КАТАЛИЗАТОРЫ

Изобретение относится к области катализа. Описаны способы приготовления предшественника катализатора, включающие на первой стадии приготовления пропитку частиц носителя для катализатора органическим соединением кобальта в пропиточной жидкости с образованием пропитанного промежуточного продукта, прокаливание пропитанного промежуточного продукта при температуре прокаливания не выше 400°C с получением прокаленного промежуточного продукта; и затем на второй стадии приготовления пропитку прокаленного промежуточного продукта первой стадии неорганической солью кобальта в пропиточной жидкости с образованием пропитанного носителя и прокаливание пропитанного носителя с получением предшественника катализатора, причем ни одну из неорганических солей кобальта, использованных на второй стадии приготовления, не используют на первой стадии приготовления. Описаны синтезы углеводородов в присутствии катализаторов, полученных описанным выше способом. Технический результат - увеличение активности катализатора ...

НИКЕЛЕВЫЙ КАТАЛИЗАТОР ГИДРИРОВАНИЯ АРЕНОВ

FIELD: chemistry. SUBSTANCE: invention relates to the hydrogenation catalyst containing nickel(II) connection and restorer, as the original compounds of nickel(II) use anhydrous bis (acetylacetonate) nickel(II) and as a reducing agent-diethylethoxyaluminium (AlEt 2 (OEt)) the next molar ratio of components: [Ni(acac) 2 ]:[AlEt 2 (OEt)]=1:(2÷10). EFFECT: development of nickel catalyst with high catalytic activity. 7 tbl, 36 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 625 452 C1 (51) МПК B01J 21/02 (2006.01) B01J 23/755 (2006.01) B01J 31/12 (2006.01) C07C 5/02 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ФОРМУЛА (21)(22) Заявка: ИЗОБРЕТЕНИЯ К ПАТЕНТУ РОССИЙСКОЙ ФЕДЕРАЦИИ 2016125480, 24.06.2016 (24) Дата начала отсчета срока действия патента: 24.06.2016 (72) Автор(ы): Шмидт Федор Карлович (RU), Титова Юлия Юрьевна (RU) 14.07.2017 Приоритет(ы): (22) Дата подачи заявки: 24.06.2016 Адрес для переписки: 664003, г. Иркутск, ул. Карла Маркса, 1, ФГБОУ ВО "ИГУ", патентный отдел 2411228 C1, 10.02.2011. US 5935897 A1, 10.08.1999. US 20110060169 A1, 10.03.2011. JP 09094462 A, 08.04.1997. R U 2 6 2 5 4 5 2 (57) Формула изобретения Катализатор гидрирования, содержащий соединение никеля(II) и восстановитель, отличающийся тем, что в качестве исходного соединения никеля(II) используют безводный бис(ацетилацетонат)никеля(II), а в качестве восстановителя диэтилэтоксиалюминий (AlEt2(OEt)) при следующем мольном соотношении компонентов: [Ni(acac)2]:[AlEt2(OEt)]=1:(2÷10). Стр.: 1 C 1 C 1 (54) НИКЕЛЕВЫЙ КАТАЛИЗАТОР ГИДРИРОВАНИЯ АРЕНОВ 2 6 2 5 4 5 2 (56) Список документов, цитированных в отчете о поиске: RU 2565673 C1, 20.10.2015. RU (45) Опубликовано: 14.07.2017 Бюл. № 20 R U (73) Патентообладатель(и): Федеральное государственное бюджетное образовательное учреждение высшего образования "Иркутский государственный университет" (ФГБОУ ВО "ИГУ") (RU) Дата регистрации:

СПОСОБ ПОЛУЧЕНИЯ ПОЛИГИДРО[60]ФУЛЛЕРЕНОВ

Изобретение относится к способу получения полигидро[60]фуллеренов формулы (I): характеризующемуся тем, что фуллерен С60 подвергают взаимодействию с треххлористым алюминием (AlCl3) в присутствии порошка Mg и катализатора цирконацендихлорида (Cp2ZrCl2), взятыми в мольном соотношении C60:AlCl3:Mg:Cp2ZrCl2=1:(95-105):(95-105):(0.15-0.25), предпочтительно 1:100:100:0.20, в атмосфере аргона в отсутствие света при комнатной температуре (20-21°С) и атмосферном давлении в среде толуола в течение 2-4 часов, с последующим гидролизом реакционной массы. Применение данного способа позволяет получать полигидро[60]фуллерены с общим выходом после гидролиза реакционной массы 80-94%. 1 табл.

