ВЫСОКОПРОИЗВОДИТЕЛЬНЫЙ КАМЕРНЫЙ СМЕСИТЕЛЬ ДЛЯ КАТАЛИТИЧЕСКИХ СУСПЕНЗИЙ МАСЛА КАК РЕАКТОР ДЛЯ ДЕПОЛИМЕРИЗАЦИИ И ПОЛИМЕРИЗАЦИИ УГЛЕВОДОРОДСОДЕРЖАЩИХ ОТХОДОВ В СРЕДНИЙ ДИСТИЛЛЯТ В КОНТУРЕ ЦИРКУЛЯЦИИ

Изобретение относится к устройству и способу получения дизельного топлива из углеводородсодержащих отходов, при этом подаваемые вещества - сухие отходы, остаточное масло, нейтрализующее вещество и катализатор - связаны с системой (103) подачи через воронку-смеситель (109) и сборник (104), который граничит с питающей емкостью (102), причем питающая емкость (102) через каналы (110) контура циркуляции масла соединена со сборником (115), высокопроизводительный камерный волновой смеситель (101) на стороне всасывания имеет соединяющий его с питающей емкостью (102) трубопровод, а на напорной стороне соединен с желобом (113) испарителя (114), соединенного с дистилляционной колонной (118), в которой установлен конденсатор (119), который через трубопроводы (124) и (126) соединен с приемником (125) продукта - дизельного топлива, причем ниже испарителя (114) расположен сборник (115), который через регулировочный клапан (130) соединен с нагревательной камерой (132), имеющей на выходной стороне шнековый ...

СИСТЕМА ПРИГОТОВЛЕНИЯ СИНТЕТИЧЕСКОЙ ПОЛИЭФИРНОЙ СМОЛЫ ИЗ БУРОГО УГЛЯ

Система приготовления синтетической полиэфирной смолы из бурого угля, отличающаяся тем, что применяется малоотходная химическая технология, в которой в качестве химического реактора для получения высокомолекулярных гуминовых и фульвокислот из бурого угля используется горизонтальная виброцентробежная мельница ЦЭМ-7, снабженная центробежным насосом, установленным на подающей линии мельницы для многократного прокачивания буроугольной суспензии через мельницу, а в качестве химического реактора для синтеза полиэфирной смолы из буроугольной карбоксилсодержащей смолы, получаемой из смеси буроугольных гуминовых кислот, используется специальный вертикальный реактор с водяной рубашкой в верхней части реактора, внутри которого установлены два стакана, из которых нижний обогреваемый стакан служит для проведения реакции поликонденсации между карбоксилсодержащей буроугольной смолой и тетраэтиленгликолем, а верхний охлаждаемый стакан, содержащий активный сорбент аэросил, служит для поглощения паров воды ...

СИСТЕМА ПРИГОТОВЛЕНИЯ СИНТЕТИЧЕСКОГО СЫРОГО ГОРНОГО ВОСКА ИЗ БУРОГО УГЛЯ

Система приготовления синтетического сырого горного воска из бурого угля, отличающаяся тем, что применяется малоотходная химическая технология, в которой в качестве химического реактора для получения высокомолекулярных гуминовых и фульвокислот из бурого угля используется горизонтальная виброцентробежная мельница ЦЭМ-7, снабженная центробежным насосом, установленным на подающей линии мельницы для многократного прокачивания буроугольной суспензии через мельницу, а в качестве химического реактора для синтеза сырого горного воска из буроугольных гуминовых кислот используется специальный вертикальный реактор с водяной рубашкой в верхней части реактора, внутри которого установлены два стакана, из которых нижний, обогреваемый стакан служит для проведения реакции конденсации между буроугольными гуминовыми кислотами и цетиловым спиртом, а верхний, охлаждаемый стакан, содержащий активный сорбент аэросил служит для поглощения паров воды, выделяющихся в процессе реакции конденсации.

СПОСОБ ПОЛУЧЕНИЯ ТОПЛИВНЫХ ДИСТИЛЛЯТОВ

Изобретение относится к производству нефтяных топлив и может быть использовано в нефтеперерабатывающей промышленности. Способ получения топливных дистиллятов, являющихся сырьем для производства моторных топлив и топлив для реактивных двигателей, заключается в том, что остаточное нефтяное сырье (мазут, гудрон) смешивают с сапропелитом и фракцией гидрированных продуктов термокрекинга, или гидрокрекинга с т.кип. 300-400oС в количестве 1-5% от массы остаточного нефтяного сырья, затем смесь подвергают по крайней мере двукратной гомогенизации в диспергаторе при 85-105o С после чего проводят термо- или гидрокрекинг. Из продуктов термо- или гидрокрекинга выделяют топливные дистилляты (бензин, дизтопливо, газойль). Техническим результатом изобретения является исключение применения тетралина или его алкилпроизводных при реализации способа при сохранении и повышении выхода топливных дистиллятов. 2 з.п.ф-лы, 3 табл.

УСТРОЙСТВО ДЛЯ ПЕРЕРАБОТКИ ОРГАНОСОДЕРЖАЩЕГО СЫРЬЯ МЕТОДОМ ПИРОЛИЗА

Устройство для переработки органосодержащего сырья методом пиролиза, включающее в себя пиролизный реактор с транспортирующим устройством сырья и устройствами отвода образующихся парогазовых фракций и твердых компонентов, отличающееся тем, что транспортирующее устройство сырья установлено с внешней стороны реактора и выполнено в виде винтового конвейера, содержащего вал с закрепленной на нем плоской спиралью, при этом часть корпуса конвейера выполнена с перфорацией для подачи к органосодержащему сырью газового теплоносителя, поступающего из устройства отвода парогазовых фракций.

ОДНОРЕАКТОРНЫЙ СПОСОБ СЖИЖЕНИЯ БИОМАССЫ

Изобретение относится к способу преобразования биомассы сжижением. Однореакторный способ сжижения биомассы включает следующие стадии: готовят суспензию, содержащую катализатор, вулканизирующий агент и биомассу, вводят в суспензию водород для проведения реакции, при этом реакцию контролируют, таким образом, чтобы она протекала под давлением 13-25 МПа и при температуре 300-500°С, в результате чего получают бионефть, при этом указанное введение водорода в суспензию включает 2 этапа: впрыскивают водород под высоким давлением в суспензию в первый раз до объемного соотношения водорода к суспензии (50-200):1; нагревают суспензию до 200-350°С и впрыскивают водород под высоким давлением в суспензию во второй раз до объемного соотношения водорода к суспензии (600-1500):1 с получением, таким образом, реакционной смеси сырья и нагревают реакционную смесь сырья до 320-450°С, подают смесь нагретого реакционного сырья в реактор с трехфазным псевдоожиженным слоем для проведения реакций гидролиза, крекинга ...

СПОСОБ ПЕРЕРАБОТКИ ПРОДУКТОВ ГИДРОГЕНИЗАЦИИ УГЛЯ

Данное изобретение относится к способу переработки продуктов гидрогенизации угля и может быть использовано в нефтеперерабатывающей и коксохимической промышленности. Способ переработки жидких продуктов гидрогенизации угля, выкипающих выше 300°С, с содержанием твердой фазы до 15 мас.%, 9-20 мас.% асфальтенов и имеющих структурную вязкость при 80°С 0,01-0,75 Па·с, включает их разделение на жидкий продукт и первый остаток фильтрованием или центрифугированием, или гидроциклонированием, или вакуумной перегонкой. Остаток, выкипающий выше 300°С, содержащий 15-30 мас.% твердой фазы, 11-25 мас.% асфальтенов и имеющий структурную вязкость при 80°С 0,15-0,9 Па·с, подвергают последующему разделению на жидкие продукты и второй остаток, выкипающий выше 300°С, содержащий 30-50 мас.% твердой фазы и имеющие структурную вязкость при 80°С 0,5-1,5 Па·с, вакуумной перегонкой или экстракцией. Полученный остаток после вакуумной перегонки затем дополнительно подвергают экстракции с выделением твердого остатка и ...

СПОСОБ ИЗГОТОВЛЕНИЯ ЖИДКОГО ТОПЛИВА ИЗ ТВЕРДЫХ ГОРЮЧИХ ИСКОПАЕМЫХ И МЕХАНОТЕРМОХИМИЧЕСКИЙ РЕАКТОР ДЛЯ ЕГО ОСУЩЕСТВЛЕНИЯ

... 1. Способ изготовления жидкофазного топлива из твердых горючих ископаемых, включающий деструкцию высокомолекулярных соединений, находящихся в расплаве в дисковой насадке, путем механического и термического воздействия на высокомолекулярное соединение, осуществляют предварительную деструкцию в червячном эктрудоре, отличающийся тем, что измельченный материал, поступающий в приемное устройство шнека под давлением без доступа воздуха на подпружиненный выталкиватель, который амортизирует гидромеханические удары и обеспечивает при вращении шнека беспрерывность подачи материала сплошным потоком в полость цилиндра, в котором осуществляют предварительную деструкцию материала, причем предварительная деструкция осуществляется при вступлении во фрикционное взаимодействие с боковой поверхностью активаторов и поверхностью цилиндра, возникает термическая деструкция вещества при влажности до 40% от его органической массы и допустимой температуре до 260°С, при этом выделенная первичная газопаровая фракция ...

УДАЛЕНИЕ СЕРОВОДОРОДА В ВИДЕ СУЛЬФАТА АММОНИЯ ИЗ ПАРОВ ПРОДУКТА ГИДРОПИРОЛИЗА

СПОСОБЫ ПРОИЗВОДСТВА БИОТОПЛИВА

... 1. Способ производства биотоплива, причем способ включает:обработку органического вещества водным растворителем и по меньшей мере одним дополнительным катализатором, который выбран из группы, состоящей из: катализатора на основе формиата щелочного металла; катализатора на основе карбоната щелочного металла; катализатора на основе переходного металла; катализатора на основе соли переходного металла; катализатора на основе формиата переходного металла; катализатора на основе соли щелочного металла; катализатора на основе соли щелочноземельного металла; кислотного катализатора; твердокислотного катализатора; катализатора конверсии водяного пара; катализатора на основе цеолита или алюмосиликата; катализатора на основе переходного металла на подложке; сульфидного катализатора; и основного катализатора, который представляет собой соль щелочного металла или соль переходного металла; при температуре между примерно 250°С и примерно 400°С и под давлением между примерно 100 бар и примерно 300 бар, ...

Способ управления процессом гидрирования непредельных углеводородов пироконденсата

Изобретение относится к способам управления процессом гидрирования непредельных углеводородов пироконденсата и позволяет снизить содержание диенов на выходе реактора. В способе дополнительно определяют время пробега катализатора, измеряют концентрации диенов и олефинов в сырье и по соотношению концентраций диенов и олефинов в сырье и времени пробега катализатора корректируют изменение расходов водородсодержащего газа, рецикла и температуры сырья на входе реактора. 1 ил.

Способ термического разложения твердого топлива

Устройство для разделения шлама ожижения угля

Способ получения бензина

Горячий сепаратор к устройству для гидрирования под давлением

Изобретение относится к горячему сепаратору, а именно к устройству для гидрирования под давлением и позволяет повысить степень предотвращения отложения твердых веществ. Горячий сепаратор содержит корпус 1 с впуском 2 разделяемой смеси продуктов гидрирования, выпуском 3 головного продукта и выпуском 4 кубового продукта. Корпус 1 имеет цилиндрическую 5 и коническую 6 части, выполненные в виде спиралеобразных полых профилей квадратного сечения с цилиндрическим отверстием и соединенные между собой посредством листового элемента 8. Цилиндрическая часть 5 снабжена впуском 11 и выпуском 12 охлаждающего агента, а коническая часть 6 снабжена впуском 13 и выпуском 14 охлаждающего агента. 3 з.п. ф-лы. 2 ил.

Способ превращения угля в жидкие продукты

СПОСОБ ПРЕВРАВЩНИЯ УГЛЯ В ЖИДКИЕ ПРОДУКТЫ путем приготовления пасты угля с растворителем, состоящим из смеси фракции с пределом кипения 35-200 С и рециркулирующего остатка после фракционирования с температурой застывания 20С и имеющего начало кипения и конец кипения , г-идрогенизации пасты в присутствии водорода и катализатора при 350-500°С, давлении 80300 атм и последующего фракциониро . вания полученных жидких продуктов, отличающийся тем, что, с целью повышения качества фракций, являющихся моторными топливами, исходный уголь делят на два потока в соотношении 3:1-1t3, первый поток смешивают с указанным растворителем в соотношении 1:1,5-1:4, второй поток угля смешивают с растворителем имеющм интервал кипения 200-ДОО С и полученным при гидрогенизации угля , в том же соотношении с последующей раздельной гидрогенизацией обоих потоков угля в течение 10120 мин и затем или раздельным сбеззоливанием и фракционированием продуктов гидрогенизации с подачей фракции 35-200°С первого потока в качестве ...

Способ производства обеззоленного твердого и жидкого топлива из угля

TORFEXTRAKTIONSAPPARAT

Verfahren zum Entschwefeln und Hydrieren von schweren Mineraloelen, ihren Destillaten, Kohlendestillaten oder Kohlenaufschwemmungen

UMWANDLUNGSVERFAHREN FUER FESTE,KOHLENWASSERSTOFFHALTIGE MATERIALIEN

IMPROVED COAL LIQUEFACTION PROCESS

KOHLEVERFLUESSIGUNGS-VERGASUNGS-SCHWERBENZINREFORMING-VERFAHREN

Schmieroelersatz

ANSPRINGREAKTOR FUER KOHLEHYDRIERUNG

VERFAHREN ZUR HYDRIERUNG VON KOHLE UND KOHLE-LOESUNGSMITTELN

Verfahren zur Druckhydrierung von Kohleaufschlaemmungen, Teeren, Mineraloelen oder deren Fraktionen

Verfahren zur Druckhydrierung von Kohlen, Teeren oder Mineraloelen

Verfahren zur Gewinnung von vaselinartigen Produkten

VERFAHREN ZUR ERZEUGUNG EINER SUSPENSION AUS BRAUNKOHLE UND OEL FUER DIE HYDRIERUNG

VERFAHREN ZUR HERSTELLUNG VON KOHLENWASSERSTOFFOELEN DURCH SPALTENDE KOHLEHYDRIERUNG

Verfahren zur Veredelung von Kohlen, Teeren, Mineraloelen u. dgl. durch Druckhydrierung

Verfahren zur Behandlung kohlenstoffhaltiger Materialien unter Druck

Verfahren zur spaltenden Druckhydrierung

IRON CATALYZED COAL LIQUEFACTION PROCESS

Process and apparatus for the production of hydrocarbons from coal and water

... 283,177. Uhlmann, A. Jan. 6, 1927, [Convention date]. Mineral oils, extracting.-Hydrocarbons are obtained by passing a pulp composed of fine coal and water through a high frequency field. The coal dust is supplied from a funnel a to a cylinder b and is mixed by a worm e with water from a pipe c, the mixture being forced by the worm through a tube d surrounded by a high frequency field produced by a coil f. The products are continuously discharged into a receiver g and the hydrocarbons separated in the usual manner by fractional distillation. The apparatus may be kept cool by mixing ice with the water or by surrounding it with a refrigerant. The Specification as open to inspection under Sect. 91 (3) (a) states that hydrogen may be passed through with the pulp. This subjectmatter does not appear in the Specification as accepted.

Improvements in, or relating to, the destructive hydrogenation of coal, tar, mineral oils, and the like

... 254,713. I. G. Farbenindustrie Akt.- Ges. July 2, 1925, [Convention date]. Hydrogenation, destructive.-In the production of liquid hydrocarbons by treating carbonaceous bodies such as coal, tar, mineral oils, and lignite with hydrogen, the gas used is obtained by the partial decomposition, by oxygen or gases richer in oxygen than air, of gases or vapours containing hydrocarbons so as to. produce hydrogen and carbon monoxide, and simultaneously or subsequently converting, partially or completely, the carbon monoxide into carbon dioxide bv means cf water vapour, with production of more hydrogen. Carbon dioxide, water vapour, or both, with or without catalysts such as nickel precipitated on magnesia, iron alloys, or molten fron or iron alloys mav be present. The hydrocarbon vapours so treated are preferably the gases obtained in the destructive hydrogenation of carbonaceous materials, may be after separation of ethane, propane or other valuable compounds e.g. by cooling or by porous adsorbents ...

Improvements in the manufacture and production of valuable hydrocarbons from varieties of coal, tars, mineral oils and the like

... Heat is supplied during a destructive hydrogenation process by adding to the reaction mixture, the treatment of which has already started, oxygen-containing compounds of carbon which under the working conditions are reduced to hydrocarbons with the evolution of heat. Suitable compounds are oxides of carbon or phenols. The initial materials are preferably preheated to 350-380 DEG C. and the oxygen-containing compounds of carbon are then added at one or more points in the reaction system. Strongly hydrogenating catalysts such as molybdenum and tungsten may be used. A petroleum fraction boiling at 200-350 DEG C. is forced by a pump H through a heat exchanger K. Hydrogen is added through a pipe J. The mixture passing out at M is heated in a coil O to 460 DEG C. and passed in a vaporous state into a reaction vessel A containing a catalyst C of zinc and molybdenum. From this vessel, the mixture passes on to enter a second vessel A<1> at B<1>; to prevent a fall in temperature ...

Improvements in and apparatus for the continuous treatment of solid substances underpressure

... Apparatus for effecting chemical reactions at high temperature and pressure in liquids, vapours or gases or mixtures of these with solids comprises a sheaf of parallel pressure-bearing tubes rotating about an axis parallel to the axes of the tubes and either internally or externally heated. The reagents pass through the tubes in parallel or in series, or several sheaves may be arranged in series. The reagents may travel in the same direction or in counter-current, or reagents may be introduced or reaction products withdrawn, at intermediate points. The movement of solid or viscous materials may be effected by worm conveyers or spiral bands within the tubes; agglomeration may be prevented by rods with sharp edges, chains, or loose solid bodies. Catalysts may be mixed with the reaction substances or inserted in the tubes in the form of loose or rigid bodies or deposited on the walls of the tubes or the latter may be composed of catalytic material. Gases may be introduced ...

Improvements relating to the catalytic destructive hydrogenation of carbonaceous materials

In destructively hydrogenating carbonaceous materials in the presence of catalysts of molybdenum, tungsten, iron, cobalt, or nickel or their compounds, using excess of hydrogen and re-cycling the unused hydrogen, the amount of hydrogen sulphide in the re-cycled gas is kept within such limits as will produce a substantial increase in activity of the catalyst. The catalysts are preferably employed initially in the form of oxides, which are converted into sulphides during the early stages of the reaction. The pressure on the liquid reaction products may be reduced in stages to allow a gas rich in hydrogen and poor in hydrogen sulphide to come off first, on further reducing the pressure to atmospheric, a gas rich in hydrocarbons and hydrogen sulphide is obtained, which may be used for enriching the re-cycled hydrogen. To avoid corrosion of pumps or other conveying devices, it is preferable to remove the hydrogen sulphide, even when in the correct amount, from the circulating gases before they ...

Process for the production of valuable products from coal varieties, tars, mineral oils and the like

In the production of oils of low boiling-point by the heat treatment of carbonaceous materials preferably in presence of hydrogen, e.g. by destructive hydrogenation or low-temperature carbonization, the treatment is carried out with the addition of solid carbonaceous material, which may be the initial material itself, into which halogen as such or as halogen halide has been incorporated by treatment of the added material with free halogen or anhydrous halogen halide, or when solid carbonaceous materials are used by pretreating these prior to the heat treatment with anhydrous halogen halide or with free halogen dissolved in an organic solvent, e.g. carbon tetrachloride. When treating brown coal it may be pretreated with halogen alone without solvent. Brown coal, which may be deashed by mechanical means or by acids, is treated at 20--50 DEG C. for 1--18 hours with bromine, iodine, or chlorine. Adsorbent materials, e.g. coke, charcoal, silica may be treated in a similar manner and then added ...

Improvements in the treatment of carbonaceous materials with hydrogenating gases

... In processes for the hydrogenation of carbonaceous materials, in which part at least of the initial materials is preheated by the reaction products, such preheating is effected in a heat exchanger so that the difference in temperature between the material to be preheated and the stream of material giving up its heat does not exceed 100 DEG C. 80 per cent of a middle oil to be subjected to destructive hydrogenation is mixed with hydrogen and heated to 200 DEG C. and then to 450 DEG C. in heat-exchangers A, B and is then mixed with the remaining 20 per cent which has been passed through a preheating coil G and the mixture is passed through a heating coil C to a reaction chamber D. 5 per cent of the liquid products of the reaction are continuously withdrawn from a separator E while the gases and vapours produced are passed through the heat exchangers A, B. The temperature of the coil G may be regulated independently by the provision of a separate burner. In a modification ...

Process for the regulation of the temperature in the treatment of carbonaceous initial materials with hydrogenating gases

In destructive hydrogenation and like hydrogenation treatments of carbonaceous materials the temperature of the reaction is controlled by introducing ammonia into the reaction system at one or more points where temperature rises are observed. The ammonia may be introduced along with the hydrogen in amounts up to 30 per cent thereof either at a point before the reaction vessel or at one or more points in the reaction vessel. Hydrogen gases, or oils, may be introduced with the ammonia. In the destructive hydrogenation of middle oil by treatment under a pressure of 200 atmospheres in the presence of tungsten disulphide the reaction temperature is maintained at 420 DEG C., by the introduction of ammonia in amount equivalent to 5 per cent by volume of the hydrogenating gases.

A process for producing hydrocarbons

Hydrogen, a carbon-containing material and crushed flux are injected into a carburized metal bath with induction coil heating elements in order to produce a required hydrocarbon compound, for example methane or acetylene. The bath is contained within a pressurized crucible-type furnace and impurities from the raw materials and by-product of the reaction are drawn off as slag or in the gaseous effluent. The carbon-containing raw material which may be any suitably prepared, dried and milled material such as solid fossil fuel or industrial waste, is far greater than in previous industrial hydrocarbon-producing processes.

Coal liquefaction

In a two-stage liquefaction, hydrogenated 850 DEG F.+ residuum from the second stage is used in formulating the first stage liquefaction solvent.

Hydrotreating of carbonaceous materials

Coal, peat or wood is converted to liquid and gaseous hydrocarbons by reaction with an alkali metal sulfide, polysulfide and/or hydrosulfide, in the presence of water, steam and/or hydrogen sulfide at 50-450 DEG C.

SEALING A ROTATABLE ELEMENT IN A CYLINDER

HYDROCRACKING OF HEAVY HYDROCARBON USING SYNTHESIS GAS

COAL HYDRATION METHOD

HYDROPYROLYSIS OF CARBONACEOUS SOLIDS

Hydrogenating and distilling hydrocarbons from bituminous substances

... 171,785. O'Dell, A. E., (Canadian-American Finance & Trading Co., Ltd.). Aug. 23, 1920. Mineral and tar oils, extracting, &c.-Bituminous materials such as bituminous sands, asphalt, pitch, &c. are distilled in presence of hydrogen to avoid decomposition and effect hydrogenation. Hydrogen, obtained for example by dissociation of natural gas is passed from a dissociator 1 by a pipe 4 to the jacket 6 of a melter 7 to which bituminous sand is fed bv a valve 8. The melted material is passed to a mixing-vessel 14 into which hydrogen is passed by a perforated pipe 15, and then by a pump 19 into a still 20. The vapours pass to a. pipe 28, compressor 30, and condenser 34 from which the uncondensed gases are returned to the dissociator 1 by a pipe 37. Hydrogen may be passed by a pipe 26 directly into the still and by a pipe 31 into the vapours passing away 'from the still.

LIQUEFACTION OF COAL

Improved manufacture of liquid organic compounds from coal

In obtaining liquid products from coal by hydrogenation under pressure and at a high pressure, as described in Specifications 18232/14 and 5021/15, coal is used which contains not more than 85 per cent of carbon referred to dry substance free from ash. In an example, 5 kilos of coal having a carbon content of 74.48 per cent on the above basis were mixed with 10 kilos tar oil and heated to 400 DEG C. for six hours under a pressure of 100 atmos. of hydrogen. Eighty-seven per cent of the coal was converted into liquid products, as against 11 per cent of a coal with a carbon content of 92.1 per cent similarly treated.

ENHANCED RECOVERY OF COAL OIL IN COAL HYDROGENATION

Hydrogenative coal liquefaction

Non-liquefied solid components of the product of a liquefaction reactor 5 are concentrated in a hot separator 6 under approximately the same pressure and temperature conditions as in the reactor 5. Gaseous and vapour components are condensed in subsequent stages 9, 10, while the pumpable residue is withdrawn from the separator 6 and expanded. Hydrogen-containing recirculation gas from a gas cleaner 12 is fed through the hot separator 6 (directly at 17 and indirectly through the reactor 5) in contact with the outlet product of the reactor in a quantity of more than 5000 Nm<3> per tonne of (dry ash-free) coal. The oil for forming a coal slurry may be obtained in an intermediate separator 31 following the hot separator. ...

Generation for recycle solvents in coal liquefaction

A method is described to improve a coal liquefaction process by the use of a recycle solvent comprised of two fractions: the first, a lower boiling fraction, is obtained by an atmospheric distillation and is subsequently hydrotreated to enrich its hydrogen donor capacity; the second is a higher boiling fraction that is enriched in desirable hydrogen transfer agents by a solvent extraction process. The combined recycle solvent thus obtained is more efficient in transferring gas phase H2 to the coal and enables other significant process improvements.

Refining and cracking carbonaceous materials

A process for hydrotreating carbonaceous materials is disclosed in which the carbonaceous material is contacted with steam and with empirical hydrates of alkali metal hydrosulfides, monosulfides, or polysulfides to hydrocrack, hydrogenate, denitrogenate, demetallize and/or desulfurize the carbonaceous material, hydrogen sulfide optionally being co-fed to the reaction zone.

