СПОСОБ ПОЛУЧЕНИЯ ТОПЛИВНЫХ ДИСТИЛЛЯТОВ

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

КРИСТАЛЛИЧЕСКИЙ ОКСИГИДРОКСИД-МОЛИБДОВОЛЬФРАМАТ ПЕРЕХОДНОГО МЕТАЛЛА

Разработан активный катализатор гидрообработки, предназначенный для использования в процессах конверсии углеводородов: гидроденитрификации, гидрообессеривания, гидродеметаллирования, гидродесиликации, гидродеароматизации, гидроизомеризации, гидроочистки, гидрофайнинга и гидрокрекинга. Катализатор представляет собой материал кристаллического оксигидроксида-молибдовольфрамата металла, имеющего формулу:(NH)M(OH)MoWO,где а находится в диапазоне от 0,1 до 10; М представляет собой металл, выбранный из Mg, Mn, Fe, Co, Ni, Cu, Zn и их смесей; b находится в диапазоне от 0,1 до 2; х находится в диапазоне от 0,5 до 1,5; у находится в диапазоне от 0,01 до 0,4; где сумма (x+y) должна быть ≤1,501; z представляет собой число, которое соответствует сумме валентностей а, M, b, x и y; при этом материал имеет порошковую рентгендифрактограмму, показывающую пики при d-расстояниях, перечисленных в таблице A:Таблица А3 н. и 7 з.п. ф-лы, 1 ил., 1 табл., 3 пр.

СПОСОБ ПОЛУЧЕНИЯ МАЛОСЕРНИСТЫХ НЕФТЯНЫХ ФРАКЦИЙ

Использование: нефтехимия. Сущность: проводят обработку нефтяных фракций в среде водорода при повышенных давлении и температуре с использованием каталитических систем, состоящих из катализаторов, обладающих функциями изменения углеводородного состава и очистки от элементоорганических соединений. При этом процесс осуществляется на каталитической системе, состоящей из двух и более катализаторов, при температуре не менее 300°С, давлении не менее 3,0 МПа, при соотношении водород:сырье (А, нм3/м3), которое вычисляется по формуле А=В+С+D, где В - соотношение водород:сырье для осуществления реакций гидрогенолиза элементоорганических соединений, нм3/м3; С - соотношение водород:сырье для осуществления реакций гидрирования непредельных соединений, нм3/м3; D - соотношение водород:сырье для осуществления реакций превращения высококипящих углеводородов, нм3/м3. Технический результат: повышение выхода светлых фракций с улучшенными экологическими показателями. 8 з.п. ф-лы, 8 табл.

ADDITIVE FOR HYDROCONVERSION HEAVY HYDROCARBON OIL

Способ переработки высококипящих фракций каменноугольной смолы

Катализатор для гидрокрекинга нефтяных фракций

Stable olefinic, low sulfur diesel fuels

A NEW ALUMINIUM HYDROXIDE PHASE AND OF IT MADE CATALYSTS

PROCEDURE FOR THE PRODUCTION OF CRACK PRODUCTS WITH LOW SULFUR AND STICKSTOFFGEHALT

METAL MIXED CATALYST COMPOSITION, THEIR PRODUCTION AND USE

PROCESS FOR PREPARING LOW POUR MIDDLE DISTILLATES AND LUBE OIL USING A CATALYST CONTAINING A SILICOALUMINOPHOSPHATE MOLECULAR SIEVE

LAYERED METAL OXIDES CONTAINING INTERLAYER OXIDES AND THEIR SYNTHESIS

Hydrocracking catalyst comprising a microporous crystalline solid material

Hydroconversion process using bulk group VIII/group VIB catalysts

HYDROCRACKING PROCESS USING BULK GROUP VIII/GROUP VIB CATALYSTS

Hydrocracking process for hydrocracking petroleum and chemical feedstocks using bulk Group VIII/Group VIB catalysts. Preferred catalysts include those comprised of Ni-Mo-W.

A NEW ALUMINUM TRIHYDROXIDE PHASE AND CATALYSTS MADE THEREFROM

A newly discovered phase of aluminum trihydroxide and supports and catalysts made therefrom. This invention also relates to methods of producing this new phase of aluminum trihydroxide and catalysts made therefrom, and to a method for improving the activity of and for regenerating catalysts having a silica- alumina support.

HYDROTREATING USING BULK MULTIMETALLIC CATALYSTS

... ▓▓▓Hydrotreating a petroleum feedstream comprised of at least 50 wt. % of an ▓atmospheric distillation distillate boiling range product stream, preferably ▓hydrodesulfurization of raw virgin petroleum distillates, using a bulk ▓multimetallic catalyst comprised of at least one Group VIII non-noble metal ▓and at least two Group VIB metal wherein the ratio of Group VIB metal to Group ▓VIII metal is from about 10:1 to 1:10.▓ ...

HYDROPROCESSING USING BULK GROUP VIII/GROUP VIB CATALYSTS

A process fo hydroprocessing petroleum and chemical feedstocks by use of a bulk multimetallic catalyst comprised of at least one Group VIII non-noble metal and at least one, preferably two Group VIB metal wherein the ratio of Group VIB metal to Group VIII metal is from about 10:1 to 1:10.

PROCESS FOR THE PREPARATION OF A SHAPED BULK CATALYST

The invention relates to a process for the preparation of a shaped bulk catalyst comprising metal oxide particles comprising one or more Group VlIl metals and two or more Group VIB metals which process comprises the steps of providing first metal oxidic particles comprising one or more first Group VIII metals and one or more first Group VIB metals, providing separately prepared second metal oxidic particles comprising one or more second Group VIII metals and one or more second Group VIB metals, wherein the composition of Group VIB and Group VIII metals in the first and second metal oxidic particles are different, combining the first and second metal oxidic particles before and/or during shaping and shaping the combined first and second metal oxide particles to form a shaped bulk catalyst. The invention further relates to the shaped bulk catalyst obtainable with the process In sulphided or unsulphided form and the use thereof in hydroprocessing.

BAYERITE AND/OR ETA ALUMINA CATALYTIC CRACKING CATALYSTS

Catalytic cracking catalysts and catalyst additives which contain silica modified bayerite and/or eta alumina are disclosed. The catalysts of the present invention may be used in the preparation of catalytic compositions.

SYNTHETIC POROUS CRYSTALLINE MATERIAL, ITS SYNTHESIS AND USE

This invention relates to a composition of matter comprising an inorganic, porou s crystalline phase material exhibiting, after calcination, an X-ray diffraction pattern with at least one peak at a d-sp acing greater than 1.8 nm and having a benzene adsorption capacity of greater than 15 grams benzene per 100 grams of said mater ial at 6.7 kPa (50 torr) and 25 .degree.C. Preferably, the crystalline phase material has a hexagonal arrangement of uniformly-sized pores at least 1.3 nm in diameter and exhibiting, after calcination, a hexagonal electron diffraction pattern that can be indexed with a d 100 value greater than 1.8 nm.

SYNTHETIC DIOCTAHEDRAL SMECTITE CLAYS

... "SYNTHETIC DIOCTAHEDRAL SMECTITE CLAYS" A novel synthetic dioctahedral smectite layered clay, a process for preparing the clay and a process using the clay is disclosed. The clays that are prepared are gallium/silicon, gallium/germanium, or aluminum/germanium smectite clays. The clay is prepared from a reaction mixture containing reactive sources of the metals, i.e., aluminum, silicon, gallium and germanium, a templating agent and water. This reaction mixture is reacted at a pH of 8.5 to 14, a temperature of 150 to 210.degree.C for a time of 1 to 20 days to give a desired composition. The clay compositions of theinstant invention can be used to catalyze various hydrocarbon conversion processes such as alkylation and hydrocracking.

PROCEDURE FOR THE PRODUCTION OF FUEL FOR GASOLINE AND DIESEL ENGINES FROM MINERAL WASTE OIL BY HYDROCRACKEN.

СЫПУЧАЯ КАТАЛИТИЧЕСКАЯ КОМПОЗИЦИЯ И СПОСОБ ПРИГОТОВЛЕНИЯ СЫПУЧЕЙ КАТАЛИТИЧЕСКОЙ КОМПОЗИЦИИ

Данное изобретение относится к сыпучей каталитической композиции, включающей в себя частицы оксидов металлов, содержащих один или более металлов VIII группы и два или более металлов VIB группы, причем сыпучая каталитическая композиция включает в себя первые частицы оксидов металлов, содержащие один или более первых металлов VIII группы и один или более первых металлов VIB группы, и отдельно приготовленные вторые частицы оксидов металлов, содержащие один или более вторых металлов VIII группы и один или более вторых металлов VIB группы, где состав металлов VIB группы и VIII группы в первых и вторых частицах оксидов металлов различен, где первые и вторые сыпучие частицы оксидов отдельно сформованы для разделения первых и вторых сформованных частиц сыпучего катализатора, которые объединяют, предпочтительно до образования гомогенной смеси, для получения сыпучей каталитической композиции. Данное изобретение также относится к способу получения сыпучей каталитической композиции и гидрообработке ...

СПОСОБ ПОЛУЧЕНИЯ ФОРМОВАННОГО СЫПУЧЕГО КАТАЛИЗАТОРА

Изобретение относится к способу получения формованного сыпучего катализатора, включающего частицы оксидов металла, включающие один или более первых металлов VIII группы и два или более первых металлов VIB группы, предложение полученных отдельно вторых частиц оксидов металла, включающих один или более вторых металлов VIII группы и один или более вторых металлов VIB группы, где сочетания металлов VIB группы и VIII группы в первых и вторых частицах оксидов металла являются различными, объединение первых и вторых частиц оксидов металла до и/или во время формования и формование объединенных первых и вторых частиц оксидов металла с образованием формованного сыпучего катализатора. Кроме того, изобретение относится к формованному сыпучему катализатору, получаемому способом, в сульфидированной или несульфидированной форме и его использованию в гидрообработке.

СЫПУЧАЯ КАТАЛИТИЧЕСКАЯ КОМПОЗИЦИЯ И СПОСОБ ПРИГОТОВЛЕНИЯ СЫПУЧЕЙ КАТАЛИТИЧЕСКОЙ КОМПОЗИЦИИ

Данное изобретение относится к сыпучей каталитической композиции, включающей в себя частицы оксидов металлов, содержащих один или более металлов VIII группы и два или более металлов VIB группы, причем сыпучая каталитическая композиция включает в себя первые частицы оксидов металлов, содержащие один или более первых металлов VIII группы и один или более первых металлов VIB группы, и отдельно приготовленные вторые частицы оксидов металлов, содержащие один или более вторых металлов VIII группы и один или более вторых металлов VIB группы, где состав металлов VIB группы и VIII группы в первых и вторых частицах оксидов металлов различен, где первые и вторые сыпучие частицы оксидов отдельно сформованы для разделения первых и вторых сформованных частиц сыпучего катализатора, которые объединяют предпочтительно до образования гомогенной смеси, для получения сыпучей каталитической композиции. Данное изобретение также относится к способу получения сыпучей каталитической композиции и гидрообработке ...

НАСЫПНОЙ КАТАЛИЗАТОР ПЕРЕРАБОТКИ, ВКЛЮЧАЮЩИЙ МЕТАЛЛ ГРУППЫ VIII И МЕТАЛЛ ГРУППЫ VIB МОЛИБДЕН

Изобретение относится к насыпному катализатору, включающему по меньшей мере 60 мас.% частиц оксидов металлов, содержащих один или более металлов группы VIII и металл группы VIB молибден, включающему менее чем 10 мол.% второго металла группы VIB (относительно суммарного количества металлов группы VIB) и включающему металл группы V в количестве меньше чем 10 мол.% (относительно суммы металлов группы VIB), где насыпной катализатор был прокален при температуре ниже температуры, при которой гексагональная метастабильная кристаллическая структура превращается в неактивную кристаллическую структуру, предпочтительно ниже 450°C, и где насыпной катализатор имеет метастабильную гексагональную фазу, характеризуемую рентгенограммой, имеющей отражения при 33-35 и 58-61°2θ. Предпочтительно, чтобы главные отражения имели полную ширину на половине максимума (FWHM) менее чем 2,5. Изобретение, кроме того, относится к способу получения насыпного катализатора, к соответствующему сульфидированному насыпному ...

Hydrogenation method of heavy hydrocarbon multi-segment fluidized bed

The invention discloses a hydrogenation method of a heavy hydrocarbon multi-segment fluidized bed. The technical process comprises the steps of: mixing thick heavy hydrocarbon raw materials with gas phase material flow which is discharged from a fluidized bed hydrogenation-desulfuration reactor and a hydrogenation-denitrification reactor to enter into a hydrogenation-demetalization reactor; cooling and purifying reacted gas phase material flow to be taken as recycle hydrogen; mixing the demetallized liquid phase material flow with hydrogen to enter into the fluidized bed hydrogenation-desulfuration reactor; mixing the desulfurated liquid phase material flow with hydrogen to enter into the hydrogenation-desulfuration reactor; and leading the denitrified liquid phase material flow to enter into a separating device. The technology adopts a new reactor assembly mode to machine heavy oil raw materials with high viscosity and bad quality, can provide a new flexible, high-efficiency and energy-saving ...

CATALYST CONTAINING METALS OF GROUP VI AND GROUP VIII PRESENT AT LEAST ENPARTIE IN the FORM Of HETEROPOLYANIONS IN the PRECURSOR OXIDIZES

Process of hydrocraquage and catalysts intended for this process

Treating petroleum charges to form a gas oil cut, comprises mild hydrocracking in a fixed catalyst bed in the presence of hydrogen and hydrotreatment by contacting with a catalyst in the presence of hydrogen and separation

L'invention concerne un procédé de traitement des charges pétrolières lourdes pour produire une coupe gazole ayant une teneur en soufre inférieure à 50 ppm et le plus souvent 10 ppm qui comprend les étapes suivantes : a) hydrocraquage doux en lit fixe de catalyseur, b) séparation du sulfure d'hydrogène, d'une coupe distillat incluant une fraction gazole et d'une fraction plus lourde que le gazole, c) hydrotraitement, par contact avec au moins un catalyseur, d'au moins une partie de ladite coupe distillat obtenue dans l'étape b) incluant la fraction gazole, en mélange avec une charge issue de source renouvelable brute ou raffinée, d) séparation d'une coupe gazole à moins de 50 ppm soufre. Avantageusement la fraction lourde est envoyée en craquage catalytique. De préférence, le procédé opère avec de l'hydrogène d'appoint amené au niveau de l'étape c) et très avantageusement tout l'hydrogène d'appoint du procédé est introduit à l'étape c). L'invention concerne également une installation utilisable ...

HYDROCONVERSION PROCESS USING BULK GROUP VIII/GROUP VIB CATALYSTS

Procédé d'hydroconversion de pétrole et de charges d'alimentation chimiques mettant en oeuvre des catalyseurs en vrac du Groupe VIII et du Groupe VIB. Des catalyseurs préférés incluent ceux contenant Ni-Mo-W.

Hydroconversion process for making lubicating oil basestocks

A process for producing a lubricating oil basestock having at least 90 wt. % saturates and a VI of at least 105 by solvent extracting a feedstock to produce a raffinate, solvent dewaxing the raffinate, selectively hydroconverting the solvent dewaxed raffinate in a two step hydroconversion zone followed by a hydrofinishing zone and a dewaxing zone.

CATALYST FOR HYDROGENATION TREATMENT AND METHOD FOR HYDROGENATION TREATMENT OF HYDROCARBON OIL USING IT

PROBLEM TO BE SOLVED: To provide a catalyst with a high desulfurization activity being useful for deep desulfurization of a hydrocarbon oil and a method for hydrogenation treatment using it. SOLUTION: There is provided a catalyst for hydrogenation treatment which comprises a carrier and at least one kind of catalyst ingredients A selected from the group consisting of the group 6A elements in the periodic table and/or at least one kind of catalyst ingredients B selected from the group consisting of the group 8 elements in the periodic table dispersed in the carrier and wherein content of the elements of the hydrogenation catalyst is 0.02-0.4 mole/mole with respect to the total mole of the elements comprising the catalyst and all the catalyst ingredients whose contents are at least 0.002 mole/mole among the catalyst ingredients satisfy the equation, Nmax-Nmin≤2×[3×(N0)0.5+0.2×N0] (wherein Nmax, Nmin and N0 are respectively the max., the min. and mean values in measured values on concentration ...

ВЫСОКОАКТИВНЫЕ ЧЕТВЕРТИЧНЫЕ МЕТАЛЛИЧЕСКИЕ МАТЕРИАЛЫ, ИСПОЛЬЗУЮЩИЕ СОЕДИНЕНИЯ КОРОТКОЦЕПОЧЕЧНОГО ЧЕТВЕРТИЧНОГО АЛКИЛАММОНИЯ

Изобретение относится к смешанному оксиду переходных металлов и его применению в качестве катализатора или предшественника катализатора, такого как катализатор или предшественник катализатора для конверсии углеводородов или, более конкретно, катализатор или предшественник катализатора гидропереработки. Материал для получения катализатора представляет собой смешанный оксид переходных металлов, имеющий формулу: (MIa)m(MIIb)n(MIIIc)o(MIVd)pOeq, где: MIпредставляет собой металл или смесь металлов, выбранных из группы IB (группа 11 по IUPAC), группы IIB (группа 12 по IUPAC), группы VIIB (группа 7 по IUPAC), группы IIIA (группа 13 по IUPAC), группы IVA (группа 14 по IUPAC) и группы IVB (группа 4 по IUPAC); MIIпредставляет собой металл или смесь металлов, выбранных из группы VIII (группы 8, 9 и 10 по IUPAC); MIIIпредставляет собой металл, выбранный из группы VIB (группа 6 по IUPAC); MIVпредставляет собой металл, выбранный из группы VIB (группа 6 по IUPAC), который отличается от MIII. Обеспечивается ...

Катализатор для гидрокрекинга нефтяного сырья

Способ получения нафталина и поглотительного масла

Катализатор для гидрокрекинга дистиллятного сырья

Способ получения кристаллического нафталина

Добавка для гидроконверсии тяжелого углеводородного масла

Использование: нефтепереработка. Сущность изобретения: добавка представляет собой суспензию в углеводородном масле, содержащую раствор соединения молибдена в кислородсодержащем полярном растворителем и частицы углеродистого материала - углеродной сажи в виде порошка или гранул со средним размером ис- ходных частиц 9-200 нм. В качестве соединения молибдена используют гетеро- полимолибденовую кислоту с гетерополиаНИОНОМ РМ012040. Р2М018062, SIMO12040, GeMoi2040, CeMoi2042, С.оМое024Нб, или смешанную гетерополикислоту с гетеропо- лианионом PMonVO/jo, PMoioW204o, SiMoi2040, PMogWaOio, 51Моэ Л/з040, РМодУз04о, SIMogV3040, или соль гетеропо- ликислоты с переходным металлом, выбранным из группы медь, кобальт, железо, никель, марганец. Суспензия содержит соединение молибдена в количестве 0,058- 97,4 мае.ч. в расчете на молибден, на 100 мае.ч. частиц углеродистого материала. Общее содержание в углеводородном масле 2,17-19,9 мас.%. Добавка может содержать серу 2-6 г-атом на 1 r-атом молибдена. 10 ...

VERFAHREN ZUR ERZEUGUNG VON CRACK-PRODUKTEN MIT NIEDRIGEM SCHWEFEL- UND STICKSTOFFGEHALT

SYNTHETISCHES PORÖSES KRISTALLINES MATERIAL, DESSEN HERSTELLUNG UND VERWENDUNG.

VERFAHREN ZUR HYDROCRACKUNG MIT KATALYSATOREN DER GRUPPEN VIII UND VIB IN SCHÜTTGUTFORM

A process for converting heavy petroleum residues to hydrogen and gaseous distillable hydrocarbons

The invention concerns a process for converting heavy petroleum residues to hydrogen and to gaseous and distillable hydrocarbons, comprising the association of a step of hydropyrolysis (inside tube 3) with a step of catalytic steam-gasification of the formed coke (outside tube 3), characterized in that the hydropyrolysis step is performed in the presence of a solid supporting a carbon gasification catalyst circulating between the hydropyrolysis zone and the coke steam-gasification zone, said steam-gasification being performed in the absence of oxygen. The petroleum residue, hydrogen and steam are introduced respectively through lines 5, 6 and 7. The products are withdrawn through line 10. Heat may be supplied by the radiating tube 4.

