МНОГОСТАДИЙНЫЙ СПОСОБ ФИШЕРА-ТРОПША

Изобретение относится к многостадийному способу для производства углеводородных продуктов из сингаза, каждая стадия способа включает следующие этапы: 1) обеспечение одного или больше реакторов конверсии сингаза, в которых сингаз частично превращается в углеводородные продукты в условиях конверсии, 2) каждый реактор конверсии имеет систему входящего потока сингаза, каковая система объединяет два или более входящих потока сингаза и каковая система поставляет объединенный сингаз в реактор конверсии сингаза, при этом система входящего сингаза объединяет А) по меньшей мере, один входящий поток сингаза, являющийся потоком сингаза, полученного в процессе неполного окисления и имеющего отношение Н2/СО между 1,6 и 2,0 для первой стадии или В) выходящий поток сингаза из предыдущей стадии, отношение Н2/СО выходящего потока сингаза находится между 0,2 и 0,9, вместе с риформинговым сингазом, имеющим отношение Н2/СО, по меньшей мере, 3,0, для всех стадий, кроме первой стадии, с другим потоком сингаза ...

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

Изобретение относится к способу получения ацетилена и синтез-газа. Способ осуществляется путем частичного окисления углеводородов при помощи кислорода, причем первый исходный поток, содержащий один или несколько углеводородов, и второй исходный поток, содержащий кислород, отдельно друг от друга нагревают, смешивают в соотношении массовых потоков из второго исходного потока и первого исходного потока, соответствующем кислородному числу, меньше или равному 0,31, причем под кислородным числом понимают соотношение из фактически присутствующего во втором исходном потоке количества кислорода и стехиометрически необходимого количества кислорода, которое требуется для полного сгорания одного или нескольких углеводородов, содержащихся в первом исходном потоке, подают в камеру сгорания, где происходит частичное окисление этих углеводородов с получением первого потока крекинг-газа, при этом первый поток крекинг-газа в предварительном гашении в результате впрыскивания водной среды для гашения охлаждают ...

Способ получения синтез-газа

Изобретение относится к способу получения углеводородов. Способ осуществляют путем получения первого (3) и второго (4) частичных сырьевых потоков из содержащего углеводороды сырьевого потока (1). Причем первый частичный сырьевой поток (3) превращают путем парциального окисления или автотермического риформинга (R) в первый поток синтез-газа (8), а второй частичный сырьевой поток (4) превращают посредством парового риформинга (D) во второй поток синтез-газа (10). 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). При этом из по меньшей мере одной части (19) остаточного газа (17) выделяют ненасыщенные углеводороды ...

СПОСОБ ЧАСТИЧНОГО ОБОГАЩЕНИЯ ТЯЖЕЛОЙ НЕФТИ И БИТУМА

Изобретение относится к вариантам способа обогащения тяжелой нефти или битума с получением частично обогащенной синтетической неочищенной нефти, к способу синтеза частично обогащенной синтетической неочищенной нефти, к способу превращения тяжелой нефти или битума в транспортабельную частично обогащенную синтетическую неочищенную нефть и вариантам частично обогащенной синтетической неочищенной нефти. Один из вариантов способа обогащения тяжелой нефти или битума включает: (a) обеспечение источника тяжелой нефти или битума в качестве исходного сырья; (b) обработку исходного сырья в установке атмосферной дистилляции (ADU) с получением первой перегнанной фракции и, необязательно, обработку первой неперегнанной атмосферной остаточной фракции в вакуумно-дистилляционной установке (VDU) с получением второй перегнанной фракции и второй неперегнанной остаточной фракции; (c) необязательно, обработку первой неперегнанной остаточной фракции или второй неперегнанной остаточной фракции в установке деасфальтизации ...

СПОСОБ ПОЛУЧЕНИЯ ПАРАФИНОВОГО ПРОДУКТА

Настоящее изобретение относится к способу получения парафинового продукта из углеродсодержащего сырья. Способ включает частичное окисление углеродсодержащего сырья для получения смеси, содержащей водород и монооксид углерода, осуществление синтеза Фишера-Тропша с использованием полученной смеси и извлечение парафинового продукта и отходящего газа, гидрогенизацию по меньшей мере части отходящего газа из синтеза Фишера-Тропша, необязательно после удаления углеводородов, используя молярное отношение пар/отходящий газ в диапазоне от 0,5 до 1,5, и катализатор, содержащий медь и цинк, или катализатор, содержащий медь, цинк и марганец, превращение по меньшей мере части образовавшегося газа, используя катализатор на основе никеля, который содержит не более 0,2 масс. % кобальта, не более 0,2 масс. % железа и не более 0,2 масс. % рутения, в расчете на общую массу катализатора, и получение водородсодержащего газа из по меньшей мере части полученного газа, используя процесс риформинга, процесс парового ...

СПОСОБ ПОЛУЧЕНИЯ СИНТЕЗ-ГАЗА ДЛЯ ПРОИЗВОДСТВА АММИАКА С ИСПОЛЬЗОВАНИЕМ ВЫСОКОТЕМПЕРАТУРНОЙ КОНВЕРСИИ И НИЗКОЙ ВЕЛИЧИНЫ ОТНОШЕНИЯ КОЛИЧЕСТВА ВОДЯНОГО ПАРА К КОЛИЧЕСТВУ УГЛЕРОДА

Настоящее изобретение относится к риформингу углеводородов с целью подготовки синтез-газа для производства аммиака. Способ получения синтез-газа для производства аммиака из содержащего углеводороды сырья во входной части установки включает стадии: конверсии указанного сырья с водяным паром с получением синтез-газа, содержащего водород, оксид углерода и диоксид углерода; обработки указанного синтез-газа, включая конверсию оксида углерода и последующее удаление диоксида углерода, причем конверсия синтез-газа включает стадию высокотемпературной конверсии с использованием катализатора на основе железа; общая величина молярного отношения водяного пара к углероду во входной части не выше 2,6; и в котором указанная конверсия с водяным паром включает: первую стадию конверсии, включающую первичную конверсию с водяным паром, обеспечивая, таким образом, получение после конверсии первого газа; вторую стадию конверсии с использованием потока оксиданта, обеспечивая, таким образом, получение синтез-газа ...

СПОСОБ ПОЛУЧЕНИЯ СИНТЕЗ-ГАЗА ДЛЯ СИНТЕЗА АММИАКА

Изобретение относится к области химии. Способ получения синтез-газа для синтеза аммиака включает подачу газового потока, содержащего углеводороды, и газового потока, содержащего пар, в установку первичной конверсии, оборудованную множеством катализаторных труб с внешним обогревом, реакцию этих углеводородов с паром в катализаторных трубах установки первичной конверсии при рабочем давлении в них по меньшей мере 45 бар с получением продуктового газа, подачу продуктового газа и потока окислительного газа в установку вторичной конверсии, реакцию продуктового газа с окислительным газом и последующую вторичную конверсию с обеспечением конверсии всех углеводородов, содержащихся в продуктовом газе, выходящем из установки первичной конверсии, и с получением конвертированного газа, содержащего водород, оксиды углерода и непрореагировавший пар, удаление оксидов углерода из конвертированного газа и получение синтез-газа, пригодного для синтеза аммиака. В качестве окислительного газа используют обогащенный ...

ДВУХСТУПЕНЧАТЫЙ ГАЗОГЕНЕРАТОР И СПОСОБ ГАЗИФИКАЦИИ С УНИВЕРСАЛЬНОСТЬЮ ОТНОСИТЕЛЬНО ПЕРЕРАБАТЫВАЕМОГО СЫРЬЯ

Изобретение относится к процессам газификации и может применяться для преобразования твердых или суспендированных сырьевых материалов, таких как уголь, нефтяной кокс и нефтяные остатки, в синтез-газ. Способ газификации включает (а) введение жидкого углеводородного сырьевого материала и по меньшей мере одного из сухого сырьевого материала или первого суспендированного сырьевого материала в нижнюю секцию реактора, причем по меньшей мере один из сухого сырьевого материала или первого суспендированного сырьевого материала вводится через два основных питательных сопла, тогда как жидкий углеводородный сырьевой материал вводится по меньшей мере через два дополнительных питательных сопла; (b) частичное сгорание сырьевых материалов в нижней секции реактора с газовым потоком, включающим кислородсодержащий газ или пар, для выделения тепла и образования продуктов, содержащих горячий синтез-газ; (с) пропускание указанного горячего синтез-газа из стадии (b) вверх в верхнюю секцию реактора; и (d) ведение ...

СПОСОБ ОЧИСТКИ СИНТЕЗ-ГАЗА, СОДЕРЖАЩЕГО ВОДОРОД И ПРИМЕСИ

СПОСОБ ОЧИСТКИ ТЯЖЕЛОЙ НЕФТИ И БИТУМА

МОДИФИЦИРОВАННЫЙ ПРОЦЕСС С ИСПОЛЬЗОВАНИЕМ ГАЗОВОЙ И ПАРОВОЙ ТУРБИНЫ С ИНТЕГРИРОВАННОЙ ГАЗИФИКАЦИЕЙ УГЛЯ ПОД ДАВЛЕНИЕМ

... 1. Способ получения и сжигания синтез-газа путем газификации с помощью воздуха, или кислорода, или обогащенного кислородом воздуха с возможной долей водяного пара, где ! - твердое или жидкое топливо подают в реактор, в котором топливо преобразуется с помощью воздуха, или кислорода, или обогащенного кислородом воздуха, а также водяного пара при повышенной температуре в синтез-газ, который в существенной степени состоит из водорода и окиси углерода, и ! - при реакции возникают капельки минеральных шлаков, которые выводятся из реактора вместе с полученным синтез-газом, при этом ! - синтез-газ без предварительного охлаждения направляют в отделяющее шлаки устройство, в котором капельки шлаков агломерируют и отделяются в виде жидких шлаков, и содержащиеся в синтез-газе парообразные щелочи, а также хлористый водород удаляют из синтез-газа за счет приведения в контакт с газопоглотительной керамикой, ! отличающийся тем, что ! - синтез-газ после очистки пропускают через турбодетандер, в котором энергия ...

СПОСОБ И СИСТЕМА ДЛЯ ПРОИЗВОДСТВА ЖИДКОГО УГЛЕВОДОРОДНОГО ПРОДУКТА С ПОМОЩЬЮ ПРОЦЕССА ФИШЕРА-ТРОПША С ИСПОЛЬЗОВАНИЕМ СИНТЕЗ-ГАЗА, ПРОИЗВЕДЕННОГО В РЕАКТОРЕ РИФОРМИНГА НА ОСНОВЕ МЕМБРАНЫ ТРАНСПОРТА КИСЛОРОДА

СИСТЕМА ДЛЯ ПРОИЗВОДСТВА АРОМАТИЧЕСКОГО СОЕДИНЕНИЯ И СПОСОБ ЕГО ПОЛУЧЕНИЯ

ВОССТАНОВЛЕНИЕ ОКСИДА ЖЕЛЕЗА ДО МЕТАЛЛИЧЕСКОГО ЖЕЛЕЗА С ПРИМЕНЕНИЕМ ПРИРОДНОГО ГАЗА

СПОСОБЫ ГАЗИЦИКАЦИИ УГЛЕРОДСОДЕРЖАЩИХ МАТЕРИАЛОВ

... 1. Способ газификации углеродсодержащих материалов в газогенераторе с образованием газа, содержащего монооксид углерода, водород и деготь;причем указанный способ включает: загрузку одного или более углеродсодержащих материалов, подачу газа, содержащего молекулярный кислород, подачу метансодержащего газа и необязательно воды или водяного пара в указанный газогенератор;причем общее количество кислорода, подаваемого в указанный газогенератор, составляет более примерно 0,75 фунта на фунт общего количества углерода, загруженного в указанный газогенератор.2. Способ по п.1, в котором общее количество кислорода, подаваемое в указанный газогенератор, составляет примерно 0,75-3,0 фунта на фунт общего количества углерода, загруженного в указанный газогенератор.3. Способ по п.1, в котором указанный метансодержащий газ включает один или более газов, которые выбирают из: алканов, алкенов, алкинов, газа из органических отходов, биогаза, газа из реактора ферментативного разложения и природного газа.4.

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 ...

СПОСОБ ПОЛУЧЕНИЯ ПАРАФИНОВОГО ПРОДУКТА

... 1. С п п п и у с в с с(a) о ч о у с д п с с в и м у(b) о с ФТ с и с п н с (а, и и п п и о г и с ФТ(c) п м м ч о г и с ФТ н п у у п г и м о по г в д о 0,5 д 1,5, и к с м и ц и к с м ц и м(d) п м м ч г о н с (с, п п и к н о н к с н б 0,2 м % к н б 0,2 м % ж и н б 0,2 м % р в р н о м к и(e) п в г и п м м ч г о н с (d), п и п р б п и п п р е б п с и п р м с в п п а п р п п р с о н и а п п р н п с и п а п р и п р м с в п2. С п п 1, в к м о по г н с (с н в д о 0,7 д 1,5, п о 0,8 д 1,2.3. С п п 1, в к т н в в р и н с (с г н в д о 200 д 300С п о 220 д 270С4. С п п 1, в к с (с г п с и д и б п р5. С п п 1, в к т н в в р и н с (d), н в д о 300 д 500С п о 350 д 500С б п о 350 д 400С6. С п п 1, в к м о пс г и д с (d), н в д о 0,5 д 1,5, п о 0,7 д 1,5, б п о 0,8 д 1,2.7. С п л и п 1-6, в к п с (b) и д с (с и о г с ФТ у у8. С п п 7, в к у и о г с ФТ у пI) к п м м ч о г и с ФТ к с в м у д у а и Cу н п о с п ж в сII) у п ж и п м м ч Cу вп и с с с I);III) у о о г в о п и с с с I);IV) о с с п м м ч п ...

Behandlung von Synthesegas

PrOx-Reaktor und Brennstoffzellenanordnung mit PrOx-Reaktor

Die Erfindung betrifft einen PrOx-Reaktor (R), umfassend ein einen Reaktionsraum einschließendes Gehäuse mit einem ersten Einlass (E1) zum Zuführen eines wasserstoffhaltigen ersten Gases (G1) in einen Reaktionsraum, einem zweiten Einlass (E2) zum Zuführen eines sauerstoffhaltigen zweiten Gases (G2) in den Reaktionsraum und einem Auslass (A) zur Ausgabe eines dritten Gases (G3), wobei sich vom zweiten Einlass (E2) eine Vielzahl von Leitungen (Kv) in den Reaktionsraum erstrecken, von denen jede zumindest eine Öffnung (O) zum Zuführen des zweiten Gases (G2) in den Reaktionsraum umfasst.

Brenner zur Synthesegaserzeugung

Brenner zur Herstellung von Synthesegas durch partielle Oxidation von flüssigen oder gasförmigen, kohlenstoffhaltigen Brennstoffen in Gegenwart eines sauerstoffhaltigen Oxidationsmittels und eines Moderators, enthaltend Wasserdampf und/oder Kohlendioxid, mit- Mitteln zum getrennten Zuführen des kohlenstoffhaltigen Brennstoffs, des sauerstoffhaltigen Oxidationsmittels und des Moderators,- einem zentralen, einen kreisförmigen Querschnitt aufweisenden, ersten Zufuhrkanal für das sauerstoffhaltige Oxidationsmittel,- einem den ersten Zufuhrkanal koaxial und konzentrisch umgebenden, zweiten Zufuhrkanal, wobei zwischen der Außenwand des ersten Zufuhrkanals und der Innenwand des zweiten Zufuhrkanals ein Ringspalt gebildet wird, durch den der Moderator zugeführt wird,- einem den zweiten Zufuhrkanal koaxial und konzentrisch umgebenden, dritten Zufuhrkanal, wobei zwischen der Außenwand des zweiten Zufuhrkanals und der Innenwand des dritten Zufuhrkanals ein Ringspalt gebildet wird, durch den der Brennstoff ...

Verfahren zum Regenerieren eines Reformers

Verfahren zum Regenerieren eines Reformers, dem im kontinuierlichen Betrieb Brennstoff (12, 14) und Oxidationsmittel (16, 18, 20) zugeführt wird, wobei die Zuführrate des Brennstoffs (12, 14) zum Zwecke der Regeneration gegenüber der Zuführrate im kontinuierlichen Betrieb herabgesetzt wird, die Zuführrate des Brennstoffs (12, 14) während mehrerer aufeinanderfolgender Zeitintervalle gegenüber der Zuführrate im kontinuierlichen Betrieb herabgesetzt ist und zwischen den aufeinanderfolgenden Zeitintervallen die Zuführrate des Brennstoffs (12, 14) größer ist als während der aufeinanderfolgenden Zeitintervalle, dadurch gekennzeichnet, dass der Reformer zwei Brennstoffzuführungen aufweist, wobei eine der Brennstoffzuführungen während der Regeneration mit einer Zuführrate arbeitet, die der Zuführrate im kontinuierlichen Betrieb im Wesentlichen entspricht.

Flugstromvergaser mit Kühlschirm und Wellrohrkompensator

Reaktor zur Vergasung von festen und flüssigen Brennstoffen im Flugstrom bei Temperaturen zwischen 1.200 und 1.900°C und Drucken zwischen Umgebungsdruck und 10 MPa (100 bar), wobei feste Brennstoffe staubfein aufgemahlene Kohlen unterschiedlichen Inkohlungsgrades, Petrolkokse oder andere feste kohlenstoffhaltige Stoffe sind und flüssige Brennstoffe Öle oder Öl-Feststoff- oder Wasser-Feststoff-Suspensionen sein können mit einem freien Sauerstoff enthaltenden Oxidationsmittel, wobei der Reaktor einen Kühlschirm (8) und einen Druckmantel (4) aufweist, der Kühlschirm über einen Wellrohrkompensator (7) mit dem Druckmantel zur Aufnahme von Längenänderungen in Richtung der Zentralachse des Reaktors gasdicht verbunden ist, dadurch gekennzeichnet, dass der Ringspalt (5) zwischen Druckmantel und Kühlschirm mit Gas beaufschlagbar ist und der Wellrohrkompensator die Brennervorrichtung (3) konzentrisch umschließt.

Kontinuierliche Rußwasserbehandlung

Verfahren zur kontinuierlichen Behandlung von Rußwasser, das bei einer Vergasung von schwermetallhaltigen flüssigen Kohlenwasserstoffen anfällt. Das Rußwasser wird ohne Zugabe von Hilfsstoffen in einer Vorentwässerungsstufe auf bis zu 10% Feststoffgehalt zentrifugiert, wobei ein pastöser, schwermetallreicher Rußschlamm erhalten wird und ein schwermetallarmes Zentrat anfällt, welches als Nutzwasser wieder in den Vergasungsprozess zurückgeführt wird.

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.

Energy conversion process for sequestration of carbon dioxide

An energy conversion process that also exports by-product CO2 at elevated pressure where a fuel gas feed stream is mixed with a reactant stream and additional CO2 is added to at least part of, the fuel gas feed stream, the reactant stream or both through desorption by contacting with a CO2-rich solvent stream in a first stage contactor to produce a mixed feed gas stream and a CO2-lean solvent stream; passing said mixed feed gas stream to a chemical conversion step, where further CO2 is produced; chilling at least part of the products of said chemical conversion step, at a pressure of at least 10 bar to condense and partially remove CO2 as a liquid and thereby produce a CO2-lean gas stream; and passing at least part of said CO2-lean gas stream said to a second stage contactor where further CO2 is removed, by absorption in a solvent stream lean in CO2 derived from said CO2-lean solvent stream, to produce a product gas stream and a solvent stream rich in CO2 from which said CO2-rich solvent ...

Gas-to-liquid technology

Process for conversion of LPG and CH4 to syngas and higher valued products

A device for producing a reducing gas in particular a shielding gas

... An apparatus for making a reducing gas comprises a combustion chamber 1, in which a carbonaceous fuel is burnt, a heat exchanger 10, 22 for the combustion products, and a catalytic carbon monoxide converter 18 for the cooled products, the apparatus comprising a structural unit. Combustion products enter at 7 a space 21, where they are cooled to about 900 DEG C., before entering an annular space 22 where cooling to 350 DEG C. takes place. The cooled products enter the converter 18 at 23 and flow down in contact with catalyst-containing tubes 6 which they enter at the lower ends. Converted gas leaves at 26, and unconverted gas may be taken off at 27. Cooling air enters at 8 and leaves at 13, passing up the annular space 10 which surrounds the space 21, 22. The air which enters at 8 may be preheated by heatexchange with the converted gas and by a burner, see Fig. 4 (not shown). Water or steam for the conversion reaction may be added to the fuel-air mixture before the ...

PRODUCTION OF SYNTHESIS GAS

Steam Reforming of Hydrocarbons

... 1,159,247. Making combustible gas. MONTECATINI EDISON S.p.A. 15 Aug., 1966 [18 Aug., 1965], No. 36468/66. Heading C5E. A combustible gas containing H 2 and CO is made by steam-reforming one stream of a liquid or gaseous hydrocarbon, e.g. in tubes 1, which may contain a catalyst, and partially combusting another stream of the hydrocarbon, e.g. at Al, the heat for the reforming being supplied by heat exchange in counter-current with the mixed products 3 of the reforming and combustion reactions. Steam may be present in the partial combustion reaction, and both reactions are performed at the same pressure.

