrogen sulfide removal zone to provide a lean compressed gas;reforming the light hydrocarbons in the lean gas in a reforming zone to provide a hydrogen rich gas, the hydrogen rich gas including carbon oxides; and,returning the hydrogen rich gas to the reaction zone.2. The process of wherein the hydrogen sulfide (removal zone comprises at least one vessel comprising an adsorbent.3. The process of wherein the adsorbent comprises zinc oxide.4. The process of wherein the hydrogen sulfide removal zone comprises at least two vessels comprising a zinc oxide adsorbent claim 3 , the at least two vessels being arranged in a lead-lag configuration.5. The process of wherein the reforming zone comprises reforming with steam.6. The process of further comprising:heating the compressed gas with the hydrogen rich gas.7. The process of further comprising:heating the lean compressed gas with the hydrogen rich gas.8. The process of further comprising:removing carbon oxides from the hydrogen rich gas in the reaction zone.9. The process of wherein the reaction zone includes a deoxygenation zone for converting a renewable feedstock into hydrocarbons.10. A process for lowering a hydrogen demand of a user claim ...

Process for reforming hydrocarbons

The invention relates to the production of synthesis gas by means of particularly a series arrangement of heat exchange reforming and autothermal reforming stages, in which the heat required for the reforming reactions in the heat exchange reforming stage, is provided by hot effluent synthesis gas from the autothermal reforming stage. More particularly, the invention relates to optimisation of the operation and control of an arrangement of heat exchange reforming and autothermal reforming stages and introduction of an additional waste heat boiler.

METHOD FOR TREATING A SYNTHESIS GAS STREAM

A process can be used to treat a synthesis gas stream comprising steam reforming firstly in a primary reformer and subsequently in a secondary reformer. Crude synthesis gas exiting the secondary reformer may be cooled in a steam generator and then further cooled in a steam superheater. The crude synthesis gas stream after exiting the secondary reformer may be split into at least two gas substreams, of which only a first gas substream is fed to the steam generator. A second gas substream may be supplied to the steam superheater, bypassing the steam generator. Only the first gas substream, after flowing through the steam generator, may be subjected to a CO conversion reaction in a first CO conversion reactor before the first gas substream is supplied to the steam superheater. 111.-. (canceled)12. A process for treating a synthesis gas stream comprising steam reforming firstly in a primary reformer and subsequently in a secondary reformer , the process comprising:splitting a crude synthesis gas stream that exits the secondary reformer into a first gas substream and a second gas substream;feeding the first gas substream to a steam generator;cooling the first gas substream in the steam generator;supplying the second gas substream to a steam superheater so as to bypass the steam generator;cooling the second gas substream in the steam superheater;subjecting only the first gas substream to a CO conversion reaction in a first CO conversion reactor after the first gas substream passes through the steam generator; andsupplying the first gas substream to the steam superheater after the first gas substream passes through the first CO conversion reactor.13. The process of comprising recombining the first and second gas substreams after the first gas substream exits the first CO conversion reactor.14. The process of comprising supplying a partially-converted crude synthesis gas stream claim 13 , which is formed by recombining the first gas substream and the second gas substream ...

Optimized FT synthesis by reforming and recycling tail gas from FT synthesis

Det blir beskrevet en fremgangsmåte for omdanning av naturgass eller andre fossile brensler til høyere hydrokarboner, omfattende de følgende trinn: a) reagere naturgass med damp og oksygeninneholdende gass i minst en reformeringssone for å produsere en syntesegass som hovedsakelig består av Hog CO i tillegg til noe CO; b) lede nevnte syntesegass til en Fischer-Tropsch-reaktor for å produsere en rå syntesestrøm bestående av lettere hydrokarboner, tyngre hydrokarboner, vann samt uomsatt syntesegass; c) . separere nevnte rå syntesestrøm i en gjennvinningssone, i en råproduktststrøm hovedsakelig inneholdende tyngre hydrokarboner, en vannstrøm og en tail-gass-strøm hovedsakelig inneholdende de øvrige bestanddelene;som er kjennetegnet ved at fremgangsmåten også omfatter de følgende trinn; d) dampreformere minst en del av tail-gassen i en separat dampreformer; e) lede den reformerte tail-gassen inn i gass-strømmen før denne ledes inn i Fischer-Tropsch-reaktoren. A process for converting natural gas or other fossil fuels to higher hydrocarbons is described, comprising the following steps: a) reacting natural gas with steam and oxygen-containing gas in at least one reforming zone to produce a synthesis gas consisting mainly of Hog CO in addition to some CO; b) passing said synthesis gas to a Fischer-Tropsch reactor to produce a crude synthesis stream consisting of lighter hydrocarbons, heavier hydrocarbons, water and unreacted synthesis gas; c). separating said crude synthesis stream in a recovery zone, in a crude product stream mainly containing heavier hydrocarbons, a water stream and a tail gas stream mainly containing the other constituents, which is characterized in that the process also comprises the following steps; d) steam reformers at least a part of the tail gas in a separate steam reformer; e) passing the reformed tail gas into the gas stream before passing it into the Fischer-Tropsch reactor.

Four-Train Catalytic Gasification Systems

Systems to convert a carbonaceous feedstock into a plurality of gaseous products are described. The systems include, among other units, four separate gasification reactors for the gasification of a carbonaceous feedstock in the presence of an alkali metal catalyst into the plurality of gaseous products including at least methane. Each of the gasification reactors may be supplied with the feedstock from a single or separate catalyst loading and/or feedstock preparation unit operations. Similarly, the hot gas streams from each gasification reactor may be purified via their combination at a heat exchanger, acid gas removal, or methane removal unit operations. Product purification may comprise trace contaminant removal units, ammonia removal and recovery units, and sour shift units.

Processes for hydromethanation of a carbonaceous feedstock

The present invention relates to processes for preparing gaseous products, and in particular a hydrogen product stream and optionally a methane product stream, via the hydromethanation of carbonaceous feedstocks in the presence of steam, carbon monoxide, hydrogen and a hydromethanation catalyst.

Integrated hydromethanation combined cycle process

The present invention relates to an integrated process for preparing combustible gaseous products via the hydromethanation of carbonaceous feedstocks in the presence of steam, carbon monoxide, hydrogen, a hydromethanation catalyst and optionally oxygen, and generating electrical power from those combustible gaseous products as well as a hydrogen and/or methane by-product stream.

Two-mode process for hydrogen production

The present invention relates to a 2-mode processes for preparing gaseous products, and in particular a hydrogen product stream, via the hydromethanation of carbonaceous feedstocks in the presence of steam, carbon monoxide, hydrogen and a hydromethanation catalyst in a first mode, and a partial oxidation of methane in a second mode.

Integrated enhanced oil recovery process

The present invention relates to an enhanced oil recovery process that is integrated with a synthesis gas generation process, such as gasification or methane reforming, involving combined capture and recycle of carbon dioxide from both processes.

Integrated enhanced oil recovery process

The present invention relates to an enhanced oil recovery process that is integrated with a synthesis gas generation process, such as gasification or reforming, and an air separation process for generating (i) an oxygen stream for use, for example, in the syngas process or a combustion process, and (ii) a nitrogen stream for EOR use.

Optimum integration of fischer-tropsch synthesis and syngas production

A method is described for conversion of natural gas or other fossil fuels to higher hydrocarbons, comprising the following steps: a) reaction of natural gas with steam and oxygenic gas in at least one reforming zone in order to produce a synthesis gas consisting primarily of H2 and CO, in addition to some CO2; b) passing said synthesis gas to a Fischer-Tropsch reactor in order to produce a crude synthesis stream consisting of lower hydrocarbons, water and non-converted synthesis gas; c) separation of said crude synthesis stream in a recovery zone, into a crude product stream mainly containing heavier hydrocarbons, a water stream and a tail gas stream mainly containing the remaining constituents; which is characterised in that the method also comprises the following steps; d) steam reformation of at least part of the tail gas in a separate steam reformer; e) introduction of the reformed tail gas into the gas stream before this is led into the Fischer-Tropsch reactor.

Optimized FT synthesis by reforming and recycling tail gas from FT synthesis

process for the conversion of natural gas or other fossil fuels to higher hydrocarbons.