PROCEDURE FOR HYDROCRACKUNG WITH CATALYSTS OF THE GROUPS OF VIII AND VIB IN BULK MATERIAL FORM

TWO-STAGE PROCEDURE FOR HYDRODESULFURIERUNG OF DISTILLATEN BY MULTI-METALLIC CATALYSTS IN BULK MATERIAL FORM

PROCEDURE FOR THE HYDRAULIC CONVERSION BY CATALYSTS OF THE GROUPS OF VIII AND VIB IN BULK MATERIAL FORM

USE OF A CATALYST FOR HYDROCRACKEN CONSISTING OF A MIKROPORÍSEN CRYSTALLINE SOLID

ACTIVATED, WITH SILICIC ACID ENRICHED MAZZIT, MANUFACTURING PROCESS AS WELL AS ITS USE

USE A ZEOLITE BETA CONTAINING CATALYST IN HYDROCARBON PROCESSES OF CONVERSION

PROCEDURE FOR THE HYDROGENATION WITH CATALYSTS OF THE GROUPS OF VIII AND VIB IN BULK MATERIAL FORM

A new aluminum trihydroxide phase and catalysts made therefrom

Improved process for preparing alcohols by the oxo process

Slurry hydroprocessing using bulk multimetallic catalysts

LAYERED METAL CHALCOGENIDES CONTAINING INTERLAYER CHALCOGENIDES AND THEIR SYNTHESIS

MOLECULAR SIEVE SSZ-71 COMPOSITION OF MATTER AND SYNTHESIS THEREOF

The present invention relates to new molecular sieve SSZ-71 prepared using a N- benzly-1-4diazabicyclo[2.2.2]octane cation as a structure/directing agent, methods for synthesizing SSZ-71 and processes employing SSZ-71 in a catalyst.

PROCESS FOR MAXIMUM MIDDLE DISTILLATE PRODUCTION WITH MINIMUM HYDROGEN CONSUMPTION

SLURRY HYDROPROCESSING USING BULK MULTIMETALLIC CATALYSTS

A slurry hydroprocessing process for upgrading a hydrocarbon feedstock containing nitrogen and sulfur using bulk multimetallic catalyst comprised of at least one Group VIII non-noble metal and at least two Group VIB metals wherein the ratio of Group VIB metal to Group VIII metal is about 10:1 to about 1:10.

HYDROCONVERSION PROCESS USING BULK GROUP VIII/GROUP VIB CATALYSTS

Hydroconversion processing of petroleum and chemical feedstocks using bulk Group VIII/Group VIB catalysts. Preferred catalysts include those comprised of Ni-Mo-W.

HYDROFINING PROCESS USING BULK GROUP VIII/GROUP VIB CATALYSTS

Hydrofining of petroleum and chemical feedstocks using bulk Group VIII/Group VIB catalysts. Preferred catalysts include those comprised of Ni-Mo-W.

ADDITIVE FOR THE HYDROCONVERSION OF A HEAVY HYDROCARBON OIL

There is provided an additive for the hydroconversion of a heavy hydrocarbon oil, which is obtained by suspending a fine powder of a carbonaceous substance and a solution of a heteropolymolybdic acid and/or transition metal salts thereof in a hydrocarbon oil. By the use of the additive of the present invention, the hydroconversion of a heavy hydrocarbon oil can be effectively performed at high conversion without occurrence of coking.

A MIXED METAL CATALYST COMPOSITION, ITS PREPARATION AND USE

... ▓▓▓The invention pertains to a process for preparing a catalyst composition ▓comprising bulk catalyst particles comprising at least one Group VIII non-▓noble metal and at least two Group VIB metals, which process comprises ▓combining and reacting at least one Group VIII non-noble metal component with ▓at least two Group VIB metal components in the presence of a protic liquid, ▓with at least one of the metal components remaining at least partly in the ▓solid state during the entire process. The invention further relates to a ▓catalyst composition obtainable by said process and to the use thereof in ▓hydroprocessing applications.▓ ...

A PROCESS FOR THE CATALYTIC CONVERSION OF MICRO CARBON RESIDUE CONTENT OF HEAVY HYDROCARBON FEEDSTOCKS AND A LOW SURFACE AREA CATALYST COMPOSITION FOR USE THEREIN

An improved process for the hydroconversion of micro carbon residue content of heavy hydrocarbon feedstocks by the use of a catalyst composition that is especially useful in the conversion of micro carbon residue of such feedstocks. The catalyst composition is a low surface area composition that further has a specifically define pore structure the combination of which provides for its enhance micro carbon residue conversion property.

The method for producing the benzene from the oil or its distillates

PROCEDE ET CATALYSEUR POUR LE TRAITEMENT DE COUPES LOURDES D'HYDROGENATS PROVENANT DE L'HYDROLIQUEFACTION DU CHARBON

L'INVENTION CONCERNE UN PROCEDE ET UN CATALYSEUR DE TRAITEMENT DE COUPES LOURDES D'HYDROGENATS PROVENANT DE L'HYDROLIQUEFACTION DU CHARBON. LES COUPES LOURDES SONT SOUMISES A L'HYDROGENOLYSE A UNE TEMPERATURE COMPRISE ENTRE 600C ET 850C ET SOUS UNE PRESSION D'HYDROGENE COMPRISE ENTRE 10 ET 120 BARS, EN PRESENCE D'AU MOINS UN CATALYSEUR COMPRENANT DE L'OXYDE DE ZIRCONIUM. APPLICATION A LA VALORISATION DU CHARBON.

VERTICAL TYPE RADIAL FLOW REACTOR

A process for treating hydrocarbons comprises (a) introducing a gas stream contg. hydrocarbon in the vertically oriented reaction vessel through the fluid inlet, (b) passing the stream through the passage circulating the inlet, (c) treating the stream by passing the stream through a catalyst bed in a radial flow type, (d) introducing the treated stream into the plenum zone formed between the outside circle screen and the vessel wall, and (e) removing the stream from the fluid inlet to the outlet. Copyright 1997 KIPO ...

HYDROTREATING CATALYST AND PROCESS FOR HYDROTREATING HYDROCARBON OILS USING THE SAME

HYDROCARBON CONVERSION PROCESS AND CATALYST USEFUL THEREIN

Cette invention concerne un procédé de transformation d'hydrocarbures faisant intervenir un catalyseur qui renferme des macrostructures avec réseau tridimensionnel de particules de composé inorganique poreux. Ces particules occupent moins de 75 % du volume total des macrostructures et sont agencées sous forme d'un réseau tridimensionnel composé de pores au diamètre supérieur à environ 20Å. Les macrostructures peuvent s'obtenir de la façon suivante: formation d'un adjuvant contenant un échangeur ionique organique poreux et d'un mélange de synthèse pouvant constituer le matériau inorganique poreux; transformation du mélange de synthèse en matériau inorganique poreux et extraction de l'échangeur ionique organique poreux du matériau inorganique.

Process for using catalyst with rapid formation of iron sulfide in slurry hydrocracking

A process is disclosed for converting heavy hydrocarbon feed into lighter hydrocarbon products. The heavy hydrocarbon feed is slurried with a catalyst comprising iron oxide and alumina to form a heavy hydrocarbon slurry and hydrocracked to produce lighter hydrocarbons. The iron oxide in the catalyst converts to catalytically active iron sulfide in the presence of hydrogen and sulfur.

CRYSTALLINE TRANSITION METAL OXY-HYDROXIDE MOLYBDOTUNGSTATE

A hydroprocessing catalyst has been developed. The catalyst is a unique crystalline transition metal oxy-hydroxide molybdotungstate material. The hydroprocessing using the crystalline ammonia transition metal oxy-hydroxide molybdotungstate material may include hydrodenitrification, hydrodesulfurization, hydrodemetallation, hydrodesilication, hydrodearomatization, hydroisomerization, hydrotreating, hydrofining, and hydrocracking. 2. The crystalline transition metal oxy-hydroxide molybdotungstate material of wherein the crystalline transition metal oxy-hydroxide molybdotungstate material is present in a mixture with at least one binder and wherein the mixture comprises up to 25 wt % binder.3. The crystalline transition metal oxy-hydroxide molybdotungstate material of wherein the binder is selected from the group consisting of silicas claim 2 , aluminas claim 2 , and silica-aluminas.4. The crystalline transition metal oxy-hydroxide molybdotungstate material of wherein the crystalline transition metal oxy-hydroxide molybdotungstate material is sulfided.6. The method of wherein the reacting is conducted at a temperature of from 10° C. to about 200° C. for a period of time from about 30 minutes to 14 days.7. The method of wherein the recovering is by filtration or centrifugation.8. The method of further comprising adding a binder to the recovered crystalline transition metal oxy-hydroxide molybdotungstate material.9. The method of wherein the binder is selected from the group consisting of aluminas claim 8 , silicas claim 8 , and alumina-silicas.10. The method of further comprising sulfiding the recovered crystalline transition metal oxy-hydroxide molybdotungstate material.12. The process of wherein the conversion process is hydroprocessing.13. The process of wherein the conversion process is selected from the group consisting of hydrodenitrification claim 11 , hydrodesulfurization claim 11 , hydrodemetallation claim 11 , hydrodesilication claim 11 , hydrodearomatization ...

Methods for producing crystalline microporous solids with the RTH topology and compositions derived from the same

This disclosure relates to new crystalline microporous solids (including silicate- and aluminosilicate-based solids), the compositions comprising 8 and 10 membered inorganic rings, particularly those having RTH topologies having a range of Si:Al ratios, methods of preparing these and known crystalline microporous solids using certain quaternized imidazolium cation structuring agents.

ПОЛИМЕТАЛЛИЧЕСКИЕ МАТЕРИАЛЫ С ИСПОЛЬЗОВАНИЕМ СОЕДИНЕНИЙ ЧЕТВЕРТИЧНОГО АЛКИЛАММОНИЯ

Разработан высокоактивный триметаллический материал, содержащий смешанный оксид переходных металлов, способ его получения и способ конверсии. Материал может быть сульфидирован с получением сульфидов металлов, которые используют в качестве катализатора в способе конверсии, например в гидропереработке. Гидропереработка может включать в себя гидроденитрификацию, гидродесульфуризацию, гидродеметаллирование, гидродесиликацию, гидродеароматизацию, гидроизомеризацию, гидроочистку, очистку гидрированием и гидрокрекинг. Материал для приготовления катализатора содержит смешанный оксид переходных металлов, имеющий формулу (MIa)m(MIIb)n(MIIIc)oOeq, где MIпредставляет собой металл или смесь металлов, выбранных из группы VIII (группы 8, 9 и 10 по IUPAC); MIIпредставляет собой металл, выбранный из группы VIB (группа 6 по IUPAC); MIIIпредставляет собой металл, выбранный из группы VIB (группа 6 по IUPAC), который отличается от MII; a, b, c и e представляют собой состояние валентности MI, MII, MIIIи O; m ...

Способ гидрокрекинга мазута

FIELD: oil refining. SUBSTANCE: invention relates to hydrocracking of oil fuel in the presence of methane and is intended for obtaining distillate products with a density of 835-850 kg/m 3 . The invention relates to a method for hydrocracking fuel oil, in which fuel oil is heated to 90-110°C, mixed with methane supplied at a pressure of 0.85-1.2 MPa, the resulting mixture of oil fuel with methane is heated to 280-380°C and fed into a hydrocracking reactor for hydrocracking in the presence of a promoted catalyst. EFFECT: simplification of the process of hydrocracking of oil fuel by performing it at reduced temperature and pressure, as well as increasing the efficiency of distillate products. 4 cl РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 760 454 C1 (51) МПК C10G 47/32 (2006.01) C10G 47/04 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК C10G 47/32 (2021.08); C10G 47/04 (2021.08) (21)(22) Заявка: 2021112753, 30.04.2021 (24) Дата начала отсчета срока действия патента: Дата регистрации: 25.11.2021 Адрес для переписки: 119421, Москва, а/я 32, ООО "Интеллектуальный капитал" (56) Список документов, цитированных в отчете о поиске: RU 2169170 C1, 20.06.2001. RU 2626393 C1, 26.07.2017. EA 23427 B1, 30.06.2016. C 1 2 7 6 0 4 5 4 R U плотностью 835-850 кг/м3. Изобретение касается способа гидрокрекинга мазута, в котором подогревают мазут до 90-110°С, смешивают его с метаном, подающимся под давлением 0,85-1,2 МПа, образованную смесь мазута с метаном Стр.: 1 нагревают до 280-380°С и подают в реактор гидрокрекинга для гидрокрекинга в присутствии промотированного катализатора. Технический результат - упрощение процесса гидрокрекинга мазута путем его выполнения при пониженных температуре и давлении, а также повышение эффективности выхода дистиллятных продуктов. 3 з.п. ф-лы. C 1 (54) Способ гидрокрекинга мазута (57) Реферат: Изобретение относится к гидрокрекингу мазута в присутствии метана и предназначено для получения ...

ВЫСОКОАКТИВНЫЙ МАТЕРИАЛ, ПРЕДСТАВЛЯЮЩИЙ СОБОЙ СМЕШАННЫЙ ОКСИД ПЕРЕХОДНЫХ МЕТАЛЛОВ, ВЫСОКОАКТИВНЫЕ ЧЕТВЕРТИЧНЫЕ МЕТАЛЛИЧЕСКИЕ МАТЕРИАЛЫ, ИСПОЛЬЗУЮЩИЕ СОЕДИНЕНИЯ КОРОТКОЦЕПОЧЕЧНОГО ЧЕТВЕРТИЧНОГО АЛКИЛАММОНИЯ

FIELD: catalysts. SUBSTANCE: invention relates to a material for producing a hydrocarbon conversion catalyst containing a mixed oxide of transition metals by the formula: (M I a ) m (M II b ) n (M III c ) o (M IV d ) p C e q H f r N g s O h t X i u S j v , wherein M I constitutes a metal or mixture of metals selected from the group IB (group 11 by IUPAC), group IIB (group 12 by IUPAC), group VIIB (group 7 by IUPAC) and group IVB (group 4 by IUPAC); M II constitutes a metal or mixture of metals selected from the group VIII (groups 8, 9 and 10 by IUPAC); M III constitutes a metal selected from the group VIB (group 6 by IUPAC); M IV constitutes a metal selected from the group VIB (group 6 by IUPAC), different from M III ; X constitutes a halide (group 17 by IUPAC); a, b, c, e, f, g, h, i and j constitute the valent state of M I , M II , M III , M IV , C, H, N, O, X, and S; m, n, o, p, q, r, s, t, u and v constitute the molar ratio of M I , M II , M III , M IV , C, H, N, O, X and S, wherein m/(m + n) > 0 and m/(m + n) ≤ 1, wherein (m + n)/(o + p) is from 1/10 to 10/1, wherein o/p > 0 and 0 ≤ p/o ≤ 100, wherein each of q, r, s, t and u is greater than 0, wherein v is greater than or equal to 0, and a, b, c, d, e, f, g, h, i, j, m, n, o, p, q, r, s, t, u and v satisfy the equation: a × m + b × n + c × o + d × p + e × q + f × r + g × s + h × t + i × u + j × v = 0. The invention also relates to a method for manufacturing a material of a hydrocarbon conversion catalyst and to a method for hydrocarbon conversion. EFFECT: production of a highly active hydrotreatment catalyst. 22 cl, 8 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (51) МПК B01J 23/00 (2006.01) B01J 23/85 (2006.01) B01J 27/047 (2006.01) B01J 27/08 (2006.01) B01J 27/24 (2006.01) B01J 37/04 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА B01J 37/20 (2006.01) ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ C10G 45/08 (2006.01) C10G 47/04 (2006.01) C10G 45/50 (2006.01) (12) (13) 2 757 295 C1 C10G 45/60 (2006.01) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК ...

ВЫСОКОАКТИВНЫЕ ЧЕТВЕРТИЧНЫЕ МЕТАЛЛИЧЕСКИЕ МАТЕРИАЛЫ, ИСПОЛЬЗУЮЩИЕ СОЕДИНЕНИЯ ГАЛОГЕНИДА КОРОТКОЦЕПОЧЕЧНОГО ЧЕТВЕРТИЧНОГО АЛКИЛАММОНИЯ

Разработан высокоактивный триметаллический материал, содержащий смешанный оксид переходных металлов, и способ его получения. Материал может быть подвергнут сульфидированию с получением сульфидов металлов, которые используют в качестве катализатора в способе конверсии, например, в гидропереработке. Гидропереработка может включать в себя гидроденитрификацию, гидродесульфуризацию, гидродеметаллирование, гидродесиликацию, гидродеароматизацию, гидроизомеризацию, гидроочистку, очистку гидрированием и гидрокрекинг. Материал для получения катализатора, содержащий смешанный оксид переходных металлов, имеющий формулу: (MIa)m(MIIb)n(MIIIc)o(MIVd)pOeq, где MIпредставляет собой металл или смесь металлов, выбранных из группы IB (группа 11 по IUPAC), группы IIB (группа 12 по IUPAC), группы VIIB (группа 7 по IUPAC) и группы IVB (группа 4 по IUPAC); MIIпредставляет собой металл или смесь металлов, выбранных из группы VIII (группы 8, 9 и 10 по IUPAC); MIIIпредставляет собой металл, выбранный из группы VIB ...

Способ переработки углеводородного сырья,содержащего серу,золу и асфальтены

Stable olefinic, low sulphur diesel fuel composition

A stable blended diesel fuel comprising an olefinic diesel fuel blending stock. The olefinic diesel fuel blending stock of the invention comprises olefins in an amount of 2 to 80 weight percent, non-olefins in an amount of 20 to 98 weight percent wherein the non-olefins are substantially comprised of paraffins, oxygenates in an amount of at least 0.012 weight percent and sulfur in an amount of less than 1 ppm. To provide acceptable stability, the blended diesel fuel comprising the olefinic diesel fuel blending stock comprises a sulfur-free antioxidant. The blended diesel fuel comprising the olefinic diesel fuel blending stock and sulfur-free antioxidant added has a peroxide content of less than 5 ppm when stored at 60{C for 4 weeks. A processes for making the stable blended diesel fuel and olefinic diesel fuel blending stocks as defined above is disclosed.

HYDROCARBON PROCESS OF CONVERSION AND HERE APPLICABLE CATALYST

Molecular sieve SSZ-70 composition of matter and synthesis thereof

OLIGOMERIZATION OF OLEFINS

A mixed metal catalyst composition, its preparation and use

HYDROCONVERSION PROCESS FOR MAKING LUBRICATING OIL BASESTOCKS

A process for producing a lubricating oil basestock having at least 90 wt % saturates and a VI of at least 105 by solvent extracting a feedstock in unit (20) to produce a raffinate, solvent dewaxing the raffinate, selectively hydroconverting the solvent dewaxed raffinate in a two step hydroconversion zone which comprises a first hydroconversion unit (42) and to a second hydroconversion unit (52) followed by a hydrofinishing zone in hydrofinishing unit (60) and a dewaxing zone in unit (74).

TWO STAGE PROCESS FOR HYDRODESULFURIZING DISTILLATES USING BULK MULTIMETALLIC CATALYST

A two stage hydrodesulfurizing process for producing low sulfur distillates. A distillate boiling range feedstock containing in excess of about 3,000 wppm sulfur is hydrodesulfurized in a first hydrodesulfurizing stage containing one or more reaction zones in the presence of hydrogen and a hydrodesulfurizing catalyst. The liquid product stream thereof is passed to a first separation stage wherein a vapor phase product stream and a liquid product stream are produced. The liquid product stream, which has a substantially lower sulfur and nitrogen content than the original feedstream is passed to a second hydrodesulfurizing stage also containing one or more reaction zones where it is reacted in the presence of hydrogen and a second hydrodesulfurizing catalyst at hydrodesulfurizing conditions. The catalyst in any one or more reaction zones is a bulk multimetallic catalyst comprised of at least one Group VIII non-noble metal and at least two Group VIB metals.