Способ повышения стабильности кислородсодержащих компонентов моторного топлива и регулирования содержания в них кислорода

FIELD: fuel. SUBSTANCE: invention describes a method of controlling content of oxygen in high-octane component of motor fuel based on carbonyl compounds of general formula, where R 1 is H, or alkoxide -O-C n H 2n+1 , or a hydrocarbon radical of general formula -C n H 2n+1 ; R 2 is a hydrocarbon radical of general formula -C n H 2n+1 ; n is a number from 1 to 5 or mixture thereof, and controlling chemical stability of this component consists in that, carbonyl compounds of said general formula or mixture thereof in gaseous phase in excess hydrogen are passed over a layer of composite material, consisting of a mechanical mixture of a hydrogenation catalyst and a dehydration catalyst, at temperature of 100–400 °C and pressure of 1–100 atm. EFFECT: technical result consists in increasing activity, selectivity and stability of operation of catalysts for hydrogenation of branched ketones to corresponding branched alkanes, and/or alcohols and/or their mixtures. 8 cl, 1 tbl, 28 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 607 902 C1 (51) МПК C10G 69/04 (2006.01) C10L 1/00 (2006.01) C07C 45/00 (2006.01) C07C 5/02 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ФОРМУЛА (21)(22) Заявка: ИЗОБРЕТЕНИЯ К ПАТЕНТУ РОССИЙСКОЙ ФЕДЕРАЦИИ 2015145147, 20.10.2015 (24) Дата начала отсчета срока действия патента: 20.10.2015 Дата регистрации: Приоритет(ы): (22) Дата подачи заявки: 20.10.2015 (45) Опубликовано: 11.01.2017 Бюл. № 2 (73) Патентообладатель(и): Акционерное общество "Газпромнефть-Московский НПЗ" (АО "Газпромнефть-МНПЗ") (RU) 2375413 C2, 10.12.2009. US 7038096 B2, 02.05.2006. RU 2475472 C2, 20.02.2013. SG 11201502428 A1, 28.05.2015. RU 2068402 C1, 27.10.1996. 2 6 0 7 9 0 2 (57) Формула изобретения 1. Способ регулирования содержания кислорода в высокооктановом компоненте моторного топлива на основе карбонильных соединений общей формулы R U (54) Способ повышения стабильности кислородсодержащих компонентов моторного топлива и регулирования содержания в них кислорода ...

ВЫСОКОАКТИВНЫЙ КАТАЛИЗАТОР ИЗОМЕРИЗАЦИИ И СПОСОБ ИЗОМЕРИЗАЦИИ

Изобретение относится к катализатору и способу для селективного повышения качества парафинового сырья с целью получения обогащенного изопарафинами продукта в качестве компонента бензина. Описан катализатор, включающий носитель из сульфатированного оксида или гидроксида из металла группы IVB (IUPAC 4), первый компонент из, по меньшей мере, одного лантанидного элемента или иттриевого компонента, которым преимущественно является иттербий, и, по меньшей мере, один металл платиновой группы, которым преимущественно является платина, и огнеупорное оксидное связующее, на котором диспергирован, по меньшей мере, один металл платиновой группы. Описан способ приготовления указанного выше катализатора, включающий сульфатирование оксида или гидроксида из металла группы IVB, нанесение первого компонента, смешение сульфатированного носителя с огнеупорным неорганическим оксидным носителем, прокаливание, нанесение второго компонента и последующее прокаливание. Описан способ конверсии углеводородов путем ...