费－托合成与合成气生产的最佳整合

本发明公开了将天然气或其它矿物燃料转化为高级烃的方法，包括以下步骤：a)在至少一个重整区中使天然气与蒸汽和含氧气体反应，以制备主要由H 2 和CO以及一些CO 2 组成的合成气；b)将所述合成气引入费-托反应器，以制备由低级烃、水和未转化的合成气组成的粗合成物流；c)在回收区中将所述粗合成物流分离为主要含有高级烃的粗产物流、水物流和主要含有残余组分的尾气物流；其特征在于该方法还包括以下步骤：d)在独立的蒸汽重整器中将至少部分尾气蒸汽重整；e)在将重整后的尾气引入费-托反应器之前，将其加入气体物流中。

Method for natural gas conversion to high hydrocarbons

FIELD: hydrocarbon manufacturing. SUBSTANCE: natural gas is brought into reaction with vapor and oxygen-containing gas in at least one reforming zone to produce syngas mainly containing hydrogen and carbon monoxide and some amount of carbon dioxide. Said gas is fed in Fisher-Tropsh synthesis reactor to obtain crude synthesis stream containing low hydrocarbons, high hydrocarbons, water, and unconverted syngas. Then said crude synthesis stream is separated in drawing zone onto crude product stream containing as main component high hydrocarbons, water stream, and exhaust gas stream, comprising mainly remained components. Further at least part of exhaust gas stream is vapor reformed in separated vapor reforming apparatus, and reformed exhaust gas is charged into gas stream before its introducing in Fisher-Tropsh synthesis reactor. EFFECT: increased hydrocarbon yield with slight releasing of carbon dioxide. 7 cl, 3 dwg, 1 tbl, 5 ex ÐÎÑÑÈÉÑÊÀß ÔÅÄÅÐÀÖÈß (19) RU (51) ÌÏÊ 7 (11) (13) 2 247 701 C2 C 07 C 1/04, C 10 G 2/00 ÔÅÄÅÐÀËÜÍÀß ÑËÓÆÁÀ ÏÎ ÈÍÒÅËËÅÊÒÓÀËÜÍÎÉ ÑÎÁÑÒÂÅÍÍÎÑÒÈ, ÏÀÒÅÍÒÀÌ È ÒÎÂÀÐÍÛÌ ÇÍÀÊÀÌ (12) ÎÏÈÑÀÍÈÅ ÈÇÎÁÐÅÒÅÍÈß Ê ÏÀÒÅÍÒÓ (21), (22) Çà âêà: 2002118218/04, 01.12.2000 (24) Äàòà íà÷àëà äåéñòâè ïàòåíòà: 01.12.2000 (30) Ïðèîðèòåò: 09.12.1999 NO 19996091 (43) Äàòà ïóáëèêàöèè çà âêè: 10.01.2004 (45) Îïóáëèêîâàíî: 10.03.2005 Áþë. ¹ 7 (73) Ïàòåíòîîáëàäàòåëü(ëè): ÑÒÀÒÎÈË ÀÑÀ È ýíä Ê ÈÐ ÏÀÒ (NO) (85) Äàòà ïåðåâîäà çà âêè PCT íà íàöèîíàëüíóþ ôàçó: 09.07.2002 (86) Çà âêà PCT: NO 00/00404 (01.12.2000) 2 2 4 7 7 0 1 R U Àäðåñ äë ïåðåïèñêè: 103735, Ìîñêâà, óë. Èëüèíêà, 5/2, ÎÎÎ "Ñîþçïàòåíò", Í.Í.Âûñîöêîé C 2 C 2 (87) Ïóáëèêàöè PCT: WO 01/42175 (14.06.2001) (54) ÑÏÎÑÎÁ ÏÐÅÂÐÀÙÅÍÈß ÏÐÈÐÎÄÍÎÃÎ ÃÀÇÀ  ÂÛÑØÈÅ ÓÃËÅÂÎÄÎÐÎÄÛ (57) Ðåôåðàò: îòõîä ùèõ ãàçîâ â îòäåëüíîì àïïàðàòå ïàðîâîãî Èñïîëüçîâàíèå: ïîëó÷åíèå óãëåâîäîðîäîâ. ðèôîðìèíãà è ââîä ò îòõîä ùèé ãàç, ïîäâåðãíóòûé Ñóùíîñòü: ïðîâîä ò âçàèìîäåéñòâèå ïðèðîäíîãî ðèôîðìèíãó, â ãàçîâûé ïîòîê äî åãî ïîäà÷è â ãàçà ñ ïàðîì è ...

Optimum integration of Fischer-Tropsch synthesis and syngas production

A method is described for conversion of natural gas or other fossil fuels to higher hydrocarbons, comprising the following steps: a) reaction of natural gas with steam and oxygenic gas in at least one reforming zone in order to produce a synthesis gas consisting primarily of hydrogen and CO, in addition to some carbon dioxide; b) passing said synthesis gas to a Fisher-Tropsch reactor in order to produce a crude synthesis stream consisting of lower hydrocarbons, water and non-converted synthesis gas; c) separation of said crude synthesis stream in a recovery zone, into a crude product stream mainly containing heavier hydrocarbons, a water stream and a tail gas stream mainly containing the remaining constituents; which is charaterized in that the method also comprises the following steps; d) stream reformation of at least part of the tail gas in a separate steam reformer; e) introduction of the reformed tail gas into the gas stream before this is led into the Fischer-Tropsch reactor.

Optimum integration of fischer-tropsch synthesis and syngas production

A method is described for conversion of natural gas or other fossil fuels to higher hydrocarbons, comprising the following steps: a) reaction of natural gas with steam and oxygenic gas in at least one reforming zone in order to produce a synthesis gas consisting primarily of H2 and CO, in addition to some CO2; b) passing said synthesis gas to a Fischer-Tropsch reactor in order to produce a crude synthesis stream consisting of lower hydrocarbons, water and non-converted synthesis gas; c) separation of said crude synthesis stream in a recovery zone, into a crude product stream mainly containing heavier hydrocarbons, a water stream and a tail gas stream mainly containing the remaining constituents; which is characterised in that the method also comprises the following steps; d) steam reformation of at least part of the tail gas in a separate steam reformer; e) introduction of the reformed tail gas into the gas stream before this is led into the Fischer-Tropsch reactor.

Catalytic reactor and process

Method for production of hydrogen rich gas mixtures

Systems and methods for the use of fischer-tropsch tail gas in a gas to liquid process

The present disclosure provides a Fischer-Tropsch tail gas recycling system, including: a Fischer-Tropsch reactor providing a source of tail gas; a first preheater for preheating the tail gas to between about 200 and 300 degrees C; a hydrogenator for hydrogenating the tail gas; an expansion device for reducing the pressure of the tail gas to between about 2.5 and 5 bar; a second preheater for preheating a feed gas comprising the tail gas and steam to between about 500 and 600 degrees C; and a catalytic reformer for reforming the feed gas in the presence of a catalyst, wherein the catalytic reformer operates at about 2 bar and about 1000 degrees C, for example. Optionally, C02 and/or natural gas are also added to the tail gas and/or steam to form the feed gas.

Process for the production of synthesis gas

Die Erfindung betrifft ein Verfahren zur Erzeugung von Kohlenwasserstoffen (23), bei dem aus einem kohlenwasserstoffhaltigen Einsatzstrom (1) ein erster (3) und ein zweiter Einsatzteilstrom (4) gewonnen werden, von denen der erste (3) mittels Partieller Oxidation oder Autothermer Reformierung (R) in einen ersten Synthesegasstrom (8) und der zweite (4) mittels Dampfreformierung (D) in einen zweiten Synthesegasstrom (10) umgesetzt und nachfolgend mit dem ersten Synthesegasstrom (8) zu einem dritten Synthesegasstrom (5) vereinigt wird, von dem zumindest ein erster Teil (11) durch Fischer-Tropsch-Synthese (F) zu einem Kohlenwasserstoffe unterschiedlicher Kettenlängen enthaltenden Rohproduktstrom (16) umgesetzt wird, von dem leichte Kohlenwasserstoffe in einem Restgas (17) abgetrennt werden, um sie zurückzuführen und in der Partiellen Oxidation oder der Autothermal Reformierung (R) einzusetzen. Kennzeichnend hierbei ist, dass ungesättigte Kohlenwasserstoffe (21) aus wenigstens einem Teil (19) des Restgases (17) abgetrennt werden, um einen weitgehend von ungesättigten Kohlenwasserstoffen freien Strom (20) als Einsatz für die Partielle Oxidation oder die Autothermal Reformierung (R) zu erhalten. The invention relates to a process for the production of hydrocarbons (23), in which from a hydrocarbon-containing feed stream (1) a first (3) and a second feedstock stream (4) are obtained, of which the first (3) by partial oxidation or autothermal reforming (R) in a first synthesis gas stream (8) and the second (4) by steam reforming (D) in a second synthesis gas stream (10) and subsequently combined with the first synthesis gas stream (8) to a third synthesis gas stream (5), of which at least a first part (11) is converted by Fischer-Tropsch synthesis (F) to a crude product stream (16) containing hydrocarbyls of different chain lengths, from which light hydrocarbons in a residual gas (17) are separated to recycle them and in the partial oxidation or autothermal reforming (R). ...