Process

Methods and systems for gasification of hydrocarbonaceous feedstocks

PROCESS FOR THE PREPARATION OF HYDROCARBONS

... 1523463 Hydrocarbon synthesis SHELL INTERNATIONALE RESEARCH MAATSCHAPPIJ BV 23 Oct 1975 [25 Oct 1974] 43597/75 Heading C5E In a process for the preparation of normally liquid hydrocarbons, a hydrogen- and carbon monoxide-containing gas is prepared by the partial combustion of a carbonaceous material with oxygen which is at a temperature in the range 200‹ to 500‹ C., the partial combustion being carried out in the presence of 5-15% by volume of steam (based on oxygen) at a temperature in the range 900‹ to 1800‹ C., a pressure in the range 1 to 200 bar abs. and a residence time in the range 0À1 to 12 seconds, the resulting gas is contacted with steam in a plurality of stages, in which the temperature of the first stage is in the range 250‹ to 450‹ C. and the temperature in the last stage is in the range 200‹ to 400‹ C. to convert carbon monoxide into carbon dioxide and hydrogen, the resulting gas is cooled at a pressure in the range 1 to 200 bar abs. to a temperature in the range -10‹ to ...

Process for co-producing synthesis gas and power.

Process for co-producing synthesis gas and power

CONVERSION OF CARBON CONTAINING FEEDSTOCK

Process for preparing a paraffin product

Process for co-producing synthesis gas and power.

Co-production of methanol and urea

Conversion of carbon containing feedstock.

Conversion of carbon containing feedstock.

Process for preparing a paraffin product

Process for preparing a paraffin product

Process for co-producing synthesis gas and power.

Co-production of methanol and urea

Conversion of carbon containing feedstock.

Co-production of methanol and urea

SYSTEMS FOR THE SHIFTING FROM FUEL AND AIR TO REFORMAT

PROCEDURE FOR THE PRODUCTION OF METHANOL, OLEFINEN AND HYDROCARBONS

HOLLOW ORGANIC/INORGANIC COMPOUND MATERIAL FIBERS, SINTERING FIBERS, MANUFACTURING PROCESSES FOR THE FIBERS, GAS SEPARATION MODULES WITH THE FIBERS AND PROCEDURES FOR THE USE OF THE MODULES

PRODUCTION OF HYDROGEN

CHANGE IN PRESSURE ADSORPTION PROCESS WITH SEVERAL ADSORPTION BEDS

Procedure and device for the continuous production of aqueous solutions with a content of active chlorine.

Procedure for the distance of carbon dioxide from gas mixtures

Micro-scale process for the direct production of liquid fuels from gaseous hydrocarbon resources

An easily transportable micro-scale process is described for the direct production of liquid fuels from flare gas, biogas, stranded natural gas, natural gas emissions from methane hydrate dissociation, and other low-volume, gas-phase hydrocarbon resources. The process involves the design of an integrated series of tubular catalytic reactors in which each consecutive catalytic reactor in the series has been designed with larger volumes of catalyst so that a single pass efficiency of about 90% or greater is achieved while keeping the temperatures and pressures of each reactor similar and without requiring tailgas recycling to the reactors. Typically, the process employs a direct fuel production catalyst that produces undetectable, detrimental carboxylic acids in the fuel and catalyst reaction water. As a result, the directly produced, premium fuels are non- corrosive and do not degrade during long-term storage.

This is a method of producing Hydrogen gas using low grade forms of coal, in particular Lignite. The method makes use of the chemical reactivity of the Lignite. By using certain catalytic compounds at low temperatures facilitates the release of Hydrogen gas. It is carried out at low temperatures using the chemical process which in turn uses a catalysing compound (ferrite and other catalytic additives) to produce an exothermic reaction. This reaction produces the Hydrogen in large quantities.

Abstract This is a method of producing Hydrogen gas using low grade forms of coal, in particular Lignite. The method makes use of the chemical reactivity of the Lignite. By using certain catalytic compounds at low temperatures facilitates the release of Hydrogen gas. It is carried out at low temperatures using the chemical process which in turn uses a catalysing compound (ferrite and other catalytic additives) to produce an exothermic reaction. This reaction produces the Hydrogen in large quantities.

INTEGRATION OF HYDROGEN LIQUEFACTION WITH GAS PROCESSING UNITS

Abstract A method of liquefying hydrogen, including dividing a hydrogen stream into at least a first fraction and a second fraction, introducing the first fraction into a refrigeration cycle of a hydrogen liquefaction unit, thereby liquefying a product hydrogen stream, withdrawing one or more warm hydrogen stream(s) from the hydrogen liquefaction unit, and returning the one or more warm hydrogen stream to the hydrogen stream, wherein the second fraction is combined with a high-pressure nitrogen stream to form an ammonia synthesis gas stream.

Reformer

Entrained-flow gasifier with cooling screen and bellows compensator

ENTRAINED-FLOW GASIFIER WITH COOLING SCREEN AND BELLOWS COMPENSATOR Abstract In a reactor for the gasification of solid and liquid fuels in the entrained flow at temperatures between 1200 and 1900 *C and pressures between ambient pressure and 10 MPa with an oxidizing agent containing free oxygen, the cooling screen is connected in a gas-tight manner to the pressure shell via a bellows compensator to accommodate linear 5 deformation. Continuous sweeping by gas of the annular gap between pressure shell and cooling screen is unnecessary and backflow by producer gas is prevented. to Fig. 1 TRN- R6RQRQ pilot burner gas 51---6 ...

Reducing gas generators and methods for generating reducing gas

One embodiment of the present invention is a unique reducing gas generator. Another embodiment is a unique method for generating a reducing gas. Other embodiments include apparatuses, systems, devices, hardware, methods, and combinations for generating reducing gas. Further embodiments, forms, features, aspects, benefits, and advantages of the present application will become apparent from the description and figures provided herewith.

Reducing gas generators and methods for generating reducing gas

One embodiment of the present invention is a unique reducing gas generator. Another embodiment is a unique method for generating a reducing gas. Other embodiments include apparatuses, systems, devices, hardware, methods, and combinations for generating reducing gas. Further embodiments, forms, features, aspects, benefits, and advantages of the present application will become apparent from the description and figures provided herewith.

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.

Maintaining low carbon monoxide levels in product carbon dioxide

A process for maintaining a low carbon monoxide content in a carbon dioxide product that is made in a synthesis gas purification process is disclosed. More particularly, the invention involves an improved process in which a portion of a loaded solvent is sent through a carbon dioxide absorber instead of to a series of carbon dioxide flash drums.

METHOD TO CONTROL A PROCESS

Control of a process

Process and plant for at least partial gasification of solid organic input material

A process (100) is proposed for at least partial gasification of solid organic input material (A), in which a tar-containing carbonization gas (B) is obtained from the input material (A) by carbonization in a low-temperature gasifier (1), and the carbonization gas (B) is then converted to a synthesis gas (D) by partial oxidation and subsequently partial reduction in a high-temperature gasifier (2). The carbonization gas (B) is contacted with a fraction of the synthesis gas (D) and/or of a gas mixture (E) diverted from the synthesis gas (D). The invention likewise provides a plant (10) set up for performance of the process (1).

A process for producing ammonia synthesis gas with high temperature shift and low steam-to-carbon ratio

A process for producing ammonia synthesis gas from a hydrocarbon-containing feedstock in a front-end, comprising the steps of steam reforming of said feedstock, obtaining a synthesis gas comprising hydrogen, carbon monoxide and carbon dioxide; a treatment of said synthesis gas including shift of carbon monoxide and subsequent removal of carbon dioxide, wherein the shift of the synthesis gas includes high-temperature shift with an iron-based catalyst and at a temperature greater than 300 °C and the global steam-to-carbon ratio of the front end is 2.6 or less; a corresponding plant and a method for revamping a front-end of an ammonia plant are also disclosed.

Process for the production of synthesis gas

A process for the manufacture of synthesis gas by partial oxidation of a liquid hydrocarbon-containing fuel using multi-orifice (co-annular) burner

Improved molten metal decomposition apparatus and process

PARTIAL OXIDATION REFORMER-REFORMING EXCHANGER ARRANGEMENT

Low-energy hydrogen production is disclosed. A reforming exchanger is placed in parallel with a partial oxidation reactor in a new hydrogen plant with improved efficiency and reduced steam export, or in an existing hydrogen plant where the hydrogen capacity can be increased by as much as 20-30 percent with reduced export of steam from the hydrogen plant.

COBALT-MOLYBDENUM SULFIDE CATALYST MATERIALS AND METHODS FOR ETHANOL PRODUCTION FROM SYNGAS

The present invention provides methods and compositions for the chemical conversion of syngas to alcohols. The invention includes catalyst compositions, methods of making the catalyst compositions, and methods of using the catalyst compositions. Certain embodiments teach compositions for catalyzing the conversion of syngas into products comprising at least one C1-C4 alcohol, such as ethanol. These compositions generally include cobalt, molybdenum, and sulfur. Preferred catalyst compositions for converting syngas into alcohols include cobalt associated with sulfide in certain preferred stoichiometries as described and taught herein.

PROCESS FOR THE PRODUCTION OF HYDROGEN AND CARBON DIOXIDE

This present invention provides a method to more efficiently recover hydrogen and carbon dioxide, preferably at least 50%, even more preferably at least 75%, and most preferably at least 90% of the carbon dioxide. The present invention further provides the design for capture of at least 80%, carbon dioxide from syngas that allows for the simultaneous production of medium to high amounts of hydrogen in the syngas as a part of the production of hydrogen in a hydrogen generation plant. By using the process of the present invention, especially in terms of a hydrogen generation plant, it is possible to increase recovery of hydrogen and capture of the carbon dioxide in the syngas stream by balancing the recycle of the hydrogen rich permeate from the hydrogen membrane separation units to the process unit and/or the water gas shift as capacity allows when a carbon dioxide separation unit, a carbon dioxide membrane separation unit and two hydrogen membrane separation units are utilized.

PROCESS FOR THE PRODUCTION OF HYDROGEN AND CARBON DIOXIDE

This present invention provides a method to more efficiently recover hydrogen and carbon dioxide, preferably at least 50%, even more preferably at least 75%, and most preferably at least 90% of the carbon dioxide. The present invention further provides the design for capture of at least 80%, carbon dioxide from syngas that allows for the simultaneous production of medium to high amounts of hydrogen in the syngas as a part of the production of hydrogen in a hydrogen generation plant. By using the process of the present invention, especially in terms of a hydrogen generation plant, it is possible to increase recovery of hydrogen and capture of the carbon dioxide in the syngas stream by balancing the recycle of the hydrogen rich permeate from the hydrogen membrane separation units to the process unit and/or the water gas shift as capacity allows when a carbon dioxide separation unit, a carbon dioxide membrane separation unit and two hydrogen membrane separation units are utilized.

PROCESS AND APPARATUS FOR REFORMING HYDROCARBONS

The invention relates to a process and apparatus for the production of synthesis gas from a hydrocarbon feedstock in a heat exchanger reformer, wherein a cooling medium is added to the heat exchange reformer.

SYSTEMS FOR REACTING FUEL AND AIR TO A REFORMATE

The invention relates to a system for reacting fuel (216) and air (218) to a reformate (220). Said system comprises a reformer (214) including a reaction chamber, a nozzle (11) for supply a fuel/air mixture to the reaction chamber, at least one supply line (24) for supplying fuel (216) to the nozzle (11) and at least one entrance channel (18) for supplying air (218) to the nozzle (11). According to the invention, the nozzle (11) comprises a swirl chamber (19, 22) into which the at least one supply line (24) for supplying fuel (216) runs in a substantially axial/central manner and the at least one entrance channel (18) runs in a substantially tangential manner and from which a nozzle outlet (23) exits. The swirl chamber (19, 22) comprises a narrowing spiral channel (19) into which the entrance channel (18) for the gaseous medium runs, and a space (22) axially contiguous thereto in the direction toward the nozzle outlet (23), into which the supply line (24) for supplying fuel (216) runs and ...

REFORMER AND METHOD FOR CONVERTING FUEL AND OXIDANT TO REFORMATE

The invention relates to a reformer for reacting fuel (12) and oxidant (16, 18, 20) to reformate (22). Said reformer comprises an oxidizing zone (24) and a reforming zone (26). A mixture of fuel (12) and oxidant (16, 18, 20) is delivered to the oxidizing zone (24) and is delivered at least in part to the reforming zone (26) following at least partial oxidation of the fuel (12). According to the invention, fuel (14) can be additionally delivered to the reforming zone (26) while heat (28) can be supplied to the reforming zone (26). The invention further relates to a method for reacting fuel (12) and oxidant (16, 18, 20) to reformate (22).

ENERGY DISTRIBUTION NETWORK

An energy distribution network for providing hydrogen fuel to a user comprising; energy source means; hydrogen production means to receive the energy from the energy resource means; hydrogen fuel user means to receive hydrogen from the hydrogen production means; and data collection, storage, control and supply means linked to the energy resource means, the hydrogen production means, and the hydrogen fuel user means to determine, control and supply hydrogen from the hydrogen production means. Preferably, the network comprises one or more water electrolysers and provides for the distribution of hydrogen, for use as a fuel for vehicles, fuel cells, electrical and thermal generators, and the like.

DIESEL FUEL BLENDS WITH IMPROVED PERFORMANCE CHARACTERISTICS

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.

METHOD FOR PARTIAL DECARBONIZATION OF HYDROCARBON FUELS ON BOARD COMBUSTION-BASED TRANSPORTATION VEHICLES TO REDUCE CO2 EMISSIONS

... ²²²A method and apparatus for the reduction of carbon dioxide emissions by the on-²board treatment of a portion or all of the hydrocarbon fuel used to power an ²internal combustion engine mounted in a conventional transportation vehicle, ²utilize known decarbonization technology to break the fuel's hydrogen-carbon ²bond. The compounds are then cooled and separated into (1) elemental carbon ²powder that is stored on-board for later recovery and industrial use, and (2) ²hydrogen, or a hydrogen-rich gas stream, that is burned as a fuel in the ICE ²and/or diverted to other on-board energy related applications.² ...

FUEL CELL SYSTEM

The invention relates to a fuel cell system comprising: a reformer (26) a nd an afterburner (48), both being used to convert at least fuel and oxidant ; and a fuel supply device (10) for providing the reformer (26) and the afte rburner (48) with fuel. In a particularly advantageous embodiment, at least one flow controller valve (16, 20) for controlling the fuel supply is connec ted upstream of the reformer (26) or afterburner (48). The invention also re lates to a motor vehicle comprising a fuel cell system of this type.

FUEL CELL SYSTEM

The invention relates to a fuel cell system comprising: a fuel cell (26), to the anode side of which a gas containing hydrogen and to the cathode sid e of which an oxidant can be fed in order to be converted into anode exhaust gas and cathode exhaust gas in the fuel cell (26); an afterburner (36), to which the anode exhaust gas can be fed; and a heat exchanger (46), to which the exhaust gases of the afterburner (36) can be fed and with which the oxid ant that is fed to the cathode side of the fuel cell (26) can be pre-heated. According to the invention, the cathode exhaust gas can be fed to the heat exchanger (46) upstream of the afterburner (36) via a cathode exhaust gas le g (44). The invention also relates to a motor vehicle comprising a fuel cell system of this type.

ENTRAINED-FLOW GASIFIER WITH COOLING SCREEN AND BELLOWS COMPENSATOR

In a reactor for the gasification of solid and liquid fuels in the entrained flow at temperatures between 1200 and 1900 .degree.C and pressures between ambient pressure and 10 MPa with an oxidizing agent containing free oxygen, the cooling screen is connected in a gas-tight manner to the pressure shell via a bellows compensator to accommodate linear deformation. Continuous sweeping by gas of the annular gap between pressure shell and cooling screen is unnecessary and backflow by producer gas is prevented.

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 ...

PROX REACTOR AND FUEL CELL ARRANGEMENT COMPRISING PROX REACTOR

The invention relates to a PrOx reactor (R) comprising a housing that encloses a reaction space and has a first inlet (E1) for supply of a hydrogenous first gas (G1) to a reaction space, a second inlet (E2) for supply of an oxygenous second gas (G2) to the reaction space and an outlet (A) for discharge of a third gas (G3), wherein there is a multitude of conduits (Kv) extending from the second inlet (E2) into the reaction space, each of which comprises at least one opening (0) for supply of the second gas (G2) to the reaction space.

SYSTEM AND METHOD FOR REDUCING IRON OXIDE TO METALLIC IRON USING NATURAL GAS

In various exemplary embodiments, the present invention provides systems and methods that can convert clean or raw natural gas, clean or dirty coke oven gas, or the like to reducing gas/syngas suitable for direct reduction with minimal processing or cleaning. Hydrocarbons and the like are converted to H2 and CO. S does not affect the conversion to reducing gas/syngas, but is removed or otherwise cleaned up by the iron bed in the direct reduction shaft furnace. Top gas may be continuously recycled or a once-through approach may be employed.

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.

MODIFIED GAS AND STEAM TURBINE PROCESS HAVING INTEGRATED COAL GASIFICATION UNDER PRESSURE

The invention relates to a method for producing, purifying, and burning syngas for generating electrical energy. The syngas is generated from a solid, carbonaceous fuel using an oxygenic gas and purified by slag extraction and alkali extraction. After purifying, the syngas produced enters an expansion turbine, where the pressure energy is used for generating electricity. The expansion turbine is protected against corrosion and mechanical attack by the purification and alkali separation. The expanded syngas is then burned under pressure, and the combustion is used for generating electricity in a combined cycle process using a gas turbine, steam generation, and a steam turbine. The process thus has a high level of efficiency. The invention further relates to a device for performing the method according to the invention.

METHODS FOR GASIFICATION OF CARBONACEOUS MATERIALS

The present disclosure is generally directed to process of gasification of carbonaceous materials to produce synthesis gas or syngas. The present disclosure provides improved methods of gasification comprising adding a molecular oxygen- containing gas and optionally adding water into said gasifier. This disclosure is also directed to process of production of one or more alcohols from said syngas via fermentation or digestion in the presence of at least one microorganism.

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.

CO-PRODUCTION OF METHANOL AND UREA

Process for the co-production of methanol and urea from a hydrocarbon feed without venting large amounts of carbon dioxide to the atmosphere.

GASIFIER FLUIDIZATION

A method of producing synthesis gas by introducing a feed material to be gasified into a gasification apparatus comprising at least one fluidized component operable as a fluidized bed, wherein the gasification apparatus is configured to convert at least a portion of the feed material into a gasifier product gas comprising synthesis gas; and maintaining fluidization of the at least one fluidized component by introducing a fluidization gas thereto, wherein the fluidization gas comprises at least one component other than steam. A system for producing synthesis gas is also provided.

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.

IMPROVED MOLTEN METAL DECOMPOSITION APPARATUS AND PROCESS

Baffles can form a chimney-effect separating the vapor space near the center of the bath. Flow through the chimney is aided by thermal convection and, optionally, by a differential pressure between the portions of the bath on either side of the baffle-chimney arrangement. Feed is added to the feed zone and oxygen is added to the oxidation zone, emitting H2 from the feed zone and CO from the oxidation zone. Products can be mixed as syngas feed for Fischer-Tropsch synthesis. Additionally, the Boudouard endothermic reaction (CO2 + C -> 2CO) can be used to control temperatures by injecting CO2 in place of oxygen. A plural zone plant and process for converting a hydrocarbon feed (e.g. coal, automobile tires, hazardous organic wastes, such as polyhalogenated organics, organic polymers, garbage, and other hydrocarbons) to synthesis gas comprising carbon monoxide and hydrogen is disclosed. The feed is contacted with a molten bath, which can comprise iron in an oxygen deficient zone at one pressure ...

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.

Method Of Operating A Fuel Processor

In situations where the demand for syngas is prolonged, a fuel processor is operated continuously to provide a syngas stream for a prolonged period. The equivalence ratio of reactants supplied to the fuel processor is controlled so that a high fuel-conversion efficiency to hydrogen and carbon monoxide is obtained at temperatures correspondent to carbon production balance, where carbon is formed and gasified at approximately the same rate in the fuel processor.

Process and System For Producing Liquid Fuel From Carbon Dioxide And Water

A process and system for producing high octane fuel from carbon dioxide and water is disclosed. The feedstock for the production line is industrial carbon dioxide and water, which may be of lower quality. The end product can be high octane gasoline, high cetane diesel or other liquid hydrocarbon mixtures suitable for driving conventional combustion engines or hydrocarbons suitable for further industrial processing or commercial use. Products, such as dimethyl ether or methanol may also be withdrawn from the production line. The process is emission free and reprocesses all hydrocarbons not suitable for liquid fuel to form high octane products. The heat generated by exothermic reactions in the process is fully utilized as is the heat produced in the reprocessing of hydrocarbons not suitable for liquid fuel.