СПОСОБ ПОЛУЧЕНИЯ ЭТИЛЕНА ИЗ ПРИРОДНОГО ГАЗА

Изобретение относится к области химической технологии получения этилена. Сущность способа - пиролиз природного газа под действием водородной плазмы с получением ацетиленсодержащего пирогаза. Ацетилен без выделения из пирогаза гидрируют до этилена в присутствии катализатора в среде жидкого растворителя, температура кипения которого близка к оптимальной температуре гидрирования ацетилена в этилен, при этом предотвращается перегрев катализатора, а тепло конденсации паров растворителя используется для получения холода. Затем этилен выделяют из продуктов гидрирования низкотемпературной ректификацией. Образующийся в процессе пиролиза водородсодержащий газ возвращают на стадию пиролиза, а избыточное количество используют в качестве топливного газа на газотурбинной установке или товарного продукта. Образующиеся в незначительном количестве жидкие продукты гидрирования ацетилена также возвращают на стадию пиролиза в качестве вторичного сырья. Применение данного способа позволит достичь высокого выхода ...

Способ гидрирования алкиленароматических соединений

Изобретение относится к способу гидрирования алкиленароматических соединений с получением полностью гидрированных циклических углеводородов. Описан способ гидрирования алкиленароматических соединений, заключающийся в непрерывной подаче смеси алкиленароматического соединения и водорода при нагревании на катализатор, представляющий собой наночастицы никеля, нанесенные на оксид алюминия. Наночастицы никеля наносят путем пропитки оксида алюминия при кипячении до обесцвечивания раствором гексагидрата хлорида никеля и карбамида в 7 масс.% водном растворе аммиака, добавления борной кислоты и кипячения в течение 2 часов при массовом соотношении оксида алюминия : гексагидрата хлорида никеля : карбамида : борной кислоты, равном 1:2:2,4:0,6, и последующего восстановления адсорбированного хлорида никеля при температуре 80-100°С в течение 1 часа смесью 0,025 масс.% водного раствора боргидрида натрия и гидразин моногидрата, взятых в мольном соотношении 4:3, с осушкой катализатора в токе водорода при ...

Способ автоматического управления процессом гидрирования ацетиленовых соединений

Изобретение относится к области автоматизации процесса гидрирования и может быть использовано в химической лромывленности при автоматизации установок получения этилена и пропилена . Целью изобретения является снижение потерь этилена и протшлена. Система управления содержит датчик (Д) 2.расхода реакционной смеси в реактор , хроматограф (X) 3, измеряющий содержание ацетиленистых соединений и окиси.углерода в этан-этиленовой фракции, Д 6 расхода водородной фракции , X 7, измеряюпщй содержание водорода в водородной фракции, и X 19, измеряющий содержание ацетиленистых соединений после реактора, подключенные к функциональному блоку (ФВ) 10, который.формирует задание регулятору ...

Катализатор для ароматизации углеводородов

КАТАЛИЗАТОР ДЛЯ АРОМАТИЗАЦИЙ УГЛЕВОДОРОДОВ, сбдержащий платину, хром и окись aJooMHHHH, о т л н- чающийся тем, что, с целью пЬвышеяия активности катализатора, он дополнительно содержит бор при сле- яукщеы содер:Ьании компонентов, мас,%:Платина0,1-0,6Хром0,001-0,5Бор0,001-2,0S Окиси алюми-:ния 'Остальное ...

Способ получения олефинов

CRYSTALLINE GALLOSILICATES, A PROCESS FOR PRODUCING THEM AND THEIR USE AS CATALYSTS

Verfahren zur Herstellung eines fluessigen Gemisches aus unvollstaendig hydrierten Kohlenwasserstoffen