Optimum integration of fischer-tropsch synthesis and syngas production

A method is described for conversion of natural gas or other fossil fuels to higher hydrocarbons, comprising the following steps: a) reaction of natural gas with steam and oxygenic gas in at least one reforming zone in order to produce a synthesis gas consisting primarily of H 2 and CO, in addition to some CO 2 ; b) passing said synthesis gas to a Fisher-Tropsch reactor in order to produce a crude synthesis stream consisting of lower hydrocarbons, water and non-converted synthesis gas; c) separation of said crude synthesis stream in a recovery zone, into a crude product stream mainly containing heavier hydrocarbons, a water stream and a tail gas stream mainly containing the remaining constituents; which is charaterised in that the method also comprises the following steps; d) stream reformation of at least part of the tail gas in a separate steam reformer. e) introduction of the reformed tail gas into the gas stream before this is led into the Fischer-Tropsch reactor.

费－托合成与合成气生产的最佳整合

本发明公开了将天然气或其它矿物燃料转化为高级烃的方法，包括以下步骤：a)在至少一个重整区中使天然气与蒸汽和含氧气体反应，以制备主要由H 2 和CO以及一些CO 2 组成的合成气；b)将所述合成气引入费－托反应器，以制备由低级烃、水和未转化的合成气组成的粗合成物流；c)在回收区中将所述粗合成物流分离为主要含有高级烃的粗产物流、水物流和主要含有残余组分的尾气物流；其特征在于该方法还包括以下步骤：d)在独立的蒸汽重整器中将至少部分尾气蒸汽重整；e)在将重整后的尾气引入费－托反应器之前，将其加入气体物流中。

Fremgangsmate for fremstilling av hydrokarboner med lang kjede fra naturgass

Naturgass reageres med damp for å generere karbonmonoksyd og hydrogen i en første katalytisk reaktor, idet den resulterende gassblanding anvendes for a gjennomføre Fischer-Tropsch syntese i en andre katalytisk reaktor. Etter utføring av Fischer-Tropsch syntesen separeres det gjenværende hydrogen fra en hydrokarbonrik strøm ved å anvende en hydrogenpermeabel membran, og den hydrokarbonrike strømmen returneres for å underkastes dampreformering. Den hydrokarbonrike strømmen tilføres foretrukket til en forbrenningskanal for å tilveiebringe varme for den endotermiske dampreformeringsreaksjonen. Den totale prosessen omdanner naturgass til langkjedede hydrokarboner og kan tilveiebringe en karbonomdannelse på mer enn 80%.

Short contact time catalytic partial oxidation process for recovering sulfur from an H2S containing gas stream

A process for removing sulfur from a H 2 S-containing gas stream is disclosed. A preferred embodiment of the process comprises incorporating a short contact time catalytic partial oxidation reactor, a cooling zone, and a condenser into a conventional refinery or gas plant process, such as a natural gas desulfurizer, a hydrotreater, coker or fluid catalytic cracker, in which sulfur removal is needed in order to produce a more desirable product. An H 2 S-containing gas stream is fed into a short contact time reactor where the H 2 S is partially oxidized over a suitable catalyst in the presence of O 2 to elemental sulfur and water.

SPOX-enhanced process for production of synthesis gas

A method, system and catalysts for improving the yield of syngas from the catalytic partial oxidation of methane or other light hydrocarbons is disclosed. The increase in yield and selectivity for CO and H 2 products results at least in part from the substitution of H 2 S partial oxidation to elemental sulfur and water for the combustion of light hydrocarbon to CO 2 and water.

Short contact time catalytic sulfur recovery system for removing H2S from a waste gas stream

An apparatus and process for recovering elemental sulfur from a H 2 S-containing waste gas stream are disclosed, along with a method of making a preferred catalyst for catalyzing the process. The apparatus preferably comprises a short contact time catalytic partial oxidation reactor, a cooling zone, and a sulfur condenser. According to a preferred embodiment of the process, a mixture of H 2 S and O 2 contacts the catalyst very briefly (i.e, less than about 200 milliseconds). Some preferred catalyst devices comprise a reduced metal such as Pt, Rh, or Pt—Rh, and a lanthanide metal oxide, or a pre-carbided form of the metal. The preferred apparatus and process are capable of operating at superatmospheric pressure and improve the efficiency of converting H 2 S to sulfur, which will reduce the cost and complexity of construction and operation of a sulfur recovery plant used for waste gas cleanup.

Recovery of sulfur from H2S and concurrent production of H2 using short contact time CPOX

A method, apparatus and system for treating a stream containing H 2 S are disclosed. A preferred method comprises mixing the stream containing H 2 S with a light hydrocarbon stream and an oxygen containing stream to form a feed stream; contacting the feed stream with a catalyst while simultaneously raising the temperature of the stream sufficiently to allow partial oxidation of the H 2 S and partial oxidation of the light hydrocarbon to produce a product stream containing elemental sulfur, H 2 O, CO and hydrogen, and cooling the product stream sufficiently to condense at least a portion of the elemental sulfur and produce a tail gas containing CO, H 2 , H 2 O and any residual elemental sulfur, and any incidental SO 2 , COS, and CS 2 from the hydrocarbon stream or produced in the process. The tail gate is contacted with a hydrogenation catalyst so that CO is then reacted with water to produce CO 2 and hydrogen and any elemental sulfur, SO 2 , COS, and CS 2 in the tail gas is preferably converted into H 2 S. The resulting H 2 and H 2 S-containing tail gas stream is then contacted with an alkanolamine absorber to remove the H 2 S, producing a hydrogen stream which may be compressed and further purified for use in a hydrogen consuming process.

Catalysts for SPOC™ enhanced synthesis gas production

A process and system for producing synthesis gas by a SPOC® enhanced catalytic partial oxidation process is disclosed. Light hydrocarbons in a H 2 S-containing feed gas are partially oxidized to produce hydrogen and carbon monoxide over a catalyst that simultaneously oxidizes the H 2 S to produce elemental sulfur. A reaction in which H 2 S is partially oxidized to elemental sulfur and water takes place instead of a secondary reaction in which a portion of the light hydrocarbon feed is combusted to form CO 2 and water. An increase in yield and selectivity for CO and H 2 products results, and readily recoverable elemental sulfur is also produced.

Hydrocarbon gas conversion system and process for producing a synthetic hydrocarbon liquid

processes and system for generating high pressure steam from the synthesis gas fermentation process.

Catalytic reactor

Steam methane reforming method

A steam methane reforming method in which a feed stream is treated in a reactor containing a catalyst that is capable of promoting both hydrogenation and partial oxidation reactions. The reactor is either operated in a catalytic hydrogenation mode to convert olefins into saturated hydrocarbons and/or to chemically reduce sulfur species to hydrogen sulfide or a catalytic oxidative mode utilizing oxygen and steam to prereform the feed and thus, increase the hydrogen content of a synthesis gas produced by a steam methane reformer. The method is applicable to the treatment of feed streams containing at least 15% by volume of hydrocarbons with two or more carbon atoms and/or 3% by volume of olefins, such as a refinery off-gas. In such case, the catalytic oxidative mode is conducted with a steam to carbon ratio of less than 0.5, an oxygen to carbon ratio of less than 0.25 and a reaction temperature of between about 500° C. and about 860° C. to limit the feed to the steam methane reformer to volumetric dry concentrations of less than about 0.5% for the olefins and less than about 10% for alkanes with two or more carbon atoms.