Process For The Production Of Hydrogen And Carbon Dioxide

This present invention provides a method to more efficiently recover hydrogen and carbon dioxide, preferably at least 50%, even more preferably at least 75%, and most preferably at least 90% of the carbon dioxide. The present invention further provides the design for capture of at least 80%, carbon dioxide from syngas that allows for the simultaneous production of medium to high amounts of hydrogen in the syngas as a part of the production of hydrogen in a hydrogen generation plant. By using the process of the present invention, especially in terms of a hydrogen generation plant, it is possible to increase recovery of hydrogen and capture of the carbon dioxide in the syngas stream by balancing the recycle of the hydrogen rich permeate from the hydrogen membrane separation units to the process unit and/or the water gas shift as capacity allows when a carbon dioxide separation unit, a carbon dioxide membrane separation unit and two hydrogen membrane separation units are utilized.

Systems and methods for extracting and processing gases from submerged sources

Systems and methods for extracting and processing gases from submerged sources are disclosed. A system for removing and processing a gas from a submerged area in accordance with a particular embodiment includes a membrane or other open-bottom structure having a port and being disposed over at least a portion of the submerged area so as to at least partially enclose a volume of the gas. The system can further include a chemical reactor coupled to the open-bottom structure to receive the gas, and positioned to conduct a non-combustion reaction to dissociate a constituent from a donor substance of the gas.

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.

System and method for heating a gasifier

A system includes a gasifier configured to gasify a gasification fuel during a gasification mode. The system also includes a first injector configured to inject a heat control fuel and an oxygen enriched air into the gasifier for combustion during a heat control mode. The heat control fuel is the same or different from the gasification fuel, and the oxygen enriched air includes air enriched with additional oxygen.

Carbon capture in fermentation

The invention relates to methods of capturing carbon by microbial fermentation of a gaseous substrate comprising CO. The methods of the invention include converting CO to one or more products including alcohols and/or acids and optionally capturing CO2 to improve overall carbon capture. In certain aspects, the invention relates to processes for producing alcohols, particularly ethanol, from industrial waste streams, particularly steel mill off-gas.

Method and System for Injecting Low Pressure Oxygen from an Ion Transport Membrane into an Ambient or Super Ambient Pressure Oxygen-Consuming Process

A stream of sub ambient oxygen from an ion transport membrane is injected into an ambient pressure or super ambient pressure oxygen-consuming process through an annular space in between concentrically disposed inner and outer tubes where a high velocity gas is injected into the process from the inner tube.

Solid oxide fuel cell device

To provide a fuel cell device capable of extending the years of service life of a reformer by suppressing thermal runaways. The present invention is a solid oxide fuel cell device, including a fuel cell module having fuel cell units; a reformer disposed above the fuel cell units, for producing hydrogen by a partial oxidation reforming reaction and a steam reforming reaction; a vaporizing chamber disposed adjacent to the reformer; a combustion chamber for heating the vaporization chamber; a water supply device; an electrical generation oxidant gas supply device; and a controller for raising the fuel cell units to a temperature at which electrical generation is possible; whereby over the entire period of the startup step, the reforming oxidant gas supply device and water supply device are controlled so that partial oxidation reforming reactions do not occur independently in the reformer.

METHODS FOR FUEL CONVERSION

In one embodiment described herein, fuel may be converted into syngas by a method comprising feeding the fuel and composite metal oxides into a reduction reactor in a co-current flow pattern relative to one another, reducing the composite metal oxides with the fuel to form syngas and reduced composite metal oxides, transporting the reduced composite metal oxides to an oxidation reactor, regenerating the composite metal oxides by oxidizing the reduced composite metal oxides with an oxidizing reactant in the oxidation reactor, and recycling the regenerated composite metal oxides to the reduction reactor for sub-sequent reduction reactions to produce syngas. The composite metal oxides may be solid particles comprising a primary metal oxide and a secondary metal oxide. 1. A method for converting fuel into syngas , the method comprising:feeding the fuel and composite metal oxides into a reduction reactor in a co-current flow pattern relative to one another, wherein the composite metal oxides are solid particles comprising a primary metal oxide and a secondary metal oxide;reducing the composite metal oxides with the fuel to form syngas and reduced composite metal oxides;transporting the reduced composite metal oxides to an oxidation reactor;regenerating the composite metal oxides by oxidizing the reduced composite metal oxides with an oxidizing reactant in the oxidation reactor; andrecycling the regenerated composite metal oxides to the reduction reactor for subsequent reduction reactions to produce syngas.2. The method of claim 1 , wherein the fuel is a gas.3. The method of claim 1 , wherein the fuel is natural gas.4. The method of claim 1 , wherein the fuel is natural gas claim 1 , coal claim 1 , biomass claim 1 , petroleum coke claim 1 , naphtha claim 1 , residual oil claim 1 , shale gas claim 1 , C-Clight hydrocarbons claim 1 , and combinations thereof.5. The method of claim 1 , wherein the oxidizing reactant comprises air claim 1 , oxygen claim 1 , steam claim 1 , ...

ENERGETICALLY ENHANCED REFORMING PROCESS

Methods and systems for producing hydrogen from methane or other fuels that has lower input heat requirements than conventional steam reformation schemes are provided. The system has a reactor with a controlled feed of fuel, water/steam, CO and recycle gases. The methods generally use significantly high amounts of steam (water) and carbon monoxide (CO) in the feed that substantially enhances the reaction rate of the water-gas shift reaction, which transforms CO and HO to COand H. Since this reaction is exothermic, its enhancement alters the endothermic nature of the overall reforming process to the point where the overall reforming process is no longer endothermic. The CO requirements may be met in part with the reverse water-gas shift reaction from COproduced by the reactor. The lower heat requirements may be satisfied with renewable sources such as solar or from hydrogen produced by the system. 1. An energy efficient method for the production of hydrogen gas , the method comprising:{'sub': 2', '4, '(a) flowing a HO/CO/CHfeed into a reactor;'}{'sub': 2', '2', '2', '4, '(b) reforming the feed gases to produce a stream of H, COand residual HO, CO and CHfeed gases;'}{'sub': '2', '(c) separating HO from the stream and recycling separated water to the reactor;'}{'sub': '2', '(d) separating COfrom the stream;'}{'sub': '2', '(e) purifying Hfrom the stream; and'}{'sub': '2', '(f) recycling remaining gases from the Hseparation to the reactor.'}2. The method of claim 1 , further comprising:{'sub': '2', 'converting COfrom the stream to CO; and'}recycling the CO to the reactor feed.3. The method of claim 1 , further comprising:combusting hydrogen gas from an output stream of purified hydrogen gas to provide system heat requirements.4. The method of claim 1 , wherein the reactor feed ratio of HO/CO/CHis 18/15/1.5. The method of claim 1 , wherein the reactor operating temperature and pressure are 1140K and 5 bar respectively.6. The method of claim 1 , wherein the heat ...

PROCESS FOR MAKING AMMONIA

A process for production of ammonia includes: providing a reaction stream including carbon monoxide and hydrogen; passing the reaction stream and steam over a water gas shift catalyst in a catalytic shift reactor, forming a shifted gas mixture depleted in carbon monoxide and enriched in hydrogen; passing the shifted gas mixture with an oxygen-containing gas over a selective oxidation catalyst at ≧175° C., forming a selectively oxidized gas stream with a portion of the carbon monoxide converted to carbon dioxide; removing some of the carbon dioxide from the selectively oxidized gas stream in a carbon dioxide removal unit; passing the carbon dioxide depleted stream over a methanation catalyst in a methanator to form a methanated gas stream, optionally adjusting its hydrogen:nitrogen molar ratio to form an ammonia synthesis gas; and passing the ammonia synthesis gas over an ammonia synthesis catalyst in an ammonia converter to form ammonia. 114-. (canceled)15. A process for the production of ammonia comprising the steps of:(a) providing a reaction stream comprising carbon monoxide and hydrogen;(b) passing the reaction stream and steam over a water gas shift catalyst in a catalytic shift reactor to form a shifted gas mixture containing methanol;(c) passing the shifted gas mixture with an oxygen-containing gas over a selective oxidation catalyst at an inlet temperature ≧175° C. to form a selectively oxidised gas stream;(d) removing at least a portion of the carbon dioxide and steam from the selectively oxidised gas stream in a carbon dioxide removal unit;(e) passing the carbon dioxide depleted stream over a methanation catalyst in a methanator to form a methanated gas stream,and(f) passing the methanated gas stream over an ammonia synthesis catalyst in an ammonia converter to form ammonia.16. A process according to wherein the inlet temperature is in the range 175° C. to 250° C.17. A process according to wherein the selective oxidation is operated adiabatically in the ...

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 ...

AMMONIA-UREA INTEGRATED PROCESS AND PLANT

A process for the production of ammonia and urea in an ammonia-urea integrated plant comprising an ammonia section and a tied-in urea section, wherein a hydrocarbon is reformed to produce ammonia make-up synthesis gas; said make-up gas is purified by shift conversion and removal of carbon dioxide; carbon dioxide is removed from the make-up gas by a first and a second CO2 removal sections;the first section removes CO2 by absorption with a suitable medium, and the second section removes CO2 by washing with a carbamate solution taken from the urea section; the make-up gas is reacted to produce ammonia; the CO2 removed from the make-up gas and at least part of the ammonia are used to produce urea. 1) A process for the production of ammonia and urea in an ammonia-urea integrated plant comprising:reforming a hydrocarbon source obtaining a make-up gas containing hydrogen and nitrogen, wherein said make-up gas after purification is converted into ammonia,at least part of the synthesized ammonia provides the ammonia feed of a urea synthesis process, said urea synthesis process also receiving a carbon dioxide feed,the urea synthesis process comprising the reaction of ammonia and carbon dioxide in a urea synthesis section to form a urea aqueous solution, and subsequent treatment of said solution in a urea recovery section,{'sub': 2', '2', '2', '2', '2', '2, 'wherein the purification of the make-up gas comprises removal of COby means of a first step of COremoval in a first COremoval unit and a second step of COremoval in a second COremoval unit, which are carried out in series or in parallel, said first and second COremoval units not being said urea synthesis section,'}{'sub': 2', '2, 'one of said first and second COremoval steps comprises washing CO-containing make-up gas with a carbamate solution taken from said urea recovery section,'}{'sub': '2', 'and said carbon dioxide feed of the urea synthesis process comprises at least part of the carbon dioxide separated from said ...

RENEWABLE ELECTRICITY CONVERSION OF LIQUID FUELS FROM HYDROCARBON FEEDSTOCKS

The present invention includes a method for converting renewable energy source electricity and a hydrocarbon feedstock into a liquid fuel by providing a source of renewable electrical energy in communication with a synthesis gas generation unit and an air separation unit. Oxygen from the air separation unit and a hydrocarbon feedstock is provided to the synthesis gas generation unit, thereby causing partial oxidation reactions in the synthesis gas generation unit in a process that converts the hydrocarbon feedstock into synthesis gas. The synthesis gas is then converted into a liquid fuel. 1. A method , comprising:generating oxygen in an oxygen separation unit utilizing electricity from wind or solar power;supplying the oxygen from the oxygen separation unit to a synthesis gas generation unit;supplying steam to the synthesis gas generation unit;producing synthesis gas in the synthesis gas generation unit using a combination of steam reformation and partial oxidation of a hydrocarbon feedstock in the synthesis gas generation unit; andconverting the synthesis gas into a fuel.2. The method of claim 1 , wherein converting the synthesis gas into the fuel includes converting the synthesis gas into a liquid fuel.3. The method of claim 1 , further comprising storing the oxygen generated by the oxygen separation unit prior to supplying the oxygen from the oxygen separation unit to the synthesis gas generation unit.4. The method of claim 3 , wherein storing the oxygen generated by the oxygen separation unit includes cryogenically storing the oxygen generated by the oxygen separation unit.5. The method of claim 1 , further comprising providing electricity to operate the oxygen separation unit from a solar or wind powered renewable energy source.6. The method of claim 1 , wherein producing synthesis gas in the synthesis gas generation unit includes operating one or more plasma electrodes in the synthesis gas generation unit to partially oxidize the hydrocarbon feedstock.7. The ...

PROCESS FOR REFORMING HYDROCARBONS

A process for the production of synthesis gas by the use of autothermal reforming in which tail gas from downstream Fischer-Tropsh synthesis is hydrogenated and then added to the autothermal reforming stage. 1. Process for the production of liquid hydrocarbons from a hydrocarbon feedstock comprising:a) passing said hydrocarbon feedstock through an ATR, CPO or POx, and withdrawing a stream of hot effluent synthesis gas from the ATR, CPO or PDX,b) converting the synthesis gas into liquid hydrocarbons via Fischer-Tropsch synthesis,{'b': '1', 'c) passing tail gas from the Fischer-Tropsch synthesis stage through a hydrogenation stage to produce a hydrogenated tail gas containing less than mol olefins, and'}d) adding the hydrogenated tail gas directly to said ATR, CPO or Pox;e) optionally recovering the liquid hydrocarbons produced.2. Process according to claim 1 , wherein said hydrocarbon feedstock is a gas that has passed through at least one adiabatic pre-reforming stage.3. Process according to claim 1 , wherein said hydrocarbon feedstock is a gas that has passed through at least one steam reforming stage.4. Process according to claim 1 , wherein said hydrocarbon feedstock is a gas mixture resulting from dividing a raw hydrocarbon feed gas into two streams claim 1 , passing the first stream through at least one steam reforming stage to form a primary reformed gas claim 1 , using the second stream as a by-pass stream to said steam reforming stage claim 1 , and subsequently combining said primary reformed gas with the by-pass stream to form said hydrocarbon feedstock.5. Process according to claim 1 , comprising dividing a raw hydrocarbon feed gas into two streams claim 1 , by which one of the streams becomes said hydrocarbon feedstock claim 1 , and passing the other stream through at least one steam reforming stage to form a reformed gas.6. Process according to claim 3 , wherein the steam reforming stage is heat exchange reforming claim 3 , and where at least a portion ...

Plasma-assisted method and system for treating raw syngas comprising tars

The invention provides a system and method for conversion of raw syngas and tars into refined syngas, while optionally minimizing the parasitic losses of the process and maximizing the usable energy density of the product syngas. The system includes a reactor including a refining chamber for refining syngas comprising one or more inlets configured to promote at least two flow zones: a central zone where syngas and air/process additives flow in a swirling pattern for mixing and combustion in the high temperature central zone; at least one peripheral zone within the reactor which forms a boundary layer of a buffering flow along the reactor walls, (b) plasma torches that inject plasma into the central zone, and (c) air injection patterns that create a recirculation zone to promotes mixing between the high temperature products at the core reaction zone of the vessel and the buffering layer, wherein in the central zone, syngas and air/process additives mixture are ignited in close proximity to the plasma arc, coming into contact with each other, concurrently, at the entrance to the reaction chamber and method of using the system.

Carbon capture in fermentation

The invention relates to a steel mill adapted to provide gas stream(s) comprising CO to a microbial fermentation, the steel mill comprising a steel mill structure containing apparatus for a steel manufacturing process wherein said apparatus produces waste gases during various stages of the steel making process, said waste gases being directed into the atmosphere by a waste stack, wherein the waste stack is connected to a fermentation system by a transfer means connected to the waste stack to divert at least a portion of the waste gases to the microbial fermentation system.

Polygeneration Production of Power and Fertilizer Through Emissions Capture

Method for the production of ammonia, and optionally urea, from a flue gas effluent from an oxy-fired process, wherein the production of ammonia and optionally urea includes a net power production. Also provided is a method to effect cooling in an oxy-fired process with air separation unit exit gases utilizing either closed or open cooling loop cycles. 1. A method for the production of ammonia from exhaust flue gases of an oxygen-fired process , the method comprising the steps of:supplying a hydrocarbon or carbonaceous feedstock and oxygen to an oxygen-fired process to produce an exhaust flue gas, said exhaust flue gas comprising carbon dioxide, carbon monoxide, and hydrogen;supplying the exhaust flue gas to a first reactor, said first reactor comprising a catalyst and being configured to convert at least a portion of the carbon monoxide to carbon dioxide and produce a modified exhaust flue gas;supplying the modified exhaust flue gas to a second reactor, said second reactor comprising a catalyst and being configured to convert any remaining carbon monoxide to carbon dioxide to produce a carbon dioxide-rich exhaust flue gas;supplying the carbon dioxide-rich exhaust flue gas from the second reactor to a first condenser to remove water and produce a gas stream comprising primarily hydrogen and carbon dioxide;supplying the gas stream comprising primarily hydrogen and carbon dioxide from the first condenser to a carbon dioxide stripper to produce a hydrogen stream and a high purity carbon dioxide stream, said carbon dioxide stripper being charged with a solvent suitable for extracting a carbon dioxide, and wherein the hydrogen stream comprises minor amounts of carbon monoxide and carbon dioxide;supplying the hydrogen stream to a third reactor, said third reactor comprising a catalyst and being configured for the production methane from the minor amounts of carbon monoxide and carbon dioxide present in the hydrogen stream, said third reactor producing a methane product ...

METHOD AND APPARATUS FOR PROCESSING OF MATERIALS USING HIGH-TEMPERATURE TORCH

A method and apparatus for reforming carbonaceous material into syngas containing hydrogen and CO gases is disclosed. In one embodiment, a hydrogen rich torch reactor is provided for defining a reaction zone proximate to torch flame. One input of the reactor receives input material to be processed. Further inputs may be provided, such as for example to introduce steam and/or gases such as methane, oxygen, hydrogen, or the like. 1. An apparatus for processing input material , comprising:a reactor vessel defining a combustion zone; the reactor vessel further having at least one input port for receiving the input feedstock, the input feedstock being directed proximally to the at least one flame;', 'the reactor vessel further having an output for discharging a primary reactor output stream;', 'at least one cooler coupled to receive the primary reactor output stream and operable to cool the primary reactor output stream and generate a secondary output stream;, 'the reactor vessel having at least one input for a combustible torch fuel to at least one torch nozzle, the at least one torch nozzle being adapted to generate at least one flame within said reactor;'}a scrubber, coupled to receive the secondary output stream from the cooler/separator, the scrubber being operable to further extract at least one gas from the secondary output stream.2. An apparatus in accordance with claim 1 , wherein the reactor vessel further has an input for receiving a supply of steam.3. An apparatus in accordance with claim 1 , wherein the combustible torch fuel comprises hydrogen.4. An apparatus in accordance with claim 2 , wherein the combustible torch fuel further comprises methane.5. An apparatus in accordance with claim 1 , wherein the combustible torch fuel is combined with oxygen.6. An apparatus in accordance with claim 1 , wherein the combustible torch fuel comprises acetylene.7. An apparatus in accordance with claim 1 , wherein the reactor vessel further having at least one input port ...

UNCONDITIONED SYNGAS COMPOSITION AND METHOD OF CLEANING UP SAME FOR FISCHER-TROPSCH PROCESSING

A system and method for processing unconditioned syngas first removes solids and semi-volatile organic compounds (SVOC), then removes volatile organic compounds (VOC), and then removes at least one sulfur containing compound from the syngas. Additional processing may be performed depending on such factors as the source of syngas being processed, the products, byproducts and intermediate products desired to be formed, captured or recycled and environmental considerations. 1. An unconditioned syngas generated by steam reforming of biomass in the presence of carbon dioxide and suitable for the production of Fischer-Tropsch products therefrom , the unconditioned syngas having a component composition comprising:(a) a carbon monoxide concentration ranging from between 5 volume percent to 35 volume percent on a dry basis;(b) a hydrogen concentration ranging from between 20 volume percent to 60 volume percent on a dry basis;(c) one or more volatile organic compounds (VOC) selected from the group consisting of benzene, toluene, phenol, styrene, xylene, cresol, and combinations thereof, the VOC concentration ranges from between 500 parts per million by volume to 10,000 parts per million by volume on a dry basis;(d) one or more semi-volatile organic compounds (SVOC) selected from the group consisting of indene, indan, napthalene, methylnapthalene, acenapthylene, acenapthalene, anthracene, phenanthrene, (methyl-) anthracenes/phenanthrenes, pyrene/fluoranthene, methylpyrenes/benzofluorenes, chrysene, benz[a]anthracene, methylchrysenes, methylbenz[a]anthracenes, perylene, benzo[a]pyrene, dibenz[a,kl]anthracene, dibenz[a,h]anthracene, and combinations thereof, the SVOC concentration ranges from between 10 parts per million by volume to 1,000 parts per million by volume on a dry basis;(e) a hydrogen chloride concentration ranging from between greater than 0 parts per million by volume to 1,000 parts per million by volume on a dry basis; and(f) a hydrogen sulfide concentration ...