NICHT-LINEARES POLYMERISAT ALS KATALYSATORVORLAEUFER UND DEREN VERWENDUNG IN EINER KATALYSATORZUSAMMENSETZUNG

PRODUCTION OF FUEL GASES

... 1434018 Vapour phase hydrogenation BRITISH GAS CORP 10 July 1973 [16 Aug 1972] 38174/72 Heading C5E A continuous process for the vapour phase hydrogenation of a hydrocarbon oil comprises continuously introducing vaporized hydrocarbon oil and hydrogen-containing gas into a thermally insulated reaction chamber constructed to define an endless path along which gas can circulate within the chamber, exothermically reacting the oil vapour with hydrogen at 600‹ to 800‹ C. at at least 5 atmospheres pressure, continuously withdrawing and passing gaseous reaction products to a second reaction chamber which may also be constructed to define an endless path along which the gas can circulate within the chamber, wherein the gas is subjected to a further hydrogenation reaction at a controlled temperature of 650‹ to 900‹ C. Aromatic compounds, e.g. benzole, may be removed from the first stage gaseous reaction product and a low molecular weight hydrocarbon, e.g. propane, may be added to the gas prior to ...

PROCESS FOR SELF-HYDROGENATION

CATALYST FOR THE CONVERSION OF HYDROCARBONS AND ITS MANUFACTURE AND USE

... 1327738 Catalyst composition INSTITUT FRANCAIS DU PETROLE DES CARBURANTS ET LUBRIFIANTS 1 March 1972 [3 March 1971] 9590/72 Heading B1E [Also in Division C5] A catalyst composition comprises: (a) a carrier which is alumina, silica, alumina-silica or magnesia; (b) 0.005-1% wt. with respect to the carrier of each of platinum and iridium; and (c) 0.005-1% at with respect to the carrier of zinc or a zinc compound (calculated as zinc oxide). The Examples describe compositions of gamma alumina, platinum, iridium, a zinc compound, e.g. the sulphate and, optionally, fluorine or chlorine. In Example 1 the composition is calcined then reduced in a stream of hydrogen before use.

HYDROGENATION OF UNSATURATED HYDROCARBONS IN HYDROCARBON- CONTAINING GAS MIXTURES

1396084 Hydrogenating hydrocarbons LINDE AG 23 May 1973 [24 May 1972] 24544/73 Heading C5E Unsaturated hydrocarbons are catalytically hydrogenated to form more saturated hydrocarbons by a two-zone hydrogenation the first zone being isothermal and the second being adiabatic. The isothermal and adiabatic reaction zones may be in a common reactor tube containing catalyst, the isothermal section (the lower) being surrounded by a liquid coolant and the adiabatic section (the upper) being surrounded by a vapour coolant preferably constituted by coolant liquid evaporated during the isothermal reaction. Reactions mentioned are the hydrogenation of acetylene in the presence of ethylene and the hydrogenation of propyne in the presence of propane. Suitable coolants are methanol or C 4 hydrocarbons.

Hydrocarbon conversion process

Molecular sieves of uniform pore of size sufficiently large to absorb benzene and containing metals, or oxides thereof, in the inner absorption regions are used as catalysts and of the appropriate conditions and at elevated temperatures for the following reactions of hydrocarbons (1) hydrocracking, polymerization, alkylation, hydroforming, isomerization, or dehydrogenation, the metal being platinum, iron, cobalt or nickel, (2) hydrogenation, the metals being platinum, iron, cobalt or nickel, (3) hydrocracking, polymerization, hydroforming, hydrogenation or dehydrogenation, the metals being chromium, tungsten, molybdenum, vanadium, or rhenium, (4) hydrocracking, polymerization, hydrogenation or dehydrogenation, the metal being copper and (5) polymerization, the metal being aluminium. Examples relate to (a) dehydrogenation of a tetralin to a naphthalene, cyclohexane to benzene, methylcyclohexane to toluene, and butanes to butenes; (b) hydrogenation of propylene to propane; (c) alkylation ...

Process for the hydrogenation of organic compounds

Organic compounds are hydrogenated by contacting them with hydrogen in the presence of a catalyst comprising a cobalt complex of the formula HnCo(CO)z(ER3)x(R2ER1ER2)y in which x, y and z represent integers satisfying the equation x+2y+2=4, while x and z have values from 0 to 3 and y from 0 to 2; n is O or 1; E is a phosphorus or arsenic atom; R1 is a bivalent unsubstituted or halogen and/or alkoxy-substituted hydrocarbon group and each R represents a hydrogen atom or a univalent group corresponding to R1. The catalyst may be a mixture of such complexes in one of which n is O and in the other is 1. The compounds which may be hydrogenated may be, for example, unsaturated hydrocarbons which give more saturated hydrocains, saturated aldehydes and ketones which yield alcohols, unsaturated compounds such as cyanides to give saturated cyanides and unsaturated ketones which may give saturated ketones or saturated alcohols. In general temperatures between 50 DEG C. and 300 DEG C. are used. Examples ...