Process for the hydrogenation of organic substances, especially of the products of the distillation of coals and petroleum oils

... 286,206. Hugel, G., Paul, M., and Boistel, M. Feb. 28, 1927, [Convention date]. Hydrogenation, destructive.- The hydrogenation of organic substances, particularly the products of distillation of coal and petroleum is effected by means of hydrides of alkali or alkaline earth metals which are coated with oil substances such as tetrahydronaphthalene or with more readily oxidizable substances such as the amides of the alkali and alkali earth metals. The process may be effected below 300‹ C. and 100 kilos pressure and is not affected by the presence of contact poisons such as nitrogen, sulphur, arsenic, and oxygen compounds. Sodium in finely-divided or fragmentary condition is introduced into an autoclave A having a stirrer a, and hydrogen is admitted under pressure through a branch pipe f by action of a compressor H which draws the gas from a holder G. The sodium hydride which is formed below 300‹ C., is stabilized as described above. The hydrogenation is effected in an autoclave B having stirrers ...

Improvements in the destructive hydrogenation of carbonaceous materials

... 308,995. Humphrey, H. A., and Imperial Chemical Industries, Ltd. Nov. 30,1927. hydrogenation, destructive.-The destructive hydrogenation of coal in suspension in oil is performed in a vertical tower such as that described in Specification 309,258. A heavy oil not readily decomposed during the reaction and which may be the product of a previous hydrogenation is used to fill the tower, the carbonaceous material being admitted at the top, and the hydrogen at the bottom of the tower, while residual material is removed at the base by, a pump. Suitable temperatures and pressure are 300-550‹ C. and 100 atmospheres. The solid carbonaceous material may also be admitted at the bottom of the tower. Specification 305,744 is also referred to.

Improvements in and relating to the manufacture of hydrocarbons and substances containing adsorbed hydrocarbons

... 278,745. General Carbonalpha Co., (Assignees of Aarts, H. C. J.). Oct. 7, 1926, [Convention date]. Liquid fuel.-Methane and other hydrocarbons are produced by heating active carbon with hydrogen or gases containing hydrogen at 150-600‹ C. with or without a catalyst, at ordinary or slightly above ordinary pressure. The hydrocarbons produced may be adsorbed in the active carbon so as to form a solid fuel suitable for use in internalcombustion engines and for other purposes. The carbon may be obtained by heating carbon monoxide to 230-600‹ C. with or without a catalyst. Activated bone charcoal, wood charcoal and other activated materials containing free carbon derived from vegetable, animal, or mineral sources may be used. It mav be advisable to add a catalyst such as nickel, which may be effected by drenching the carbon with finely divided nickel oxalate or nitrate and reducing with hydrogen at a suitable temperature. When the process is effected at 150-400‹ C. the products are mainly saturated ...

COAL LIQUEFACTION

Improvements in the manufacture and production of valuable hydrocarbons and in particular those of low boiling point range

... 320,473. Johnson, J. Y., (I. G. Farbenindustrie Akt.-Ges.). Aug. 31, 1928. Hydrogenation, destructive.-In a multi-stage process of destructive hydrogenation of carbonaceous materials, the residual material not appreciably affected by the first stage treatment is separated and treated under more vigorous conditions. The intensification of the treatment may be carried out by an increase of temperature or pressure, or by an increase in the partial pressure of the hydrogen, or by the employment of a more active catalyst. The materials may also, between successive stages, be subjected to physical or chemical treatment such as oxidation by an air current, condensation with aluminium chloride, extraction by solvents, or the action of an electric discharge. A topped American crude oil, containing 80 per cent of a non-distillable residue, is treated with hydrogen and a tungsten catalyst at 400‹ C. and 200 atmospheres pressure whereby 20 per cent is converted into light oils which are drawn off in ...

Improvements in the purification of hydrogen for destructive hydrogenation

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

Improvements in the treatment with hydrogenating gases of distillable carbonaceous material

In the treatment with hydrogenating gases of carbonaceous materials, more particularly by destructive hydrogenation, in which the reaction products contain corrosive halogen, corrosion is obviated by cooling the reaction products through the temperature range 350--200 DEG C., in a vessel constructed of resistant material, e.g. high chromium nickel steel, or lined with enamel glass or brick, or protected by a film of liquid, e.g. oil. Cooling is preferably effected in the presence of an amount of ammonia equivalent to the hydrogen halide present, e.g. ammonium chloride may be added to the initial materials or at a later stage. Cooling may be effected by a nonaqueous liquid, e.g. oil introduced as a shower or as a film over packing elements; or indirectly by flowing a film of cooling liquid over the outside walls of the vessel. In an example, a coal-oil paste of a bituminous coal containing chlorine is passed into a reaction vessel, together with hydrogen, under a pressure of 200 atmospheres ...

Improvements in and apparatus for introducing and withdrawing solid substances into and out of vessels containing a medium under high pressure

Solid substances are fed to or withdrawn from a vessel A, Fig 1, containing a medium under high pressure by means of a plurality of chambers B arranged in series and in which the pressure increases or decreases in successive chambers. The stage vessels or chambers B are separated from one another by valves C, C<1> respectively connected to operating means D, D<1> and are connected to each other by pressure equalizing valves E, E<1>. These valves are opened so that the pressure between two adjacent stage vessels is equalized and then the valve C or C<1> separating the chambers is opened for the solid material to pass from one chamber into the other on its way to the vessel A. If the vessel A is subjected to a pressure 5p then the pressure in the chambers B may be indicated by Op, 1p, 2p, &c. Each chamber B is connected by a pipe to a pressure regulating device F set to pressures 1p, 2p, &c. so that when the pressure in two adjacent chambers is equalized, the common pressure is higher than ...

Improved process and apparatus for destructive hydrogenation

... 326,586. Tate, W. R., Stephenson, H. P., and Imperial Chemical Industries, Ltd. Dec. 31, 1928. Hydrogenation, destructive. - Oils and liquid pastes of carbonaceous material are destructively hydrogenated in the form of a continuously falling annular film heated by a central heating element. A cylindrical high pressure converter 1 containing a central tubular heating element 2 is provided with an annular trough 3 from which the materials to be treated supplied bv a line 7 overflow and fall down the sides of the converter in a film 4. The materials are recirculated through a line 5 and pump 6. Hydrogen is passed through a line 9, an annular passage 11, a heat exchanger 12 where it exchanges heat with the products of the reaction passing off through a line 16, and a heater 13, and then passes down the inside of the Heater 2 and upwards in counter current to the film 4. The gas stripped of its condensible contents is returned to the line 9 make-up hydrogen being added through a line 10. In ...

A process for the treatment with hydrogenating gases of extraction products of solidcarbonaceous materials

Valuable hydrocarbons are obtained by extracting solid carbonaceous materials, e.g. bituminous and brown coal, peat, &c. with solvents, adding an organic diluent of higher boiling point than the solvent, expelling the solvent by distillation and destructively hydrogenating the mixture of extract and diluent. Insoluble and infusible constituents are preferably removed after addition of the diluent. Solvents specified for the extraction treatment are tetrahydronaphthalene and mixtures thereof with phenols or middle oils of boiling point range between 170 and 230 DEG C., and the extraction is carried out at 250-470 DEG C. preferably in presence of catalysts, e.g. inorganic acids, organic carboxylic acids, halogens, halogen compounds of metalloids with heavy metals or their compounds, e.g. finely divided tin, lead, germanium, iron, nickel, or cobalt. Diluents specified are tar fractions of boiling point above 230 DEG C., e.g. middle oils obtained in a prior hydrogenation. The destructive hydrogenation ...

Improvements in the treatment with hydrogenating gases of carbonaceous materials

... In the treatment of carbonaceous materials with hydrogenating gases congestions in the apparatus, particularly in the tube heaters, are mitigated by ascertaining attendant fluctuations in pressure and introducing into or before that part of the apparatus, where the fluctuations occur, a quantity of liquid, e.g. viscous oil not substantially volatile under the reaction conditions. The oil is preferably introduced so as not to mix with the reacting materials and to avoid intermixing no pumps or other devices causing mixing should be situated between the point of introduction of the oil and the point of congestion. If the congestion is caused by deposition of salts, e.g. ammonium chloride or carbonate, water is introduced as the liquid. Small fluctuations in pressure are measured by a U-tube U half filled with mercury and connected to a pressure balance D of usual type through lines L, M, and a catchpot B. The free ends O, P of the balance and U-tube are connected through ...

Improvements in the destructive hydrogenation or pressure extraction of solid carbonaceous substances

... 505,496. Destructive hydrogenation ; extracting oils. JOHNSON, G. W. (I. G. Farbenindustrie Akt.-Ges.) Nov. 8, 1937, No. 30646. [Classes 32 and 91] , In the destructive hydrogenation or pressure extraction of solid carbonaceous materials with solvents while flowing the reacting materials through a tower-like reaction vessel fromwhich the main portion of the products is removed into an adjacent hot separator, a portion of the reacting materials is removed from the lower part of the reaction space before the end of the reaction and the reaction products, after leaving the separator, are freed from solid constituents. The process is applicable to the limited hydrogenation of carbonaceous materials in which at most 5 per cent hydrogen is consumed in the reaction. Brown coal is( dried with 3 per cent Bayer Mass (the dried red sludge obtained in the disintegration of sludge according to the Bayer process) and pasted with " run. back oil " and " separator sludge " obtained in the process. It is ...

PRODUCTION OF LIQUID HYDROCARBONS FROM COAL

CONVERTING COAL WITH GASEOUS AND LIQUID FUELS

PROCESS FOR MAKING LOW-SULPHUR AND LOWASH FUELS

... 1504452 Low-ash formcoke CONSOLIDATION COAL CO 9 Jan 1976 [10 Jan 1975] 00835/76 Heading C5E Coal is treated by a simultaneous solvent extraction and hydrogenation under hydrodesulphurizing conditions to produce an extract which is separated into a first part low in solids, which is distilled to separate extraction solvent and pelletized in admixture with a solid carbonaceous material, and a second part high in solids, from which extraction solvent and volatiles are removed to leave a solid residue which is gasified to produce a high Btu gas. The pellets can be calcined at 800-950‹ C. Volatiles 19 and 38 can be separated into distillate fuel products 21 and 40 and recycle solvent 12 and 13; liquefaction can be carried out in the presence of hydrogen produced from a portion of the high Btu gas 34 and the solid carbonaceous material 24 used for pelletization can be recycled off-size pellets. Fig. 2 (not shown) illustrates a process in which the liquefaction is carried out in the presence ...

HYDROGENATION CATALYSTS

PROCESS FOR PRODUCING COAL LIQUID PRODUCT

CONVERSION OF COAL INTO HYDROCARBONS

... 1479521 Converting coal and water into hydrocarbons WESTINGHOUSE ELECTRIC CORP 20 Jan 1975 [29 Jan 1974] 2385/75 Heading C5E A method for converting coal and water into hydrocarbons, e.g. methane, comprises: (a) processing, e.g. pulverizing, the coal to facilitate reaction with hydrogen, (b) converting the water into H 2 and O 2 separately from the coal, (c) reacting part of the H 2 with the coal to produce at least a first hydrocarbon, (d) reacting the O 2 with the residue of the coal produced in step (c) to produce CO and (e) reacting the CO with the H 2 to produce additional hydrocarbons. A nuclear reactor provides heat to react the H 2 with the coal and to produce the H 2 and O 2 either thermally or by electrolysis.

Conversion process for solid hydrocarbonaceous materials

Solid, hydrocarbonaceous materials, such as coal, are converted to valuable liquid and gaseous products by an efficient process comprising: ...

MANUFACTURE OF SYNTHETIC CRUDE OIL

... 1493364 Oil from coal LUMMUS CO 2 Dec 1974 [12 Dec 1973] 52142/74 Heading C5E Synthetic crude oil is produced by contacting coal with a coal liquefaction solvent and hydrogen, separating insoluble material by gravity settling after the addition of a promoter liquid and catalytically hydrogenating at least a portion of the liquefied coal to produce an oil having a hydrogen to carbon atomic ratio between 1 2 and 1À8. The liquefaction is carried out at 650-900‹ F. and 500-4000 p.s.i.g. with a hydrogen consumption of 4000-12,000 SCF/ton MAF coal, either non- catalytically or in the presence of a catalyst such as cobalt molybdate, nickel molybdate, tungsten nickel sulphide or tungsten sulphide on alumina or silica-alumina. The promoter liquid has a 5 volume per cent distillation temperature of at least 250‹ F., a 95 volume per cent distillation temperature of at least 350‹ F. and no greater than 750‹ F. and a characterization factor (k) which is at least 9À75 and greater than that of the liquefaction ...

Production of hydrogenated hydrocarbons

Solid carbonaceous material, such as coal, is pyrolyzed in a pyrolysis reaction zone (18) in the presence of a particulate source of heat and gaseous hydrogen to yield a particulate carbon- containing residue of pyrolysis and volatilized hydrocarbons while the volatilized hydrocarbons are simultaneously hydrogenated. The particulate source of heat is formed by oxidizing carbon in the particulate residue to heat the particles and the hydrogen for hydrogenation is obtained by reacting a portion of the particulate residue with steam. The oxidation and hydrogen production may be carried out separately in an oxidation zone (12) and a conversion zone (14) or may alternatively be carried out together in a combined oxidation-conversion zone (13). Steam and/or carbon dioxide can be introduced into the pyrolysis reaction zone to react with carbon-containing residue and increase the yield of liquid hydrocarbon values. ...

A continuous reaction/separation method for nucleated growth reactions

A solid product resulting from the nucleated growth of the product on solid material of either the same or different composition and having a density higher than the reaction medium is formed from one or more liquid phase reactants by a method which comprises tangentially introducing the liquid phase reaction medium into the lower, smaller end of an inverted, frusto-conical reactor-separator, thereby imparting an upward swirling motion to the reaction medium in the reactor-separator, the horizontal velocity at the bottom of the reactor-separator being sufficiently large to cause fluidization of larger, solid product particles and concentration of them in the central lower portion of the reactor-separator and the vertical velocity at the top of the reactor-separator being sufficiently small to avoid carry-over of the smaller solid particles but sufficiently large to concentrate them in the upper portion of the reactor-separator; at least periodically recovering the larger, solid product ...

Process for liquefying a solid carbonaceous material

A solid carbonaceous material, for example a coal, is slurried in a vessel (10) with solvent and then preheated by passage through the convection section (19, 20) of a hybrid boiler (21) which also produces steam (e.g. in a radiant section 51 to satisfy process steam requirements and produce at least some of the electrical power required for the liquefaction process. The preheated slurry is subjected to conventional liquefaction (29) to provide gaseous material (32), normally liquid liquefaction products (34, 35, 36) and a normally solid bottoms product (33). At least a portion of the bottoms product is combusted in the combustion section (22) of the hybrid boiler (21) to provide at least some of the heat for preheating the slurry. Preferably another portion is gasified (45) to produce hydrogen, which can be employed for solvent-hydrogenation (48, 37) and/or the liquefaction (17, 15, 29). ...

COAL LIQUEFACTION PROCESS

MULTI-ZONE CONVERSION PROCESS AND REACTOR ASSEMBLY

Enhanced process for the hydroconversion of heavy oils through ebullated-bed systems

Enhanced process for the hydroconversion of heavy oils through eebullated-bed systems

Process of treatment by the carbonaceous matter hydrogen.

Apparatus for the extraction of peat

Enhanced process for the hydroconversion of heavy oils through ebullated-bed systems

Enhanced process for the hydroconversion of heavy oils through ebullated-bed systems

WIRBELSCHICHTREAKTOR ZUR ERZEUGUNG VON DAMPF, BRENNBAREN GASEN UND FLUESSIGEN NEBENPRODUKTE AUS KOHLE

PROCEDURE FOR THE PRODUCTION OF LIGHT HYDROCARBONS FROM NATURAL BITUMEN OR FUEL OILS

IMPROVED PROCEDURE FOR HYDROGENATING SPLITTING CARBON OF ABSTENTIONS OF SYNTHETIC WASTES

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

PROCEDURE AND APPARATUS FOR MAKING A LIQUID HYDROCARBON PRODUCT OF COAL.

THERMALMECHANICAL CRACKING AND HYDROGENATION PROCEDURE

PRODUCTION OF HYDROCARBON LIQUIDS AND GASES FROM OIL SHALE

COAL LIQUEFACTION

REMOVAL OF OXYGEN AND NITROGEN AND SULPHUR COMPOUNDS FROM CRUDE OIL DERIVED FROM COAL

METHOD FOR THE HYDROGENATION OF FLUID CARBON-CONTAINING APPLIED SUBSTANCES

LIQUEFACTION OF COAL

COAL HYDROGENATION

MULTIPHASE REACTOR WITH EXOTHERMIC HEATING EFFECTS

Systems for increasing catalyst concentration in heavy oil and/or coal resid hydrocracker

Systems for hydrocracking a heavy oil feedstock employ a colloidally or molecularly dispersed catalyst (e.g., molybdenum sulfide) which provide for concentration of the colloidally dispersed catalyst within the lower quality materials requiring additional hydrocracking. In addition to increased catalyst concentration, the inventive systems and methods provide increased reactor throughput, increased reaction rate, and of course higher conversion of asphaltenes and lower quality materials. Increased conversion levels of asphaltenes and lower quality materials also reduces equipment fouling, enables the reactor to process a wider range of lower quality feedstocks, and can lead to more efficient use of a supported catalyst if used in combination with the colloidal or molecular catalyst.

Coal Liquefaction System

The present disclosure relates to a coal liquefaction system for utilizing a hydrogenated vegetable oil to liquefy coal. The system includes a reactor for exposing a coal to a hydrogenated vegetable oil in the presence of a coal-derived solvent to form a slurry, a heater that elevates the temperature of the slurry in the reactor to facilitate liquefying the coal and liberating a volatile matter, and a centrifuge that separates the insoluble components from the slurry to obtain a de-ashed coal extract, wherein the coal extract is suitable for downstream processing. The system may also include a distillation column that distills the de-ashed coal extract to obtain a pitch. The system may also include a coker that cokes at least one of the de-ashed coal extract and the pitch to obtain a coke

Rubber Material in Coal Liquefaction

The present disclosure provides methods and systems for coal liquefaction using a rubber material. A method of obtaining a de-ashed coal extract includes exposing a coal to a rubber material in the presence of a coal-derived solvent to form a slurry, elevating the temperature of the slurry to facilitate liquefying the coal and liberating a volatile matter, and separating the insoluble components from the slurry to obtain a de-ashed coal extract, wherein the coal extract is suitable for downstream processing.

Sewage Material in Coal Liquefaction

The present disclosure provides methods and systems for coal liquefaction using a sewage material. A method of obtaining a de-ashed coal extract includes exposing a coal to a sewage material in the presence of a coal-derived solvent to form a slurry, elevating the temperature of the slurry to facilitate liquefying the coal and liberating a volatile matter, and separating the insoluble components from the slurry to obtain a de-ashed coal extract, wherein the coal extract is suitable for downstream processing.

Method of Obtaining a High Quality Coke from Low Rank Coal Liquefaction

The present disclosure provides methods and systems for coal liquefaction and obtaining a obtaining a high quality coke from a low rank coal extract. A method of obtaining a high quality coke from a low rank coal extract may include exposing a coal to a hydrogenated vegetable oil in the presence of a coal-derived solvent to form a slurry, elevating the temperature of the slurry to facilitate liquefying the coal and liberating a volatile matter, separating the insoluble components from the slurry to obtain a de-ashed coal extract that is quinoline insoluble-free, distilling the coal extract under vacuum to obtain a pitch with a suitable softening point, and coking the pitch to obtain a coke. The coke may be at least one of an anisotropic coke, a metallurgical coke, a graphite coke, an anode coke, and a needle coke.

Serial Deconstruction of Biomass

The present invention provides processes for deconstructing biomass using water. The method generally includes loading a reactor with biomass and water, heating the reactor to a first deconstruction temperature and establishing a first deconstruction pressure, maintaining the reactor at the first deconstruction temperature and a first deconstruction pressure for a first deconstruction period, flushing the reactor with water, and repeating these steps one or more times after establishing a second deconstructing temperature and second deconstruction pressure.

Methods and apparatuses for producing aromatic hydrocarbon-containing effluent

Embodiments of methods and apparatuses for producing an aromatic hydrocarbon-containing effluent are provided herein. The method comprises the step of rapidly heating a biomass-based feedstock to a first predetermined temperature of from about 300 to about 650° C. in the presence of a catalyst, hydrogen, and an organic solvent within a time period of about 20 minutes or less to form the aromatic hydrocarbon-containing effluent. The biomass-based feedstock comprises lignocellulosic material, lignin, or a combination thereof.

SYSTEM, APPARATUS AND PROCESS FOR EXTRACTION OF BITUMEN FROM OIL SANDS

A separation process and system for extracting hydrocarbons from a mixture. In some embodiments, a process for separating a bitumen froth stream containing bitumen froth, water and fine solids into a bitumen enriched froth stream and a water and fine solids stream, comprises: (a) receiving the bitumen froth stream in a concentrator vessel, (b) distributing the bitumen froth stream in the concentrator vessel as a substantially uniform and generally horizontal flow of the bitumen froth stream at a first flow velocity, (c) slowing the bitumen froth stream to a second flow velocity, slower than the first flow velocity, in a separation region of the concentrator vessel to promote separation of the bitumen froth from the water and fine solids, and then (d) collecting a bitumen enriched froth stream and (e) collecting a separate water and fine solids stream. Related embodiments of systems and apparatus may also be provided. 1. A process for separating a bitumen froth stream containing bitumen froth , water and fine solids into a bitumen enriched froth stream and a water and fine solids stream , the process comprising:receiving the bitumen froth stream in a concentrator vessel;distributing the bitumen froth stream in the concentrator vessel as a substantially uniform and generally horizontal flow of the bitumen froth stream at a first flow velocity;slowing the bitumen froth stream to a second flow velocity, slower than the first flow velocity, in a separation region of the concentrator vessel to promote separation of the bitumen froth from the water and fine solids, the bitumen froth accumulating as a bitumen froth layer atop a water layer with the fine solids settling within the water layer;collecting the bitumen froth layer as the bitumen enriched froth stream; andcollecting the water layer and fine solids as the water and fine solids stream.2. The process of wherein the bitumen froth layer is continuously collected at an overflow outlet while the water layer and fine ...

PROCESS OF CONVERSION OF BIOMASS TO FUEL

The present invention is directed to processes for the direct conversion of lipidic biomass fuelstock to combustible fuels. In particular, the invention provides a process for the direct conversion of animal fats to transportations fuels suitable as replacement for petroleum-derived transportation fuels. In one embodiment, the method comprises the steps of hydrolyzing a lipidic biomass to form free fatty acids, catalytically deoxygenating the free fatty acids to form n-alkanes, and reforming at least a portion of the n-alkanes into a mixture of compounds in the correct chain length, conformations, and ratio to be useful transportation fuels. Particularly, the product prepared according to the invention comprises mixtures of hydrocarbon compounds selected from the group consisting of n-alkanes, isoalkanes, aromatics, cycloalkanes, and combinations thereof. 1. A process for forming a hydrocarbon compound , said process comprising: performing catalytic deoxygenation on a stream comprising a free fatty acid by a decarboxylation reaction pathway to form a product stream comprising a paraffin.2. The process according to claim 1 , wherein said catalytic deoxygenation proceeds via a decarboxylation reaction pathway and a decarbonylation reaction pathway.3. The process according to claim 1 , wherein said catalytic deoxygenation comprises gas-phase deoxygenation.4. The process according to claim 1 , wherein said catalytic deoxygenation comprises the use of a fixed-bed catalyst.5. The process according to claim 1 , wherein said catalytic deoxygenation comprises liquid-phase catalytic deoxygenation carried out in a hydrocarbon solvent.6. The process according to claim 5 , wherein the hydrocarbon solvent comprises a paraffin from the product stream.7. The process according to claim 1 , wherein said catalytic deoxygenation is carried out at a temperature of up to 325° C.8. The process according to claim 1 , wherein said catalytic deoxygenation step comprises the use of a catalyst ...

PROCESS TO PRODUCE BIOFUELS VIA ORGANIC PHASE THERMAL HYDROCATALYTIC TREATMENT OF BIOMASS

Biofuels can be produced via an organic phase hydrocatalytic treatment of biomass using an organic solvent that is partially miscible with water. An organic hydrocarbon-rich phase from the hydrocatalytically treated products can be recycled to form at least a portion of the organic phase. 1. A method comprising:(a) providing a biomass feedstock containing cellulose and water;(b) contacting the biomass feedstock with an organic solvent having partial miscibility with water at 25° C. to form a digested biomass stream containing the organic solvent and water at an organic solvent to water mass ratio of greater than 1:1;(c) contacting the digested biomass stream with molecular hydrogen in the presence of a metal catalyst capable of activating molecular hydrogen, under organic phase hydrothermal conditions to form a hydrocatalytically treated mixture that contains a plurality of hydrocarbon molecules and oxygenated hydrocarbon molecules;(d) phase separating the hydrocatalytically treated mixture, by liquid-liquid separation, into an organic hydrocarbon-rich phase and a water phase comprising water soluble oxygenated hydrocarbons;(e) providing at least a portion of the organic hydrocarbon-rich phase to step (b) to form at least a portion of the organic solvent; and(f) processing at least a portion of the water phase, at least a portion of the organic hydrocarbon-rich phase, or at least a portion of both water phase and organic hydrocarbon-rich phase, to form a fuel blend comprising higher hydrocarbons.2. The method of wherein water is present in the organic phase at a concentration of less than 50 weight percent.3. The method of wherein water is present in the organic phase at a concentration of less than 15 weight percent.4. The method of wherein the fuel blend comprises at least one composition selected from the group consisting of: a fuel additive claim 1 , a gasoline fuel claim 1 , a diesel fuel claim 1 , and a jet fuel.5. The method of wherein step (f) comprises ...

