СПОСОБ ПРЕВРАЩЕНИЯ ОЛЕФИНА ИЛИ СПИРТА И СПОСОБ ПОЛУЧЕНИЯ ПРОПИЛЕНА ИЛИ АРОМАТИЧЕСКОГО СОЕДИНЕНИЯ

Изобретение относится к способу превращения олефина или спирта и способу получения пропилена или ароматического соединения. Способ превращения олефина или спирта включает этап предварительной обработки, в котором получают проводящий катализатор путем загрузки реактора с псевдоожиженным слоем непроводящим катализатором, содержащим цеолит и/или оксид кремния, и подачи нагретого углеводородного газа в реактор с псевдоожиженным слоем для осаждения углеродистого кокса и нанесения на непроводящий катализатор, и этап превращения олефина или спирта с помощью реакции в псевдоожиженном слое, в котором используют данный проводящий катализатор, где скорость подачи газа составляет 0,40 м/с или менее на стадии предварительной обработки в виде скорости потока газа в реакторе с псевдоожиженным слоем, и скорость подачи газа составляет 0,5 м/с или более на стадии превращения олефина или спирта в виде скорости потока газа в реакторе с псевдоожиженным слоем. Изобретение обеспечивает подавление электростатического ...

КАТАЛИЗАТОРЫ

Изобретение относится к предшественникам катализаторов Фишера-Тропша, содержащим носитель и кобальт на данном носителе, к катализаторам Фишера-Тропша, способу получения предшественников катализаторов и к применению карбоновой кислоты в указанном способе. Предшественник катализатора содержит (i) носитель катализатора, содержащий оксид кремния и 11-18% масс. TiO; и (ii) кобальт на данном носителе катализатора. Другой предшественник содержит (i) носитель катализатора, включающий оксид кремния и TiO; и (ii) 35-60% масс. Co, представленного как CoOна данном носителе катализатора, где среднечисловой диаметр частиц CoOсоставляет меньше чем 12 нм, определенный с помощью XRD, и С-величина логарифмически нормального распределения размера частиц CoOсоставляет от 0,19 до 0,31; или (b) D-величина логарифмически нормального распределения размера частиц составляет от 19 до 23,5. Способ получения предшественника катализатора включает следующие стадии: осаждают раствор или суспензию, содержащую, по меньшей ...

СПОСОБ СИНТЕЗА УГЛЕВОДОРОДОВ

... 1. Способ трехфазного низкотемпературного синтеза Фишера-Тропша, в котором сырьевые Н2 и СО конвертируют в углеводороды и, возможно, их оксигенаты путем введения в контакт Н2 и СО в присутствии в зоне реакции катализатора синтеза Фишера-Тропша на основе железа, при этом молярное отношение Н2:СО в исходном сырье составляет 0,5 и менее 1,0, и активируют катализатор синтеза Фишера-Тропша на основе железа на стадиях, на которых: ! (а) используют катализатор на основе железа, содержащий железо с положительной степенью окисления, и ! (б) в реакторе вводят в контакт катализатор на основе железа с восстановительным газом, выбранным из СО и сочетания Н2 и СО, при температуре восстановления, по меньшей мере, 245°С и ниже 280°С, давлении восстановительного газа выше 0,5 МПа, но не выше 2,2 МПа и часовой объемной скорости (GHSV) всего подаваемого в реактор газа по меньшей мере 6000 мл(Н)/г катализатора/ч, в результате чего восстанавливают в катализаторе железо с положительной степенью окисления. !

КАТАЛИЗАТОР СЕЛЕКТИВНОГО ГИДРИРОВАНИЯ И СПОСОБ ЕГО ПОЛУЧЕНИЯ

... 1. Катализатор, включающий никель на носителе-оксиде алюминия, причем вышеуказанный алюминийоксидный носитель имеет в прокаленном состоянии дифрактограмму, полученную дифрактометрией рентгеновских лучей, включающую спектральные линии, которые соответствуют следующим межплоскостным расстояниям d и относительным интенсивностям l/l0: ! Межплоскостные расстояния, d (10-10 м) Относительные интенсивности, I/I0 (%) 5,03-5,22 1-5 4,56-4,60 1-10 4,06-4,10 1-5 2,80-2,85 5-20 2,73 15-35 2,60 5-10 2,43 35-40 2,29 30-40 1,99 60-95 1,95 25-50 1,79 1-10 1,53 5-10 1,51 5-10 1,41 40-60 1,39 100 1,23-1,26 1-5 1,14 5-10 1,11 1-5 1,04 1-5 1 5-10 0,97 1-5 ! 2. Катализатор по п.1, в котором алюминийоксидный носитель имеет в прокаленном состоянии дифрактограмму, включающую только спектральные линии, которые соответствуют следующим межплоскостным расстояниям и относительным интенсивностям: ! Межплоскостные расстояния, d (10-10 м) Относительные интенсивности, I/I0 (%) 5,41-5,47 0-5 5,03-5,22 1-54,56-4,60 1-10 4,06 ...

СПОСОБ АКТИВАЦИИ КАТАЛИЗАТОРОВ ГИДРООБРАБОТКИ

ПРОМОТИРОВАННЫЙ КАТАЛИЗАТОР СИНТЕЗА ФИШЕРА-ТРОПША, СПОСОБ ЕГО ПОЛУЧЕНИЯ И СПОСОБ СИНТЕЗА УГЛЕВОДОРОДОВ ФИШЕРА-ТРОПША

... 1. Нанесенный на носитель катализатор синтеза Фишера-Тропша, который включает каталитический материал, промотор и материал носителя; причем каталитический материал содержит кобальт в количестве, по меньшей мере, 4% от массы катализатора и, по меньшей мере, часть кобальта обладает каталитической активностью в синтезе Фишера-Тропша; промотор содержит никель, причем количество присутствующего никеля меньше, чем количество кобальта; и материал носителя содержит оксид металла, выбранного или из алюминия, или титана, или циркония. 2. Катализатор по п.1, в котором материал носителя состоит из оксида металла, выбранного или из алюминия, или титана, или циркония. 3. Катализатор по п.1 или 2, в котором материал носителя, по существу, состоит из оксида металла, выбранного или из алюминия, или титана, или циркония. 4. Катализатор по п.1, в котором материал носителя представляет собой альфа- или гамма-оксид алюминия, предпочтительно альфа-оксид алюминия. 5. Катализатор по п.1, в котором материал носителя ...

Verfahren zum Aktivieren eines Katalysators

Verfahren zur Umwandlung von Methanol zu flüssigen Kohlenwasserstoffen.

KATALYTISCHES VERFAHREN ZUR HERSTELLUNG VON LEICHTEN OLEFINEN AUS METHANOL IN EINEM FLUIDISIERTEN BETTREAKTOR

Catalytic reactor treatment process

PROCESS FOR RE-ACTIVATION OF SOLID ACID CATALYST

Fischer-tropsch synthesis

CATALYTIC PROCESS FOR THE CONVERSION OF A SYNTHESIS GAS TO HYDROCARBONS

PROCESS FOR THE PREPARATION OF A CATALYST INTENDED FOR USE IN A FISCHER-TROPSCH REACTION

Catalytic process for the conversion of a synthesis gas to hydrocarbons

PROCESS FOR THE PREPARATION OF A CATALYST INTENDED FOR USE IN A FISCHER-TROPSCH REACTION

Catalytic process for the conversion of a synthesis gas to hydrocarbons

PROCESS FOR THE PREPARATION OF A CATALYST INTENDED FOR USE IN A FISCHER-TROPSCH REACTION

Catalytic process for the conversion of a synthesis gas to hydrocarbons

ACTIVATION OF HYDROGENATION CATALYSTS OF MEANS CARBON MONOXIDE AND USE FROM CATALYSTS TO THE HYDROGENATION

POROUS INORGANIC MACRO STRUCTURES AND PROCEDURES FOR THE PRODUCTION THE SAME

DESULPHURISATION AND FOR THIS SUITABLE SORBENS

Fischer-Tropsch catalysts

Process for activating a hydrotreating catalyst

Fischer-Tropsch catalysts

A method of producing an alumina-supported cobalt catalyst for use in a Fischer-Tropsch synthesis reaction, which comprises: calcining an initial -alumina support material at a temperature to produce a modified alumina support material; impregnating the modified alumina support material with a source of cobalt; calcining the impregnated support material, activating the catalyst with a reducing gas, steam treating the activated catalyst, and activating the steam treated catalyst with a reducing gas.

System and method for pretreatment of solid carbonaceous material

Method for the preparation of a hydrocarbon synthesis catalyst material and the use thereof in a hydrocarbon synthesis process

This invention relates to a method for the preparation of a hydrocarbon synthesis catalyst material, in the form of a hydrocarbon synthesis catalyst precursor and/or catalyst, preferably, a Fischer Tropsch synthesis catalyst precursor and/or catalyst. The invention also extends to the use of a catalyst precursor and/or catalyst prepared by the method according to the invention in a hydrocarbon synthesis process, preferably, a Fischer Tropsch synthesis process. According to this invention, a method for the preparation of a hydrocarbon synthesis catalyst material includes the steps of treating Fe(II) carboxylate in solution with an oxidising agent to convert it to Fe(III) carboxylate in solution under conditions which ensure that such oxidation does not take place simultaneously with any dissolution of Fe(0); and hydrolysing the Fe(III) carboxylate solution resulting from step (iii) and precipitating one or more Fe(III) hydrolysis products.

Process for the preparation of a catalyst intended for use in a Fischer-Tropsch reaction

PATENT OF INVENTION IFP Energies nouvelles 5 PROCESS FOR THE PREPARATION OF A CATALYST INTENDED FOR USE IN A FISCHER-TROPSCH REACTION Inventors: Fabrice DIEHL and Jean-Christophe VIGUIE 10 Abstract The process makes it possible to prepare a catalyst, intended for use in a Fischer-Tropsch reaction. In a reactor I a catalyst support impregnated with a solution of cobalt nitrate is oxidized at 15 a calcining temperature comprised between 4000C and 450C in order to produce a catalyst precursor comprising cobalt oxides. Then, the catalyst precursor is brought into contact in the reduction reactor A with the reducing gas rich in hydrogen and with a low water content , by circulating the flow of reducing gas, so as to reduce the cobalt oxides to Co and to produce water. Then, the water content is reduced to 200 ppmvol of the flow of 20 reducing gas laden with water recovered at the outlet of the reactor A, and at least a part of the flow of reducing gas is recycled to the reactor A. In the process ...

High frequency energy application to petroleum feed processing

A novel mixed metal catalyst, its preparation by co-precipitation, and its use

Catalyst activation and rejuvenation process

AMMONIUM ACTIVATION OF SEOLITES IN THE PRESENCE OF GASEOUS AMMONIA

CATALYST COMPOSITION, ITS PREPARATION AND USE

An unsupported catalyst composition which comprises one or more Group VIb metals, one or more Group VIII metals, and a refractory oxide material which comprises 50 wt% or more titania, on oxide basis, which is prepared by precipitation techniques, finds use in the hydroprocessing of hydrocarbonaceous feedstocks.

OLIGOMERISATION IN THE PRESENCE OF BOTH A TETRAMERISATION CATALYST AND A FURTHER OLIGOMERISATION CATALYST

SLURRY HYDROCARBON SYNTHESIS WITH FRESH CATALYST ACTIVITY INCREASE DURING HYDROCARBON PRODUCTION

Fresh catalyst particles are added to a slurry hydrocarbon synthesis reactor and their activity increased by contact with hydrogen in-situ in the slurry in a catalyst activity increasing means, while the reactor is producing hydrocarbons. The means may be a simple, vertically oriented and hollow tube, open at the top and bottom, into which slurry and a hydrogen treat gas are passed. The treat gas acts a a lift which provides slurry circulation into and out of the means and back into the slurry body, while increasing the activity of the catalyst particles. During the activity increase of the fresh catalyst, partially and reversibly activated catalyst particles are rejuvenated. The activity increasing means may be inside the reactor and at least partially immersed in the slurry or external of the reactor, or both.

IMPROVED CATALYST ACTIVATION METHOD FOR SELECTIVE CAT NAPHTHA HYDRODESULFURIZATION

An improved catalyst activation process for olefinic naphtha hydrodesulfurization. This process maintains the sulfur removal activity of the catalyst while reducing the olefin saturation activity.

PROCESS FOR THE PREPARATION OF HYDROCARBONS

ABSTRACT PROCESS FOR THE PREPARATION OF HYDROCARBONS A C3/C4 fraction obtained as a by-product in the preparation of aromatic gasoline from synthesis gas over a crystalline aluminium or iron silicate comprising catalyst system, is converted into aromatic gasoline by partial oxidation or partial dehydrogenation followed by conversion over a crystalline aluminium or iron silicate catalyst of the partial oxidation or dehydrogenation product.

SYNTHETIC CRYSTALLINE METAL SILICATE AND BOROSILICATE COMPOSITIONS AND PREPARATION THEREOF

Crystalline metal silicates and metal borosilicate compositions exhibit useful catalytic properties when the reaction mixture from which they are prepared includes a metal whose oxide precipitates at a pH above 7 and an amount of urea or other compound which upon hydrolysis releases ammonia. The precipitated metal hydroxide is incorporated into the crystalline composition as it forms. These compositions exhibit the X-ray pattern of a ZSM-5 zeolite and have an aluminum content of less than 100 wppm and a composition expressed in terms of its oxides as follows: < IMG > where R is tetramethyl ammonium cation, ammonium cation, hydrogen cation, an alkali metal cation, metal cation or mixtures thereof, n is the valence of R, M is a metal whose hydroxide precipitates at a pH above 7 and m is the valence of said metal. These crystalline silicates and borosilicates are usefully employed as catalysts in hydrocarbon conversions.

FISCHER-TROPSCH CATALYSTS

A catalyst for use in a Fischer-Tropsch synthesis reaction which comprises cobalt supported on alumina, in which: the catalyst average particle size is in the range 20 to 100 ~m; the specific surface area of the impregnated and calcined catalyst particles is greater than 80 m2/g; the average pore size of the impregnated and calcined catalyst is at least 90.ANG. (9nm); and the pore volume of the impregnated and calcined catalyst is greater than 0.35 cm3/g.

METHOD FOR PRESULFIDING AND PRECONDITIONING OF RESIDUUM HYDROCONVERSION CATALYST

An improved method is described for presulfiding and preconditioning a residuum hydrotreating or hydrocracking catalyst as an integrated part of the hydroconversion process in which catalyst is added on-stream intermittently or continuously without interruption of the hydroconversion process. The method is used to condition, activate, or presulfide fresh or regenerated catalyst prior to its addition to the hydroconversion reactor utilizing product streams from the hydroconversion process.

CATALYST AND PROCESS FOR THE PRODUCTION OF DIESEL FUEL FROM NATURAL GAS, NATURAL GAS LIQUIDS, OR OTHER GASEOUS FEEDSTOCKS

A process is described that operates efficiently to produce diesel fuel blend from hydrogen and carbon monoxide. The process uses a reduced catalyst on a metal oxide catalyst support which are configured to selectively convert the hydrogen and carbon monoxide into a hydrocarbon product stream, wherein the hydrocarbon product stream comprises light gases, diesel fuel and a wax. These are then condensed, and the diesel fuel blended with a petroleum derived fuel, to produce a diesel fuel blend.

PROCESS FOR PRODUCING LOW SULPHUR OXYGEN CONTAINING RENEWABLE OIL

The invention relates to a process for producing an upgraded renewable oil from renewable carbonaceous material(-s) comprising providing a low sulphur oxygen containing renewable crude oil having a sulphur content of less than 0.5 wt % and an oxygen content from about 2.0 wt to about 20 wt %, pressurising the low sulphur oxygen containing renewable crude oil to an operational pressure in the range 20 to 200 bar, adding and mixing hydrogen to the pressurized low sulphur oxygen containing crude oil, heating the oil to an operational temperature in the range 180-410 °C in one or more steps, contacting said oil with at least one heterogeneous catalyst contained in a first reaction zone, contacting the effluent from said first reaction zone with at least one heterogeneous catalyst contained in a second reaction zone, where in at least one of the heterogeneous catalaysts in the first reaction zone and/or the second reaction zone is on a non-suplhided form.

A PROCESS FOR REACTING OXYGEN CARRYING REGENERATED CATALYST PRIOR TO USE IN A FLUIDIZED BED REACTOR

A process to react an oxygen containing regenerated catalyst stream prior to use in a fluidized bed reactor comprising providing a regenerated catalyst stream which comprises at least 0.001 wt% oxygen; reacting the regenerated catalyst stream with a fuel source thereby forming oxides and reducing the amount of oxygen in the regenerated catalyst stream to produce a usable regenerated catalyst stream; and injecting the usable regenerated catalyst stream into a hydrocarbon fluidized bed reactor is provided.