Steam methane reforming method

A steam methane reforming method in which a feed stream is treated in a reactor containing a catalyst that is capable of promoting both hydrogenation and partial oxidation reactions. The reactor is either operated in a catalytic hydrogenation mode to convert olefins into saturated hydrocarbons and/or to chemically reduce sulfur species to hydrogen sulfide or a catalytic oxidative mode utilizing oxygen and steam to prereform the feed and thus, increase the hydrogen content of a synthesis gas produced by a steam methane reformer. The method is applicable to the treatment of feed streams containing at least 15% by volume of hydrocarbons with two or more carbon atoms and/or 3% by volume of olefins, such as a refinery off-gas. In such case, the catalytic oxidative mode is conducted with a steam to carbon ratio of less than 0.5, an oxygen to carbon ratio of less than 0.25 and a reaction temperature of between about 500° C. and about 860° C. to limit the feed to the steam methane reformer to volumetric dry concentrations of less than about 0.5% for the olefins and less than about 10% for alkanes with two or more carbon atoms.

가스화 로, 가스화 시스템, 개질 장치 및 개질 시스템

타르의 생성량이 적은 형태로 바이오매스 자원을 가스화할 수 있는 가스화로. 가스화 로(10)는 로 내를 상하로 구획하는 펀칭 플레이트(11)와, 펀칭 플레이트(11) 위에 바이오매스 자원을 공급하기 위한 바이오매스 자원 공급구(10a)와, 로 내에 산화제를 공급하기 위한 제 1 산화제 공급구(10c) 및 제 2 산화제 공급구(10d)와, 제 1 산화제 공급구(10c)로부터의 산화제를 펀칭 플레이트(11)의 상방으로부터 하방을 향하여 공급하는 제 1 산화제 공급로와, 제 2 산화제 공급구(10d)로부터의 펀칭 플레이트(11) 근방의 소정 범위 내의 복수 개소에 분배 공급하는 제 2 산화제 공급로, 펀칭 플레이트(11) 위의 바이오매스 자원의 부분 산화 및 열분해에 의해 생성된 건류 가스를 외부로 배출하는 건류 가스 배출구(10b)를 구비한다.

Fuel processor providing improved warming up structure for CO removing unit and managing method thereof

CO 제거유닛의 워밍업 구조가 개선된 연료개질기 및 그 운영방법이 개시된다. 개시된 연료개질기는, 연료원을 물과 반응시켜서 수소가스를 추출해내는 리포머와, 리포머를 수소 추출 반응에 적합한 온도로 가열하는 버너와, 리포머에서의 수소 추출 반응 중 생성된 일산화탄소를 제거하는 CO 쉬프트기와 CO제거기 및, 리포머에서 열을 흡열하여 CO 쉬프트기에서 방열하기 위한 수증기의 이동라인을 구비한다. 이와 같은 구성의 연료개질기를 운영하면, 초기 스타트 시 수증기의 열교환을 이용한 CO 쉬프트기의 급속 가열이 가능하므로, 연료개질기의 정상 가동까지 걸리는 시간을 대폭 단축할 수 있다. A fuel reformer having an improved warm-up structure of a CO removal unit and a method of operating the same are disclosed. The disclosed fuel reformer includes a reformer for extracting hydrogen gas by reacting a fuel source with water, a burner for heating the reformer to a temperature suitable for the hydrogen extraction reaction, a CO shifter for removing carbon monoxide generated during the hydrogen extraction reaction in the reformer, And a moving line of steam for absorbing heat from the CO remover and radiating heat from the CO shifter. By operating the fuel reformer having such a configuration, it is possible to rapidly heat the CO shifter using heat exchange of water vapor at the initial start, thereby significantly reducing the time required for the normal operation of the fuel reformer.

Method of producing synthetic gas

FIELD: chemistry. ^ SUBSTANCE: in order to produce synthetic gas containing hydrogen and carbon monoxide, starting material containing methane undergoes partial oxidation using a multichannel burner fitted with a system of separate channels. Methane-containing material, at temperature higher than 500C, flows through one channel of the burner and oxidising gas flows through another channel. The channel for the methane-containing material and the channel for the oxidising gas are separated from each other by a channel through which a second gas containing hydrogen, carbon monoxide and/or hydrocarbon flows, where the second gas is at temperature 10C lower than its spontaneous ignition temperature. The second gas is obtained from gaseous by-products of a Fischer-Tropsch synthesis process or from gaseous by-products of a methanol synthesis process. ^ EFFECT: improved process. ^ 22 cl, 2 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2 437 830 (13) C2 (51) МПК C01B 3/36 (2006.01) C07C 29/151 (2006.01) C07C 1/04 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (21)(22) Заявка: 2009104481/05, 09.07.2007 (24) Дата начала отсчета срока действия патента: 09.07.2007 (72) Автор(ы): МАРТЕНС Франсискус Йоханна Арнольдус (NL) (43) Дата публикации заявки: 20.08.2010 Бюл. № 23 2 4 3 7 8 3 0 (45) Опубликовано: 27.12.2011 Бюл. № 36 (56) Список документов, цитированных в отчете о поиске: WO 9603345 A1, 08.02.1996. SU 1766282 A3, 30.09.1992. RU 2221737 C2, 20.01.2004. EP 0111376 A2, 20.06.1984. WO 2005108336 A1, 17.11.2005. WO 0238699 A1, 16.05.2002. GB 2183672 A, 10.06.1987. 2 4 3 7 8 3 0 R U (86) Заявка PCT: EP 2007/056927 (09.07.2007) C 2 C 2 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 11.02.2009 (87) Публикация заявки РСТ: WO 2008/006787 (17.01.2008) Адрес для переписки: 103735, Москва, ул. Ильинка, 5/2, ООО "Союзпатент", Е.В.Воробьевой (54) СПОСОБ ПОЛУЧЕНИЯ СИНТЕЗ-ГАЗА (57) Реферат: Изобретение относится к области химии. ...

Method and device for producing acetylene and synthesis gas

FIELD: chemistry. SUBSTANCE: invention relates to improved method of producing acetylene and synthetic gas. Disclosed is method of producing acetylene and synthetic gas by partial oxidation of hydrocarbons with oxygen, wherein initial gases, which enter stream containing hydrocarbon, and flow containing oxygen, first, preliminary heated separately, then mixed in mixing zone, and after flowing via burners cause their reaction in combustion chamber, then quickly cooled. At that, to block of burners surface facing combustion chamber stream of washing gas flow is added. this washing gas is introduced via several holes through burner unit, wherein averaged ratio of effective area of unit of burners surface to number of these holes for gas flushing flow in burners ranges from 5 to 100 cm 2 , wherein averaged ratio of unit of burners effective surface to number of these holes for gas flushing flow in burners is calculated from ratio of total effective surface of unit of burners to total number of holes for gas flushing and carried out through holes for washing flow to gas distributing devices so that 70-100 vol% of supplied washing gas flow is directed parallel to surface of burners unit side facing combustion chamber. EFFECT: invention allows to produce synthesis gas and acetylene using improved method of partial oxidation of hydrocarbons, which prevents deposits on surface of unit of burners without using mechanical treatment. 7 cl, 4 dwg, 3 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 591 940 C2 (51) МПК C01B 3/36 (2006.01) C07C 2/78 (2006.01) B01J 4/00 (2006.01) F23D 14/62 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ (21)(22) Заявка: ИЗОБРЕТЕНИЯ К ПАТЕНТУ 2013126499/05, 27.10.2011 (24) Дата начала отсчета срока действия патента: 27.10.2011 Приоритет(ы): (30) Конвенционный приоритет: (43) Дата публикации заявки: 20.12.2014 Бюл. № 35 R U 11.11.2010 US 61/412406 (72) Автор(ы): РУСС Михаэль (DE), ГРОССШМИДТ Дирк (DE), РЕНЦЕ Петер (DE), ВИКАРИ ...