PROCESS FOR CONVERSION OF A CELLULOSIC MATERIAL

A process for conversion of a cellulosic material comprising 1. A method for conversion of a cellulosic material comprising contacting a cellulosic material with a liquid solvent at a temperature of equal to or more than about 200° C.; or', 'contacting a cellulosic material with a liquid solvent at a temperature of equal to or more than about 100° C. in the presence of a catalyst; and, 'a liquefaction step to produce a final liquefied product, the liquefaction step comprisinga catalytic cracking step to produce at least one cracked product, the catalytic cracking step comprising contacting at least part of the final liquefied product with a fluidized catalytic cracking catalyst at a temperature of equal to or more than about 400° C.2. The method of claim 1 , wherein the liquid solvent comprises water and/or an organic solvent.3. The method of claim 1 , wherein the liquefaction step comprises simultaneously contacting the cellulosic material with an organic solvent claim 1 , a source of hydrogen claim 1 , an acid catalyst and a hydrogenation catalyst at a temperature of equal to or more than about 150° C.4. The method of claim 1 , wherein the liquefaction step comprises contacting the cellulosic material with an organic solvent in the presence of an acid catalyst at a temperature of equal to or more than about 150° C. to produce an intermediate liquefied product; and subsequently hydrotreating the intermediate liquefied product with a source of hydrogen in the presence of a hydrotreatment catalyst to produce a final liquefied product.5. The method of claim 1 , wherein the liquid solvent is an organic solvent and wherein the process further comprises a separation step claim 1 , wherein at least a portion of the final liquefied product produced in the liquefaction step is separated from at least part of the organic solvent.6. The method of wherein the separated portion of the organic solvent is used in the liquefaction step.7. The method of claim 1 , wherein the ...

Systems and Methods for Developing Terrestrial and Algal Biomass Feedstocks and Bio-Refining the Same

Methods and systems for developing and bio-refining or processing biomass feedstocks into a spectrum of bio-based products which can be used as a substitute for fossil oil derivatives in various types of product manufacturing processes and/or the production of bio-energy are disclosed. In addition, methods and systems for identifying, measuring and controlling key parameters in relation to specific biomass developing processes and bio-refining processes so as to maximize the efficiency and efficacy of such processes while standardizing the underlying parameters to facilitate and enhance large-scale production of bio-based products and/or bio-energy are disclosed. 1. A method for processing standardized biomass feedstocks to yield bio-based products , comprising:providing a standardized biomass feedstock;formatting the standardized biomass feedstock for subsequent refinement; andprocessing the standardized biomass feedstock to yield bio-based products therefrom.2. The method of claim 1 , wherein providing a standardized biomass feedstock comprises providing one of: a terrestrial biomass feedstock and a high moisture content biomass feedstock.3. The method of claim 2 , wherein the terrestrial biomass feedstock comprises one of: a herbaceous biomass feedstock claim 2 , a woody biomass feedstock claim 2 , an agricultural food claim 2 , an agricultural feed crop claim 2 , an agricultural crop waste claim 2 , an agricultural residue claim 2 , a wood waste claim 2 , a wood residue claim 2 , an aquatic plant claim 2 , a vegetable oil claim 2 , a livestock manure claim 2 , a municipal waste claim 2 , and an industrial waste.4. The method of claim 2 , wherein the high moisture content biomass feedstock comprises one of: algae claim 2 , beet pulp claim 2 , and sludge.5. The method of claim 1 , wherein providing a standardized biomass feedstock comprises providing a standardized mixture of constituent biomass feedstock components.6. The method of claim 5 , wherein the mixture ...

PROFITABLE METHOD FOR CARBON CAPTURE AND STORAGE

The present invention generally relates to a method for sequestering carbon dioxide. Biomass is converted into paraffinic hydrocarbons. The paraffinic hydrocarbons are steam cracked into olefins. The olefins are polymerized into non-biodegradable polyolefins. 1. A method comprising steam cracking paraffinic hydrocarbons into olefins , wherein the paraffinic hydrocarbons are derived from a biomass.2. The method of claim 1 , wherein the paraffinic hydrocarbons are produced by gasification followed by Fischer-Tropsch conversion3. The method of claim 2 , wherein the biomass is wood chips.4. The method of claim 1 , wherein the paraffinic hydrocarbons are produced by the hydrotreating of fatty acids and/or fatty acid esters.5. The method of claim 4 , wherein the fatty acids and/or fatty acid esters are oils from plants.6. The method of claim 4 , wherein the fatty acids and/or fatty acid esters are fats from animals.7. The method of claim 4 , wherein the fatty acids and/or fatty acid esters are oils from algae.8. The method of claim 7 , wherein the algae are grown in ponds and/or photo-bioreactors with COsupplied from stationary emission sources.9. The method of claim 8 , wherein the stationary emission source is a coal-fired power plant.10. The method of claim 1 , wherein the olefins comprise ethylene claim 1 , propylene claim 1 , butenes claim 1 , and butadiene.11. The method of claim 1 , wherein bio-derived hydrogen is produced as byproduct of steam cracking.12. The method of claim 1 , wherein bio-derived pyrolysis gasoline is produced as byproduct of steam cracking.13. The method of claim 12 , wherein the pyrolysis gasoline is used as motor gasoline blend stock.14. The method of claim 13 , wherein the pyrolysis gasoline is hydrogenated prior to use as motor gasoline.15. The method of claim 1 , wherein bio-derived fuel gas is produced as byproduct of steam cracking.16. The method of claim 1 , wherein the pyrolysis fuel oil yield is less than 1 wt % of the paraffinic ...

PROCESS FOR COAL CONVERSION COMPRISING AT LEAST ONE STEP OF LIQUEFACTION FOR THE MANUFACTURE OF AROMATICS

The invention relates to a process for coal conversion, optionally in co-processing with other feedstocks, notably of the biomass type, comprising at least one liquefaction step, followed by a fixed-bed hydrocracking step and a catalytic reforming step. With this process, aromatic compounds can be obtained from a feedstock containing coal. 1. Process for conversion of coal to aromatic compounds comprising the following steps:a) a coal liquefaction step in the presence of hydrogen,b) a step of separation of the effluent obtained at the end of step a) into a light fraction of hydrocarbons containing compounds boiling at most at 500° C. and a residual fraction,c) a hydrocracking step in the presence of hydrogen of at least a proportion of said light fraction of hydrocarbons obtained at the end of step b) in at least one reactor containing a fixed-bed hydrocracking catalyst, the conversion of the fraction 200° C. in the hydrocracking step being greater than 30 wt %,d) separation of the effluent obtained at the end of step c) into at least a fraction containing naphtha and a fraction heavier than the naphtha fraction,e) a catalytic reforming step of the fraction containing naphtha, giving hydrogen and a reformate containing aromatic compounds,f) a separation step of the aromatic compounds from the reformate.2. Process according to in which the liquefaction step a) in the presence of hydrogen is carried out in the presence of an ebullating-bed supported catalyst claim 1 , in the presence of a catalyst dispersed in an entrained bed or without catalyst added.3. Process according to in which the liquefaction step a) is carried out in at least two reactors arranged in series each containing an ebullating-bed supported catalyst.4. Process according to in which the liquefaction step a) operates at a temperature between 300° C. and 440° C. for the first reactor and a temperature between 350° C. and 470° C. for the second reactor claim 1 , then at a pressure between 15 and 25 MPa ...

PROCESS FOR MAKING A DISTILLATE PRODUCT AND/OR C2-C4 OLEFINS

A process for making a distillate product and one or more C2-C4 olefins from a FCC feedstock containing a cellulosic material and a hydrocarbon co-feed is provided. 1. A process for making a distillate product and one or more C2-C4 olefins comprising:a) contacting a FCC feedstock with a FCC catalyst at a temperature of at least 400° C. in a riser reactor to produce a distillate product and a spent FCC catalyst, wherein the FCC feedstock comprises a cellulosic material and a hydrocarbon co-feed;b) separating at least a portion of the distillate product from the spent FCC catalyst;c) regenerating the spent FCC catalyst to produce a regenerated FCC catalyst;d) contacting an intermediate reactor feedstock with at least a portion of the regenerated FCC catalyst at a temperature of at least 500° C. in an intermediate reactor to produce one or more C2-C4 olefins and a used regenerated FCC catalyst;e) separating at least a portion of the one or more C2-C4 olefins from the used regenerated catalyst; andf) providing at least a portion of the used regenerated FCC catalyst as FCC catalyst in step a).2. The process of wherein the FCC feedstock comprises a hydrocarbon co-feed and at least one cellulosic material selected from the group consisting of a solid cellulosic material claim 1 , a pyrolysis oil derived from cellulosic material claim 1 , and a mixture thereof.3. The process of wherein the hydrocarbon co-feed comprises at least 8 wt % elemental hydrogen claim 1 , based on the total weight of the hydrocarbon co-feed on a dry basis.4. The process of wherein the hydrocarbon co-feed comprises in the range from at least 20 wt % to at most 100 wt % of at least one paraffin claim 1 , based on the total weight of the hydrocarbon co-feed.5. The process of wherein the combination of the cellulosic material and the hydrocarbon co-feed has an overall molar ratio of hydrogen to carbon (H/C) of equal to or more than 1.1 (1.1/1).6. The process of wherein the cellulosic material is a solid ...

Methods for Producing Hydrocarbon Products from Bio-Oils and/or Coal-Oils

The present invention relates to a method for producing a hydrocarbon product from coal and/or biomass comprising the following steps: converting the coal to a coal-oil and/or converting the biomass to bio-oil, optionally processing the coal-oil and/or bio-oil in a hydroprocessing reaction to remove one or more of oxygen, nitrogen or sulfur from hydrocarbon compounds in the coal-oil and/or bio-oil; and using at least a portion of the coal-oil and/or bio-oil as a feedstock in a cracking reaction to convert hydrocarbon compounds in the feedstock into a mixture of smaller hydrocarbon compounds comprising the hydrocarbon product. 1. A method for producing a hydrocarbon product from coal comprising the following steps:converting the coal to a coal-oil by thermal or hydrothermal conversion;processing the coal-oil in a hydroprocessing reaction to remove one or more of oxygen, nitrogen or sulfur from hydrocarbon compounds in the coal-oil; andusing at least a portion of the coal-oil as a feedstock in a cracking reaction to convert hydrocarbon compounds in the feedstock into a mixture of smaller hydrocarbon compounds comprising the hydrocarbon product.2. A method for producing a hydrocarbon product from biomass comprising the following steps:converting the biomass to bio-oil by thermal or hydrothermal conversion;processing the bio-oil in a hydroprocessing reaction to remove one or more of oxygen, nitrogen or sulfur from hydrocarbon compounds in the bio-oil; andusing at least a portion of the bio-oil as a feedstock in a cracking reaction to convert hydrocarbon compounds in the feedstock into a mixture of smaller hydrocarbon compounds comprising the hydrocarbon product.3. The method of claim 2 , wherein the feedstock is comprised of at least:(i) 50% of said bio-oil and said hydrocarbon product is at least a 50% renewable product;(ii) 75% of said bio-oil and said hydrocarbon product is at least a 75% renewable product; or(iii) 90% of said bio-oil and said hydrocarbon product is ...

Methods for Biofuel Production

The invention relates generally to methods for the production of biofuels from organic matter, the methods comprising treating the organic matter with an aqueous solvent and at least one additional catalyst under conditions of heat and pressure. The invention also relates to biofuel products obtainable by the methods. 1. A method for producing a biofuel , the method comprising treating organic matter with an aqueous solvent and at least one additional catalyst at a temperature of between about 250° C. and about 400° C. , and a pressure of between about 100 bar and about 300 bar.2. The method claim 1 , according to claim 1 , wherein said additional catalyst is an additional base catalyst.3. The method according to claim 2 , wherein said additional base catalyst is an alkali metal hydroxide catalyst or a transition metal hydroxide catalyst.4. The method according to or claim 2 , wherein said additional base catalyst is sodium hydroxide or potassium hydroxide.5. The method according to any one of to claim 2 , wherein said treating is performed under conditions of continuous flow.6. The method according to any one of to claim 2 , wherein said treating comprises use of at least one additional catalyst that enhances incorporation of hydrogen into said organic matter.7. The method according to claim 6 , wherein said catalyst that enhances incorporation of hydrogen is selected from the group consisting of alkali metal formate catalysts claim 6 , transition metal formate catalysts claim 6 , reactive carboxylic acid catalysts claim 6 , transition metal catalysts claim 6 , sulphide catalysts claim 6 , noble metal catalysts claim 6 , water-gas-shift catalysts claim 6 , and combinations thereof.8. The method according to claim 7 , wherein said catalyst is sodium formate.9. The method according to any one of to claim 7 , wherein said treating comprises use of at least one additional catalyst that enhances removal of oxygen from said organic matter.10. The method according to ...

CO-PROCESSING OF BIOMASS AND SYNTHETIC POLYMER BASED MATERIALS IN A PYROLYSIS CONVERSION PROCESS

Disclosed is a process for biomass conversion which includes co-processing the biomass with thermoplastic and non-thermoplastic polymer based materials in a catalytic pyrolysis reactor to convert such to liquid hydrocarbons; wherein hydrogen atoms originating with the polymer materials can remove oxygen from oxygenated hydrocarbons produced in the conversion of the biomass in the reactor. 1. A process comprising charging a feed comprising a biomass and a synthetic thermoplastic polymer based material to a reactor for contact with a catalyst and conversion to a product comprising liquid hydrocarbons; wherein the weight ratio of said biomass to said synthetic thermoplastic polymer based material is greater than about 1:4.2. The process of wherein hydrogen atoms originating with said synthetic thermoplastic polymer based material remove oxygen from oxygenated hydrocarbons produced in the conversion of said biomass in said reactor.3. The process of wherein the weight ratio of said biomass to said synthetic thermoplastic polymer based material is greater than about 1:2.4. The process of wherein the weight ratio of said biomass to said synthetic thermoplastic polymer based material is greater than about 1:1.5. The process of wherein said reactor is a fluid bed reactor claim 1 , a moving bed reactor claim 1 , or a cyclone reactor.6. The process of wherein said reactor is operated at a temperature of from about 150 to about 600° C. and in an oxygen-poor atmosphere.7. The process of wherein said reactor is operated at a temperature of from about 250 to about 550° C. and in an oxygen-poor atmosphere.8. The process of wherein said biomass portion of said feed is subjected to pretreatment prior to charging to said reactor; wherein said pretreatment comprises a method selected from the group consisting of: a) drying; b) heat treatment in an oxygen-poor or oxygen-free atmosphere; c) solvent explosion; d) mechanical treatment with catalyst particles; e) demineralization; f) ...

Two-Stage Reactor And Process For Conversion Of Solid Biomass Material

A two-stage reactor/process is disclosed for the conversion of solid particulate biomass material and includes: a first stage, in which solid particulate biomass material is pyrolyzed to primary reaction products, and a second stage in which the primary reaction products are catalytically converted in a second stage which is operated at a temperature higher than that of the first stage. 1. A two-stage reactor for the conversion of a solid particulate biomass material , the two-stage reactor comprising:{'b': '1', '(i) a first stage reactor operated at a temperature T in which at least part of said solid particulate biomass material is subjected to a pyrolysis reaction, thereby forming primary reaction products; and'}{'b': 2', '1, '(ii) a second stage reactor operated at a temperature T, which is higher than T, in which at least part of said primary reaction products are subjected to a catalytic conversion reaction, thereby forming secondary reaction products, wherein said second stage reactor is in fluid communication with said first stage reactor.'}2. The two-stage reactor according to wherein a part of said solid particulate biomass material passes from said first stage reactor to said second stage reactor and is subjected to a pyrolysis reaction in said second stage reactor to form products which become a part of said primary reaction products.3. The two-stage reactor according to wherein said first stage reactor and said second stage reactor each have an internal diameter claim 1 , and wherein the internal diameter of the second stage reactor is less than the internal diameter of said first stage reactor.4. The two-stage reactor according to further comprising: a separator for removing solid particles from said secondary reaction products claim 1 , wherein said solid particles comprise deactivated catalyst particles; a stripper for stripping volatile materials from said deactivated catalyst particles claim 1 , thereby forming stripped catalyst particles; and a ...

METHOD FOR THE CONVERSION OF POLYMER CONTAMINATED FEEDSTOCKS

A method for producing hydrocarbons from biomass is provided. The method involves supplying a feed stream; supplying a heated hydrocarbon solvent; combining the feed stream and the heated hydrocarbon solvent to produce a reactor feed, and hydrodeoxygenating the reactor feed to produce hydrocarbons; where the feed stream includes a synthetic polymer as well as biomass having fatty acids, glycerides, or combinations thereof. 1. A method for producing hydrocarbons from biomass , comprising:supplying a feed stream;supplying a heated hydrocarbon solvent;combining the feed stream and the heated hydrocarbon solvent to produce a reactor feed, andhydrodeoxygenating the reactor feed to produce hydrocarbons;wherein the feed stream comprises a synthetic polymer and biomass having fatty acids, glycerides, or combinations thereof.2. The method of claim 1 , wherein the feed stream comprises a member from the group consisting of animal fats claim 1 , poultry oil claim 1 , soybean oil claim 1 , canola oil claim 1 , rapeseed oils claim 1 , palm oil claim 1 , palm kernel oil claim 1 , jatropha oil claim 1 , castor oil claim 1 , camelina oil claim 1 , algae oil claim 1 , seaweed oil claim 1 , halophile oils claim 1 , rendered fats claim 1 , restaurant greases claim 1 , brown grease claim 1 , yellow grease claim 1 , waste industrial frying oils claim 1 , fish oils claim 1 , and tall oil.3. The method of claim 1 , wherein the biomass comprises waste from a municipality claim 1 , industrial operations claim 1 , or both.4. The method of claim 1 , wherein the biomass comprises a member selected from the group consisting of waste vegetable oils claim 1 , restaurant greases claim 1 , trap grease from municipalities claim 1 , waste industrial frying oils claim 1 , and spent oils from industrial packaged food operations.5. The method of claim 1 , wherein the synthetic polymer is a component of plastic film packaging.6. The method of claim 1 , wherein the feed stream comprises one or more ...

PROCESS FOR CONVERTING A SOLID BIOMASS MATERIAL

A process for converting a solid biomass material, comprising contacting the solid biomass material and a hydrocarbon co-feed with a catalytic cracking catalyst at a temperature of more than 400° C. in a riser reactor to produce one or more cracked products, wherein the solid biomass material is introduced to the riser reactor at a location downstream of the location where the hydrocarbon co-feed is introduced to the riser reactor. 1. A process for converting a solid biomass material comprising: contacting , in a riser reactor , the solid biomass material and a hydrocarbon co-feed with a catalytic cracking catalyst at a temperature of more than 400° C. to produce one or more cracked products , said solid biomass material is introduced to the riser reactor at a location downstream of the location where the hydrocarbon co-feed is introduced to the riser reactor.2. The process of wherein the solid biomass material and the hydrocarbon co-feed is contacted with the catalytic cracking catalyst in the presence of a liftgas at a temperature of more than 400° C. claim 1 , said liftgas is introduced to the riser reactor at a location upstream of the location where the hydrocarbon co-feed is introduced to the riser reactor.3. The process of wherein the liftgas does not contain vaporized oil and/or vaporized oil fractions.4. The process of wherein the vaporized oil fraction is selected from the group consisting of vaporized liquefied petroleum gas claim 3 , vaporized gasoline claim 3 , vaporized diesel claim 3 , vaporized kerosene and vaporized naphtha.5. The process of wherein the hydrocarbon co-feed comprises straight run (atmospheric) gas oils claim 1 , flashed distillate claim 1 , vacuum gas oils (VGO) claim 1 , coker gas oils claim 1 , gasoline claim 1 , naphtha claim 1 , diesel claim 1 , kerosene claim 1 , atmospheric residue (“long residue”) and vacuum residue (“short residue”) and/or mixtures thereof.6. The process of wherein equal to or more than 60 wt % of the ...

PROCESSING OF ORGANIC MATTER

The invention relates generally to the field of fuel production. More specifically, the invention relates to biofuel production from high temperature oil-based processing of organic matter. 1. A method for producing biofuel , the method comprising:producing a slurry comprising organic matter feedstock, water and oil;treating the slurry in a reactor apparatus at a temperature of between about 200° C. and about 450° C. and a pressure of between about 100 bar and about 350 bar; andcooling the slurry and releasing said pressure thereby providing a product comprising said biofuel.2. The method of claim 1 , wherein the slurry comprises between about 20% and about 60% by weight of said oil.3. The method of claim 1 , wherein the slurry comprises between about 20% and about 40% by weight of said organic matter.4. The method of claim 1 , wherein the slurry further comprises an aqueous alcohol.5. The method of claim 4 , wherein the aqueous alcohol is ethanol or methanol.6. The method of claim 4 , wherein the slurry comprises a percentage by weight of said alcohol of: between about 5 wt % and about 40 wt % claim 4 , between about 5 wt % and about 30 wt % claim 4 , between about 5 wt % and about 25 wt % claim 4 , between about 5 wt % and about 20 wt % claim 4 , between about 5 wt % and about 15 wt % claim 4 , or between about 5 wt % and about 10 wt %.7. The method of claim 1 , wherein the organic matter feedstock is lignocellulosic matter or lignite.8. (canceled)9. The method of claim 1 , wherein said treating comprises contacting the slurry with subcritical or supercritical steam in a chamber of said reactor apparatus claim 1 , and wherein said slurry is at ambient or near ambient temperature and pressure prior to said contacting with the subcritical or supercritical steam.10. (canceled)11. The method of comprising treating organic matter with an oil-based solvent comprising less than about 50 wt % water at a temperature of between about 200° C. and about 400° C. claim 1 , and ...

METHOD OF PRODUCING DROP-IN DIESEL

Methods are disclosed for producing renewable diesel from hydrocarbon-containing feedstock using microwave energy and hydrotreatment. 1. A method for producing a fuel , comprising:forming pellets comprising at least one hydrocarbon-containing feedstock and at least one catalyst; crude oil;', 'biochar; and', [{'sub': '2', 'H;'}, 'CO; and', {'sub': '2', 'optionally, CO;'}], 'optionally, syngas comprising], 'depolymerizing said hydrocarbon-containing feedstock in the presence of said catalyst using high-frequency microwave energy at a temperature of about 275° C. and 350° C. to form a composition comprising{'sub': '2', 'reacting said crude oil with Hto remove impurities and to form an upgraded crude oil; and'}distilling said upgrading crude oil to form a phenol fraction and a diesel fraction.2. A method of claim 1 , further comprising:blending said diesel fraction with at least one additive.3. A method of claim 1 , further comprising:blending said diesel fraction with at least one fossil fuel.4. A method of claim 1 ,wherein said depolymerizing step is carried out at a temperature of about 280° C.5. A method of claim 1 ,wherein said pellets have a density sufficient to permit said depolymerizing step and said hydrotreating step without substantially mechanically degrading said pellets.6. A method of claim 1 , further comprising:drying said hydrocarbon-containing feedstock prior to forming said pellets.7. A method of claim 6 , further comprising:combusting at least a portion of said syngas in said drying step.8. A method of claim 1 , further comprising:recovering heat from said biochar to form a cooled biochar.9. A method of claim 8 , further comprising:storing said cooled biochar.10. A method of claim 1 , further comprising:storing said phenol fraction.11. A method of claim 1 ,wherein said phenol fraction comprises methoxyphenol.12. A method of claim 1 , further comprising:storing said diesel fraction.13. A method of claim 1 ,wherein said catalyst is a zeolite.14. A ...

METHODS AND SYSTEMS FOR PROCESSING BIOMASS MATERIAL

Embodiments of the present invention provide for production and recovery of volatile organic compounds and higher hydrocarbons from biomass material. One embodiment comprises contacting a solid component of a biomass material with a digestive solvent to form a digested biomass stream, and at least a portion of the digested biomass is further thermocatalytically treated to generate higher hydrocarbons. The solid component is generated by a method comprising introducing a biomass material to a compartment of a solventless recovery system, wherein the biomass material contains one or more volatile organic compounds; contacting the biomass material with a superheated vapor stream in the compartment to vaporize at least a portion of an initial liquid content in the biomass material; separating a vapor component and a solid component from the heated biomass material; retaining at least a portion of the gas component for use as part of the superheated vapor stream. 1. A method for processing a biomass material comprising:introducing a biomass material to a compartment of a solventless recovery system, wherein the biomass material contains one or more volatile organic compounds;contacting the biomass material with a superheated vapor stream in the compartment to vaporize at least a portion of an initial liquid content in the biomass material, said superheated vapor stream comprising at least one volatile organic compound;separating a vapor component and a solid component from the heated biomass material, said vapor component comprising at least one volatile organic compound;retaining at least a portion of the gas component for use as part of the superheated vapor stream;discharging the solid component from the solventless recovery system;contacting at least a portion of the solid component with a digestive solvent to form a digested biomass stream comprising carbohydrates;contacting the digested biomass stream with molecular hydrogen in the presence of a molecular hydrogen ...