REACTOR FOR USE IN UPGRADING HEAVY OIL ADMIXED WITH A HIGHLY ACTIVE CATALYST COMPOSITION IN A SLURRY

The instant invention relates to a reactor useful in upgrading heavy oils admixed with a catalyst composition in a slurry. The liquid recirculating reactor of this invention employs a dispersed bubble flow regime, which requires a high liquid to gas ratio. A dispersed bubble flow regime results in more even flow patterns, increasing the amount of liquid that can be upgraded in a single reactor.

CATALYSTS

The invention relates to improvements in the design of Fischer-Tropsch catalysts comprising a support and cobalt on the support.

CATALYST ACTIVATION IN FISCHER-TROPSCH PROCESSES

A system for activating Fischer-Tropsch catalyst comprising a reactor having an outlet for overhead gas and operable under conditions whereby a catalyst in a volume of liquid carrier comprising Fischer-Tropsch diesel, hydrocracking recycle oil, or a combination thereof may be activated in the presence of an activation gas; a condenser comprising an inlet fluidly connected to the reactor outlet for overhead gas and comprising a condenser outlet for condensed liquids; and a separation unit comprising an inlet fluidly connected to the condenser outlet and a separator outlet for a stream comprising primarily Fischer-Tropsch diesel; and a recycle line fluidly connecting the separator outlet, a hydrocracking unit, or both to the reactor, whereby Fischer-Tropsch diesel recovered from reactor overhead gas, hydrocracking recycle oil, or a combination thereof may serve as liquid carrier for catalyst in the reactor. A method for activating Fischer-Tropsch catalyst is also provided.

HYDROPROCESSING PROCESS WITH IMPROVED CATALYST ACTIVITY

This invention relates to a hydroprocessing process with improved catalyst activity when hydroprocessing petroleum based feedstock or an oxygen containing feedstock. This invention also relates to a hydrotreating process with improved hydrodesulfurization (HDS) activity of a hydrotreating catalyst such as Co/Mo by co-feeding carbon monoxide or its precursors. Such inventive process confirms that adding a small amount of CO to H2 in a hydrotreater for a few days leads to an increase in product sulfur due to the inhibition of CO on the hydrotreating catalyst such as CO/Mo. However, it has been unexpectedly found that after the CO was removed from the hydrogen stream, product sulfur levels decreased to values below they were before CO addition which means the activity of the hydrotreating catalyst increased after the CO treatment.

AGGLOMERATION-RESISTANT DESULFURIZING PRODUCT

Disclosed herein is an agglomeration-resistant desulfurizing product for removing contaminants from a fluid stream. The agglomeration-resistant desulfurizing product comprising a metal oxide composition for reacting with contaminants and a polymeric crystallization inhibitor for reducing the agglomeration of the desulfurizing product resulting from using the desulfurizing product. A method to produce the agglomeration-resistant desulfurizing product and a method to treat a fluid stream is also disclosed.

PROCESS FOR THE ACTIVATION OF A CATALYST

T 5397 PROCESS FOR THE ACTIVATION OF A CATALYST A Fischer-Tropsch catalyst is activated by a process comprising reducing the catalyst by contact with a hydrogencontaining gas, the hydrogen concentration and the space velocity of the gas contacting the catalyst increasing step-wise or continuously during the activation. The process may be employed to activate a fresh catalyst prior to its use or to regenerate an exhausted or partially exhausted catalyst. The catalyst, once activated, may be used in a process for the preparation of hydrocarbons from carbon monoxide and hydrogen. THl/T5397FF ...

ACTIVATION CONDITIONS TO MAXIMIZE THE HCS ACTIVITY OF SUPPORTED COBALT CATALYSTS

The activity of supported cobalt catalysts for hydrocarbon synthesis is maximized by carrying out the reduction at conditions that keep both the partial pressure of water vapor and the maximum reduction temperature below critical maximum values. For titania supported cobalt catalysts, the preferred maximum water partial pressure is one atmosphere and the preferred maximum reduction temperature is 375.degree.C.

METHOD OF REMOVING SALT FROM ORGANIC LIQUID STI

REACTOR WITH ENRICHED BOILING LAYER, USED WITH RAW MATERIAL QUALITY OF DAMAGED

FISCHER - TROPSCH SYNTHESIS CATALYSTS

APPLICATION OF HIGH FREQUENCY ENERGY FOR PROCESSING OF RAW MATERIAL OIL

DOUBLE CATALYTIC SYSTEM FOR ENRICHMENT OF FLUIDIZED BED FOR PRODUCTION OF PRODUCT OF VACUUM RESIDUES OF HIGHER QUALITY

CATALYST AND METHODS OF PRODUCTION DIESEL FUEL FROM NATURAL GAS, LIQUID POSTS FROM NATURAL GAS OR OTHER GASEOUS RAW MATERIAL

СПОСОБ ГИДРОПЕРЕРАБОТКИ СЫРОЙ НЕФТИ С ИСПОЛЬЗОВАНИЕМ ЖИДКОСТНОГО РЕЦИРКУЛЯЦИОННОГО РЕАКТОРА

Рассматриваемое изобретение относится к способу гидропереработки сырой нефти с использованием жидкостного рециркуляционного реактора, включающему: (а) объединение перед реактором нагретой подаваемой сырой нефти, активной катализаторной пульпы и водородсодержащего газа для образования смеси; (b) пропускание смеси стадии (а) в жидкостной рециркуляционный реактор и поддержание указанной смеси при повышенных температуре и давлении, причём жидкостной рециркуляционный реактор поддерживается в зоне рассеянного пузырькового потока; (с) отвод из восходящего потока реактора через выход в верхней части реактора смеси, включающей продукты и водород, также как непреобразованный материал и катализаторную пульпу, и пропускания указанной смеси к сепаратору до дополнительной обработки; и (d) рециркулирование материала, не прошедшего сверху, посредством трубы с нисходящим потоком. Кроме того, изобретение касается реактора для осуществления указанного способа.

СПОСОБ ГИДРОПЕРЕРАБОТКИ СЫРОЙ НЕФТИ (ВАРИАНТЫ)

Предлагается новая мазутная полностью реакторная система гидропереработки шлама, которая позволяет катализатору, непреобразованной нефти и преобразованной нефти циркулировать в непрерывной смеси по всему реактору без застаивания смеси. Смесь частично разделяется внутри реакторов для отвода только продуктов и водородного газа, в то же время позволяя непреобразованной нефти и катализаторной пульпе продолжать передвигаться в следующий последовательный реактор. Часть непреобразованной нефти затем преобразуется в более низкокипящие углеводороды в очередной раз, создавая смесь непреобразованной нефти, продуктов, водорода и катализаторной пульпы. Дополнительная гидрообработка может происходить в дополнительных реакторах, полностью преобразовывая нефть. Дополнительная нефть может быть добавлена в промежуточной стадии через вход подачи, по возможности в комбинации со шламом. Нефть может быть поочередно частично преобразована, оставляя высоко концентрированный катализатор в непреобразованной нефти ...

ПРОЦЕСС ФИШЕРА-ТРОПША

В изобретении описан способ превращения синтез-газа в углеводороды, в частности в углеводороды в C5-С60 диапазоне, особенно подходящем для применения в качестве жидких моторных топлив, в суспензионном реакторе в присутствии катализатора Фишера-Тропша, содержащего кобальт и оксид цинка, при осуществлении которого перед контактированием с синтез-газом в суспензионном реакторе катализатор Фишера-Тропша активируют восстановительным газом, состоящим из водорода и инертного газа, при температуре от 330 до 400°С.

СПОСОБ ПОВЫШЕНИЯ КАЧЕСТВА ТЯЖЕЛОГО МАСЛА С ИСПОЛЬЗОВАНИЕМ ВЫСОКОАКТИВНОГО СУСПЕНДИРОВАННОГО КАТАЛИЗАТОРНОГО СОСТАВА

Настоящее изобретение направлено на способ повышения качества тяжелых масел с использованием суспендированного катализаторного состава. Суспендированный состав готовят с помощью последовательности этапов, включающей в себя смешивание оксида металла VI B группы и водного раствора аммиака с образованием водной смеси и сульфидирование смеси с образованием суспензии. Суспензию затем активируют металлом VIII группы. Последующие этапы включают в себя смешивание суспензии с углеводородным маслом и соединение получающейся в результате смеси с водородом (при условиях, которые сохраняют воду в жидкой фазе) с получением активного суспендированного катализатора.

DOUBLE CATALYTIC SYSTEM FOR ENRICHMENT OF FLUIDIZED BED FOR PRODUCTION OF PRODUCT OF VACUUM RESIDUES OF HIGHER QUALITY

АКТИВАЦИЯ КАТАЛИЗАТОРА В ПРОЦЕССАХ ФИШЕРА-ТРОПША

Система активации катализатора Фишера-Тропша, состоящая из реактора с выпускным отверстием для отбираемого сверху газа, функционирующего в режиме, благодаря которому катализатор в объеме жидкого носителя, содержащего дизельное топливо по Фишеру-Тропшу, рециркулированный продукт гидрокрекинга нефти или их комбинацию, может активироваться в присутствии активирующего газа; конденсатора, содержащего впускное отверстие, связанное через текучую среду с выпускным отверстием реактора для отбираемого сверху газа, и выпускное отверстие для конденсированных жидкостей; и сепаратора, содержащего впускное отверстие, связанное через текучую среду с выпускным отверстием конденсатора, и выпускное отверстие для потока, содержащего главным образом дизельное топливо по Фишеру-Тропшу; и рециркуляционного трубопровода, связывающего через текучую среду выпускное отверстие сепаратора, установку для гидрокрекинга или то и другое с реактором, благодаря чему дизельное топливо по Фишеру-Тропшу, извлеченное из отбираемого ...

ПРОЦЕСС ПОЛУЧЕНИЯ КАТАЛИЗАТОРА НА ОСНОВЕ КОБАЛЬТА НА ПОДКЛАДКЕ ДЛЯ СИНТЕЗА ФИШЕРА-ТРОПША

Процесс получения катализатора на основе кобальта на подкладке для синтеза Фишера-Тропша, который включает: на первом этапе активации – обработку предшественника катализатора газом-восстановителем при первой скорости нагревания HR1, пока предшественник не достигнет температуры Т1, где 80°C≤T1≤180 °C, чтобы получить частично обработанный предшественник катализатора, на втором этапе активации – обработку частично обработанного предшественника катализатора газом-восстановителем при второй скорости нагревания HR2, где 0≤HR2HR2, пока частично восстановленный предшественник катализатора не достигнет температуры Т2, и выдержку частично восстановленного предшественника катализатора при ...

НАСЫПНОЙ КАТАЛИЗАТОР ГИДРОПЕРЕРАБОТКИ И СПОСОБЫ ЕГО ИЗГОТОВЛЕНИЯ

Изобретением обеспечивается насыпной катализатор гидропереработки. Изобретением обеспечивается способ изготовления насыпного катализатора гидропереработки. Катализатор гидропереработки имеет формулу (Rp)i(Mt)a(Lu)b(Sv)d(Cw)e(Hx)f(Oy)g(Nz)h, в которой М означает, по меньшей мере, переходный металл; L означает, по меньшей мере, переходный металл, отличный от переходного металла М; t, u, v, w, х, у, z означают общий заряд каждого из компонентов (М, L, S, С, Н, О и N, соответственно); R является необязательным, в одном из вариантов осуществления изобретения R представляет собой лантаноид; 0<=i<=l; pi+ta+ub+vd+we+xf+yg+zh=0; 0 Подробнее

СПОСОБ АКТИВАЦИИ УСИЛЕННОГО ЖЕЛЕЗНОГО КАТАЛИЗАТОРА ДЛЯ СУСПЕНЗИОННЫХ РЕАКТОРОВ

Способ активации железного катализатора для процесса Фишера-Тропша путем введения инертного газа в реактор, содержащий суспензию катализатора при первой температуре, увеличения температуры реактора от первой температуры до второй температуры с первой скоростью изменения температуры, при этом вторая температура находится в диапазоне от примерно 150 до 250°С, введения синтез-газа, имеющего соотношение Н2:СО, в реактор с объемной скоростью и увеличения температуры реактора от второй температуры до третьей температуры с второй скоростью изменения температуры, при этом третья температура находится в диапазоне от примерно 270 до 300°С. Железный катализатор для процесса Фишера-Тропша может представлять собой осажденный железный катализатор без подложки, получение которого также предложено.

КАТАЛИЗАТОРЫ ФИШЕРА-ТРОПША

Способ приготовления кобальтового катализатора на алюмооксидном носителе для использования в реакции синтеза Фишера-Тропша, который включает прокаливание исходного материала γ-алюмооксидного носителя при температуре, позволяющей получать материал модифицированного алюмооксидного носителя; пропитку материала модифицированного алюмооксидного носителя источником кобальта; прокаливание пропитанного материала носителя; активирование катализатора восстановительным газом; обработку активированного катализатора водяным паром и активирование обработанного водяным паром катализатора восстановительным газом.

ПРОЦЕСС ФИШЕРА-ТРОПША

В заявке описан способ превращения синтез-газа в углеводороды, в частности в углеводороды в C5-С60диапазоне, особенно подходящем для применения в качестве жидких моторных топлив, в суспензионном реакторе в присутствии катализатора Фишера-Тропша, содержащего кобальт и оксид цинка, при осуществлении которого перед контактированием с синтез-газом в суспензионном реакторе катализатор Фишера-Тропша активируют восстановительным газом, состоящим из водорода и инертного газа, при температуре от 330 до 400°С.

ПРОЦЕСС ДЛЯ ПОВЫШЕНИЯ КАЧЕСТВА ТЯЖЕЛОГО МАСЛА С ИСПОЛЬЗОВАНИЕМ ВЫСОКОАКТИВНОГО СУСПЕНДИРОВАННОГО КАТАЛИЗАТОРНОГО СОСТАВА

Настоящее изобретение направлено на способ повышения качества тяжелых масел с использованием суспендированного катализаторного состава. Суспендированный состав готовят с помощью последовательности этапов, включающей в себя смешивание оксида металла VI В группы и водного раствора аммиака с образованием водной смеси, и сульфидирования смеси с образованием суспензии. Суспензию затем активируют металлом VIII группы. Последующие этапы включают в себя смешивание суспензии с углеводородным маслом и соединение получающейся в результате смеси с водородом и вторым углеводородным маслом, имеющим более низкую вязкость, чем первое масло. Таким образом получается активный катализаторный состав.

СПОСОБ АКТИВАЦИИ КАТАЛИЗАТОРА ПРОЦЕССА ФИШЕРА-ТРОПША

Изобретение относится к отрасли катализа процесса Фишера-Тропша, в частности активации катализатора Фишера-Тропша. Способ активации катализатора процесса Фишера-Тропша на основе железа, который содержит железо в состоянии позитивного окисления, контактирование в реакторе указанного катализатора на основе железа с восстановительным газом, выбранным из группы, которая состоит из СО и комбинации Н2 и CO, при молярном соотношении Н2 и CO от 100:1 до 1:100, при температуре как минимум 245 °C и ниже 280 °C, при давлении восстановительного газа более 0,5 МПа и не более чем 2,2 МПа и при среднечасовой скорости (GHSV) подачи всего газа, который подают в реактор, как минимум 6000 мл(норм.)/г кат./час, с восстановлением железа, которое находится в состоянии окисления в катализаторе.

СПОСОБ АКТИВАЦИИ И ВОССТАНОВЛЕНИЯ АКТИВНОСТИ КАТАЛИЗАТОРА

КАТАЛИЗАТОРЫ СИНТЕЗА ФИШЕРА-ТРОПША

Предлпгпется катализатор для использования в процессе синтеза Фишера-Тропша, содержащий кобальт, нанесенный на оксид алюминия, в котором средний размер частиц катализатора составляет от 20 до 100 мкм; удельная площадь поверхности пропитанных и прокаленных частиц катализатора больше чем 80 м2/г; средний размер пор пропитанного и прокаленного катализатора составляет по меньшей мере 90Å (9 нм) и объем пор пропитанного и прокаленного катализатора больше чем 0,35 см3/г.

СПОСОБ УДАЛЕНИЯ СОЛИ ИЗ ОРГАНИЧЕСКОЙ ЖИДКОСТИ

Изобретение относится к способу удаления соли из органической жидкости в процессе переработки органического сырья путем подачи первого импульса электромагнитного излучения (30) на органическое сырье, достаточного для нагревания воды, содержащейся в органическом сырье, для увеличения растворимости соли в воде. Подают второй импульс, достаточный для испарения части каждой из капель воды, содержащей соль, для образования водного комплекса жидкость-пар и перемещения водного комплекса жидкость-пар, содержащего соль, к поверхности органического сырья с образованием жидкого комплекса. Удаляют жидкий комплекс из органической жидкости.