PROCEDE DE CONVERSION DE RESIDUS PETROLIERS LOURDS EN HYDROGENE ET HYDROCARBURES GAZEUX ET DISTILLABLES

La présente invention concerne un procédé intégré de conversion de résidus pétroliers lourds en hydrogène et en hydrocarbures gazeux et distillables, caractérisé en ce qu'il comporte: a) une première étape dans laquelle le résidu pétrolier et de l'hydrogène sont simultanément mis en contact pendant 0,1 à 60 secondes avec un catalyseur supporté renfermant au moins un oxyde ou carbonate de métal alcalin ou alcalino-terreux, provenant de l'étape b), à une température de 530 à 800.degree. C, sous une pression 15 à 100 bars, pour produire des hydrocarbures gazeux et vapeur et du coke qui se dépose sur le catalyseur, et le catalyseur coké est séparé desdits hydrocarbures, b) une deuxième étape dans laquelle le catalyseur coké, séparé des hydrocarbures à l'étape a), est mis en contact avec de la vapeur d'eau, en l'absence substantielle d'oxygène moléculaire, à une température de 600 à 800.degree. C, sous une pression de 15 à 100 bars, pendant un temps suffisant pour gazéifier sous forme d'hydrogène ...

OLIGOMERIZATION OF OLEFINS

OLIGOMERIZATION OF OLEFINS A method for oligomerizing olefins comprises contacting an olefin-containing feed with a catalyst which contains a thermally stable layered chalcogenide having adjacent layers separated by chalcogenide pillars at a temperature of 100-500.degree.C and a pressure of 10-20000 kPa.

LAYERED METAL CHALCOGENIDES CONTAINING INTERLAYER CHALCOGENIDES AND THEIR SYNTHESIS

LAYERED METAL CHALCOGENIDES CONTAINING INTERLAYER CHALCOGENIDES AND THEIR SYNTHESIS A layered product comprises a layered chalcogenide of at least one element having an atomic number of 4, 5, 12 to 15, 20 to 33, 38 to 51, 56 to 83 and greater than 90, inclusive, and pillars of a chalcogenide of at least one element selected from Group IB, IIB, IIIA, IIIB, IVA, IVB, VA, VB, VIA, VIIA, VIIIA, of the Periodic Table of the Elements separating the chalcogenide layers, at least one of the chalcogens of the layered chalcogenide and said pillars being other than oxygen.

PROCESS FOR MAXIMUM MIDDLE DISTILLATE PRODUCTION WITH MINIMUM HYDROGEN CONSUMPTION

... "PROCESS FOR MAXIMUM MIDDLE DISTILLATE PRODUCTION WITH MINIMUM HYDROGEN CONSUMPTION" A process for the conversion of an aromatic-rich, distillable gas oil charge stock to selectively produce large quantities of high quality middle distillate while minimizing hydrogen consumption which process comprises the steps of reacting the charge stock with hydrogen, in a catalytic hydrocracking reaction zone, at hydrocracking conditions including a maximum catalyst bed temperature in the range of 315 to 454oC selected to convert at least a portion of the charge stock to middle distillate and to convert at least about 10 volume percent of the aromatic hydrocarbon compounds contained in the charge stock to paraffin hydrocarbons; separating a hydrocracking zone effluent to provide a middle distillate product stream and a paraffin-rich hydrocarbonaceous stream boiling at a temperature greater than 371oC; recovering the middle distillate product stream; reacting the paraffinrich hydrocarbonaceous stream ...

A BULK CATALYST COMPOSITION AND A PROCESS PREPARING THE BULKCATALYST COMPOSITION

The invention relates to a bulk catalyst composition comprising metal oxidic particles comprising one or more Group VIII metals and two or more Group VIB metals, which bulk catalyst composition comprises first metal oxidic particles comprising one or more first Group VIII metals and one or more first Group VIB metals and separately prepared second metal oxidic particles comprising one or more second Group VIII metals and one or more second Group VIB metals, wherein the composition of Group VIB and Group VIII metals in the first and second metal oxidic particles are different, wherein the first and second oxidic bulk particles-are separately shaped to separate first and second shaped bulk catalyst particles, which are combined, preferably into a homogeneous blend, to form the bulk catalyst composition. The invention further relates to a process for the preparation of the bulk catalyst composition and to hydroprocessing a hydrocarbon feed using the bulk catalyst composition.

LOW PRESSURE PROCESS FOR THE HYDROCONVERSION OF HEAVY HYDROCARBONS

This invention relates to a process of catalytic hydroconversion of a heavy hydrocarbon oil containing a substantial portion of components having an atmospheric boiling point above 565 .degree.C to give a product hydrocarbon oil containing components having a boiling point below about 565 .degree.C. The process includes steps of mixing a heav y hydrocarbon oil with an oil soluble molybdenum compound, introducing the resulting mixture into a hydroconversion zone, introducing a reactor feed gas into the hydroconversion zone, and recovering the product hydrocarbon oil from the hydroconversion zone.

NICKEL MOLYBDOTUNGSTATE HYDROTREATING CATALYSTS

A hydrodenitrogenation catalyst is prepared by decomposing a nickel (ammoniu m) molybdotungstate precursor and sulfiding, either pre-use or in situ, the decomposition product.

HIGHLY ACTIVE MIXED TRANSITION METAL OXIDE MATERIAL

ВЫСОКОАКТИВНЫЕ ТРИМЕТАЛЛИЧЕСКИЕ МАТЕРИАЛЫ, ИСПОЛЬЗУЮЩИЕ СОЕДИНЕНИЯ КОРОТКОЦЕПОЧЕЧНОГО ЧЕТВЕРТИЧНОГО АЛКИЛАММОНИЯ

FIELD: chemistry. SUBSTANCE: developed is a highly active trimetallic material containing mixed transition metal oxide and a method for production thereof. The material can be subjected to sulphidation producing metal sulphides used as a catalyst in a method for conversion, e.g., in hydrotreatment. Hydrotreatment can include hydrodenitrification, hydrodesulphurisation, hydrodemetallisation, hydrodesilication, hydrodearomatisation, hydroisomerisation, hydrorefining, hydrogenation purification, and hydrocracking. The material for preparing the catalyst comprises a mixed transition metal oxide with the formula: (M I a ) m (M II b ) n (M III c ) o O e q , wherein M I constitutes a metal or a mixture of metals selected from group VIII (group 8, 9 and 10 according to IUPAC); M II constitutes a metal selected from group VIB (group 6 according to IUPAC); M III constitutes a metal selected from group VIB (group 6 according to IUPAC), different from M II ; a, b, c, and e constitute the valence state of M I , M II , M III and O; m, n, o, and q constitute the molar ratio of M I , M II , M III , and O, wherein m/(n + o) equals 1/10 to 10/1, wherein n/o > 0 and 0 ≤ o/n ≤ 100, wherein q is greater than 0; and wherein a, b, c, e, m, n, o, and q satisfy the equation: a × m + b × n + c × o + e × q = 0, wherein the mixed transition metal oxide is characterised by an X-ray diffraction pattern containing the peaks visualised in Table A: Table A, 2θ (°) - d (Å) - 100 (I/I o ); 8 to 14 - 6.320 to 11.043 - very weak; 34.5 to 36.5 - 2.460 to 2.598 - very strong; 53 to 55 - 1.668 to 1.726 - strong to very strong; 55 to 58 - 1.589 to 1.668 - weak to average; 58.5 to 62.5 - 1.485 to 1.576 - very weak; 62.8 to 63.8 - 1.458 to 1.478 - average; wherein the peak between the values of 2 θ(°) at 55 to 58 has a full width at the level of half of the maximum of more than 3°. EFFECT: high activity of the hydrotreatment catalyst. 23 cl, 2 dwg, 1 tbl, 4 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (51) МПК ...

СПОСОБ ПОЛУЧЕНИЯ ЖИДКИХ НЕФТЕПРОДУКТОВ ГИДРОГЕНИЗАЦИЕЙ И ДЕМЕТАЛЛИЗАЦИЕЙ ТЯЖЕЛОГО НЕФТЯНОГО СЫРЬЯ

Способ получения жидких продуктов путем гидрогенизации тяжелого нефтяного и углеводородного сырья и т. п. , в присутствии водорода и катализатора на основе фосфатов поливалентных металлов, отличающийся тем, что в качестве катализатора используют полифосфат железа геле- или ксерогельной структуры в количестве 4-6 мас. % на сырье; катализатор содержит 92-97 мас. % полифосфата железа при соотношении Р2О5: Fе2О3= 0,5-1,5, переходные металлы V-VIII подгрупп 0-4 мас. %, в количестве от 0,001 до 1,0 мас. % каждого, остальное вода и примеси оксидов Са, Si, Na, Mg; процесс проводят при температуре 380-450oС; давление водорода РН2= 2-6 Мпа, в течении 0,5-2,0 ч. 2. Способ по п. 1 отличается тем, что процесс проводят непрерывно в присутствии катализатора и 1,0-3,0 мас. % поверхностно-активного вещества, вводимых в сырье диспергированием.

СПОСОБ И СИСТЕМА ГИДРОКРЕКИНГА

СПОСОБ ПОЛУЧЕНИЯ МАЛОСЕРНИСТЫХ НЕФТЯНЫХ ФРАКЦИЙ

... 1. Способ получения малосернистых нефтяных фракций путем их обработки в среде водорода при повышенных давлении и температуре с использованием каталитических систем, состоящих из катализаторов, обладающих функциями изменения углеводородного состава и очистки от элементоорганических соединений, отличающийся тем, что процесс осуществляется на каталитической системе, состоящей из двух и более катализаторов, при температуре не менее 300° С, давлении не менее 3,0 МПа, при соотношении водород: сырье (А, нм3/м3), которое вычисляется по формуле А=В+С+D, где В - соотношение водород: сырье для осуществления реакций гидрогенолиза элементоорганических соединений, нм3/м3; С - соотношение водород: сырье для осуществления реакций гидрирования непредельных соединений, нм3/м3; D - соотношение водород: сырье для осуществления реакций превращения высококипящих углеводородов, нм3/м3. 2. Способ по п.1, отличающийся тем, что соотношение водород: сырье для осуществления реакций гидрогенолиза элементоорганических ...

СПОСОБ ПОЛУЧЕНИЯ ТОПЛИВНЫХ ДИСТИЛЛЯТОВ, УСТАНОВКА (ВАРИАНТЫ) И КОМПЛЕКС ДЛЯ ЕГО ОСУЩЕСТВЛЕНИЯ

... 1. Способ получения топливных дистиллятов термическим гидрокрекингом смеси, содержащей нефтяное сырье и катализатор, при повышенных температуре и давлении в присутствии водородсодержащего сырья с последующим выделением целевых продуктов, отличающийся тем, что в качестве катализатора используют природные породы (шунгит, серпентинит) в виде частиц дисперсностью 2 мм в количестве 2-40% от массы нефтяного сырья и поверхностно-активное вещество, а процесс термического гидрокрекинга осуществляют под действием электрического и/или магнитного поля при непрерывной механоактивации смеси со скоростью 0,1- 100, 0 м/с при пульсирующих с частотой пульсации 0,01-100,0 Гц, температуре в пределах 100-480oС и давлении в пределах 0,1-40,0 МПа. 2. Установка для получения топливных дистиллятов (вариант 1), содержащая корпус, состоящий из трех жестко соединенных частей: верхней - с входным отверстием, средней - набранной из n кольцевых пластин, установленных радиально и образующих после установки радиальные ...

Siliciumdioxid enthaltenden Bayerit oder Eta-Aluminiumoxid und Crackkatalysatoren

VERFAHREN ZUR HYDROKATALYTISCHEN VERARBEITUNG SCHWERER MINERALOELPRODUKTE

Hydroconversion multi-metallic catalyst and method for making thereof

In a process for forming a bulk hydroprocessing catalyst by sulfiding a catalyst precursor made in a co-precipitation reaction, up to 60% of the metal precursor feeds do not react to form catalyst precursor and end up in the supernatant. In the present disclosure, the metals can be recovered via any of chemical precipitation, ion exchange, electro-coagulation, and combinations thereof to generate an effluent stream containing less than 50 mole % of metal ions in at least one of the metal residuals, and for at least one of the metal residuals is recovered as a metal precursor feed, which can be recycled for use in the co-precipitation reaction. An effluent stream from the process to waste treatment contains less than 50 ppm metal ions.

HIGH SURFACE AREA COMPOSITION FOR USE IN THE CATALYTIC HYDROCONVERSION OF A HEAVY HYDROCARBON FEEDSTOCK, A METHOD MAKING SUCH COMPOSITION AND ITS USE

A catalyst composition that is especially useful in the hydroconversion of pitch, micro carbon residue and sulfur contents of a heavy hydrocarbon feedstock without the excessive formation of sediment. The catalyst composition is a reasonably high surface area composition containing alumina and a low molybdenum content with a high ratio of nickel-to-molybdenum. The catalyst composition further has a unique pore distribution that in combination with the special metals loading provide for good conversion of pitch and micro carbon residue without an excessive yield of sediment. 1. A catalyst composition comprising a molybdenum component in an amount of greater than or equal to 5 wt. % and less than 11 wt. % , with the wt. % being based on the total weight of said catalyst composition and assuming said molybdenum component is in the oxide form (MoO) regardless of its actual form , and a nickel component present in an amount such that said catalyst composition has a weight ratio of said nickel component-to-said molybdenum component exceeding 0.25 , with said weight ratio being computed assuming said nickel component and said molybdenum component are each in the oxide form regardless of their actual forms , and wherein said catalyst composition has a total surface area in the range of from 240 m/g to 360 m/g , a total pore volume in the range of from 0.65 cc/g to 1.1 cc/g and a pore size distribution such that from 11% to 30.5% of the total pore volume is present in macropores of diameter greater than or equal to 250 Å.2. A catalyst composition as recited in claim 1 , having a pore size distribution such that from 50% to 80% of the total pore volume of said catalyst composition is present as pores having diameters in the range of from 55 Å to 115 Å claim 1 , and from 16% to 30% of the total pore volume of said catalyst composition is present in macropores of diameter greater than 500 Å.3. A catalyst composition as recited in claim 2 , wherein more than 20% of the total ...

METHOD FOR PREPARING HYDROREFINING CATALYST

A method for preparing hydrorefining catalyst comprises the following steps: (1) mixing an aqueous ammonia solution with a polyamine complexing agent to form a mixed solvent; (2) adding a cobalt salt to the mixed solvent, dissolving the cobalt salt, and then adding a molybdenum salt and optional salts of other active components, and dissolving them to prepare an impregnating solution; and (3) impregnating a support with the impregnating solution, followed by aging, drying, and activating the impregnated support to form a hydrorefining catalyst. The hydrorefining catalyst prepared by this method has good activity, selectivity and stability in use. 1. A method for preparing hydrorefining catalyst , comprising:supporting active components on a support, the active components comprising cobalt and molybdenum, wherein mixing an aqueous ammonia with a polyamine complexing agent to form a mixed solvent;adding a salt comprising the active component cobalt to the mixed solvent, dissolving the cobalt salt, and then adding a molybdenum salt or a molybdenum salt and salts of other active components and promoters, and dissolving them to prepare an impregnation solution; andimpregnating a support with the impregnating solution, followed by aging, drying and activating the impregnated support to obtain the hydrorefining catalyst.2. The method for preparing hydrorefining catalyst according to claim 1 , wherein a nickel salt claim 1 , a tungsten salt and/or a soluble alkali or carbonate compound of a Group IA element is added during formulation of the impregnation solution.3. The method for preparing hydrorefining catalyst according to claim 1 , wherein the impregnation solution has a pH value of above 10 claim 1 ,4. The method for preparing hydrorefining catalyst according to claim 1 , wherein the polyamine complexing agent is one or more of EDTA claim 1 , triethylene tetramine claim 1 , triethanolamine and ethylenediamine.5. The method for preparing hydrorefining catalyst according ...

BULK CATALYST COMPOSITION COMPRISING BULK METAL OXIDE PARTICLES

The invention relates to a process for preparing bulk metal oxide particles comprising the steps of combining in a reaction mixture (i) dispersible nanoparticles having a dimension of less than about 1 μm upon being dispersed in a liquid, (ii) at least one Group VIII non-noble metal compound, (iii) at least one Group VIB metal compound, and (iv) a protic liquid; and reacting the at least one Group VIII non-noble metal compound and the at least one Group VIB metal in the presence of the nanoparticles. It also relates to bulk metal hydroprocessing catalysts obtainable by such method. 1. A process for preparing bulk metal oxide particles comprising the steps of combining in a reaction mixture (i) dispersible nanoparticles having a dimension of less than about 1 μm upon being dispersed in a liquid , (ii) at least one Group VIII non-noble metal compound , (iii) at least one Group VIB metal compound , and (iv) a protic liquid; and reacting the at least one Group VIII non-noble metal compound and the at least one Group VIB metal in the presence of the nanoparticles , wherein said nanoparticles are different in composition from said at least one Group VIII non-noble metal compound and said at least one Group VIB metal compound.2. The process according to claim 1 , wherein the nanoparticles are clay mineral particles.3. The process according to or claim 1 , wherein at least one Group VIII non-noble metal compound and at least two Group VIB metal compounds are combined in the reaction mixture.4. The process according to any one of or claim 1 , wherein the reaction mixture further comprises a Group V metal compound.5. The process according to any one of or claim 1 , wherein the metal compounds are at least partly in the solid state during the process.6. The process according to any one of or claim 1 , wherein the nanoparticles are added to the reaction mixture after the metal compounds.8. The process according to claim 7 , wherein the at least one Group VIII non-noble metal ...

PROCESSING OF HEAVY HYDROCARBON FEEDS

Systems and methods are provided for hydroconversion of a heavy oil feed under slurry hydroprocessing conditions and/or solvent assisted hydroprocessing conditions. The systems and methods for slurry hydroconversion can include the use of a configuration that can allow for improved separation of catalyst particles from the slurry hydroprocessing effluent. In addition to allowing for improved catalyst recycle, an amount of fines in the slurry hydroconversion effluent can be reduced or minimized. This can facilitate further processing or handling of any “pitch” generated during the slurry hydroconversion. The systems and methods for solvent assisted hydroprocessing can include processing of a heavy oil feed in conjunction with a high solvency dispersive power crude. 1. A process for producing a hydroprocessed product , comprising:exposing a feedstock to a catalyst under effective slurry hydroconversion conditions to form a slurry hydroprocessing effluent, the effective slurry hydroconversion conditions being effective for conversion of at least about 90 wt % of the feedstock relative to a conversion temperature, the catalyst comprising catalyst particles having a particle size of at least about 2 μm; andseparating at least about 95 wt % of the catalyst particles having a particle size of at least about 2 μm from the slurry hydroprocessing effluent using a catalyst recovery system comprising one or more drum separators and a cross-flow filter.2. The process of claim 1 , wherein the feedstock has a T95 distillation point of about 600° C. or less.3. The process of claim 1 , wherein the feedstock has a 10% distillation point of at least about 900° F. (˜482° C.) claim 1 , a Conradson carbon residue of at least about 27.5 wt % claim 1 , or a combination thereof.4. The process of claim 1 , wherein the one or more drum separators comprise cyclone separators.5. The process of claim 1 , further comprising exposing the feedstock to a demetallization catalyst under slurry ...

Feed Flexible Hydrocracking Operations

A hydrocracking process for converting a petroleum feed to lower boiling products. The process comprises hydrotreating a petroleum feed in a pre-treating zone in the presence of hydrogen to produce a hydrotreated effluent stream comprising a liquid product. At least a portion of the hydrotreated effluent stream is then passed to an MMS catalyst zone, and then to a hydrocracking zone. In one embodiment, the MMS catalyst zone comprises a self-supported multi-metallic catalyst prepared from a precursor in the oxide or hydroxide form. The percentage work of the hydrotreating in the pre-treating zone is maintained at a level of at least 56%. 1. A hydrocracking process for converting a petroleum feed to lower boiling products ,which process comprises:(i) hydrotreating a petroleum feed in the presence of hydrogen in a pre-treating zone to produce a hydrotreated effluent stream comprising a liquid product;(ii) passing the hydrotreated effluent stream to an MMS catalyst zone comprising an MMS catalyst for reaction to create a resulting effluent; and(iii) passing at least a portion of the resulting effluent from (ii) to a hydrocracking zone having a reaction zone to produce a hydrocracked effluent stream;with a work percentage for the pre-treating zone (i) maintained at a level of at least 56%.2. The process of claim 1 , wherein the MMS catalyst in the MMS catalyst zone in (ii) comprises a self-supported multi-metallic catalyst prepared from a precursor in the oxide or hydroxide form.3. The process of claim 2 , wherein the MMS catalyst in the MMS catalyst zone comprises a self-supported multi-metallic catalyst prepared from a precursor in the hydroxide form.4. The process of claim 2 , wherein the hydrocracked effluent is passed to a distillation column.5. The process of claim 2 , wherein the hydrocracking zone comprises up to three reaction zones.6. The process of claim 5 , wherein effluent from a bottom reaction zone is passed to a distillation column.7. The process of claim ...