Systems and Methods For Hydrotreating A Shale Oil Stream Using Hydrogen Gas That Is Concentrated From The Shale Oil Stream

Systems and methods for hydrotreating a liquid fraction of a shale oil stream using hydrogen gas that is concentrated from a gaseous fraction of the shale oil stream. The systems and methods include providing a portion of the gaseous fraction to a sorptive separation assembly and separating a concentrated hydrogen stream from the portion of the gaseous fraction within the sorptive separation assembly. The system and methods further include providing the concentrated hydrogen stream and the liquid fraction to a hydrotreater and reacting the concentrated hydrogen stream with the liquid fraction within the hydrotreater to produce the hydrotreated liquid stream. The systems and methods may include generating the shale oil stream within a subterranean formation using an in situ process, such as an in situ shale oil conversion process and/or providing a supplemental hydrogen stream to the hydrotreater. 1. A method of hydrotreating a liquid fraction of a shale oil stream with hydrogen gas concentrated from a gaseous fraction of the shale oil stream , the method comprising:separating the liquid fraction of the shale oil stream from the gaseous fraction of the shale oil stream;providing a portion of the gaseous fraction to a sorptive separation assembly;separating, in the sorptive separation assembly, a concentrated hydrogen stream from the portion of the gaseous fraction;providing the concentrated hydrogen stream and the liquid fraction to a hydrotreater; andreacting, in the hydrotreater, the concentrated hydrogen stream with the liquid fraction to produce a hydrotreated liquid stream.2. The method of claim 1 , wherein the method further includes generating the shale oil stream within a subterranean formation using at least one of a pyrolysis reaction claim 1 , an in situ pyrolysis reaction claim 1 , a shale oil retort process claim 1 , a shale oil heat treating process claim 1 , a hydrogenation reaction claim 1 , a thermal dissolution process claim 1 , and an in situ shale ...

METHOD FOR CONVERTING A HYDROCARBONACEOUS MATERIAL TO A FLUID HYDROCARBON PRODUCT COMPRISING P-XYLENE

The invention relates to a method for producing a fluid hydrocarbon product, and more specifically, to a method for producing a fluid hydrocarbon product via catalytic pyrolysis. The reactants comprise hydrocarbonaceous materials (e.g., biomass). The catalyst comprises a zeolite catalyst treated with a silicone compound. The product comprises p-xylene. 1. A method for producing a fluid hydrocarbon product comprising p-xylene from a hydrocarbonaceous material , comprising:feeding the hydrocarbonaceous material to a reactor;pyrolyzing within the reactor at least a portion of the hydrocarbonaceous material under reaction conditions sufficient to produce a pyrolysis product; andcatalytically reacting at least a portion of the pyrolysis product under reaction conditions in the presence of a zeolite catalyst to produce the fluid hydrocarbon product;the zeolite catalyst comprising pores with pore mouth openings and catalytic sites on the external surface of the catalyst, and an effective amount of a treatment layer derived from a silicone compound to reduce the size of the pore mouth openings and to render at least some of the catalytic sites on the external surface of the catalyst inaccessible to the pyrolysis product.2. The method of wherein catalytic sites are positioned in the pores near the pore mouth openings claim 1 , and the treatment layer renders at least some of the catalytic sites in the pores near the pore mouth openings inaccessible to the pyrolysis product.3. The method of or wherein the fluid hydrocarbon product comprises xylenes with a p-xylene selectivity in the xylenes of at least about 40% claim 1 , or at least about 45% claim 1 , or at least about 50% claim 1 , or at least about 55% claim 1 , or at least about 60% claim 1 , or at least about 65% claim 1 , or at least about 70% claim 1 , or at least about 75% claim 1 , or at least about 80% claim 1 , or at least about 85% claim 1 , or at least about 90%.4. The method of any of the preceding claims ...

COMBINED HYDROTHERMAL LIQUEFACTION AND CATALYTIC HYDROTHERMAL GASIFICATION SYSTEM AND PROCESS FOR CONVERSION OF BIOMASS FEEDSTOCKS

A combined hydrothermal liquefaction (HTL) and catalytic hydrothermal gasification (CHG) system and process are described that convert various biomass-containing sources into separable bio-oils and aqueous effluents that contain residual organics. Bio-oils may be converted to useful bio-based fuels and other chemical feedstocks. Residual organics in HTL aqueous effluents may be gasified and converted into medium-BTU product gases and directly used for process heating or to provide energy. 1. A biomass conversion process , comprising the steps of:hydrothermally liquefying (HTL) a biomass-containing feedstock in an aqueous medium at a temperature and pressure selected to form a biomass conversion product comprising a bio-oil fraction and an aqueous fraction containing residual organics remaining after conversion of the biomass-containing feedstock, each fraction separable from the other fraction; andcatalytically hydrothermally gasifying (CHG) the residual organics in the aqueous fraction over a selected catalyst at a temperature and pressure selected to form a product gas containing at least one medium-BTU gas.2. The process of claim 1 , wherein the biomass-containing feedstock comprises biomass that is not solvent extracted.3. The process of claim 1 , wherein the biomass-containing feedstock is a biomass-containing aqueous slurry.4. The method of claim 1 , wherein the hydrothermal liquefaction includes separating the bio-oil fraction from the aqueous fraction containing the residual organics.5. The method of claim 1 , wherein the liquefaction includes flowing the biomass-containing feedstock through an HTL stage and the gasification includes flowing aqueous effluents released from the HTL stage containing the residual organics into a CHG stage without a change in operating pressure.6. The method of claim 1 , wherein the liquefaction and gasification are performed in separate reactor stages concurrently or sequentially.7. The method of claim 1 , wherein the ...

HYDROPYROLYSIS OF BIOMASS FOR PRODUCING HIGH QUALITY LIQUID FUELS

A self-sustaining process for producing liquid fuels from biomass in which the biomass is hydropyrolyzed in a reactor vessel containing molecular hydrogen and a deoxygenating catalyst, producing a partially deoxygenated pyrolysis liquid, which is hydrogenated using a hydroconversion catalyst, producing a substantially fully deoxygenated pyrolysis liquid and a gaseous mixture comprising CO and light hydrocarbon gases (C-C). The gaseous mixture is reformed in a steam reformer, producing reformed molecular hydrogen, which is then introduced into the reactor vessel for hydropyrolizing the biomass. The deoxygenated liquid product is further processed to produce diesel fuel and gasoline. 1. (canceled)2. A process for a producing a liquid hydrocarbon-containing product from biomass , the process comprising:(a) pyrolyzing the biomass in the presence of hydrogen and a deoxygenation catalyst to provide a hydropyrolysis effluent comprising a partially deoxygenated hydropyrolysis product and char, and(b) hydroconverting the partially deoxygenated hydropyrolysis product in the presence of a hydroconversion catalyst to provide a hydroconversion effluent comprising the liquid hydrocarbon-containing product and a water-containing product,wherein deoxygenation in step (a) and hydroconversion in step (b) are carried out to an extent whereby the liquid hydrocarbon-containing product has sufficiently low oxygen content to be phase-separable from the water-containing product.3. The process of claim 2 , further comprising(c) separating the liquid hydrocarbon-containing product from the water-containing product by phase separation.4. The process of claim 3 , wherein claim 3 , following separation in step (c) claim 3 , the water-containing product contains less than 2000 ppm dissolved total organic carbon (TOC).5. The process of claim 3 , wherein the hydroconversion reactor effluent further comprises a gaseous mixture comprising CO and C-Chydrocarbons claim 3 , the process further ...

ENHANCED METHODS OF SYNTHETIC CHEMICAL AND FUEL PRODUCTION THROUGH INTEGRATED PROCESSING AND EMISSION RECOVERY

The process described in this embodiment relates to the field of synthetic fuel and synthetic chemical production through co-processing methods such as pyrolysis, combustion, gasification, distillation, catalytic synthesis, methanol synthesis, hydro-treatment, and hydrogenation, cavitation, bioreaction, and water treatment. The inventions described herein relates to synthetic hydrocarbons derived from various carbonaceous materials such as biomass, solid municipal waste and coal which can be converted into typical industrial products and various unique synthetic fuels. The byproducts of each process are directed to other processes for additional product yield and to reduce waste and emissions. 1. A process of producing synthetic fuels and chemical products comprising:a. integrating three or more fuel/chemical production processes such that one or more byproducts of one or more production processes are applied to other processes for additional product yield and to reduce waste and emissions;b. a raw feedstock includes various carbonaceous materials such as biomass, solid municipal waste and coal; andc. integrating three or more facilities that utilize said chemical product/fuel production processes such that one or more byproducts produced at one or more said facilities are used in the production of fuel/chemical product at other said facilities for additional product yield and to reduce waste and emissions;d. operating the integrated fuel/chemical production processes to produce synthetic fuel and chemical products such that one or more byproducts of one or more production processes are utilized in an operation of other fuel/chemical production processes.2. The process of claim 1 , wherein said fuel/chemical production processes are selected from the group consisting of feedstock preparation claim 1 , pyrolysis claim 1 , combustion claim 1 , distillation claim 1 , gasification claim 1 , water treatment claim 1 , catalytic synthesis claim 1 , hydro-treatment/ ...

BIOMASS CONVERSION SYSTEMS PROVIDING INTEGRATED STABILIZATION OF A HYDROLYSATE USING A SLURRY CATALYST FOLLOWING BIOMASS PRETREATMENT AND METHODS FOR USE THEREOF

Digestion of cellulosic biomass solids to form a hydrolysate may be conducted with integrated catalytic reduction during digestion to transform soluble carbohydrates in the hydrolysate into a more stable reaction product. Such integrated catalytic reduction may be conducted using a slurry catalyst. Biomass conversion systems for performing integrated catalytic reduction can comprise: a hydrothermal digestion unit that contains a slurry catalyst capable of activating molecular hydrogen; an optional hydrogen feed line that is operatively connected to the hydrothermal digestion unit; a fluid circulation loop comprising the hydrothermal digestion unit and a catalytic reduction reactor unit, the catalytic reduction reactor unit also containing the slurry catalyst; a pretreatment digestion unit that is not part of the fluid circulation loop and does not contain the slurry catalyst; and a solids transport mechanism operatively connecting the pretreatment digestion unit to the hydrothermal digestion unit. 1. A biomass conversion system comprising:a hydrothermal digestion unit that contains a slurry catalyst capable of activating molecular hydrogen;an optional hydrogen feed line that is operatively connected to the hydrothermal digestion unit;a fluid circulation loop comprising the hydrothermal digestion unit and a catalytic reduction reactor unit, the catalytic reduction reactor unit also containing the slurry catalyst;a pretreatment digestion unit that is not part of the fluid circulation loop and does not contain the slurry catalyst; anda solids transport mechanism operatively connecting the pretreatment digestion unit to the hydrothermal digestion unit.2. The biomass conversion system of claim 1 , wherein the solids transport mechanism operatively connects the bottom of the pretreatment digestion unit to the top of the hydrothermal digestion unit.30. The biomass conversion system of claim claim 1 , wherein the solids transport mechanism is capable of conveying a biomass ...

BIOMASS CONVERSION SYSTEMS PROVIDING INTEGRATED STABILIZATION OF A HYDROLYSATE USING A SLURRY CATALYST AND METHODS FOR USE THEREOF

Digestion of cellulosic biomass solids to form a hydrolysate may be conducted with integrated catalytic reduction during digestion to transform soluble carbohydrates in the hydrolysate into a more stable reaction product. Such integrated catalytic reduction may be conducted using a slurry catalyst. Biomass conversion systems for performing integrated catalytic reduction can comprise: a hydrothermal digestion unit that contains a slurry catalyst capable of activating molecular hydrogen; an optional hydrogen feed line that is operatively connected to the hydrothermal digestion unit; and a fluid circulation loop comprising the hydrothermal digestion unit and a catalytic reduction reactor unit, the catalytic reduction reactor unit also containing the slurry catalyst. 1. A biomass conversion system comprising:a hydrothermal digestion unit that contains a slurry catalyst capable of activating molecular hydrogen;an optional hydrogen feed line that is operatively connected to the hydrothermal digestion unit; anda fluid circulation loop comprising the hydrothermal digestion unit and a catalytic reduction reactor unit, the catalytic reduction reactor unit also containing the slurry catalyst.2. The biomass conversion system of claim 1 , wherein the fluid circulation loop is configured to establish upward fluid flow in the hydrothermal digestion unit.3. The biomass conversion system of claim 1 , further comprising:a retention mechanism within the hydrothermal digestion unit that is operable to retain cellulosic biomass solids having a particle size of about 3 mm or above.4. The biomass conversion system of claim 1 , further comprising:a reaction product takeoff line in fluid communication with the fluid circulation loop, the reaction product takeoff line being located between the hydrothermal digestion unit and an outlet of the catalytic reduction reactor unit.5. The biomass conversion system of claim 4 , further comprising:a solids separation mechanism that is operatively ...

Integrated Oil Production and Upgrading Using Molten Alkali Metal

A method that combines the oil retorting process (or other process needed to obtain/extract heavy oil or bitumen) with the process for upgrading these materials using sodium or other alkali metals. Specifically, the shale gas or other gases that are obtained from the retorting/extraction process may be introduced into the upgrading reactor and used to upgrade the oil feedstock. Also, the solid materials obtained from the reactor may be used as a fuel source, thereby providing the heat necessary for the retorting/extraction process. Other forms of integration are also disclosed. 1. A method for upgrading an oil feedstock comprising:retorting oil shale to produce shale oil and shale gas;upgrading the shale oil using an alkali metal, wherein shale gas obtained from the retorting step is used as the reactant gas in the upgrading step.2. The method of claim 1 , wherein the shale gas comprises a quantity of hydrogen sulfide claim 1 , wherein the hydrogen sulfide is added to the shale oil during the upgrading step.3. The method of claim 1 , wherein the upgrading step produces a solid material containing organic matter claim 1 , wherein this solid material is used to provide heat during the retorting step.4. The method of claim 1 , wherein the upgrading step produces a solid material containing organic matter claim 1 , wherein this solid material is used as a feedstock in the retorting step.5. The method of claim 1 , wherein the upgrading step produces a solid material containing organic matter claim 1 , wherein this solid material is used during the retorting step.6. The method of claim 1 , wherein the upgrading step produces products a solid material claim 1 , wherein the solid material is used produce power for an electrolytic regeneration of the alkali metal.7. A method for upgrading a heavy oil or bitumen from oil sands comprisingheating the oil sands to cause the heavy oil or bitumen to flow, wherein a gas is also produced by this heating;upgrading the heavy oil or ...

BIOMASS CONVERSION SYSTEMS CONTAINING A MOVING BED CATALYST FOR STABILIZATION OF A HYDROLSATE AND METHODS FOR USE THEREOF

Digestion of cellulosic biomass solids to form a hydrolysate may be conducted with in situ catalytic reduction to transform soluble carbohydrates in the hydrolysate into a more stable reaction product. Biomass conversion systems for performing such a transformation can comprise: a hydrothermal digestion unit that also contains a first catalyst capable of activating molecular hydrogen, the first catalyst being fluidly mobile within the hydrothermal digestion unit; an optional hydrogen feed line that is operatively connected to the hydrothermal digestion unit; a fluid circulation loop comprising the hydrothermal digestion unit and a catalytic reduction reactor unit that contains a second catalyst capable of activating molecular hydrogen; and a catalyst transport mechanism external to the hydrothermal digestion unit, the catalyst transport mechanism being capable of conveying at least a portion of the first catalyst to another location from a catalyst collection zone located within the hydrothermal digestion unit. 1. A biomass conversion system comprising:a hydrothermal digestion unit that also contains a first catalyst capable of activating molecular hydrogen, the first catalyst being fluidly mobile within the hydrothermal digestion unit;an optional hydrogen feed line that is operatively connected to the hydrothermal digestion unit;a fluid circulation loop comprising the hydrothermal digestion unit and a catalytic reduction reactor unit that contains a second catalyst capable of activating molecular hydrogen; anda catalyst transport mechanism external to the hydrothermal digestion unit, the catalyst transport mechanism being capable of conveying at least a portion of the first catalyst to another location from a catalyst collection zone located within the hydrothermal digestion unit.2. The biomass conversion system of claim 1 , wherein at least a portion of the first catalyst is non-buoyant in a fluid phase.3. The biomass conversion system of claim 1 , wherein the ...

METHODS, SYSTEMS, AND DEVICES FOR CONTINUOUS LIQUID FUEL PRODUCTION FROM BIOMASS

Methods, systems, and devices for continuous production of liquid fuels from biomass are provided. Some embodiments utilize a thermochemical process to produce a bio-oil in parallel with a thermochemical process to produce a hydrogen-rich synthesis gas. Both product streams may be fed into a third reaction chamber that may enrich the bio-oil with the hydrogen gas, for example, in a continuous production process. One product stream may include a liquid fuel such as diesel. Some embodiments may also produce other product streams including, but not limited to, electrical power generation and/or biochar. 1. A method of continuous liquid fuel production utilizing biomass , the method comprising:receiving one or more biomass feedstocks;utilizing a first portion of the one or more biomass feedstocks to produce synthesis gas from a first thermochemical process;utilizing a second portion of the one or more biomass feedstocks to produce bio-oil from a second thermochemical process; andgenerating a liquid fuel through combining the produced synthesis gas and the produced bio-oil.2. The method of claim 1 , wherein the first thermochemical process comprises:combining water with the first portion of the one or more biomass feedstocks to from a wet biomass feedstock;transferring the wet biomass feedstock to a reaction chamber; andheating the wet biomass feedstock within the reaction chamber such that the elements comprised by the wet biomass feedstock dissociate and react to form at least the synthesis gas.3. The method of claim 2 , where the elements comprises by the wet biomass feedstock dissociate and react through a non-oxidation reaction to form at least the synthesis gas.4. The method of claim 3 , wherein the non-oxidation reaction comprises a hydrous pyrolysis reaction.5. The method of claim 1 , wherein the synthesis gas comprises hydrogen gas.6. The method of claim 1 , wherein the one or more biomass feedstocks comprises at least cellulose claim 1 , lignin claim 1 , or ...

SYSTEM FOR MAKING RENEWABLE FUELS INCLUDING GASOLINE, DIESEL, AND JET FUEL

Multiple catalytic processing stations coupled with a system which produces volatile gas streams from biomass decomposition at discrete increasing temperatures or constant temperature. These catalytic processing stations can be programmed to maximize conversion of biomass to jet fuel components. The system may also include a processing station for subjecting biomass within the stations to at least one programmable starting temperature (T) and for incrementing an individual processing station temperature by programmable increments (ΔT) to produce a volatile and a non-volatile component. Further, methods for converting biomass and char to renewable jet fuel, diesel, and kerosene are disclosed. 1. A system for the conversion of biomass to diesel or jet fuel , comprising:a device containing a number of processing stations (N) and a series of catalysts;{'sub': 'start', 'each processing station capable of subjecting biomass within the station to at least one starting temperature (T) to produce a volatile and a non-volatile component;'}at least one catalyst reactor for receiving volatile components generated in each processing station; andwherein, the at least one catalyst reactor contains a catalyst selected from the group consisting of: dehydration catalysts, olefin oligomerization catalysts and hydrotreating catalysts.2. The system of claim 1 , further comprising additional catalyst reactors.3. The system of claim 2 , wherein the additional catalyst reactors are used in series.4. The system of claim 2 , wherein the additional catalyst reactors are used in parallel.5. The system of claim 1 , further comprising a temperature controller for incrementing an individual processing station temperature by increments (ΔT).6. The system of claim 1 , wherein the non-volatile component is a carbonaceous material.7. The system of claim 1 , further comprising a gasifier for converting the carbonaceous material to syngas.8. The system of claim 7 , further comprising a conduit from the ...

Rotating Fluidized Bed Catalytic Pyrolysis Reactor

Reactors for the pyrolysis of pyrolyzable matter, pyrolysis systems incorporating the reactors and methods of using the reactors are provided. Also provided are systems and methods for integrating the pyrolysis and hydrodeoxygenation of pyrolyzable matter. The pyrolysis reactors create a horizontally rotating, fluidized-bed to which pyrolyzable matter, such as biomass, may be converted via pyrolysis into liquid fuels and/or value-added chemicals. 1. A reactor for pyrolysis comprising:a horizontal, rotatable reactor drum comprising an annular wall disposed around a horizontal axis, wherein the annular wall is permeable to particulate material;a rotation drive connected to the rotatable reactor drum and configured to rotate the rotatable reactor drum about the horizontal axis;a feed conduit configured to transport pyrolyzable matter from a source of pyrolyzable matter into the rotatable reactor drum; anda reaction chamber in which the rotatable reactor drum and at least a portion of the feed conduit are housed.2. The reactor of claim 1 , wherein the annular wall defines a plurality of holes that extend through the annular wall claim 1 , the holes having diameters in the range from about 0.5 to about 30 mm.3. The reactor of claim 1 , wherein the reaction chamber forms an annular space around the rotatable reactor drum and at least a portion of the feed conduit claim 1 , and further wherein the annular space is in fluid communication with the rotatable reactor drum claim 1 , such that vapor-phase pyrolysis products formed in the rotatable reactor drum are able to flow into the annular space.4. The reactor of claim 1 , further comprising a radiation source disposed within the rotatable reactor drum and configured to emit radiation toward the annular wall.5. The reactor of claim 4 , wherein the radiation source emits ultraviolet radiation.6. The reactor of claim 1 , further comprising:a product collection chamber, the product collection chamber comprising an input port ...

PYROLYSIS VAPOR RAPID FILTRATION AND CONVERSION TO FUEL

The present disclosure pertains to biomass pyrolysis processes and systems that decrease entrainment of char and other contaminants in the pyrolysis vapors by filtering the vapors in a heated container comprising a moving bed granular filter (MBGF), which in turn, comprises granular heat carrier. The granular heat carrier is heated within the MBGF and fed directly to the pyrolysis reactor, optionally along with filtered solids such as char. In certain embodiments, the MBGF additionally comprises at least one upgrading catalyst that contacts the vapors to produce a hydrocarbon mixture fungible with a petroleum-derived transportation fuel, a hydrocarbon transportation fuel component, or mixtures thereof. 1. A biomass pyrolysis process , comprising the steps of:(a) providing a heated container that encloses a moving bed granular filter, wherein the moving bed granular filter comprises a granular heat carrier;(b) heating the granular heat carrier in the heated container to produce a heated granular heat carrier that is conveyed to a pyrolysis reactor;(c) pyrolyzing a biomass feedstock in the pyrolysis reactor to produce pyrolysis vapors comprising a residual amount of entrained char particles, wherein rapid heating of the biomass feedstock is facilitated by contact with the heated granular heat carrier;(d) conveying the pyrolysis vapors out of the pyrolysis reactor and through the moving bed granular filter to separate at least a portion of the residual entrained char particles, thereby producing low-particulate pyrolysis vapors and a solid stream comprising char and the heated granular heat carrier of step (a).2. The process of claim 10 , further comprising contacting the low-particulate upgraded pyrolysis vapors with at least one upgrading catalyst within the heated container to produce a hydrocarbon mixture fungible with a petroleum-derived transportation fuel or a component thereof.3. The process of claim 1 , further comprising contacting the low-particulate ...

FIELD REPLACEABLE MULTIFUNTIONAL CARTRIDGE FOR WASTE CONVERSION INTO FUEL

Disclosed herein is a field replaceable multifunction cartridge for the conversion of composite high molecular weight hydrocarbon vapours, extracted from homogenous or heterogeneous, segregated or unsegregated, wet or dry, unclean miscellaneous multi-feed waste input, to produce low molecular weight fractions of industriously combustible fuel products through catalytic cracking. The multifunction cartridge system is constructed in a modular fashion is capable of performing the catalytic, cleaning and scrubbing functions through the temperature range ranging from ambient to 500° C., owing to the high mechanical strength, low coefficient of expansion, resistance to thermal fatigue etc. 2020203040105. A field replaceable multifunctional cartridge () as claimed in claim 1 , wherein claim 1 , the said cartridge () is arranged in a plurality of rows () claim 1 , each of the said rows consisting of a plurality of cartridges () enclosed in tubes ( and ) connected in parallel between a common inlet valve () and an common outlet valve ().3080810110709. A field replaceable multifunctional cartridge as claimed in claim 2 , wherein claim 2 , each of said tubes () contain the field replaceable multifunctional cartridge () between said motorized inlet valve () and motorized outlet valve () claim 2 , monitored by inlet pressure sensor () and outlet pressure sensor () claim 2 , wherein claim 2 , said valves are hydraulically or pneumatically or electrically controlled by microprocessors.407091011. A field replaceable multifunctional cartridge as claimed in claim 3 , wherein said inlet pressure sensor () and outlet pressure sensor () monitor change in pressure at said motorized inlet valve () and motorized outlet valve () caused by contamination of said catalyst bed.51011. A field replaceable multifunctional cartridge as claimed in claim 4 , wherein claim 4 , said motorized inlet valve () and motorized outlet valve () are enabled to shut down in case of any malfunctioning due to ...

SYSTEM AND METHOD FOR MAKING RENEWABLE FUELS

Multiple catalytic processing stations enable a method for producing volatile gas streams from biomass decomposition at discrete increasing temperatures. These catalytic processing stations can be programmed to maximize conversion of biomass to useful renewable fuel components based on input feedstock and desired outputs. 1. A method for converting biomass to renewable fuels , comprising:providing a system containing a number of processing stations (N) in communication with a series of catalysts;heating a biomass within the stations at a starting temperature (Tstart) to produce a volatile and a non-volatile component, said biomass and said heating selected to provide volatile components of a predetermined composition; andsubjecting the volatile components of a predetermined composition generated in at least one station through the series of catalysts to produce at least one renewable fuel.2. The method of claim 1 , wherein said series of catalysts is selected based on said starting temperature.3. The method of claim 1 , wherein said series of catalyst is based on the biomass composition.4. The method of claim 3 , wherein the biomass is a lipid-rich biomass and the volatile components from the lipid-rich biomass is contacted with a dehydration catalyst to produce a product which on cooling to a temperature range of 1-20° C. produces a second volatile component claim 3 , a first renewable fuel and water.5. The method of claim 3 , wherein the biomass is a hemicellulose-rich biomass and a volatile components from the hemicellulose-rich biomass is contacted directly with an aromatization catalyst to produce a product which on cooling to a temperature of 0-5° C. produces a second volatile component claim 3 , a first renewable fuel and water.6. The method of claim 3 , wherein the biomass is a lignin-rich biomass and the volatile component from the lignin-rich biomass is contacted with a dehydration catalyst to produce a product which on cooling to 2-20° C. produces a ...