Method for processing waste water using zero process water discharge

A method for processing wastewater is provided. The method includes pretreating a flow of the wastewater using at least one of a softening/clarification system, a sludge handling system, a filtration system, and an ammonia stripping system, evaporating the pretreated flow to produce at least a distillate and an evaporator brine; separating the evaporator brine to produce a liquid recycle stream and salt crystal mixture; and channeling the liquid recycle stream to a feed stream. The method eliminates the salt drying process that significantly reduces the costs of construction and operation of the standard zero process water discharge process.

PROCESS, SYSTEM AND INSTALLATION FOR TREATING LIQUID AND/OR PASTY HYDROCARBON MATERIALS

The invention relates to a process for treating liquid and/or pasty hydrocarbon materials, more particularly fuel oil, more particularly still heavy fuel oil, in which the hydrocarbon materials are firstly brought to the autoignition temperature, then mixed with a controlled amount of oxygen in order to obtain a first gaseous stream and a non-gaseous mass, more particularly a solid mass, comprising solid hydrocarbon molecules which are then oxidized by a gaseous stream of COin order to obtain a second gaseous stream. The first and second gaseous streams are then mixed in order to obtain a third gaseous stream comprising carbon monoxide having a high energy value. The invention also relates to a system implementing the process according to the invention and an installation implementing such a system. 1. A process for treating liquid and/or pasty hydrocarbon-based materials comprising a gaseous volatile part and a non-gaseous solid part , more particularly heavy fuel oil , for example heavy fuel oil of category 2 or higher , tar sands or earths polluted by hydrocarbons , the process comprising the following steps:bringing of said hydrocarbon-based materials to a temperature greater than or equal to the autoignition temperature of said hydrocarbon-based materials; [{'sub': 2', '2, 'a first gaseous stream at a temperature of greater than or equal to 800° C. comprising CO and HO molecules, hydrocarbon-based molecules in the gaseous phase and Hmolecules, and'}, 'a non-gaseous feedstock comprising non-gaseous hydrocarbon-based molecules;, 'gasification of said hydrocarbon-based materials by injection of a controlled amount of oxygen, said gasification producing{'sub': 2', '2', '2', '2', '2, 'oxidation of said non-gaseous hydrocarbon-based molecules contained in said non-gaseous feedstock, by means of an oxidation gaseous stream consisting of Oand COat a temperature of between 1000° C. and 1200° C., said oxidation producing a second gaseous stream comprising CO, Oand HO ...

Process for producing ammonia synthesis gas and a related front-end of an ammonia plant

A process for producing ammonia synthesis gas from a hydrocarbon source, comprising: conversion of the hydrocarbon source into a raw synthesis gas ( 14 ) in ATR or POX reactor ( 11 ) which is fired with oxygen ( 12 ) or oxygen-enriched air ( 28 ); a water-gas shift treatment of the raw synthesis gas ( 14 ), which consist of a medium-temperature shift ( 15 ) at a temperature of 200-300° C., thus obtaining a shifted synthesis gas ( 16 ); purification of said shifted synthesis gas ( 16 ) including at least a step of pressure-swing adsorption ( 17 ) to remove residual carbon oxides and methane from the synthesis gas, obtaining a purified synthesis gas ( 18 ), and optionally, addition of nitrogen ( 19 ) to said purified synthesis gas ( 18 ), thus obtaining ammonia synthesis gas with a desired hydrogen to nitrogen ratio.

PROCESS AND APPARATUS FOR THE PRODUCTION OF SYNTHESIS GAS

Reactive diluent fluid () is introduced into a stream of synthesis gas (or “syngas”) produced in a heat-generating unit such as a partial oxidation (“PDX”) reactor () to cool the syngas and form a mixture of cooled syngas and reactive diluent fluid. Carbon dioxide and/or carbon components and/or hydrogen in the mixture of cooled syngas and reactive diluent fluid is reacted () with at least a portion of the reactive diluent fluid in the mixture to produce carbon monoxide-enriched and/or solid carbon depleted syngas which is fed into a secondary reformer unit () such as an enhanced heat transfer reformer in a heat exchange reformer process. An advantage of the invention is that problems with the mechanical integrity of the secondary unit arising from the high temperature of the syngas from the heat-generating unit are avoided.

Engine Reformer Systems For Lower Cost, Smaller Scale Manufacturing Of Liquid Fuels

A reformer-liquid fuel manufacturing system that utilizes an engine to generate hydrogen-rich gas is disclosed. The engine operates at very rich conditions, such as 2.5<φ<4.0. In doing so, it creates an exothermic reaction, which results in the production of syngas. In addition, the system utilizes the energy from the exothermic reaction to rotate a shaft and also utilizes the heat in the syngas to heat the reactants. A mechanical power plant is in communication with the rotating shaft and can be used to produce oxygen, provide electricity or operate a compressor, as require. The hydrogen-rich gas is supplied to a chemical reactor, which converts the gas into a liquid fuel, such as methanol.

Calcium Sulfate Looping Cycles for Sour Gas Combustion and Electricity Production

A calcium looping combustion process for sour gas combustion comprising a system that includes several reaction zones. The system is configured to provide oxygen transfer media production, generation of a syngas product stream, and in-situ HS removal from the sour gas. The system is also configured such that the calcium-based transfer media and the calcium-based oxygen carrier are reproduced via reactions in another reaction zone, and recirculated in the system.

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.

PROCESS FOR GENERATING SYNGAS FROM A CO2-RICH HYDROCARBON-CONTAINING FEED GAS

A process for generating a syngas from a CO-rich and hydrocarbon-containing feed gas, wherein a CO-rich and hydrocarbon-containing feed gas is provided and is reacted in a syngas generation step by means of partial oxidation or steam reforming to give an H- and CO-comprising syngas. At least COis removed from the feed gas in a scrubbing of the feed gas by means of a scrubbing medium, before the feed gas is fed to the syngas generation step. 1. Process for generating a syngas from a CO2-rich and hydrocarbon-containing feed gas , wherein a CO2-rich and hydrocarbon-containing feed gas is provided and is reacted in a syngas generation step by means of partial oxidation or steam reforming to give an H2- and CO-comprising syngas ,characterized in that at least CO2 is removed from the feed gas in a scrubbing of the feed gas by means of a scrubbing medium, before the feed gas is fed to the syngas generation step, wherein, during the scrubbing, a CO2-rich stream is generated that has a pressure in the range from 20 bar to 100 bar, and wherein the CO2-rich stream is used as feed for a synthesis or to support the extraction of oil, wherein the CO2-rich stream is injected into an oil deposit in order to increase the pressure in the oil deposit.2. Process according claim 1 , characterized in that the feed gas is conducted downstream of the scrubbing through an adsorber unit claim 1 , wherein one or more sulfur compounds that are still present in the feed gas are adsorbed in the adsorber unit and in this case removed from the feed gas.3. Process according to claim 1 , characterized in that the syngas that is generated is divided into first and second syngas substreams claim 1 , wherein the first syngas substream is used as feed for a synthesis claim 1 , and wherein the second syngas substream is subjected to a water-gas shift reaction claim 1 , wherein CO of the second syngas substream is reacted with H2O to form H2 and CO2 in order to reduce the CO content in the second syngas ...

PROCESS FOR PURIFYING A SYNTHESIS GAS

The present invention provides for a pressure swing adsorption (PSA) process for the substantial removal of HO and COfrom a synthesis gas to obtain a multicomponent product gas substantially free of HO and COwith high recovery of the product gas. Further, the present invention provides an integrated process that achieves sufficiently high Hand CO recoveries such that compression and recycling of the syngas purification PSA tailgas is not necessary to be economically advantageous compared to the conventional processes. 1. An integrated process for the individual recovery of at least a purified H-rich gas and a purified CO-rich gas from a hydrocarbon feedstock comprising:{'sub': 2', '4', '2', '2, 'a. introducing a hydrocarbon feedstock into a syngas generating unit and generating a superatmospheric pressure syngas stream consisting essentially of at least H, CO, CH, CO, and HO;'}{'sub': 2', '2, 'b. feeding the generated superatmospheric pressure syngas stream to a pressure swing adsorption (PSA)-based purification process unit to produce a superatmospheric pressure syngas stream substantially free of HO and CO,'}{'sub': 2', '2', '2, 'c. routing the superatmospheric pressure syngas stream substantially free of HO and COto a separation system producing at least a H-rich stream and a CO-rich stream; and'}{'sub': 2', '2', '2', '2, 'd. wherein the PSA-based purification process unit is purged with high-purity Nstream for a first portion of a purge phase and with H-containing gas substantially free of HO and COfor a second portion of the purge phase.'}2. The integrated process of claim 1 , wherein the syngas generation system is selected from a steam reformer claim 1 , an autothermal reformer claim 1 , or a partial oxidation reactor.3. The integrated process of claim 1 , wherein the hydrocarbon feedstock is natural gas.4. The integrated process of claim 1 , wherein the high-purity Na stream used during the first portion of the purge phase is generated by a cryogenic air ...

METHOD AND REACTOR TO PRODUCE SYNGAS

Disclosed herein is a method and a reactor for the conversion of a hydrocarbon gas to syngas. The method and reactor utilizes a oxy-hydrogen flame to partially oxidize hydrocarbon gas to syngas by provide an excess flow of oxygen gas. The oxy-hydrogen flame is generated by a multi-tubular oxy-hydrogen burner. 1. A method of producing syngas comprising the steps of:a) providing an oxy-hydrogen flame generated by a multi-tubular oxy-hydrogen burner comprising an inner tube and an outer tube by delivering a flow of hydrogen gas through the inner tube and delivering a flow of oxygen gas through the outer tube of the multi-tubular oxy-hydrogen burner, wherein the delivered oxygen gas is provided in excess to the stoichiometric amount to completely burn the delivered hydrogen gas; andb) directly interacting hydrocarbon gas with the oxy-hydrogen flame by introducing the hydrocarbon gas upstream of the multi-tubular oxy-hydrogen burner to flow in a direction substantially parallel to the oxy-hydrogen flame, wherein the excess of the oxygen gas in the oxy-hydrogen flame partially oxidizes the hydrocarbon gas to produce syngas.2. The method of claim 1 , wherein the method further comprises adjusting the flow of the hydrogen gas and the oxygen gas to minimize their consumption per the syngas produced.3. The method of claim 1 , wherein the method further comprises adjusting the flow of the hydrogen gas and the oxygen gas to obtain a desired ratio of hydrogen gas:carbon monoxide in the produced syngas.4. The method of claim 1 , wherein the method further comprises adjusting the flow of the hydrogen gas and the oxygen gas to maintain a stable flame plume and to suppress soot formation in continuous operation.5. The method of claim 1 , wherein the superficial velocity of the flow of the hydrogen is from about 100 ft/s to about 400 ft/s.6. The method of claim 1 , wherein the superficial velocity of the flow of the oxygen is from about 10 ft/s to about 50 ft/s.7. The method of claim ...

PROCESS TO PREPARE A CHAR PRODUCT

The invention is directed to a process to prepare a char product by pyrolysis or mild gasification of a solid biomass feed thereby obtaining a gaseous fraction comprising hydrogen, carbon monoxide and a mixture of gaseous organic compounds and a solid fraction comprising of char particles having a reduced atomic hydrogen over carbon ratio and a reduced oxygen over carbon ratio relative to the solid biomass feed. The solid biomass feed are pellets of a solid torrefied biomass feed. The pyrolysis or mild gasification is performed at a temperature of between 500 and 800° C. and at a solid residence time of between 10 and 60 minutes. 116.-. (canceled)17. A process to prepare a char product the method comprising mild gasification of a solid biomass feed ,thereby obtaining a gaseous fraction comprising hydrogen, carbon monoxide and a mixture of gaseous organic compounds and a solid fraction comprising of char particles having a reduced atomic hydrogen over carbon ratio and a reduced oxygen over carbon ratio relative to the solid biomass feed;wherein the solid biomass feed are pellets of a solid torrefied biomass feed having a content of volatiles of between 50 and 75 wt %; andwherein the mild gasification is performed at a temperature of between 500 and 800° C. and at a solid residence time of between 10 and 60 minutes and in the presence of oxygen and steam.18. The process according to claim 17 , wherein the mild gasification is performed in an elongated reactor wherein the biomass is continuously transported from a solids inlet at one end of an elongated reactor to a solids outlet at the other end of the elongated reactor.19. The process according to claim 17 , wherein the solid biomass feed is subjected to a mild gasification by contacting the solid biomass feed with an oxygen comprising gas and wherein the amount of oxygen is between 0.1 and 0.3 mass oxygen per mass biomass.20. The process according to claim 19 , wherein the oxygen comprising gas is air.21. The ...

Catalysts, related methods and reaction products

The present invention generally relates to improved catalysts that provide for reduced product contaminants, related methods and improved reaction products. It more specifically relates to improved direct fuel production and redox catalysts that provide for reduced levels of certain oxygenated contaminants, methods related to the use of those catalysts, and hydrocarbon fuel or fuel-related products that have improved characteristics. In one aspect, the present invention is directed to a method of converting one or more carbon-containing feedstocks into one or more hydrocarbon liquid fuels. The method includes the steps of: converting the one or more carbon-containing feedstocks into syngas; and, converting the syngas to one or more hydrocarbons (including liquid fuels) and a water fraction. The water fraction comprises less than 500 ppm of one or more carboxylic acids. 1. A method of converting one or more carbon-containing feedstocks into one or more hydrocarbons comprising:a) converting the one or more carbon-containing feedstocks into syngas;b) converting the syngas to one or more hydrocarbons and a water fraction wherein the water fraction comprises less than 500 ppm of one or more carboxylic acids.2. The method according to claim 1 , wherein the one or more carbon-containing feedstocks are selected from a group consisting of: gas-phase feedstocks; liquid-phase feedstocks; and claim 1 , solid-phase feedstocks.3. The method according to claim 1 , wherein the one or more carboxylic acids are selected from a group consisting of: methanoic acid; ethanoic acid;propanoic acid; butanoic acid; pentanoic acid; hexanoic acid; and octanoic acid.4. The method according to claim 1 , wherein a conversion catalyst is used to convert the syngas to one or more hydrocarbons and a water fraction claim 1 , and wherein the conversion catalyst comprises a substrate claim 1 , and wherein the substrate comprises a surface having a pH ranging from about 6.0 to about 8.0.5. The method ...

TREATMENT OF CRUDE SYNTHESIS GAS

A process for treating steam-saturated crude gases from an entrained flow gasification of fuels before entry into heat exchangers sited upstream of a crude gas converting operation. To avoid solid deposits in an entrance region of the heat exchangers, the crude gas is converted from a saturated into a superheated state by supply of a hot gas to the crude gas. Hot gas contemplated is superheated high pressure steam or recycled superheated converted crude gas. 1. A process for processing of crude synthesis gas from a gasification facility that subjects fuels to partial oxidation , for a crude gas converting operation , the process comprising:in a plurality of scrubbing stages, crude synthesis gas generated in a reactor of the gasification facility is, by injection of water into the gas, the gas is largely cleaned of entrained particles, cooled, and steam-saturated;converting the steam-saturated crude synthesis gas into a superheated state thereof; andheating the superheated crude synthesis gas in a heat exchange to an entry temperature of the crude gas converting process.2. The process as claimed in claim 1 , further comprising steam saturating the crude synthesis gas at a first temperature and superheating the crude synthesis gas at a second temperature claim 1 , and a temperature difference between the first steam-saturated state at a lower temperature and the superheated state at a higher temperature is at least 5° C.3. The process as claimed in claim 1 , further comprising converting the steam-saturated crude synthesis gas into the superheated state by directly supplying hot gas to the crude synthesis gas.4. The process as claimed in claim 3 , wherein the hot gas comprises high pressure steam.5. The process as claimed in claim 1 , further comprising converting the steam-saturated crude synthesis gas into the superheated state by directly supplying a fraction of the crude synthesis gas obtained in the crude gas converting operation which is exothermic.6. The ...

SYSTEM TO MAXIMIZE CO FROM FLUID CATALYTIC CRACKING (FCC) PROCESS BY COKE OXIDATION WITH METAL OXIDES

Provided is a process capable of converting the cokes on spent catalysts in a fluid catalytic cracking (FCC) process into synthesis gas. The produced synthesis gas contains high concentrations of CO and Hand may be utilized in many downstream applications such as syngas fermentation for alcohol production, hydrogen production and synthesis of chemical intermediates. A reducer/regenerator reactor for a fluid catalytic process comprising a chemical looping system to produce synthesis gas is also described. 1. A method for producing synthesis gas from catalyst coke generated from a fluid catalytic cracking process bya) providing a chemical looping system comprising a reducer/regenerator reactor, an oxidizer reactor and a combustor reactor;b) feeding catalyst coke particles and metal oxide particles into the reducer/regenerator reactor of the chemical looping system to produce a plurality of streams comprising a regenerated catalyst stream, a synthesis gas stream and a reduced metal oxide particle stream;c) feeding the stream of reduced metal oxide particles and a stream of water vapor into the oxidizer reactor of the chemical looping system to produce a plurality of streams comprising a hydrogen stream and a stream of oxidized metal oxide particles; andd) feeding the stream of oxidized metal oxide particles and a stream of air into the combustor reactor of the chemical looping system to produce heat and a stream of metal oxide particles.2. The method of claim 1 , wherein the reducer/regenerator reactor is a moving bed reactor.3. The method of claim 2 , wherein the reduced metal oxide particle stream and the regenerated catalyst stream of the moving bed reactor flow in the same direction.4. The method of claim 1 , wherein the reducer/regenerator reactor is a fluidized bed reactor.5. The method of claim 4 , wherein the reduced metal oxide particle stream and the regenerated catalyst stream of the fluidized bed reactor flow in the same direction.6. The method of claim 2 , ...

PROCESS FOR REFORMING HYDROCARBONS

A process for the production of synthesis gas by the use of autothermal reforming in which tail gas from downstream Fischer-Tropsh synthesis is hydrogenated and then added to the autothermal reforming stage. 1. A method for reducing metal dusting in an apparatus , said apparatus containing an off-gas , said method comprising the removal of olefins from said off-gas.2. The method according to claim 1 , wherein olefins are removed by hydrogenation thereof.3. The method according to claim 1 , wherein the apparatus is an ATR claim 1 , CPO or POx.4. A method of using a gas free of olefins for the reduction of metal dusting of the metal parts of an apparatus in direct contact with said gas.5. The method according to claim 4 , wherein the apparatus in direct contact with the gas is an ATR claim 4 , CPO or POx.6. The method according to claim 4 , wherein the gas is a tail gas from a Fischer Tropsch synthesis.7. The method according to claim 4 , wherein the gas free of olefins is obtained by hydrogenation of said olefins to alkanes. This is a divisional of U.S. application Ser. No. 14/129,244, filed on Jan. 31, 2014, which is a 371 of International Application No. PCT/EP2012/061809, filed on Jun. 20, 2012, which claims priority to Denmark Application No. PA 2011 00485, filed on Jun. 29, 2011, European Application No. 11009101.4, filed on Nov. 26, 2011, and Denmark Application No. PA 2011 00947, filed on Dec. 6, 2011.The present invention relates to a process for the production of synthesis gas used for the production of hydrocarbons by Fischer-Tropsch synthesis. The invention relates in particular to a process for the production of synthesis gas by the use of autothermal reforming in which tail gas from a downstream process, in particular Fischer-Tropsh synthesis, is hydrogenated and then added to the autothermal reforming. In a more general aspect the invention encompasses the removal of olefins in a gas to reduce metal dusting of metal parts in contact with the gas, ...

PROCESS FOR REFORMING HYDROCARBONS

A process for the production of synthesis gas by the use of autothermal reforming in which tail gas from downstream Fischer-Tropsh synthesis is hydrogenated and then added to the autothermal reforming stage. 1. A process for the production of synthesis gas from a hydrocarbon feedstock with reduced metal dusting in at least the burner parts of an autothermal reformer (ATR) , catalytic partial oxidation reactor (CPO) , or partial oxidation reactor (POx) , the process comprising the steps of:passing said hydrocarbon feedstock through an ATR, CPO or POx, and withdrawing a stream of hot effluent synthesis gas from the ATR, CPO or POx;passing tail gas from a Fischer-Tropsch synthesis stage through a hydrogenation stage to produce a hydrogenated tail gas; andadding the hydrogenated tail gas directly to said ATR, CPO or POx.2. The process according to claim 1 , wherein said hydrocarbon feedstock is a gas that has passed through at least one adiabatic pre-reforming stage.3. The process according to claim 1 , wherein said hydrocarbon feedstock is a gas that has passed through at least one steam reforming stage.4. The process according to claim 1 , wherein said hydrocarbon feedstock is a gas mixture resulting from dividing a raw hydrocarbon feed gas into two streams claim 1 , passing the first stream through at least one steam reforming stage to form a primary reformed gas claim 1 , using the second stream as a by-pass stream to said steam reforming stage claim 1 , and subsequently combining said primary reformed gas with the by-pass stream to form said hydrocarbon feedstock.5. The process according to claim 1 , comprising dividing a raw hydrocarbon feed gas into two streams claim 1 , by which one of the streams becomes said hydrocarbon feedstock claim 1 , and passing the other stream through at least one steam reforming stage to form a reformed gas.6. The process according to claim 3 , wherein the steam reforming stage is heat exchange reforming claim 3 , and where at least a ...