PROCESS FOR THE PRODUCTION OF SATURATED MONOCYCLIC MONOTERPENES

... 1318598 Saturated monocyclic terpenes CHEMISCHE WERKE HULS AG 19 Oct 1970 [20 Oct 1969] 49528/70 Heading C5E A saturated monocyclic terpene is prepared by hydrogenating an ether of a monocyclic terpene at superatmospheric pressure and elevated temperature in the presence of a catalyst which in the unreduced condition contains: 10-60 wt. per cent Ni, 10-87À3 wt. per cent calcined Al 2 O 3 , 0-40 wt. per cent ZnO and 0-5 wt. per cent SiO 2 . Preferably the feedstock is eucalyptol, which may also contain unsaturated monocyclic terpenes such as limonenes, dipentene, -terpininene, and terpinols; the product being p-menthane. Up to 80 wt. per cent of a conventional nickel impregnation catalyst may be employed with the Ni-Al 2 O 3 catalyst. The reaction may be effected at 100-300‹ C. and 50-350 atmos. gauge.

HYDROGENATION OF UNSATURATED COMPOUNDS

1380026 Hydrogenating hydrocarbons INSTITUT FRANCAIS DU PETROLE 28 Feb 1973 [3 March 1972] 9822/73 Heading C5E Unsaturated hydrocarbons are hydrogenated by contact in liquid phase containing dissolved catalyst with gaseous H 2 under conditions such that the 50-99% of the hydrogenated product is vaporized, the remaining liquid fraction being contacted with an adsorbent to remove catalyst therefrom, and the gaseous fraction being condensed. The treated liquid product may either be added to the condensed gaseous product or recycled to the reactor. The homogenous catalyst may be a salt of a transition metal reduced with an organoaluminium compound, an organolithium compound or, a hydride of Al and Li or Na or derivative thereof. The feed may be a C 2 -C 20 cyclic or acyclic unsaturated hydrocarbon and the hydrogenation may be complete or partial. The hydrogenation may be carried out at 25-200‹ C., under a H 2 partial pressure of 0À5-20 atmospheres and in a heavy solvent (e.g. cetane). The adsorbent may be Al 2 O 3 bauxite, SiO 2 , kieselguhr, bleaching clay, active carbon or fly ash. Examples describe the hydrogenation of propylene to propane and an unsaturated C 4 cut to a mixture of butane and butenes using in each case Ni stearate/AlEt 3 as catalyst and Al 2 O 3 as adsorbent.

PROCESS

ORGANOMETALLIC COMPLEXES AND CHEMICAL PROCESS USING SAME

... 1,217,417. Organometallic complexes. NATIONAL DISTILLERS & CHEMICAL CORP. 5 July, 1968 [14 July, 1967; 17 July, 1967], No. 32314/68. Headings C2C and C2J. [Also in Division C5E] The invention comprises organometallic complexes of the formula where n is zero or an integer from 1 to 4; each R is selected from lower alkyl (C 1 -C 4 ) group, aryl group having from 6 to 16 carbon atoms, hydroxy group, nitro group, halide, dialkyl. amino, diarylamino and alkarylamino groups having 2 to 12 carbon atoms, or alkoxy or aryloxy group having 1 to 6 carbon atoms; M is Ru, Pt, Os, Pd, Ir, or Rh; Y is chloride bromide, nitrate, acetate, thiocyanate or cyanide group; A is -CR1 =N- (where R1 is hydrogen or an alkyl or aryl group having 1 to 10 carbon atoms), and Z is an alkyl group having 1 to 10 carbon atoms, aryl group or alkaryl, an alkoxy or aryloxy group having 1 to 10 carbon atoms, a hydroxy group, or an alkylamino, dialkylamino, arylamino or diarylamino group having 1 to 12 carbon ...