BIOMASS CONVERSION SYSTEMS HAVING A SINGLE-VESSEL HYDROTHERMAL DIGESTION UNIT/CATALYTIC REDUCTION REACTOR UNIT FOR INTEGRATED STABILIZATION OF A HYDROLYSATE AND METHODS FOR USE THEREOF

Digestion of cellulosic biomass solids may be conducted in a pressure vessel that contains both a hydrothermal digestion unit and a catalytic reduction reactor unit. Biomass conversion systems incorporating such a feature may comprise: a pressure vessel that comprises a first section comprising a hydrothermal digestion unit and a second section comprising a first catalytic reduction reactor unit that contains a first catalyst capable of activating molecular hydrogen; wherein the hydrothermal digestion unit and the first catalytic reduction reactor unit are in fluid communication with one another; a biomass feed mechanism that is operatively connected to the pressure vessel, the biomass feed mechanism being capable of introducing cellulosic biomass solids to the pressure vessel and also capable of withdrawing a reaction product from the first catalytic reduction reactor unit; and a hydrogen feed line that is operatively connected to the first catalytic reduction reactor unit. 1. A biomass conversion system comprising: 'wherein the hydrothermal digestion unit and the first catalytic reduction reactor unit are in fluid communication with one another;', 'a pressure vessel comprising a first section and a second section, the first section comprising a hydrothermal digestion unit and the second section comprising a first catalytic reduction reactor unit that contains a first catalyst capable of activating molecular hydrogen;'}a biomass feed mechanism that is operatively connected to the pressure vessel, the biomass feed mechanism being capable of introducing cellulosic biomass solids to the pressure vessel and also capable of withdrawing a reaction product from the first catalytic reduction reactor unit; anda hydrogen feed line that is operatively connected to the first catalytic reduction reactor unit.20. The biomass conversion system of claim , wherein the pressure vessel comprises an annular structure , with the first section comprising an outer portion of the annular ...

PROCESS FOR LIQUEFYING A CELLULOSIC MATERIAL

A process for liquefying a cellulosic material to produce a liquefied product comprising contacting the cellulosic material with a hydrogenation catalyst a liquid medium; and a source of hydrogen. The hydrogenation catalyst comprises a hydrogenating metal or precursor thereof and a megaporous structure, wherein the megaporous structure comprises a porosity of at least 60% by volume and at least 30 volume % of the pore volume of the megaporous structure is present in megapores having a diameter of equal to or more than 1 micrometer. 1. A process comprising:contacting a cellulosic material with a hydrogenation catalyst, a liquid medium; and a source of hydrogen;wherein the hydrogenation catalyst comprises a hydrogenating metal or precursor thereof and a megaporous structure,wherein the megaporous structure comprises a porosity of at least 60% by volume; andwherein at least 30 volume % of the pore volume comprises a plurality of pores having a diameter of equal to or more than 1 micrometer.2. The process of wherein the contacting step comprises:contacting the cellulosic material in the liquid medium with the hydrogenation catalyst in a fixed bed.3. The process of claim 1 , wherein the megaporous structure is a monolitic foam or honeycomb.4. The process of claim 1 , wherein the hydrogenation catalyst comprises a hydrogenating metal and/or precursor thereof carried on a graphite sheet having a porosity of at least 60% by volume and at least 30 volume % of the pore volume comprises a plurality of pores having a pore size of at least 1 micrometer.5. The process of claim 1 , wherein the hydrogenation metal is selected from the group consisting of iron claim 1 , cobalt claim 1 , nickel claim 1 , copper ruthenium claim 1 , rhodium claim 1 , palladium claim 1 , iridium claim 1 , platinum claim 1 , gold claim 1 , and any combination thereof6. The process of claim 1 , wherein the megaporous structure comprises an inorganic metal oxide.7. The process of claim 1 , wherein at least ...

Process for producing liquid hydrocarbon

The invention relates to a continuous process for converting carbonaceous material contained in one or more feedstocks into a liquid hydrocarbon product, said feedstocks including the carbonaceous material being in a feed mixture including one or more fluids, said fluids including water and further liquid organic compounds at least partly produced by the process in a concentration of at least 1% by weight, where the process comprises converting at least part of the carbonaceous material by pressurising the feed mixture to a pressure in the range 50-400 bar, heating the feed mixture to a temperature in the range 250-500° C., and maintaining said pressurized and heated feed mixture in the desired pressure and temperature ranges in a reaction zone for a predefined time; cooling the feed mixture to a temperature in the range 25-200° C. and expanding the feed mixture to a pressure in the range of 1-70 bar, thereby causing the carbonaceous material to be converted to a liquid hydrocarbon product; separating a fraction comprising liquid hydrocarbon product, and leaving a residual fraction; feeding said residual fraction into a bioreactor for the production of biomass such as algae and/or bacteria such as cyano bacteria.

DIRECT PRODUCTION OF FRACTIONATED AND UPGRADED HYDROCARBON FUELS FROM BIOMASS

Multistage processing of biomass to produce at least two separate fungible fuel streams, one dominated by gasoline boiling-point range liquids and the other by diesel boiling-point range liquids. The processing involves hydrotreating the biomass to produce a hydrotreatment product including a deoxygenated hydrocarbon product of gasoline and diesel boiling materials, followed by separating each of the gasoline and diesel boiling materials from the hydrotreatment product and each other. 1. A process for producing hydrocarbon fuels from biomass , the process comprising: hydropyrolyzing the biomass in a reactor containing molecular hydrogen and a deoxygenating and hydrogen addition catalyst at hydropyrolysis reaction conditions to produce a deoxygenated hydrocarbon hydropyrolysis product comprising char and vapors;', 'separating substantially all of said char and particles from said deoxygenated hydrocarbon hydropyrolysis product to produce a substantially char and particle-free hydropyrolysis product;, '(a) hydrotreating biomass at hydrotreatment reaction conditions to produce a hydrotreatment product comprising a deoxygenated hydrocarbon product including gasoline and diesel boiling-point range materials, said hydrotreating comprising(b) separating each of said gasoline and diesel boiling-point range fractions from said hydrotreatment product and each other;(c) separating said gasoline boiling-point range materials from said diesel boiling-point range fractions;(d) upgrading said separated gasoline and diesel boiling-point range fractions.2. The process of wherein said separated gasoline boiling-point range fraction is catalytically upgraded at catalytic gasoline upgrade conditions to form an upgraded gasoline product.3. The process of wherein said separated diesel boiling-point range fraction is treated to produce an ultra-low sulfur diesel product.4. The process of wherein the treatment of the separated diesel boiling-point range fraction to produce an ultra-low ...

FORMATE-ASSISTED PYROLYSIS

The present invention provides, among other thing, methods for creating significantly deoxygenated bio-oils form biomass including the steps of providing a feedstock, associating the feedstock with an alkali formate to form a treated feedstock, dewatering the treated feedstock, heating the dewatered treated feedstock to form a vapor product, and condensing the vapor product to form a pyrolysis oil, wherein the pyrolysis oil contains less than 30% oxygen by weight. 1. A method comprisingproviding a feedstock;associating the feedstock with an alkali formate to form a treated feedstock;dewatering the treated feedstock;heating the dewatered treated feedstock to form a vapor product; andcondensing the vapor product to form a pyrolysis oil;wherein the pyrolysis oil contains less than 30% oxygen by weight.2. The method of claim 1 , wherein the feedstock is selected from the group consisting of cellulosic biomass claim 1 , wood claim 1 , wood waste claim 1 , lignin claim 1 , spent pulping/fractionation liquors claim 1 , algal biomass claim 1 , food waste claim 1 , sludges and municipal solid waste claim 1 , and mixtures thereof.3. The method of claim 1 , wherein the alkali formate is selected from the group consisting of calcium formate claim 1 , magnesium formate claim 1 , sodium formate claim 1 , potassium formate claim 1 , lithium formate claim 1 , zinc formate claim 1 , and mixtures thereof.4. The method of claim 1 , wherein the dewatered treated feedstock is heated to between about 200° C. and about 600° C.5. The method of claim 1 , wherein the dewatered treated feedstock is heated to between about 375° C. and about 500° C.6. The method of claim 1 , wherein the dewatered treated feedstock is heated for between about one second and about four hours.7. The method of claim 1 , wherein at least one of the associating claim 1 , dewatering claim 1 , heating and condensing steps is carried out at a pressure between about vacuum and about 10 bar.8. A method comprisingproviding ...

HYDROPYROLYSIS OF BIOMASS-CONTAINING FEEDSTOCKS

Various techniques are disclosed for pretreating municipal solid waste (MSW) and other biomass-containing feedstocks that may be of a poorer quality and consequently more difficult, or even impossible, to convert to higher value liquid products (e.g., transportation fuels) using conventional processes. Such conventional processes may otherwise be satisfactory for the conversion of the biomass portion of the feedstock alone. The pretreatment of biomass-containing feedstocks may generally include steps carried out prior to a hydropyrolysis step and optionally further steps, in order to change one or more characteristics of the feedstock, rendering it more easily upgradable. 1. A process for producing liquid products from a biomass-containing feedstock comprising the steps of:a) devolatilizing the feedstock in a pre-reactor vessel containing hydrogen and a solid bed material selected from the group consisting of a pretreating catalyst, a sorbent, a heat transfer medium, and mixtures thereof, to produce a pre-reactor vapor stream comprising entrained solid particles; andb) hydropyrolyzing at least a portion of the pre-reactor vapor stream in a hydropyrolysis reactor vessel containing hydrogen and a deoxygenating catalyst, producing a hydropyrolysis reactor output comprising at least one non-condensable gas, a partially deoxygenated hydropyrolysis product and char particles.2. The process of claim 1 , further comprising:c) removing substantially all of the char particles from the hydropyrolysis reactor output to provide a purified hydropyrolysis reactor vapor stream having a reduced char content; andd) hydroconverting at least a portion of the purified hydropyrolysis reactor vapor stream in a hydroconversion reactor vessel containing hydrogen and a hydroconversion catalyst, producing a hydroconversion reactor output; ande) recovering a substantially fully deoxygenated hydrocarbon liquid and a gaseous mixture from the hydroconversion reactor output.3. The process of claim ...

SYSTEMS FOR FUELS FROM BIOMASS

The present application generally relates to a system to prepare a fuel from a biomass and a petroleum fraction wherein a renewable fuel oil is obtained via pyrolysis, delivered to the injection point of a refinery system, and then co-processed with a petroleum fraction in the presence of a catalyst. 1. A system to prepare a fuel from a biomass and a petroleum fraction , comprising:a pyrolysis system for producing a renewable fuel oil from the biomass;a refinery system comprising a conversion unit to co-process the renewable fuel oil and the petroleum fraction as reactants in the presence of a catalyst;a delivery system to deliver the renewable fuel oil to an injection point of the conversion unit; anda control system to control the delivery of renewable fuel oil to the refinery system.2. The system of claim 1 , wherein the pyrolysis system is a rapid thermal processing system producing an unenriched renewable fuel oil.3. The system of claim 1 , wherein the pyrolysis system is co-located with the refinery system.4. The system of claim 1 , wherein the conversion unit comprises a fluidized catalytic cracker.5. The system of claim 4 , wherein the fluidized catalytic cracker comprises a retro-fitted fluidized catalytic cracker.6. The system of claim 5 , further comprising one or more modified injection ports through which the renewable fuel oil is injected into a riser of the fluidized catalytic cracker.7. The system of claim 6 , wherein at least one of the one or more modified injection ports comprises a modified nozzle.8. The system of claim 1 , wherein the conversion unit comprises a hydrotreating unit or a hydrocracking unit.9. The system of claim 1 , wherein the delivery system delivers 0.05-20 wt. % renewable fuel oil as a percentage of reactants.10. The system of claim 1 , wherein the delivery system comprises a storage tank and a pre-heater.11. The system of claim 1 , wherein the control system monitors and adjusts the addition of renewable fuel oil so as to ...

METHODS FOR REMOVING CONTAMINANTS FROM OILS USING BASE WASHING AND ACID WASHING

Methods for processing algal oils are provided. In an embodiment, a method for removing a contaminant from an oil includes contacting the oil with a base to form an intermediate solution. Further, the method includes contacting the intermediate solution with an acid to form an acidic solution. The method separates the acidic solution into an oil portion and an aqueous waste portion including the contaminant. 1. A method for removing a contaminant from an oil , the method comprising the steps of:contacting the oil with a base to form an intermediate solution;contacting the intermediate solution with an acid to form an acidic solution; andseparating the acidic solution into an oil portion and an aqueous waste portion, wherein the aqueous waste portion includes the contaminant.2. The method of wherein contacting the oil with a base to form an intermediate solution comprises mixing equal amounts of the oil and a 2% basic solution.3. The method of wherein contacting the oil with a base to form an intermediate solution comprises mixing the oil and a basic solution to form a cloudy solution including soap claim 1 , and wherein the method further comprises agitating the cloudy solution for a selected time period.4. The method of wherein contacting the intermediate solution with an acid to form an acidic solution comprises mixing the intermediate solution with an acid to form an acidic solution having a pH of no more than about 2.5. The method of wherein the intermediate solution is cloudy and includes soap claim 1 , and wherein contacting the intermediate solution with an acid to form an acidic solution comprises mixing the intermediate solution with an acid to form a clear acidic solution and soap solids.6. The method of wherein separating the acidic solution into an oil portion and an aqueous waste portion comprises separating the acidic solution by centrifugation.7. The method of further comprising separating aqueous waste from the intermediate solution before contacting ...

Integrated Coal To Liquids Process With Co2 Mitigation Using Algal Biomass

An ICBTL system and method having a low GHG footprint for converting coal or coal and biomass to liquid fuels and a biofertilizer in which a carbon-based feed is converted to liquids by direct liquefaction and optionally by indirect liquefaction and the liquids are upgraded to produce premium fuels. COproduced by the process is used to a produce cyanobacteria containing algal biomass and other photosynthetic microorganisms in a photobioreactor. Optionally, lipids extracted from the some of the algal biomass is hydroprocessed to produce fuel components and biomass residues and the carbon-based feed our gasified to produce hydrogen and syngas for the direct and indirect liquefaction processes. Some or all of the algal biomass and photosynthetic microorganisms are used to produce a natural biofertilizer. COmay also be produced by a steam methane reformer for supplying COto produce the algal biomass and photosynthetic microorganisms. 1. A method converting a coal containing solid carbonaceous material to liquid fuels and cyanobacteria based biofertilizer , comprising the steps of:{'sub': '2', 'a. directly liquefying a coal containing solid carbonaceous material by subjecting said material to elevated temperatures and pressures in the presence of a solvent and a molybdenum containing catalyst for a time sufficient for producing hydrocarbon liquids and byproduct CO;'}b. upgrading hydrocarbon liquids produced by step a to liquid fuels and byproduct ammonia;{'sub': '2', 'c. producing hydrogen and byproduct COfrom a carbonaceous feed, and supplying at least a portion of said hydrogen as inputs to said direct liquefaction and said upgrading steps;'}{'sub': '2', 'd. reproducing a soil-based, nitrogen fixing cyanobacteria containing inoculant in a photobioreactor with the use of byproduct COproduced by one or both of said direct liquefaction and hydrogen producing steps and ammonia produced by said upgrading step; and'}e. producing a biofertilizer incorporating said inoculant.2 ...

RELATING TO COAL TO LIQUID PROCESSES

A method of increasing the hydrogen/carbon monoxide (H/CO) ratio in a syngas stream derived from a carbonaceous fuel including coal, brown coal, peat, and heavy residual oil fractions, preferably coal. The fuel-derived syngas stream is divided into at least two sub-streams, one of which undergoes a catalytic water shift conversion reaction. The so-obtained converted sub-stream is combined with the non-converted sub-stream(s) to form a second syngas stream with an increased H/CO ratio. The method of the present invention can provide a syngas with a H/CO ratio more suitable for efficient hydrocarbon synthesis carried out on a given catalyst, such as in one or more Fischer-Tropsch reactors, as well as being able to accommodate variation in the H/CO ratio of syngas formed from different qualities of feedstock fuels. 1. A process for the preparation of hydrogen-enriched fuel-derived syngas derived from a carbonaceous fuel , comprising:providing a fuel-derived syngas stream;dividing the fuel-derived syngas stream into at least two sub-streams;letting one of the at least two sub-streams undergo a catalytic water shift conversion reaction followed by passing the converted stream through a carbon dioxide/hydrogen sulphide removal system to obtain a converted and cleaned sub-stream;passing the other stream(s) through a carbon dioxide/hydrogen sulphide removal system to obtain a cleaned non-converted sub-stream(s);{'sub': '2', 'combining the obtained converted and cleaned sub-stream with the cleaned non-converted sub-stream(s) to form a hydrogen-enriched fuel-derived syngas stream having an increased H/CO ratio of between 1.4 and 1.95.'}2. The process of claim 1 , wherein the H/CO ratio in the fuel-derived syngas stream is less than 1.3. The process of claim 1 , wherein the H/CO ratio in the hydrogen-enriched fuel-derived syngas stream is greater than 1.5.4. The process of claim 1 , wherein the H/CO ratio in the hydrogen-enriched fuel-derived syngas stream is in the range 1.6- ...

METHODS AND SYSTEMS FOR PROCESSING LIGNIN THROUGH VISCOSITY REDUCTION DURING HYDROTHERMAL DIGESTION OF CELLULOSIC BIOMASS SOLIDS

Digestion of cellulosic biomass solids may be complicated by lignin release therefrom, which can produce a highly viscous phenolics liquid phase comprising lignin polymer. Systems for processing a phenolics liquid phase comprising lignin polymer may comprise: a hydrothermal digestion unit; a viscosity measurement device within the hydrothermal digestion unit or in flow communication with the hydrothermal digestion unit; a temperature control device within the hydrothermal digestion unit or in flow communication with the hydrothermal digestion unit; and a processing device communicatively coupled to the viscosity measurement device and the temperature control device, the processing device being configured to actuate the temperature control device if the viscosity of a fluid phase comprising lignin exceeds a threshold value in the biomass conversion system. 1. A method comprising: a hydrothermal digestion unit;', 'a viscosity measurement device within the hydrothermal digestion unit or in flow communication with the hydrothermal digestion unit;', 'a temperature control device within the hydrothermal digestion unit or in flow communication with the hydrothermal digestion unit, the temperature control device configured to control a temperature in the hydrothermal digestion unit; and', 'a processing device communicatively coupled to the viscosity measurement device and the temperature control device;, 'providing a biomass conversion system comprisingproviding the hydrothermal digestion unit with cellulosic biomass solids in the presence of a digestion solvent, molecular hydrogen, and a slurry catalyst capable of activating molecular hydrogen;heating the cellulosic biomass solids to a temperature of at least 150 degrees C. to form a reaction product comprising a fluid phase comprising lignin, an aqueous phase comprising an alcoholic component derived from the cellulosic biomass solids, and an optional light organics phase;measuring a viscosity of the fluid phase ...

BIOMASS CONVERSION PROCESS TO HYDROCARBONS

A process for the production of a higher hydrocarbon useful to produce diesel components from solid biomass is provided. The process provides for improved production of diesel components by contacting the stable oxygenated hydrocarbon intermediate containing diols produced from digestion and hydrodoxygenation of the solid biomass to an amorphous silica alumina catalyst to reduce the diols content, and removing water prior to contacting with the condensation catalyst to produce the higher hydrocarbon. 1. A process for the production of a higher hydrocarbon from solid biomass , said process comprising:a. providing a biomass solid containing cellulose, hemicellulose, and lignin;b. digesting and hydrodeoxygenating the biomass solid in a liquid digestive solvent, said digestive solvent containing a solvent mixture having a boiling point of at least 40° C. in the presence of a hydrothermal hydrocatalytic catalyst in the presence of hydrogen at a temperature in the range of from 110° C. to less than 300° C. at a pressure in a range of from 20 bar to 200 bar to form a stable oxygenated hydrocarbon intermediate product having a viscosity of less than 100 centipoise (at 50° C.), a diol content of at least 2 wt %, less than 2wt % of sugar, and less than 2wt % acid (based on acetic acid equivalent), based on the intermediate product, and at least 60% of carbon exists in molecules having 9 carbon atoms or less;c. reacting at least a portion of the stable oxygenated hydrocarbon intermediate product with an acidic amorphous silica alumina catalyst at a temperature in the range from 300° C. to 400° C. thereby producing monooxygenated stream containing water and monooxygenates having a boiling point of at least 40° C.;d. condensing the monooxygenated stream to liquid phase producing an aqueous phase and an organic phase;e. removing at least a portion of aqueous phase from the organic phase to provide a condensed organic stream containing the monooxygenates;f. contacting the ...

Combined Hydrothermal Liquefaction and Catalytic Hydrothermal Gasification System and Process for Conversion of Biomass Feedstocks

A combined hydrothermal liquefaction (HTL) and catalytic hydrothermal gasification (CHG) system and process are described that convert various biomass-containing sources into separable bio-oils and aqueous effluents that contain residual organics. Bio-oils may be converted to useful bio-based fuels and other chemical feedstocks. Residual organics in HTL aqueous effluents may be gasified and converted into medium-BTU product gases and directly used for process heating or to provide energy. 119-. (canceled)20. A continuous biomass conversion process , comprising the steps of:providing a biomass conversion product comprising a bio oil fraction and an aqueous fraction, wherein each fraction is separable from the other fraction;without the aid of gravitational separation, continuously separating the bio oil fraction from the aqueous fraction; andconverting at least a portion of the aqueous fraction to a product gas containing a fuel gas.21. The process of claim 20 , wherein prior to continuously separating the bio oil fraction from the aqueous fraction claim 20 , further comprising removing solids from the biomass conversion product.22. The process of claim 20 , further comprising combusting the product gas to generate power.23. The process of claim 20 , wherein the product gas comprises one or more of methane claim 20 , hydrocarbons with a carbon number greater than that of methane claim 20 , and carbon dioxide claim 20 , wherein the product gas optionally comprises less than 5% hydrogen by weight.24. A continuous biomass conversion process claim 20 , comprising the steps of:providing a biomass conversion product comprising a bio oil fraction and an aqueous fraction, wherein each fraction is separable from the other fraction;using centrifugal force, continuously separating the bio oil fraction from the aqueous fraction; andconverting at least a portion of the aqueous fraction to a product gas containing a fuel gas.25. The process of claim 24 , wherein the separation is ...

A COAL AND OIL CO-HYDROTREATING PROCESSING TECHNOLOGY AND EQUIPMENT

An oil-coal co-hydrotreating processing includes the following steps: pulverized coal, vacuum residue and recycle oil are mixed to prepare coal slurry. After mixed with hydrogen, catalyst and additive, oil-coal slurry is preheated into a slurry bed reactor with high reacting pressure for thermal cracking and hydrogenation reaction. After reaction, all the products go into the hot high pressure separator for separation of solid from the bottom and gas from the top. The gas obtained goes into the fixed bed reactor for further hydrocracking or refining, and the distillate obtained enter the fractionating tower. The vacuum gas oil from the bottom of fractionating tower is taken as recycle oil piped to the oil-coal slurry mixing device as solvent. 1. A oil-coal co-hydrotreating processing technology , characterized as the following steps:first of all, pulverizing the coal and drying, wherein the pulverized coal is mixed with one or several of crude oil, atmospheric residue, vacuum residue, FCC slurry oil, deasphalted oil, vacuum gas oil, coal tar in the coal and oil mixing and pulping device to prepare oil-coal slurry; after mixed with hydrogen, catalyst and additive, the oil-coal slurry is preheated into a slurry bed reactor with reacting pressure for thermal cracking and hydrogenation reaction; the coke, asphaltene and heavy metals are adsorbed on the catalyst, additives and unreacted coal in the reaction process; after reaction, all the products go into the hot high pressure separator for separation of solid from the bottom and gas from the top, and the gas goes into the fixed bed reactor for further hydrocracking or refining; distillate obtained enters the fractionating tower, and bottom vacuum gas oil is recycled to the coal and oil mixing and pulping device; wherein the catalyst is a mixture of molybdate and iron, the additive is a sulfurizing reagent, and the reaction pressure in the slurry bed reactor is in the range of 17-20 MPa.2. A oil-coal co-hydrotreating ...

PROCESSING COMBUSTIBLE MATERIAL METHODS AND SYSTEMS

Methods, systems and units for liquefaction of combustible material are provided. After separating the combustible material from waste rock gravitationally in an aqueous salt solution selected to have a density which is intermediate between a density of the combustible material and a density of the waste rock and after heating and grinding the separated combustible material to yield a paste of purified combustible material, the paste is fluidizing and hydrogenated underground in a hydrogenation chamber including a Segner turbine. The described processes significantly reduce the energy consumption of the process, remove environmental hazards and result in more efficient liquefaction with respect to existing technologies. 1. A method of separating and hydrogenating combustible material , the method comprising:separating the combustible material from waste rock gravitationally in an aqueous salt solution selected to have a density which is intermediate between a density of the combustible material and a density of the waste rock;heating and grinding the separated combustible material to yield a paste of purified combustible material;fluidizing the paste; andhydrogenating the fluidized paste in association with a Segner turbine.2. The method of claim 1 , further comprising successively reducing particle size of the separated combustible material in the solution and removing residual waste rock and gas therefrom claim 1 , wherein the heating and grinding comprises heating and grinding the combustible material of reduced particle size.3. The method of claim 2 , further comprising recycling the aqueous salt solution which is removed in the separating and in the successive particle size reduction.4. The method of claim 2 , wherein the aqueous salt solution is selected to catalyze the separating and the successive particle size reduction.5. The method of claim 2 , wherein the successive particle size reduction is carried out within the aqueous salt solution.6. The method of ...