Method of producing methane-hydrogen mixture

FIELD: chemistry. SUBSTANCE: invention relates to a method of producing a methane-hydrogen mixture for producing hydrogen and can be used in chemical industry for processing hydrocarbon gases, as well as in methane-hydrogen mixture application technologies, including in electric energy accumulation systems. Method includes catalytic conversion of methane-containing gas in adiabatic reactor with supply of water vapor preheated by electric heater therein, wherein conversion is carried out without supply of oxygen-containing gases, maintaining temperature at reactor outlet at level of not higher than 700 °C. EFFECT: invention increases thermodynamic efficiency of the method of producing methane-hydrogen mixture and efficiency of methane conversion, high content of hydrogen and reduced content of ballast gases in the produced gas, higher fire-explosion safety, as well as reduced capital costs and metal consumption. 13 cl, 1 dwg, 3 tbl РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 730 829 C1 (51) МПК C01B 3/38 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК C01B 3/38 (2020.02) (21)(22) Заявка: 2020107757, 20.02.2020 (24) Дата начала отсчета срока действия патента: (73) Патентообладатель(и): Столяревский Анатолий Яковлевич (RU) Дата регистрации: 26.08.2020 Приоритет(ы): (22) Дата подачи заявки: 20.02.2020 (45) Опубликовано: 26.08.2020 Бюл. № 24 2 7 3 0 8 2 9 R U (54) СПОСОБ ПОЛУЧЕНИЯ МЕТАНО-ВОДОРОДНОЙ СМЕСИ (57) Реферат: Изобретение относится к способу получения ведут без подвода кислородсодержащих газов, метано-водородной смеси для производства поддерживая температуру на выходе из реактора водорода и может быть использовано в на уровне не выше 700°С. Изобретение химической промышленности для переработки обеспечивает повышение термодинамической углеводородных газов, а также в технологиях эффективности способа получения метаноприменения метано-водородной смеси, в том водородной смеси и эффективности конверсии числе в ...

注入氮气的整合的提高石油采收率的方法

本发明涉及提高石油采收率的方法，其与诸如气化或重整的合成气产生方法和用于产生(i)供例如在合成气方法或燃烧方法中使用的氧气流和(ii)供EOR使用的氮气流的空气分离方法整合。

整体加氢甲烷化联合循环方法

本发明涉及一种整体方法，用于在蒸汽、一氧化碳、氢气、加氢甲烷化催化剂和任选的氧气存在下，经碳质原料的加氢甲烷化制备可燃气态产物和由那些可燃气态产物以及氢气和/或甲烷副产物流产生电力。

Heat exchanger for cooling of hot gases, and heat exchange system

FIELD: heating. SUBSTANCE: heat exchanger includes the following: at least one vertically oriented tank containing a bath of cooling fluid medium and having a space for collection of a vapour phase generated above the above said bath of cooling fluid medium, one vertical tubular element inserted inside the above tank, open on ends and coaxial to the above tank, one spiral channel that is turned about the tank axis, inserted in the above coaxial tubular element, one outlet for vapour phase generated in the upper part of the above tank; with that, at least one transportation line is inserted in the lower part of the vertical tank, open on both ends, one of which is connected to the vertical tank and the other one is free and is located outside the above said tank; with that, the above said transportation line is tubular and projects sideways outside the above said heat exchanger, includes at least one central internal channel that is interconnected as to fluid medium with the spiral channel and passes vertically along the tubular element inserted in the vertical tank; with that, the channel has an external jacket in which cooling fluid medium circulates. EFFECT: increasing safety and serviceability of a heat exchange system. 20 cl, 1 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 552 623 C2 (51) МПК F28D 7/02 (2006.01) F28F 9/02 (2006.01) F22B 1/18 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ (21)(22) Заявка: ИЗОБРЕТЕНИЯ К ПАТЕНТУ 2013135413/06, 29.12.2011 (24) Дата начала отсчета срока действия патента: 29.12.2011 (72) Автор(ы): ВИЛЬХЕЛЬМ Альфред Йоахим (IT), БАЗИНИ Лука Эудженио (IT) (73) Патентообладатель(и): ЭНИ С.П.А. (IT) Приоритет(ы): (30) Конвенционный приоритет: (43) Дата публикации заявки: 10.02.2015 Бюл. № 4 R U 29.12.2010 IT MI 2010 A 002445 (45) Опубликовано: 10.06.2015 Бюл. № 16 C 2 R U 2 5 5 2 6 2 3 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 29.07.2013 (86) Заявка PCT: EP 2011/074201 (29.12.2011) (87) ...

Systems and methods of producing superpure hydrogen under high pressure

FIELD: chemistry. SUBSTANCE: invention relates to field of chemistry. Exothermally generated product 4 of synthesis-gas is produced in the first reactor by conversion of the first part of hydrocarbon raw material flow. Endothermally converted product 7 of synthesis-gas, in which, at least, part of heat is used from exothermally generated synthesis-gas product, is obtained in heat-exchange reforming installation. Flow 7 is cooled. Cooled flow 8 is passed through high-temperature shift reactor, in which part of CO reacts with vapour with production of carbon dioxide and hydrogen. Obtained flow 9 is directed into low-temperature shift reactor. Obtained flow 11 is supplied into separator, which separates methane from combination of exothermally generated synthesis-gas product and endothermally converted synthesis-gas product with obtaining flow of discharge gas. Heater burns, at least, part of discharge gas, using exhaust from gas turbine as oxidiser, producing flows of overheated vapour and hydrocarbon raw material, used in exothermally- and endothermally generated synthesis-gas product. Generator generates energy, using gas turbine to bring oxygen-producing installation into action, providing oxygen for synthesis-gas generation. EFFECT: invention makes it possible to obtain highly pure hydrogen under high pressure. 29 cl, 16 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 516 527 C2 (51) МПК C01B 3/38 (2006.01) F01K 23/06 (2006.01) F02C 3/28 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ (21)(22) Заявка: ИЗОБРЕТЕНИЯ К ПАТЕНТУ 2011110497/05, 19.08.2009 (24) Дата начала отсчета срока действия патента: 19.08.2009 (72) Автор(ы): АЛЛАМ Родни Дж. (GB) (73) Патентообладатель(и): ДжиТиЭлПЕТРОЛ ЭлЭлСи (US) Приоритет(ы): (30) Конвенционный приоритет: (43) Дата публикации заявки: 27.09.2012 Бюл. № 27 R U 21.08.2008 US 61/090,799 (45) Опубликовано: 20.05.2014 Бюл. № 14 2119700 C1, 27.09.1998. US 20020103264 A1, 01.08.2002. US 4725381 A, 16.02.1988. SU ...

System of electric power generation at fermentation of synthesis gas

FIELD: technological processes. SUBSTANCE: method for production of high pressure steam during fermentation of synthesis gas involves bringing in contact of hot synthesis gas with a temperature higher than 760°C (1400 °F) with cooled synthesis gas with a temperature from 177 °C to 232 °C (350 °F-450 °F), herewith the cooled synthesis gas is mixed with the hot synthesis gas in a ratio from 0.1 to 20 to produce in the inlet orifice of the waste heat recovery boiler a preliminary cooled synthesis gas with the temperature of 760 °C (1400 °F) or less, and supply of the preliminary cooled synthesis gas in the waste heat recovery boiler producing a high pressure steam and the cooled synthesis gas. EFFECT: invention provides high-efficiency production of high pressure steam during fermentation of synthesis gas. 10 cl, 4 dwg, 2 tbl РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (51) МПК C10J 3/86 (11) (13) 2 603 663 C2 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ 2013149044/05, 04.04.2012 (21)(22) Заявка: (24) Дата начала отсчета срока действия патента: 04.04.2012 Приоритет(ы): (30) Конвенционный приоритет: US US US US (73) Патентообладатель(и): ИНЕОС БИО СА (CH) 61/516,646; 61/516,704; 61/516,667; 13/324,321 (45) Опубликовано: 27.11.2016 Бюл. № 33 (56) Список документов, цитированных в отчете о поиске: US 4823741 A, 25.04.1989;US 7552701 B2, 30.06.2009;RU 2120469 C1, 20.10.1998;RU 2117687 C1, 20.08.1998;US 4238403 A, 09.12.1980. (86) Заявка PCT: C 2 C 2 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 06.11.2013 US 2012/032180 (04.04.2012) (87) Публикация заявки PCT: 2 6 0 3 6 6 3 WO 2012/138766 (11.10.2012) R U 2 6 0 3 6 6 3 (43) Дата публикации заявки: 20.05.2015 Бюл. № 14 R U 06.04.2011 06.04.2011 06.04.2011 13.12.2011 (72) Автор(ы): БЕЛЛ Петер С (US), ОКФЕМИА Ким (US), БЕРНСТЭД Стивен Джон (GB), ПАРКЕР Грэм (GB) Адрес для переписки: 119019, Москва, Гоголевский бульвар, 11, этаж 3, "Гоулингз Интернэшнл Инк.", Соболеву А.Ю ...