PROCESS FOR PREPARING A CRYSTALLINE ALUMINOSILICATE HYDROCONVERSION CATALYST

... 1452521 Hydroconversion catalyst SHELL INTERNATIONALE RESEARCH MAATSCHAPPIJ BV 17 Oct 1973 [19 Oct 1972 (3)] 48473/73 Heading B1E [Also in Division C5] A hydroconversion catalyst is formed by physically mixing 10-90% wt of a zeolite having a channel pore structure, e.g. zeolite L or zeolite omega, with 90-10% wt of a zeolite having a three-dimensional pore structure, e.g. natural faujasite or zeolites X or Y, neither of the zeolites having an apparent pore size substantially below 8A‹, decationising if necessary either before or after mixing to an alkali metal and/or alkaline earth metal content of less than 0.5% wt and then incorporating a hydrogenative metal into the zeolites, drying and calcining. The hydrogenative metal component may be a group VIII and/or Gp VIB metal i,.e. platinum and/or palladium or nickel and tungsten. The catalyst may be sulphided before use.

Binuclear rhodium complex and hydroformylation and hydrogenation processes

The present invention relates to hydrogenation and hydroformylation catalysts based on a binuclear rhodium complex having the formula: wherein X and X' can be the same or different; when X and X' are the same they are organic tertiary phosphite groups and when different X is a CO group and X' is an organic tertiary phosphite group or an aromatic phosphine group, and SY and SY' are thiolato groups. The invention also comprises the processes of hydroformylation and hydrogenation using such catalytic complex.

Hydrogenation process

Hydrocarbon feedstocks containing C2, C3 or C4 unsaturated hydrocarbons and having a major molar proportion in relation to the total C2, C3 and C4 unsaturates of mono-olefines and a minor molar proportion of unsaturated hydrocarbons with a higher degree of unsaturation than mono-olefines, i.e. olefines containing more than one double bond and acetylenes, are hydrogenated over a supported nickel-containing catalyst, which, under the operating conditions, is present in major proportion as elemental nickel, said catalyst having previously been modified by treatment with a sulphur compound which is a thiophene or a thiocycloalkane having at least 4 carbon atoms per ring or a dialkyl monosulphide, so that the nickel in the catalyst is thereby combined with 1-40 mol per cent of sulphur, the hydrogenation being effected at 50-250 DEG C. at a space velocity of 100-10,000 v./v./hr. so that at least a proportion of the unsaturates with a higher degree of unsaturation are selectively hydrogenated ...

Process for the preparation of fischer-tropsch catalysts and their use.

Process for the preparation of fischer-tropsch catalysts and their use

Method for the preparation of hydrogenated hydrocarbons.

Process for the preparation of fischer-tropsch catalysts and their use.

Process for the preparation of fischer-tropsch catalysts and their use.

PROCEDURE FOR THE REDUCTION OF A REFINING CATALYST BEFORE ITS APPLICATION.

HYDROGENATION PROCEDURE.

PROCEDURE AND INTERMEDIATE CONNECTIONS FUER n (S-3ALKYL-HEPTANOYL) - D-GAMMA-GLUTAMYL-GLYCyl-DALANINE ONES.

USE OF 1,3-DIALKYL-CYCLOHEXANVERBINDUNGEN AS COSMETIC OEL COMPONENT.

PROCEDURE FOR the TRANSFORMATION OF 1,2-DICHLORPROPAN IN PROPYLENE

TITANIUM-ALUMINUM-SILICON-OXIDE MOLECULAR SIEVE COMPOSITIONS

Layered catalyst composition and processes for preparing and using the composition

Process for converting perchloroethylene to trichloroethylene

Processes for converting chlorinated alkane byproducts or waste products to useful, less chlorinated alkenes