ПРИМЕНЕНИЕ ВЫСОКОЧАСТОТНОЙ ЭНЕРГИИ ДЛЯ ПЕРЕРАБОТКИ НЕФТЯНОГО СЫРЬЯ

Изобретение относится к способу и устройству для сохранения активности катализатора (10) в процессе переработки органического сырья (22) путем подачи импульсов электромагнитного излучения (30) на катализатор в реакторе (24). Подача импульсов избирательно нагревает и охлаждает катализатор и может регулировать относительное внутреннее давление частиц катализатора, чтобы стимулировать ускорение массообмена макромолекул нефти через поверхность и поры частиц катализатора. Это позволяет удалять крекированные молекулы нефти из частиц катализатора. Подача электромагнитных импульсов позволяет также регулировать активность катализатора. Под действием электромагнитного излучения уменьшается образование кокса на катализаторе и увеличивается срок работы катализатора в реакторе.

СПОСОБ ПОЛУЧЕНИЯ КОБАЛЬТОВЫХ КАТАЛИЗАТОРОВ НА НОСИТЕЛЕ ИЗ ДИОКСИДА ТИТАНА

Катализаторы, содержащие кобальт на носителе из диоксида титана, получают смешиванием вместе частиц твердого носителя из диоксида титана и водного раствора аминокарбоната кобальта и нагревом до повышенной температуры, достаточной для осуществления разложения аминокарбоната кобальта и осаждения разновидностей кобальта на носитель. Катализаторы применимы при гидрировании и в реакциях Фишера-Тропша.

СПОСОБ ОБЕЗВОЖИВАНИЯ ОРГАНИЧЕСКОГО СЫРЬЯ

Предлагается способ обезвоживания органического сырья, заключающийся в том, что подают импульс электромагнитного излучения на органическое сырье, достаточный для испарения по меньшей мере части капель воды, содержащейся в органическом сырье, устанавливают продолжительность импульса в пределах от 10-6 до 100 с, удаляют водный комплекс из органического сырья.

PROCEDURE OF STARTING UP, INTENDED FOR METHOD FISCHER - TROPSCH

ВЫСОКОАКТИВНАЯ КАТАЛИТИЧЕСКАЯ КОМПОЗИЦИЯ В ВИДЕ СУСПЕНЗИИ

Настоящее изобретение направлено на получение каталитической композиции в виде суспензии. Каталитическая композиция в виде суспензии получена в результате последовательности стадий, включающих в себя смешивание оксида металла VIB группы и водного раствора аммиака с образованием водной смеси и сульфидирование смеси с образованием суспензии. Затем коллоидную суспензию активируют с соединением металла VIII группы. Последующие стадии включают в себя смешивание суспензии с углеводородным маслом и объединение полученной в результате смеси с газом водорода (в условиях, при которых сохраняется вода в жидкой фазе) с формированием при этом активной каталитической композиции.

METHOD OF PRODUCING ACTIVATED CATALYST FOR REACTION OF SYNTHESIS OF FISCHER - TROPSCH, METHOD OF PRODUCING CATALYST SUSPENSION AND METHOD OF FEEDING CATALYST SUSPENSION IN FISCHER - TROPSCH SYNTHESIS REACTOR

APPLICATION OF HIGH FREQUENCY ENERGY FOR PROCESSING OF RAW MATERIAL OIL

CATALYST AND METHODS FOR PREPARING DIZELNGO FUEL FROM NATURAL GAS, LIQUID POSTS FROM NATURAL GAS OR OTHER GASEOUS RAW MATERIAL

HYDROPROCESSING BULK CATALYST AND PROCESSES FOR PREPARATION THEREOF

DESULFURIZATION AND NOVEL SORBENTS FOR SAME

PROCESS FOR THE PREPARATION OF A CATALYST INTENDED FOR USE IN A FISCHER-TROPSCH REACTION

UPGRADED EBULLATED BED REACTOR WITH INCREASED PRODUCTION RATE OF CONVERTED PRODUCTS

Oligomerization Of Alpha Olefins Using Metallocene-ssa Catalyst Systems And Use Of The Resultant Polyalphaolefins To Prepare Lubricant Blends

This disclosure provides for alpha olefin oligomers and polyalphaolefins (or PAOs) and methods of making the alpha olefin oligomers and PAOs. This disclosure encompasses metallocene- based alpha olefin oligomerization catalyst systems, including those that include at least one metallocene and an activator comprising a solid oxide chemically-treated with an electron withdrawing anion. The alpha olefin oligomers and PAOs prepared with these catalyst systems can have a high viscosity index combined with a low pour point, making them particularly useful in lubricant compositions and as viscosity modifiers.

Use of molecular sieves for the conversion of oxygenates to olefins

COMPOSITIONS CRISTALLINES SYNTHETIQUES DE SILICATE ET DE BOROSILICATE METALLIQUES, LEUR PROCEDE DE PREPARATION ET LEURS APPLICATIONS

L'INVENTION CONCERNE UNE CLASSE NOUVELLE DE COMPOSITIONS CRISTALLINES DE SILICATE ET DE BOROSILICATE METALLIQUES. ON PREPARE CES COMPOSITIONS PAR UN PROCEDE QUI EXIGE QUE LA QUANTITE D'ALUMINIUM DANS LE MELANGE REACTIONNEL SOIT SOIGNEUSEMENT REGLEE ET, EN OUTRE, QUE LE MELANGE CONTIENNE A UN METAL DONT L'HYDROXYDE PRECIPITE A UN PH SUPERIEUR A 7 ET B.DE L'UREE OU UN COMPOSE QUI LIBERE DE L'AMMONIAC EN S'HYDROLYSANT, LA LIBERATION D'AMMONIAC CAUSANT LA FORMATION DE L'HYDROXYDE DU METAL DANS LE MELANGE. CES COMPOSITIONS PEUVENT ETRE UTILISEES COMME CATALYSEURS DANS DES PROCEDES DE CONVERSION CATALYTIQUE.

CATALYST Of SELECTIVE HYDROGENATION AND ITS METHOD OF PREPARATION

METHOD OF CATALYST PREPARATION INTENDED TO BE BROUGHT INTO ŒUVRE IN A FISCHER-TROPSCH REACTION.

Hydrotreating catalyst comprising Group VIII and VIB metals on a refractory oxide support comprises an organic compound comprising two thiol groups separated by a ketone- or ether-functional hydrocarbon group

L'invention concerne un catalyseur d'hydroconversion d'hydrocarbures, comprenant un support à base d'au moins un oxyde réfractaire, au moins un métal du groupe VIII et au moins un métal du groupe VIB, caractérisé en ce qu'il comprend en outre au moins un composé organique comportant au moins deux fonctions thiol séparées par au moins un groupement oxygéné de formule (I) : HS-CxHyOz-SH (I) dans laquelle x est un nombre entier de 1 à 20, de préférence de 2 à 9, par exemple x est égal à 6, y est un nombre entier de 2 à 60, de préférence de 4 à 12, et z est un nombre entier de 1 à 10, de préférence de 1 à 6. Procédé de préparation et procédé d'activation dudit catalyseur, et utilisation du catalyseur activé pour l'hydrotraitement et/ou l'hydrocraquage d'hydrocarbures.

CATALYTIC PROCESS FOR the CONVERSION Of a GAS OF SYNTHESIS INTO HYDROCARBONS

Procédé catalytique de conversion au moins partielle d'un mélange gazeux contenant du CO et du H2 en mélange d'hydrocarbures, comportant une étape de mise en contact dudit mélange gazeux avec un catalyseur solide, ledit catalyseur solide comportant - un support poreux comportant un matériau composite comportant du SiC et un carbure de titane (composite appelé « SiC/TiC ») et/ou un oxyde de titane (composite appelé « SiC/TiO2 »), et - une phase active. Le support peut être préparé sous la forme de grains, billes, ou extrudés, ou sous la forme de cylindres ou plaques de mousse alvéolaire. Sa teneur molaire en titane par rapport à la somme molaire Si + Ti est avantageusement comprise entre 0,5% et 15%.

SYNTHETIC CRYSTALLINE COMPOSITIONS OF METAL SILICATE AND BOROSILICATE, THEIR METHOD OF PREPARATION AND THEIR APPLICATIONS

저품질 탄화수소질 공급원료의 수소첨가전환 방법

... 본 발명은 슬러리 촉매 조성물을 사용하는 저품질 탄소질 공급원료의 업그레이드 방법에 관한 것이다. 분산된 활성 촉매에 대한 전구체로서 특정 유기금속 화합물의 사용은 코크스 형성 감소를 가능하게 한다.

SELECTIVE HYDROGENATION CATALYST AND METHOD FOR PREPARING SAME

SELF-SULFIDING OF GUARD REACTOR CATALYST FOR SOLVENT ASSISTED TAR CONVERSION PROCESSES

METHODS AND PRODUCTS FOR CONVERTING CARBON DIOXIDE TO ONE OR MORE SMALL ORGANIC COMPOUNDS

Method for the preparation of SAPO molecular sieves and SAPO molecular sieves

FISCHER-TROPSCH SYNTHESIS

A process for the preparation of an F-T catalyst in which the presence of alkaline earth metals is minimised in the support itself and in the processing conditions, in order to provide a catalyst with an alkaline earth metal content of less than 2000 ppm.

HIGHLY ACTIVE SLURRY CATALYST COMPOSITION

The instant invention is directed to the preparation of a catalyst composition suitable for the hydroconversion of heavy oils. The catalyst composition is prepared by a series of steps, involving mixing a group VIB metal oxide and aqueous ammonia to form an aqueous mixture, and sulfiding the mixture to form a slurry. The slurry is then promoted with a Group VIII metal. Subsequent steps involve mixing the slurry with a hydrocarbon oil and combining the resulting mixture with hydrogen gas and a second hydrocarbon oil having a lower viscosity than the first oil. An active catalyst composition is thereby formed.

Hydroprocessing catalysts and methods for making thereof

An improved process to make a slurry catalyst for the upgrade of heavy oil feedstock is provided. In the process, at least a metal precursor feedstock is portioned and fed in any of the stages: the promotion stage; the sulfidation stage; or the transformation stage of a water-based catalyst precursor to a slurry catalyst. In one embodiment, the promoter metal precursor feedstock is split into portions, the first portion is for the sulfiding step, the second portion is for the promotion step; and optionally the third portion is to be added to the transformation step in the mixing of the sulfided promoted catalyst precursor with a hydrocarbon diluent to form the slurry catalyst. In another embodiment, the Primary metal precursor feedstock is split into portions.

Process for hydrocracking a hydrocarbon feed in the presence of a sulphide catalyst prepared using a cyclic oligosaccharide

Hydrocracking a hydrocarbon feed in the presence of a catalyst comprising an acidic support and an active phase formed from at least one metal from group VIII and at least one metal from group VIB, said catalyst being prepared using a process comprising, in succession: contacting a pre-catalyst comprising said metal from group VIII, said metal from group VIB and said acidic support with a cyclic oligosaccharide of at least 6α-(1,4)-bonded glucopyranose subunits; contacting the acidic support with a solution containing a precursor of metal from group VIII, a precursor of said metal from group VIB and a cyclic oligosaccharide of at least 6α-(1,4)-bonded glucopyranose subunits; and contacting acidic support with a cyclic oligosaccharide of at least 6α-(1,4)-bonded glucopyranose subunits followed by a second contacting acidic solid with a precursor of metal from group VIII and a precursor of metal from group VIB; drying; heat treatment; sulphurization.

Catalyst treatment

A method of preparing a Fischer-Tropsch catalyst for handling, storage, transport and deployment, including the steps of impregnating a porous support material with a source of cobalt, calcining the impregnated support material activating the catalyst, and passivating the activated catalyst.

Method for efficiently operating an ebbulated bed reactor and an efficient ebbulated bed reactor

A hydroprocessing method and system involves introducing heavy oil and well-dispersed metal sulfide catalyst particles, or a catalyst precursor capable of forming the well-dispersed metal sulfide catalyst particles in situ within the heavy oil, into a hydroprocessing reactor. The well-dispersed or in situ metal sulfide catalyst particles are formed by 1) premixing a catalyst precursor with a hydrocarbon diluent to form a precursor mixture, 2) mixing the precursor mixture with heavy oil to form a conditioned feedstock, and 3) heating the conditioned feedstock to decompose the catalyst precursor and cause or allow metal from the precursor to react with sulfur in the heavy oil to form the well-dispersed or in situ metal sulfide catalyst particles. The well-dispersed or in situ metal sulfide catalyst particles catalyze beneficial upgrading reactions between the heavy oil and hydrogen and eliminates or reduces formation of coke precursors and sediment.

Metal nanoparticle deposited inorganic nanostructure hybrids, uses thereof and processes for their preparation

This invention relates to a hybrid component comprising at least one nanoparticle of inorganic layered compound (in the form of fullerene-like structure or nanotube), and at least one metal nanoparticle, uses thereof as a catalyst, (e.g. photocatalysis) and processes for its preparation.

High Density Cyclic Fuels Derived From Linear Sesquiterpenes

A method to generate cyclic hydrocarbons from farnesene to increase both the density and net heat of combustion of the product fuels. The high density hydrocarbons produced by this method have applications for missile, UAV, jet, and diesel propulsion.

PROCESS FOR THE PREPARATION OF A CATALYST INTENDED FOR USE IN A FISCHER-TROPSCH REACTION

In a reactor I a catalyst support impregnated with a solution of cobalt nitrate is oxidized at a calcining temperature comprised between 400° C. and 450° C. in order to produce a catalyst precursor comprising cobalt oxides. This catalyst precursor is contacted in reduction reactor A with reducing gas rich in hydrogen and with a low water content, by circulating the flow of reducing gas, so as to reduce the cobalt oxides to Co and to produce water. Water content is reduced to 200 ppmvol of the flow of reducing gas laden with water recovered at the outlet of the reactor A, and at least a part of the flow of reducing gas is recycled to the reactor A. In the process, the reducing gas is maintained at a water content less than 10,000 ppmvol in reactor A. 1. Process for the preparation of a catalyst intended for utilization in a Fischer-Tropsch reaction , in which the following successive stages are carried out:a) A support impregnated with a solution of cobalt nitrate is provided,b) said support impregnated with a cobalt nitrate solution is oxidized at a calcining temperature comprised between 400° C. and 450° C. in order to produce a catalyst precursor comprising cobalt oxides,c) a reducing gas is provided, comprising at least 99% by volume of hydrogen and less than 200 ppmvol of water,d) said catalyst precursor is brought into contact with the reducing gas by circulating the flow of reducing gas over a bed of said catalyst precursor, so as to reduce the cobalt oxides to metallic cobalt in order to produce a reduced catalyst and a flow of reducing gas laden with water,e) the water content of the flow of reducing gas laden with water recovered in stage d) is reduced, so as to produce a flow of reducing gas comprising less than 200 ppmvol of water, thenf) at least a part of the flow of reducing gas is recycled to stage d),process in which in staged) the reducing gas is maintained at a water content of less than 10,000 ppmvol.2. Process according to in which claim 1 , in ...

Fischer-tropsch process using reductively-activated cobalt catalyst

A process for the conversion of a feed comprising a mixture of hydrogen and carbon monoxide to hydrocarbons, the hydrogen and carbon monoxide in the feed being present in a ratio of from 1:9 to 9:1 by volume, the process comprising the steps of: pre-treating a catalyst composition comprising titanium dioxide support and oxidic cobalt or a cobalt compound decomposable thereto, for a period of from 1 to 50 hours, with a hydrogen gas-containing stream comprising less than 10% carbon monoxide gas by volume of carbon monoxide gas and hydrogen gas, to form a reductively-activated catalyst; and contacting the feed at elevated temperature and atmospheric or elevated pressure with the reductively-activated catalyst; wherein the step of pre-treating the catalyst composition is conducted within a temperature range of from 200° C. to less than 300° C., preferably from 220° C. to 280° C., more preferably from 250° C. to 270° C.