PROCESSES FOR LIQUEFYING CARBONACEOUS FEEDSTOCKS AND RELATED COMPOSITIONS

Methods for the conversion of lignites, subbituminous coals and other carbonaceous feedstocks into synthetic oils, including oils with properties similar to light weight sweet crude oil using a solvent derived from hydrogenating oil produced by pyrolyzing lignite are set forth herein. Such methods may be conducted, for example, under mild operating conditions with a low cost stoichiometric co-reagent and/or a disposable conversion agent. 187-. (canceled)88. A method for the preparation of synthetic oil (synoil) , comprising:mixing a carbonaceous feedstock with a slurry oil to generate a slurry;contacting the slurry with an iron-containing conversion agent to generate a slurry-agent mixture;reacting the slurry-agent mixture at a hydrogen pressure of from 700 psi to 1,200 psi and a temperature of from 280° C. to 450° C. to generate a reaction-product mixture, whereby some or all of the carbonaceous feedstock is converted into synthetic oil (synoil); andseparating solids from the reaction-product mixture to prepare a synoil.89. The method of claim 88 , wherein the slurry oil comprises light crude oil claim 88 , pyrolysis oil claim 88 , hydrogenated pyrolysis oil claim 88 , intermediate crude oil claim 88 , used motor oil claim 88 , diesel claim 88 , xylenes claim 88 , tetralin claim 88 , aliphatic hydrocarbons or aromatic hydrocarbons or mixtures thereof claim 88 , pyrolysis oil derived from a carbonaceous feedstock claim 88 , pyrolysis oil derived from lignite claim 88 , comprises hydrogenated pyrolysis oil derived from lignite.90. The method of claim 88 , wherein the carbonaceous feedstock comprises lignite claim 88 , lignite with an ash content of less than 26% on a dry basis claim 88 , lignite with an ash content of less than 15% .91. The method of claim 88 , wherein the carbonaceous feedstock comprises sub-bituminous coal claim 88 , low-ranked coal claim 88 , heavy petroleum.92. The method of claim 88 , wherein the iron-containing conversion agent comprises a ...

INTEGRATED ETHANOL AND RENEWABLE DIESEL FACILITY

An integrated facility for the co-production of ethanol and renewable diesel fuel is provided. Corn oil, an ethanol production by-product, is utilized as a feedstock for a renewable diesel plant operating within the same general facility as the corn ethanol plant. By-products of the renewable diesel plant, such as fuel gas, steam, and/or naphtha, can be utilized in various parts of the ethanol plant to increase the operating efficiency thereof. 1. An integrated process for the co-production of ethanol and renewable diesel fuel comprising:distilling an ethanol-containing beer within distillation apparatus of an ethanol plant to produce an ethanol-rich overhead stream and a solids-containing, whole stillage stream;recovering a corn oil product from said ethanol plant, and directing a stream of said corn oil product to a renewable diesel plant; andreacting said corn oil product stream received from said ethanol plant with hydrogen in a reaction system of said renewable diesel plant to produce a mixture of reaction products comprising renewable diesel fuel, fuel gas, and naphtha.2. The process according to claims 1 , including the steps of directing said reaction products to a distillation system of said renewable diesel plant claims 1 , and separating said reaction products into a renewable diesel fuel stream claims 1 , a fuel gas stream claims 1 , and a naphtha stream.3. The process according to claim 2 , including the step of combusting at least a portion of said fuel gas stream within one or more devices located within or utilized during the operation of said ethanol plant and/or said renewable diesel plant.4. The process according to claim 3 , wherein said renewable diesel plant comprises a reactants heater located upstream of said reaction system claim 3 , said reactants heater combusting at least a portion of said fuel gas stream to supply heat to said corn oil product and hydrogen entering said reaction system.5. The process according to claim 1 , wherein said ...

INTEGRATED ETHANOL AND RENEWABLE DIESEL FACILITY

An integrated facility for the co-production of ethanol and renewable diesel fuel is provided. Corn oil, an ethanol production by-product, is utilized as a feedstock for a renewable diesel plant operating within the same general facility as the corn ethanol plant. By-products of the renewable diesel plant, such as fuel gas, steam, and/or naphtha, can be utilized in various parts of the ethanol plant to increase the operating efficiency thereof. 1. An integrated process for the co-production of ethanol and renewable diesel fuel comprising:distilling an ethanol-containing beer within distillation apparatus of an ethanol plant to produce an ethanol-rich overhead stream and a solids-containing, whole stillage stream;recovering a corn oil product from said ethanol plant;reacting said corn oil product from said ethanol plant with hydrogen in a reaction system of a renewable diesel plant to produce a mixture of reaction products comprising renewable diesel fuel, fuel gas, and naphtha;directing said reaction products to a distillation system of said renewable diesel plant for separation of said reaction products into a renewable diesel fuel stream, a fuel gas stream, and a naphtha stream; andcombusting at least a portion of said fuel gas stream within one or more devices located within or utilized during the operation of said ethanol plant.2. The process according to claim 1 , wherein said fuel gas comprises one or more members selected from group consisting of butane claim 1 , propane claim 1 , ethane claim 1 , and methane.3. The process according to claim 1 , wherein said renewable diesel plant comprises a reactants heater located upstream of said reaction system claim 1 , said reactants heater combusting at least a portion of said fuel gas stream to supply heat to said corn oil product and hydrogen entering said reaction system.4. The process according to claim 1 , wherein said corn oil product is recovered from said whole stillage stream within whole stillage processing ...

PRESSURE REDUCTION IN HIGH PRESSURE PROCESSING SYSTEM

The invention relates to a pressure reduction unit for use in processing equipment handling high pressure fluid, where the pressure reduction unit comprises at least one inlet and an outlet, the pressure reduction unit being adapted to receive a pressurized fluid at process pressure level at the inlet, being adapted to isolate the received pressurized fluid from the upstream process and from the outlet and being adapted to reduce the pressure of the fluid to a lower predetermined level and further being adapted to output the fluid through the outlet while still isolated towards the upstream process. 120-. (canceled)21. A pressure reduction unit for use in processing equipment handling high pressure fluid , where the pressure reduction unit comprises at least one inlet and an outlet , the pressure reduction unit being adapted to receive a pressurized fluid at process pressure level at the inlet , being adapted to isolate the received pressurized fluid from the upstream process and from the outlet and being adapted to reduce the pressure of the fluid to a lower predetermined level and further being adapted to output the fluid through the outlet while still isolated towards the upstream process , where the unit comprises a valve at the inlet and a valve at the outlet and between the inlet valve and the outlet valve a de-pressurization device , where means are provided for measuring the pressure upstream the inlet valve , between the inlet valve and the outlet valve and downstream the outlet valve and further comprising a control system , where the control system is adapted to allow opening of the valves when a certain maximum pressure difference is present on either side of the valve to be opened.22. The pressure reduction unit according to claim 21 , where a position indicator is provided indicating the cycle position of the pressure reduction device and being adapted to provide a control signal for opening or closing at least one valve in the pressure reduction unit. ...

LOW COMPLEXITY, HIGH YIELD CONVERSION OF HEAVY HYDROCARBONS

A process for producing pipeline-ready or refinery-ready feedstock from heavy hydrocarbons using a high-performance solvent extraction process with high local solvent-to-process fluid ratios yet maintaining low overall solvent-to-process fluid ratios, by first performing mild thermal cracking on the heavy hydrocarbons and then separating asphaltene-rich fractions from a resulting thermally affected fluid so that the high solvent-to-oil ratio portion of the process acts only on those asphaltene-rich fractions, and producing a dry, solid asphaltene as an end-product. 1. Process apparatus for processing heavy hydrocarbons to produce pipeline-ready or refinery-ready feedstock , comprising:(a) a process fluid preparation component for mixing heavy hydrocarbon with other substances as required to prepare a process fluid;(b) transport means to move the process fluid to a pre-heater;(c) the pre-heater for heating the process fluid to a temperature close to or at a desired operating temperature of a reactor;(d) transport means to move the heated process fluid to the reactor;(e) the reactor having heat exchange means to provide a desired heat flux to the process fluid and maintain the process fluid in-reactor at a substantially uniform desired temperature for a desired residence time;(f) means to provide sweep gas to the process fluid in the reactor; (i) non-condensable vapours', '(ii) light liquid hydrocarbons', '(iii) thermally-affected asphaltene-rich fractions, '(g) means to remove various produced substances from the reactor at the end of the residence time, those substances comprising at least(h) means to separate non-condensable vapours from light liquid hydrocarbons;(i) transport means to move the thermally affected asphaltene-rich fractions to a solvent extraction processor;(j) the solvent extraction processor including means to supply C4-C8 solvent and to mix the solvent with the thermally affected asphaltene rich fractions, and means to keep the processor and ...

HIGH SURFACE AREA GRAPHENE-SUPPORTED METAL CHALCOGENIDE ASSEMBLY

A composition comprising at least one graphene-supported assembly, which comprises a three-dimensional network of graphene sheets crosslinked by covalent carbon bonds, and at least one metal chalcogenide compound disposed on said graphene sheets, wherein the chalcogen of said metal chalcogenide compound is selected from S, Se and Te. Also disclosed are methods for making and using the graphene-supported assembly, including graphene-supported MoS. Monoliths with high surface area and conductivity can be achieved. Lower operating temperatures in some applications can be achieved. Pore size and volume can be tuned. Electrochemical methods can be used to make the materials. 1. A composition comprising at least one graphene-supported assembly , which comprises (i) a three-dimensional network of graphene sheets crosslinked by covalent carbon bonds and (ii) at least one metal chalcogenide compound disposed on said graphene sheets , wherein the chalcogen of said metal chalcogenide compound is selected from S , Se and Te.2. The composition of claim 1 , wherein metal chalcogenide compound is a catalyst for hydrogenation claim 1 , hydrodeoxygenation claim 1 , hydrodesulfurization claim 1 , hydrodenitrogenation claim 1 , and/or hydrocracking.3. The composition of claim 1 , wherein the graphene-supported assembly is electrically conductive.4. The composition of claim 1 , wherein the graphene-supported assembly has a conductivity of at least 0.5 S/cm.5. The composition of claim 1 , wherein the graphene-supported assembly is a monolith having a size of at least 1 mm claim 1 , or in the form of a powder produced by grinding or ball-milling said monolith.6. The composition of claim 1 , wherein the graphene-supported assembly has an elastic modulus of at least 10 MPa.7. The composition of claim 1 , wherein the chalcogen is S.8. The composition of claim 1 , wherein the metal chalcogenide compound comprises one or more of Mo claim 1 , W claim 1 , Fe claim 1 , Cd claim 1 , In claim 1 , ...

INTEGRATED PROCESS FOR THE PRODUCTION OF RENEWABLE DROP-IN FUELS

A process for producing renewable biofuels from biomass is provided wherein a bio-oil containing stream is hydrotreated in an integrated system which uses streams and components generated or obtained from the biomass treatment and conversion. 1. A process for producing a renewable fuel from biomass , the process comprising:(a) converting biomass in a biomass conversion unit in the presence of a biomass conversion catalyst and separating the converted biomass into a fluid phase and a solid phase;(b) separating the fluid phase into a non-condensable gas phase, a renewable bio-oil and process water;{'sub': '6', '(c) fractionating the renewable bio-oil into a water stream, a full range bio-naphtha stream and a topped bio-oil stream, wherein the topped bio-oil stream comprises Cor higher oxygenates;'}{'sub': 5', '6, '(d) molecularly recombining the oxygenates of Cor lower within the process water, the full range bio-naphtha stream and the water stream to produce a recovered organic stream (ROS) comprising Cor greater oxygenates and a clear aqueous stream;'}(e) forming a slurry catalyst mix from the ROS and a soluble hydroprocessing active phase;(f) feeding at least a portion of biomass conversion catalyst and the catalyst mix into a slurry-phase hydroprocessor reactor;(g) forming in the slurry-phase hydroprocessor reactor a solid-phase slurry dispersed catalyst comprising atomically dispersoids of the active phase onto a support comprising the biomass conversion catalyst;(h) feeding the topped bio-oil stream into the slurry-phase hydroprocessor reactor and subjecting the topped bio-oil stream to hydrogenation in the presence of the solid-phase slurry dispersed catalyst; and(i) obtaining renewable fuels originating from hydrogenated topped bio-oil stream.2. The process of claim 1 , wherein the soluble hydroprocessing active phase is an organometallic salt selected from the group of acetylacetonates claim 1 , naphthenates claim 1 , oxalates claim 1 , tartrates claim 1 , or ...

METHOD FOR PROCESSING HYDROCARBON FUELS USING MICROWAVE ENERGY

A method of operating a hydrocarbon material processing system includes feeding a hydrocarbon feedstock from a hydrocarbon feedstock source into a reaction tube positioned within an opening of a waveguide, feeding a process gas from a process gas source into the reaction tube, receiving microwaves in the waveguide from a microwave generator, energy from the waveguide in the reaction tube to cause the feedstock and process gas to react and form into a product stream comprising a fuel product. The method also includes periodically delivering a cleaning gas into the reaction tube, without stopping the propagation of the energy and without pausing the feeding of the hydrocarbon feedstock and the process gas into the reaction tube. 1. A method of operating a hydrocarbon material processing system , comprising:feeding a hydrocarbon feedstock from a hydrocarbon feedstock source into a reaction tube positioned within an opening of a waveguide;feeding a process gas from a process gas source into the reaction tube;receiving microwaves in the waveguide from a microwave generator;propagating energy from the waveguide to the reaction tube to cause the feedstock and process gas to react and form into a product stream comprising a fuel product; andperiodically, without stopping the propagation of the energy and without pausing the feeding of the hydrocarbon feedstock and the process gas into the reaction tube, delivering a cleaning gas into the reaction tube.2. The method of claim 1 , further comprising:forming a plasma from the cleaning gas; andmaintaining the plasma for a predetermined period of time within the reaction tube sufficient to burn off carbon residue from an inner sidewall of the reaction tube.3. The method of claim 1 , further comprising:vacuuming or flushing the carbon residue from the reaction tube; andafter the vacuuming or flushing, resuming the feeding of the hydrocarbon feedstock and the process gas into the reaction tube.4. The method of claim 1 , wherein:the ...

TORREFACTION REDUCTION OF COKE FORMATION ON CATALYSTS USED IN ESTERIFICATION AND CRACKING OF BIOFUELS FROM PYROLYSED LIGNOCELLULOSIC FEEDSTOCKS

A bio-oil production process involving torrefaction pretreatment, catalytic esterification, pyrolysis, and secondary catalytic processing significantly reduces yields of reactor char, catalyst coke, and catalyst tar relative to the best-case conditions using non-torrefied feedstock. The reduction in coke as a result of torrefaction was 28.5% relative to the respective control for slow pyrolysis bio-oil upgrading. In fast pyrolysis bio-oil processing, the greatest reduction in coke was 34.9%. Torrefaction at 275° C. reduced levels of acid products including acetic acid and formic acid in the bio-oil, which reduced catalyst coking and increased catalyst effectiveness and aromatic hydrocarbon yields in the upgraded oils. The process of bio-oil generation further comprises a catalytic esterification of acids and aldehydes to generate such as ethyl levulinate from lignified biomass feedstock. 1. A method for reducing coke deposition on a catalyst used in cracking of a pyrolysis oil vapor , the method comprising:(a) subjecting a biomass to torrefaction;(b) pyrolyzing the torrefaction-treated biomass, thereby generating a heated pyrolysis oil vapor;(c) catalytically esterifying the heated pyrolysis oil vapor or components thereof, thereby providing a heated pyrolysis oil vapor having a reduced acid and aldehyde content compared to a heated pyrolysis oil vapor not catalytically esterified; and(d) cracking the catalytically esterified heated pyrolysis oil vapor, thereby generating a bio-oil, wherein said cracking step comprises contacting the heated pyrolysis oil vapor with a second catalyst, and wherein said catalyst accumulates a reduced coke deposition compared to when the heated pyrolysis oil vapor is generated from a biomass not treated with torrefaction.2. The method of claim 1 , wherein in step (c) the heated pyrolysis oil vapor is contacted with an aqueous composition comprising at least one alcohol and a first catalyst selected to catalyze the esterification of at ...

INTEGRATED PROCESS AND UNIT OPERATION FOR CONDITIONING A SOOT-CONTAINING SYNGAS

The present invention relates to a method for conditioning a soot-containing syngas stream in a single integrated apparatus containing a scrubbing vessel wherein particulate matter is decoupled from the waste water stream. 1. An integrated process for conditioning a soot-containing synthesis gas stream , comprising:(a) introducing a raw soot-containing synthesis gas having particulate matter and gaseous contaminants therein at a temperature of less than about 900° F. into a quenching device to reduce the temperature of said synthesis gas to a range of about 250-400° F., thereby forming a two-phase stream;(b) routing the two-phase stream through a first scrubber device to substantially transfer majority of particulate matter from the gas phase to the liquid phase;(c) directing said two-phase stream to a second scrubbing device wherein the two-phase stream is separated into a water phase fluid contaminated with particulate matter and a gas phase fluid having water-soluble contaminants at a lower section of the scrubbing device;(d) cleaning and cooling the gas phase fluid having water-soluble contaminants in an upper section of the second scrubbing device where the gas phase fluid comes in direct contact with process water cooled to a temperature below 150° F. dispensed through a spray nozzle device thereby reducing the temperature of the gas phase fluid below the dew point temperature and removing water soluble impurities and remaining particulate matter therefrom;(e) further routing the cooled and cleaned gas phase fluid of step (d) through a mist eliminating device disposed in the upper section of the second scrubbing device to remove substantially all of the remaining entrained water droplets, thereby producing a cooled and substantially soot free synthesis gas stream.2. The integrated process of claim 1 , further comprising: recycling at least a portion of said water phase fluid contaminated with particulate matter from said second scrubbing device to said ...

Process and apparatus for producing liquid hydrocarbon

The invention relates to a continuous process for converting carbonaceous material contained in one or more feedstocks into a liquid hydrocarbon product, said feedstocks including the carbonaceous material being in a feed mixture including one or more fluids, said fluids including water and further liquid organic compounds at least partly produced by the process in a concentration of at least 1% by weight, where the process comprises converting at least part of the carbonaceous material by pressurising the feed mixture to a pressure in the range 250-400 bar; heating the feed mixture to a temperature in the range 370-450° C., and maintaining said pressurized and heated feed mixture in the desired pressure and temperature ranges in a reaction zone for a predefined time; cooling the feed mixture to a temperature in the range 25-200° C. and expanding the feed mixture to a pressure in the range of 1-70 bar, thereby causing the carbonaceous material to be converted to a liquid hydrocarbon product and separating from the converted feed mixture a fraction comprising liquid hydrocarbon product.

WAVE MODES FOR THE MICROWAVE INDUCED CONVERSION OF COAL

A system for converting hydrocarbon materials into a product includes a hydrocarbon feedstock source, a process gas source, an energy generator, and a cylindrical reaction chamber. The reaction chamber has a conductive inner surface that forms a resonant cavity. The resonant cavity is configured to support a standing TM010 electromagnetic wave. The reaction chamber is also configured to receive feedstock from the feedstock source, process gas from the process gas source, and convert the feedstock into a product stream in the presence of the TM010 electromagnetic wave. 1. A method for converting hydrocarbon materials into a product , comprising:receiving, in a cylindrical reaction chamber, a hydrocarbon feedstock, wherein the cylindrical reaction chamber comprises a conductive inner surface to form a resonant cavity;receiving, in the first reaction chamber, a process gas;forming, in the cylindrical reaction chamber, a standing TM010 electromagnetic wave in the presence of microwave energy from a microwave generator; andconverting, in the cylindrical reaction chamber, the hydrocarbon feedstock into a product stream in the presence of the TM010 electromagnetic wave, wherein the product stream comprises at least one oil product that has an API gravity of at least 8.2. The method of claim 1 , wherein the at least one oil product has an aromaticity of less than 55%.3. The method of claim 1 , wherein converting the hydrocarbon feedstock into the product stream comprises directing the flow of the hydrocarbon feedstock and the process gas through at least one node of the TM010 electromagnetic wave to form a plasma within the reaction chamber and converting the hydrocarbon feedstock into the product stream in presence of the plasma to promote conversion of the hydrocarbon feedstock.4. The method of claim 1 , wherein forming the standing TM010 electromagnetic wave comprises forming a standing TM010 electromagnetic wave that has a resonant frequency of 915 MHz claim 1 , 434 MHz ...

METHOD FOR EXTRACTING BIOCHEMICAL PRODUCTS OBTAINED FROM A PROCESS OF HYDROTHERMAL CARBONIZATION OF BIOMASS

The invention relates to a method for extracting biochemical products obtained from a process of hydrothermal carbonization of biomass, which includes feeding an aqueous mixture of biomass from a preheating tube for the aqueous mixture of biomass to a vertical reactor with a predetermined level of floatation and an area for accumulation of steam and gases in the upper part thereof, wherein said method for extracting biochemical products is characterized in that it includes (a) heating the aqueous mixture of biomass to, or above, evaporation temperature in said vertical reactor and/or in a previous stage of preheating the aqueous mixture of biomass, increasing the generation of stream and/or gases at the predetermined flotation level of the vertical reactor, (b) extracting the steam and/or gases generated in the previous stage and accumulated in the upper part of the vertical reactor, and (c) cooling the gases and/or condensing the steam extracted in the previous stage at different levels of temperature and pressure. The invention likewise relates to the biochemical product obtainable from said method, as well as to a system for implementing said method. 1. Method for extracting biochemical products during a process of hydrothermal carbonization of biomass , comprising feeding an aqueous mixture of biomass from a preheating tube of the aqueous mixture of biomass to a vertical reactor with a defined level of flotation and an area for the accumulation of steam and gases in its upper portion , where said method for extracting biochemical products is characterized in that it comprises:(a) Heating the aqueous mixture of biomass up to or over the evaporation temperature in the same vertical reactor and/or in a prior preheating stage of the aqueous biomass mixture, increasing the generation of steam and/or gases at the set level of floatation of the vertical reactor.(b) Extracting the biochemicals alongside the steam and/or gasses generated in the previous stage, which ...

USE OFCARBON DIOXIDE GENERATED BY HYDROPYROLYSIS FOR PROCESS INERTIZATION

A hydropyrolysis process comprises feeding both (i) hydrogen and (ii) a biomass-containing feedstock or a biomass-derived feedstock, to a hydropyrolysis reactor vessel. The process comprises producing a CO-containing vapor stream and at least one liquid product. A COproduct, separated from the CO-containing vapor stream, is advantageously used for at least one inertization function of the hydropyrolysis process. Representative inertization functions include operation of solids transport equipment, blanketing of liquid containers, drying of biomass-containing feedstock or biomass-derived feedstock, conveying or separating solids, and combinations thereof. Importantly, COproducts utilized for these inertization functions may be obtained predominantly, if not completely (depending on the nature of the feedstock), from renewable carbon in biomass. 1. A hydropyrolysis process , comprising:feeding both (i) hydrogen and (ii) a biomass-containing feedstock or a biomass-derived feedstock, to a hydropyrolysis reactor vessel,{'sub': '2', 'producing a CO-containing vapor stream and at least one liquid product,'}{'sub': 2', '2, 'using a COproduct, separated from the CO-containing vapor stream, for at least one inertization function of the hydropyrolysis process, the inertization function selected from the group consisting of operation of solids transport equipment, blanketing of liquid containers, drying of biomass-containing feedstock, conveying or separating solids, and combinations thereof.'}2. The hydropyrolysis process of claim 1 , wherein the CO-containing vapor stream claim 1 , from which the COproduct is separated claim 1 , is selected from the group consisting of (i) a hydropyrolysis reactor vapor claim 1 , obtained from a hydropyrolysis reactor output claim 1 , (ii) a hydroconversion zone output claim 1 , (iii) a vapor stream or a purified pre-reactor vapor stream claim 1 , (iv) a regeneration effluent and (v) a hydrogasification effluent claim 1 , and combinations ...

Combined Hydrothermal Liquefaction and Catalytic Hydrothermal Gasification System and Process for Conversion of Biomass Feedstocks

A combined hydrothermal liquefaction (HTL) and catalytic hydrothermal gasification (CHG) system and process are described that convert various biomass-containing sources into separable bio-oils and aqueous effluents that contain residual organics. Bio-oils may be converted to useful bio-based fuels and other chemical feedstocks. Residual organics in HTL aqueous effluents may be gasified and converted into medium-BTU product gases and directly used for process heating or to provide energy. 115-. (canceled)16: A system for conversion of a biomass , the system comprising:a hydrothermal liquefaction (HTL) stage that hydrothermally liquefies the biomass in an aqueous medium at a temperature and pressure selected to form a conversion product comprising a separable bio-oil and an aqueous fraction containing residual organics therein; anda catalytic hydrothermal gasification (CHG) stage operatively coupled to the HTL stage configured to receive the aqueous fraction containing residual organics from the HTL stage at a selected temperature and pressure that forms a product gas containing at least one medium BTU product gas.17: The system of claim 16 , further including an upgrade stage configured to upgrade the bio-oil released from the HTL stage over a hydrogenation catalyst at a temperature up to about 450° C. and a hydrogen partial pressure up to about 150 atmospheres (1.52×104 kPa) that yields a green crude.18: The system of claim 16 , wherein the product gas when combusted generates sufficient energy such that the sum of the energy demands for conversion of the biomass feedstock to the product gas is a net positive.19: The system of claim 16 , further including one or more heat exchangers positioned to distribute heat to selected locations in the HTL stage and/or the CHG stage. This application claims priority from U.S. Provisional Patent Application No. 61/657,416 filed 8 Jun. 2012 entitled “Combined Hydrothermal Liquefaction and Catalytic Hydrothermal Gasification for ...