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 for converting biomass into fischer-tropsch products with carbon dioxide recycling

A system and method for processing unconditioned syngas first removes solids and semi-volatile organic compounds (SVOC), then removes volatile organic compounds (VOC), and then removes at least one sulfur containing compound from the syngas. Additional processing may be performed depending on such factors as the source of syngas being processed, the products, byproducts and intermediate products desired to be formed, captured or recycled and environmental considerations.

CARBON CAPTURE IN FERMENTATION

The invention relates to methods of capturing carbon by microbial fermentation of a gaseous substrate comprising CO into one or more first products which, in turn, may be incorporated into an article of manufacture or one or more second products. 1. A method of capturing carbon by microbial fermentation , the method comprising:i. receiving off or waste gas stream(s) comprising CO from an industrial process;ii. passing the gas stream(s) to a bioreactor containing a culture of one or more microorganisms;iii. fermenting the culture in the bioreactor to produce one or more first products; andiv. incorporating the one or more products into an article or converting the one or more products into one or more second products.2. The method of wherein at least one first product is selected from ethanol claim 1 , isopropanol claim 1 , isopropanol and monoethylene glycol.3. The method of claim 1 , wherein the first product comprises ethanol and the article is antiseptic hand rubs claim 1 , therapeutic treatments for methylene glycol and methanol poisoning claim 1 , solvents claim 1 , antimicrobial preservatives claim 1 , engine fuels claim 1 , rocket fuels claim 1 , fuel cells claim 1 , home fireplace fuel claim 1 , industrial chemical precursors claim 1 , winterization extraction solvents claim 1 , paint masking products claim 1 , paints claim 1 , tinctures claim 1 , nucleic acid purifiers claim 1 , or cooling bath medium.4. The method of claim 1 , wherein the first product comprises ethanol and the second product is ethylene.5. The method of further comprising incorporating the ethylene into anaesthetics claim 4 , fruit ripening agents claim 4 , fertilizers claim 4 , safety glass claim 4 , metal cutting gases claim 4 , welding gases claim 4 , high velocity thermal sprays claim 4 , or refrigerants.6. The method of claim 4 , further comprising converting the ethylene into polyethylene (PE) claim 4 , polyethylene terephthalate (PET) claim 4 , polyvinyl chloride (PVC) claim 4 , or ...

Method of natural gas pretreatment

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

METHODS FOR FUEL CONVERSION

In one embodiment described herein, fuel may be converted into syngas by a method comprising feeding the fuel and composite metal oxides into a reduction reactor in a co-current flow pattern relative to one another, reducing the composite metal oxides with the fuel to form syngas and reduced composite metal oxides, transporting the reduced composite metal oxides to an oxidation reactor, regenerating the composite metal oxides by oxidizing the reduced composite metal oxides with an oxidizing reactant in the oxidation reactor, and recycling the regenerated composite metal oxides to the reduction reactor for subsequent reduction reactions to produce syngas. The composite metal oxides may be solid particles comprising a primary metal oxide and a secondary metal oxide. 1. A method for converting carbonaceous fuel into syngas , the method comprising:feeding the fuel and composite metal oxides into a reduction reactor having a top and a bottom, wherein the fuel and the composite metal oxides are fed into the top of the reduction reactor, whereupon the composite metal oxides form a packed bed and the composite metal oxides and the fuel flow downward through the reactor in a co-current flow pattern relative to one another;reducing the composite metal oxides with the fuel in the reduction reactor to form syngas and reduced composite metal oxides;removing the syngas and the reduced composite metal oxides from the bottom of the reduction reactor wherein the syngas comprises hydrogen and carbon monoxide;transporting the reduced composite metal oxides to an oxidation reactor;regenerating the composite metal oxides by oxidizing the reduced composite metal oxides with an oxidizing reactant in the oxidation reactor; andrecycling the regenerated composite metal oxides to the reduction reactor for subsequent reduction reactions to produce syngas in the reduction reactor;{'sub': 2', '2', '3, 'wherein the composite metal oxides comprise iron, titanium and oxygen and the reduced metal ...

SYSTEMS AND PROCESSES FOR PRODUCING ULTRAPURE, HIGH PRESSURE HYDROGEN

In various implementations, feed streams that include methane are reacted to produce synthesis gas. The synthesis gas may be further processed to produce ultrapure, high-pressure hydrogen streams. 1. A method for producing hydrogen , comprising;exothermically reacting a first portion of a hydrocarbon feed stream with at least one of steam or an oxidant gas comprising molecular oxygen in a first reactor to produce an exothermically generated syngas product, wherein the feed stream includes methane;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; [{'sub': 4', '2, 'generating, at a pressure above 60 bar, a ratio of methane (CH) to hydrogen plus carbon monoxide (H+CO) of above 5% molar in the endothermically-reformed syngas product from heat exchange reformer tubes;'}, 'separating at least the methane from a combination of the exothermically-generated syngas product and the endothermically-reformed syngas product as part of a waste-gas stream;', 'combusting at least a portion of the waste gas using exhaust from a gas turbine as an oxidant to produce superheated steam and hydrocarbon feed streams used in the exothermically and endothermically generated synthesis gas production; and', 'generating power using the gas turbine to power an oxygen production unit providing the oxygen for synthesis gas generation., 'wherein the endothermically-reformed syngas product is further processed as follows2. The method of claim 1 , wherein the exothermically-generated syngas product is generated using a partial oxidation burner followed by a catalytic section reforming section in an autothermal reformer.3. The method of claim 1 , wherein the ratio of CHto (H+CO) in the ...

AN INTEGRATED AND TUNABLE SYSTEM FOR THE PRODUCTION OF SYNGAS AND CHEMICALS VIA SOLAR-ASSISTED ELECTROLYSIS AND COMBINED REFORMING

A method and system for producing syngas The method includes providing separate streams of oxygen gas and hydrogen gas, the oxygen gas and the hydrogen gas generated from electrolysis of water. The separate stream of oxygen gas is introduced into a reforming module configured to generate a reformed syngas feed, where the oxygen gas oxidizes natural gas supplied to the reforming module. The separate stream of hydrogen gas and the reformed syngas feed are mixed to adjust a ratio of hydrogen gas to carbon monoxide gas (H:CO) to produce a syngas product feed. The system includes a reforming module to receive a stream of oxygen gas, where the oxygen gas oxidizes natural gas supplied to the reforming module to generate a reformed syngas feed. The system includes a mixing module to receive the reformed syngas feed and a stream of hydrogen gas to thereby adjust a ratio of hydrogen gas to carbon monoxide gas (H:CO) in a syngas product feed released from the mixing module. The stream of oxygen gas and the stream of hydrogen gas are generated from electrolysis of water. 1. A method for producing syngas , comprising:providing separate streams of oxygen gas and hydrogen gas, the oxygen gas and the hydrogen gas generated from electrolysis of water;introducing the separate stream of oxygen gas into a reforming module configured to generate a reformed syngas feed, wherein the oxygen gas oxidizes natural gas supplied to the reforming module; and{'sub': '2', 'mixing the separate stream of hydrogen gas and the reformed syngas feed to adjust a ratio of hydrogen gas to carbon monoxide gas (H:CO) to produce a syngas product feed.'}2. The method of claim 1 , further including feeding one or both of steam or carbon dioxide into the reforming module.3. The method of claim 1 , wherein energy for forming electricity to cause the electrolysis of water is supplied from a photovoltaic cell or a thermal collector/turbine generation unit.4. The method of claim 1 , wherein energy requirements to ...

Engine Reformer Systems For Lower Cost, Smaller Scale Manufacturing Of Liquid Fuels

A reformer-liquid fuel manufacturing system that utilizes an engine to generate hydrogen-rich gas is disclosed. The engine operates at very rich conditions, such as 2.5<φ<4.0. In doing so, it creates an exothermic reaction, which results in the production of syngas. In addition, the system utilizes the energy from the exothermic reaction to rotate a shaft and also utilizes the heat in the syngas to heat the reactants. A mechanical power plant is in communication with the rotating shaft and can be used to produce oxygen, provide electricity or operate a compressor, as require. The hydrogen-rich gas is supplied to a chemical reactor, which converts the gas into a liquid fuel, such as methanol.

SYNGAS PRODUCTION WITH CYCLIC OXIDATION HEAT SUPPLY

Processes and units are provided, which carry out cyclic steps of zinc oxidation and reduction of zinc oxide to combine an exothermic heat delivering step with an endothermic syngas production step, respectively. Both steps use zinc as the pivotal element that enables the process to be carried out cyclically. Heat is delivered from the exothermic step to the endothermic syngas via heat storage elements of various types which are arranged according to the reaction's conditions and characteristic temperatures. Thus, energy efficient syngas production methods and units are provided. 1. A method comprising:storing heat produced by oxidation of zinc;using the stored heat to react the produced zinc oxide with methane to form syngas; andre-using zinc reduced by the reaction with methane for the oxidation,wherein the oxidation of zinc and the reduction of the zinc oxide carried out cyclically, to yield syngas continuously.2. The method of claims 1 , further comprising carrying out the oxidation of zinc and the reaction of the produced zinc oxide with methane continuously in a single chamber.3. The method of or claims 1 , wherein the exothermic oxidation of zinc and the endothermic reduction of zinc are carried out under conditions in which the heat released by the zinc oxidation is at least as large as the heat used for the zinc oxide reduction.4. The method of any one of - claims 1 , configured to be carried out in a single chamber by alternating zinc oxidation and zinc oxide reduction processes.5. The method of any one of - claims 1 , further comprising regenerating the reduced zinc during cooling of the syngas.6. The method of claim 5 , wherein the oxidation and regeneration are carried out in a first chamber claim 5 , the method further comprising carrying out the regeneration in a second chamber claim 5 , and carrying out consequent zinc oxidation and zinc oxide reduction in the second chamber.7. The method of claim 5 , further comprising repeatedly alternating roles ...

METHOD FOR PRODUCING HYDROGEN-CONTAINING GAS AND REACTOR FOR IMPLEMENTING SAID METHOD

The invention is for use in gas chemistry for producing hydrogen-containing gas on the base of a CO and Hmixture (syngas) from natural gas and other hydrocarbon gases. The object of the invention is to suppress side reactions resulting in soot formation when conducting the process in high productivity mode, and also to provide for an uncomplicated reactor design while maintaining compact dimensions thereof. The method for producing a hydrogen-containing gas comprises mixing natural gas with oxygen, partially oxidizing the natural gas with oxygen at a temperature ranging from 1300° C. to 1700° C. resulting in obtaining hydrogen-containing gas, and cooling the stream of the hydrogen-containing gas produced. Said cooling is performed until the temperature drops below 550° C. and at a rate above 100000° C./sec. The reactor comprises the following steps, which are arranged in series along the technological process: means for supplying natural gas and oxygen, a natural gas and oxygen mixing zone, a zone for conducting the reaction by partially oxidizing the natural gas with oxygen, and a zone for cooling the stream of the hydrogen-containing gas produced, which is equipped with a cooling body of revolution in order to provide an intensive cooling of the stream of hydrogen-containing gas by contacting thereof with said body of revolution. 1. A method for producing hydrogen-containing gas , said method comprising mixing natural gas with oxygen , partial oxidation of natural gas by oxygen at the temperature ranging from 1300° C. to 1700° C. to produce hydrogen-containing gas , and cooling the stream of obtained hydrogen-containing gas , where the stream of hydrogen-containing gas is cooled to the temperature lower 550° C. at the cooling rate more than 100000° C./s.2. The method according to claim 1 , where cooling the stream of hydrogen-containing gas is carried out by contacting said stream with a body of revolution.3. The method according to claim 2 , where the stream of ...

THERMAL INTEGRATION IN SYNTHESIS GAS PRODUCTION BY PARTIAL OXIDATION

A process and a plant are proposed for producing a synthesis gas including hydrogen and carbon oxides by partial oxidation of carbon-containing fuel in the presence of an oxygen-containing oxidant and a moderator, wherein the obtained raw synthesis gas is laden with soot particles. According to the invention the cooling of the raw synthesis gas is carried out using a crossflow heat exchanger, a shell and tube heat exchanger or a spiral heat exchanger, wherein the carbon-containing input stream or the oxidant stream or the moderator stream or a plurality of these streams serve as the first coolant and are thus preheated before introduction into the partial oxidation plant. 2. The process according to claim 1 , wherein at least a second heat exchanger for cooling the hot quench medium stream by indirect heat exchange is present claim 1 , wherein the second heat exchanger is operated with a second coolant selected from the group of: carbon-containing input stream and oxidant stream.3. The process according to claim 1 , wherein a proportion of the hot or cooled quench medium stream is discharged continuously or batchwise from the quench medium stream circuit as a purge stream and quantitatively replaced by fresh water or solids-free condensate streams.4. The process according to claim 1 , wherein the quench medium stream is supplied to an apparatus for solids separation before recycling to the cooling chamber.5. The process according to claim 4 , wherein the hot quench medium stream is supplied to the apparatus for solids separation before introduction into the first heat exchanger.6. The process according to claim 4 , wherein the cold quench medium stream is supplied to the apparatus for solids separation after discharging from the first heat exchanger.7. The process according to claim 1 , wherein claim 1 , when using a shell and tube heat exchanger or a crossflow heat exchanger the tubes traversed by the coolant are arranged vertically and the hot quench medium is run ...

Method for forming synthesis gas using a plasma-catalyzed fuel reformer

A method of forming a synthesis gas utilizing a reformer is disclosed. The method utilizes a reformer that includes a plasma zone to receive a pre-heated mixture of reactants and ionize the reactants by applying an electrical potential thereto. A first thermally conductive surface surrounds the plasma zone and is configured to transfer heat from an external heat source into the plasma zone. The reformer further includes a reaction zone to chemically transform the ionized reactants into synthesis gas comprising hydrogen and carbon monoxide. A second thermally conductive surface surrounds the reaction zone and is configured to transfer heat from the external heat source into the reaction zone. The first thermally conductive surface and second thermally conductive surface are both directly exposed to the external heat source. A corresponding apparatus and system are also disclosed herein.

PROCESS FOR THE PRODUCTION OF HYDROGEN-ENRICHED SYNTHESIS GAS

Provided is a process for the production of hydrogen-enriched synthesis gas by a catalytic water-gas shift reaction operated on a raw synthesis gas. The reaction is carried out in the presence of at least one compound of formula (I): 2. The process according to claim 1 , wherein the compound of formula (I) is selected from dimethyl disulphide and dimethyl sulfoxide.3. The process according to claim 1 , wherein the catalytic water-gas shift reaction is carried out in a reactor with an inlet gas temperature of at least 260° C.4. The process according to claim 1 , wherein the compound of formula (I) is continuously injected at a flow rate of 0.1 NI/h to 10 Nm/h.5. The process according to claim 1 , wherein the catalytic water-gas shift reaction is carried out in the presence of a sulfur-resistant shift catalyst.6. The process according to claim 5 , wherein the sulfur-resistant shift catalyst comprises an alkali metal.7. The process according to claim 1 , wherein the catalytic water-gas shift reaction is carried out at a pressure of at least 10 bar.8. The process according to claim 1 , wherein the raw synthesis gas comprises water and carbon monoxide in a molar ratio of water to carbon monoxide of at least 1.9. The process according to claim 1 , wherein the residence time in the reactor ranges from 20 to 60 seconds.1011-. (canceled)12. The process according to claim 1 , wherein the catalytic water-gas shift reaction is carried out in the presence of a sulfur-resistant shift catalyst claim 1 , and wherein the sulfur-resistant shift catalyst is a cobalt and molybdenum-based catalyst.13. The process according to claim 5 , wherein the sulfur-resistant shift catalyst comprises an alkali metal selected from sodium claim 5 , potassium or caesium. The present invention relates to a process for the production of hydrogen-enriched synthesis gas by a catalytic water-gas shift reaction operated on a raw synthesis gas.Synthesis gas, or briefly syngas, is a combustible gas mixture ...

PROCESS FOR THE PRODUCTION OF HYDROGEN-ENRICHED SYNTHESIS GAS

Provided is a process for the production of hydrogen-enriched synthesis gas by a catalytic water-gas shift reaction operated on a raw synthesis gas. The process includes introducing a gaseous flow that includes at least one compound of formula (I) as defined herein in a first reactor containing including at least one metal selected from groups VI B and VII of the periodic table. The process also includes collecting a sulfur-containing gaseous flow from the first reactor, introducing the raw synthesis gas in a second reactor, and introducing the sulfur-containing gaseous flow in the second reactor, where the catalytic water-gas shift reaction takes place and includes a sulfur-resistant shift catalyst X, the sulfur-containing gaseous flow being introduced in the second reactor either directly through flow and/or after mixture through flow with the raw synthesis gas. The process also includes collecting an outlet flow from the second reactor containing hydrogen-enriched synthesis gas. 2. The process according to claim 1 , wherein the compound of formula (I) is selected from dimethyl disulphide and dimethyl sulfoxide.3. The process according to claim 1 , wherein the catalytic water-gas shift reaction is carried out with an inlet gas temperature of at least 230° C.4. The process according to claim 1 , wherein the first reactor is used at a temperature ranging from 100 to 600° C.5. The process according to claim 1 , wherein the first reactor is used at a pressure ranging from 0 to 60 bar.6. The process according to claim 1 , wherein the compound of formula (I) is continuously injected in the first reactor at a flow rate of 1 NI/h to 10 Nm/h.7. The process according to claim 1 , wherein a hydrogen flow is introduced in the first reactor claim 1 , said hydrogen flow coming from an exogenous source or being collected from the outlet flow of the second reactor.8. The process according to claim 1 , wherein the catalyst Xcomprises molybdenum claim 1 , tungsten claim 1 , nickel ...

PROCESS TO PREPARE A CHAR PRODUCT AND A SYNGAS MIXTURE

The invention is directed to a process to prepare a char product and a syngas mixture comprising hydrogen and carbon monoxide from a solid biomass feed comprising the following steps: (i) performing a continuously operated partial oxidation of the solid biomass feed at a gas temperature of between 700 and 1100° C. and at a solids residence time of less than 5 seconds, (ii) continuously separating the formed char particles as the char product from the formed gaseous fraction and (iii) subjecting the gaseous fraction obtained in step (ii) to a continuously operated partial oxidation and/or to a steam reforming to obtain the syngas mixture. The solid biomass feed has been obtained by torrefaction of a starting material comprising lignocellulose and is a sieve fraction wherein 99 wt % of the solid biomass particles is smaller than 2 mm. 1. A process to prepare a char product and a syngas mixture comprising hydrogen and carbon monoxide from a solid biomass feed comprising the following steps:(i) performing a continuously operated partial oxidation of the solid biomass feed at a gas temperature of between 700 and 1100° C. and at a solids residence time of less than 5 seconds thereby obtaining a gaseous fraction comprising hydrogen, carbon monoxide and a mixture of gaseous organic compounds and a solid fraction comprising of char particles,(ii) continuously separating the char particles as the char product from the gaseous fraction, and(iii) subjecting the gaseous fraction obtained in step (ii) to a continuously operated partial oxidation or to a steam reforming, or both, to obtain the syngas mixture, wherein the solid biomass feed has been obtained by torrefaction of a starting material comprising lignocellulose and wherein the solid biomass feed is a sieve fraction wherein 99 wt % of the solid biomass particles is smaller than 2 mm.2. The process according to claim 1 , wherein the gas temperature in step (i) is between 750 and 1000° C.3. The process according to claim 1 ...

TREATMENT METHOD FOR SEPARATING CARBON DIOXIDE AND HYDROGEN FROM A MIXTURE

The invention relates to a method fro treating a mixture in order to separate carbon dioxide and hydrogen from said mixture, in which: i) the mixture is cooled and partially condensed and a first liquid is separated from the rest of the mixture in a first phase separator; ii) a gas from or derived from a gas from the first phase separator is treated in a hydrogen pressure swing adsorption module in order to produce a hydrogen-rich gas and a hydrogen-depleted residual gas; and iii) said hydrogen-depleted residual gas or a gas derived from said depleted gas is cooled and partially condensed and a second liquid is separated from the remaining gas in a second phase separator, separate from the first phase separator, wherein the first and/or second liquid being rich in carbon dioxide. The invention also relates to an installation for implementing such a method. 115-. (canceled)16. A process for treating a mixture for the purpose of separating carbon dioxide and hydrogen from this mixture , the process comprising the steps of:i) cooling and partially condensing the mixture is cooled and then separating a first liquid from the mixture in a first phase separator;ii) treating a gas originating or derived from a top gas from the first phase separator in a pressure swing adsorption module for hydrogen to produce a hydrogen-rich gas and a hydrogen- depleted residual gas; andiii) cooling and partially condensing said hydrogen-depleted residual gas or a gas derived from said hydrogen-depleted gas and then separating a second liquid the remaining gas in a second phase separator that is different from the first phase separator,wherein the first liquid and/or second liquid or a liquid derived from the first liquid and/or second liquid originating from the first phase separator and/or from the second phase separator are rich in carbon dioxide as compared to the mixture,wherein the partial condensations in steps i) and iii) are performed in the same cryogenic unit.17. The process as ...