CATALYSTS POSSESSING AN IMPROVED RESISTANCE TO POISONING

The present invention relates generally to the field of catalysts for use in connection with one or more types of emissions control (e.g., emissions control associated with the combustion of one or more types of fossil fuel) and, in particular to catalyst compositions that possess an improved resistance to at least one type of poisoning. In another embodiment, the catalysts of the present invention are designed to be utilized in conjunction with an SCR and possess an improved resistance to phosphorus poisoning. 1. A poison-resistant SCR catalyst composition comprising:(i) at least one vanadium compound or metal;(ii) at least one tungsten compound or metal;(iii) at least one titanium compound or metal; and(iv) at least one additional compound selected from one or more molybdenum compounds or metal,{'sub': 2', '3, 'wherein poison-resistance in the SCR catalyst is achieved due to the molar ratio of the metal portion of component (iv) to the metal portion of component (i) falling in the range of about 10:1 to about 1:1 and wherein the catalyst composition has an SOto SOconversion, or oxidation, rate that is about 2 percent or less.'}2. The catalyst composition of claim 1 , wherein the molar ratio of the metal portion of component (iv) to the metal portion of component (i) is in the range of about 9:1 to about 1:1.3. The catalyst composition of claim 1 , wherein the molar ratio of the metal portion of component (iv) to the metal portion of component (i) is in the range of about 8:1 to about 1:1.4. The catalyst composition of claim 1 , wherein the molar ratio of the metal portion of component (iv) to the metal portion of component (i) is in the range of about 7:1 to about 1:1.5. The catalyst composition of claim 1 , wherein the molar ratio of the metal portion of component (iv) to the metal portion of component (i) is in the range of about 4:1 to about 1:1.6. The catalyst composition of claim 1 , wherein the molar ratio of the metal portion of component (iv) to the metal ...

PROCESS FOR THE CATALYTIC CONVERSION OF MICRO CARBON RESIDUE CONTENT OF HEAVY HYDROCARBON FEEDSTOCKS AND A LOW SURFACE AREA CATALYST COMPOSITION FOR USE THEREIN

An improved process for the hydroconversion of micro carbon residue content of heavy hydrocarbon feedstocks by the use of a catalyst composition that is especially useful in the conversion of micro carbon residue of such feedstocks. The catalyst composition is a low surface area composition that further has a specifically define pore structure the combination of which provides for its enhance micro carbon residue conversion property. 1. A process for converting at least a portion of an MCR content of a heavy hydrocarbon feedstock to yield a product having a reduced MCR content , wherein said process includes contacting said heavy hydrocarbon feedstock with a catalyst under MCR conversion process conditions and yielding said product , wherein the improvement comprises: enhancing the conversion of said MCR content of said heavy hydrocarbon feedstock by using as said catalyst in said process a calcined particulate of a co-mulled mixture , wherein said co-mulled mixture that is formed into a particulate , which is subsequently calcined to provide said calcined particulate , comprises a molybdenum component , a nickel component , an uncalcined pseudo-boehmite powder prepared by a two-step precipitation process and comprising at least 90 weight percent pseudo-boehmite , a mineral acid , and a catalyst fines portion having a particle size between 5 and 50 microns (μm) and a mean pore diameter between 40 Å and 150 Å , and wherein said calcined particulate is prepared under conditions so that it has specifically defined physical properties including:{'sup': 2', '2, '(a) a total surface area of greater than 160 m/g and less than 240 m/g;'}(b) a median pore diameter in the range of from 85 Å to 120 Å;(c) from 8% to 22% of the total pore volume of said calcined particulate in the macropores having a pore diameter of 250 Å or greater; and(d) greater than 40% and no more than 60% of the total pore volume of said calcined particulate within its pores having a diameter in the range ...

PROCESS FOR SLURRY HYDROCRACKING USING CATALYST WITH LOW DIASPORE ALUMINA

A process is disclosed for using an iron oxide and alumina catalyst with no more than more than about 55 wt % of the alumina in the diaspore phase or in the alpha phase in SHC. Alpha alumina is less effective catalyst component for slurry hydrocracking in terms of TIOR conversion. Drying procedures should avoid more than about 51 wt % of the alumina change to the alpha phase. The SHC catalyst is for converting heavy hydrocarbon feed into lighter hydrocarbon products. 1. A process for converting heavy hydrocarbon feed into lighter hydrocarbon products comprising:providing catalyst particles comprising iron oxide and alumina, said alumina comprising no more than about 55 wt % diaspore and said alumina comprising less than about 15 wt % water;mixing said heavy hydrocarbon liquid feed with hydrogen and said catalyst particles to form a heavy hydrocarbon slurry comprising hydrocarbon liquid and catalyst particles;hydrocracking hydrocarbons in said heavy hydrocarbon slurry in the presence of said hydrogen and said catalyst particles in a hydrocracking reactor to produce a hydrocracked slurry product comprising lighter hydrocarbon products; andwithdrawing said hydrocracked slurry product from said hydrocracking reactor.2. The process of further comprising heat treating said catalyst particles prior to mixing with said heavy hydrocarbon liquid.3. The process of further wherein said alumina in said catalyst particle comprises less than about 10 wt % water.4. The process of further comprising heat treating said catalyst particles at a temperature between about 150 and about 800° C.5. The process of wherein said alumina in said catalyst particles comprise at least about 40 wt % of gibbsite alumina and/or boehmite alumina.6. The process of further comprising heat treating said catalyst particles at a temperature between about 150 and about 600° C.7. The process of wherein said alumina in said catalyst particles comprise at least about 0.5 wt % diaspore alumina.8. A process for ...

MULTI-METALLIC BULK HYDROPROCESSING CATALYSTS

Multi-metallic bulk catalysts and methods for synthesizing the same are provided. The multi-metallic bulk catalysts contain nickel, molybdenum tungsten, copper, and optionally, titanium and/or niobium. The catalysts are useful for hydroprocessing, particularly hydrodesulfurization and hydrodenitrogenation, of hydrocarbon feedstocks. 1. A bulk catalyst precursor comprising:(a) 1 to 60 wt. % of Ni, on a metal oxide basis;(b) 1 to 40 wt. % of Mo, on a metal oxide basis;(c) 5 to 80 wt. % of W, on a metal oxide basis;(d) 0.01 to 20 wt. % of Cu, on a metal oxide basis;(e) 0 to 45 wt. % of Ti, on a metal oxide basis; and(f) 0 to 20 wt. % of Nb, on a metal oxide basis.2. The bulk catalyst precursor of claim 1 , further comprising an organic compound-based component.3. The bulk catalyst precursor of claim 2 , wherein the organic compound-based component is selected from the group of an organic acid or salt thereof claim 2 , a sugar claim 2 , a sugar alcohol claim 2 , or a combination thereof.4. The bulk catalyst precursor of claim 2 , wherein the organic compound-based component is selected from the group of glyoxylic acid claim 2 , pyruvic acid claim 2 , lactic acid claim 2 , malonic acid claim 2 , oxaloacetic acid claim 2 , malic acid claim 2 , fumaric acid claim 2 , maleic acid claim 2 , tartaric acid claim 2 , gluconic acid claim 2 , citric acid claim 2 , oxamic acid claim 2 , serine claim 2 , aspartic acid claim 2 , glutamic acid claim 2 , iminodiacetic acid claim 2 , ethylenediaminetetraacetic acid claim 2 , fructose claim 2 , glucose claim 2 , galactose claim 2 , mannose claim 2 , sucrose claim 2 , lactose claim 2 , maltose claim 2 , erythritol claim 2 , xylitol claim 2 , mannitol claim 2 , sorbitol claim 2 , or a combination thereof.5. The bulk catalyst precursor of claim 2 , wherein a molar ratio of Ni to the organic compound-based component is in a range of 3:1 to 20:1.6. The bulk catalyst precursor of claim 1 , wherein a molar ratio of Cu/(Ni+Mo+W+Ti+Nb) is in a ...

HIGHLY-DISPERSED HYDROGENATION CATALYST, PREPARATION METHOD THEREOF, AND USE THEREOF IN PREPARATION OF BIOFUEL FROM PALM OIL OR OTHER OIL

A highly-dispersed hydrogenation catalyst, a preparation method thereof, and use thereof in the preparation of biofuel from palm oil or other oil are provided. The combination of maleic anhydride-grafted polypropylene (MA-PP) and a silane coupling agent (SCA) is introduced into an aluminum oxide composite carrier through organic amidation to obtain a uniformly-dispersed composite carrier with regular pores. Moreover, through a multi-stage impregnation and roasting process, a particle size of an active component is greatly reduced, and the dispersion of the active component and the number of active sites are improved. A hydrogenation catalyst with high hydrothermal stability, high hydrogenation activity, and long life is prepared based on the composite carrier with regular pores and used in the preparation of biofuel from vegetable oil or other oil through hydrodeoxygenation (HDO), which has great industrial application value. 1. An aluminum oxide composite carrier , wherein maleic anhydride-grafted polypropylene (MA-PP) and a silane coupling agent (SCA) undergo amidation to obtain a reaction product , then γ-AlOand tetrabutyl titanate (TBT) are added into the reaction product to obtain a solid material , and the solid material is dried and roasted to form the aluminum oxide composite carrier , wherein the aluminum oxide composite carrier is an aluminum oxide-titanium dioxide carrier.2. An aluminum oxide composite carrier , wherein MA-PP and an SCA undergo amidation to obtain a reaction product , then γ-AlOand tetrabutyl zirconate (TBZ) are added into the reaction product to obtain a solid material , and the solid material is dried and roasted to form the aluminum oxide composite carrier , wherein the aluminum oxide composite carrier is an aluminum oxide-zirconium dioxide carrier.3. The aluminum oxide composite carrier according to claim 1 , wherein a mass percentage of the titanium dioxide in the aluminum oxide composite carrier is 5% to 20%.4. The aluminum oxide ...

PROCEDURE TO PREPARE A SUPPORTED TRIMETALLIC CATALYST FOR PRODUCTION OF ULTRA LOW SULFUR DIESEL AND ITS APPLICATION

According to this invention, a Ni—Mo—W trimetallic catalyst supported on porous alumina is obtained that shows very high activity for hydrotreating (HDT) of gasoils, particularly deep hydrodesulfurization (HDS) and hydrodesnitrogenation (HDN) of straight run gasoil in conditions of moderate pressure. 1. A procedure to obtain a supported trimetallic catalytic formulation for the deep hydrodesulfurization of straight run gasoil and for the production of ultra low sulfur diesel (ULSD) , comprising the following steps:a) preparation of solution containing tungsten (solution a), b) preparation of solution containing molybdenum, nickel and phosphorus (solution b), c) preparation of solution containing nickel and EDTA (solution c), d) preparation of solution containing nickel, molybdenum and EDTA (solution d) and e) mixture of solutions (c) and (d); e) drying the catalytic support at a temperature of 100 to 120° C., for 3 to 6 hours, f) impregnation of the solution (a), ageing of the material for 10 to 15 hours, drying at a temperature of 100 to 120° C. for 3 to 5 hours, g) impregnation of the solution (b), ageing of the material for 8 to 10 hours, drying at a temperature of 100 to 120° C. for 4 to 6 hours, h) impregnation of the mixture of the solutions c+d, ageing of the material during 30-40 minutes, no longer aging time is allowed, and drying at a temperature of 60 to 200° C., for 4 to 15 hours, i) wetting of the catalyst with SRGO, j) sulfiding the impregnated catalyst.2. A procedure according to claim 1 , wherein the following solutions are prepared;a) aqueous solution containing a metal of group VIB as tungsten, from ammonium metatungstate in water, until obtaining a completely transparent and crystalline solution;b) acid solution containing a metal of group VIB, such as Mo and a metal of group VIIIB as Ni, dissolved in a phosphoric acid solution;c) solution containing a metal of group VIIIB as Ni, and an organic compound such as ethylenediaminetetraacetic acid ( ...

NOVEL MIXED METAL OXIDES

A unique mixed metal molybdotungstate material has been developed. The material may be used as a hydroprocessing catalyst. The hydroprocessing may include hydrodenitrification, hydrodesulfurization, hydrodemetallation, hydrodearomatization, hydrodesilication, hydroisomerization, hydrotreating, hydrofining, and hydrocracking. 2. The mixed metal oxide material of wherein the mixed metal oxide is present in a mixture with at least one binder and wherein the mixture comprises up to 25 wt % binder.3. The mixed metal oxide material of wherein the binder is selected from the group consisting of silicas claim 2 , aluminas claim 2 , and silica-aluminas.4. The mixed metal oxide material of wherein M is nickel or cobalt.5. The mixed metal oxide material of wherein M is nickel.6. The mixed metal oxide material of wherein the mixed metal oxide is sulfided.8. The method of wherein the recovering is by filtration or centrifugation.9. The method of further comprising adding a binder to the recovered bis-ammonia transition metal molybdotungstate precursor material or to the recovered mixed metal oxide or both.10. The method of wherein the binder is selected from the group consisting of aluminas claim 9 , silicas claim 9 , and alumina-silicas.11. The method of further comprising sulfiding the recovered bis-ammonia transition metal molybdotungstate precursor material or the recovered mixed metal oxide or both.13. The process of wherein the conversion process is hydroprocessing.14. The process of wherein the hydroprocessing process is selected from the group consisting of hydrodenitrification claim 13 , hydrodesulfurization claim 13 , hydrodemetallation claim 13 , hydrodearomatization claim 13 , hydroisomerization claim 13 , hydrotreating claim 13 , hydrofining claim 13 , and hydrocracking.15. The process of wherein the mixed metal oxide is present in a mixture with at least one binder and wherein the mixture comprises up to 25 wt % binder.16. The process of wherein the binder is ...

CRYSTALLINE AMMONIA TRANSITION METAL MOLYBDATE

A hydroprocessing catalyst has been developed. The catalyst is a unique crystalline ammonia transition metal molybdate material. The hydroprocessing using the crystalline ammonia transition metal molybdate material may include hydrodenitrification, hydrodesulfurization, hydrodemetallation, hydrodesilication, hydrodearomatization, hydroisomerization, hydrotreating, hydrofining, and hydrocracking. 2. The crystalline ammonia transition metal molybdate material of wherein the crystalline ammonia transition metal molybdate material is present in a mixture with at least one binder and wherein the mixture comprises up to 25 wt % binder.3. The crystalline ammonia transition metal molybdate material of wherein the binder is selected from the group consisting of silicas claim 2 , aluminas claim 2 , and silica-aluminas.4. The crystalline ammonia transition metal molybdate material of wherein M is nickel or cobalt.5. The crystalline ammonia transition metal molybdate material of wherein M is nickel.6. The crystalline ammonia transition metal molybdate material of wherein the crystalline ammonia transition metal molybdate material is sulfided.8. The method of wherein the recovering is by filtration claim 7 , centrifugation or evaporation of solvent.9. The method of further comprising adding a binder to the recovered crystalline ammonia transition metal molybdate material.10. The method of wherein the binder is selected from the group consisting of aluminas claim 9 , silicas claim 9 , and alumina-silicas.11. The method of further comprising sulfiding the recovered crystalline ammonia transition metal molybdate material.13. The process of wherein the conversion process is hydroprocessing.14. The process of wherein the hydroprocessing process is selected from the group consisting of hydrodenitrification claim 13 , hydrodesulfurization claim 13 , hydrodemetallation claim 13 , hydrodesilication claim 13 , hydrodearomatization claim 13 , hydroisomerization claim 13 , hydrotreating ...

CRYSTALLINE TRANSITION METAL TUNGSTATE

A hydroprocessing catalyst has been developed. The catalyst is a unique transition metal tungstate material. The hydroprocessing using the crystalline ammonia transition metal dimolybdotungstate material may include hydrodenitrification, hydrodesulfurization, hydrodemetallation, hydrodesilication, hydrodearomatization, hydroisomerization, hydrotreating, hydrofining, and hydrocracking. 5. The crystalline transition metal tungstate material of wherein M is nickel.6. The crystalline transition metal tungstate material of wherein the crystalline transition metal tungstate material is sulfided.2. The crystalline transition metal tungstate material of wherein the crystalline transition metal tungstate material is present in a mixture with at least one binder and wherein the mixture comprises up to 25 wt % binder.3. The crystalline transition metal tungstate material of wherein the binder is selected from the group consisting of silicas claim 2 , aluminas claim 2 , and silica-aluminas.4. The crystalline transition metal tungstate material of wherein M is nickel or cobalt.(d) recovering the crystalline transition metal tungstate material.8. The method of wherein the reacting is conducted at a temperature of from 30° C. to about 130° C. for a period of time from about 30 minutes to 14 days.9. The method of wherein the recovering is by filtration claim 7 , centrifugation or drying.10. The method of further comprising adding a binder to the recovered crystalline transition metal tungstate material.11. The method of wherein the binder is selected from the group consisting of aluminas claim 10 , silicas claim 10 , and alumina-silicas.12. The method of further comprising sulfiding the recovered crystalline transition metal tungstate material.14. The process of wherein the conversion process is hydroprocessing.15. The process of wherein the conversion process is selected from the group consisting of hydrodenitrification claim 13 , hydrodesulfurization claim 13 , hydrodemetallation ...

CRYSTALLINE AMMONIA TRANSITION METAL MOLYBDOTUNGSTATE

A hydroprocessing catalyst has been developed. The catalyst is a unique crystalline ammonia transition metal molybdotungstate material. The hydroprocessing using the crystalline ammonia transition metal molybdotungstate material may include hydrodenitrification, hydrodesulfurization, hydrodemetallation, hydrodesilication, hydrodearomatization, hydroisomerization, hydrotreating, hydrofining, and hydrocracking. 2. The crystalline ammonia transition metal molybdotungstate material of wherein the crystalline ammonia transition metal molybdotungstate material is present in a mixture with at least one binder and wherein the mixture comprises up to 25 wt % binder.3. The crystalline ammonia transition metal molybdotungstate material of wherein the binder is selected from the group consisting of silicas claim 2 , aluminas claim 2 , and silica-aluminas.4. The crystalline ammonia transition metal molybdotungstate material of wherein M is nickel or cobalt.5. The crystalline ammonia transition metal molybdotungstate material of wherein M is nickel.6. The crystalline ammonia transition metal molybdotungstate material of wherein the crystalline ammonia transition metal molybdotungstate material is sulfided.8. The method of wherein the recovering is by filtration or centrifugation or evaporation of solvent9. The method of further comprising adding a binder to the recovered crystalline ammonia transition metal molybdotungstate material.10. The method of wherein the binder is selected from the group consisting of aluminas claim 7 , silicas claim 7 , and alumina-silicas.11. The method of further comprising sulfiding the recovered crystalline ammonia transition metal molybdotungstate material.13. The process of wherein the conversion process is hydroprocessing.14. The process of wherein the hydroprocessing process is selected from the group consisting of hydrodenitrification claim 13 , hydrodesulfurization claim 13 , hydrodemetallation claim 13 , hydrodesilication claim 13 , ...

CRYSTALLINE TRANSITION METAL MOLYBDOTUNGSTATE

A hydroprocessing catalyst has been developed. The catalyst is a unique transition metal tungstate material. The hydroprocessing using the crystalline transition metal molybdotungstate material may include hydrodenitrification, hydrodesulfurization, hydrodemetallation, hydrodesilication, hydrodearomatization, hydroisomerization, hydrotreating, hydrofining, and hydrocracking. 2. The crystalline transition metal molybdotungstate material of wherein the crystalline transition metal molybdotungstate material is present in a mixture with at least one binder and wherein the mixture comprises up to 25 wt % binder.3. The crystalline transition metal molybdotungstate material of wherein the binder is selected from the group consisting of silicas claim 2 , aluminas claim 2 , and silica-aluminas.4. The crystalline transition metal molybdotungstate material of wherein M is nickel or cobalt.5. The crystalline transition metal molybdotungstate material of wherein M is nickel.6. The crystalline transition metal molybdotungstate material of wherein the crystalline transition metal molybdotungstate material is sulfided.8. The method of wherein the reacting is conducted at a temperature of from 30° C. to about 130° C. for a period of time from about 30 minutes to 14 days.9. The method of wherein the recovering is by filtration claim 7 , centrifugation or drying.10. The method of further comprising adding a binder to the recovered crystalline transition metal molybdotungstate material.11. The method of wherein the binder is selected from the group consisting of aluminas claim 7 , silicas claim 7 , and alumina-silicas.12. The method of further comprising sulfiding the recovered crystalline transition metal molybdotungstate material.14. The process of wherein the conversion process is hydroprocessing.15. The process of wherein the conversion process is selected from the group consisting of hydrodenitrification claim 13 , hydrodesulfurization claim 13 , hydrodemetallation claim 13 , ...