Process for Depolymerizing Coal to Co-Produce Pitch and Naphthalene

A method of depolymerizing coal includes preparing a high temperature depolymerizing medium consisting of heavy hydrocarbon oils and mixing it with coal to form a mixture, performing an optional first distillation at a temperature below 250° C. to recover naphthalene, heating the mixture to a temperature between 350° C. and 450° C. to create a digested coal, centrifuging the digested coal to remove ash and obtain a centrate, and distillation of the centrate into separate fractions. The high temperature depolymerizing medium may be a heavy hydrocarbon with a hydrogen to carbon (H/C) ratio higher than 7.0% and may include liquids chosen from the group consisting of: coal tar distillate, decant oil, anthracene oil, and heavy aromatic oils. The high temperature depolymerizing medium may be blended with an oil, preferably with H/C ratio higher than 10.0%, such as soybean oil, other biomass derived oil, lignin, petroleum oil, pyrolysis oil such that the overall hydrogen-to-carbon mass ratio in a digestion reactor is over 7.0% for the mixture of depolymerizing medium and coal. The depolymerized coal is an aromatic liquid that can itself be, either wholly or in part, a depolymerizing medium so that the process can be repeated. 1. A method of depolymerizing coal , comprising:preparing a high temperature depolymerizing medium consisting of heavy hydrocarbon oils and mixing it with coal to form a mixture;performing a first distillation to recover naphthalene;heating the mixture to a temperature of at least 350° C. to create a digested coal slurry; andcentrifuging the slurry to produce a centrate liquid with ash content less than 0.5% by mass.2. The method of claim 1 , wherein the high temperature depolymerizing medium is a heavy hydrocarbon with H/C ratio higher than 7.0%.3. The method of claim 1 , wherein the high temperature depolymerizing medium consists of liquids chosen from the group consisting of: coal tar distillate claim 1 , decant oil claim 1 , anthracene oil claim 1 ...

METHODS AND SYSTEMS FOR SUPPLYING HYDROGEN TO A HYDROCATALYTIC REACTION

Systems and methods for supplying hydrogen to a hydrocatalytic reaction of a biomass feedstock by gasification of a biomass material. In a preferred embodiment, the biomass material comprises hog fuel. In one embodiment, an overhead fraction of the hydrocatalytic reaction is further processed to generate higher molecular weight compounds, which can be used to produce a fuel product. In one embodiment, the biomass material comprises an outer bark layer of wood logs used as part of the biomass feedstock subject to the hydrocatalytic reaction. 1. A method comprising:(a) providing a biomass feedstock containing cellulose and water;(b) contacting the biomass feedstock with hydrogen in the presence of a catalyst capable of activating molecular hydrogen to form a hydrocatalytically treated mixture;(c) partially oxidizing at least a biomass material to produce a gas mixture comprising carbon monoxide and hydrogen, wherein the biomass material does not include the hydrocatalytically treated mixture;(d) providing the gas mixture to a water gas shift reaction zone external to where the biomass feedstock is contacted with hydrogen to generate hydrogen and carbon dioxide; and(e) providing at least a portion of the hydrogen from step (d) for use in step (b).2. The method of wherein the hydrocatalytically treated mixture comprises a plurality of hydrocarbon and oxygenated hydrocarbon molecules claim 1 , said method further comprising processing at least a portion of the plurality of hydrocarbon and oxygenated hydrocarbon molecules to form a fuel blend comprising a higher hydrocarbon.3. The method of wherein the partially oxidizing step comprises using a gasifier.4. The method of wherein the gasifier is selected from the group consisting of a moving-bed gasifier claim 3 , a fluid-bed gasifier claim 3 , an entrained-flow gasifier claim 3 , and any combination thereof.5. The method of further comprising routing the biomass material to the gasifier claim 4 , wherein said portion can ...

METHODS AND SYSTEMS FOR SUPPLYING HYDROGEN TO A HYDROCATALYTIC REACTION

A bottom fraction of a product of a hydrocatalytic reaction is gasified to generate hydrogen for use in further hydrocatalytic reactions. In one embodiment, one or more volatile organic compounds is also vaporized using heat generated in the gasification process. In one embodiment, an overhead fraction of the hydrocatalytic reaction is further processed to generate higher molecular weight compounds. In another embodiment, a product of the further processing is separated into a bottom fraction and an overhead fraction, where the bottom fraction is also gasified to generate hydrogen for use in further hydrocatalytic reactions. 1. A method comprising:(a) providing a biomass feedstock containing cellulose and water;(b) contacting the biomass feedstock with hydrogen in the presence of a catalyst capable of activating molecular hydrogen to form a hydrocatalytically treated mixture;(c) separating the hydrocatalytically treated mixture into at least a first bottom fraction and a first overhead fraction, wherein the first bottom fraction comprises (i) at least one compound having a separation point having a temperature in a range of about 100 to 600 degrees C. and a pressure of about atmospheric pressure, and (ii) at least one volatile organic compound;(d) vaporizing the at least one volatile organic compound from the first bottom fraction using at least a heat exchange medium;(e) partially oxidizing the first bottom fraction without the vaporized at least one compound to generate a gas mixture comprising hydrogen and carbon monoxide, wherein the heat exchange medium comprises the gas mixture;(f) providing the gas mixture to a water gas shift reaction zone external to where the biomass feedstock is contacted with hydrogen to generate hydrogen and carbon dioxide; and(g) providing the hydrogen from step (f) for use in step (b).2. The method of wherein the first bottom fraction comprises at least one compound having a separation point having a temperature in a range of about ...

METHODS AND SYSTEMS FOR SUPPLYING HYDROGEN TO A HYDROCATALYTIC REACTION

A bottom fraction of a product of a hydrocatalytic reaction is gasified to generate hydrogen for use in further hydrocatalytic reactions. In one embodiment, one or more volatile organic compounds is also vaporized using heat generated in the gasification process. In one embodiment, an overhead fraction of the hydrocatalytic reaction is further processed to generate higher molecular weight compounds. In another embodiment, a product of the further processing is separated into a bottom fraction and an overhead fraction, where the bottom fraction is also gasified to generate hydrogen for use in further hydrocatalytic reactions. 1. A method comprising:(a) providing a biomass feedstock containing cellulose and water;(b) contacting the biomass feedstock with hydrogen in the presence of a catalyst capable of activating molecular hydrogen to form a hydrocatalytically treated mixture;(c) separating the hydrocatalytically treated mixture into at least a first bottom fraction and a first overhead fraction, wherein the first bottom fraction comprises (i) at least one compound having a separation point having a temperature in a range of about 100 to 600 degrees C. and a pressure of about atmospheric pressure, and (ii) one or more volatile organic compounds;(d) vaporizing at least one volatile organic compound from the first bottom fraction in a first flasher;(e) depositing the at least one compound having a separation point having a temperature in a range of about 100 to 600 degrees C. and a pressure of about atmospheric pressure on a surface in the first flasher;(f) placing the first flasher in standby mode;(g) vaporizing at least one volatile organic compound from the first bottom fraction in a second flasher;(h) partially oxidizing the deposited at least one compound in the first flasher to generate a gas mixture comprising hydrogen and carbon monoxide;(i) providing the gas mixture to a water gas shift reaction zone external to where the biomass feedstock is contacted with ...

PROCESS TO PRODUCE BIOFUELS FROM BIOMASS

A process for producing biofuels from biomass is provided by removing sulfur compounds and nitrogen compounds from the biomass by contacting the biomass with a digestive solvent to form a pretreated biomass containing soluble carbohydrates and having less than 35% of the sulfur content and less than 35% of the nitrogen content, based on untreated biomass on a dry mass basis, prior to carrying out aqueous phase reforming and further processing to form a liquid fuel. 1. A system comprising: a digester that receives a biomass feedstock and a digestive solvent operating under conditions to effectively remove nitrogen compounds and sulfur compounds from said biomass feedstock and discharges a treated stream comprising a carbohydrate having less than 35% of the sulfur content and less than 35% of the nitrogen content based on untreated biomass feedstock on a dry mass basis; an aqueous phase reforming reactor comprising an aqueous phase reforming catalyst that receives the treated stream and discharges an oxygenated intermediate stream , wherein a first portion of the oxygenated intermediate stream is recycled to the digester as at least a portion of the digestive solvent; and a fuels processing reactor comprising a condensation catalyst that receives a second portion of the oxygenated intermediate stream and discharges a liquid fuel.2. A system comprising: a digester that receives a biomass feedstock and a digestive solvent operating under conditions to effectively remove nitrogen , phosphorus and sulfur compounds from said biomass feedstock and discharges a treated stream comprising a carbohydrate having less than 35% of the sulfur content and less than 35% of the nitrogen content based on untreated biomass feedstock on a dry mass basis; an aqueous phase reforming reactor comprising an aqueous phase reforming catalyst that receives the treated stream and discharges an oxygenated intermediate , wherein a first portion of the oxygenated intermediate stream is recycled to ...

ORGANO-CATALYTIC BIOMASS DECONSTRUCTION

The present invention provides processes for catalytic deconstruction of biomass using a solvent produced in a bioreforming reaction. 1. A method of making a biomass hydrolysate , the method comprising:{'sub': 2+', '1+', '2+', '1-3, 'A. catalytically reacting water and a water-soluble CO oxygenated hydrocarbon in a liquid or vapor phase with H2 in the presence of a deoxygenation catalyst at a deoxygenation temperature and deoxygenation pressure to produce a biomass processing solvent comprising a COhydrocarbon in a reaction stream;'}B. reacting the biomass processing solvent with a solid biomass component, hydrogen and a deconstruction catalyst at a deconstruction temperature and a deconstruction pressure to produce a biomass hydrolysate comprising at least one member selected from the group consisting of a water-soluble lignocellulose derivative, a water-soluble cellulose derivative, a water-soluble hemicellulose derivative, a carbohydrate, a starch, a monosaccharide, a disaccharide, a polysaccharide, a sugar, a sugar alcohol, an alditol and a polyol, wherein the solid biomass component is selected from the group consisting of agricultural residues, wood materials, municipal solid waste and energy crops; andC. recycling the biomass hydrolysate into the reactants of step B.2. The method of claim 1 , wherein the biomass processing solvent comprises a member selected from the group consisting of an alcohol claim 1 , ketone claim 1 , aldehyde claim 1 , cyclic ether claim 1 , ester claim 1 , diol claim 1 , triol claim 1 , hydroxy carboxylic acid claim 1 , carboxylic acid claim 1 , and a mixture thereof.3. The method of claim 1 , wherein the deconstruction catalyst comprises an acidic resin or a basic resin.4. The method of claim 3 , wherein the deconstruction catalyst further comprises a member selected from the group consisting of Fe claim 3 , Co claim 3 , Ni claim 3 , Cu claim 3 , Ru claim 3 , Rh claim 3 , Pd claim 3 , Pt claim 3 , Re claim 3 , Mo claim 3 , W claim 3 ...

CATALYTIC PYROLYSIS USING UZM-39 ALUMINOSILICATE ZEOLITE

A new family of coherently grown composites of TUN and IMF zeotypes has been synthesized and shown to be effective catalysts for catalytic pyrolysis of biomass. These zeolites are represented by the empirical formula. 3. The process of wherein the hydrocarbons produced include aromatic compounds and the selectivity to aromatic compounds within the condensable portion of the pyrolysis gases is greater than 33% by weight.4. The process of wherein the hydrocarbons produced include aromatic compounds and the selectivity to aromatic compounds within the condensable portion of the pyrolysis gases is greater 50% by weight.5. The process of wherein the hydrocarbons produced include aromatic compounds and the yield of aromatic compounds is greater than 2% by weight based upon the biomass.6. The process of wherein the hydrocarbons produced include aromatic compounds and the yield of aromatic compounds is greater than 3% by weight based upon biomass.7. The process of wherein the pyrolysis conditions include a temperature from about 300° C. to about 800° C.8. The process of wherein the catalyst is in a fluidized state.9. The process of wherein the contacting a carbonaceous biomass feedstock with a microporous crystalline zeolitic catalyst is carried out using a catalyst-to-carbonaceous biomass feedstock ratio of about 0.1 to about 200.10. The process of wherein the coherently grown composite of TUN and IMF zeotypes is thermally stable up to a temperature of greater than 600° C.11. The process of wherein the coherently grown composite of TUN and IMF zeotypes has a micropore volume as a percentage of total pore volume of greater than 60%.12. The process of wherein the microporous crystalline zeolitic catalyst comprises the heat transfer medium of a fast pyrolysis process.13. The process of further comprising regenerating the catalyst after contacting with the feedstock to form a regenerated catalyst and recycling the regenerated catalyst to the contacting step.15. The process of ...

PROCESS FOR PRODUCING TRANSPORTATION FUELS FROM OIL SANDS-DERIVED CRUDE

Disclosed are processes for extracting deasphalted crude oil from oil sand. Deasphalted crude oil can be extracted using a hydrocarbon recycle solvent stream having specified Hansen blend parameters, with the oil sand being contacted with the hydrocarbon recycle solvent stream in a contact zone of a vessel to separate not greater than 80 wt % of the bitumen present on the oil sand. The separated bitumen is considered a deasphalted crude oil stream, since it has an asphaltenes content substantially lower than that of the total bitumen initially present on the oil sand. The deasphalted crude oil stream can be treated using a hydrotreating catalyst or catalytic cracking catalyst to produce transportation fuel. 1. A process for treating deasphalted crude oil extracted from oil sand , comprising:supplying a hydrocarbon recycle solvent stream to a contact zone of a vessel, wherein the recycle solvent has a Hansen dispersion blend of not greater than 16, a Hansen polarity blend of less than 1 and a Hansen polarity blend of less than 2;supplying a feed stream of oil sand to the contact zone of the vessel, wherein the oil sand is comprised of at least 4 wt % total bitumen, based on total weight of the supplied oil sand;contacting the oil sand with the hydrocarbon recycle solvent in the contact zone of the vessel to separate not greater than 80 wt % of the bitumen present on the oil sand;removing at least a portion of the hydrocarbon solvent and the separated bitumen from the contact zone of the vessel;separating the hydrocarbon solvent from the separated bitumen to produce the hydrocarbon recycle solvent stream and a deasphalted crude oil stream, wherein the deasphalted crude oil stream has an ASTM D7169 5% distillation point of from 400° F. to 700° F., an asphaltenes content of not greater than 10 wt %, a Conradson Carbon Residue (CCR) of not greater than 15 wt % and sulfur content of not greater than 4 wt %, andtreating the deasphalted crude oil stream with a hydrotreating ...

Recycling a Used Absorbent Hygiene Product or its Components Using Hydrothermal Treatment

Used AHP or its components is converted into low molecular weight hydrocarbons using HTT reactor. These low molecular weight hydrocarbons produce ethylene, propylene, and other chemicals when fed into a steam cracker, which can be used to produce recycled components of the AHP or a fully recycled AHP.

Feedstock Conversion To Fuel On High Pressure Circulating Fluidized Bed

There is provided a process and systems for producing fuels via pyrolysis of carbonaceous feedstock under pressure and temperature in an efficient manner using a circulating fluidized bed with catalyst(s). The pressure and temperature are selected to provoke supercritical conditions, and pyrolysis, hydropyrolysis, hydrotreating, and optionally reforming treatment of the carbonaceous feedstock is carried out simultaneously in one reactor on a recirculating fluidized bed containing catalysts. 1. A process for the production of fuel comprising ,(a) providing in a reaction vessel a carbonaceous feedstock, a lift gas mixture of inert gas components, hydrogen, a fluidized bed of inert particulate solids and a hydrogenation catalyst; 'wherein the pyrolyzing comprises simultaneous pyrolysis, hydropyrolysis and hydrotreating of the carbonaceous feedstock to form said fuel.', '(b) pyrolyzing the carbonaceous feedstock to form fuel product components under temperature and pressure so as to establish supercritical conditions of temperature and pressure of at least one component of the carbonaceous feedstock, lift gas, hydrogen, water or fuel product;'}2. The process of wherein a hydrocarbon is present in said reaction vessel and said simultaneous pyrolysis claim 1 , hydropyrolysis and hydrotreating further includes simultaneous reforming wherein said hydrocarbon is reacted with water to form carbon monoxide and hydrogen.3. The process of wherein the reaction vessel is at a temperature of at least 647° K and a pressure of at least 22.1 MPa.4. The process of wherein said carbonaceous feedstock has a water content of 0% by weight to 97% by weight.5. The process of wherein the carbonaceous feedstock has a residence time is said reaction vessel of less than or equal to 5.0 seconds.6. The process of wherein said fuel has an oxygen level of less than or equal to 1000 ppm claim 1 , a nitrogen level of less than or equal to 15 ppm and a sulfur content of less than or equal to 3000 ppm.7 ...

Methods and systems for processing cellulosic biomass

Digestion of cellulosic biomass solids may be complicated by release of lignin therefrom. Methods and systems for processing a reaction product containing lignin-derived products, such as phenolics, can comprise hydrotreating the reaction product to convert the lignin-derived products to desired higher molecular weight compounds. The methods and systems can further include separating the higher molecular weight compounds from unconverted products, such as unconverted phenolics, and recycling the unconverted phenolics for use as at least a portion of the digestion solvent and for further conversion to desired higher molecular weight compounds with additional hydrotreatment. The methods and systems can further include a further hydrotreatment step configured for additional lignin conversion and/or a further hydrotreatment step configured for generating hydrogen.

DEVICE AND METHOD FOR PREPARING OXYGEN-CONTAINING LIQUID FUEL BY BIO-OIL CATALYTIC CONVERSION

Devices and methods for preparing oxygen-containing liquid fuel by bio-oil catalytic conversion. A device includes a biomass fast thermal cracking system for preparing bio-oil, a bio-oil oil-water separating system for separating the bio-oil into oil phase bio-oil and water phase bio-oil that is output to an oil phase bio-oil chemical chain hydrogen production system, and a water phase bio-oil catalytic hydrogenation system. The hydrogen production system outputs produced hydrogen to the water phase bio-oil catalytic hydrogenation system to prepare a liquid fuel. A method includes the steps: thermally cracking the biomass to prepare bio-oil, separating the water phase and the oil phase, producing hydrogen from the oil phase bio-oil through a chemical chain method so as to provide a hydrogen source for the water phase bio-oil to carry out two-stage catalytic hydrogenation in a slurry bed, and separating and purifying the hydrogenated products to obtain an oxygen-containing liquid fuel. 1. A device for preparing oxygen-containing liquid fuel by catalytic conversion of bio-oil , comprising:a system for oil preparation by fast thermal cracking of biomass for preparing bio-oil; a bio-oil oil-water separation system for receiving the bio-oil, separating the bio-oil into oil-phase bio-oil and water-phase bio-oil and delivering the oil-phase bio-oil and the water-phase bio-oil to an oil-phase bio-oil chemical chain hydrogen production system and a water-phase bio-oil catalytic hydrogenation system, respectively;an oil-phase bio-oil chemical chain hydrogen production system for receiving the oil-phase bio-oil, turning it into hydrogen and low-valence metallic oxide, and delivering hydrogen to a water-phase bio-oil catalytic hydrogenation system;a water-phase bio-oil catalytic hydrogenation system for receiving the water-phase bio-oil and hydrogen, and taking low-temperature catalytic hydrogenation reaction with a catalyst to generate a hydrogenated gas-phase product;an ...

PROCESSES FOR PRODUCING BIOMASS-DERIVED PYROLYSIS OILS

Processes for pyrolyzing biomass. A catalyst is used to both pyrolyze and deoxygenate the biomass within the pyrolysis zone. A source of carbon monoxide is also passed to the pyrolysis reactor. The source of carbon monoxide may comprise a stream of gas that includes carbon monoxide, or a material capable of generating or being converted in carbon monoxide within the pyrolysis zone. The carbon monoxide may be used as a reactant for a water gas shift reaction or as a reducing agent to remove oxygen from oxygenated hydrocarbons. The catalyst preferably comprises iron (III) oxide. 1. A process for producing biomass derived pyrolysis oil , the process comprising:pyrolyzing a carbonaceous biomass feedstock in a pyrolysis zone having a catalyst to provide a pyrolized effluent including oxygenated hydrocarbons;deoxygenating oxygenated hydrocarbons within the pyrolysis zone; andincreasing an amount of carbon monoxide in the pyrolysis zone with a source of carbon monoxide, wherein the source of carbon monoxide is different than the carbonaceous biomass feedstock.2. The process of wherein the catalyst comprises iron (III) oxide.3. The process of wherein the catalyst comprises hematite.4. The process of wherein the catalyst further comprises silicon oxide.5. The process of further comprising reacting water in the presence of the catalyst with carbon monoxide to provide hydrogen gas and carbon dioxide.6. The process of wherein the catalyst comprises a portion of pitch.7. The process of wherein a second portion of the pitch comprises the source of carbon monoxide.8. The process of further comprising regenerating catalyst in a regeneration zone claim 1 , the regeneration zone providing an off gas including carbon monoxide.9. The process of wherein at least a portion of the off gas comprises the source of carbon monoxide.10. A process for producing biomass derived pyrolysis oil claim 8 , the process comprising:passing a carbonaceous biomass feedstock into a pyrolysis zone having a ...

CATALYTIC PROCESS FOR CO-PROCESSING OF CELLULOSIC BIOMASS AND HEAVY PETROLEUM FUELS

Disclosed herein is an economically viable co-process for converting biomass to liquid biohydrocarbon fuels and for upgrading heavy deteriorate petrol-oils to high value transportation fuels. In the process, cellulose, hemi-cellulose and lignin, which are composed of ligno-cellulosic biomass, are converted to the bio-hydrocarbons (alkanes and aromatics) that are currently derived almost exclusively from fossil fuels. The resulted hydrocarbon liquid can be separated against their boiling points for gasoline, diesel and heavy oils. The heavy oils can then cracked into lower molecular weight hydrocarbons. Meanwhile, the co-processed heavy petro-fuels are partially converted into lower molecular weight hydrocarbons that fall in the boiling point range of gasoline and diesel. 1. A process for co-processing of lignocellulosic biomass and heavy petroleum fuels , comprising:mixing lignocellulosic biomass, heated heavy petroleum fuels and a metal oxide based catalyst in a mixer to produce a mixture;{'sub': 2', '2, 'flowing the mixture to a reactor maintained at a pressure in a range from about 101 kPa to about 10 kPa and maintained at a temperature in a range from about 200° C. to about 450° C. and applying external forces to the mixture to produce longitudinal waves and shear stress in the mixture wherein responsively adiabatically erupting bubbles accompanied by high temperature and pressure are produced, and wherein in-situ hydrogen is generated, and wherein lignocellulosic biomass depolymerizes thereby generating a variety of free radicals and intermediates, wherein the free radicals and intermediates react with hydrocarbon molecules in the heavy petroleum fuels such that large hydrocarbon molecules are cracked into smaller hydrocarbon molecules, and a combination of intermediate with hydrocarbon molecules and in which oxygen is eliminated in the form of CO, COand HO;'}withdrawing gaseous products from the reactor to a distillation unit;flowing remaining solids and ...

Wave modes for the microwave induced conversion of coal

A system for converting hydrocarbon materials into a product includes a hydrocarbon feedstock source, a process gas source, an energy generator, and a cylindrical reaction chamber. The reaction chamber has a conductive inner surface that forms a resonant cavity. The resonant cavity is configured to support a standing TM010 electromagnetic wave. The reaction chamber is also configured to receive feedstock from the feedstock source, process gas from the process gas source, and convert the feedstock into a product stream in the presence of the TM010 electromagnetic wave.

CO-PROCESSING OF BIOMASS OIL IN COKER

Systems and methods are provided for co-processing of biomass oil with mineral coker feeds in a coking environment. The coking can correspond to any convenient type of coking, such as delayed coking or fluidized coking. The biomass oil can correspond to biomass oil with a molar ratio of oxygen to carbon of 0.24 or less on a dry basis. Such types of biomass oil can be formed from pyrolysis methods such as hydrothermal pyrolysis, and are in contrast to biomass oils formed from pyrolysis methods such as fast pyrolysis. By using a biomass oil with a molar ratio of oxygen to carbon of 0.24 or less, improved yields of light coker gas oil can be achieved in conjunction with a reduction in the yield of heavy coker gas oil. 1. A method for co-processing biomass , comprising:exposing a biomass oil comprising an oxygen to carbon molar ratio of 0.10 to 0.24 on a dry basis and a feedstock comprising a vacuum resid boiling range fraction to a catalyst in a reactor under coking conditions to form one or more liquid product fractions, the biomass oil comprising 2.5 wt % to 50 wt % of a combined weight of the biomass oil and the feedstock.2. The method of claim 1 , wherein the biomass oil comprises a hydrogen to carbon molar ratio of 1.2 or more.3. The method of claim 1 , wherein the biomass oil comprises an effective molar ratio of hydrogen to carbon of 0.7 or more.4. The method of claim 1 , wherein the biomass oil comprises 1.0 wt % to 20 wt % of oxygen.5. The method of claim 1 , wherein the method further comprises converting a biomass feed under pyrolysis conditions to form the biomass oil.6. The method of claim 5 , wherein the pyrolysis conditions comprise hydrothermal pyrolysis conditions claim 5 , hydropyrolysis conditions claim 5 , catalytic pyrolysis conditions claim 5 , or a combination thereof.7. The method of claim 1 , wherein the coking conditions comprise delayed coking conditions.8. The method of claim 1 , wherein the coking conditions comprise fluidized coking ...