Fuel processor providing temperature control function for CO shift reactor and managing method thereof

CO 제거유닛의 워밍업 구조가 개선된 연료처리장치 및 그 운영방법이 개시된다. 개시된 연료처리장치는, 연료원을 물과 반응시켜서 수소가스를 생성해내는 리포머와, 리포머를 수소 생성 반응에 적합한 온도로 가열하는 버너와, 리포머에서의 수소 생성 반응 중 생성된 일산화탄소를 제거하는 CO 쉬프트기와, CO 쉬프트기를 리포머의 배기가스로 가열하기 위한 가열수단 및, CO 쉬프트기를 냉각수나 냉각가스로 냉각시키기 위한 냉각수단을 포함한다. 이와 같은 구성의 연료처리장치를 운영하면, CO 쉬프트기의 온도를 능동적으로 제어할 수 있으므로, 일산화탄소의 제거 성능을 항상 안정적으로 유지할 수 있다. Disclosed are a fuel processing apparatus and a method of operating the same, wherein the warm-up structure of the CO removal unit is improved. The disclosed fuel processing apparatus includes a reformer that generates a hydrogen gas by reacting a fuel source with water, a burner that heats the reformer to a temperature suitable for a hydrogen generation reaction, and a CO that removes carbon monoxide generated during the hydrogen generation reaction in the reformer. A shifter, heating means for heating the CO shifter with the exhaust gas of the reformer, and cooling means for cooling the CO shifter with cooling water or cooling gas. By operating the fuel processing device having such a configuration, the temperature of the CO shifter can be actively controlled, so that the performance of removing carbon monoxide can be kept stable at all times.

탄화수소 공급 가스의 촉매적 스팀 개질에 의한 합성 가스 제조 공정 및 설비

탄화수소 공급 가스의 촉매적 스팀 개질에 의해 수소와 일산화탄소를 주성분으로 하는 합성 가스를 제조하기 위한 공정 및 설비로서, 연도 가스를 생성함으로써 화학 개질 반응이 일어나는 데 필요한 버너의 열이 발생되고, 합성 가스와 연도 가스에 포함된 열을 이용하여, 보일러 급수로부터 순수 스팀이 생성되고, 프로세스 응축액으로부터 프로세스 스팀이 생성되며, 순수 스팀의 생성을 위해 합성 가스 및 연도 가스가 사용되고, 프로세스 스팀의 생성을 위해 순수 스팀의 일부가 열전달 매체로서 사용되고 순수 스팀의 나머지 부분은 공정으로부터 배출 스팀으로서 배출되는 공정 및 설비.

液体重烃进料向气态产物的转化

本发明涉及由“液体”重烃进料生成轻烯烃、甲烷和其它较高价值气态烃的方法和仪器。

Conversion of liquid heavy hydrocarbon feedstocks to gaseous products

본 발명은 "액체" 중질 탄화수소 공급원료로부터 경질 올레핀, 메탄 및 부가가치가 있는 다른 가스상 탄화수소의 생성 방법 및 장치에 관한 것이다. The present invention relates to a method and apparatus for the production of light olefins, methane and other gaseous hydrocarbons with added value from "liquid" heavy hydrocarbon feedstocks.

Method of producing syngas and a device for cooling syngas

FIELD: chemistry; manufacturing technology.SUBSTANCE: invention relates to a method of producing syngas containing hydrogen and carbon monoxide from preheated methane-containing gas and to a cooling device for cooling hot crude gas. Method comprises the following steps: (a) carrying out a reaction between preheated methane-containing gas and an oxidant gas to obtain hot crude syngas, containing carbon monoxide and hydrogen; (b) cooling hot crude syngas obtained at step (a) to obtain syngas by indirect heat exchange with water to obtain saturated steam; (c) additional cooling of crude syngas obtained at step (b) by indirect heat exchange with methane-containing gas to obtain cooled crude gas-phase syngas and preheated methane-containing gas for use in step (a), wherein (i) steps (b) and (c) pass in a single cooling device for combined indirect heat exchange with water and a methane-containing gas; and (ii) preheated methane-containing gas obtained at step (c) has temperature of 400 to 650 °C.EFFECT: technical result consists in providing a method in which heat contained in hot crude syngas can be more efficiently regenerated.9 cl, 3 dwg, 3 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 721 837 C2 (51) МПК C01B 3/36 (2006.01) C01B 3/38 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК C01B 3/36 (2020.02); C01B 3/38 (2020.02) (21)(22) Заявка: 2017143599, 04.05.2016 (24) Дата начала отсчета срока действия патента: (73) Патентообладатель(и): ШЕЛЛ ИНТЕРНЭШНЛ РИСЕРЧ МААТСХАППИЙ Б.В. (NL) Дата регистрации: 22.05.2020 14.05.2015 EP 15167763.0 (43) Дата публикации заявки: 14.06.2019 Бюл. № 17 (56) Список документов, цитированных в отчете о поиске: EP 1094030 A2, 25.04.2001. WO 2007131975 A1, 22.11.2007. WO 2010133621 A1, 25.11.2010. RU 2331575 C2, 20.08.2008. RU 2144494 C1, 20.01.2000. (45) Опубликовано: 22.05.2020 Бюл. № 15 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 14.12.2017 2 7 2 1 8 3 7 Приоритет( ...

产生超纯高压氢气的系统和方法

在各实施方式中，使包含甲烷的原料流发生反应以产生合成气。可进一步处理所述合成气以产生超纯高压氢气流。

Catalytic steam reforming of hydrocarbons

The hot effluent from the catalytic steam reforming of a major portion of a fluid hydrocarbon feed stream in the reformer tubes of a primary reformer, or said effluent after secondary reforming thereof, is mixed with the hot effluent from the catalytic steam reforming of the remaining portion of the feed discharged from the reformer tubes of a primary reformer-exchanger. The combined gas steam is passed on the shell side of the reformer-exchanger countercurrently to the passage of feed in the reformer tubes thereof, thus supplying the heat for the reforming of the portion of the feed passed through the reformer tubes of the reformer-exchanger. At least about 2/3 of the hydrocarbon feed stream is passed to the reformer tubes of said primary reformer, heated by radiant heat transfer and/or by contact with combustion gases, at a steam/hydrocarbon mole ratio of about 2-4/1. The remainder of said feed stream is passed to the reformer tubes of said reformer-exchanger at a steam/hydrocarbon mole ratio of about 3-6/1. The reformer shell of the reformer-exchanger is internally insulated by a refractory lining or by use of a double shell with passage of water or a portion of the feed material between the inner and outer shells. There is no significant difference between the pressure inside and outside of the reformer tubes of said primary reformer-exchanger.

Ceramic oxygen transport membrane array reactor and reforming method

FIELD: chemistry.SUBSTANCE: invention relates to an oxygen transport membrane panel for transferring radiant heat to catalytic reforming reactors, a membrane module assembly, a reforming reactor assembly, a synthesis gas furnace line and a membrane-based synthesis gas plant. Membrane panel comprises and a panel framework and a plurality of membrane units. Each unit comprises two or more membrane tubes connected to each other. Each membrane tube has a permeate side located on an interior surface and a retentate side located on an exterior surface. Membrane units are able to separate oxygen from a stream that is in communication with their exterior side. Oxygen passing through the membrane reacts with a hydrogen- and hydrocarbon-containing stream, as a result of which radiant heat and water vapour are released. Catalytic reforming reactors are located in a plane parallel to membrane panels and are capable of producing synthesis gas in the presence of radiant heat and a hydrocarbon-containing stream.EFFECT: improved operability and processability of the synthesis gas production system, improved thermal connection of reactor membrane tubes and catalyst reforming tubes are provided.51 cl, 20 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 680 048 C2 (51) МПК B01J 8/06 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК B01J 8/06 (2018.08); B01J 19/2425 (2018.08); B01J 19/2475 (2018.08); B01J 8/009 (2018.08) (21)(22) Заявка: 2016117903, 07.10.2014 (24) Дата начала отсчета срока действия патента: Дата регистрации: 14.02.2019 07.10.2013 US 61/887,751; 29.01.2014 US 61/932,974; 29.04.2014 US 61/985,838; 07.10.2014 US 14/508,297 (73) Патентообладатель(и): ПРАКСАЙР ТЕКНОЛОДЖИ, ИНК. (US) (56) Список документов, цитированных в отчете о поиске: EP 1504811 A1, 09.02.2005. US 2013/ (43) Дата публикации заявки: 15.11.2017 Бюл. № 32 0009102 A1, 10.01.2013. EP 0984500 A2, 08.03.2000. US 2009/0120379 A1, 14.05.2009. 2 6 8 0 0 4 8 ...