TRANSITION METAL TUNGSTEN OXY-HYDROXIDE

A hydroprocessing catalyst has been developed. The catalyst is a unique transition metal tungsten oxy-hydroxide material. The hydroprocessing using the transition metal tungsten oxy-hydroxide material may include hydrodenitrification, hydrodesulfurization, hydrodemetallation, hydrodesilication, hydrodearomatization, hydroisomerization, hydrotreating, hydrofining, and hydrocracking. 2. The transition metal tungsten oxy-hydroxide material of wherein the transition metal tungsten oxy-hydroxide material is present in a mixture with at least one binder and wherein the mixture comprises up to 25 wt % binder.3. The transition metal tungsten oxy-hydroxide material of wherein the binder is selected from the group consisting of silicas claim 2 , aluminas claim 2 , and silica-aluminas.4. The transition metal tungsten oxy-hydroxide material of wherein M is nickel or cobalt.5. The transition metal tungsten oxy-hydroxide material of wherein M is nickel.6. The transition metal tungsten oxy-hydroxide material of wherein the transition metal tungsten oxy-hydroxide material is sulfided.8. The method of wherein the reacting is conducted at a temperature ranging from about 60° C. to about 120° C. for a period of time ranging from 30 minutes to around 2 days.9. The method of wherein the recovering is by filtration or centrifugation.10. The method of further comprising adding a binder to the recovered metal tungsten oxy-hydroxide material11. The method of wherein the binder is selected from the group consisting of aluminas claim 10 , silicas claim 10 , and alumina-silicas.12. The method of further comprising sulfiding the recovered transition metal tungsten oxy-hydroxide material.14. The process of wherein the conversion process is hydroprocessing.15. The process of wherein the conversion process is selected from the group consisting of hydrodenitrification claim 13 , hydrodesulfurization claim 13 , hydrodemetallation claim 13 , hydrodesilication claim 13 , hydrodearomatization claim 13 ...

ALIPHATIC CRACKING AND DEALKYLATION WITH HYDROGEN DILUENT

A naphtha cracking feed stream is taken, heated and passed to a cracking reactor. Hydrogen is added to the cracking reactor to mitigate catalyst deactivation. The aliphatic compounds are selectively cracked and at least a portion of the alkyl groups on the aromatic compounds are selectively dealkylated in the presence of a cracking catalyst to produce a cracked effluent stream comprising aromatic compounds and cracked olefins. 1. A process for making aromatics comprising:taking a cracking feed stream boiling in the naphtha range comprising aromatic compounds and aliphatic compounds, wherein at least a portion of the aromatic compounds contain alkyl groups;passing the cracking feed stream at a temperature of at least 500° C. to a cracking reactor comprising a cracking catalyst including a zeolite with a maximum pore diameter of greater than 5 Angstroms;adding at least about 60 mol % hydrogen to the cracking reactor to preserve the cracking catalyst against deactivation;selectively cracking the aliphatic compounds and selectively dealkylating the alkyl groups on the aromatic compounds in the presence of the cracking catalyst in the cracking reactor under cracking conditions to cracked olefins and aromatic compounds in a cracked effluent stream.2. The process of further comprising reforming a naphtha stream in a reforming unit under reforming conditions to produce a reformer effluent stream and taking said cracking feed stream from said reformer effluent stream.3. The process of wherein the zeolite comprises MFI zeolite.4. The process of wherein the zeolite comprises a silicalite catalyst having a zeolite silica to alumina molar ratio of greater than about 250.5. The process of wherein the hydrogen mol % in the cracking reactor is no more than 90.6. The process of wherein the hydrogen partial pressure in the cracking reactor is between about 62 kPa (9 psia) and about 345 kPa (50 psia).7. The process of wherein the hydrogen to hydrocarbon mole ratio is at least 2:1 at ...

HIGHLY ACTIVE QUATERNARY METALLIC MATERIALS USING SHORT-CHAIN ALKYL QUATERNARY AMMONIUM COMPOUNDS

A highly active quaternary mixed transition metal oxide material has been developed. The material may be sulfided to generate metal sulfides which are used as a catalyst in a conversion process such as hydroprocessing. The hydroprocessing may include hydrodenitrification, hydrodesulfurization, hydrodemetallation, hydrodesilication, hydrodearomatization, hydroisomerization, hydrotreating, hydrofining, and hydrocracking. 2. The mixed transition metal oxide material of wherein the mixed transition metal oxide material is present in a mixture with at least one binder and wherein the mixture comprises up to 80 wt % binder.3. The mixed transition metal oxide material of wherein the binder is selected from silicas claim 2 , aluminas claim 2 , silica-aluminas claim 2 , titanias claim 2 , zirconias claim 2 , natural clays claim 2 , synthetic clays claim 2 , and mixtures thereof.4. The mixed transition metal oxide material of wherein Mis Si claim 1 , Zr claim 1 , Mn claim 1 , Cu claim 1 , Zn claim 1 , or any mixture thereof.5. The mixed transition metal oxide material of wherein Mis Fe claim 1 , Co claim 1 , Ni claim 1 , or any mixture thereof.6. The mixed transition metal oxide material of wherein Mis Cr claim 1 , Mo claim 1 , or W.7. The mixed transition metal oxide material of wherein Mis Cr claim 1 , Mo claim 1 , or W and is different from M.8. The mixed transition metal oxide material of wherein the novel mixed transition metal oxide material is sulfided.10. The method of wherein the recovering is by decantation claim 9 , filtration or centrifugation.11. The method of further comprising adding a binder to the reaction mixture or to the recovered mixed transition metal oxide material.12. The method of wherein the binder is selected from aluminas claim 11 , silicas claim 11 , alumina-silicas claim 11 , titanias claim 11 , zirconias claim 11 , natural clays claim 11 , synthetic clays claim 11 , and mixtures thereof.13. The method of further comprising sulfiding at least a ...

HIGHLY ACTIVE TRIMETALLIC MATERIALS USING SHORT-CHAIN ALKYL QUATERNARY AMMONIUM COMPOUNDS

A highly active trimetallic mixed transition metal oxide material has been developed. The material may be sulfided to generate metal sulfides which are used as a catalyst in a conversion process such as hydroprocessing. The hydroprocessing may include hydrodenitrification, hydrodesulfurization, hydrodemetallation, hydrodesilication, hydrodearomatization, hydroisomerization, hydrotreating, hydrofining, and hydrocracking. 2. The mixed transition metal oxide material of wherein the mixed transition metal oxide material is present in a mixture with at least one binder and wherein the mixture comprises up to 80 wt % binder.3. The mixed transition metal oxide material of wherein the binder is selected from silicas claim 2 , aluminas claim 2 , silica-aluminas claim 2 , titanias claim 2 , zirconias claim 2 , natural clays claim 2 , synthetic clays claim 2 , and mixtures thereof.4. The mixed transition metal oxide material of wherein Mis Fe claim 1 , Co claim 1 , Ni claim 1 , or any mixture thereof.5. The mixed transition metal oxide material of wherein Mis Cr claim 1 , Mo claim 1 , or W.6. The mixed transition metal oxide material of wherein Mis Cr claim 1 , Mo claim 1 , or W and is different from M.7. The mixed transition metal oxide material of wherein the novel mixed transition metal oxide material is sulfided.9. The method of wherein the recovering is by decantation claim 8 , filtration or centrifugation.10. The method of further comprising adding a binder to the reaction mixture or to the recovered mixed transition metal oxide material.11. The method of wherein the binder is selected from aluminas claim 10 , silicas claim 10 , alumina-silicas claim 10 , titanias claim 10 , zirconias claim 10 , natural clays claim 10 , synthetic clays claim 10 , and mixtures thereof.12. The method of further comprising sulfiding at least a portion of the recovered mixed transition metal oxide material.13. The method of further comprising adjusting the pH of the reaction mixture using an ...

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.

CO-MIXED CATALYST PRODUCED FROM SOLUTIONS CONTAINING HETEROPOLYANIONS, METHOD FOR THE PRODUCTION THEREOF, AND USE OF SAME IN HYDROCONVERSION OF HEAVY HYDROCARBON FEEDSTOCK

The present invention relates to a process for the preparation of catalyst(s), comprising the cokneading of boehmite with an active phase comprising a salt of heteropolyanion of Keggin and/or lacunary Keggin and/or substituted lacunary Keggin and/or Anderson and/or Strandberg type, and their mixtures, exhibiting, in its structure, molybdenum and cobalt and/or nickel. The present invention also relates to a process for the hydrotreating and/or hydroconversion of a heavy hydrocarbon feedstock in the presence of catalyst(s) prepared according to said process. 1. A process for the preparation of a catalyst comprising an active phase comprising molybdenum and nickel and/or cobalt , and an oxide matrix predominantly composed of alumina , said catalyst comprising a total pore volume of at least 0.6 ml/g , a macropore volume of between 10.0% and 40.0% of the total pore volume , a mesopore volume of at least 0.5 ml/g and a mean mesopore diameter of greater than 5.0 nm , comprising the following stages:a) a stage of preparation of an aqueous solution of aluminum precursors comprising a first acidic aluminum precursor, chosen from aluminum sulfate, aluminum chloride, aluminum nitrate and their mixtures, and a first basic aluminum precursor, chosen from sodium aluminate, potassium aluminate, ammonia, sodium hydroxide, potassium hydroxide and their mixtures;b) a stage of bringing the solution obtained on conclusion of stage a) into contact with a second basic precursor, chosen from sodium aluminate, potassium aluminate, ammonia, sodium hydroxide, potassium hydroxide and their mixtures, and with a second acidic precursor chosen from aluminum sulfate, aluminum chloride, aluminum nitrate, sulfuric acid, hydrochloric acid, nitric acid and their mixtures, in order to obtain a suspension, with at least one of the second basic or acidic precursors comprising aluminum, the relative flow rate of the second acidic and basic precursors being chosen so as to obtain a pH of the reaction ...

CRYSTALLINE AMMONIA TRANSITION METAL MOLYBDOTUNGSTATE

A hydroprocessing catalyst or catalyst precursor has been developed. The catalyst is a unique crystalline ammonia transition metal molybdotungstate material. The hydroprocessing using the crystalline ammonia transition metal molybdotungstate material or a decomposition product thereof may include hydrodenitrification, hydrodesulfurization, hydrodemetallation, hydrodesilication, hydrodearomatization, hydroisomerization, hydrotreating, hydrofining, and hydrocracking. 2. The process of wherein the conversion process is hydroprocessing.3. The process of wherein the hydroprocessing process is selected from the group consisting of hydrodenitrification claim 1 , hydrodesulfurization claim 1 , hydrodemetallation claim 1 , hydrodesilication claim 1 , hydrodearomatization claim 1 , hydroisomerization claim 1 , hydrotreating claim 1 , hydrofining claim 1 , and hydrocracking.4. The process of wherein the crystalline ammonia transition metal molybdotungstate material is present in a mixture with at least one binder and wherein the mixture comprises up to 25 wt % binder.5. The process of wherein the binder is selected from the group consisting of silicas claim 4 , aluminas claim 4 , and silica-aluminas.6. The process of wherein the feed comprises sulfur and the decomposition by sulfidation comprises contacting the crystalline ammonia transition metal molybdotungstate material with the sulfur containing feed.7. The process of wherein the decomposition by sulfidation comprises contacting the crystalline ammonia transition metal molybdotungstate material with a gaseous mixture of HS/H.8. The process of wherein the sulfidation is conducted at a temperature ranging from about 50° C. to about 600° C.9. The process of wherein the sulfidation is conducted at a temperature ranging from about 150° C. to about 500° C.10. The process of wherein the sulfidation is conducted at a temperature ranging from about 250° C. to about 450° C.12. The method of wherein the recovering is by filtration or ...

CRYSTALLINE TRANSITION METAL MOLYBDOTUNGSTATE

A hydroprocessing catalyst or catalyst precursor has been developed. The catalyst is a transition metal tungstate material, or the decomposition product thereof. The hydroprocessing using the crystalline transition metal molybdotungstate material may include hydrodenitrification, hydrodesulfurization, hydrodemetallation, hydrodesilication, hydrodearomatization, hydroisomerization, hydrotreating, hydrofining, and hydrocracking. 2. The process of wherein the conversion process is hydroprocessing.3. The process of wherein the conversion process is selected from the group consisting of hydrodenitrification claim 1 , hydrodesulfurization claim 1 , hydrodemetallation claim 1 , hydrodesilication claim 1 , hydrodearomatization claim 1 , hydroisomerization claim 1 , hydrotreating claim 1 , hydrofining claim 1 , and hydrocracking.4. The process of wherein the crystalline transition metal molybdotungstate material claim 1 , or the decomposition product claim 1 , or both is present in a mixture with at least one binder and wherein the mixture comprises up to 25 wt % binder.5. The process of wherein the binder is selected from the group consisting of silicas claim 4 , aluminas claim 4 , and silica-aluminas.6. The process of wherein the feed comprises sulfur and the decomposition by sulfidation comprises contacting the crystalline transition metal molybdotungstate material with the sulfur containing feed.7. The process of wherein the decomposition by sulfidation comprises contacting the crystalline transition metal molybdotungstate material with a gaseous mixture of HS/H.8. The process of wherein the sulfidation is conducted at a temperature ranging from about 50° C. to about 600° C.9. The process of wherein the sulfidation is conducted at a temperature ranging from about 150° C. to about 500° C.10. The process of wherein the sulfidation is conducted at a temperature ranging from about 250° C. to about 450° C.12. The method of wherein the reacting is conducted at a temperature of ...

TRANSITION METAL TUNGSTEN OXY-HYDROXIDE

A hydroprocessing catalyst or catalyst precursor has been developed. The catalyst is a unique transition metal tungsten oxy-hydroxide material. The hydroprocessing using the transition metal tungsten oxy-hydroxide material or the decomposition product thereof may include hydrodenitrification, hydrodesulfurization, hydrodemetallation, hydrodesilication, hydrodearomatization, hydroisomerization, hydrotreating, hydrofining, and hydrocracking. 2. The process of wherein the conversion process is hydroprocessing.3. The process of wherein the conversion process is selected from the group consisting of hydrodenitrification claim 1 , hydrodesulfurization claim 1 , hydrodemetallation claim 1 , hydrodesilication claim 1 , hydrodearomatization claim 1 , hydroisomerization claim 1 , hydrotreating claim 1 , hydrofining claim 1 , and hydrocracking.4. The process of wherein the transition metal tungsten oxy-hydroxide material claim 1 , or the decomposition product claim 1 , or both claim 1 , are present in a mixture with at least one binder and wherein the mixture comprises up to 25 wt % binder.5. The process of wherein the binder is selected from the group consisting of silicas claim 4 , aluminas claim 4 , and silica-aluminas6. The process of wherein the feed comprises sulfur and the decomposition by sulfidation comprises contacting the metal tungsten oxy-hydroxide material with the sulfur containing feed.7. The process of wherein the decomposition by sulfidation comprises contacting the metal tungsten oxy-hydroxide material with a gaseous mixture of HS/H.8. The process of wherein the sulfidation is conducted at a temperature ranging from about 50° C. to about 600° C.9. The process of wherein the sulfidation is conducted at a temperature ranging from about 150° C. to about 500° C.10. The process of wherein the sulfidation is conducted at a temperature ranging from about 250° C. to about 450° C.12. The method of wherein the reacting is conducted at a temperature ranging from about ...

PROCESS FOR PREPARING A MULTIELEMENT OXIDE COMPRISING BISMUTH AND TUNGSTEN BY COPRECIPITATION

Shaped catalyst bodies comprising a multielement oxide I having the general stoichiometry I [BiWO][MoZZFeZZZO](I), where Z=Ni or Co, Z=alkali metal or alkaline earth metal, Z=zinc, phosphorus, arsenic, boron, antimony, tin, cerium, vanadium, chromium or bismuth, Z=silicon, aluminum, titanium, tungsten or zirconiurn, Z=copper, silver, gold, yttrium, lanthanum and lanthanides, a=0.1 to 3, b=0.1 to 10, c=1 to 10, d=0.01 to 2, e=0.01 to 5, f=0 to 5, g=0 to 10, h=0 to 1 and x, y=numbers determined by the valence and abundance of the elements other than oxygen in I, as active composition are produced by preforming a mixed oxide BiWOby coprecipitation from an aqueous environment at a pH in the range from 1.5 to 3 and isolation of the precipitate by means of a mechanical separation process and mixing the preformed mixed oxide BiWOwith a precursor having the stoichiometry [MoZZFeZZZO], shaping the mixture to form shaped bodies and thermally treating and calcining the shaped bodies at elevated temperature to give the shaped catalyst bodies. The process leads to homogeneous precipitation products having a stoichiometric composition. It is an alternative to the energy-intensive production by spray drying. 1: A process for producing a shaped catalyst body comprising a multi-element oxide formula I as an active composition ,{'br': None, 'sub': 1', 'b', 'x', 'a', '12', 'c', 'd', 'e', 'f', 'g', 'h', 'y', '1, 'sup': 1', '2', '3', '4', '5, '[BiWO][MoZZFeZZZO]\u2003\u2003(I),'}wherein{'sup': '1', 'Zis at least one element selected from the group consisting of nickel and cobalt,'}{'sup': '2', 'Zis at least one element selected from the group consisting of alkali metals and alkaline earth metals,'}{'sup': '3', 'Zis at least one element selected from the group consisting of zinc, phosphorus, arsenic, boron, antimony, tin, cerium, vanadium, chromium and bismuth,'}{'sup': '4', 'Zis at least one element selected from the group consisting of silicon, aluminum, titanium, tungsten and ...

PROCESS FOR PRODUCING CHLOROSILANES USING A CATALYST SELECTED FROM THE GROUP OF CO, MO, W

Generally unusable or difficultly useable dusts of ultrahigh purity silicon can be used to produce chlorosilanes under reasonable reaction conditions by employing a catalyst containing one or more of Co, Mo, W. The process may be incorporated into an integral plant for the production of polycrystalline silicon. 114.-. (canceled)15. A process for producing chlorosilanes in a fluidized bed reactor comprising: reacting a hydrogen chloride-containing reaction gas with a particulate contact mass containing ultrahigh purity silicon having a purity of >99.9% and a catalyst , wherein the catalyst comprises at least one element from the group comprising Co , Mo and W , wherein the chlorosilanes have the general formula HSiCland/or HClSiwhere n=1-4 and m=0-4 , and wherein the catalyst is present in the contact mass in a proportion of 100 to 400 ppmw , based on the weight of the contact mass.16. The process of claim 15 , wherein the catalyst further comprises at least one element from the group comprising Zn claim 15 , Cr and Ni.17. The process of claim 15 , wherein the catalyst is present in the contact mass in metallic claim 15 , oxidic claim 15 , carbidic claim 15 , alloyed and/or salt-like form.18. The process of claim 15 , wherein the contact mass is a byproduct in the deposition of polycrystalline silicon and/or in the mechanical processing of polycrystalline/multicrystalline or single-crystal silicon.19. The process of claim 15 , wherein the catalyst is a constituent of an abraded material from comminution equipment claim 15 , plant parts and/or pipelines associated with silicon production or processing.20. The process of claim 15 , wherein the ultrahigh purity silicon has a Sauter mean diameter dof 0.5 to 150 μm.21. The process of claim 15 , wherein the ultrahigh purity silicon has a Sauter mean diameter dof 1 to 100 μm.22. The process of claim 15 , wherein the ultrahigh purity silicon has a Sauter mean diameter dof 5 to 80 μm.23. The process of claim 15 , wherein the ...