TRANSITION METAL CATALYST COMPOSITIONS AND THEIR PRECURSORS

TITANIUM-ALUMINUM-SILICON-OXIDE MOLECULAR SIEVE COMPOSITIONS

CRYSTALLINE GALLOPHOSPHATE COMPOSITIONS

HIGH-ACTIVITY ISOMERIZATION CATALYST AND PROCESS

SHELL CATALYSTS, METHOD FOR PRODUCING THE SAME, AND THE USE THEREOF

The invention relates to a shell catalyst with a core and at least one shell surrounding the core, said core being composed of an inert carrier material, and the at least one shell being composed of a porous carrier substance. The shell is physically adhered to the core and the at least one shell contains a catalytically active metal selected from the group of metals of the 10th and 11th group of the periodic table of elements in a finely divided form, or a precursor of the catalytically active metal in a uniformly divided form. The inventive shell catalyst is suitable for reducing unsaturated hydrocarbons and allows for better selectivities in comparison with shell catalysts known so far. The invention further relates to a method for producing the inventive shell catalyst.

CRYSTALLINE FERROALUMINOPHOSPHATES

CRYSTALLINE FERROALUMINOPHOSPHATES Novel class of crystalline microporous ferroaluminophosphate compositions containing as lattice constituents in addition to AlO2 and PO2 structural units, ferric and/or ferrous iron in tetrahedral coordination with oxygen atoms. These compositions are prepared hydrothermally using organic templating agents and are suitably employed as catalysts or adsorbents.

MOLECULAR SIEVE COMPOSITIONS

MOLECULAR SIEVE COMPOSITIONS Crystalline molecular sieves having threedimensional microporous framework structure of MO2, AlO2, and PO2 tetrahedral oxide units are disclosed. These molecular sieves have an empirical chemical composition on an anhydrous basis expressed by the formula: mR : (MxAlyPz)O2 wherein "R" represents at least one organic templating agent present in the intracrystalline pore system; "m" represents the molar amount of "R" present per mole of (MxAlyPz)O2; "M" represents at least one element capable of forming framework tetrahedral oxides and selected from the group consisting of arsenic, beryllium, boron, chromium, gallium, germanium, lithium and vanadium; and "x", "y" and "z" represent the mole fractions of "M", aluminum and phosphorus, respectively, present as tetrahedral oxides. Their use as adsorbents, catalysts, etc. is disclosed.

MOLECULAR SIEVE COMPOSITIONS

MOLECULAR SIEVE COMPOSITIONS Crystalline molecular sieves having three-dimensional microporous framework structures of MO?, AlO2, and PO2 tetrahedral oxide units are disclosed. These molecular sieves have an empirical chemical composition on an anhydrous basis expressed by the formula: mR : (MxAlyPz)O2 wherein "R" represents at least one organic templating agent present in the intracrystalline pore system; "M" represents iron and/or titanium, and at least one of cobalt, magnesium, manganese and zinc: "n" is 0. -1 or -2; "m" represents the molar amount of "R" present per mole of (MxAlyPz)O2; and "x", "y" and "z" represent the mole fractions of "M", aluminum and phosphorus, respectively, present as tetrahedral oxides. Their use as adsorbents, catalysts, etc. is also disclosed.

HYDROGENATION OF OLEFINS

A catalytic process for hydrogenation of unsaturated organic compounds is carried out in a two-phase aqueous/organic medium, in which the catalytic complex is dissolved in the aqueous phase and to which is added an amphiphilic reagent to facilitate phase boundary crossing of dissolved species. Catalyst separation from reaction products is thereby rendered more efficient. The catalytic complex is preferably formed in situ and contains a water-soluble phosphine ligand, preferably a hydroxy- or carboxy-aryl phosphine.

PROCESS FOR THE SELECTIVE HYDROGENATION OF POLYUNSATURATED HYDROCARBONS IN HYDROCARBON MIXTURES

The invention describes a novel process for the hydrogenation of hydrocarbons, with three and more carbon atoms and several double bonds or with triple bonds in monoene-containing hydrocarbon mixtures. These compounds are selectively hyarogenated to monoenes in a practically quantitative fashion. Before beginning the hydrogenation, a small amount of carbon monoxide and once to twice the stoichiometric quantity of hydrogen are homogeneously dissolved in the hydrocarbon mixture. The mixture is hydrogenated as a homogeneous liquid phase on a fixed palladium catalyst under a moderately high pressure and at a moderately high temperature. No isomerization can be found in the monoenes and no side reactions or secondary reactions occur.