REACTOR AND PROCESS FOR PARTIAL OXIDATION

A process of partial oxidation is performed in a reactor which includes a reaction chamber and a burner assembly, wherein: the burner assembly has a single oxidant nozzle located within an fuel channel, said oxidant nozzle comprises a nozzle pipe and a nozzle outlet, the nozzle pipe and the fuel channel are arranged to produce a diffusion flame, the nozzle outlet has a shape with two or more elongate lobes projecting from a center of the nozzle pipe. 1. A process of partial oxidation of a gaseous hydrocarbon fuel to form a product gas containing hydrogen and carbon monoxide , wherein:said process is performed in a reactor including a vessel, a reaction chamber and at least one burner assembly;said burner assembly has a single oxidant nozzle;said reactor includes at least one fuel channel which is in communication with an inlet of said gaseous hydrocarbon fuel;said oxidant nozzle comprises an oxidant nozzle pipe and an oxidant nozzle outlet,the oxidant nozzle pipe and the fuel channel are arranged to produce a diffusion flame;the oxidant nozzle outlet has a shape with two or more elongate lobes projecting from an axis of the oxidant nozzle pipe;the process includes: feeding an oxidant in the oxidant nozzle of the reactor;feeding an hydrocarbon fuel in the fuel channel of the reactor, forming a diffusion flame at the outlet of the fuel nozzle.2. The process according to claim 1 , wherein said oxidant nozzle outlet of the reactor has two elongate lobes symmetrically arranged opposite to each other.3. The process according to claim 1 , wherein said oxidant nozzle outlet of the reactor has three or more elongate lobes which are radially arranged around the center of the oxidant nozzle pipe.4. The process according to claim 3 , wherein the radially arranged elongate lobes of the reactor have a regular angular spacing.5. The process according to claim 3 , wherein the number of radially arranged lobes of the reactor is two to eight.6. The process according to claim 1 , ...

Method of Producing a Cooled Syngas of Improved Quality

A system and method for processing unconditioned syngas first removes solids and semi-volatile organic compounds (SVOC), then removes volatile organic compounds (VOC), and then removes at least one sulfur containing compound from the syngas. Additional processing may be performed depending on such factors as the source of syngas being processed, the products, byproducts and intermediate products desired to be formed, captured or recycled and environmental considerations.

PROCESS FOR PREPARING A SYNGAS AND SYNGAS COOLING DEVICE

The invention relates to a process for the preparation of a syngas comprising hydrogen and carbon monoxide comprising the steps of: 1. A process for the preparation of a syngas comprising hydrogen and carbon monoxide comprising the steps of:(a) reacting a preheated methane comprising gas with an oxidizing gas to obtain a hot raw syngas comprising carbon monoxide and hydrogen;(b) cooling the hot raw syngas resulting from step (a) to obtain the syngas by indirect heat exchange against water to produce saturated steam;(c) further cooling the raw syngas obtained in step (b) by indirect heat exchange against a methane comprising gas to obtain a cooled raw syngas and the preheated methane comprising gas for use in step (a),wherein:(i) steps (b) and (c) take place in a single cooling device for combined indirect heat exchange against water and against the methane comprising gas; and(ii) the preheated methane comprising gas obtained in step (c) has a temperature between 400 and 650° C.2. The process according to claim 1 , wherein the methane comprising gas used in step (c) is first preheated to a temperature of up to 400° C. by indirect heat exchange against the cooled raw syngas leaving the single cooling device to obtain a further cooled raw syngas.3. The process according to claim 2 , wherein the water used in step (b) is first preheated by indirect heat exchange against the further cooled raw syngas.4. The process according to claim 1 , wherein the process comprises the further step of:(d) further cooling the cooled raw syngas obtained in step (c) by indirect heat exchange against water in the single cooling device to obtain further saturated steam and further cooled raw syngas.5. The process according to claim 1 , wherein the process comprises the further step of:(d′) further cooling the cooled raw syngas obtained in step (c) by indirect heat exchange against the saturated steam obtained in step (a) in the single cooling device to obtain superheated steam and further ...

METHOD AND DEVICE FOR PRODUCING SYNTHESIS GAS WITH CARBON DIOXIDE RETURN

A method and to a device for producing a synthesis gas, which contains carbon monoxide and hydrogen, wherein natural gas having a first carbon dioxide partial pressure (COpressure) is provided and is processed inter alia by means of a pressure increase to form a natural gas input for a thermochemical conversion, in which a synthesis raw gas having a second COpressure greater than the first COpressure is produced, from which synthesis raw gas at least carbon dioxide is subsequently separated in order to obtain the synthesis gas and carbon dioxide, at least some of which is returned and is used in the thermochemical conversion of the natural gas input. To separate carbon dioxide, the synthesis raw gas is conducted across the one membrane on the retentate side, which membrane is permeable to carbon dioxide and is flushed on the permeate side by the provided natural gas.

SYSTEMS AND METHODS FOR CONTROLLING ON-BOARD GENERATION AND USE OF HYDROGEN FUEL MIXTURES

This is a system for generating hydrogen on-board the vehicle from compressed natural gas (CNG) in select ratios to create hydrogen-enriched CNG (HCNG) fuel for use in internal combustion engines. The on-board generation of hydrogen is comprised of a reforming system of CNG fuel with direct contact with exhaust gases. The reforming system controls for production of HCNG fuel mixtures is based on specific engine operating conditions. The vehicle's engine controls and operating parameters are modified for combustion of selective ratios of HCNG fuel mixtures throughout engine operating cycle. The reforming system controls and engine controls modifications are also used to minimize combustion emissions and optimize engine performance. 1. An engine method of controlling an engine system , comprising:a combustion system configured to combust natural gas to generate energy and exhaust gas;a pre-reforming system configured to receive unreformed natural gas and coupled to the combustion system to receive at least a portion of the exhaust gas, the pre-reforming system configured to generate a partial oxidation reaction between the unreformed natural gas and the exhaust gas to generate partial oxidation reaction products;a reforming system coupled to the pre-reforming system and configured to reform the partial oxidation reaction products to produce reformed natural gas;a mixing system coupled to the reforming system and configured to mix reformed natural gas and unreformed natural gas that is provided as the natural gas to the combustion system; anda reforming control system coupled to the pre-reforming system and configured to control the supply of the exhaust gas to the pre-forming system so the supplied exhaust gas has a first ratio with the unreformed natural gas based on a first operating condition and is configured to control the supply of the exhaust gas so the supplied exhaust gas has a second ratio with the unreformed natural gas based on a second operating condition ...

Methods, Systems, And Apparatuses For Recycling Fischer-Tropsch Water And Fischer-Tropsch Tail Gas

A method of producing reformed gas as part of a Fischer-Tropsch (“FT”) hydrocarbon synthesis is disclosed, including the steps of superheating at least a first portion of an FT tail gas produced as a by-product of an FT synthesis process, and forming a mixed gas by injecting at least a portion of an FT water stream, produced as a by-product of an FT synthesis process, into the superheated FT tail gas to form a mixed gas. The mixed gas is used as a feed to a front end of a syngas preparation unit. The amount of at least a portion of the FT water stream is selected to keep the mixed gas at least mostly and preferably entirely in a vapor phase. In some embodiments, a water-gas shift reactor converts the mixed gas to a converted mixed gas upstream of the front end. Other methods, apparatuses and systems are disclosed. 1. A method of producing Fischer-Tropsch (“FT”) hydrocarbons via FT synthesis in an FT reactor having an FT synthesis catalyst , the method comprising:a. producing a reformed gas comprising hydrogen and carbon monoxide in a syngas preparation unit having a front end and a feed comprising a carbonaceous feedstock and steam;b. conditioning the reformed gas by removing process condensate therefrom;c. producing liquid FT hydrocarbons, an FT tail gas and an FT water stream using the conditioned reformed gas in the FT reactor, under FT conditions;d. superheating at least a first portion of the FT tail gas;e. injecting at least a first portion of the FT water stream into the at least a first portion of the superheated FT tail gas to form a mixed gas, wherein the amount of the at least a first portion of the FT water stream to be injected into the at least a first portion of the superheated FT tail gas to form the mixed gas is selected to keep the mixed gas in an at least mostly vapor phase; andf. recycling the mixed gas as part of the feed to the front end of the syngas preparation unit.2. The method of claim 1 , wherein the superheating step (d) comprises ...

TWO-STAGE GASIFIER AND GASIFICATION PROCESS WITH FEEDSTOCK FLEXIBILITY

A two-stage gasification reactor may include a reactor lower section and a reactor upper section. The reactor lower section may include (a) a lower reactor body, (b) two primary feed nozzles, configured to introduce at least one of a dry feedstock or a first slurried feedstock and located on opposing terminal ends of the lower reactor body, and (c) at least two secondary feed nozzles, configured to introduce a liquid hydrocarbon feedstock, located on the lower reactor body. The reactor upper section may include (a) an upper reactor body, (b) at least one upper feed nozzle, configured to introduce at least one of a dry feedstock or a first slurried feedstock, located on the upper reactor body, and (c) an outlet. 112-. (canceled)13. A two-stage gasification reactor , comprising: (a) a lower reactor body;', '(b) two primary feed nozzles, configured to introduce at least one of a dry feedstock or a first slurried feedstock, located on opposing terminal ends of the lower reactor body; and', '(c) at least two secondary feed nozzles, configured to introduce a liquid hydrocarbon feedstock, located on the lower reactor body;, 'a reactor lower section comprising (a) an upper reactor body;', '(b) at least one upper feed nozzle, configured to introduce at least one of a dry feedstock or a first slurried feedstock, located on the upper reactor body; and', '(c) an outlet., 'a reactor upper section comprising14. The two-stage gasification reactor of claim 13 , wherein the at least two secondary feed nozzles are oriented so they provide feeds along secondary feed vectors that maintain a vertical symmetry within the reactor lower section with feeds along primary feed vectors from the primary feed nozzles.15. The two-stage gasification reactor of claim 13 , wherein the at least two secondary feed nozzles and the primary feed nozzle are oriented so they provide feeds along feed vectors that intersect at a feed intersection point that is substantially in the center of the lower reactor ...

GENERATING POWER FROM A NATURAL GAS WITH CARBON DIOXIDE CAPTURE

In some implementations, one or more methods can include producing a hydrogen rich fuel gas for a gas turbine ballasted with nitrogen and steam and superheated to a temperature above its dew point. The fuel gas may have a minimal or reduced content of COor fuel components CO and CHwhich contain carbon so that when combusted in a suitable gas turbine there may be minimal or reduced emissions of COto the atmosphere. These example methods may result in a capture of the bulk of the carbon present in the total natural gas feed as COcompressed to pipeline delivery pressure for sequestration. 1. A method for producing fuel gas mixture comprising;exothermically reacting a first portion of a hydrocarbon feed stream with at least one of steam or an oxidant gas comprising molecular oxygen to produce an exothermically generated syn-gas 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 syn-gas product, wherein at least a portion of heat used in generation of the endothermically-reformed syn-gas product is obtained by recovering heat from the exothermically-generated syn-gas product and the endothermically reformed syn-gas product;cooling the combined syn-gas stream to produce steam in a heat recovery boiler;{'sub': '2', 'reducing the pressure of the cooled syn-gas stream in a power producing expansion turbine to the pressure required for a substantially COfree fuel gas feed stream to a power producing gas turbine;'}{'sub': 2', '2, 'catalytically reacting a combination of the endothermically-reformed syn-gas product and the exothermically-generated syn-gas product in one or more catalytic carbon monoxide shift reactors to generate a combined stream including additional Hand CO;'}cooling the combined syn-gas stream to near ambient temperature in a multipassage multi stream plate-fin heat exchanger which heats water required for steam production for the syn- ...

Methanol production system and methanol production method

A methanol production system of the present disclosure includes: a reformer including a reaction furnace configured to reform methane in a raw material gas to produce a reformed gas containing CO and H2; a reduced-gas generator configured to reduce CO2 to produce a reduced gas containing CO; and a methanol-containing gas generator configured to produce a methanol-containing gas which contains methanol from a reformed gas produced in the reaction furnace and a reduced gas produced in the reduced-gas generator.

Methods, Systems, And Apparatuses For Recycling Fischer-Tropsch Water And Fischer-Tropsch Tail Gas

A method of producing reformed gas as part of a Fischer-Tropsch (“FT”) hydrocarbon synthesis is disclosed, including the steps of superheating at least a first portion of an FT tail gas produced as a by-product of an FT synthesis process, and forming a mixed gas by injecting at least a portion of an FT water stream, produced as a by-product of an FT synthesis process, into the superheated FT tail gas to form a mixed gas. The mixed gas is used as a feed to a front end of a syngas preparation unit. The amount of at least a portion of the FT water stream is selected to keep the mixed gas at least mostly and preferably entirely in a vapor phase. In some embodiments, a water-gas shift reactor converts the mixed gas to a converted mixed gas upstream of the front end. Other methods, apparatuses and systems are disclosed. 1. A system for producing a syngas , the system comprising:a. a superheater for superheating a Fischer-Tropsch (“FT”) tail gas produced by an FT reactor;b. an injector for injecting at least a portion of an FT water stream produced by an FT reactor into the superheated FT tail gas to form a mixed gas for use as a feed to a front end of a syngas preparation unit.2. The system of claim 1 , wherein the syngas preparation unit comprises a steam methane reformer.3. The system of claim 1 , wherein the syngas preparation unit comprises an autothermal reformer.4. The system of claim 1 , wherein the syngas preparation unit comprises a partial oxidation reformer.5. The system of claim 1 , wherein claim 1 , wherein the syngas preparation unit comprises a hybrid reformer.6. The system of claim 1 , wherein the injector is configured to inject a pre-selected amount of the at least a portion of the FT water stream into the superheated FT tail gas to form the mixed gas claim 1 , the pre-selected amount being selected to keep the mixed gas in at least a mostly vapor phase.7. The system of claim 6 , further comprising a separator drum positioned to remove excess water from ...

A process for producing ammonia synthesis gas with high temperature shift and low steam-to-carbon ratio

A process for producing ammonia synthesis gas from a hydrocarbon-containing feedstock in a front-end, comprising the steps of steam reforming of said feedstock, obtaining a synthesis gas comprising hydrogen, carbon monoxide and carbon dioxide; a treatment of said synthesis gas including shift of carbon monoxide and subsequent removal of carbon dioxide, wherein the shift of the synthesis gas includes high-temperature shift with an iron-based catalyst and at a temperature greater than 300° C. and the global steam-to-carbon ratio of the front end is 2.6 or less; a corresponding plant and a method for revamping a front-end of an ammonia plant are also disclosed.

PROCESS AND PLANT FOR AT LEAST PARTIAL GASIFICATION OF SOLID ORGANIC FEED MATERIAL

A process for at least partial gasification of solid organic feed material, in which a tar-containing low-temperature carbonization gas is obtained by low-temperature carbonization from the feed material in a low-temperature gasifier and the low-temperature carbonization gas is then converted to a synthesis gas in a high-temperature gasifier by partial oxidation and subsequent partial reduction. The low-temperature carbonization gas is admixed with a second gas. A plant equipped for carrying out the process includes a low-temperature gasifier for obtaining the low-temperature carbonization gas from the feed material, a high-temperature gasifier for obtaining synthesis gas from the low-temperature carbonization gas, and means for admixing the low-temperature carbonization gas with the second gas. 1. A process for at least partial gasification of solid organic feed material , in which a tar-containing low-temperature carbonization gas is obtained by low-temperature carbonization from the feed material in a low-temperature gasifier and the low-temperature carbonization gas is then converted to a synthesis gas in a high-temperature gasifier by partial oxidation and subsequent partial reduction , characterized in that the low-temperature carbonization gas is admixed with a second gas comprising a fraction of the synthesis gas , of a gas mixture derived from the synthesis gas , or a combination thereof.2. The process as claimed in claim 1 , in which the low-temperature carbonization gas is admixed with the second gas in the low-temperature gasifier or between the low-temperature gasifier and the high-temperature gasifier.3. The process as claimed in claim 1 , in which the second gas is established at least on the basis of a tar content or a temperature difference of the low-temperature carbonization gas.4. The process as claimed in claim 1 , in which the low-temperature carbonization gas in the low-temperature gasifier is obtained from the solid organic feed material by ...

SYSTEMS AND METHODS FOR CONTROLLING ON-BOARD GENERATION AND USE OF HYDROGEN FUEL MIXTURES

This is a system for generating hydrogen on-board the vehicle from compressed natural gas (CNG) in select ratios to create hydrogen-enriched CNG (HCNG) fuel for use in internal combustion engines. The on-board generation of hydrogen is comprised of a reforming system of CNG fuel with direct contact with exhaust gases. The reforming system controls for production of HCNG fuel mixtures is based on specific engine operating conditions. The vehicle's engine controls and operating parameters are modified for combustion of selective ratios of HCNG fuel mixtures throughout engine operating cycle. The reforming system controls and engine controls modifications are also used to minimize combustion emissions and optimize engine performance. 1. A method for generating on-board hydrogen to produce HCNG for use in CNG power vehicles.2. A system with integrated control systems for producing HCNG alternative fuel , with calibrated ratios of hydrogen enrichment , on-board a motor vehicle comprising: a POX reformer;', 'a steam reformer;', 'a carbon dioxide reformer;', 'a high-temperature water gas shift reformer;', 'a low-temperature water gas shift reformer;, 'an on-board reforming system comprisinga reforming system controls, synchronized with ECU, to produce calibrated ratios of hydrogen in HCNG alternative fuel;{'sub': '2', 'an Engine Controls Unit, ECU, configured to operate with variable Hratios in HCNG alternative fuel.'} The present application claims the benefit of US Provisional Patent Application No. 61/873,491, filed Sep. 4, 2013, which application is incorporated by reference herein in its entirety.This invention relates generally to the on-board vehicle generation of hydrogen-enriched natural gas fuel for use as an alternative fuel, and particularly to integrated control systems for generation of hydrogen fuel mixtures and use in internal combustion engines.Hydrogen-enriched Compressed Natural Gas (HCNG) is a clean alternative fuel that combines the advantages of ...

METHOD, APPARATUS, AND COMPUTER-READABLE MEDIA FOR VORTEX ARC REACTOR

Vortex arc reactor apparatus and method provide a nozzle with converging, throat, and diverging portions. Input structure inputs a reactant and an oxidant into the converging portion. Ignition structure ignites the input reactant and oxidant. A vortex-creating structure creates a vortex of the ignited reactant and oxidant in the converging portion. The input structure, the vortex-creating structure, and the nozzle converging and throat portions are configured to provide a throat-portion-vortex of ignited reactant and oxidant that has an angular velocity which provides (i) negatively-charged particles in an exterior portion of the throat-portion-vortex, (ii) positively-charged particles in an interior portion of the throat-portion-vortex, and (iii) at least one arcing reaction between the positively-charged particles and the negatively-charged particles, to form syngas and at least one aromatic liquid in the nozzle diverging portion. Gas/liquid separation structure is preferably configured to separate the formed syngas from the at least one aromatic liquid. 1. Apparatus for producing a syngas and at least one aromatic liquid , comprising:a nozzle having a converging portion, a throat portion, and a diverging portion;input structure configured to input a reactant and an oxidant into the converging portion of the nozzle;ignition structure configured to ignite the input reactant and oxidant;vortex-creating structure configured to create a vortex of the ignited reactant and the oxidant in the converging portion of the nozzle; andthe input structure, the vortex-creating structure, and the nozzle converging and throat portions being configured to provide a throat-portion-vortex of ignited reactant and oxidant that has an angular velocity which provides (i) negatively-charged particles in an exterior portion of the throat-portion-vortex, (ii) positively-charged particles in an interior portion of the throat-portion-vortex, and (iii) at least one reaction between the ...

GAS-TO-LIQUID TECHNOLOGY

Gas-to-liquids processes for treating natural gas, including the steps of subjecting the natural gas to expansion through a flow restrictor so as to undergo cooling through the Joule Thomson effect. The processes then separate the resulting liquids from the remaining natural gas and processing the natural gas to form a synthesis gas. The synthesis gas is subjected to Fischer-Tropsch synthesis and the output from the Fischer-Tropsch synthesis is separated into a hydrocarbon product and an aqueous phase and the aqueous phase is steam stripped to extract the oxygenates which are then injected into the natural gas stream upstream of the flow restrictor. 119-. (canceled)20. A gas-to-liquids process for treating natural gas , including the steps of subjecting the natural gas to expansion through a flow restrictor so as to undergo cooling through the Joule Thomson effect , followed by separating the resulting liquids from the remaining natural gas , further comprising the steps of processing the natural gas to form a synthesis gas , and subjecting the synthesis gas to Fischer-Tropsch synthesis and wherein the output from the Fischer-Tropsch synthesis is separated into a hydrocarbon product and an aqueous phase , wherein the aqueous phase is steam stripped to extract the oxygenates which are then injected into the natural gas stream upstream of the flow restrictor.21. A process as claimed in including the step of transferring heat between the natural gas before it reaches the flow restrictor claim 20 , and at least one fluid that has been cooled by passage through the flow restrictor.22. A process as claimed in claim 20 , wherein the step of subjecting the natural gas to expansion through a flow restrictor is carried out only once.23. A process as claimed in claim 20 , wherein the step of processing the natural gas to form a synthesis gas results in a synthesis gas containing excess hydrogen claim 20 , and further comprising the step of removing excess hydrogen from the ...