Upgrading Hydrocarbon Pyrolysis Products

A hydrocarbon conversion process comprises providing a hydrocarbon feedstock comprising an effluent fraction from a pyrolysis process, wherein the effluent fraction has an initial boiling point at atmospheric pressure of at least 177° C. and a final boiling point at atmospheric pressure of no more than 343° C. and comprises at least 0.5 wt. % of olefinic hydrogen atoms based on the total weight of hydrogen atoms in the effluent fraction. The hydrocarbon feedstock is hydroprocessed in at least one hydroprocessing zone in the presence of treatment gas comprising molecular hydrogen under catalytic hydroprocessing conditions to produce a hydroprocessed product comprising less than 0.5 wt. % of olefinic hydrogen atoms based on the total weight of hydrogen atoms in the hydroprocessed product. The hydroprocessing conditions comprise a temperature from 150 to 350° C. and a pressure from 500 to 1500 psig (3550 to 10445 kPa-a). 1. A hydrocarbon conversion process comprising:(a) providing a hydrocarbon feedstock comprising an effluent fraction from a pyrolysis process, wherein the effluent fraction has an initial boiling point at atmospheric pressure of at least 177° C. and a final boiling point at atmospheric pressure of no more than 343° C. and comprises at least 0.5 wt. % of olefinic hydrogen atoms based on the total weight of hydrogen atoms in the effluent fraction; and(b) hydroprocessing the hydrocarbon feedstock in at least one hydroprocessing zone in the presence of treatment gas comprising molecular hydrogen under catalytic hydroprocessing conditions to produce a hydroprocessed product comprising less than 0.5 wt. % of olefinic hydrogen atoms based on the total weight of hydrogen atoms in the hydroprocessed product, wherein the hydroprocessing conditions comprise a temperature from 150 to 350° C. and a pressure from 500 to 1500 psig (3550 to 10445 kPa-a).2. The process of claim 1 , wherein the effluent fraction has an initial boiling point at atmospheric pressure of at ...

PROCESSING OF HEAVY HYDROCARBON FEEDS

Systems and methods are provided for hydroconversion of a heavy oil feed under slurry hydroprocessing conditions and/or solvent assisted hydroprocessing conditions. The systems and methods for slurry hydroconversion can include the use of a configuration that can allow for improved separation of catalyst particles from the slurry hydroprocessing effluent. In addition to allowing for improved catalyst recycle, an amount of fines in the slurry hydroconversion effluent can be reduced or minimized. This can facilitate further processing or handling of any “pitch” generated during the slurry hydroconversion. The systems and methods for solvent assisted hydroprocessing can include processing of a heavy oil feed in conjunction with a high solvency dispersive power crude. 115.-. (canceled)16. A process for producing a hydroprocessed product , comprising:{'sup': '−1', 'exposing a combined feedstock comprising a heavy oil feed component and at least about 5 wt % of a High Solvency Dispersive Power (HSDP) crude component to a hydroprocessing catalyst under effective fixed bed hydroprocessing conditions to form a hydroprocessed effluent, the effective fixed bed hydroprocessing conditions including a pressure of about 1500 psig (˜10.3 MPa) or less, a temperature of at least about 360° C., and a liquid hourly space velocity of the fraction of the combined feedstock boiling above 1050° F. (˜566° C.) of at least about 0.10 hr,'}the HSDP crude component having a TAN of at least about 0.3 and a solubility blending number of at least about 75, the HSDP crude component optionally comprising an aromatics content of at least about 50 wt %.17. The process of claim 16 , wherein the HSDP crude component has a 10% distillation point of at least about 800° F. (˜427° C.).18. The process of claim 16 , wherein the heavy oil feed component has a 10% distillation point of at least about 900° F. (˜482° C.).19. The process of claim 16 , wherein the effective fixed bed hydroprocessing conditions are ...

HYDROCONVERSION PROCESS TO UPGRADE THE TRANSPORT PROPERTIES OF HEAVY AND EXTRA-HEAVY CRUDE OILS AT LOW SEVERITY CONDITIONS USING DISPERSED-PHASE CATALYST

The present invention relates to a catalytic hydroconversion process in dispersed phase of extra-heavy and heavy crude oils for upgrading their transport properties, that operates at low severity conditions, in such a way that the obtained product can be transported by conventional pumping to the distribution and refining centers. 1. A catalytic hydroconversion process in dispersed-phase at low severity to upgrade the transport properties of extra-heavy and heavy crude oils with API gravity between 3 to 16 and kinematic viscosity at 37.8° C. higher than 6000 cSt , said process is characterized by a hot extra heavy-heavy crude oil at temperature in the range of 50 to 200° C. is fed to a feed/product heat exchanger with the aim of recovering heat from the reactor effluent before entering the direct tire heater , the extra-heavy or heavy crude oil is mixed with a hydrogen stream in a hydrogen/hydrocarbon ratio between 400-2500 ft/bbl and a catalyst stream in concentrations of 0.5 to 2 wt. % with respect to the reactor feed. The hydrogen stream is a mixture of make-up hydrogen plus the gaseous effluent from the liquid/gas products separator; the reaction mixture is added to an adiabatic reactor in which the hydroconversion reactions take place at a temperature of 320-400° C. , pressure of 30-100 Kg/cm , liquid space-velocity between 0.1 and 3.0 h; the hot reactor effluent product is recovered in a gas/liquid separator and it is used to preheat the fresh feed. In this equipment , the hydroconverted liquid hydrocarbon fraction is separated with appropriated properties for transportation by conventional processing lines; the gaseous fraction is recycled to the direct fire heater for its feedback to the process; the composition of this gas includes hydrogen , hydrogen sulfide and light hydrocarbons at low concentrations.2. The catalytic hydroconversion process at low severity in accordance with claim 1 , characterized by the catalyst addition to the feed flow by dissolving ...

PROCESSING OF HEAVY HYDROCARBON FEEDS

Systems and methods are provided for hydroconversion of a heavy oil feed under slurry hydroprocessing conditions and/or solvent assisted hydroprocessing conditions. The systems and methods for slurry hydroconversion can include the use of a configuration that can allow for improved separation of catalyst particles from the slurry hydroprocessing effluent. In addition to allowing for improved catalyst recycle, an amount of fines in the slurry hydroconversion effluent can be reduced or minimized. This can facilitate further processing or handling of any “pitch” generated during the slurry hydroconversion. The systems and methods for solvent assisted hydroprocessing can include processing of a heavy oil feed in conjunction with a high solvency dispersive power crude. 120.-. (canceled)21. A process for producing a hydroprocessed product , comprising:passing a feedstock comprising resid to a first reactor operating at about 1000 psig (˜6.9 MPag) or less,demetallizing at least about 60 wt % and up of the feedstock to create a liquid product,passing the liquid product from the first reactor to a fractionator,separating out in the fractionator a heavy residuum fraction having a boiling point of about 1050° F. (˜566° C.),passing the heavy residuum fraction from the fractionator to a second reactor operating at from about 1500 psig (˜10.4 MPag) to about 3400 psig (˜23.5 MPag).22. The process of claim 21 , wherein the temperature of first reactor is between 650° F. (˜343° C.) and 850° F. (˜454° C.).23. The process of claim 21 , wherein demetallizing further comprises exposing the feedstock to a demetallization catalyst at a pressure of about 300 psig (˜2.1 MPag) to about 800 psig (˜5.6 MPag) and a temperature of about 600° F. (˜316° C.) to about 1000° F. (˜538° C.).24. The process of claim 23 , whereina) the demetallization catalyst has a mean pore diameter of 60 Å or less,{'sup': 2', '3, 'b) the demetallization catalyst comprises a catalyst with a surface area of at least ...

High purity olefinic naphthas for the production of ethylene and propylene

A hydrogenation catalyst and use thereof

A hydrogenation catalyst comprises a support, metal active components consisting of Ni, Mo and W which are carried on the support, and auxiliary active components selected from the group consisting of F , P or their combination. Another hydrogenation catalyst comprises a support having molecular sieve component, metal active components consisting of Ni, Mo and W which are carried on the support . The catalysts can be used in methods for hydrogenation of hydrocarbon oil .The catalysts have higher catalytic activity than conventional catalysts.

Highly stable hydrocarbon-soluble molybdenum catalyst precursors and methods for making same

Hydrocarbon-soluble molybdenum catalyst precursors include a plurality of molybdenum cations and a plurality of carboxylate anions having at least 8 carbon atoms. The carboxylate anions are alicyclic, aromatic, or branched, unsaturated and aliphatic, and can derived from carboxylic acids selected from 3-cyclopentylpropionic acid, cyclohexanebutyric acid, biphenyl-2-carboxylic acid, 4-heptylbenzoic acid, 5-phenylvaleric acid, geranic acid, 10-undecenoic acid, dodecanoic acid, and combinations thereof. The molybdenum salts have decomposition temperatures higher than 210° C. The catalyst precursors can form a hydroprocessing molybdenum sulfide catalyst in heavy oil feedstocks. Also disclosed are methods for making catalyst precursors and hydrocracking heavy oil using active catalysts.

一种加氢催化剂组合物和加氢处理的方法

本公开涉及一种加氢催化剂组合物和加氢处理的方法，该加氢催化剂组合物包括加氢催化剂I和加氢催化剂II；以体积计并以所述加氢催化剂组合物为基准，所述加氢催化剂I的含量为5‑95％；所述加氢催化剂I包括载体、加氢活性金属元素和金属助剂元素，所述加氢活性金属元素含有第VIB族金属元素和第VIII族金属元素；其中，所述加氢催化剂I的制备方法包括：将负载有含加氢活性金属元素的化合物、第一有机络合剂和金属助剂元素的载体进行第一干燥和焙烧，得到半成品催化剂；将第二有机络合剂负载到所述半成品催化剂上，并进行第二干燥且不进行焙烧，得到所述加氢催化剂I。将本公开提供的加氢催化剂组合物应用于加氢处理时，活性好，寿命长。

一种加氢处理催化剂及其制备方法和应用

本发明公开了一种加氢处理催化剂，其包括金属活性组分和负载所述金属活性组分的载体，其中，所述金属活性组分包含WO 3 、NiO、CoO和MoO 3 ，所述载体的结构中包括MgO和含孔道的金属氧化物基体，所述MgO均匀分散在含孔道的金属氧化物基体中，且至少大部分MgO均匀分散在所述含孔道的金属氧化物基体的孔道表面。该加氢处理催化剂在低温条件下兼具高脱硫、脱氮、烯烃饱和性能，是性能优异的馏分油加氢精制催化剂，适用于所有馏分油以及煤制油的加氢处理过程。本发明还公开了该加氢处理催化剂的制备方法和应用。

A hydrogenation catalyst and its application

Catalyst for deep hydrofining oil fractions and method of preparation thereof

FIELD: chemistry. SUBSTANCE: invention relates to production of hydrotreating catalysts. Described is a hydrofining catalyst for petroleum fractions which includes nickel, molybdenum, tungsten and a carrier, characterized in that NiO, MoO 3 and WO 3 are deposited on a calcined support from a co-solution containing mixed heteropoly compounds H 4 [SiMo n W 12-n O 40 ] (n = 1–6), nickel carbonate NiCO 3 ×H 2 O and organic additive, followed by activation of catalyst with mixture of dimethyl disulphide and kerosene fraction at 240 °C for 10 hours and at 340 °C for 10 hours. Content of metals in calcined catalyst is: MoO 3 - 1.0–9.0 wt. %, WO 3 - 13.0–25.0 wt. %, NiO - 3.0–5.0 wt. %; the rest is a porous carrier with carbon content of 0–4 wt. %. Catalyst has specific surface area of not less than 180 m 2 /g, specific pore volume of not less than 0.5 cm 3 /g, effective pore diameter of not less than 6.0 nm. Organic additive used is at least one of the following: citric acid C 6 H 8 O 7 , tartaric acid C 4 H 6 O 6 , ethylene glycol C 2 H 6 O 2 . EFFECT: technical result is obtaining a catalyst characterized by high activity during hydrofining of oil fractions. 4 cl, 2 tbl, 10 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 741 303 C1 (51) МПК B01J 23/883 (2006.01) B01J 23/888 (2006.01) B01J 21/04 (2006.01) B01J 21/12 (2006.01) B01J 27/047 (2006.01) B01J 31/22 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА B01J 37/02 (2006.01) ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ C10G 45/08 (2006.01) (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК B01J 23/883 (2020.08); B01J 23/8885 (2020.08); B01J 21/04 (2020.08); B01J 21/12 (2020.08); B01J 27/047 (2020.08); B01J 31/2208 (2020.08); B01J 37/0203 (2020.08); C10G 45/08 (2020.08) (21)(22) Заявка: 2019144318, 27.12.2019 27.12.2019 Дата регистрации: 25.01.2021 (45) Опубликовано: 25.01.2021 Бюл. № 3 Адрес для переписки: 443100, г. Самара, ул. Молодогвардейская, 244, Главный корпус ФГБОУ ВО "СамГТУ" 2 7 4 1 3 0 3 C 1 (56) Список документов, цитированных в отчете о поиске: RU ...

Method of coating a catalyst to a support for use in acrolein oxidation

A method of coating a catalyst to a support for use in acrolein oxidation reaction. Metallic salt components of the catalyst including molybdate, vanadate and tungstate are dissolved in a liquid to form a suspension of particles of the catalyst. The precipitation of the catalyst particles is controlled by homogenizing the catalyst particles suspended in the liquid. The phase separation between the catalyst particles and the liquid can be substantially slowed down by the homogenization. Then the catalyst is coated on an inert support by applying the suspension of the catalyst particles to the support. In the suspension, the total weight of water is about 0.8 to about 5 times of the total weight of the metallic salts in the catalyst. This method of preparing suspension minimizes the amount of the liquid required to dissolve the metallic salts, which reduces the amount of time and energy to be used in evaporating the liquid from the suspension. Additionally, in obtaining catalyst from the suspension prepared by this method, it is possible to avoid the deterioration of the catalytic performance since less heat is required to evaporate the water.

本体催化剂组合物以及制备本体催化剂组合物的方法

本发明涉及包含金属氧化物颗粒的本体催化剂组合物，所述金属氧化物颗粒包括一种或者多种VIII族金属和两种或者更多种VIB族金属，所述本体催化剂组合物包含第一金属氧化物颗粒和单独制备的第二金属氧化物颗粒，所述第一金属氧化物颗粒含有一种或者多种第一VIII族金属和一种或者多种第一VIB族金属；所述第二金属氧化物颗粒含有一种或者多种第二VIII族金属和一种或者多种第二VIB族金属，其中，在所述第一和第二金属氧化物颗粒中VIB族和VIII族金属的组成是不同的，其中所述第一和第二氧化物本体颗粒被分别成形，以分离第一和第二成形的本体催化剂颗粒，将所述第一和第二成形的本体催化剂颗粒混合，优选混合成为均匀的混合物，以形成本体催化剂组合物。本发明还涉及用于制备所述本体催化剂组合物的方法，以及涉及使用所述本体催化剂组合物对烃类原料进行加氢处理。

Preparation of ctalyst for partially oxidizing of acrolein

본 발명은 아크롤레인의 부분 산화에 의해 아크릴산을 제조하는데 사용되는, 하기 일반식 (1)의 촉매성분을 가지는 담체상 촉매의 제조 방법에 있어서, 일반식 (1)에 표시된 각 금속 성분의 염 수용액을 교반하에 혼합하여 촉매 현탁액을 제조하고, 현탁액 제조 후 또는 현탁액 제조와 동시에 현탁액중의 침전물을 분쇄하고, 상기 현탁액을 불활성 담체상에 열풍건조하에 분사시키는 단계를 포함하는 것을 특징으로 하는 방법을 제공한다. The present invention provides a method for producing a carrier catalyst having a catalyst component of formula (1), which is used to produce acrylic acid by partial oxidation of acrolein, wherein an aqueous solution of salt of each metal component represented by formula (1) Mixing under stirring to prepare a catalyst suspension, pulverizing the precipitate in the suspension after or at the same time as preparing the suspension, and spraying the suspension under hot air drying on an inert carrier. . [화학식 1] [Formula 1]

Hydrocarbon conversion process using novel silica-substituted aluminas

Hydrocarbons are reduced in molecular weight in a conversion process wherein they are contacted with a non-zeolitic solid catalyst comprising an alumina, such as gamma alumina, which has been isomorphously substituted with silicon. The treated alumina will have a fluorine to silicon mole ratio of about 0.8:1 to about 1.3:1. For use in hydrocracking, the catalyst contains a metal hydrogenation component and possibly one or more other inorganic oxides such as silica-alumina. Other non-zeolitic materials such as delaminated clay or silica-alumina may also be composited into the catalysts.

一种将源自混合塑料热解的热解油同时进行脱氯化氢和加氢裂化并同时实现c9+芳烃的选择性加氢脱烷基化的方法

一种对烃流进行加氢脱烷基化的方法，其包括：(a)使烃流在氢气存在下在加氢处理反应器中与加氢处理催化剂接触，得到烃产物，其中所述烃流含有C 9 +芳烃；和(b)从所述烃产物中回收经处理的烃流，其中所述经处理的烃流包含C 9 +芳烃，其中由于源自所述烃流的至少一部分C 9 +芳烃在步骤(a)接触期间的加氢脱烷基化，所述经处理的烃流中C 9 +芳烃的量小于所述烃流中C 9 +芳烃的量。

催化柴油的加工处理方法

本发明公开了一种催化裂化柴油加工处理方法。将催化柴油原料切割为轻组分和重组分；轻组分进行加氢精制及加氢转化反应，得到汽油和柴油组分；所得重组分进行分离，得到三环芳烃组分和非三环芳烃组分；所得非三环芳烃进行加氢精制和加氢转化，所得三环芳烃组分进行加氢精制及加氢转化，得到汽油组分和柴油组分；各部分汽油混合后得到汽油产品，各部分柴油组分混合后得到柴油产品。本发明通过合理的分离及加工过程，可以针对不同类型原料进行选择性的单独加工，从而能够合理地利用劣质催化裂化柴油生产出合格的汽油及柴油产品。

Preparation of w/mo/alumina catalyst for hydrodesulfurization of petroleum

본 발명은 나프타, 등유, 경유 및 중질유의 수소화탈황과 수소화처리 반응을 수행하는데 있어서 CoO-MoO 3 또는 NiO-MoO 3 촉매와 같은 기존의 몰리브데늄계 알루미나 담지촉매에 숫자를 증가시키고 또한 활성전의 촉매표면에서의 분산도를 높임으로써 촉매의 반응활성도를 증가시키면서, 아울러 반응기에서의 사용중 카본의 침적 및 촉매 활성상의 소결(Sintering)으로 인한 비활성화를 최소화하는 효과를 얻기 위한 촉매의 조성, 제조방법 및 그 특성에 관한 것이다. The present invention increases the number of existing molybdenum-based alumina supported catalysts such as CoO-MoO 3 or NiO-MoO 3 catalysts in carrying out the hydrodesulfurization and hydrotreating reactions of naphtha, kerosene, diesel and heavy oil. By increasing the dispersity at the surface of the catalyst, the catalyst composition, preparation method, and method for increasing the reaction activity of the catalyst and at the same time minimizing deactivation due to deposition of carbon and sintering of the catalyst active phase in the reactor and It's about the characteristics.