Process for Depolymerizing Coal to Co-Produce Pitch and Naphthalene

A method of depolymerizing coal includes preparing a high temperature depolymerizing medium consisting of heavy hydrocarbon oils and mixing it with coal to form a mixture, performing an optional first distillation at a temperature below 250° C. to recover naphthalene, heating the mixture to a temperature between 350° C. and 450° C. to create a digested coal, centrifuging the digested coal to remove ash and obtain a centrate, and distillation of the centrate into separate fractions. The high temperature depolymerizing medium may be a heavy hydrocarbon with a hydrogen to carbon (H/C) ratio higher than 7.0% and may include liquids chosen from the group consisting of: coal tar distillate, decant oil, anthracene oil, and heavy aromatic oils. The high temperature depolymerizing medium may be blended with an oil, preferably with H/C ratio higher than 10.0%, such as soybean oil, other biomass derived oil, lignin, petroleum oil, pyrolysis oil such that the overall hydrogen-to-carbon mass ratio in a digestion reactor is over 7.0% for the mixture of depolymerizing medium and coal. The depolymerized coal is an aromatic liquid that can itself be, either wholly or in part, a depolymerizing medium so that the process can be repeated.

CONVERSION OF SOLID BIOMASS INTO A LIQUID HYDROCARBON MATERIAL

The present invention provides a process for producing liquid hydrocarbon products from a solid biomass feedstock, said process comprising the steps of: 1. A process for producing liquid hydrocarbon products from a solid biomass feedstock , said process comprising the steps of:a) providing in a first hydropyrolysis reactor vessel a first hydropyrolysis catalyst composition, said composition comprising one or more active metals selected from cobalt, molybdenum, nickel, tungsten, ruthenium, platinum, palladium, iridium and iron on an oxide support, wherein the active metals are present in a partially sulfided form to the extent that the first hydropyrolysis catalyst composition contains sulfur in an amount of from 10 to 90% of a full stoichiometric amount;{'sub': 2', '2', '2', '1', '3, 'b) contacting the solid biomass feedstock with said first hydropyrolysis catalyst composition and molecular hydrogen in said first hydropyrolysis reactor vessel at a temperature in the range of from 350 to 600° C. and a pressure in the range of from 0.50 to 7.50 MPa, to produce a product stream comprising partially deoxygenated hydropyrolysis product, HO, H, CO, CO, C-Cgases, char and catalyst fines;'}c) removing said char and catalyst fines from said product stream;{'sub': 2', '2', '2', '1', '3', '2', '2', '1', '3, 'd) hydroconverting said partially deoxygenated hydropyrolysis product in a hydroconversion reactor vessel in the presence of one or more hydroconversion catalyst and of the HO, CO, CO, H, and C-Cgas generated in step a), to produce a vapour phase product comprising substantially fully deoxygenated hydrocarbon product, HO, CO, CO, hydrogen and C-Cgases.'}2. A process according to claim 1 , wherein the active metals are selected from one or more of cobalt claim 1 , molybdenum claim 1 , nickel claim 1 , tungsten claim 1 , and iron.3. A process according to claim 1 , wherein the hydroconversion catalyst is selected from sulfided catalysts comprising one or more metals from the ...

PROCESS FOR PRODUCING HYDROCARBONS

A process for converting biomass to products is described. Biomass is contacted with hydrogen in the presence of a fluidized bed of hydropyrolysis catalyst in a reactor vessel under hydropyrolysis conditions; and products and char are removed from the reactor vessel. The products leave the fluidized bed at an exit bed velocity, the char has a settling velocity that is less than the exit bed velocity and hydropyrolysis catalyst has a settling velocity that is greater than the exit bed velocity. 2. A process as claimed in wherein the settling velocity of the char is less than 90% of the exit bed velocity.3. A process as claimed in wherein the settling velocity of the char is less than 75% of the exit bed velocity.4. A process as claimed in wherein the settling velocity of the hydropyrolysis catalyst is greater than 110% of the exit bed velocity.5. A process as claimed in wherein the settling velocity of the hydropyrolysis catalyst is greater than 150% of the exit bed velocity.6. A process as claimed in wherein the hydropyrolysis conditions comprise a temperature in the range of from 270° C. to 450° C. and a pressure in the range of from 1 MPa to 7.5 MPa.7. A process as claimed in wherein the biomass is selected from the group consisting of lignin claim 1 , wood claim 1 , algae claim 1 , paper claim 1 , and cardboard.9. A process as claimed in wherein the settling velocity of the char is less than 90% of the exit bed velocity.10. A process as claimed in wherein the settling velocity of the char is less than 75% of the exit bed velocity.11. A process as claimed in wherein the settling velocity of the hydropyrolysis catalyst is greater than 110% of the exit bed velocity.12. A process as claimed in wherein the settling velocity of the hydropyrolysis catalyst is greater than 150% of the exit bed velocity.13. A process as claimed in wherein the settling velocity of the small catalyst particles is less than 90% of the exit bed velocity.14. A process as claimed in wherein the ...

PROCESS FOR PYROLYSIS AND GASIFICATION OF A COAL FEED

A process for gasifying and pyrolyzing coal is described. A first coal feed is pyrolyzed into a coal tar stream and a coke stream in a pyrolysis zone. A second coal feed is gasified in a gasification zone to produce an effluent stream. Contaminants are removed from the effluent stream to provide a purified effluent stream. The purified effluent stream is introduced to the pyrolysis zone. 1. A process comprising:pyrolyzing a first coal feed into a coal tar stream and a coke stream in a pyrolysis zone;gasifying a second coal feed in a gasification zone to produce an effluent stream;removing contaminants from the effluent stream to provide a purified effluent stream; andintroducing the purified effluent stream to said pyrolysis zone.2. The process of wherein the gasification zone is selected from the group consisting of a moving bed gasifier claim 1 , a fluidized bed gasifier claim 1 , and an entrained flow gasifier.3. The process of wherein the second coal feed is pulverized and dry-fed into the gasification zone.4. The process of wherein gasifying the second coal feed takes place at a temperature between about 800° C. and about 1 claim 1 ,400° C.5. The process of wherein the effluent stream comprises hydrogen claim 1 , carbon monoxide claim 1 , carbon dioxide claim 1 , hydrogen sulfide claim 1 , steam claim 1 , or a combination.6. The process of wherein removing contaminants from the effluent stream comprises filtering particulate matter from the effluent stream.7. The process of wherein removing contaminants from the effluent stream comprises removing one or more of carbon dioxide claim 1 , hydrogen sulfide claim 1 , arsenic claim 1 , and mercury.8. The process of wherein removing contaminants comprises performing a water shift gas reaction to generate hydrogen and carbon dioxide from carbon monoxide and steam in the effluent stream.9. The process of further comprising:fractionating the coal tar stream to provide at least a hydrocarbon stream.10. The process of ...

PROCESS FOR PRODUCING HYDROGEN-RICH COAL TAR

A process for producing hydrogen-rich coal tar includes introducing a coal feed into a pyrolysis zone, and contacting the coal feed with a hydrogen donor stream and a multifunctional catalyst in the pyrolysis zone. The multifunctional catalyst includes a hydrogenation function for increasing a hydrogen content of said coal tar stream. The process further includes pyrolyzing the coal feed with the hydrogen donor stream and the multifunctional catalyst to produce a coke stream and a coal tar stream comprising hydrocarbon vapor. 1. A process for producing hydrogen-rich coal tar , comprising:introducing a coal feed into a pyrolysis zone;contacting said coal feed with a hydrogen donor stream and a multifunctional catalyst in said pyrolysis zone, said multifunctional catalyst comprising a hydrogenation function for increasing hydrogen content of said coal tar stream;pyrolyzing said coal feed with the hydrogen donor stream and said multifunctional catalyst to produce a coke stream and a coal tar stream comprising hydrocarbon vapor.2. The process of claim 1 , further comprising:hydrotreating at least a portion of said coal tar stream, wherein said hydrotreating produces water, and the water is recycled to said pyrolysis zone as the hydrogen donor stream.3. The process of claim 1 , further comprising:hydrotreating at least a portion of said coal tar stream, wherein said hydrotreating produces ammonia, and said ammonia is recycled to said pyrolysis zone as said hydrogen donor stream,wherein said multifunctional catalyst further comprises a function for decomposing ammonia to nitrogen and hydrogen, said hydrogen reacting on said hydrogenation function of said multifunction catalyst to increase a hydrogen content of said coal tar stream.4. The process of claim 1 , wherein said hydrogenation function increases said hydrogen content of said coal tar stream by at least partially hydrogenating at least a portion of said hydrocarbon vapor.5. The process of claim 4 , further ...

PROCESS FOR PYROLYSIS OF COAL

A process for pyrolyzing a coal feed is described. The coal feed is pyrolyzed into a coal tar stream and a coke stream in a pyrolysis zone. The coal tar stream is fractionated into at least a pitch stream. The pitch stream is hydrogenated, and the hydrogenated pitch stream is recycled into the pyrolysis zone. The hydrocarbon stream may be processed further by at least one of hydrotreating, hydrocracking, fluid catalytic cracking, alkylation, and transalkylation. 1. A process comprising:pyrolyzing a coal feed into a coal tar stream and a coke stream in a pyrolysis zone;separating the coal tar stream into at least a pitch stream;hydrogenating the pitch stream; andrecycling the hydrogenated pitch stream into the pyrolysis zone.2. The process of wherein hydrogenating the pitch stream comprises contacting the pitch stream with a hydrogenation catalyst consisting of metal selected from the group consisting of Group VI metals (Cr claim 1 , Mo claim 1 , W) claim 1 , Group VII metals (Mn claim 1 , Tc claim 1 , Re) claim 1 , or Group VIII metals (Fe claim 1 , Co claim 1 , Ni claim 1 , Ru claim 1 , Rh claim 1 , Pd claim 1 , Os claim 1 , Ir claim 1 , Pt) and combinations thereof supported on an inorganic oxide claim 1 , carbide or sulfide support claim 1 , including AlO claim 1 , SiO claim 1 , SiO—AlO claim 1 , zeolites claim 1 , non-zeolitic molecular sieves claim 1 , ZrO claim 1 , TiO claim 1 , ZnO claim 1 , and SiC.3. The process of wherein hydrogenating the pitch stream takes place at a temperature between about 250° C. and about 500° C.4. The process of wherein the hydrogenation takes place at a pressure between about 1.72 MPa (about 250 psig) and about 20.7 MPa (about 3 claim 1 ,000 psig).5. The process of wherein separating the coal tar stream further provides a hydrocarbon stream.6. The process of further comprising:recovering at least one product from the hydrocarbon stream.7. The process of further comprising:feeding additional coal feed into the pyrolysis zone; ...

HYDROTREATING PROCESS AND MULTIFUNCTION HYDROTREATER

A multifunction hydrotreater includes a particulate removal zone having a particulate trap to remove particulate contaminants from a coal tar stream and a demetallizing zone including a demetallizing catalyst to remove organically bound metals from the departiculated stream. The demetallizing zone is positioned after the particulate removal zone. The hydrotreater also includes a hydrodesulfurization, hydrodenitrogenation, and hydrodeoxygenation zone positioned after the demetallization zone, which includes at least one hydrodesulfurization, hydrodenitrogenation, and hydrodeoxygenation catalyst to provide a hydrotreated coal tar stream. 1. A multifunction hydrotreater comprising:a particulate removal zone comprising a particulate trap to remove particulate contaminants from a coal tar stream;a demetallizing zone comprising a demetallizing catalyst to remove organically bound metals from the de-particulated stream, the demetallizing zone positioned after the particulate removal zone; anda hydrodesulfurization, hydrodenitrogenation, and hydrodeoxygenation zone comprising at least one hydrodesulfurization, hydrodenitrogenation, and hydrodeoxygenation catalyst to provide a hydrotreated coal tar stream, the hydrodesulfurization, hydrodenitrogenation, and hydrodeoxygenation zone positioned after the demetallizing zone.2. The multifunction hydrotreater of claim 1 , wherein said hydrodesulfurization claim 1 , hydrodenitrogenation claim 1 , and hydrodeoxygenation zone comprises:a first zone comprising a first hydrodesulfurization, hydrodenitrogenation, and hydrodeoxygenation catalyst; anda second zone comprising a second hydrodesulfurization, hydrodenitrogenation, and hydrodeoxygenation catalyst.3. The multifunction hydrotreater of claim 2 , wherein each of said first and second catalysts includes one or more of a nickel-molybdenum catalyst claim 2 , a cobalt-molybdenum catalyst claim 2 , a nickel-tungsten catalyst claim 2 , and a nickel-cobalt-molybdenum catalyst.4. The ...

CONVERSION OF SOLID BIOMASS INTO A LIQUID HYDROCARBON MATERIALS

The present invention provides a process for producing liquid hydrocarbon products from a solid biomass feedstock, said process comprising the steps of: a) providing in a first hydropyrolysis reactor vessel a first hydropyrolysis catalyst composition, said composition comprising one or more active metals selected from cobalt, molybdenum, nickel, tungsten, ruthenium, platinum, palladium, iridium and iron on an oxide support, wherein the one or more active metals are present in an oxidic state; b) contacting the solid biomass feedstock with said first hydropyrolysis catalyst composition and molecular hydrogen in said first hydropyrolysis reactor vessel at a temperature in the range of from 350 to 600° C. and a pressure in the range of from 0.50 to 7.50 MPa, to produce a product stream comprising partially deoxygenated hydropyrolysis product, HO, H, CO, CO, C-Cgases, char and catalyst fines; c) removing said char and catalyst fines from said product stream; d) hydroconverting said partially deoxygenated hydropyrolysis product in a hydroconversion reactor vessel in the presence of one or more hydroconversion catalyst and of the HO, CO, CO, H, and C-Cgas generated in step a), to produce a vapour phase product comprising substantially fully deoxygenated hydrocarbon product, HO, CO, CO, and C-Cgases. 1. A process for producing liquid hydrocarbon products from a solid biomass feedstock , said process comprising the steps of:a) providing in a first hydropyrolysis reactor vessel a first hydropyrolysis catalyst composition, said composition comprising one or more active metals selected from cobalt, molybdenum, nickel, tungsten, ruthenium, platinum, palladium, iridium and iron on an oxide support, wherein the one or more active metals are present in an oxidic state;{'sub': 2', '2', '2', '1', '3, 'b) contacting the solid biomass feedstock with said first hydropyrolysis catalyst composition and molecular hydrogen in said first hydropyrolysis reactor vessel at a temperature in the ...

BUBBLING BED CATALYTIC HYDROPYROLYSIS PROCESS UTILIZINIG LARGER CATALYST PARTICLES AND SMALL BIOMASS PARTICLES FEATURING AN ANTI-SLUGGING REACTOR

This invention relates to a process for thermochemically transforming biomass or other oxygenated feedstocks into high quality liquid hydrocarbon fuels. In particular, a catalytic hydropyrolysis reactor, containing a deep bed of fluidized catalyst particles is utilized to accept particles of biomass or other oxygenated feedstocks that are significantly smaller than the particles of catalyst in the fluidized bed. The reactor features an insert or other structure disposed within the reactor vessel that inhibits slugging of the bed and thereby minimizes attrition of the catalyst. Within the bed, the biomass feedstock is converted into a vapor-phase product, containing hydrocarbon molecules and other process vapors, and an entrained solid char product, which is separated from the vapor stream after the vapor stream has been exhausted from the top of the reactor. When the product vapor stream is cooled to ambient temperatures, a significant proportion of the hydrocarbons in the product vapor stream can be recovered as a liquid stream of hydrophobic hydrocarbons, with properties consistent with those of gasoline, kerosene, and diesel fuel. Separate streams of gasoline, kerosene, and diesel fuel may also be obtained, either via selective condensation of each type of fuel, or via later distillation of the combined hydrocarbon liquid. 1. (canceled)2. A method for hydropyrolyzing an oxygenated organic feedstock , the method comprising:(a) introducing the oxygenated organic feedstock and a fluidizing gas comprising hydrogen into a fluidized bed hydropyrolysis reactor comprising a fluidized bed of solid particles, including catalyst, under hydropyrolysis conditions sufficient to generate product vapors from thermal decomposition and hydropyrolysis of the oxygenated organic feedstock; and(b) recovering from the product vapors a product stream containing substantially fully deoxygenated hydrocarbon species and less than about 4% oxygen by mass;wherein the fluidized bed of solid ...

Producing Liquid Fuel from Organic Material such as Biomass and Waste Residues

A process for producing liquid fuel from biomass feed stock comprising feeding a biomass feedstock into a one stage atmospheric pressure thermo-catalytic plasma gasifier, contacting the feedstock with oxygen or steam or both to obtain a syngas stream; splitting the syngas stream into first and second streams; conveying the first stream to a water gas shift reactor for producing a modified syngas stream containing CO and hydrogen; the second stream bypassing the water gas shift reactor and being added to the modified syngas steam; optionally reforming natural gas by steam methane reforming to produce a synthetic gas and optionally adding the synthetic gas to the water gas shift reactor; thereby obtaining a syngas having a H:CO ratio of about 1:1 to about 2:1; subjecting the syngas to a Fischer Tropsch reaction thereby producing a wax product; and subjecting the product to a hydrogen cracking process to produce liquid fuel; and apparatus therefore. 1. A process for producing liquid fuel from biomass feed stock which comprises:a) feeding a biomass feedstock into a one stage atmospheric pressure thermo-catalytic plasma gasifier, contacting the feedstock with oxygen or oxygen enriched air or steam or mixtures thereof to convert organic components of the biomass into a syngas stream;b) cooling the syngas through a heat exchanger, cleaning it to remove its particulate matter and chemical impurities and compress it from or about atmospheric pressure;c) splitting the syngas stream into a first stream and a second stream; conveying the first stream to a water gas shift reactor for producing a modified syngas stream containing CO and hydrogen;d) the second stream bypassing the water gas shift reactor and being added to the modified syngas steam from the water gas shift reactor;e) optionally reforming natural gas by steam methane reforming to produce a synthetic gas and optionally adding the synthetic gas to the water gas shift reactor;{'sub': '2', 'f) obtaining syngas having a ...

One-Pot Liquefaction Process for Biomass

The present invention discloses a one-pot liquefaction process for biomass. The one-pot liquefaction process for biomass comprises the following steps: preparing a slurry containing a catalyst, a vulcanizing agent and a biomass, and introducing hydrogen into the slurry to carry out a reaction, thereby obtaining a bio-oil wherein the reaction is controlled to be carried out under a pressure of 13-25 MPa and a temperature of 300-500 DEG C.; and the catalyst comprises amorphous alumina or biomass charcoal loading an active component, and the active component comprises one or more selected from oxides of metals of group VIB, group VIIB or group VIII in the periodic table of elements. The process provided by the present invention has high reaction efficiency, no coke formation and high liquid yield. 1. A one-pot liquefaction process for biomass , comprising the following steps:preparing a slurry containing a catalyst, a vulcanizing agent and a biomass, and introducing hydrogen into the slurry to carry out a reaction, wherein the reaction is controlled to be carried out under a pressure of 13-25 MPa and a temperature of 300-500 DEG C., thereby obtaining a bio-oil.2. The one-pot liquefaction process for biomass according to claim 1 , wherein the catalyst comprises:amorphous alumina loading a first active component, orbiomass charcoal loading the first active component,wherein the first active component comprises one or more selected from oxides of metals of group VIB, group VIIB or group VIII in the periodic table of elements.3. The one-pot liquefaction process for biomass according to claim 2 , wherein the catalyst further comprises:amorphous iron oxyhydroxide, and/orbiomass charcoal loading a second active component,wherein the second active component comprises one or more selected from oxides of Mo, W, Fe, Co, Ni and Pd.4. The one-pot liquefaction process for biomass according to claim 1 , wherein the slurry has a biomass content of 10-50 wt % claim 1 , preferably 30-40 ...

Method for Producing Light Oil through Liquefying Biomass

The present invention discloses a method for producing light oil through liquefying biomass. The method comprises the following steps: (1) mixing a biomass, a hydrogenation catalyst and a solvent oil to prepare a biomass slurry; (2) carrying out a first liquefaction reaction with the biomass slurry and hydrogen gas to obtain a first reaction product; (3) carrying out a second liquefaction reaction with the first reaction product and hydrogen gas to obtain a second reaction product; (4) subjecting the second reaction product to a first separation operation to produce a light component and a heavy component; (5) carrying out vacuum distillation on the heavy component to obtain a light fraction; (6) mixing the light component with the light fraction to form a mixture, carrying out a hydrogenation reaction on the mixture to obtain a hydrogenation product; and (7) subjecting the hydrogenation product to fractionation operation to obtain a light oil. The two steps of liquefaction on the biomass, followed by separation, vacuum distillation and hydrogenation reaction enable the yield of the light oil to be increased. 1. A method for producing light oil through liquefying biomass , comprising the following steps:(1) mixing a biomass, a hydrogenation catalyst and a solvent oil to prepare a biomass slurry;(2) carrying out a first liquefaction reaction with the biomass slurry and hydrogen gas to obtain a first reaction product;(3) carrying out a second liquefaction reaction with the first reaction product and hydrogen gas to obtain a second reaction product;(4) subjecting the second reaction product to a first separation operation to produce a light component and a heavy component;(5) carrying out vacuum distillation on the heavy component to obtain a light fraction;(6) mixing the light component with the light fraction to form a mixture, carrying out a hydrogenation reaction on the mixture to obtain a hydrogenation product; and(7) subjecting the hydrogenation product to ...

Method for Direct Liquefaction of Biomass

The present invention discloses a method for direct liquefaction of biomass. The method comprises the following steps: (1) mixing a biomass, a hydrogenation catalyst and a hydrogen-donor solvent to prepare a biomass slurry; (2) carrying out a first liquefaction reaction with the biomass slurry and hydrogen gas to obtain a first reaction product; (3) carrying out a second liquefaction reaction with the first reaction product and hydrogen gas to obtain a second reaction product; (4) subjecting the second reaction product to a first gas-liquid separation at a temperature of 290-460 DEG C. to produce a first liquid phase and a first gas phase; (5) subjecting the first gas phase to a second gas-liquid separation at a temperature of 30-60 DEG C. to obtain a second liquid phase, and mixing the first liquid phase with the second liquid phase to obtain a liquid phase mixture; (6) carrying out a first distillation on the liquid phase mixture to obtain a light fraction and a heavy fraction; and (7) carrying out a second distillation on the heavy fraction to separate out a distillate oil and a residue, wherein the light fraction and the distillate oil are final liquid of the liquefaction. By utilizing the method for direct liquefaction of biomass, the obtained final liquid has a high yield and a low solid content of residue. 1. A method for direct liquefaction of biomass , comprising the following steps:(1) mixing a biomass, a hydrogenation catalyst and a hydrogen-donor solvent to prepare a biomass slurry;(2) carrying out a first liquefaction reaction with the biomass slurry and hydrogen gas to obtain a first reaction product;(3) carrying out a second liquefaction reaction with the first reaction product and hydrogen gas to obtain a second reaction product;(4) subjecting the second reaction product to a first gas-liquid separation at a temperature of 290-460 DEG C. to produce a first liquid phase and a first gas phase;(5) subjecting the first gas phase to a second gas-liquid ...

Biomass liquefaction process, and fuel oils and chemical materials prepared by the same

The present invention relates to the field of biological energy, in particular to a biomass liquefaction process and fuel oil and chemical raw materials prepared by the same. The biomass liquefaction process comprises the following steps: preparing a slurry comprising a first catalyst and a biomass; performing a first hydrogenation reaction by introducing hydrogen to the slurry to obtain a first stage hydrogenation product; performing a second hydrogenation reaction by adding a second catalyst and introducing hydrogen into the first stage hydrogenation product to obtain a second stage hydrogenation product; and subjecting the second stage hydrogenation product to separation operation to obtain a fuel oil and chemical raw material; wherein the first hydrogenation reaction is controlled to have a reaction pressure of 13-25 MPa and a reaction temperature of 200-350° C., and the second hydrogenation reaction is controlled to have a reaction pressure of 13-25 MPa and a reaction temperature of 380-480° C. The present invention provides a biomass liquefaction process with high reaction efficiency and high liquid yield without coke generation.

INTEGRATED PROCESS FOR THE PRODUCTION OF BIOFUELS FROM SOLID URBAN WASTE

Integrated process for the production of biofuels from solid urban waste which comprises: 1. An integrated process for the production of biofuels from solid urban waste which comprises:subjecting said waste to liquefaction obtaining a mixture comprising an oily phase consisting of bio-oil, a solid phase and an aqueous phase;subjecting the mixture obtained from said liquefaction to separation obtaining an oily phase consisting of bio-oil, a solid phase and an aqueous phase; andsubjecting the oily phase consisting of bio-oil obtained from said separation to hydroconversion in slurry phase, in the presence of at least one nanodispersed hydrogenation catalyst;wherein said liquefaction is carried out at a temperature ranging from 150° C. to 350° C., at a pressure ranging from 5 bar to 170 bar, and for a time ranging from 5 minutes to 240 minutes.2. The integrated process for the production of biofuels from solid urban waste according to claim 1 , wherein said solid urban waste is selected from:the organic fraction of solid urban waste deriving from selected collection;prunings deriving from the maintenance of public parks;agribusiness waste products and waste products of large retailers;primary and/or biological sludges produced by urban water treatment plants;or mixtures thereof.3. The integrated process for the production of biofuels from solid urban waste according to claim 1 , wherein said solid urban waste is treated by subjecting it to a preliminary grinding or sizing process before being subjected to said liquefaction.4. The integrated process for the production of biofuels from solid urban waste according to claim 1 , wherein said solid urban waste is wet.5. The integrated process for the production of biofuels from solid urban waste according to claim 4 , wherein said solid urban waste has a water content higher than or equal to 50% by weight with respect to the total weight of said solid urban waste.6. The integrated process for the production of biofuels from ...