METHOD FOR MINIMIZING NOx EMISSIONS DURING POX BASED SYNGAS PLANT STARTUP

A method for heating a partial oxidation reactor system including a burner system is provided. The method includes utilizing a flue gas stream derived from combustion process using an oxygen rich stream and a hydrocarbon fuel stream. The method may include a first burner system utilized during normal plant operation performing partial combustion, a second burner system utilized for heating during start-up phase performing complete combustion. The first burner system may be different than, or the same as, the second burner system. The method may include a second flue gas stream exiting the partial oxidation reactor, and wherein at least a portion of the second flue gas stream is recycled back to the burner system. The method may include a third flue gas stream derived from a downstream located equipment, wherein at least of portion of the third flue gas stream is recycled back to the burner system. 1. A method for heating a partial oxidation reactor system comprising a burner system , the method comprising utilizing a flue gas stream derived from combustion process using an oxygen rich stream and a hydrocarbon fuel stream.2. The method of claim 1 , the burner system further comprising a first burner system utilized during normal plant operation performing partial combustion claim 1 , a second burner system utilized for heating during start-up phase performing complete combustion.3. The method of claim 2 , wherein the first burner system is different than the second burner system4. The method of claim 3 , wherein the first burner system is the same as the second burner system5. The method of claim 1 , further comprising a second flue gas stream exiting the partial oxidation reactor claim 1 , and wherein at least a portion of the second flue gas stream is recycled back to the burner system.6. The method of claim 1 , further comprising a third flue gas stream derived from a downstream located equipment claim 1 , wherein at least of portion of the third flue gas stream ...

Zero emissions sulphur recovery process with concurrent hydrogen production

Disclosed is a process for the concurrent production of hydrogen and sulphur from a H 2 S-containing gas stream, with zero emissions. The method comprises the thermal oxidative cracking of H 2 S so as to form H 2 and S 2 . Preferably, the oxidation is conducted using oxygen-enriched air, preferably pure oxygen. The ratio H 2 S/O 2 in the feedstock is higher than 2:1, preferably in the range of 3:1-5:1.

Reducing and/or harvesting drag energy from transport vehicles, including for chemical reactors, and associated systems and methods

The present disclosure is directed to systems and methods for reducing and/or harvesting drag energy from transport vehicles. A system in accordance with a particular embodiment includes a mobile transport platform, a donor substance source carried by the platform, and a thermochemical reactor carried by the platform and coupled to the donor substance. The reactor is configured to carry out a non-combustion dissociation process that dissociates the donor substance into a first constituent and a second constituent. An energy extraction system carried by the transport platform and positioned to extract energy from an airstream passing the transport platform is coupled to the reactor to provide energy for the dissociation process.

PROCESS FOR GAS-HEATED REFORMING OF A HYDROCARBON SOURCE AND A RELATED PLANT

A process and equipment for steam reforming of a hydrocarbon source gas, where the hydrocarbon source gas and a steam flow are partially reformed while passing in a bundle of tubes () of a reformer (), with a catalytically active inner surface; a partially reformed product gas () leaving said tubes is mixed with an oxidation agent () and subject to a combustion process; a combusted partially reformed gas () is introduced in the shell side of said reformer and further reformed by contact with the outer surface of said tubes (), said outer surface of the tubes being also catalytically active. 1. A process for reforming of a source gas containing a hydrocarbon source , comprising the steps of:a first stage of reforming of said source gas by feeding the source gas into a plurality of externally heated tubes, which form a tube side of a reformer, at least a portion of the inner surface of said tubes being catalytically active, thus producing a primarily reformed first product gas;a partial combustion of said first product gas, which is effected with a suitable oxidation agent, thus obtaining a second product gas, anda second stage of reforming of said second product gas, which is carried out in a shell side of said reformer, by contact with the outer surface of said tubes, at least a portion of said outer surface of the tubes being catalytically active, and said second product gas also providing the external heating of said tubes and heat input for the first-stage reforming of the source gas.2. The process according to claim 1 , where said partial combustion of said first product gas takes place in a burner external or internal to said reformer.3. The process according to any of the preceding claim 1 , the process being a steam reforming process and said source gas comprising steam and a hydrocarbon source.4. The process according to claim 3 , the hydrocarbon source being natural gas or methane.5. An equipment for reforming of a source gas containing a hydrocarbon claim ...

PROCESS AND PLANT FOR PREPARATION OF ONE OR MORE REACTION PRODUCTS

A process for preparing one or more reaction products, in which a first methane-rich feed stream is subjected to a partial oxidation process and/or an autothermal reforming process and a second methane-rich feed stream is subjected to a steam reforming process, in which a first synthesis gas-containing output stream is formed from the first methane-rich feed stream and a second synthesis gas-containing output stream is formed from the second methane-rich feed stream and these synthesis gas streams are used to form a collective synthesis gas stream and fluid from the collective synthesis gas stream is subjected to a molecular weight-increasing reaction in a synthesis feed stream to obtain a synthesis output stream comprising carbon dioxide and the reaction product(s). At least one carbon dioxide-rich first recycle stream is formed from fluid from the synthesis output stream and fluid from the first recycle stream is subjected to the steam reforming process. 1. A process for preparing one or more reaction products , in which a first methane-rich feed stream is subjected to a partial oxidation process and/or an autothermal reforming process and a second methane-rich feed stream is subjected to a steam reforming process , and in which a first synthesis gas-containing output stream is formed by means of the partial oxidation process and/or the autothermal reforming process and a second synthesis gas-containing output stream is formed by means of the steam reforming process , where synthesis gas from the first output stream and synthesis gas from the second output stream are used to form a collective synthesis gas stream and fluid from the collective synthesis gas stream is subjected to a molecular weight-increasing reaction in a synthesis feed stream to obtain a synthesis output stream comprising carbon dioxide and the reaction products , characterized in that at least one carbon dioxide-rich first recycle stream is formed from fluid from the synthesis output stream , ...

Liquid fuel cpox reformers and methods of cpox reforming

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

SYSTEMS AND METHODS FOR POWER PRODUCTION WITH INTEGRATED PRODUCTION OF HYDROGEN

The present disclosure relates to systems and methods useful for power production. In particular, a power production cycle utilizing COas a working fluid may be configured for simultaneous hydrogen production. Beneficially, substantially all carbon arising from combustion in power production and hydrogen production is captured in the form of carbon dioxide. Further, produced hydrogen (optionally mixed with nitrogen received from an air separation unit) can be input as fuel in a gas turbine combined cycle unit for additional power production therein without any atmospheric COdischarge. 1. A system for combined power production and hydrogen production , the system comprising:a power production unit wherein pressurized carbon dioxide is expanded for power production;a hydrogen production unit wherein a hydrocarbon fuel is partially oxidized to produce a synthesis gas from which hydrogen is separated; andone or more flow components configured for passage of one or more streams between the power production unit and the hydrogen production unit.2. The system of claim 1 , wherein the power production unit comprises:a combustor configured to receive a hydrocarbon fuel and oxygen and output a heated stream comprising at least the pressurized carbon dioxide;a turbine configured to receive and expand the heated stream comprising the pressurized carbon dioxide from the combustor to produce the power and form a heated stream comprising the expanded carbon dioxide;a recuperative heat exchanger configured to receive the heated stream comprising the expanded carbon dioxide and form a cooled stream comprising carbon dioxide;a separator configured to receive the cooled stream comprising the carbon dioxide from the recuperative heat exchanger and provide a stream of the carbon dioxide; anda compressor configured to receive the stream of the carbon dioxide from the separator and compress the carbon dioxide.3. The system of claim 2 , wherein the hydrogen production unit comprises:a ...

PLANT AND PROCESS FOR THE EFFICIENT UTILIZATION OF EXCESS ELECTRIC ENERGY

In a plant comprising a first apparatus for the electrochemical or electrothermal production of hydrogen, which produces a first hydrogen stream; a second apparatus for producing hydrogen from a hydrocarbon by steam reforming, partial oxidation or dehydrogenation, which produces a second hydrogen stream; a hydrogen conduit or a hydrogen consumer to which both the first hydrogen stream and the second hydrogen stream are fed; and a control device which matches the production of hydrogen in the first apparatus and in the second apparatus in such a way that the total amount of first hydrogen stream and second hydrogen stream corresponds to a predetermined value, excess electric energy can be efficiently utilized by operating the apparatus for the electrochemical or electrothermal production of hydrogen with excess electric energy. 114-. (canceled)15. A plant for the efficient utilization of excess electric energy , comprising:a) a first apparatus for the electrochemical or electrothermal production of hydrogen, which produces a first hydrogen stream;b) a second apparatus for producing hydrogen from a hydrocarbon by steam reforming, partial oxidation or dehydrogenation, which produces a second hydrogen stream;c) a hydrogen conduit or a hydrogen consumer to which both the first hydrogen stream and the second hydrogen stream are fed; andd) a control device matching the production of hydrogen in the first apparatus and in the second apparatus in such a way that the total amount of first hydrogen stream and second hydrogen stream corresponds to a predetermined value.16. The plant of claim 15 , wherein the second apparatus is an apparatus for the steam reforming of natural gas.17. The plant of claim 15 , wherein the first apparatus is an apparatus for the electrolysis of an aqueous solution to form hydrogen and oxygen.18. The plant of claim 15 , wherein the first apparatus is an apparatus for chloralkali electrolysis.19. The plant of claim 15 , wherein the first apparatus is ...

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 ...

SYSTEMS AND METHODS RELATED TO SYNGAS TO OLEFIN PRODUCTION

In accordance with the present invention, disclosed herein is a method comprising the steps for producing lower molecular weight hydrocarbons. Also disclosed herein, is a system utilized to produce low molecular weight hydrocarbons. 1. A method comprising the steps of:{'sub': '2', 'a) providing natural gas comprising methane and N;'}{'sub': 2', '2, 'b) removing at least a portion of the Nfrom the natural gas, thereby producing a first gas comprising methane and less than about 2 mole % of N;'}{'sub': '2', 'c) converting at least a portion of the first gas to synthesis gas comprising Hand CO;'}{'sub': '2', 'd) converting at least a portion of the synthesis gas to a first product stream comprising methane, C2-C9 hydrocarbons, C10+ hydrocarbons, unreacted synthesis gas, and CO; and'}e) separating at least a portion of the methane from the first product stream.2. The method of claim 1 , wherein the step of converting at least a portion of the first gas to synthesis gas comprising Hand CO is performed by a partial oxidation process in a partial oxidation reactor.3. The method of claim 2 , wherein the method further comprises the steps of:f) separating at least a portion of the C10+ hydrocarbons from the first product stream; and{'sub': '2', 'g) recycling at least a portion of the separated C10+ hydrocarbons back into the step of converting at least a portion of the first gas to synthesis gas comprising Hand CO is performed by partial oxidation process in a partial oxidation reactor.'}4. The method of claim 1 , wherein the first gas comprises less than about 1.5 mole % of N.5. The method of claim 1 , wherein at least about 80 wt % of the first gas is converted to the synthesis gas comprising Hand CO.6. The method of claim 1 , wherein the first product stream comprises at least about 60 wt % of C2-C5 hydrocarbons.7. The method of claim 1 , wherein the first product stream comprises from about 40 wt % to about 70 wt % of C2-C5 olefins.8. The method of claim 1 , wherein the ...

SYSTEM FOR MANUFACTURING AROMATIC COMPOUND AND METHOD FOR MANUFACTURING SAME

A system (A) for manufacturing an aromatic compound according to the present invention includes: a first manufacturing device () that synthesizes a target substance from natural gas; a second manufacturing device that synthesizes an aromatic compound by a catalytic reaction from the natural gas and supplies a mixed gas mainly including unreacted methane and by-product hydrogen to the first manufacturing device () to manufacture the target substance; and a hydrogen separation device (A) that separates hydrogen from purge gas generated from the first manufacturing device () and supplies the same to the second manufacturing device (A) to regenerate the catalyst used for the catalytic reaction. 1. A system for manufacturing an aromatic compound , the system comprising:a first manufacturing device that synthesizes a target substance from natural gas;a second manufacturing device that synthesizes an aromatic compound from the natural gas via a catalytic reaction, and supplies a mixed gas mainly including unreacted methane and by-product hydrogen to the first manufacturing device to manufacture the target substance; anda hydrogen separation device that separates hydrogen from purge gas generated from a synthesis reaction of the first manufacturing device, and supplies the hydrogen to the second manufacturing device to regenerate a catalyst used in the catalytic reaction.2. The system for manufacturing an aromatic compound according to claim 1 , further comprising:a third manufacturing device that synthesizes methane via a methanation reaction from carbon dioxide recovered from exhaust gas of the first manufacturing device and the hydrogen supplied from the hydrogen separation device, and supplies the methane to the second manufacturing device as a raw material.3. The system for manufacturing an aromatic compound according to claim 1 , wherein:the target substance is ammonia;the aromatic compound is one or more types of aromatic compound selected from the group consisting ...

Carbon Efficient Process for Converting Methane to Olefins and Methanol by Oxidative Coupling of Methane

A method for producing olefins and methanol comprising introducing a first reactant mixture comprising CHand Oto a first reaction zone; allowing the first reactant mixture to react via an OCM reaction to form a first product mixture characterized by a first H/CO molar ratio; introducing a second reactant mixture comprising the first product mixture and an ethane stream to a second reaction zone, wherein ethane of the second reactant mixture undergoes a cracking reaction to produce ethylene; recovering a second product mixture from the second reaction zone, wherein the second product mixture is characterized by a second H/CO molar ratio, and wherein the second H/CO molar ratio is greater than the first H/CO molar ratio; recovering from the second product mixture a methanol production feed stream comprising methane, Hand CO; and introducing the methanol production feed stream to a third reaction zone to produce methanol. 1. A method for producing olefins and methanol comprising:{'sub': 4', '2, '(a) introducing a first reactant mixture to a first reaction zone, wherein the first reactant mixture comprises methane (CH) and oxygen (O), and wherein the first reaction zone is characterized by a first reaction zone temperature of from about 700° C. to about 1,100° C.;'}{'sub': 4', '2+', '2', '2', '2', '2', '2+', '2', '3+', '2', '2', '6', '2', '4, '(b) allowing at least a portion of the first reactant mixture to react via an oxidative coupling of CH(OCM) reaction to form a first product mixture, wherein the first product mixture comprises C hydrocarbons, hydrogen (H), carbon monoxide (CO), water, CO, and unreacted methane, wherein the first product mixture is characterized by a first hydrogen (H) to carbon monoxide (CO) (H/CO) molar ratio, wherein the C hydrocarbons comprise Chydrocarbons and C hydrocarbons, and wherein the Chydrocarbons comprise ethane (CH) and ethylene (CH);'}(c) introducing a second reactant mixture comprising at least a portion of the first product ...

BURNER FOR THE PRODUCTION OF SYNTHESIS GAS

A burner suitable for the over stoichiometric combustion of a hydrocarbon source, comprising a nozzle () for the formation of a diffusion flame outside the burner, and said nozzle () comprising one () or more () tubular bodies which define a channel () or a plurality of coaxial channels () for respective reactant streams, wherein the or each of the tubular bodies forming said nozzle () are made of a technical ceramic material. 1. A process burner suitable for the over stoichiometric combustion of a hydrocarbon source , the burner comprising a body and a nozzle associated to said body , wherein: said nozzle is arranged for the formation of a diffusion flame outside said process burner , said process burner has a feeding side with at least one inlet for a reactant stream , and an opposite end side with an outlet section which defines a boundary between a feeding region and a combustion region , the burner being configured in such a way that combustion take place downstream of said outlet section , said nozzle comprises at least one tubular body to define at least one channel for said reactant stream , ending at said outlet section of said nozzle , and said at least one tubular body is integrally made of a technical ceramic material , and said at least one reactant stream are confined by said at least one ceramic body until the reaching of said outlet section.2. The burner according to claim 1 , said at least one tubular body being made in a single piece.3. The burner according to claim 1 , said nozzle comprising a plurality of tubular bodies to define coaxial channels for respective reactant streams such as for example fuel and oxidant.4. The burner according to claim 1 , said technical ceramic material having a thermal conductivity of at least 10 W/(m K) claim 1 , and an elastic modulus of at least 40 GPa.5. The burner according to claim 4 , said technical ceramic material having at least one of the following properties: a thermal conductivity in the range 10 to 230 ...

Gasifier Having Integrated Fuel Cell Power Generation System

A direct carbonaceous material to power generation system integrates one or more solid oxide fuel cells (SOFC) into a fluidized bed gasifier. The fuel cell anode is in direct contact with bed material so that the Hand CO generated in the bed are oxidized to HO and COto create a push-pull or source-sink reaction environment. The SOFC is exothermic and supplies heat within a reaction chamber of the gasifier where the fluidized bed conducts an endothermic reaction. The products from the anode are the reactants for the reformer and vice versa. A lower bed in the reaction chamber may comprise engineered multi-function material which may incorporate one or more catalysts and reactant adsorbent sites to facilitate excellent heat and mass transfer and fluidization dynamics in fluidized beds. The catalyst is capable of cracking tars and reforming hydrocarbons. 1. A method of steam reforming carbonaceous material to produce Hand CO while simultaneously producing power , the method comprising:providing a steam reformer vessel having a fluidized bed containing bed material;providing at least one fuel cell element which protrudes into the fluidized bed, the at least one fuel cell element comprising an outer anode and an inner cathode with the outer anode being in direct contact with the bed material and the cathode being supplied with an oxidant;introducing carbonaceous material and superheated steam into the fluidized bed; and (i) the fuel cell element outputs power;', '(ii) the superheated steam reacts with the carbonaceous material to produce hydrogen and carbon monoxide in the fluidized bed;', '(iii) oxygen is transported from the cathode to the anode and reacts with hydrogen in the fluidized bed to produce additional steam for steam reforming the carbonaceous material into additional hydrogen and carbon monoxide; and', '(iv) the bed material operates at a temperature of about 600° C. to about 1,000° C., 'operating the fluidized bed such that2. The method according to claim ...

PROCESS AND PLANT FOR PRODUCING A PURIFIED AND CONVERTED SYNTHESIS GAS

An integrated process for producing a purified and converted synthesis gas and a corresponding plant including initially converting in a synthesis gas generation stage a carbon-containing input material into a raw synthesis gas which in a subsequent CO conversion zone is altered in respect of its H/CO ratio and finally sent to a gas scrubbing zone operating according to a physical gas scrubbing process with methanol as the absorption medium in which the content of unwanted gas constituents, in particular of acidic gas constituents, in the synthesis gas is reduced. 2. The process of claim 1 , wherein before introduction into the CO conversion zone the raw synthesis gas product stream passes through a protective bed filled with an adsorbent or absorbent selective for metal carbonyls claim 1 , wherein the methanol purge stream is added to the raw synthesis gas product stream upstream of the protective bed.3. The process of claim 2 , wherein the methanol purge stream is added to the raw synthesis gas product stream in liquid form.4. The process of claim 2 , wherein the methanol purge stream is evaporated before or during its addition to the raw synthesis gas product stream claim 2 , wherein the evaporation heat is supplied by direct or indirect heat exchange with the raw synthesis gas product stream.5. The process of claim 1 , wherein the CO conversion zone operates according to the principle of raw gas conversion (raw gas shift).6. The process of claim 1 , wherein the CO conversion zone comprises a plurality of regions filled with one or more catalysts active for the raw gas conversion.7. The process of claim 1 , wherein the gas scrubbing zone comprises a hot regeneration apparatus for regeneration of methanol laden with acidic gas constituents claim 1 , wherein the liquid methanol purge stream laden with trace impurities is obtained from the bottoms product and/or the reflux from the hot regeneration apparatus and is discharged from the hot regeneration apparatus.9. ...