Process for the preparation of a shaped bulk catalyst

본 발명은 하나 이상의 VIII 족 금속 및 둘 이상의 VIB 족 금속을 포함하는 금속 산화 입자를 포함하는 성형 벌크 촉매의 제조 방법에 관한 것으로서, 하나 이상의 제 1 VIII 족 금속 및 하나 이상의 제 1 VIB 족 금속을 포함하는 제 1 금속 산화 입자를 제공하고, 하나 이상의 제 2 VIII 족 금속 및 하나 이상의 제 2 VIB 족 금속을 포함하는, 별도로 제조된 제 2 금속 산화 입자를 제공하고, 여기서, 상기 제 1 및 제 2 금속 산화 입자 내의 VIB 족 및 VIII 족 금속의 조성이 상이하고 성형 전 및/또는 성형 동안 제 1 및 제 2 금속 산화 입자를 배합시키고 배합된 제 1 및 제 2 금속 산화 입자를 성형하여 성형 벌크 촉매를 형성하는 것을 포함한다. 추가적으로, 본 발명은 상기 방법에 의해 황화 또는 비황화된 형태로 수득 가능한 성형 벌크 촉매 및, 이의 수소가공에서의 용도에 관한 것이다. The present invention relates to a process for the production of shaped bulk catalysts comprising metal oxide particles comprising at least one Group VIII metal and at least two Group VIB metals, comprising at least one Group 1 VIII metal and at least one Group 1 VIB metal Providing a first metal oxide particle, and separately prepared second metal oxide particle comprising at least one second Group VIII metal and at least one second Group VIB metal, wherein the first and second metals The composition of the Group VIB and Group VIII metals in the oxide particles is different and the first and second metal oxide particles are blended before and / or during molding and the combined first and second metal oxide particles are molded to form a shaped bulk catalyst. It involves doing. In addition, the present invention relates to shaped bulk catalysts obtainable in sulfided or unsulfurized form by the above process, and their use in hydroprocessing. 성형 벌크 촉매, 금속 산화 입자, 수소가공 Formed bulk catalyst, metal oxide particles, hydrogen processing

By the production of the steam cracked stock with high ethylene, propylene and polymer yield that vegetable oil hydrotreating is made

本发明涉及获自可再生资源的原料的处理方法，包括在固定床催化剂(所述催化剂包含加氢‑脱氢官能和非晶载体)存在下在50至450℃的温度、1 MPa至10 MPa的压力、0.1 h ‑1 至10 h ‑1 的时空速度下和在使得氢/原料比为50至1000 Nm 3 氢/m 3 原料的与原料混合的总氢量存在下的加氢处理步骤，接着从获自阶段a)的加氢处理流出物中分离出氢、气体和至少一种包括至少50%直链正链烷烃的液体烃流出物，和获自阶段b)的至少一部分液体烃流出物的蒸汽裂化。

A kind of nontoxic high temperature alkali resistant metal denitrating catalyst and its preparation method and application

本发明属于大气污染控制技术领域，具体涉及一种无毒中高温抗碱金属脱硝催化剂及其制备方法和应用。本发明脱硝催化剂以二氧化钛为载体，以铈氧化物、铁氧化物、镍氧化物中的一种或多种为活性组分，以铌氧化物、钼氧化物和钨氧化物中的一种或多种为助剂。本发明脱硝催化剂在300～400℃和6,000～100,000h ‑1 空速的条件下，脱硝效率稳定在95%以上，N 2 选择性高于92%，且在含有0～3000mg/m 3 的SO 2 和5‑20%H 2 O的氮氧化物烟气下依旧保持90%以上，N 2 选择性高于90%，具有强抗硫抗水能力，且该催化剂在负载0‑400μmol/g碱金属后活性基本不变，特别适用于电站锅炉等烟气的氮氧化物排放控制。

Preparation method of efficient bulk phase hydrogenation catalyst

本发明为一种高效体相加氢催化剂的制备方法，该方法包括：将含Ni化合物、硅藻土、分散剂和去离子水混合形成高度分散体系，然后加入导向剂，使Ni源颗粒以高度分散状态均匀分布于硅藻土基体的孔道结构中，再依次加入含Mo化合物和含W化合物，与含Ni化合物结合形成高分散性Ni‑Mo和Ni‑W活性相，然后加入硅藻土，对体系中可溶性金属组分进行吸附，然后过滤浆液得到滤饼；将滤饼适当烘干后挤条、干燥、焙烧得到催化剂。本发明方法制备的催化剂活性相晶粒尺寸小、分布均匀、分散性好，活性相有效利用率高，孔结构性质优良，对高硫劣质柴油具有较好的脱硫效果，该方法还可显著降低金属损失率和制备成本，使制备工艺更加高效化、绿色化。

Hydroconversion multi-metallic catalyst and method for making thereof

In a process for forming a bulk hydroprocessing catalyst by sulfiding a catalyst precursor made in a co-precipitation reaction, up to 60% of metal ions in at least one of the metal precursor feeds do not react to form catalyst precursor and end up in the supernatant as metal residuals. In the present disclosure, the metals can be recovered via ion-exchange, wherein an exchange resin is provided for a portion of the metal ions in the supernatant to be exchanged and bound onto the resin. The previously resin-bound metals can be subsequently recovered, or the effluent stream for the exchange resin column can also be recovered, forming at least a metal precursor feed which can be used in the co-precipitation reaction.

Hydroconversion multi-metallic catalyst and method for making thereof

In a process for forming a bulk hydroprocessing catalyst by sulfiding a catalyst precursor in a co-precipitation reaction, up to 60% of the metal precursor feeds do not react to form catalyst precursor and stay in the supernatant. In one embodiment, at least a precipitant is added to the product mixture at a molar ratio of precipitant to metal residuals in the supernatant ranging from 1.5:1 to 20:1 to precipitate at least 50 mole % of metal ions in the residuals forming additional catalyst precursor. The remaining metal residuals can be recovered via any of chemical precipitation, ion exchange, electro-coagulation, and combinations thereof to generate an effluent stream containing less than 50 mole % of at least one of the metal residuals. In one embodiment, at least one of the metal residuals is recovered and recycled for use as a metal precursor feed in the co-precipitation reaction.

Hydroconversion multi-metallic catalyst and method for making thereof

In a process for forming a bulk hydroprocessing catalyst by sulfiding a catalyst precursor made in a co-precipitation reaction, up to 60% of the metal precursor feeds do not react to form catalyst precursor and end up in the supernatant. In the present disclosure, the metals can be recovered via any of chemical precipitation, ion exchange, electro-coagulation, and combinations thereof to generate an effluent stream containing less than 50 mole % of metal ions in at least one of the metal residuals, and for at least one of the metal residuals is recovered as a metal precursor feed, which can be recycled for use in the co-precipitation reaction. An effluent stream from the process to waste treatment contains less than 50 ppm metal ions.

Hydroprocessing oil sands-derived, bitumen compositions

Disclosed are processes for producing deasphalted bitumen and heavy bitumen compositions from oil sands and processes for upgrading the bitumen compositions. The processes for producing the deasphalted bitumen and heavy bitumen compositions involve a Phase I and/or Phase II extraction solvent. According to the Phase I process, a high quality oil sands-derived, deasphalted bitumen can be produced using a Phase I type solvent. According to the Phase II process, a substantial amount of the heavy bitumen on the oil sand can be extracted using a Phase II type solvent, while producing a relatively a tailings by-product that is non-harmful to the environment. The heavy bitumen from the Phase II type extraction process can be hydroprocessed for ready conversion into relatively high volumes of high quality transportation fuels.

Preparation method of hydrofining catalyst

本发明公开了一种加氢精制催化剂的制备方法。该加氢精制催化剂是先将含Ni、W的混合溶液A与偏铝酸钠溶液并流进行成胶反应，其中在反应前和/或反应过程中加入表面活性剂，然后对所得浆液进行老化，再将含W、Mo、Al的混合溶液B、聚乙二醇与氨水并流加到上述老化后的浆液中进行成胶反应，再进行老化，然后经干燥、成型再洗涤、干燥、焙烧等步骤制成加氢精制催化剂。该催化剂可在柴油馏分超深度加氢脱硫、脱氮反应中应用，具有较高的加氢脱硫和加氢脱氮反应活性，特别是处理高氮高硫含量的柴油原料。

A method of upgrading heavy hydrocarbon streams to jet products

Catalyst preparation unit for use in processing of heavy hydrocarbons

A catalyst preparation unit for producing an activated hydrocarbon-catalyst mixture. The catalyst preparation unit includes one or more catalyst reactant input conduits; a hydrocarbon input conduit; a water input conduit; one or more catalyst reactant mixing and conveyance systems for receiving and mixing catalyst reactants from the catalyst component input conduits and water provided by the water input conduit to provide one or more catalyst reactant solutions; one or more hydrocarbon mixing and conveyance systems for receiving and mixing the catalyst reactant solutions and hydrocarbons provided by the hydrocarbon input conduit to produce a hydrocarbon-catalyst reactant mixture; at least one reactor located downstream of the mixers, for receiving and activating the hydrocarbon-catalyst reactant mixture, thereby producing the activated hydrocarbon catalyst mixture; a gas/liquid separator located downstream of the reactor, for removing vapors and gas from the activated hydrocarbon-catalyst mixture; and an output conduit for transporting the activated hydrocarbon-catalyst mixture away from the catalyst preparation unit.

Transition metal tungsten oxy-hydroxide

A hydroprocessing catalyst has been developed. The catalyst is a unique transition metal tungsten oxy-hydroxide material. The hydroprocessing using the transition metal tungsten oxy-hydroxide material may include hydrodenitrification, hydrodesulfurization, hydrodemetallation, hydrodesilication, hydrodearomatization, hydroisomerization, hydrotreating, hydrofining, and hydrocracking.

Crystalline transition metal tungstate

A hydroprocessing catalyst has been developed. The catalyst is a unique transition metal tungstate material. The hydroprocessing using the crystalline ammonia transition metal dimolybdotungstate material may include hydrodenitrification, hydrodesulfurization, hydrodemetallation, hydrodesilication, hydrodearomatization, hydroisomerization, hydrotreating, hydrofining, and hydrocracking.

Crystalline ammonia transition metal molybdotungstate

A hydroprocessing catalyst has been developed. The catalyst is a unique crystalline ammonia transition metal molybdotungstate material. The hydroprocessing using the crystalline ammonia transition metal molybdotungstate material may include hydrodenitrification, hydrodesulfurization, hydrodemetallation, hydrodesilication, hydrodearomatization, hydroisomerization, hydrotreating, hydrofining, and hydrocracking.

Crystalline transition metal molybdotungstate

A hydroprocessing catalyst has been developed. The catalyst is a unique transition metal tungstate material. The hydroprocessing using the crystalline transition metal molybdotungstate material may include hydrodenitrification, hydrodesulfurization, hydrodemetallation, hydrodesilication, hydrodearomatization, hydroisomerization, hydrotreating, hydrofining, and hydrocracking.

Crystalline transition metal oxy-hydroxide molybdotungstate

A hydroprocessing catalyst has been developed. The catalyst is a unique crystalline transition metal oxy-hydroxide molybdotungstate material. The hydroprocessing using the crystalline ammonia transition metal oxy-hydroxide molybdotungstate material may include hydrodenitrification, hydrodesulfurization, hydrodemetallation, hydrodesilication, hydrodearomatization, hydroisomerization, hydrotreating, hydrofining, and hydrocracking.

Mixed metal oxides

A unique mixed metal molybdotungstate material has been developed. The material may be used as a hydroprocessing catalyst. The hydroprocessing may include hydrodenitrification, hydrodesulfurization, hydrodemetallation, hydrodearomatization, hydrodesilication, hydroisomerization, hydrotreating, hydrofining, and hydrocracking.

Highly active trimetallic materials using short-chain alkyl quaternary ammonium compounds

A highly active trimetallic mixed transition metal oxide material has been developed. The material may be sulfided to generate metal sulfides which are used as a catalyst in a conversion process such as hydroprocessing. The hydroprocessing may include hydrodenitrification, hydrodesulfurization, hydrodemetallation, hydrodesilication, hydrodearomatization, hydroisomerization, hydrotreating, hydrofining, and hydrocracking.

Highly active quaternary metallic materials using short-chain alkyl quaternary ammonium compounds

A highly active quaternary mixed transition metal oxide material has been developed. The material may be sulfided to generate metal sulfides which are used as catalyst in a conversion process such as hydroprocessing. The hydroprocessing may include hydrodenitrification, hydrodesulfurization, hydrodemetallation, hydrodesilication, hydrodearomatization, hydroisomerization, hydrotreating, hydrofining, and hydrocracking.

Highly active quaternary metallic materials using short-chain alkyl quaternary ammonium compounds

A highly active quaternary mixed transition metal oxide material has been developed. The material may be sulfided to generate metal sulfides which are used as a catalyst in a conversion process such as hydroprocessing. The hydroprocessing may include hydrodenitrification, hydrodesulfurization, hydrodemetallation, hydrodesilication, hydrodearomatization, hydroisomerization, hydrotreating, hydrofining, and hydrocracking.

Crystalline oxy-hydroxide transition metal molybdotungstate

A unique crystalline transition metal molybdotungstate material has been developed. The material may be sulfided to generate metal sulfides which are used as a catalyst in a conversion process such as hydroprocessing. The hydroprocessing may include hydrodenitrification, hydrodesulfurization, hydrodemetallation, hydrodesilication, hydrodearomatization, hydroisomerization, hydrotreating, hydrofining, and hydrocracking.

Highly active trimetallic materials using short-chain alkyl quaternary ammonium compounds

A highly active trimetallic mixed transition metal oxide material has been developed. The material may be sulfided to generate metal sulfides which are used as a catalyst in a conversion process such as hydroprocessing. The hydroprocessing may include hydrodenitrification, hydrodesulfurization, hydrodemetallation, hydrodesilication, hydrodearomatization, hydroisomerization, hydrotreating, hydrofining, and hydrocracking.

Poorly crystalline transition metal molybdotungstate

A hydroprocessing catalyst or catalyst precursor has been developed. The catalyst is a poorly crystalline transition metal molybdotungstate material or a metal sulfide decomposition product thereof. The hydroprocessing using the crystalline ammonia transition metal molybdotungstate material may include hydrodenitrification, hydrodesulfurization, hydrodemetallation, hydrodesilication, hydrodearomatization, hydroisomerization, hydrotreating, hydrofining, and hydrocracking.

Nickel molybodtungstate hydrotreating catalysts (law444)

A hydrodenitrogenation catalyst is prepared by decomposing a nickel (ammonium) molybdotungstate precursor and sulfiding, either pre-use or in situ, the decomposition product.

Processing of heavy hydrocarbon feeds

Systems and methods are provided for hydroconversion of a heavy oil feed under slurry hydroprocessing conditions and/or solvent assisted hydroprocessing conditions. The systems and methods for slurry hydroconversion can include the use of a configuration that can allow for improved separation of catalyst particles from the slurry hydroprocessing effluent. In addition to allowing for improved catalyst recycle, an amount of fines in the slurry hydroconversion effluent can be reduced or minimized. This can facilitate further processing or handling of any "pitch" generated during the slurry hydroconversion. The systems and methods for solvent assisted hydroprocessing can include processing of a heavy oil feed in conjunction with a high solvency dispersive power crude.

Processing of heavy hydrocarbon feeds

Systems and methods are provided for hydroconversion of a heavy oil feed under slurry hydroprocessing conditions and/or solvent assisted hydroprocessing conditions. The systems and methods for slurry hydroconversion can include the use of a configuration that can allow for improved separation of catalyst particles from the slurry hydroprocessing effluent. In addition to allowing for improved catalyst recycle, an amount of fines in the slurry hydroconversion effluent can be reduced or minimized. This can facilitate further processing or handling of any “pitch” generated during the slurry hydroconversion. The systems and methods for solvent assisted hydroprocessing can include processing of a heavy oil feed in conjunction with a high solvency dispersive power crude.

Highly active trimetallic materials using short-circuit quaternary alkylammonium compounds

FIELD: chemistry.SUBSTANCE: invention relates to catalytically active materials. The material is a mixed oxide of transition metals having the formula (MIa)m(MIIb)n(MIIIc)oCeqHfrNgsOhtXiuSjvwhere MIis a metal or a mixture of metals selected from group VIII (groups 8, 9 and 10 according to IUPAC); MIIis a metal selected from group VIB (group 6 according to IUPAC); MIIIis a metal selected from Group VIB (IUPAC Group 6), which is different from MII; X is a halide (IUPAC group 17); a, b, c, e, f, g, h, i and j - valence state of MI, MII, MIII, C, H, N, O, X and S; m, n, o, q, r, s, t, u and v are the molar ratio of MI, MII, MIII, C, H, N, O, X and S. The material can be sulfided.EFFECT: catalyst with a higher intrinsic activity is provided.23 cl, 4 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 744 338 C1 (51) МПК B01J 23/85 (2006.01) B01J 27/047 (2006.01) B01J 27/08 (2006.01) B01J 27/24 (2006.01) B01J 37/03 (2006.01) B01J 37/20 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА C10G 45/08 (2006.01) ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ C10G 45/50 (2006.01) (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК B01J 23/002 (2020.08); B01J 23/85 (2020.08); B01J 37/03 (2020.08); B01J 37/04 (2020.08); B01J 37/20 (2020.08); C10G 45/08 (2020.08); C10G 45/50 (2020.08); C10G 49/04 (2020.08) (21)(22) Заявка: 2020121871, 18.12.2018 18.12.2018 Дата регистрации: Приоритет(ы): (30) Конвенционный приоритет: (56) Список документов, цитированных в отчете о поиске: US 2009/0054225 A1, 26.02.2009. CN 101306374 A, 19.11.2008. RU 2417124 C2, 27.04.2011. RU 2554941 C2, 10.07.2015. 20.12.2017 US 62/608,344 (45) Опубликовано: 05.03.2021 Бюл. № 7 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 02.07.2020 2 7 4 4 3 3 8 (73) Патентообладатель(и): ЮОП ЛЛК (US) 05.03.2021 R U (24) Дата начала отсчета срока действия патента: (72) Автор(ы): ПАНЬ, Вэй (US), КОСТЕР, Сьюзан К. (US), ОСМАН, Зара (US) (86) Заявка PCT: 2 7 4 4 3 3 8 R U C 1 C 1 US 2018/066221 (18.12.2018) (87) Публикация заявки PCT: WO 2019/126159 (27.06.2019) ...

Crystalline transition metal oxy-hydride molybdo tungstate

수소화처리 촉매가 개발되었다. 촉매는 독특한 결정성 전이 금속 옥시-히드록시드 몰리브도텅스테이트 물질이다. 결정성 암모니아 전이 금속 옥시-히드록시드 몰리브도텅스테이트 물질을 사용하는 수소화처리는 수소화탈질, 수소화탈황, 수소화탈금속, 수소화탈규산, 수소화탈방향족, 수소화이성화, 수소처리, 수소화정제, 및 수소화분해를 포함할 수 있다. Hydrotreating catalysts have been developed. The catalyst is a unique crystalline transition metal oxy-hydroxide molybdo tungstate material. Hydrogenation using crystalline ammonia transition metal oxy-hydride molybdo tungstate materials includes hydrodenitrification, hydrodesulfurization, hydrodemetallization, hydrodesilicate, hydrodearomatic, hydroisomerization, hydrotreatment, hydropurification, Hydrocracking.

A method of upgrading heavy hydrocarbon streams to jet products

A process of upgrading a heavy hydrocarbon feedstock comprising contacting a heavy hydrocarbon feedstock with a catalyst in the presence of hydrogen in a reactor system, containing the catalyst as the only catalyst, wherein the catalyst, is prepared by sulfiding a catalyst precursor obtained by mixing at reaction conditions, to form a precipitate or cogel, at least a Promoter metal compound in solution; at least a Group VIB metal compound in solution; and, at least an organic oxygen containing ligand in solution, and thereby producing a fuel product.

Bulk Catalyst Composition And A Process Preparing The Bulk Catalyst Composition

The invention relates to a bulk catalyst composition comprising metal oxidic particles comprising one or more Group VIII metals and two or more Group VIB metals, which bulk catalyst composition comprises first metal oxidic particles comprising one or more first Group VIII metals and one or more first Group VIB metals and separately prepared second metal oxidic particles comprising one or more second Group VIII metals and one or more second Group VIB metals, wherein the composition of Group VIB and Group VIII metals in the first and second metal oxidic particles are different, wherein the first and second oxidic bulk particles-are separately shaped to separate first and second shaped bulk catalyst particles, which are combined, preferably into a homogeneous blend, to form the bulk catalyst composition. The invention further relates to a process for the preparation of the bulk catalyst composition and to hydroprocessing a hydrocarbon feed using the bulk catalyst composition.

Process For The Preparation Of A Shaped Bulk Catalyst

The invention relates to a process for the preparation of a shaped bulk catalyst comprising metal oxide particles comprising one or more Group VIII metals and two or more Group VIB metals which process comprises the steps of providing first metal oxidic particles comprising one or more first Group VIII metals and one or more first Group VIB metals, providing separately prepared second metal oxidic particles comprising one or more second Group VIII metals and one or more second Group VIB metals, wherein the composition of Group VIB and Group VIII metals in the first and second metal oxidic particles are different, combining the first and second metal oxidic particles before and/or during shaping and shaping the combined first and second metal oxide particles to form a shaped bulk catalyst. The invention further relates to the shaped bulk catalyst obtainable with the process In sulphided or unsulphided form and the use thereof in hydroprocessing.