SYSTEMS AND METHODS FOR HYDROPROCESSING HEAVY OIL

A system and method for preparing and conditioning a heavy oil feedstock for hydroprocessing in a hydroprocessing system includes forming metal sulfide catalyst particles in situ within the heavy oil feedstock. The metal sulfide catalyst particles are formed in situ by (1) premixing a catalyst precursor with a hydrocarbon diluent to form a diluted precursor mixture, (2) mixing the diluted precursor mixture with the heavy oil feedstock to form a conditioned feedstock, and (3) heating the conditioned feedstock to decompose the catalyst precursor and cause or allow metal from the precursor to react with sulfur in the heavy oil feedstock to form metal sulfide catalyst particles in situ in the heavy oil feedstock. The in situ formed metal sulfide catalyst particles catalyze beneficial upgrading reactions between the heavy oil feedstock and hydrogen and eliminates or reduces formation of coke precursors and sediment. 1. A system for preparing and conditioning a heavy oil feedstock for hydroprocessing in a hydroprocessing system , comprising:a catalyst precursor;a hydrocarbon diluent;a heavy oil feedstock separate from the hydrocarbon diluent;a first mixing vessel configured for receiving and mixing the catalyst precursor with the hydrocarbon diluent below a temperature at which a significant portion of the catalyst precursor decomposes to form a diluted precursor mixture comprising mixture products of the catalyst precursor and the hydrocarbon diluent;a second mixing vessel, downstream from the first mixing vessel, configured for receiving and mixing the diluted precursor mixture with the heavy oil feedstock without heating to a temperature at which a substantial portion of the catalyst precursor decomposes to form a conditioned feedstock comprising mixture products of the catalyst precursor, the hydrocarbon diluent, and the heavy oil feedstock; anda heater, downstream from the second mixing vessel and upstream from a hydroprocessing reactor and/or that comprises the ...

Catalyst Activation in Fischer-Tropsch Processes

A system for activating Fischer-Tropsch catalyst comprising a reactor having a reactor outlet for overhead gas and operable under suitable conditions whereby a catalyst in a volume of liquid carrier comprising Fischer-Tropsch diesel, hydrocracking recycle oil, or a combination thereof may be activated in the presence of an activation gas; a condenser comprising an inlet fluidly connected to the reactor outlet for overhead gas and comprising a condenser outlet for condensed liquids; and a separation unit comprising an inlet fluidly connected to the condenser outlet and a separator outlet for a stream comprising primarily Fischer-Tropsch diesel; and a recycle line fluidly connecting the separator outlet, a hydrocracking unit, or both to the reactor, whereby Fischer-Tropsch diesel recovered from the reactor overhead gas, hydrocracking recycle oil, or a combination thereof may serve as liquid carrier for catalyst in the reactor. A method for activating Fischer-Tropsch catalyst is also provided. 1. A method for activating a Fischer-Tropsch catalyst , the method comprising:contacting a catalyst with a gas, in the presence of a liquid carrier comprising hydrocracking recycle oil in an activation reactor, wherein the gas is a carbon monoxide-rich activation gas consisting essentially of synthesis gas having a molar ratio of hydrogen to carbon monoxide in the range of from about 0.5 to about 1.5, wherein the catalyst is a supported Fischer-Tropsch catalyst and is combined as a slurry with at least a portion of the liquid carrier prior to introduction thereof into the activation reactor;operating the activation reactor under activation conditions whereby the catalyst is activated, wherein said activation reactor comprises a heat transfer structure fluidly connected to a steam drum configured to preheat the catalyst activation reactor to operating temperature or maintain a temperature or temperature profile within the activation reactor or control the heating rate;removing an ...

A process for reacting oxygen carrying regenerated catalyst prior to use in a fluidized bed reactor

A process to react an oxygen containing regenerated catalyst stream prior to use in a fluidized bed reactor comprising providing a regenerated catalyst stream which comprises at least 0.001 wt % oxygen; reacting the regenerated catalyst stream with a fuel source thereby forming oxides and reducing the amount of oxygen in the regenerated catalyst stream to produce a usable regenerated catalyst stream; and injecting the usable regenerated catalyst stream into a hydrocarbon fluidized bed reactor is provided.

SUPERCRITICAL REACTOR SYSTEMS AND PROCESSES FOR PETROLEUM UPGRADING

Provided herein are supercritical upgrading reactors and reactor systems for upgrading a petroleum-based composition by using one or more supercritical upgrading reactors and one or more supercritical standby reactors that alternate functions such that the supercritical upgrading reactor is converted to a supercritical standby reactor and the supercritical standby reactor is converted to a supercritical upgrading reactor. The supercritical upgrading reactor upgrades a combined feed stream while a supercritical standby reactor delivers a cleaning fluid into the supercritical standby reactor. The supercritical reactors may have one or more catalyst layers and one or more purging fluid inlets, and the catalyst layers may have differing void volume ratios. 1. A process for upgrading a petroleum-based composition comprising:combining a supercritical water stream with a pressurized, heated petroleum-based composition in a mixing device to create a combined feed stream,introducing the combined feed stream into an upgrading reactor system comprising one or more supercritical upgrading reactors and one or more supercritical standby reactors,where the supercritical upgrading reactor and the supercritical standby reactor both operate at a temperature greater than a critical temperature of water and a pressure greater than a critical pressure of water,where the supercritical upgrading reactor and the supercritical standby reactor both comprise at least one catalyst layer, andupgrading the combined feed stream in the supercritical upgrading reactor to produce an upgraded product;cleaning the supercritical standby reactor by passing a cleaning fluid into the supercritical standby reactor, while the upgrading step is being performed in the supercritical upgrading reactor; andalternating functions of the supercritical upgrading reactor and the supercritical standby reactor, such that the supercritical upgrading reactor is converted to a supercritical standby reactor undergoing a ...

HEAVY AROMATIC SOLVENTS FOR CATALYST REACTIVATION

Compositions and methods for restoring catalytic activity by dissolving soft coke with a solvent, one method including detecting soft coke deposition on a catalyst composition; preparing an aromatic bottoms composition with a Hildebrand solubility parameter of at least about 20 SI to remove the soft coke from the catalyst composition; and washing the catalyst composition with the aromatic bottoms composition until at least a portion of the soft coke deposition is removed. 1. A method for restoring catalytic activity by dissolving soft coke with a solvent , the method comprising the steps of:detecting soft coke deposition on a catalyst composition;preparing an aromatic bottoms composition with a Hildebrand solubility parameter of at least about 20 (SI) to remove the soft coke from the catalyst composition; andwashing the catalyst composition with the aromatic bottoms composition until at least a portion of the soft coke deposition is removed.2. The method according to claim 1 , where the step of detecting soft coke deposition on the catalyst composition comprises detecting a pressure drop increase over a catalyst bed comprising the catalyst composition of at least about 1 bar.3. The method according to claim 1 , where the step of detecting soft coke deposition on the catalyst composition comprises detecting a radial temperature profile change in a reactor of at least about 1° C.4. The method according to claim 1 , where the aromatic bottoms composition comprises aromatic bottoms from an aromatic recovery complex.5. The method according to claim 1 , where the aromatic bottoms composition comprises aromatic bottoms from a xylene rerun column of an aromatic recovery complex.6. The method according to claim 1 , where the aromatic bottoms composition consists essentially of aromatic bottoms from a xylene rerun column of an aromatic recovery complex.7. The method according to claim 1 , where the aromatic bottoms composition consists of aromatic bottoms from a xylene rerun ...

NITROGEN EXTRACTION FROM A GASEOUS CARBON DIOXIDE REACTANT STREAM

An input stream of gaseous nitrogen and carbon dioxide is introduced into a first interior volume of a separation vessel that is divided into first and second interior volumes by a separation membrane that includes a metal layer. The metal layer selectively permits movement of nitrogen through the metal layer. An output stream of gaseous nitrogen and carbon dioxide is conveyed out of the first interior volume and into a reaction vessel. The volume fraction of carbon dioxide is greater in the output stream than in the input stream; the volume fraction of nitrogen is reduced in the output stream relative to the input stream. Nitrogen is removed from the second interior volume to maintain a gradient of nitrogen partial pressure across the separation membrane that causes net transport of nitrogen from the first interior volume through the separation membrane into the second interior volume. 1. A method for generating a gaseous reduced-nitrogen carbon dioxide reactant stream , the method comprising:(a) introducing into a first interior volume of a separation vessel a gaseous input stream of a mixture of nitrogen and carbon dioxide, wherein the input stream is characterized by an input volume fraction of nitrogen and an input volume fraction of carbon dioxide, and wherein the separation vessel is divided into the first interior volume and a second interior volume by a separation membrane that includes a metal layer that selectively permits movement of nitrogen through the metal layer;(b) conveying, from the first interior volume of the separation vessel into a reaction vessel, a gaseous output stream of a mixture of nitrogen and carbon dioxide as the gaseous reduced-nitrogen carbon dioxide reactant stream, wherein the reactant stream is characterized by an output volume fraction of nitrogen that is less than the input volume fraction of nitrogen and an output volume fraction of carbon dioxide that is greater than the input volume fraction of carbon dioxide; and(c) ...

VACUUM RESID UPGRADATION AND GRAPHITE PRODUCTION

The present invention discloses a catalyst and process for hydrocracking of heavy hydrocarbon oils having majority portion boiling above 525° C. in the presence of hydrogen. A process comprising first step of converting heavy oil into lighter products in the presence of catalyst and hydrogen in slurry phase is disclosed. The process further comprises recycling of part of liquid products (HVGO) along with fresh heavy oil for improving the product selectivity. This recycled HVGO is having high concentrations of aromatics compounds. The separation of particles generated during the reaction at reactor exit also avoids the chances of choking of downstream sections. 1. A method of producing in situ catalyst in a hydrocracking process , comprising:(a) providing a mixture of hydrogen, heavy hydrocarbon oil, and an oil soluble catalyst, and{'sup': −1', '−1, '(b) decomposing the oil soluble catalyst by preheating the mixture at a predetermined fast enough velocity to predetermined temperature and passing through a confined hydrocracking zone maintained at a temperature between about 250° C. and 550° C., pressure between 40 to 250 bar and a space velocity of 0.5 hup to 4 h, to obtain a finely dispersed nano sized metallic iron particles in hydrocarbon oil, wherein, the nano sized metallic iron particles act as hydrogenating catalyst.'}2. The method of claim 1 , wherein the oil soluble catalyst is used in the range of about 0.01-2% by weight of heavy hydrocarbon oil.3. The method of claim 1 , wherein the oil soluble catalyst is ferrocene.4. The method of claim 1 , wherein the nano sized iron particles is composed of only few iron atoms.5. The method of claim 1 , wherein the decomposition starts from around 400° C. and gets completed before the feed and the catalyst reaches the slurry reactor.6. A method of producing graphite claim 1 , comprising:(a) providing a mixture of hydrogen, heavy hydrocarbon oil, and an oil soluble catalyst,{'sup': −1', '−1, '(b) decomposing the oil ...

Catalyst for preparing light olefin, preparation method therefor, and method for preparing light olefin by using same

The present invention relates to a catalyst for preparing a light olefin, a preparation method therefor, and a method for preparing a light olefin by using same, and can provide a catalyst for preparing a light olefin, a preparation method therefor, and a method for preparing a light olefin by using same, the catalyst comprising a porous zeolite, a clay, an inorganic oxide binder, and Ag2O and P2O5 which are supported in the pores and/or on the surface of the porous zeolite.

Method for Preparing Carbonized Silk Photocatalyst and Use Thereof

Disclosed is a method for preparing a carbonized silk photocatalyst, comprising; soaking a natural silk and an activator in water, taking out the soaked silk, and drying the same; and roasting the dried silk under the protection of an inert atmosphere to prepare a carbonized silk photocatalyst. Also disclosed is a method for photocatalytic desulfurization of a fuel oil, comprising: mixing a fuel oil to be desulfurated, an extraction agent and a carbonized silk photocatalyst, with air being used as an oxidizing agent, to conduct a photocatalytic reaction under light irradiation, and separating an upper oil phase to obtain a desulfurated fuel oil. The catalyst has a simple preparation process, and can effectively reduce dibenzothiophene sulfides, which are difficult to remove, in the fuel oil under UV light radiation. Desulfurization can be achieved at room temperature, and reaction conditions are mild.

SYSTEMS AND METHODS FOR THE SYNTHESIZING ZSM-22 ZEOLITES

According to one or more embodiments, non-agglomerated, nano-sized ZSM-22 zeolites may be synthesized by methods comprising operating a mechanical rotation drum unit at a first temperature of from 40° C. to 60° C. and a first speed of from 200 rpm to 1000 rpm for a first time period of from 1.3 hours to 2.7 hours; operating the mechanical rotation drum unit at a second speed of from 30 rpm to 90 rpm for a second time period of from 0.05 hours to 0.4 hours; heating the mechanical rotation drum unit at a ramping temperature of from 8° C./minute to 12° C./minute to a second temperature of from 115° C. to 185° C. at the second speed; operating the mechanical rotation drum unit at the second temperature and the second speed for a third time period of from 30 hours to 90 hours; and cooling the mechanical rotation drum unit at a fourth speed of 0 rpm. 1. A method of synthesizing a non-agglomerated , nano-sized ZSM-22 zeolite , the method comprising:passing a silica solution and an aluminate solution into a mechanical rotation drum unit;operating the mechanical rotation drum unit at a first temperature of from 40° C. to 60° C. and a first speed of from 200 rpm to 1000 rpm for a first time period of from 1.3 hours to 2.7 hours;operating the mechanical rotation drum unit at a second speed of from 30 rpm to 90 rpm for a second time period of from 0.05 hours to 0.4 hours;heating the mechanical rotation drum unit at a ramping temperature of from 8° C./minute to 12° C./minute to a second temperature of from 115° C. to 185° C. at the second speed of from 30 rpm to 90 rpm;operating the mechanical rotation drum unit at the second temperature of from 115° C. to 185° C. and the second speed of from 30 rpm to 90 rpm for a third time period of from 30 hours to 90 hours; and{'b': '0', 'cooling the mechanical rotation drum unit at a fourth speed of rpm to produce the non-agglomerated, nano-sized ZSM-22 zeolite; and'}wherein the non-agglomerated, nano-sized ZSM-22 zeolite comprises ...

Supercritical reactor systems and processes for petroleum upgrading

Supercritical upgrading reactors and reactor systems for upgrading a petroleum-based compositions comprising one or more catalyst layers and, in some embodiments, one or more purging fluid inlets, where one or more catalyst layers at least partially sift and convert heavy hydrocarbon fractions to light hydrocarbon fractions to produce an upgraded supercritical reactor product. In some embodiments, upgrading reactor systems comprise one or more supercritical upgrading reactors and one or more supercritical standby reactors alternating functions such that a supercritical upgrading reactor is converted to a supercritical standby reactor and the supercritical standby reactor is converted to a supercritical upgrading reactor, where the supercritical upgrading reactor upgrades a combined feed stream while a supercritical standby reactor delivers a cleaning fluid into the supercritical standby reactor.

SUPERCRITICAL REACTOR SYSTEMS AND PROCESSES FOR PETROLEUM UPGRADING

Supercritical upgrading reactors and reactor systems for upgrading a petroleum-based compositions comprising one or more catalyst layers and, in some embodiments, one or more purging fluid inlets, where one or more catalyst layers at least partially sift and convert heavy hydrocarbon fractions to light hydrocarbon fractions to produce an upgraded supercritical reactor product. In some embodiments, upgrading reactor systems comprise one or more supercritical upgrading reactors and one or more supercritical standby reactors alternating functions such that a supercritical upgrading reactor is converted to a supercritical standby reactor and the supercritical standby reactor is converted to a supercritical upgrading reactor, where the supercritical upgrading reactor upgrades a combined feed stream while a supercritical standby reactor delivers a cleaning fluid into the supercritical standby reactor. 1. A process for upgrading a petroleum-based composition comprising:combining a supercritical water stream with a pressurized, heated petroleum-based composition in a mixing device to create a combined feed stream; where the downflow supercritical upgrading reactor comprises a first catalyst layer and a second catalyst layer, the second catalyst layer disposed vertically below the first catalyst layer in the downflow supercritical upgrading reactor,', 'where the first catalyst layer comprises a heterogeneous porous metal containing catalyst having a first void volume ratio and the second catalyst layer comprises a heterogeneous porous metal containing catalyst having a second void volume ratio,', 'where the second void volume ratio differs from the first void volume ratio, and', 'where the downflow supercritical upgrading reactor includes one or more purging fluid inlets disposed on one or more side locations of the downflow supercritical upgrading reactor proximate the first catalyst layer, the second catalyst layer, or both;, 'introducing the combined feed stream into an ...

Supercritical reactor systems and processes for petroleum upgrading

Supercritical upgrading reactors and reactor systems are provided for upgrading a petroleum-based composition using one or more purging fluid inlets to prevent plugging of the catalyst layer in the reactor. Processes for upgrading petroleum-based compositions by utilizing a reactor having at least one purging fluid inlet are also provided.