METHOD FOR THE PRODUCTION OF LONG-RIVETTY

アンモニア製造プラントおよびアンモニアの製造方法

本発明のアンモニア製造プラントは、炭素系原料からアンモニアを製造するためのアンモニア製造プラントであって、アンモニアを合成するためのアンモニア合成設備と、炭素系原料からアンモニア合成用の合成ガスを生成するための合成ガス生成設備と、動力を得るための動力発生設備とを備え、合成ガス生成設備は、合成ガス生成時に発生する排熱を回収する排熱回収部を有し、動力発生設備は、酸素と燃料とを燃焼させる燃焼装置と、当該燃焼装置で得られたＣＯ２ガスを含む燃焼ガスを動力として駆動することにより動力を発生するガスタービンとを有し、且つガスタービンから排出されたＣＯ２ガスをリサイクルガスとして燃焼装置に供給するように構成され、動力発生設備で得られた動力は、少なくともアンモニア合成設備の動力として使用され、排熱回収部で回収された排熱は、リサイクルガスを加熱するために使用される。

Patent RU2017143599A3

7 ВУ"? 2017143599” АЗ Дата публикации: 26.07.2019 Форма № 18 ИЗ,ПМ-2011 Федеральная служба по интеллектуальной собственности Федеральное государственное бюджетное учреждение 9 «Федеральный институт промышленной собственности» (ФИПС) ОТЧЕТ О ПОИСКЕ 1. . ИДЕНТИФИКАЦИЯ ЗАЯВКИ Регистрационный номер Дата подачи 2017143599/05(075050) 04.05.2016 РСТ/ЕР2016/059994 04.05.2016 Приоритет установлен по дате: [ ] подачи заявки [ ] поступления дополнительных материалов от к ранее поданной заявке № [ ] приоритета по первоначальной заявке № из которой данная заявка выделена [ ] подачи первоначальной заявки № из которой данная заявка выделена [ ] подачи ранее поданной заявки № [Х] подачи первой(ых) заявки(ок) в государстве-участнике Парижской конвенции (31) Номер первой(ых) заявки(ок) (32) Дата подачи первой(ых) заявки(ок) (33) Код страны 1. 15167763.0 14.05.2015 ЕР* Название изобретения (полезной модели): [Х] - как заявлено; [ ] - уточненное (см. Примечания) СПОСОБ ПОЛУЧЕНИЯ СИНГАЗА И УСТРОЙСТВО ДЛЯ ОХЛАЖДЕНИЯ СИНГАЗА Заявитель: ШЕЛЛ ИНТЕРНЭШНЛ РИСЕРЧ МААТСХАППИЙ Б.В., М1. 2. ЕДИНСТВО ИЗОБРЕТЕНИЯ [Х] соблюдено [ ] не соблюдено. Пояснения: см. Примечания 3. ФОРМУЛА ИЗОБРЕТЕНИЯ: [Х] приняты во внимание все пункты (см. Примечания) [ ] приняты во внимание следующие пункты: [ ] принята во внимание измененная формула изобретения (см. Примечания) 4. КЛАССИФИКАЦИЯ ОБЪЕКТА ИЗОБРЕТЕНИЯ (ПОЛЕЗНОЙ МОДЕЛИ) (Указываются индексы МПК и индикатор текущей версии) СОТВ 3/36 (2006.01) СО1В 3/38 (2006.01) 5. ОБЛАСТЬ ПОИСКА 5.1 Проверенный минимум документации РСТ (указывается индексами МПК) СО1В 3/00-3/58 5.2 Другая проверенная документация в той мере, в какой она включена в поисковые подборки: 5.3 Электронные базы данных, использованные при поиске (название базы, и если, возможно, поисковые термины): РУ/РТ, Езрасепе, Соозе, Соое Ржеп$, РАТЕМТЫСОРЕ, Ра еагсь, КОРТО, ОЗРТО, Уапдех 6. ДОКУМЕНТЫ, ОТНОСЯЩИЕСЯ К ПРЕДМЕТУ ПОИСКА Кате- Наименование документа с указанием (где необходимо) частей, Относится к ...

신가스 냉각기 시스템 및 작동 방법

신가스를 냉각하는 방법 및 시스템은 효과적인 신가스 냉각을 제공하고, 그리고 신가스 냉각 장치에서 감소된 파울링 레벨로 이어진다. 신가스를 냉각하는 방법은 신가스 냉각기의 입구에서 약 600 ℉ 내지 약 1400 ℉ 의 온도를 갖는 혼합된 신가스를 제공하기 위해서 효과적인 양으로 신가스를 냉각된 리싸이클링 신가스와 혼합하는 것을 포함한다. 혼합된 신가스는 신가스 냉각기의 입구 전에 적어도 한 번 유동 방향을 변경한다.

Carbon monoxide conversion process and reactor.

Теплообменный реактор для производства водорода с помощью встроенного пучка парогенератора

1. Теплообменный реактор, предназначенный для проведения эндотермических реакций, содержащий множество байонетных труб (4), подвешенных к верхнему своду (2) упомянутого реактора и простирающихся до уровня нижнего дна (3), при этом байонетные трубы (4) используются для проведения одной или нескольких эндотермических химических реакций и заключены в кожух (1), содержащий впускной патрубок (Е) для горячих дымовых газов, передающих тепло байонетным трубам (4), и, по меньшей мере, один выпускной патрубок (S) для отвода дымовых газов, охлажденных после теплообмена, причем теплообменный реактор содержит пучок парогенератора, образованный множеством вертикальных труб (5), также подвешенных к верхнему своду (2) теплообменного реактора и заключенных в периферийное пространство между внутренней перегородкой, по существу, параллельной вертикальной стенке кожуха (1), и упомянутой вертикальной стенкой, при этом упомянутая внутренняя перегородка (Bi) содержит, по меньшей мере, одно отверстие (Oi) для прохода дымовых газов из середины реактора к периферийному пространству, причем вертикальные трубы (5) служат для генерации пара и питаются водой из нижнего распределителя (9), расположенного в нижней части периферийного пространства (8), а пароводяная смесь, выходящая из вертикальных труб (5), собирается в верхнем коллекторе (7), расположенном над верхним сводом (2) теплообменного реактора, причем нижняя линия (14) связывает жидкую фазу сепараторного резервуара (6) с верхним коллектором (7), а верхняя линия (13) связывает верхний коллектор (7) с паровой фазой сепараторного резервуара (6).2. Теплообменный реактор по п.1, в котором каждая труба (5) парогене РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (51) МПК B01J 8/00 (11) (13) 2012 136 474 A (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21)(22) Заявка: 2012136474/05, 24.08.2012 (71) Заявитель(и): ИФП ЭНЕРЖИ НУВЕЛЛЬ (FR) Приоритет(ы): (30) Конвенционный приоритет: 26.08.2011 FR 11/02602 Адрес для ...

Oxidation process using microchannel technology and novel catalyst useful therefor

This invention relates to an apparatus, comprising: at least one process microchannel having a height, width and length, the height being up to about 10 mm, the process microchannel having a base wall extending in one direction along the width of the process microchannel and in another direction along the length of the process microchannel; at least one fin projecting into the process microchannel from the base wall and extending along at least part of the length of the process microchannel; and a catalyst or sorption medium supported by the fin.

Method of removing carbon dioxide emissions from in-situ recovery of bitumen and heavy oil

The present invention, in one configuration, is directed to producing a methane- containing gas from a hydrocarbon fuel energy source extracted from an in-situ recovery operation, such as a SAGD or HAGD operation, and subsequently converting at least a portion of the gas into steam, electrical power and diluents for subsequent use in the aforementioned in-situ recovery operation while emitting only controlled amounts of carbon dioxide into the environment.