Crystalline transition metal oxy-hydroxide molybdotungstate

A hydrogenation catalyst and its application

본 발명은 캐리어 및 상기 캐리어 상에 담지된 Ni, Mo 및 W로 이루어진 금속 활성 성분, 및 F, P 또는 이들의 조합으로 이루어지는 군으로부터 선택되는 보조 활성 성분을 함유하는 수소첨가 촉매에 관한 것이다. 또 다른 수소첨가 촉매는, 분자체 성분을 가진 캐리어, 상기 캐리어 상에 담지된 Ni, Mo 및 W로 이루어진 금속 활성 성분을 포함한다. 상기 촉매는 탄화수소유의 수소첨가 방법에 사용될 수 있다. 상기 촉매는 종래의 촉매보다 높은 촉매 활성도를 가진다. The present invention relates to a hydrogenation catalyst containing a carrier and a metal active component consisting of Ni, Mo and W supported on the carrier, and an auxiliary active component selected from the group consisting of F, P or a combination thereof. Another hydrogenation catalyst comprises a carrier having a molecular sieve component, a metal active component consisting of Ni, Mo and W supported on the carrier. The catalyst can be used in a hydrogenation method of hydrocarbon oil. The catalyst has a higher catalytic activity than a conventional catalyst. 수소첨가 촉매, 탈황, 탈질소, 수소화 정제, 분자체, 제올라이트, 실리카-알루미나 Hydrogenated Catalyst, Desulfurization, Denitrogen, Hydrogenation Purification, Molecular Sieve, Zeolite, Silica-Alumina

Method of hydrocracking with suspended catalyst layer

FIELD: chemistry. SUBSTANCE: invention relates to a method of hydrocracking with suspended catalyst layer. Method comprises feeding one or more hydrocarbon compounds, having initial boiling point of at least 340 °C, and suspension catalyst in hydrocracking zone with a suspended catalyst layer. Suspended catalyst contains red mud, in which there is 1) from 40 to 50 wt% of iron; 2) from 3 to 14 wt% of aluminium; 3) not more than 10 wt% of sodium; 4) from 3 to 8 wt% of calcium. All values of percentage content of catalytic component relate to metal and are obtained per weight of dried suspension catalyst. EFFECT: proposed method simplifies process and reduces costs for raw materials due to use as catalyst of red mud with increased content of iron, minimises toluene-insoluble organic residues. 8 cl, 4 tbl, 1 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (51) МПК C10G 47/02 C10G 47/26 B01J 23/78 B01J 21/04 (11) (13) 2 606 117 C2 (2006.01) (2006.01) (2006.01) (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ФОРМУЛА (21)(22) Заявка: ИЗОБРЕТЕНИЯ К ПАТЕНТУ РОССИЙСКОЙ ФЕДЕРАЦИИ 2015118126, 12.09.2013 (24) Дата начала отсчета срока действия патента: 12.09.2013 Дата регистрации: (73) Патентообладатель(и): ЮОП ЛЛК (US) Приоритет(ы): (30) Конвенционный приоритет: R U 09.12.2016 (72) Автор(ы): БАУЕР Лоренц Дж. (US), БРИКЕР Маурин Л. (US), МЕЦЦА Бикей Дж. (US), БХАТТАЧАРИИЯ Алакананда (US) (56) Список документов, цитированных в отчете о поиске: US 4559129, 17.12.1985. US 6248302 15.10.2012 US 13/652,439 B1, 19.06.2001. SU 621312, 25.08.1978. (45) Опубликовано: 10.01.2017 Бюл. № 1 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 15.05.2015 (86) Заявка PCT: US 2013/059428 (12.09.2013) (87) Публикация заявки PCT: 2 6 0 6 1 1 7 (43) Дата публикации заявки: 10.12.2016 Бюл. № 34 2 6 0 6 1 1 7 R U C 2 C 2 WO 2014/062314 (24.04.2014) Адрес для переписки: 109012, Москва, ул. Ильинка, 5/2, ООО "Союзпатент" (54) СПОСОБ ГИДРОКРЕКИНГА СО ВЗВЕШЕННЫМ СЛОЕМ КАТАЛИЗАТОРА (57) ...

A kind of preparation method of active isomer phase hydrogenation catalyst

本发明为一种高效体相加氢催化剂的制备方法，该方法包括：将含Ni化合物、硅藻土、分散剂和去离子水混合形成高度分散体系，然后加入导向剂，使Ni源颗粒以高度分散状态均匀分布于硅藻土基体的孔道结构中，再依次加入含Mo化合物和含W化合物，与含Ni化合物结合形成高分散性Ni‑Mo和Ni‑W活性相，然后加入硅藻土，对体系中可溶性金属组分进行吸附，然后过滤浆液得到滤饼；将滤饼适当烘干后挤条、干燥、焙烧得到催化剂。本发明方法制备的催化剂活性相晶粒尺寸小、分布均匀、分散性好，活性相有效利用率高，孔结构性质优良，对高硫劣质柴油具有较好的脱硫效果，该方法还可显著降低金属损失率和制备成本，使制备工艺更加高效化、绿色化。

Preparation method and application of cracking catalyst

本发明涉及一种裂化催化剂的制备方法，所述制备方法包括以水热反应和浸渍、醇洗、干燥、焙烧等步骤，制备出硼改性的纳米氧化物催化剂，可用于悬浮床裂化催化剂的生产和加工中。该发明至少由如下原料得到：去离子水，氧氯化锆或硝酸氧锆，硫酸铝或硝酸铝，钛酸四丁酯或其它含钛酯，硼酸或硼砂，无水乙醇或丁醇，分散剂，交联剂，尿素，氨水，柠檬酸，本发明通过硼对氧化物的改性，可以调控氧化物表面的酸强度、酸类型、酸位点的数量，增强其裂化能力，同时具备粒径小，比表面积大等特点，可有效解决在悬浮床加氢裂化过程中，主要依赖高温裂化，催化剂分散性差，传统催化剂不适用，而导致的裂化能力差，反应条件苛刻和催化剂添加量高等问题。

A bulk catalyst composition and a process preparing the bulk catalyst composition

본 발명은 하나 이상의 VIII 족 금속 및 둘 이상의 VIB 족 금속을 포함하는 금속 산화 입자를 포함하는 벌크 촉매 조성물에 관한 것으로서, 상기 벌크 촉매 조성물은 하나 이상의 제 1 VIII 족 금속 및 하나 이상의 제 1 VIB 족 금속을 포함하는 제 1 금속 산화 입자 및 하나 이상의 제 2 VIII 족 금속 및 하나 이상의 제 2 VIB 족 금속을 포함하는, 별도로 제조된 제 2 금속 산화 입자를 포함하고, 여기서 상기 제 1 및 제 2 금속 산화 입자 내의 VIB 족 및 VIII 족 금속의 조성이 상이하고, 제 1 및 제 2 산화 벌크 입자는 별도로 성형되어 제 1 및 제 2 성형 벌크 촉매 입자로 분리되고, 바람직하게는 균질한 블렌딩으로 배합되어 벌크 촉매 조성물을 형성한다. 본 발명은 또한, 상기 벌크 촉매 조성물의 제조 방법 및 상기 벌크 촉매 조성물을 사용한 탄화수소 공급물의 수소가공에 관한 것이다. The present invention relates to a bulk catalyst composition comprising metal oxide particles comprising at least one Group VIII metal and at least two Group VIB metals, wherein the bulk catalyst composition comprises at least one Group VIII metal and at least one Group VIB metal. A first metal oxide particle comprising a first metal oxide particle and a second metal oxide particle separately prepared, comprising at least one second Group VIII metal and at least one second Group VIB metal, wherein the first and second metal oxide particles The composition of Group VIB and Group VIII metals in the interior is different, and the first and second oxidized bulk particles are molded separately and separated into first and second shaped bulk catalyst particles, preferably blended in a homogeneous blend to provide bulk catalyst composition. To form. The invention also relates to a process for preparing the bulk catalyst composition and to hydrogenation of a hydrocarbon feed using the bulk catalyst composition. 벌크 촉매 조성물, 금속 산화 입자, 수소가공 Bulk catalyst composition, metal oxide particles, hydrogen processing

PROCESS FOR CONVERTING HEAVY OIL RESIDUES INTO HYDROGEN AND GASEOUS AND DISTILLABLE HYDROCARBONS

Catalyst suitable for production of aviation kerosene from synthetic fischer-tropsch oil from biomass, and process for preparation thereof

FIELD: chemistry. SUBSTANCE: invention relates to a catalyst suitable for the production of aviation kerosene from synthetic Fischer-Tropsch oil from biomass, and a process for its preparation. Claimed catalyst comprises: 20 to 50 weight percent amorphous aluminium silicate; from 5 to 20 weight percent of aluminium oxide as binder; from 20 to 60 weight percent of hydrothermally modified zeolite; from 0.5 to 1.0 weight percent of sesbania powder; from 0.5 to 5 weight percent nickel oxide and from 5 to 15 weight percent molybdenum oxide, wherein the hydrothermally modified zeolite is hydrogen-type steam-modified dealuminated ZSM-22 zeolite. EFFECT: technical result consists in the preparation of a catalyst with high activity and high selectivity, an increase in the degree of isomerisation of long-chain alkanes, a decrease in the freezing point of aviation kerosene fractions, and an increase in the yield of aviation kerosene. 23 cl, 3 tbl, 8 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (51) МПК B01J 29/48 B01J 37/02 C10G 49/04 C10G 49/08 (11) (13) 2 656 598 C1 (2006.01) (2006.01) (2006.01) (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК B01J 29/48 (2006.01); B01J 29/7884 (2006.01); B01J 37/02 (2006.01); B01J 37/0201 (2006.01); C10G 49/04 (2006.01); C10G 49/08 (2006.01) (21)(22) Заявка: 2016148862, 06.02.2015 06.02.2015 Дата регистрации: Приоритет(ы): (30) Конвенционный приоритет: 14.05.2014 CN 201410201892.1 (56) Список документов, цитированных в отчете о поиске: CN 1184843 A, 17.06.1998. CN (45) Опубликовано: 06.06.2018 Бюл. № 16 102295955 A, 28.12.2011. CN 1884446 A, 27.12.2006. US 4696732 A1, 29.09.1987. US 8679323 B2, 25.03.2014. RU 2501736 C2, 20.12.2013. (85) Дата начала рассмотрения заявки PCT на национальной фазе: 14.12.2016 (86) Заявка PCT: 2 6 5 6 5 9 8 (73) Патентообладатель(и): УХАНЬ КАЙДИ ИНДЖИНИРИНГ ТЕКНОЛОДЖИ РИСЕРЧ ИНСТИТЬЮТ КО., ЛТД. (CN) 06.06.2018 R U (24) Дата начала отсчета срока действия патента: (72) ...

Manufacturing method of environmentally low load type fuel and environmentally low load type fuel

A process for producing an environmentally friendly fuel which comprises a hydrocracking step in which a feedstock oil comprising a fat ingredient derived from an animal/vegetable fat and optionally having undergone a given pretreatment step is brought into contact in the presence of hydrogen with a hydrocracking catalyst comprising at least one metal selected from the group consisting of metals belonging to Groups 6A and 8 of the Periodic Table and an inorganic oxide having an acid nature, wherein the fat ingredient comprises a fraction having boiling points of 230°C and higher.

PRODUCTION OF HIGH PERFORMANCE VAPOCRABAGE FILLERS IN ETHYLENE, PROPYLENE AND POLYMERS RESULTING FROM VEGETABLE OIL HYDROTREATMENT

The invention describes a process for treatment of a feedstock that is obtained from a renewable source that comprises a hydrotreatment stage in the presence of at least one fixed-bed catalyst, whereby said catalyst comprises a hydro-dehydrogenating function and an amorphous substrate, at a temperature of between 50 and 450° C., at a pressure of between 1 MPa and 10 MPa, at an hourly volumetric flow rate of between 0.1 h−1 and 10 h−1, and in the presence of a total quantity of hydrogen that is mixed with the feedstock such that the hydrogen/feedstock ratio is between 50 and 1000 Nm3 of hydrogen/m3 of feedstock, followed by a separation from the hydrotreated effluent that is obtained from stage a) of hydrogen, gases, and at least one liquid hydrocarbon effluent that consists of at least 50% linear n-paraffins, and a steam-cracking of at least one portion of the liquid hydrocarbon effluent that is obtained from stage b).

PRODUCTION OF HIGH PERFORMANCE VAPOCRABAGE FILLERS IN ETHYLENE, PROPYLENE AND POLYMERS RESULTING FROM VEGETABLE OIL HYDROTREATMENT

L'invention décrit un procédé de traitement d'une charge issue d'une source renouvelable comprenant une étape d'hydrotraitement en présence d'au moins un catalyseur en lit fixe, ledit catalyseur comprenant une fonction hydro-déshydrogénante et un support amorphe, à une température comprise entre 50 et 450 degres C, à une pression comprise entre 1 MPa et 10 MPa, à une vitesse spatiale horaire comprise entre 0,1 h-1 et 10 h-1 et en présence d'une quantité totale d'hydrogène mélangée à la charge telle que le ratio hydrogène/charge soit compris entre 50 et 1000 Nm3 d'hydrogène/m3 de charge, suivie d'une séparation à partir de l'effluent hydrotraité issu de l'étape a) de l'hydrogène, des gaz et d'au moins un effluent liquide hydrocarboné constitué d'au moins 50 % de n-paraffines linéaires, et d'un vapocraquage d'au moins une partie de l'effluent liquide hydrocarboné issu de l'étape b). The invention describes a method of treating a feedstock from a renewable source comprising a hydrotreatment step in the presence of at least one fixed bed catalyst, said catalyst comprising a hydro-dehydrogenating function and an amorphous support, at a temperature of between 50 and 450 degrees C, at a pressure of between 1 MPa and 10 MPa, at a space velocity ranging between 0.1 h -1 and 10 h -1 and in the presence of a total amount of hydrogen mixed with the feedstock such that the hydrogen / feedstock ratio is between 50 and 1000 Nm 3 of hydrogen / m 3 of feedstock, followed by separation from the hydrotreated effluent from step a) of hydrogen, gases and at least one hydrocarbon liquid effluent consisting of at least 50% of linear n-paraffins, and steam-cracking of at least a portion of the hydrocarbon liquid effluent from step b).

Hydroprocessing oil sands-derived, bitumen compositions

Disclosed are processes for producing deasphaited bitumen and heavy bitumen compositions from oil sands and processes for upgrading the bitumen compositions. The processes for producing the deasphaited bitumen and heavy bitumen compositions involve a Phase I and/or Phase II extraction solvent. According to the Phase I process, a high quality oil sands-derived, deasphaited bitumen can be produced using a Phase I type solvent. According to the Phase II process, a substantial amount of the heavy bitumen on the oil sand can be extracted using a Phase II type solvent, while producing a relatively a tailings by-product that is non-harmful to the environment. Tire heavy bitumen from tire Phase II type extraction process can be hydroprocessed for ready conversion into relatively high volumes of high quality transportation fuels.

Production of stable olefinic Fischer-Tropsch fuel with minimal hydrogen consumption

OPTIMIZED BIOMASS CONVERSION PROCESS FOR THE PRODUCTION OF PETROCHEMICAL BASES

La présente invention concerne un procédé de production de bases pétrochimiques, en particulier en composés oléfiniques et aromatiques, à partir d'une charge liquide comprenant au moins une bio-huile , ladite charge étant introduite dans au moins une étape d'hydroreformage en présence d'hydrogène et d'un catalyseur d'hydroreformage comprenant au moins un métal de transition choisi parmi les éléments des groupes 3 à 12 de la classification périodique et au moins un support choisi parmi les charbons actifs, les carbures de silicium, les silices, les alumines de transition, les silices alumine, l'oxyde de zirconium, l'oxyde de cérium, l'oxyde de titane et les aluminates de métaux de transition, pris seul ou en mélange, pour obtenir au moins un effluent liquide comprenant au moins une phase aqueuse et au moins une phase organique, une étape d'hydrotraitement d'au moins une partie de la phase organique de l'effluent issu de la première étape d'hydroreformage, une troisième étape d'hydrocraquage d'au moins une partie de l'effluent issu de la deuxième étape d'hydrotraitement, dans laquelle au moins une partie de la fraction bouillant à une température supérieure à 160°C séparée à l'issue de ladite troisième étape d'hydrocraquage est recyclée dans ladite troisième étape d'hydrocraquage, une séparation de l'effluent obtenu à l'issue de la troisième étape d'hydrocraquage en au moins une fraction contenant du naphta et une fraction bouillant à une température supérieure à 160°C, une quatrième étape de vapocraquage de la fraction contenant du naphta issue de la séparation permettant d'obtenir de l'hydrogène, des composés oléfiniques ayant un nombre d'atome de carbone compris entre 2 et 6 et des composés aromatiques. The present invention relates to a process for producing petrochemical bases, in particular olefinic and aromatic compounds, from a liquid feedstock comprising at ...

Catalyst suitable for production of aviation kerosene from biomass fischer-tropsch synthesis oil and preparation method therefor

Disclosed are a catalyst suitable for production of aviation kerosene from biomass Fischer-Tropsch synthesis oil and a preparation method therefor. Various components by weight in percentage in the catalyst are: 20-50% of an amorphous aluminium-silicon, 5-20% of an aluminium oxide binder, 20-60% of a hydrothermally modified ZSM-22 molecular sieve, 0.5-5% of nickel oxide, and 5-15% of molybdenum oxide. The preparation method is as follows: firstly performing an NH 4 + exchange treatment on the K-ZSM-22 molecular sieve to obtain an H-ZSM-22 molecular sieve, then performing a hydrothermal treatment to obtain a modified H-ZSM-22 molecular sieve, and then after uniform mixing with the amorphous aluminium-silicon, adding the aluminium oxide binder and a sesbania powder, mixing and kneading same, grinding into clusters, forming same by band extrusion, then drying and calcinating same, and finally loading active metals Ni and Mo. The catalyst obtained from the present invention has a high activity and a high selectivity, increases the isomerization degree of long-chain alkanes, reduces the freezing points of the fractions of aviation kerosene, and improves the yield of the aviation kerosene.

Catalyst preparation unit for use in processing of heavy hydrocarbons

A catalyst preparation unit for producing an activated hydrocarbon-catalyst mixture. The catalyst preparation unit includes one or more catalyst reactant input conduits; a hydrocarbon input conduit; a water input conduit; one or more catalyst reactant mixing and conveyance systems for receiving and mixing catalyst reactants from the catalyst component input conduits and water provided by the water input conduit to provide one or more catalyst reactant solutions; one or more hydrocarbon mixing and conveyance systems for receiving and mixing the catalyst reactant solutions and hydrocarbons provided by the hydrocarbon input conduit to produce a hydrocarbon-catalyst reactant mixture; at least one reactor located downstream of the mixers, for receiving and activating the hydrocarbon-catalyst reactant mixture, thereby producing the activated hydrocarbon catalyst mixture; a gas/liquid separator located downstream of the reactor, for removing vapors and gas from the activated hydrocarbon-catalyst mixture; and an output conduit for transporting the activated hydrocarbon-catalyst mixture away from the catalyst preparation unit.

Production of base oils from petrolatum

Methods are provided for producing lubricant base oils from petrolatum. After solvent dewaxing of a brightstock raffmate to form a brightstock base oil, petrolatum is generated as a side product. The petrolatum can be hydroprocessed to form base oils in high yield. The base oils formed from hydroprocessing of petrolatum have an unexpected pour point relationship. For a typical lubricant oil feedstock, the pour point of the base oils generated from the feedstock increases with the viscosity of the base oil. By contrast, lubricant base oils formed from hydroprocessing of petrolatum have a relatively flat pour point relationship, and some of the higher viscosity base oils unexpectedly have lower pour points than lower viscosity base oils generated from the same petrolatum feed. The base oils from petrolatum are also unusual in yielding both high viscosity and high viscosity index and can be generated while maintaining a high yield.

Process for catalytic conversion of micro-residual carbon content of heavy hydrocarbon feedstock and low surface area catalyst for use in said process