PROCESS FOR HYDROCRACKING HEAVY OIL AND OIL RESIDUE

A process for the hydrocracking of heavy oils and/or oil residues, the process comprising the step of contacting the heavy oils and/or oil residues with a non-metallised carbonaceous additive in the presence of a hydrogen-containing gas at a temperature of from 250° C. to 600° C. wherein the non-metallised carbonaceous additive has an average pore size of at least 2 nm. 1. A process for the hydroprocessing of heavy oils and/or oil residues , the process comprising the step of:(a) contacting the heavy oils and/or oil residues with a non-metallised carbonaceous additive in the presence of a hydrogen-containing gas at a temperature of from 250° C. to 600° C.; wherein the non-metallised carbonaceous additive has an average pore size of at least 2 nm.2. A process according to claim 1 , wherein the non-metallised carbonaceous additive has an average pore size of from 2 nm to 10 nm claim 1 , preferably from 2.25 nm to 8 nm claim 1 , more preferably from 2.5 nm to 6 nm and even more preferably from 3 nm to 5 nm.3. A process according to claim 1 , wherein the non-metallised carbonaceous additive is selected from the list consisting of: anthracite cokes claim 1 , lignite cokes claim 1 , carbon blacks claim 1 , activated cokes claim 1 , petroleum cokes claim 1 , furnace dusts claim 1 , dusts from Winkler gasification of coal claim 1 , red mud claim 1 , electrostatic filter dusts and cyclone dusts claim 1 , preferably wherein the non-metallised carbonaceous additive is a lignite coke.4. A process according to claim 1 , wherein the non-metallised carbonaceous additive comprises one or more metals in a combined amount of at least 6000 ppm claim 1 , preferably from 6000 ppm to 100000 ppm claim 1 , more preferably from 7000 ppm to 30000 ppm claim 1 , even more preferably from 8000 ppm to 20000 ppm claim 1 , even more preferably still from 9000 ppm to 15000 ppm and yet more preferably still from 10000 ppm to 13000 ppm claim 1 , by weight of the non-metallised carbonaceous additive.5 ...

Catalyst and process for the production of diesel fuel from natural gas, natural gas liquids, or other gaseous feedstocks

A unique process and catalyst is described that operates efficiently for the direct production of a high cetane diesel type fuel or diesel type blending stock from stochiometric mixtures of hydrogen and carbon monoxide. This invention allows for, but is not limited to, the economical and efficient production high quality diesel type fuels from small or distributed fuel production plants that have an annual production capacity of less than 10,000 barrels of product per day, by eliminating traditional wax upgrading processes. This catalytic process is ideal for distributed diesel fuel production plants such as gas to liquids production and other applications that require optimized economics based on supporting distributed feedstock resources. 3. A process for the production of a hydrocarbon mixture comprising; a pore diameter greater than 80 angstroms and;', 'a crush strength of greater than 3 lbs/mm and;', 'a BET surface area of greater than 110 m2/g;', 'a dispersion value between 2% and 10%,, 'reacting a feed gas that contains hydrogen and carbon monoxide with a catalyst having,'}producing a product stream comprising light gases, diesel fuel and a wax from reacting the feed gas with the supported catalyst.4. The process of claim 1 , wherein the catalyst is reduced with hydrogen at temperatures below 650 F.5. The process of claim 1 , wherein the diesel fuel fraction produced is about ⅔ of the non-gas product produced.6. The process of claim 1 , wherein the supported catalyst comprises a lobed support with more than four lobes and an effective pellet radius of less than 600 microns.7. The process of claim 4 , where all of the lobes are not equal lengths.8. The process of claim 4 , wherein the supported catalyst further comprises about 0.01 weight percent to about 2.0 weight percent of a promoter selected from the group consisting of cerium claim 4 , ruthenium claim 4 , lanthanum claim 4 , platinum claim 4 , rhenium. gold claim 4 , nickel claim 4 , or rhodium and a ...

Method for hydrotreatment of vacuum distillates implementing a specific concatenation of catalysts

A method for hydrotreatment of a vacuum-distillate-type hydrocarbon feedstock that contains sulfur and nitrogen compounds is described, with said method for hydrotreatment of a vacuum-distillate-type feedstock comprising a specific concatenation of catalysts that makes it possible to increase the overall activity and the overall stability of the method.

INTEGRATED PROCESS FOR ACTIVATING HYDROPROCESSING CATALYSTS WITH IN-SITU PRODUCED SULFIDES AND DISULPHIDES

The invention involves an integrated process in which a hydrocarbon feedstock is treated with a caustic (alkaline) extraction to remove sulfides, disulfides, and mercaptans. These extracted materials are further treated, and are then used to activate hydrotreating catalysts. 1. An integrated process for removing sulfur containing hydrocarbons from a hydrocarbon feedstock and activating a hydroprocessing catalyst , comprising:(i) contacting said hydrocarbon feedstock to an alkaline extraction solution in an extraction vessel, to remove sulfides, disulfides, and mercaptans;(ii) reacting the mercaptans with an alkali in said alkaline extraction solution to form thiolates;(iii) contacting said thiolates with oxygen in the presence of a catalyst, to form a mixture of sulfides and disulfides;(iv) removing any sulfides and disulfides from said alkaline solution by adsorbing said sulfides and disulfides to an adsorbent to form a mixture;(v) removing any non-sulfur compounds from said mixture, and(vi) activating a hydroprocessing catalyst by contact of said sulfur containing compounds to said hydroprocessing catalyst.2. The process of claim 1 , comprising carrying out (i) and (ii) at a temperature of 15° C. to 80° C.3. The process of claim 2 , comprising carrying out (i) and (ii) at a temperature of 40° C. to 60° C.4. The process of claim 1 , comprising carrying out (i) and (ii) at a pressure of 10-50 bars.5. The process of claim 1 , comprising carrying out (iii) at a temperature of from 20° C. to 300° C.6. The process of claim 5 , comprising carrying out (iii) at a temperature of from 20° C. to 80° C.7. (canceled)7. (canceled)8. (canceled)9. The process of claim 1 , comprising removing water soluble sulfur containing compounds in (iv) via a water wash.10. (canceled)11. The method of claim 10 , wherein said adsorbent is activated carbon alumina claim 10 , silica alumina claim 10 , sand claim 10 , a zeolite claim 10 , or a regenerated spent catalyst.12. The method of claim 1 ...

Catalyst and process for the production of diesel fuel from natural gas, natural gas liquids, or other gaseous feedstocks

A unique process and catalyst is described that operates efficiently for the direct production of a high cetane diesel type fuel or diesel type blending stock from stochiometric mixtures of hydrogen and carbon monoxide. This invention allows for, but is not limited to, the economical and efficient production high quality diesel type fuels from small or distributed fuel production plants that have an annual production capacity of less than 10,000 barrels of product per day, by eliminating traditional wax upgrading processes. This catalytic process is ideal for distributed diesel fuel production plants such as gas to liquids production and other applications that require optimized economics based on supporting distributed feedstock resources. 3. A process for the production of a hydrocarbon mixture comprising: a pore diameter greater than 80 angstroms and;', 'a crush strength of greater than 3 lbs/mm and;', 'a BET surface area of greater than 110 m2/g;', 'a dispersion value between 2% and 10%,, 'reacting a feed gas that contains hydrogen and carbon monoxide with a catalyst having,'}producing a product stream comprising light gases, diesel fuel and a wax from reacting the feed gas with the supported catalyst.4. The process of claim 1 , wherein the catalyst is reduced with hydrogen at temperatures below 650 F.5. The process of claim 1 , wherein the diesel fuel fraction produced is about ⅔ of the non-gas product produced.6. The process of claim 1 , wherein the supported catalyst comprises a lobed support with more than four lobes and an effective pellet radius of less than 600 microns.7. The process of claim 4 , where all of the lobes are not equal lengths.8. The process of claim 4 , wherein the supported catalyst further comprises about 0.01 weight percent to about 2.0 weight percent of a promoter selected from the group consisting of cerium claim 4 , ruthenium claim 4 , lanthanum claim 4 , platinum claim 4 , rhenium claim 4 , gold claim 4 , nickel claim 4 , or rhodium ...

Supercritical reactor systems and processes for petroleum upgrading

Supercritical upgrading reactors and reactor systems are provided for upgrading a petroleum-based composition using one or more purging fluid inlets to prevent plugging of the catalyst layer in the reactor. Processes for upgrading petroleum-based compositions by utilizing a reactor having at least one purging fluid inlet are also provided.

A process which does simultaneous dehydrochlorination and hydrocracking of pyrolysis oils from mixed plastic pyrolysis while achieving selective hydrodealkylation of c9+ aromatics

A process for hydrodealkylating a hydrocarbon stream comprising (a) contacting the hydrocarbon stream with a hydroprocessing catalyst in a hydroprocessing reactor in the presence of hydrogen to yield a hydrocarbon product, wherein the hydrocarbon stream contains C 9 + aromatic hydrocarbons; and (b) recovering a treated hydrocarbon stream from the hydrocarbon product, wherein the treated hydrocarbon stream comprises C 9 + aromatic hydrocarbons, wherein an amount of C 9 + aromatic hydrocarbons in the treated hydrocarbon stream is less than an amount of C 9 + aromatic hydrocarbons in the hydrocarbon stream due to hydrodealkylating of at least a portion of C 9 + aromatic hydrocarbons from the hydrocarbon stream during the step (a) of contacting.

Process for Activation and Operation of a Hydrocarbon Upgrading Catalyst

The present invention provides a process for upgrading a Fischer-Tropsch product by hydrocracking in the presence of a hydrocracking catalyst in a reactor, wherein the process is initiated by a series of steps (i) to (iv). The hydrocracking catalyst is (i) contacted with a hydrogen-containing stream having a feed temperature of from 360° C. to 420° C.; (ii) the feed temperature of the hydrogen-containing stream is reduced to a temperature of from 220° C. to 280° C.; (iii) the catalyst is contacted with a Fischer-Tropsch product stream having a feed temperature of from 220° C. to 280° C., which is co-fed with the hydrogen-containing stream; and (iv) the catalyst is co-fed with a Fischer-Tropsch product stream and hydrogen-containing stream having feed temperatures of from 380° C. and 400° C. for at least four days and wherein the hydrocracking catalyst is not activated by sulfiding. 1. A process for upgrading a Fischer-Tropsch product by contacting a hydrocracking catalyst in a reactor with a Fischer-Tropsch product stream having a feed temperature in the range of from 360° C. to 420° C. , wherein , before the catalyst is contacted with the Fischer-Tropsch product stream having a feed temperature in the range of from 360° C. to 420° C. , said process is initiated by;(i) contacting the hydrocracking catalyst with a hydrogen-containing stream having a feed temperature in the range of from 360° C. to 420° C.;(ii) reducing the feed temperature of the hydrogen-containing stream to a temperature in the range of from 220° C. to 280° C.; and(iii) contacting the catalyst with a Fischer-Tropsch product stream having a feed temperature in the range of from 220° C. and 280° C. by co-feeding with the hydrogen-containing stream;(iv) contacting the catalyst with Fischer-Tropsch product stream having a feed temperature in the range of from 380° C. and 400° C. by co-feeding with the hydrogen-containing stream andwherein the catalyst is not activated by sulfiding.2. A process ...

Conversion of biomass into a liquid hydrocarbon material

The present invention provides a process for producing liquid hydrocarbon products from a biomass, biomass containing and/or biomass-derived feedstock, said process comprising the steps of: a) contacting the feedstock with a first hydropyrolysis catalyst composition and molecular hydrogen in a 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, H2O, H2, CO2, CO, C1-C3 gases, char and catalyst fines; b) removing said char and catalyst fines from said product stream; c) hydroconverting said partially deoxygenated hydropyrolysis product in a hydroconversion reactor vessel in the presence of one or more hydroconversion catalyst compositions and of the H2O, CO2, CO, H2, and C1-C3 gas generated in step a), to produce a vapour phase product comprising substantially fully deoxygenated hydrocarbon product, H2O, CO, CO2, and C1-C3 gases, wherein one or more of the first hydropyrolysis catalyst composition and the hydroconversion catalyst composition is prepared by a process comprising combining a porous support with one or more catalytically active metals selected from Group VI and Group VIII of the Periodic Table, thereby forming a catalyst precursor having a volatile content, and reducing the volatile content of the catalyst precursor in one or more steps, wherein at least one volatile content reduction step is performed in the presence of one or more sulfur containing compounds; and wherein the catalyst precursor does not reach calcining temperatures prior to said at least one combined volatile content reduction-sulfurizing step.

Method for restoring activity to a spent hydroprocessing catalyst, a spent hydroprocessing catalyst having restored catalytic activity, and a hydroprocessing process

A regenerated spent hydroprocessing catalyst treated with a chelating agent and having incorporated therein a polar additive.

Process for Preparation of Hydrocracking Catalyst for Use in Hydrocracking of Hydrocarbon Streams

A process for activating and maintaining a catalyst for use in hydrocracking a hydrocarbon stream includes continuously contacting a hydrocarbon stream with a hydroprocessing catalyst in the presence of hydrogen. Sulphides and chloride compounds in the hydrocarbon stream are used such that the hydroprocessing catalyst has the ability to hydrogenate, dechlorinate, and hydrocrack components of the hydrocarbon stream. 1. A process for activating and maintaining a catalyst for use in hydrotreating a hydrocarbon stream to simultaneously reduce heavier boiling components , chlorides , and olefins , comprising:continuously contacting the hydrocarbon stream with a hydroprocessing catalyst in the presence of hydrogen, wherein the hydrocarbon stream comprises one or more chloride compounds and one or more sulphides.2. The process of claim 1 , wherein the one or more sulphides comprise dimethyl disulphide claim 1 , mercaptans claim 1 , carbon disulphide claim 1 , hydrogen sulphide claim 1 , or combinations thereof.3. The process of claim 1 , wherein the one or more sulfides of the hydrocarbon stream are present in an amount such that a sulphur content of the hydrocarbon stream is about 0.5 wt % to about 5 wt % based on a total weight of the hydrocarbon stream.4. The process of claim 1 , further comprising:before the step of continuously contacting the hydrocarbon stream with the hydroprocessing catalyst in the presence of hydrogen, contacting a catalyst activating stream with the hydroprocessing catalyst, wherein the catalyst activating stream comprises one or more sulphides.5. The process of claim 4 , wherein the one or more sulfides of the catalyst activating stream are present in an amount such that a sulphur content of the catalyst activating stream is about 0.5 wt % to about 5 wt % based on a total weight of the catalyst activating stream.6. The process of claim 4 , wherein after the step of contacting and during the step of continuously contacting claim 4 , the ...

HYDROPROCESSING CATALYSTS AND THEIR PRODUCTION

The precursor of a hydroprocessing catalyst is made by impregnating a metal oxide component comprising at least one metal from Group 6 of the Periodic Table and at least one metal from Groups 8-10 of the Periodic Table with an amide formed from a first organic compound containing at least one amine group, and a second organic compound containing at least one carboxylic acid group. Following impregnation heat treatment follows to form in situ generated unsaturation additional to that in the two organic compounds. The catalyst precursor is sulfided to form an active, sulfide hydroprocessing catalyst. 1. (canceled)2. A method for hydroprocessing a biocomponent feedstock , comprising:exposing a biocomponent feedstock comprising a bio-derived fraction and a mineral oil fraction to a bulk mixed metal catalyst, in the presence of hydrogen under effective deoxygenation conditions, the bulk mixed metal catalyst comprising at least one Group VI metal selected from Mo and W and at least one Group VIII metal selected from Co and Ni; and forming a deoxygenated effluent.3. The method of claim 2 , wherein the bio-derived fraction makes up about 20 wt % of the biocomponent feedstock.4. The method of claim 2 , wherein the bio-derived fraction includes a lipids fraction claim 2 , wherein about 2 wt % to about 40 wt % of lipids in the lipids fraction claim 2 , based on the weight of the bio-derived fraction claim 2 , is sourced from algal sources.5. The method of claim 2 , wherein the deoxygenated effluent is substantially oxygen free.6. The method of claim 2 , wherein the dexoygenation conditions comprise a hydrogen partial pressure of from about 5 barg (0.5 MPag) to about 300 barg (30 MPag) claim 2 , a reaction temperature of from about 392° F. to about 842° F. (200° C. to 450° C.) claim 2 , a liquid hourly space velocity of from about 0.05 hrto about 10 hr claim 2 , and a hydrogen treat gas rate from about 200 scf/B (34 Nm/m) to about 10 claim 2 ,000 scf/B (1685 Nm/m).7. The method ...