METHOD AND DEVICE FOR INTRODUCING REACTIVE GASSES INTO A REACTION CHAMBER

A method and a device for the separate introduction of a fuel gas and also of an oxidizing agent into the reaction chamber of a tubular reactor, in order there to be mixed and reacted with the release of heat. Not only the fuel gas but also the oxidizing agent are introduced into the reaction chamber in each case in more than three gas jets, wherein the margin between a fuel gas jet and an oxidizing agent jet as adjacent as possible thereto, on entry into the reaction chamber, is between 2 and 500 mm, preferably between 5 and 50 mm. 12500. A method for the separate introduction of a fuel gas and an oxidizing agent into the reaction chamber of a tubular reactor , in order there to be mixed and reacted with the release of heat , characterized in that the fuel gas and also the oxidizing agent are introduced into the reaction chamber in more than three gas jets , wherein the spacing between a fuel gas jet and an oxidizing agent jet as adjacent as possible thereto , on entry into the reaction chamber , is between and mm.2. The method according to claim 1 , characterized in that the oxidizing agent jets are introduced into the reaction chamber in parallel to one another.3. The method according to claim 2 , characterized in that at least one fuel gas jet is assigned to an oxidizing agent jet in such a manner that the axes of the two gas jets enclose an angle which is between 5° and 75°.4. The method according to claim 3 , characterized in that at least two fuel gas jets are assigned to an oxidizing agent jet in such a manner that they drive a turbulent flow around the axis of the oxidizing agent jet.5. method according to claim 1 , characterized in that fuel gas and oxidizing agent are introduced into the reaction chamber at minimum velocities which are greater in each case by the factor 1/F than the mean flow velocity of the product gas formed in the reaction of the two gasses in the reaction chamber of the tubular reactor claim 1 , wherein F is dependent on the pressure ...

PROCESS FOR PROVIDING HEAT TO INDUSTRIAL FACILITIES

A process for providing heat to an industrial facility comprises contacting a hydrocarbon fuel with oxygen in a reaction zone under partial oxidation conditions including a below stoichiometric oxygen to fuel molar ratio for full combustion to generate heat in the reaction zone and produce a gaseous effluent stream containing carbon monoxide. At least part of the carbon monoxide from the gaseous effluent stream is converted to one or more of chemical products different from carbon monoxide transferring at least part of the heat generated in reaction zone and/or contained in the gaseous effluent stream is transferred to a separate operation in the industrial facility. 1. A process for providing heat to an industrial facility , the process comprising:(a1) contacting a hydrocarbon fuel with oxygen in a reaction zone under partial oxidation conditions including a below stoichiometric oxygen to fuel molar ratio for full combustion to generate heat in the reaction zone and produce a gaseous effluent stream containing carbon monoxide;(b1) converting at least part of the carbon monoxide from the gaseous effluent stream to one or more of chemical products different from carbon monoxide; and(c1) transferring at least part of the heat generated in reaction zone and/or contained in the gaseous effluent stream to an operation in the industrial facility other than the contacting (a1) and the converting (b1).2. The process of claim 1 , wherein steam is also supplied to the reaction zone in (a1).3. The process of claim 2 , wherein the reaction zone includes an auto-thermal reforming reactor.4. The process of claim 1 , wherein the industrial facility is a refinery or a petrochemical plant.5. The process of claim 1 , wherein the gaseous effluent stream exiting the reaction zone is at a temperature of at least 1500° F. (815° C.).6. The process of claim 1 , wherein the operation in the industrial facility is conducted at an inlet temperature of 980° F. (527° C.) or below.7. The process ...

PROCESS FOR INTEGRATING A PARTIAL OXIDATION PLANT WITH AN OXY-COMBUSTION PLANT UTILIZING A STEAM TURBINE

A method of co-producing a carbon dioxide containing stream and a syngas stream, including introducing a high-pressure hydrocarbon containing stream and a high-pressure oxygen containing stream into a syngas generator, thereby producing a high-pressure syngas stream, introducing a low-pressure hydrocarbon containing stream and a low-pressure oxygen containing stream into an oxy-combustion device, thereby producing a low-pressure carbon dioxide containing stream, and introducing the low-pressure carbon dioxide containing stream into a waste het boiler, thereby producing steam, and introducing the steam into a work expander, thereby generating work and a carbon dioxide containing stream. 1. A method of co-producing a carbon dioxide containing stream and a syngas stream , comprising:introducing a high-pressure hydrocarbon containing stream and a high-pressure oxygen containing stream into a syngas generator, thereby producing a high-pressure syngas stream,introducing a low-pressure hydrocarbon containing stream and a low-pressure oxygen containing stream into an oxy-combustion device, thereby producing a low-pressure carbon dioxide containing stream, andintroducing the low-pressure carbon dioxide containing stream into a waste het boiler, thereby producing steam, andintroducing the steam into a work expander, thereby generating work and a carbon dioxide containing stream.2. The method of claim 1 , wherein the high-pressure syngas stream is suitable for producing a downstream product.3. The method of claim 1 , wherein the high-pressure syngas stream is suitable for producing a downstream product without further syngas compression.4. The method of claim 1 , wherein the carbon dioxide containing stream is suitable for downstream separation.5. The method of claim 1 , wherein the downstream product is methanol produced in a methanol reactor.6. The method of claim 1 , wherein the downstream product is ammonia produced in an ammonia reactor.7. The method of claim 6 , wherein ...

NOVEL PROCESS FOR INTEGRATING A PARTIAL OXIDATION SYNGAS PRODUCTION PLANT WITH AN OXYGEN COMBUSTION PROCESS

A method of co-producing a carbon dioxide containing stream and a syngas stream, including, introducing a first high-pressure hydrocarbon containing stream and a first high-pressure oxygen containing stream into a syngas generator, thereby producing a high-pressure syngas stream, introducing a second high-pressure hydrocarbon containing stream and a second high-pressure oxygen containing stream into an oxy-combustion device, thereby producing a high-pressure carbon dioxide containing stream, and introducing the high-pressure carbon dioxide containing stream into a work expander, thereby generating work and a carbon dioxide containing stream. 1. A method of co-producing a carbon dioxide containing stream and a syngas stream , comprising:introducing a first high-pressure hydrocarbon containing stream and a first high-pressure oxygen containing stream into a syngas generator, thereby producing a high-pressure syngas stream,introducing a second high-pressure hydrocarbon containing stream and a second high-pressure oxygen containing stream into an oxy-combustion device, thereby producing a high-pressure carbon dioxide containing stream, andintroducing the high-pressure carbon dioxide containing stream into a work expander, thereby generating work and a carbon dioxide containing stream.2. The method of claim 1 , wherein the high-pressure syngas stream is suitable for producing a downstream product.3. The method of claim 1 , wherein the high-pressure syngas stream is suitable for producing a downstream product without further syngas compression.4. The method of claim 1 , wherein the carbon dioxide containing stream is suitable for downstream separation.5. The method of claim 1 , wherein the downstream product is methanol produced in a methanol reactor.6. The method of claim 1 , wherein the downstream product is ammonia produced in an ammonia reactor.7. The method of claim 6 , wherein a high-pressure nitrogen stream is combined with the high-pressure syngas stream claim 6 , ...

Process for using biogenic carbon dioxide derived from non-fossil organic material

The present disclosure provides a process for forming a biogenic carbon-based fuel or a fuel intermediate from biogenic carbon dioxide and hydrogen. The hydrogen is sourced from a process that produces hydrogen and fossil carbon dioxide from a fossil-fuel hydrocarbon and separates the fossil carbon dioxide from the hydrogen. The process may further comprise carrying out or arranging for one or more parties to carry out at least one step that contributes to a reduction in the GHG emissions of the biogenic carbon-based fuel, or a fuel made from the fuel intermediate, of at least 20% relative to a gasoline baseline. In various embodiments this includes (a) introducing the fossil carbon dioxide underground, and/or (b) using a biogenic carbon-based product selected from a chemical and energy product produced from the non-fossil organic material to displace the use or production of a corresponding fossil-based product.

PROCESS AND PLANT FOR PRODUCING A SYNTHESIS GAS PRODUCT STREAM HAVING AN ADJUSTABLE H2/CO RATIO AND A PURE HYDROGEN STREAM

Proposed are a process and a plant for producing a synthesis gas product stream having an adjustable H/CO ratio and a pure hydrogen stream, wherein it is provided according to the invention that a substream of a deacidified synthesis gas stream is supplied to a membrane separation plant fitted with a hydrogen-selective membrane and the remaining substream is supplied to a pressure swing adsorption plant, wherein the latter affords a pure hydrogen stream and a fuel gas stream. The hydrogen-enriched permeate stream obtained from the membrane separation is likewise supplied to the pressure swing adsorption plant, thus enhancing the yield of pure hydrogen. The hydrogen-depleted retentate stream obtained from the membrane separation is discharged as a synthesis gas product stream and if of a suitable composition may be utilized as oxo gas. 1. A process for producing a synthesis gas product stream having an adjustable hydrogen-carbon monoxide ratio (H/CO ratio) and a pure hydrogen stream from an input stream containing hydrocarbons , comprising:(a) providing the input stream containing hydrocarbons; (b1) a steam reforming stage, or', '(b2) an autothermal reforming stage (ATR), or', '(b3) a partial oxidation stage (POX), or', '(b4) a combination of at least two of the stages (b1) to (b3);, '(b) supplying the input stream containing hydrocarbons to a synthesis gas production plant comprising{'sub': '2', '(c) at least partial conversion of the input stream containing hydrocarbons in the synthesis gas production plant under synthesis gas production conditions to afford a raw synthesis gas stream containing hydrogen (H) and carbon monoxide (CO);'}(d) discharging a raw synthesis gas stream from the synthesis gas production plant;(e) introducing at least a first proportion of the raw synthesis gas stream into a CO conversion plant comprising at least one CO conversion stage, converting the proportion of the raw synthesis gas stream introduced into the CO conversion plant under ...

Integration of hydrogen liquefaction with gas processing units

A method of liquefying hydrogen, including dividing a hydrogen stream into at least a first fraction and a second fraction, introducing the first fraction into a refrigeration cycle of a hydrogen liquefaction unit, thereby liquefying a product hydrogen stream, withdrawing one or more warm hydrogen stream(s) from the hydrogen liquefaction unit, and returning the one or more warm hydrogen stream to the hydrogen stream, wherein the second fraction is combined with a high-pressure nitrogen stream to form an ammonia synthesis gas stream.

PROCESS FOR PRODUCTION OF AMMONIA AND DERIVATIVES, IN PARTICULAR UREA

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

METHOD FOR THE MANUFACTURE OF UREA

A method for producing urea. A methane-containing feed gas stream is reacted with oxygen by partial oxidation to form a synthesis gas stream containing hydrogen and carbon monoxide. The carbon monoxide is reacted with water in a water gas-shift reaction to form carbon dioxide and hydrogen. The synthesis gas stream is separated into a first synthesis gas substream a second synthesis gas substream. The first synthesis gas substream is subjected to pressure-swing adsorption to separate hydrogen and the second synthesis gas substream is subjected to temperature-swing adsorption to separate carbon dioxide. The separated is reacted with nitrogen to form ammonia and the ammonia is reacted with the carbon dioxide to form urea. 1. A method for producing urea , comprising the steps:reacting a methane-containing feed gas stream with oxygen by partial oxidation to form a synthesis gas stream comprising hydrogen and carbon monoxide,reacting the carbon monoxide of the synthesis gas stream in a water gas-shift reaction with water to form carbon dioxide and hydrogen,dividing the synthesis gas stream into a first synthesis gas substream and a second synthesis gas substream,subjecting the first synthesis gas substream to a pressure-swing adsorption to separate hydrogen from the first synthesis gas substream,subjecting the second synthesis gas substream to a temperature-swing adsorption to separate carbon dioxide from the second synthesis gas substream,reacting the hydrogen separated from the first synthesis gas substream with nitrogen to form ammonia, andreacting the ammonia with the carbon dioxide separated from the second synthesis gas substream to form urea.2. The method according to claim 1 , wherein the carbon dioxide separated from the second synthesis gas substream is provided at a pressure of at least 10 bar.3. The method according to claim 2 , wherein the carbon dioxide is provided at a pressure of at least 20 bar.4. The method according to claim 3 , wherein the carbon ...

METHOD FOR CONVERTING NATURAL GAS TO DIMETHYL ETHER

Systems and methods for upgrading natural gas that may include the division of a natural gas feed steam into two parts—one that is partially oxidized into syngas and a second that is “dry” reformed into syngas with the assistance of heat from the partial oxidation. Each of the resulting syngas products may then be combined, and after water is condensed from the syngas, the combined syngas product may be converted to dimethyl ether. 1. A method of upgrading natural gas comprising:partially oxidizing a first natural gas feed stream to make a first syngas product;heating a second natural gas feed stream with the first syngas product;reforming the second natural gas feed stream and carbon dioxide to make a second syngas product;combining the first syngas product and second syngas product into a combined syngas product; andconverting the combined syngas product to a converted product stream comprising dimethyl ether.2. The method of claim 1 , further comprising condensing water from the combined syngas product.3. The method of claim 2 , wherein the combined syngas product comprises less than 1 mole % water after the step of condensing water from the combined syngas product.4. The method of claim 1 , wherein at least 50% of carbon in the first and second natural gas feed streams is converted to dimethyl ether.5. The method of claim 1 , wherein at least 70% of carbon in the first and second natural gas feed streams is converted to dimethyl ether.6. The method of claim 1 , wherein the step of converting the combined syngas product to dimethyl ether comprises contacting the combined syngas product with a catalyst system comprising a first catalyst for converting syngas to methanol an a second catalyst for dehydrating methanol to dimethyl ether.7. The method of claim 6 , wherein the first catalyst and the second catalyst are present in a common catalyst particle.8. The method of claim 1 , wherein the converted product stream further comprises carbon dioxide.9. The method of ...

PROCESS FOR PRODUCTION OF AMMONIA AND DERIVATIVES, IN PARTICULAR UREA

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

POLYGENERATION PRODUCTION OF HYDROGEN FOR USE IN VARIOUS INDUSTRIAL PROCESSES

Provided are processes for production of hydrogen to be used in various industrial processes, including in processes for production of ammonia and urea. Included are polygeneration processes that result in ultra-low emissions. 1. A method for the production of hydrogen from synthesis gases of an oxygen supplied partial oxidation process , the method comprising the steps of:supplying a hydrocarbon or carbonaceous feedstock and oxygen to an oxygen supplied partial oxidation process to produce a synthesis gas, the synthesis gas comprising carbon dioxide, carbon monoxide, and hydrogen;supplying the synthesis gas to a first reactor, the first reactor comprising a catalyst and being configured to convert at least a portion of the carbon monoxide to carbon dioxide and produce a modified synthesis gas;supplying the modified synthesis gas to a second reactor, the second reactor comprising a catalyst and being configured to convert remaining carbon monoxide to carbon dioxide to produce a carbon dioxide-rich synthesis gas;supplying the carbon dioxide-rich synthesis gas from the second reactor to a first condenser to remove water and produce a gas stream comprising hydrogen and carbon dioxide;supplying the hydrogen and carbon dioxide stream to a pressure swing adsorption process to produce a pure hydrogen stream and pressure swing adsorption tail gas; andextracting exothermic heat for the production of power, heating and cooling of the process, or export of steam.2. The method of claim 1 , further comprising the step of:supplying the pure hydrogen stream and nitrogen gas from an air separation unit to a fourth reactor, the fourth reactor comprising a catalyst and being configured to produce an ammonia product stream.3. The method of claim 1 , further comprising the step of:supplying the pure hydrogen stream to a Fischer Tropsch gas to liquids process.4. The method of claim 1 , further comprising the step of:supplying the synthesis gas or modified synthesis gas to a soot removal ...

SYSTEM AND METHOD FOR GASIFICATION

A system includes a gasifier configured to gasify a feed to generate syngas. The gasifier comprises a first axis. The system also includes a first gasification reaction zone disposed in the gasifier. The first gasification reaction zone is defined at least partially by a first wall substantially perpendicular to the first axis. The system also includes a first feed injector coupled to the gasifier. The first feed injector is configured to inject the feed into the first gasification reaction zone beneath the first wall in a first direction relative to the first axis. 1. A system , comprising:a gasifier configured to gasify a feed to generate syngas, wherein the gasifier comprises a first axis;a first gasification reaction zone disposed in the gasifier, wherein the first gasification reaction zone is defined at least partially by a first wall substantially perpendicular to the first axis; anda first feed injector coupled to the gasifier, wherein the first feed injector is configured to inject the feed into the first gasification reaction zone beneath the first wall in a first direction relative to the first axis.2. The system of claim 1 , wherein the first wall is concave and is configured to direct the syngas in the first direction.3. The system of claim 1 , comprising a reaction zone outlet disposed in a second wall disposed opposite from the first wall claim 1 , wherein the reaction zone outlet is configured to direct the syngas in the first direction substantially parallel to the first axis.4. The system of claim 1 , wherein the gasifier comprises a gasifier outlet configured to convey the syngas from the gasifier in a second direction substantially opposite from the first direction substantially parallel to the first axis.5. The system of claim 1 , comprising a second feed injector coupled to the gasifier claim 1 , wherein the second feed injector is disposed substantially opposite from the first feed injector.6. The system of claim 1 , wherein the first wall ...

CATALYST, METHOD FOR PRODUCING CATALYST, AND METHOD FOR PRODUCING HYDROGEN-CONTAINING GAS USING CATALYST, AND HYDROGEN GENERATING DEVICE, FUEL CELL SYSTEM, AND SILICON-SUPPORTED CEZR-BASED OXIDE

The present invention provides a catalyst in which a reaction initiation temperature at which self-heating function is exhibited is low and which is capable of suppressing carbon accumulation even when a reaction is repeated. The catalyst of the present invention includes a CeZr-based oxide, silicon, and a catalytically active metal, wherein the CeZr-based oxide satisfies CeZrO(x+y=1) and the silicon satisfies molar ratios of 0.02≦Si/Zr and 0.01 Подробнее

METHOD FOR SYNGAS CLEAN-UP OF SEMI-VOLATILE ORGANIC COMPOUNDS WITH METAL REMOVAL

A system and method for processing unconditioned syngas first removes solids and semi-volatile organic compounds (SVOC), then removes volatile organic compounds (VOC), and then removes at least one sulfur containing compound from the syngas. Additional processing may be performed depending on such factors as the source of syngas being processed, the products, byproducts and intermediate products desired to be formed, captured or recycled and environmental considerations. 1. A method for cleaning unconditioned syngas for introduction into a syngas processing technology application , the unconditioned syngas including semi-volatile organic compounds (SVOC) , at least one or both of hydrogen chloride and hydrogen sulfide , and having a metal concentration greater than 0 ppm to less than or equal to 30 ppm; the method comprising:(a) contacting the unconditioned syngas with water to reduce the temperature of the syngas to below the SVOC condensation temperature to thereby form an intermediate SVOC-depleted syngas containing steam, and a first mixture comprising SVOC, solids and water;(b) removing steam from the intermediate SVOC-depleted syngas containing steam to form (i) a first depleted syngas stream which has a reduced amount of SVOC and solids relative to the unconditioned gas, and (ii) a second mixture comprising SVOC, solids and water;(c) after step (b), removing hydrogen chloride and/or hydrogen sulfide from the first depleted syngas stream with a scrubber;(d) after step (c), compressing the syngas to a pressure ranging from 100 PSIG to 2,000 PSIG;(e) after step (d), removing at least one metal from the syngas, said metal being one or more from the group consisting of mercury, arsenic, lead, and cadmium;(f) after step (e), removing at least one sulfur containing compound from the syngas; and 'wherein:', '(g) after step (f), removing carbon dioxide from the syngas with one or more from the group consisting of a membrane, an adsorber and an absorber;'}(i) the metal ...

REACTOR SYSTEM WITH UNEQUAL REACTOR ASSEMBLY OPERATING PRESSURES

A reactor system comprising a first reactor assembly, a first pressure transition assembly, a second reactor assembly and a second pressure transition assembly. 1. A reactor system , comprising:{'b': 1', '1', '1', '1', '1, 'a first reactor assembly, which comprises one or more first reactor assembly reactors, each configured to operate at a pressure P, wherein the first reactor assembly is configured to receive first solid particles at the pressure P, convert the first solid particles at the pressure P to second solid particles at the pressure P, and discharge the second solid particles at the pressure P;'}{'b': 1', '1', '2', '1', '2, 'a first pressure transition assembly in fluid communication with the first reactor assembly and a second reactor assembly, wherein the first pressure transition assembly is configured to receive the second solid particles at the pressure P, transition the pressure surrounding the second solid particles from the pressure P to a pressure P that is different from the pressure P, and discharge the second solid particles at the pressure P;'}{'b': 2', '2', '2', '2', '2, 'the second reactor assembly, which comprises one or more second reactor assembly reactors, each configured to operate at the pressure P, wherein the second reactor assembly is configured to receive the second solid particles at the pressure P, convert the second solid particles at the pressure P to third solid particles at the pressure P, and discharge the third solid particles at the pressure P;'}{'b': 2', '2', '3', '2', '3, 'a second pressure transition assembly in fluid communication with the second reactor assembly and the first reactor assembly, the second pressure transition assembly configured to receive third solid particles at the pressure P, transition the pressure surrounding the third solid particles from the pressure P to a pressure P that is different from the pressure P, and discharge the third solid particles at the pressure P from the second pressure ...