Method involving an exothermic catalytic reaction of synthesis gas, and a corresponding installation

FIELD: gas synthesis SUBSTANCE: invention relates to a method involving an exothermic catalytic reaction of a synthesis gas. A synthesis method involves steam reforming of a gaseous hydrocarbon raw material, an exothermic reaction of the resulting synthesis gas, the removal of heat from the specified exothermic reaction, while steam is obtained, the use of the specified steam as heat incoming in steam reforming, where steam reforming includes: a) forming a mixture containing steam and hydrocarbons at least at the stage of adding the first water stream to the hydrocarbon raw material, b) heating the specified mixture using indirect heat exchange with synthesis gas, c) reforming of the specified mixture after the specified heating stage b). EFFECT: technical result is the elimination of the dependence of the pre-preparation section on the synthesis section. 15 cl, 2 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 751 112 C2 (51) МПК C01B 3/38 (2006.01) C07C 29/151 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК C01B 3/38 (2021.02); C07C 29/151 (2021.02) (21)(22) Заявка: 2019125617, 31.01.2018 (24) Дата начала отсчета срока действия патента: (73) Патентообладатель(и): КАСАЛЕ СА (CH) Дата регистрации: 08.07.2021 14.02.2017 EP 17156052.7 (43) Дата публикации заявки: 16.03.2021 Бюл. № 8 (56) Список документов, цитированных в отчете о поиске: GB 2066841 A, 15.07.1981. US 5324452 A, 28.06.1994. US 6387963 B1, 14.05.2002. US 2003022948 A1, 30.01.2003. SU 1407898 A1, 07.07.1988. (45) Опубликовано: 08.07.2021 Бюл. № 19 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 16.09.2019 2 7 5 1 1 1 2 Приоритет(ы): (30) Конвенционный приоритет: R U 31.01.2018 (72) Автор(ы): МОРЕО Пьетро (CH), САССИ Фабио (IT) 2 7 5 1 1 1 2 R U EP 2018/052348 (31.01.2018) C 2 C 2 (86) Заявка PCT: (87) Публикация заявки PCT: WO 2018/149638 (23.08.2018) Адрес для переписки: 105082, Москва, пер. Спартаковский, 2, стр. 1, секция 1, этаж 3 ...

Method of ammonia production and superheater

FIELD: chemistry. SUBSTANCE: ammonia is produced from synthesis-gas, obtained as a result of reforming hydrocarbon raw material. Partially reformed gas, after stage of primary reforming, passes through stage of heat-exchange reforming and stage of secondary reforming. Partially reformed gas at the stage of heat-exchange reforming is reformed by indirect heat-exchange with synthesis-gas, removed from stage of secondary reforming. All steam, produced in steam recovery boilers of reforming and at enterprise sector of ammonia production, is heated in one or more superheaters, located behind ammonia converter of enterprise sector of ammonia production. EFFECT: invention makes it possible to improve thermal integration of ammonia obtaining process, reduce predisposition to metal dusting, nitration and stress corrosion in steam recovery boilers and superheaters of enterprise. 9 cl, 2 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2 505 482 (13) C2 (51) МПК C01C 1/04 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (21)(22) Заявка: 2011102620/05, 17.06.2009 (24) Дата начала отсчета срока действия патента: 17.06.2009 (72) Автор(ы): СТАЛЬ Хенрик Отто (DK), ХАН Пат А. (DK) (73) Патентообладатель(и): ХАЛЬДОР ТОПСЕЭ А/С (DK) R U Приоритет(ы): (30) Конвенционный приоритет: 26.06.2008 DK PA200800881 (43) Дата публикации заявки: 10.08.2012 Бюл. № 22 2 5 0 5 4 8 2 (45) Опубликовано: 27.01.2014 Бюл. № 3 (56) Список документов, цитированных в отчете о поиске: US 20060228284 А1, 12.10.2006. US 5845703 А, 08.12.1998. RU 2283272 С2, 27.05.2003. US 4213954 А1, 22.07.1980. US 4545976 А, 08.10.1985. US 6726851 B1, 27.04.2004. 2 5 0 5 4 8 2 R U (86) Заявка PCT: EP 2009/004360 (17.06.2009) C 2 C 2 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 26.01.2011 (87) Публикация заявки РСТ: WO 2009/156085 (30.12.2009) Адрес для переписки: 105064, Москва, а/я 88, "Патентные поверенные Квашнин, Сапельников и партнеры", пат.пов. В.П. Квашнину, рег ...

METHOD FOR IMPLEMENTING THE FISHER-TROPSH PROCESS AT LOW PRESSURE

1. Способ осуществления процесса Фишера-Тропша для получения жидких углеводородов, содержащих в основном дизельное топливо или дизельную смесь, с получением жидкого углеводородного продукта, содержащего менее 10 мас.% воска (>С23) и более 65% дизельной фракции (С9-С23), включающий:работу при давлении ниже 200 фунт/кв. дюйм (абс) и использование кобальтового катализатора, включающего носитель катализатора Фишера-Тропша с кристаллитами металлического кобальта на нем, причем кристаллиты металлического кобальта имеют средний диаметр более 16 нм.2. Способ по п.1, в котором указанный носитель катализатора Фишера-Тропша выбирают из группы, состоящей из оксида алюминия, гамма-оксида алюминия, оксида циркония, оксида титана, оксида кремния и их смесей.3. Способ по п.1, в котором кобальтовый катализатор содержит металлический кобальт и содержание металлического кобальта в кобальтовом катализаторе составляет по меньшей мере 15 мас.%.4. Способ по п.1, в котором конверсия СО в подаваемом газе составляет по меньшей мере 60%.5. Способ по любому из пп.1-4, в котором используют промотор и указанные промотор выбирают из группы, состоящей из рутения, рения, родия, никеля, циркония, титана и их смесей.6. Способ по любому из пп.1-4, в котором проводят однократную дистилляцию для уменьшения крекинга легких углеводородов, имеющих более низкую температуру кипения, чем дизельная фракция.7. Способ по п.1, в котором используют реактор Фишера-Тропша без рецикла отходящего газа.8. Способ по любому из пп.1-4 или 7, в котором используют установку риформинга с воздухом в качестве источника кислорода.9. Способ по любому из пп.1-4 или 7, в котором используемый в указанном спо� РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (51) МПК C10G 2/00 (13) 2011 130 432 A (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21)(22) Заявка: 2011130432/04, 21.12.2009 (71) Заявитель(и): ВМ ГТЛ, ИНК. (US) Приоритет(ы): (30) Конвенционный приоритет: (72) Автор(ы): АЯССЕ Конрад (CA) 22.12 ...

使合成气和合成气衍生产物的产率最大化的气化系统和工艺

气化系统和方法。该系统可包括气化器和流体偶联到气化器的净化单元，该净化单元接收来自气化器的粗合成气并产生废气和合成气产物。该系统还可包括流体偶联到净化单元的第一重整器，该第一重整器接收所述废气的第一部分并产生重整烃。该系统可进一步包括第二重整器，其具有流体偶联到净化单元的第一入口、流体偶联到第一重整器的第二入口和流体偶联到净化单元的出口。该第二入口从第一重整器接收重整烃，该第一入口接收来自净化单元的所述废气的第二部分。第二重整器可产生导入净化单元的回收粗合成气。

The method of producing synthesis gas

РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2017 107 429 A (51) МПК C01B 3/24 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21)(22) Заявка: 2017107429, 07.03.2017 (71) Заявитель(и): ЛИНДЕ АКЦИЕНГЕЗЕЛЛЬШАФТ (DE) Приоритет(ы): (30) Конвенционный приоритет: 08.03.2016 DE 102016002728.2 25 R U (57) Формула изобретения 1. Способ получения углеводородов (23), согласно которому из содержащего углеводороды сырьевого потока (1) получают первый (3) и второй (4) частичные сырьевые потоки, при этом первый частичный сырьевой поток (3) превращают путем парциального окисления или автотермического риформинга (R) в первый поток синтезгаза (8), а второй частичный сырьевой поток (4) превращают посредством парового риформинга (D) во второй поток синтез-газа (10) и затем объединяют с первым потоком синтез-газа (8) с образованием третьего потока синтез-газа (5), по меньшей мере первую часть (11) которого посредством синтеза Фишера-Тропша (F) превращают в поток неочищенного продукта (16), содержащий углеводороды с разными длинами цепей, из которого легкие углеводороды отделяют в остаточный газ (17), чтобы вернуть их в процесс и использовать в парциальном окислении или автотермическом риформинге (R), отличающийся тем, что из по меньшей мере одной части (19) остаточного газа (17) выделяют ненасыщенные углеводороды (21), чтобы получить по существу не содержащий ненасыщенных углеводородов поток (20) для применения в качестве сырья для парциального окисления или автотермического риформинга (R). 2. Способ по п. 1, отличающийся тем, что ненасыщенные углеводороды (21), выделенные из по меньшей мере одной части (19) остаточного газа (17), используют в процессе для нижнего обогрева или выпускают как актив в качестве продукта для вторичной переработки или сжигания. 3. Способ по п. 1, отличающийся тем, что соотношение объемных расходов первого частичного сырьевого потока (3) и второго частичного сырьевого потока (4) регулируют так, чтобы установить соотношение ...