PROCESS FOR THE PREPARATION OF A CATALYST, CATALYST AND ITS USE IN A HYDROCONVERSION AND/OR HYDROTREATMENT PROCESS

The invention concerns a process for the preparation of a catalyst starting from a pre-catalyst comprising at least one catalytic metal and a support, said pre-catalyst having undergone a heat treatment at at least 60° C. without calcining, in which process said pre-catalyst is impregnated with a basic solution having a pH of more than 7.5 and containing at least one molecule in the zwitterionic form, and the impregnated pre-catalyst is dried at a temperature of at most 240° C. without subsequent calcining. 1. A process for the preparation of a catalyst starting from a pre-catalyst comprising at least one catalytic metal and a support , said pre-catalyst having undergone a heat treatment at at least 60° C. without calcining , in which process said pre-catalyst is impregnated with a basic solution having a pH of more than 7.5 and containing at least one molecule in the zwitterionic form , and the impregnated pre-catalyst is dried at a temperature of at most 240° C. without subsequent calcining , and the molecule in the zwitterionic form is selected from the group formed by amino-alcohol acids containing secondary or tertiary amine groups and containing at least one carboxylic acid function and at least one alcohol function.2. The process according to claim 1 , in which said molecule has a single carboxylic acid function.3. The process according to claim 1 , in which the molecule in the zwitterionic form is bicine.4. The process according to claim 1 , in which the molecule in the zwitterionic form is tricine.5. The process according to claim 1 , in which impregnation is carried out at a pH of more than 8.5 claim 1 , preferably more than 10.6. The process according to claim 5 , in which the base is ammonia.7. The process according to claim 1 , in which after impregnation claim 1 , the pre-catalyst undergoes a maturation step claim 1 , preferably for 0.1 to 10 h and at a temperature of 15° C. to 80° C.8. The process according to claim 1 , in which drying is carried out ...

CATALYTIC ACTIVATION AND ALKYLATION OF ISOPENTANE-ENRICHED MIXTURES

The present disclosure relates generally to processes and systems for producing liquid transportation fuels by converting a feed stream that comprises both isopentane and n-pentane, and optionally, some C6+ hydrocarbons. Isopentane and smaller hydrocarbons are separated to form a first fraction while n-pentane and larger components of the feed stock form a second fraction. Each fraction is then catalytically-activated in a separate reaction zone with a separate catalyst, where the conditions maintained in each zone maximize the conversion of each fraction to olefins and aromatics, while minimizing the production of C1-C4 light paraffins. In certain embodiments, the first fraction is activated at a lower temperature than the second fraction. Certain embodiments additionally comprise mixing at least a portion of the two effluents and contacting with an alkylation catalyst to provide enhanced yields of mono-alkylated aromatics that are suitable for use as a blend component of liquid transportation fuels or other value-added chemical products. 1. A method for converting a feedstock comprising pentanes to produce a liquid transportation fuel , comprising:a. providing a hydrocarbon feed stream comprising at least 50 wt. % pentanes, including both n-pentane and isopentane, wherein the hydrocarbon feed stream further comprises less than 10 wt. % of hydrocarbons containing four or fewer carbons; i. a first fraction comprising at least 80% of the isopentane present in the feed stream, and at least 90% of hydrocarbons present in the feed stream that are characterized by a vapor pressure equal to or greater than the vapor pressure of isopentane;', 'ii. a second fraction that comprises at least 80% of the n-pentane present in the feed stream and at least 90% of any hydrocarbons containing six or more carbons that were in the feed stream;, "b. at least partially separating various constituents in the hydrocarbon feed stream according to each constituent's characteristic vapor ...

SYSTEMS FOR CATALYTIC ACTIVATION OF ISOPENTANE-ENRICHED MIXTURES

The present disclosure relates generally to systems operable to produce liquid transportation fuels by converting a hydrocarbon feed stream that comprises both isopentane and n-pentane, and optionally, some C6+ hydrocarbons. The system separates the hydrocarbon feed stream to form a first fraction comprising isopentane and smaller hydrocarbons, and a second fraction comprising n-pentane and larger components of the hydrocarbon feeds stream. Each fraction is then catalytically-activated in a separate activation reactor containing a separate activation catalyst, where the conditions maintained in each reactor are selected to maximize the conversion of each fraction to olefins and aromatics, while minimizing the production of C1-C4 light paraffins. In certain embodiments, the first activation reactor is maintained at a lower temperature than the second activation reactor. Certain embodiments of the system mix at least a portion of the effluents from the first and second activation reactor and convert the resulting mixed effluent in either an oligomerization reactor containing an oligomerization catalyst or an oligomerization reactor containing an alkylation catalyst to provide enhanced yields of upgraded hydrocarbon products that are characterized as a liquid transportation fuel or a blend component thereof. 1. A system configured to convert a feedstock comprising pentanes to produce a liquid transportation fuel , the system comprising:a) a hydrocarbon feed stream comprising at least 50 wt. % pentanes, including both n-pentane and isopentane, wherein the hydrocarbon feed stream further comprises less than 10 wt. % of hydrocarbons containing four or fewer carbons; i. a first fraction comprising at least 80% of the isopentane present in the feed stream, and at least 90% of hydrocarbons present in the hydrocarbon feed stream that are characterized by a vapor pressure equal to or greater than the vapor pressure of isopentane;', 'ii. a second fraction that comprises at ...

Agglomeration-Resistant Desulfurizing Product

Disclosed herein is an agglomeration-resistant desulfurizing product for removing contaminants from a fluid stream. The agglomeration-resistant desulfurizing product comprising a metal oxide composition for reacting with contaminants and a polymeric crystallization inhibitor for reducing the agglomeration of the desulfurizing product resulting from using the desulfurizing product. A method to produce the agglomeration-resistant desulfurizing product and a method to treat a fluid stream is also disclosed. 1. An agglomeration-resistant desulfurizing product for removing contaminants from a fluid stream , the desulfurizing product comprising:{'sub': '2', '(a) a metal oxide composition that comprises a primary component, wherein the primary component comprises at least one metal oxide of the formula MexOy .(H0)z, wherein Me is selected from groups 4-12 of the periodic table of elements, 0 is oxygen; 1 s; x s; 3; 1 ::5 y s; 4, and 0 s; z ::5 1O; and'}(b) a polymeric crystallization inhibitor.2. The agglomeration-resistant desulfurizing product of claim 1 , wherein the polymeric crystallization inhibitor is at an amount that is in the range of about 1000 ppm by weight to about 10 wt % based on the weight of the metal oxide composition.3. The agglomeration-resistant desulfurizing product of claim 2 , wherein the polymeric inhibitor comprises:a salt of acrylamido-methyl propane sulfonate/acrylic acid copolymer (AMPS/AA);a phosphonated maleic copolymer (PHOS/MA);a salt of polymaleic acid/acrylic acid/acrylamido-methyl propane sulfonate terpolymers (PMAfAMPS); ora copolymer that comprises an acrylamide moiety, a quaternary ammonium moiety, a quaternary ammonium salt moiety, an acrylate moiety, an acrylic acid moiety, orcombination thereof; of a combination thereof.4. The agglomeration-resistant desulfurizing product of claim 1 , wherein the polymeric crystallization inhibitor comprises an acrylamide moiety claim 1 , a quaternary ammonium moiety claim 1 , a quaternary ammonium ...

SUPERCRITICAL REACTOR SYSTEMS AND PROCESSES FOR PETROLEUM UPGRADING

Supercritical upgrading reactors and reactor systems are provided for upgrading a petroleum-based composition using one or more purging fluid inlets to prevent plugging of the catalyst layer in the reactor. Processes for upgrading petroleum-based compositions by utilizing a reactor having at least one purging fluid inlet are also provided. 1. A process for upgrading a petroleum-based composition comprising:combining a supercritical water stream with a pressurized, heated petroleum-based composition in a mixing device to create a combined feed stream; 'where the downflow supercritical upgrading reactor comprises at least one catalyst layer and one or more purging fluid inlets disposed on one or more side locations of the downflow supercritical upgrading reactor proximate the catalyst layer;', 'introducing the combined feed stream into an upgrading reactor system comprising at least one downflow supercritical upgrading reactor operating at a temperature greater than a critical temperature of water and a pressure greater than a critical pressure of water,'}passing the combined feed stream through the at least one catalyst layer to at least partially convert the combined feed stream to an upgraded product comprising light hydrocarbons;injecting purging fluid through the purging inlets to contact the at least one catalyst layer to reduce plugging; andpassing upgraded product out of the downflow supercritical upgrading reactor.2. The process of claim 1 , where the purging fluid inlets are vertically disposed above the at least one catalyst layer.3. The process of claim 1 , wherein the supercritical upgrading reactor comprises at least a first catalyst layer and a second catalyst layer claim 1 , and the purging fluid inlets are vertically disposed between the first catalyst layer and the second catalyst layer.4. The process of claim 1 , where the purging fluid inlets comprise one or more angled linear pipes claim 1 , the angle being relative to a horizontal plane defined ...

PROCESS FOR THE SYNTHESIS OF HYDROCARBONS FROM SYNTHESIS GAS IN THE PRESENCE OF A CATALYST BASED ON COBALT TRAPPED IN A MESOPOROUS OXIDE MATRIX AND OBTAINED FROM AT LEAST ONE MONOMERIC PRECURSOR

A process for the synthesis of linear paraffinic hydrocarbons from a feed of carbon monoxide and dihydrogen in the presence of a catalyst of a mesoporous oxide matrix and a content by weight of the element cobalt of 0.5% to 60%, wherein the catalyst is prepared by 1. A process for the synthesis of linear paraffinic hydrocarbons from a feed comprising carbon monoxide and dihydrogen in the presence of a catalyst comprising a mesoporous oxide matrix and a content by weight of the element cobalt in the range 0.5% to 60% , expressed as the % by weight of metal with respect to the total weight of said catalyst , said catalyst being prepared in accordance with a preparation process comprising at least the steps of:a) mixing, in an aqueous or hydro-organic solvent, at least one molecular precursor comprising cobalt and at least one molecular precursor of said mesoporous oxide matrix comprising at least one element X selected from the group constituted by silicon, aluminium, titanium, zirconium, cerium and mixtures thereof, said molecular precursors being dissolved in said aqueous or hydro-organic solvent;b) aerosol spray drying the mixture obtained in step a) in order to result in the formation of spherical liquid droplets;c) drying said spherical droplets in order to obtain solid particles at a temperature in the range 10° C. to 300° C.;d) activation of said solid particles by means of a reduction treatment in a manner such as to form nanoparticles of cobalt with an oxidation state of 0.2. The process as claimed in claim 1 , in which said mixture in accordance with said step a) comprises molecular precursors comprising the element silicon as the only molecular precursors of said mesoporous oxide matrix.3. The process as claimed in claim 1 , in which said mixture in accordance with said step a) comprises claim 1 , as the only molecular precursors of said mesoporous oxide matrix claim 1 , molecular precursors comprising the element silicon and molecular precursors comprising ...

DUAL CATALYST SYSTEM FOR EBULLATED BED UPGRADING TO PRODUCE IMPROVED QUALITY VACUUM RESIDUE PRODUCT

An ebullated bed hydroprocessing system is upgraded using a dual catalyst system that includes a heterogeneous catalyst and dispersed metal sulfide particles to improve the quality of vacuum residue. The improved quality of vacuum residue can be provided by one or more of reduced viscosity, reduced density (increased API gravity), reduced asphaltene content, reduced carbon residue content, reduced sulfur content, and reduced sediment. Vacuum residue of improved quality can be produced while operating the upgraded ebullated bed reactor at the same or higher severity, temperature, throughput and/or conversion. Similarly, vacuum residue of same or higher quality can be produced while operating the upgraded ebullated bed reactor at higher severity, temperature, throughput and/or conversion. 1. A method of upgrading an ebullated bed hydroprocessing system that includes one or more ebullated bed reactors to improve vacuum residue quality , comprising:operating an ebullated bed reactor using a heterogeneous catalyst to hydroprocess heavy oil at an initial rate of production of converted products and produce an initial rate and quality of bottoms product;thereafter upgrading the ebullated bed reactor to operate using a dual catalyst system comprised of dispersed metal sulfide catalyst particles and heterogeneous catalyst; andoperating the upgraded ebullated bed reactor using the dual catalyst system to hydroprocess heavy oil at a rate of production of converted products at least as high as the initial rate and producing bottoms product with a higher quality than the initial quality.2. The method of claim 1 , wherein the heavy oil comprises at least one of heavy crude oil claim 1 , oil sands bitumen claim 1 , residuum from refinery processes claim 1 , atmospheric tower bottoms having a nominal boiling point of at least 343° C. (650° F.) claim 1 , vacuum tower bottoms having a nominal boiling point of at least 524° C. (975° F.) claim 1 , resid from a hot separator claim 1 , ...

Reactivated Hydroprocessing Catalysts for Use in Sulfur Abatement

Disclosed herein are methods, systems, and compositions for providing catalysts for tail gas clean up in sulfur recovery operations. Aspects of the disclosure involve obtaining catalyst that was used in a first process, which is not a tailgas treating process and then using the so-obtained catalyst in a tailgas treating process. For example, the catalyst may originally be a hydroprocessing catalyst. A beneficial aspect of the disclosed methods and systems is that the re-use of spent hydroprocessing catalyst reduces hazardous waste generation by operators from spent catalyst disposal. Ultimately, this helps reduce the environmental impact of the catalyst life cycle. The disclosed methods and systems also provide an economically attractive source of high-performance catalyst for tailgas treatment, which benefits the spent catalyst generator, the catalyst provider, and the catalyst consumer.

Start-up Procedure for a Fischer-Tropsch Process

The present invention generally relates to a Fischer-Tropsch process, in particular a Fischer-Tropsch process for converting a feed comprising a mixture of hydrogen and carbon monoxide gases, preferably in the form of a synthesis gas mixture, to hydrocarbons by contacting a cobalt-containing Fischer-Tropsch synthesis catalyst with a mixture of hydrogen and carbon monoxide in a reactor at a pressure of 4.0 MPa absolute or greater, wherein the process is initiated by a start-up procedure comprising the steps of: i) providing a feed comprising a mixture of hydrogen and carbon monoxide gases, preferably in the form of a synthesis gas mixture, to a reactor containing a cobalt-containing Fischer-Tropsch synthesis catalyst, wherein the pressure inside the reactor is 3.5 MPa absolute or below; and ii) maintaining the feed to the reactor, removing a product stream comprising hydrocarbons and maintaining the pressure inside the reactor at 3.5 MPa absolute or below for at least 15 hours, preferably for at least 50 hours.

Catalyst and process for the production of diesel fuel from national gas, natural gas liquids, or other gaseous feedstocks

A unique process and catalyst is described that operates efficiently for the direct production of a high cetane diesel type fuel or diesel type blending stock from stochiometric mixtures of hydrogen and carbon monoxide. This invention allows for, but is not limited to, the economical and efficient production high quality diesel type fuels from small or distributed fuel production plants that have an annual production capacity of less than 10,000 barrels of product per day, by eliminating traditional wax upgrading processes. This catalytic process is ideal for distributed diesel fuel production plants such as gas to liquids production and other applications that require optimized economics based on supporting distributed feedstock resources. 3. A process for the production of a hydrocarbon mixture comprising; a pore diameter greater than 80 angstroms and;', 'a crush strength of greater than 3 lbs/mm and;', 'a BET surface area of greater than 110 m2/g;', 'a dispersion value between 2% and 10%,, 'reacting a feed gas that contains hydrogen and carbon monoxide with a catalyst having,'}producing a product stream comprising light gases, diesel fuel and a wax from reacting the feed gas with the supported catalyst.4. The process of claim 1 , wherein the catalyst is reduced with hydrogen at temperatures below 650 F.5. The process of claim 1 , wherein the diesel fuel fraction produced is about ⅔ of the non-gas product produced.6. The process of claim 1 , wherein the supported catalyst comprises a lobed support with more than four lobes and an effective pellet radius of less than 600 microns.7. The process of claim 4 , where all of the lobes are not equal lengths.8. The process of claim 4 , wherein the supported catalyst further comprises about 0.01 weight percent to about 2.0 weight percent of a promoter selected from the group consisting of cerium claim 4 , ruthenium claim 4 , lanthanum claim 4 , platinum claim 4 , rhenium. gold claim 4 , nickel claim 4 , or rhodium and a ...

Method for activating strengthened iron catalyst for slurry reactors

A method of activating an iron Fischer-Tropsch catalyst by introducing an inert gas into a reactor comprising a slurry of the catalyst at a first temperature, increasing the reactor temperature from the first temperature to a second temperature at a first ramp rate, wherein the second temperature is in the range of from about 150° C. to 250° C., introducing synthesis gas having a ratio of H 2 :CO to the reactor at a space velocity, and increasing the reactor temperature from the second temperature to a third temperature at a second ramp rate, wherein the third temperature is in the range of from about 270° C. to 300° C. The iron Fischer-Tropsch catalyst may be a precipitated unsupported iron catalyst, production of which is also provided.

Oligomerizacion de alfa oleifinas usando sistemas de catalizador de metaloceno-ssa y uso de las polialfaolefinas resultantes para preparar mezclas lubricantes.

Esta descripción proporciona oligómeros de alfa olefina y polialfaolefinas (o PAOs) y métodos para elaborar los oligómeros de alfa olefina y PAOs. Esta descripción abarca sistemas catalizadores de oligomerización de alfa olefina a base de metaloceno, que incluyen los que comprenden por lo menos un metaloceno y un activador que comprende un óxido sólido tratado químicamente con un anión de extracción de electrones. Los oligómeros de alfa olefina y las PAOs preparados con estos sistemas catalizadores pueden tener un índice de viscosidad alto combinado con un bajo punto de vertido, haciéndolos particularmente útiles en las composiciones lubricantes y como modificadores de viscosidad.

Oligomerization of olefin waxes using metallocene-based catalyst systems

This disclosure provides for olefin wax oligomer compositions, methods of producing olefin wax oligomer composition, and methods for oligomerizing olefin waxes. This disclosure encompasses metallocene-based olefin wax oligomerization catalyst systems, including those that include a metallocene and an aluminoxane, a metallocene and a solid oxide chemically-treated with an electron withdrawing anion, and a metallocene, a solid oxide chemically-treated with an electron withdrawing anion, and an organoaluminum compound. The olefin wax oligomers prepared with these catalyst systems can decreased needle penetrations, increased viscosity, and an increased drop melt, making them useful as an additive in candles, stone polishes, liquid polishes, and mold release formulations.

Oligomerization of alpha olefins using metallocene-ssa catalyst systems and use of the resultant polyalphaolefins to prepare lubricant blends

This disclosure provides for alpha olefin oligomers and polyalphaolefins (or PAOs) and methods of making the alpha olefin oligomers and PAOs. This disclosure encompasses metallocene- based alpha olefin oligomerization catalyst systems, including those that include at least one metallocene and an activator comprising a solid oxide chemically-treated with an electron withdrawing anion. The alpha olefin oligomers and PAOs prepared with these catalyst systems can have a high viscosity index combined with a low pour point, making them particularly useful in lubricant compositions and as viscosity modifiers.

Compositions comprising polyalphaolefins

Compositions comprising polyalphaolefins are disclosed. The polyalphaolefin may be produced from a C 6 to C 16 normal alpha olefin and the polyalphaolefin may comprise less than 1 weight % saturated alpha olefin monomer; less than 3 weight % saturated dimers; and greater than 80 weight % saturated higher oligomers; and have a 100 °C kinematic viscosity of at least 25 cSt; a viscosity index greater than 160; and a pour point less than -35°C. Alternatively, the polyalphaolefin may be produced from a C 6 to C 16 normal alpha olefin comprising at least 80 weight percent of a C 8 normal alpha olefin and the polyalphaolefin may have a pour point less than 0°C; and a Bernoulli index less than 1.65. Alternatively, the polyalphaolefins may be alpha olefin oligomers that may be produced from a C 6 to C 16 normal alpha olefin comprising at least 90 weight percent of a C 8 normal alpha olefin and the alpha olefin oligomer product may comprise less than 1 weight % residual alpha olefin monomer; less than 3 weight % dimers; and greater than 80 weight % higher oligomers; and have a 100 °C kinematic viscosity of at least 25 cSt; and a viscosity index greater than 170. The polyalphaolefins have no discernable crystallization as determined by differential scanning calorimetry using ASTM D 3418.

Methods for hydrocracking a heavy oil feedstock using an in situ colloidal or molecular catalyst and recycling the colloidal or molecular catalyst

A hydrocracking system involves introducing a heavy oil feedstock and a colloidal or molecular catalyst, or a precursor composition capable of forming the colloidal or molecular catalyst, into a hydrocracking reactor. The colloidal or molecular catalyst is formed in situ within the heavy oil feedstock by intimately mixing a catalyst precursor composition into a heavy oil feedstock and raising the temperature of the feedstock to above the decomposition temperature of the precursor composition to form the colloidal or molecular catalyst. The colloidal or molecular catalyst catalyzes upgrading reactions between the heavy oil feedstock and hydrogen and eliminates or reduces formation of coke precursors and sediment. At least a portion of a resid fraction containing residual colloidal or molecular catalyst is recycled back into the hydrocracking reactor to further upgrade the recycled resid fraction portion and provide recycled colloidal or molecular catalyst within the hydrocracking reactor.

Process for preparing hydroprocessing bulk catalysts

A process to prepare hydroprocessing bulk catalysts is provided. The hydroprocessing catalyst has the formula (M t ) a (X u ) b (S v ) d (C w ) e (H x ) f (O y ) g (N z ) h , wherein M is at least one group VIB metal; X is at least at least a metal compound selected from a non-noble Group VIII metal, a Group VIIIB metal, a Group VIB metal, a Group IVB metal, and a Group IIB metal (“Promoter Metal”); t, u, v, w, x, y, z representing the total charge for each of the components (M, X, S, C, H, O and N, respectively); ta+ub+vd+we+xf+yg+zh=0; and 0=<b/a=<5, (a+0.5b)<=d<=(5a+2b), 0<=e<=11(a+b), 0<=f<=7(a+b), 0<=g<=5(a+b), 0<=h<=0.5(a+b). In one embodiment, the process comprises the steps of: combining and reacting at least one Group VIB metal compound with at least one group VIII non-noble metal compound to obtain an intermediate mixture; sulfiding the intermediate mixture with a sulfiding agent forming a catalyst precursor; and mixing the catalyst precursor with a hydrocarbon compound to form the hydroprocessing catalyst composition.

Ebullated bed hydroprocessing systems

An ebullated bed hydroprocessing system, and also a method for upgrading a pre-existing ebullated bed hydroprocessing system, involves introducing a colloidal or molecular catalyst, or a precursor composition capable of forming the colloidal or molecular catalyst, into an ebullated bed reactor. The colloidal or molecular catalyst is formed by intimately mixing a catalyst precursor composition into a heavy oil feedstock and raising the temperature of the feedstock to above the decomposition temperature of the precursor composition to form the colloidal or molecular catalyst in situ. The improved ebullated bed hydroprocessing system includes at least one ebullated bed reactor that employs both a porous supported catalyst and the colloidal or molecular catalyst to catalyze hydroprocessing reactions involving the feedstock and hydrogen. The colloidal or molecular catalyst provides catalyst in what would otherwise constitute catalyst free zones within the ebullated bed hydroprocessing system. Asphaltene or other hydrocarbon molecules too large to diffuse into the pores of the supported catalyst can be upgraded by the colloidal or molecular catalyst. A slurry phase reactor may be positioned upstream from one or more ebullated bed reactors or converted from a pre-existing ebullated bed reactor.

Process for upgrading heavy oil using a highly active slurry catalyst compositon

The instant invention is directed to a process for upgrading heavy oils using a slurry composition. The slurry composition is prepared in a series of steps, involving mixing a Group VIB metal oxide with aqueous ammonia to form an aqueous mixture and sulfiding the mixture to form a slurry. The slurry is then promoted with a Group VIII metal compound. Subsequent steps involve mixing the slurry with a hydrocarbon oil, and combining the resulting mixture with hydrogen gas (under conditions which maintain the water in a liquid phase) to produce the active slurry catalyst.

使用高活性浆料催化剂组合物进行重油改质的方法

申请人开发了新的渣油完全加氢转化浆料反应器系统，该系统允许所述催化剂、未转化的油和转化了的油以连续混合物的形式循环遍及整个反应器，而对所述混合物没有限制。所述混合物在所述反应器之间被部分分离以仅移出所述产物和氢气，而允许未转化的油和浆料催化剂继续进入下一个后续反应器。然后将一部分未转化的油转化成较低沸点的烃，再次产生未转化的油、产物、氢气和浆料催化剂的混合物。可以在另外的反应器中进行进一步加氢处理，完全转化所述油。可以将额外的油加入到级间原料入口，原料有可能与浆料混合。可以交替地部分转化所述油，留下位于未转化的油中的高度浓缩的催化剂，可将其直接再循环到所述第一反应器中。

Process for producing novel synthetic basestocks

This disclosure relates to a liquid syndiotactic polyalphaolefϊn, sPAO, comprising one or more C 4 to C 24 monomers, said sPAO having: a) an rr triad content of 5 to 50 % as measured by 13 C NMR; b) an mr triad content of 25 to 60 % as measured by 13 C NMR, where the mr to mm triad ratio is at least 1.0; c) a pour point of Z °C or less, where Z = 0.0648X-51.2, where X = kinematic viscosity at 100 °C as reported in centistokes (cSt); d) a kinematic viscosity at 100 °C of 100 cSt or more (alternatively 200 cSt or more); e) a ratio of mr triads to rr triad (as determined by 13 C NMR) of less than 9; f) a ratio of vinylidene to 1,2-disubstituted olefins (as determined by 1 H NMR) of less than 8; g) a viscosity index of 120 or more; and h) an Mn of 40,000 or less. This disclosure further relates to processes to make and use sPAOs, including those having any combination of characterics a) to h).

Lubricants from mixed alpha-olefin feeds

This invention discloses an improved process which employs mixed alpha-olefms as feed over activated metallocene catalyst systems to provide essentially random liquid polymers particularly useful in lubricant components or as functional fluids.

Process for producing novel synthetic basestocks

This disclosure relates to a liquid syndiotactic polyalphaolefin, sPAO, comprising one or more C 4 to C 24 monomers, said sPAO having: a) an rr triad content of 5 to 50% as measured by 13 C NMR; b) an mr triad content of 25 to 60% as measured by 13 C NMR, where the mr to mm triad ratio is at least 1.0; c) a pour point of Z° C. or less, where Z=0.0648X−51.2, where X=kinematic viscosity at 100° C. as reported in centistokes (cSt); d) a kinematic viscosity at 100° C. of 100 cSt or more (alternatively 200 cSt or more); e) a ratio of mr triads to rr triad (as determined by 13 C NMR) of less than 9; f) a ratio of vinylidene to 1,2-disubstituted olefins (as determined by 1 H NMR) of less than 8; g) a viscosity index of 120 or more; and h) an Mn of 40,000 or less. This disclosure further relates to processes to make and use sPAOs, including those having any combination of characterics a) to h).

Process for producing novel synthetic basestocks

This disclosure relates to a liquid syndiotactic polyalphaolefin, sPAO, comprising one or more C 4 to C 24 monomers, said sPAO having: a) an rr triad content of 5 to 50% as measured by 13 C NMR; b) an mr triad content of 25 to 60% as measured by 13 C NMR, where the mr to mm triad ratio is at least 1.0; c) a pour point of Z ° C. or less, where Z=0.0648X−51.2, where X=kinematic viscosity at 100° C. as reported in centistokes (cSt); d) a kinematic viscosity at 100° C. of 100 cSt or more (alternatively 200 cSt or more); e) a ratio of mr triads to rr triad (as determined by 13 C NMR) of less than 9; f) a ratio of vinylidene to 1,2-disubstituted olefins (as determined by 1 H NMR) of less than 8; g) a viscosity index of 120 or more; and h) an Mn of 40,000 or less. This disclosure further relates to processes to make and use sPAOs, including those having any combination of characteristics a) to h).

Lubricants from mixed alpha-olefin feeds

This invention discloses an improved process which employs mixed alpha-olefms as feed over activated metallocene catalyst systems to provide essentially random liquid polymers particularly useful in lubricant components or as functional fluids.

Process for Producing Novel Synthetic Basestocks

This disclosure relates to a liquid syndiotactic polyalphaolefin, sPAO, comprising one or more C 4 to C 24 monomers, said sPAO having: a) an rr triad content of 5 to 50% as measured by 13 C NMR; b) an mr triad content of 25 to 60% as measured by 13 C NMR, where the mr to mm triad ratio is at least 1.0; c) a pour point of Z ° C. or less, where Z=0.0648X-51.2, where X=kinematic viscosity at 100° C. as reported in centistokes (cSt); d) a kinematic viscosity at 100° C. of 100 cSt or more (alternatively 200 cSt or more); e) a ratio of mr triads to rr triad (as determined by 13 C NMR) of less than 9; f) a ratio of vinylidene to 1,2-disubstituted olefins (as determined by 1 H NMR) of less than 8; g) a viscosity index of 120 or more; and h) an Mn of 40,000 or less. This disclosure further relates to processes to make and use sPAOs, including those having any combination of characteristics a) to h).

用于生产新型合成基础油料的方法

本公开涉及液体间规聚α‑烯烃sPAO，其包含一种或多种C 4 －C 24 单体，所述sPAO具有:a)5－50％的rr三单元组含量，通过 13 C NMR测定；b)25－60％的mr三单元组含量，通过 13 C NMR测定，其中mr与mm三单元组之比为至少1.0；c)Z℃或更低的倾点，其中Z＝0.0648X‑51.2，其中X＝在100℃的运动粘度，单位为厘沲(cSt)；d)100cSt或更大(或者200cSt或更大)的在100℃的运动粘度；e)小于9的mr三单元组与rr三单元组之比，通过 13 C NMR测定；f)小于8的亚乙烯基与1,2‑二取代烯烃之比，通过 1 H NMR测定；g)120或更大的粘度指数；和h)40,000或更小的Mn。本公开还涉及制备和使用包括具有特征a)‑h)的任何组合的那些sPAO在内的sPAO的方法。

Silicoaluminophosphate molecular sieve

The present invention relates to a silicoaluminophosphate molecular sieve comprising at least one intergrown phase of molecular sieves having AEI and CHA framework types, wherein said intergrown phase has an AEI/CHA ratio of from about 5/95 to 40/60 as determined by DIFFaX analysis, using the powder X-ray diffraction pattern of a calcined sample of said silicoaluminophosphate molecular sieve. It also relates to methods for its preparation and to its use in the catalytic conversion of methanol to olefins.

Silicoaluminophosphate molecular sieve

The present invention relates to a silicoaluminophosphate molecular sieve comprising at least one intergrown phase of molecular sieves having AEI and CHA framework types, wherein said intergrown phase has an AEI/CHA ratio of from about 5/95 to 40/60 as determined by DIFFaX analysis, using the powder X-ray diffraction pattern of a calcined sample of said silicoaluminophosphate molecular sieve. It also relates to methods for its preparation and to its use in the catalytic conversion of methanol to olefins.

Oligomer oils and their manufacture

A multistep process for the selective production of an oligomer oil having predetermined properties in which the first step involves the polymerization of a feedstock containing one or more C 3 to C 20 1-olefins in the presence of a catalyst comprising a bulky ligand transition metal catalyst and in which a subsequent step involves the olgiomerization of at least a preselected fraction of the product of the first step.

Lubricants from mixed alpha-olefin feeds

Oligomerization of alpha olefins using metallocene-ssa catalyst systems and use of the resultant polyalphaolefins to prepare lubricant blends

This disclosure provides for alpha olefin oligomers and polyalphaolefins (or PAOs) and methods of making the alpha olefin oligomers and PAOs. This disclosure encompasses metallocene-based alpha olefin oligomerization catalyst systems, including those that include at least one metallocene and an activator comprising a solid oxide chemically-treated with an electron withdrawing anion. The alpha olefin oligomers and PAOs prepared with these catalyst systems can have a high viscosity index combined with a low pour point, making them particularly useful in lubricant compositions and as viscosity modifiers.

Oligomerization of olefin waxes using metallocene-based catalyst systems

This disclosure provides for olefin wax oligomer compositions, methods of producing olefin wax oligomer composition, and methods for oligomerizing olefin waxes. This disclosure encompasses metallocene-based olefin wax oligomerization catalyst systems, including those that include a metallocene and an aluminoxane, a metallocene and a solid oxide chemically-treated with an electron withdrawing anion, and a metallocene, a solid oxide chemically-treated with an electron withdrawing anion, and an organoaluminum compound. The olefin wax oligomers prepared with these catalyst systems can decreased needle penetrations, increased viscosity, and an increased drop melt, making them useful as an additive in candles, stone polishes, liquid polishes, and mold release formulations.

Oligomerization of alpha olefins using metallocene-SSA catalyst systems and use of the resultant polyalphaolefins to prepare lubricant blends

This disclosure provides for alpha olefin oligomers and polyalphaolefins (or PAOs) and methods of making the alpha olefin oligomers and PAOs. This disclosure encompasses metallocene-based alpha olefin oligomerization catalyst systems, including those that include at least one metallocene and an activator comprising a solid oxide chemically-treated with an electron withdrawing anion. The alpha olefin oligomers and PAOs prepared with these catalyst systems can have a high viscosity index combined with a low pour point, making them particularly useful in lubricant compositions and as viscosity modifiers.

Oligomerization of alpha olefins using metallocene-SSA catalyst systems and use of the resultant polyalphaolefins to prepare lubricant blends

This disclosure provides for alpha olefin oligomers and polyalphaolefins (or PAOs) and methods of making the alpha olefin oligomers and PAOs. This disclosure encompasses metallocene-based alpha olefin oligomerization catalyst systems, including those that include at least one metallocene and an activator comprising a solid oxide chemically-treated with an electron withdrawing anion. The alpha olefin oligomers and PAOs prepared with these catalyst systems can have a high viscosity index combined with a low pour point, making them particularly useful in lubricant compositions and as viscosity modifiers.

Oligomerization of alpha olefins using metallocene-SSA catalyst systems and use of the resultant polyalphaolefins to prepare lubricant blends

Methods for making alpha olefin oligomers and polyalphaolefins include a step of contacting a C 4 to C 20 alpha olefin monomer and a catalyst system containing a metallocene, a first activator comprising a solid oxide chemically-treated with an electron withdrawing anion, and a second activator comprising an organoaluminum compound. The alpha olefin oligomers and polyalphaolefins prepared with these catalyst systems can have a high viscosity index combined with a low pour point, making them particularly useful in lubricant compositions and as viscosity modifiers.

Activation of hydrocarbon synthesis catalyst

Zeolite Supported Cobalt Hybrid Fischer-Tropsch Catalyst

A method for forming a catalyst for synthesis gas conversion comprises impregnating a zeolite extrudate using a solution, for example, a substantially non-aqueous solution, comprising a cobalt salt to provide an impregnated zeolite extrudate and activating the impregnated zeolite extrudate by a reduction-oxidation-reduction cycle.

Zeolite supported cobalt hybrid fischer-tropsch catalyst

A method for performing synthesis gas conversion is disclosed which comprises contacting synthesis gas with a hybrid Fischer-Tropsch catalyst formed by impregnating a ZSM-12 zeolite extrudate using a solution, for example, a substantially non-aqueous solution, comprising a cobalt salt and activating the impregnated zeolite extrudate by a reduction-oxidation-reduction cycle. The method results in reduced methane yield and increased yield of liquid hydrocarbons substantially free of solid wax.

Process for preparing cobalt catalysts on a titanium oxide support

Fischer-Tropsch catalysts

A method of producing an alumina-supported cobalt catalyst for use in a Fischer-Tropsch synthesis reaction, which comprises: calcining an initial γ-alumina support material at a temperature to produce a modified alumina support material; impregnating the modified alumina support material with a source of cobalt; calcining the impregnated support material, activating the catalyst with a reducing gas, steam treating the activated catalyst, and activating the steam treated catalyst with a reducing gas.

Method for activating strengthened iron catalyst for slurry reactors

Method of activating a Fischer-Tropsch catalyst

This invention relates to the field of Fischer-Tropsch catalysis, in particular to activation of a Fischer-Tropsch catalyst. More particularly the invention relates to a method of activating an iron based Fischer-Tropsch catalyst which includes iron in a positive oxidation state by contacting in a reactor said iron based catalyst with a reducing gas selected from the group consisting of CO and a combination of H 2 and CO; at a temperature of at least 245° C. and below 280° C.; at a reducing gas pressure of above 0.5 MPa and not more than 2.2 MPa; and at a GHSV of total gas fed to the reactor of at least 6000 ml(N)/g cat/h, thereby reducing the iron that is in a positive oxidation step in the catalyst.

Fischer-tropsch catalysts

A method of producing an aluminum oxide supported catalyst for use in a Fischer-Tropsch synthesis reaction, which comprises: spray-drying a slurry of γ-alumina and a source of a spinel forming metal to form a solid precursor material; calcining the precursor material to form a modified support material including a metal aluminate spinel; impregnating the modified alumina support material with a source of cobalt; calcining the impregnated support material, and activating the catalyst.

Catalyst activation in fischer-tropsch processes

A system for activating Fischer-Tropsch catalyst comprising a reactor having a reactor outlet for overhead gas and operable under suitable conditions whereby a catalyst in a volume of liquid carrier comprising Fischer-Tropsch diesel, hydrocracking recycle oil, or a combination thereof may be activated in the presence of an activation gas; a condenser comprising an inlet fluidly connected to the reactor outlet for overhead gas and comprising a condenser outlet for condensed liquids; and a separation unit comprising an inlet fluidly connected to the condenser outlet and a separator outlet for a stream comprising primarily Fischer-Tropsch diesel; and a recycle line fluidly connecting the separator outlet, a hydrocracking unit, or both to the reactor, whereby Fischer-Tropsch diesel recovered from the reactor overhead gas, hydrocracking recycle oil, or a combination thereof may serve as liquid carrier for catalyst in the reactor. A method for activating Fischer-Tropsch catalyst is also provided.

Protected Fischer-Tropsch catalyst and method of providing same to a Fischer-Tropsch process

A method of preparing a spray dried catalyst by combining spray dried catalyst particles with wax so the spray dried catalyst particles are coated with wax, yielding wax coated catalyst particles, and shaping the wax coated catalyst to provide shaped wax coated catalyst. A method of activating Fischer-Tropsch catalyst particles containing oxides by contacting the catalyst particles with a reducing gas in an activation vessel to produce an activated catalyst, wherein contacting is performed in the absence of a liquid medium under activation conditions. A system for activating a Fischer-Tropsch catalyst containing an activation reactor configured to introduce an activation gas to a fixed or fluidized bed of the Fischer-Tropsch catalyst in the absence of a liquid medium and at least one separation device configured to separate a gas stream comprising entrained catalyst fines having an average particle size below a desired cutoff size from the activation reactor.

A hydrocarbon synthesis process

This invention relates to a Fischer Tropsch process using a catalyst activated in accordance with the invention. More particularly the invention relates to a three phase Low Temperature Fischer Tropsch process wherein CO and H2 are converted to hydrocarbons and possibly oxygenates thereof by contacting syngas including CO and H2 in the presence of an iron based Fischer Tropsch catalyst, wherein the ratio of H2:CO in the feed is between 2.5 and 1, and wherein the iron based Fischer Tropsch catalyst is activated according to the steps of: (a) providing an iron catalyst including iron in a positive oxidation state; and (b) contacting the iron catalyst in a reactor with a reducing gas selected from CO and a combination of H2 and CO; at a temperature of at least 245°C and below 28O°C; at a reducing gas pressure of above 0.5 MPa and not more than 2.2 MPa; and at a GHSV of total gas fed to the reactor of at least 6000 ml(N)/g cat/h, thereby reducing the iron that is in a positive oxidation step in the catalyst.

Method for activating strengthened iron catalyst for slurry reactors

A method of activating an iron Fischer-Tropsch catalyst by introducing an inert gas into a reactor comprising a slurry of the catalyst at a first temperature, increasing the reactor temperature from the first temperature to a second temperature at a first ramp rate, wherein the second temperature is in the range of from about 150°C to 250°C, introducing synthesis gas having a ratio of H2:CO to the reactor at a space velocity, and increasing the reactor temperature from the second temperature to a third temperature at a second ramp rate, wherein the third temperature is in the range of from about 270°C to 300°C. The iron Fischer-Tropsch catalyst may be a precipitated unsupported iron catalyst, production of which is also provided.

Catalysts

A process for producing a supported cobalt-based Fischer-Tropsch synthesis catalyst includes, in a first activation stage, treating a particulate catalyst precursor with a reducing gas, at a heating rate, HR1, until the precursor has reached a temperature, T1, where 80°C≤T1 ≤180°C, to obtain a partially treated precursor. In a second activation stage, the partially treated precursor is treated with a reducing gas, at an average heating rate, HR2, with x step increments, where 0<HR2<HR1, for a time, t1, where t1 is from 0.1 to 20 hours, to obtain a partially reduced precursor. Thereafter, in a third activation stage, the partially reduced precursor is treated with a reducing gas, at a heating rate, HR3, where HR3>HR2 until the partially reduced precursor reaches a temperature, T2. The partially reduced precursor is maintained at T2 for a time, t2, where t2 is from 0 to 20 hours, to obtain an activated catalyst.

Fischer tropsch process

The present invention relates to a process for converting synthesis gas to hydrocarbons, in particular to hydrocarbons in the C5-C60 range particularly suitable for use as liquid motor fuels, in a slurry reactor in the presence of a Fischer-Tropsch catalyst comprising cobalt and zinc oxide wherein the Fischer-Tropsch catalyst is activated with a reducing gas consisting of hyrogen and an inert gas at 330 to 400 °C prior to contact with synthesis gas in the slurry reactor.

Fischer Tropsch Process

The present invention relates to a process for converting synthesis gas to hydrocarbons, in particular to hydrocarbons in the C5-C60 range particularly suitable for use as liquid motor fuels, in a slurry reactor in the presence of a Fischer-Tropsch catalyst comprising cobalt and zinc oxide wherein the Fischer-Tropsch catalyst is activated with a reducing gas consisting of hydrogen and an inert gas at 330 to 400° C. prior to contact with synthesis gas in the slurry reactor.

Method for activating strengthened iron catalyst for slurry reactors

A method of activating an iron Fischer-Tropsch catalyst by introducing an inert gas into a reactor comprising a slurry of the catalyst at a first temperature, increasing the reactor temperature from the first temperature to a second temperature at a first ramp rate, wherein the second temperature is in the range of from about 150°C to 250°C, introducing synthesis gas having a ratio of H2:CO to the reactor at a space velocity, and increasing the reactor temperature from the second temperature to a third temperature at a second ramp rate, wherein the third temperature is in the range of from about 270°C to 300°C. The iron Fischer-Tropsch catalyst may be a precipitated unsupported iron catalyst, production of which is also provided.

Method for the preparation of a hydrocarbon synthesis catalyst material and the use thereof in a hydrocarbon synthesis process

This invention relates to a method for the preparation of a hydrocarbon synthesis catalyst material, in the form of a hydrocarbon synthesis catalyst precursor and/or catalyst, preferably, a Fischer Tropsch synthesis catalyst precursor and/or catalyst. The invention also extends to the use of a catalyst precursor and/or catalyst prepared by the method according to the invention in a hydrocarbon synthesis process, preferably, a Fischer Tropsch synthesis process. According to this invention, a method for the preparation of a hydrocarbon synthesis catalyst material includes the steps of treating Fe(II) carboxylate in solution with an oxidising agent to convert it to Fe(III) carboxylate in solution under conditions which ensure that such oxidation does not take place simultaneously with any dissolution of Fe(0); and hydrolysing the Fe(III) carboxylate solution resulting from step (iii) and precipitating one or more Fe(III) hydrolysis products.

Cobalt catalysts

Catalysts comprising cobalt on a titania support are produced by mixing together particles of a solid titania support and an aqueous solution of cobalt amine carbonate, and heating to an elevated temperature sufficient to effect decomposition of the cobalt amine carbonate and precipitation of a cobalt species onto said support. The catalysts are useful in hydrogenation and Fischer-Tropsch reactions.

Method for activating strengthened iron catalyst for slurry reactors

A method of activating an iron Fischer-Tropsch catalyst by introducing an inert gas into a reactor comprising a slurry of the catalyst at a first temperature, increasing the reactor temperature from the first temperature to a second temperature at a first ramp rate, wherein the second temperature is in the range of from about 150° C. to 250° C., introducing synthesis gas having a ratio of H 2 :CO to the reactor at a space velocity, and increasing the reactor temperature from the second temperature to a third temperature at a second ramp rate, wherein the third temperature is in the range of from about 270° C. to 300° C. The iron Fischer-Tropsch catalyst may be a precipitated unsupported iron catalyst, production of which is also provided.

Method for activating strengthened iron catalyst for slurry reactors

A method of activating an iron Fischer-Tropsch catalyst by introducing an inert gas into a reactor comprising a slurry of the catalyst at a first temperature, increasing the reactor temperature from the first temperature to a second temperature at a first ramp rate, wherein the second temperature is in the range of from about 150 to 250°C, introducing synthesis gas having a ratio of H:CO to the reactor at a space velocity, and increasing the reactor temperature from the second temperature to a third temperature at a second ramp rate, wherein the third temperature is in the range of from about 270 to 300°C. The iron Fischer-Tropsch catalyst may be a precipitated unsupported iron catalyst, production of which is also provided.

Method for activating strengthened iron catalyst for slurry reactors

A method of activating an iron Fischer-Tropsch catalyst by introducing an inert gas into a reactor comprising a slurry of the catalyst at a first temperature, increasing the reactor temperature from the first temperature to a second temperature at a first ramp rate, wherein the second temperature is in the range of from about 150°C to 250°C, introducing synthesis gas having a ratio of H2:CO to the reactor at a space velocity, and increasing the reactor temperature from the second temperature to a third temperature at a second ramp rate, wherein the third temperature is in the range of from about 270°C to 300°C. The iron Fischer-Tropsch catalyst may be a precipitated unsupported iron catalyst, production of which is also provided.

浆料反应器用强化型铁催化剂的活化方法

本发明公开了活化铁费-托催化剂的方法，所述方法包括将惰性气体导入处于第一温度下的包含催化剂浆料的反应器，将反应器温度以第一变温速率从第一温度升高到第二温度，其中第二温度在约150℃至250℃的范围内，将具有一定H 2 ∶CO比率的合成气以一定的空速导入反应器，并将反应器温度以第二变温速率从第二温度升高到第三温度，其中第三温度在约270℃至300℃的范围内。铁费-托催化剂可以是沉淀无载体铁催化剂，其生产也提供在本发明中。

Method for activating strengthened iron catalyst for slurry reactors

A method of activating an iron Fischer-Tropsch catalyst by introducing an inert gas into a reactor comprising a slurry of the catalyst at a first temperature, increasing the reactor temperature from the first temperature to a second temperature at a first ramp rate, wherein the second temperature is in the range of from about 150°C to 250°C, introducing synthesis gas having a ratio of H2:CO to the reactor at a space velocity, and increasing the reactor temperature from the second temperature to a third temperature at a second ramp rate, wherein the third temperature is in the range of from about 270°C to 300°C. The iron Fischer-Tropsch catalyst may be a precipitated unsupported iron catalyst, production of which is also provided.

Three phase low temperature fischer tropsch process

This invention relates to a Fischer Tropsch process using a catalyst activated in accordance with the invention. More particularly the invention relates to a three phase Low Temperature Fischer Tropsch process wherein CO and Hare converted to hydrocarbons and possibly oxygenates thereof by contacting syngas including CO and Hin the presence of an iron based Fischer Tropsch catalyst, wherein the ratio of H:CO in the feed is between 2.5 and 1, and wherein the iron based Fischer Tropsch catalyst is activated according to the steps of: (a) providing an iron catalyst including iron in a positive oxidation state; and (b) contacting the iron catalyst in a reactor with a reducing gas selected from CO and a combination of Hand CO; at a temperature of at least and below ; at a reducing gas pressure of above 0.5 MPa and not more than 2.2 MPa; and at a GHSV of total gas fed to the reactor of at least 6000 ml(N)/g cat/h, thereby reducing the iron that is in a positive oxidation step in the catalyst.

Method for activating strengthened iron catalyst for slurry reactors

A method of activating an iron Fischer-Tropsch catalyst by introducing an inert gas into a reactor comprising a slurry of the catalyst at a first temperature, increasing the reactor temperature from the first temperature to a second temperature at a first ramp rate, wherein the second temperature is in the range of from about 150°C to 250°C, introducing synthesis gas having a ratio of H2:CO to the reactor at a space velocity, and increasing the reactor temperature from the second temperature to a third temperature at a second ramp rate, wherein the third temperature is in the range of from about 270°C to 300°C. The iron Fischer-Tropsch catalyst may be a precipitated unsupported iron catalyst, production of which is also provided.

浆料反应器用强化型铁催化剂的活化方法

本发明公开了活化铁费-托催化剂的方法，所述方法包括将惰性气体导入处于第一温度下的包含催化剂浆料的反应器，将反应器温度以第一变温速率从第一温度升高到第二温度，其中第二温度在约150℃至250℃的范围内，将具有一定H 2 ∶CO比率的合成气以一定的空速导入反应器，并将反应器温度以第二变温速率从第二温度升高到第三温度，其中第三温度在约270℃至300℃的范围内。铁费-托催化剂可以是沉淀无载体铁催化剂，其生产也提供在本发明中。

Method for activating strengthened iron catalyst for slurry reactors

A method of activating an iron Fischer-Tropsch catalyst by introducing an inert gas into a reactor comprising a slurry of the catalyst at a first temperature, increasing the reactor temperature from the first temperature to a second temperature at a first ramp rate, wherein the second temperature is in the range of from about 150°C to 250°C, introducing synthesis gas having a ratio of H2:CO to the reactor at a space velocity, and increasing the reactor temperature from the second temperature to a third temperature at a second ramp rate, wherein the third temperature is in the range of from about 270°C to 300°C. The iron Fischer-Tropsch catalyst may be a precipitated unsupported iron catalyst, production of which is also provided.

Method for activating strengthened iron catalyst for slurry reactors

Method for activating strengthened iron catalyst for slurry reactors