CRYSTALLINE GALLOSILICATES, A PROCESS FOR PRODUCING THEM AND THEIR USE AS CATALYSTS

Crystalline gallosilicates, a process for producing them and their use as catalysts This invention reates to crystalline gallosilicates having the following composition in terms of the mole ratios of the oxides: 0.9 ? 0.25M2/nO : Ga2O3 : xSiO2 : yH2O.zQ wherein M is at least one cation having a valence n, x is at least 10, y/x is from 0 to 30, Q is a template used in the synthesis of the gallosilicate and z/x is 0-20, wherein the gallosilicate in the organic free hydrogen-form has an X-ray diffraction pattern substantially as set forth in Table A of this specification. The gallosilicates may be used, whether or not impregnated and/or ion-exchanged, admixed, supported or bound, for catalysing a reaction selected from alkylation, dealkylation, dehydrocyclodimerisation, aromatisation, transalkylation, isomerisation, dehydrogenation, hydrogenation, cracking, hydrocracking, cyclisation, oligomerisation, polymerisation, conversion of carbon monoxide/hydrogen mixtures to hydrocarbons and dehydration ...

LAYERED COMPLEX METAL SILICATE COMPOSITION, THEIR PREPARATION AND USE IN HYDROCARBON CONVERSION TIONS

PROCESS AND APPARATUS FOR HYDROGENATION

The present invention relates hydrogenation reactions of different fractions in oil refining. It also relates to the process device applicable thereto and use of said device for hydrogenation of various feedstocks, especially relating to arrangements during campaign changes.

CATALYSTS

A process for preparing a catalyst precursor includes, in a first preparation step, impregnating a particulate catalyst support with an organic metal compound in a carrier liquid. The metal of the organic metal compound is an active catalyst component. An impregnated intermediate is formed, and is calcined to obtain a calcined intermediate. Thereafter, in a second preparation step, the calcined intermediate from the first preparation step is impregnated with an inorganic metal salt in a carrier liquid. The metal of the inorganic metal salt is an active catalyst component. An impregnated support is obtained, and is calcined, to obtain the catalyst precursor. The metal is in particular cobalt. The precursor is reduced, in particular with hydrogen, to obtain the active catalyst. Also claimed is a process for the hydrogenation of CO, as well as a process for the hydrogenation of an organic compound using the so-prepared catalyst.

TRANSITION METAL CATALYSTS FOR HYDROGENATION AND HYDROSILYLATION

Phosphoranimide-metal catalysts and their role in hydrogenation and hydrosilylation are disclosed. The catalysts comprise first row transition metals such as nickel, cobalt or iron. The catalysts have a metal to anionic phosphoranimide ratio of 1:1. This disclosure presents a process for catalytic hydrogenation and hydrosilylation of a range of unsaturated organic compounds under lower temperature and pressure conditions than conditions associated with industrial hydrogenation and hydrosilylation.

PROCESS FOR SELECTIVE HYDROGENATION OF CRACKED HYDROCARBONS

The invention relates to a process to selectively hydrogenate di-olefinically, poly-olefinically, and acetylenically unsaturated hydrocarbon components a C2 to C5+ or a C3 to C5+ fraction of a cracked hydrocarbon stream. The process comprises removing from a deethanizer or depropanizer a heavy stream enriched in a C3 to C5+ or a C4 to C5+ fraction; reacting the heavy stream with hydrogen for selective hydrogenation; and returning at least a portion of the hydrogenated stream to the deethanizer or depropanizer. Embodiments are disclosed where the heavy stream is removed by a side draw or by means of the reboiler circuit. The invention is applicable to front-end demethanizer, deethanizer, or depropanizer fractional distillation process sequences such as may be used with steam cracking or catalytic cracking.

Verfahren zur Herstellung eines Katalysators, nach diesem Verfahren hergestellter Katalysator und Verwendung des nach dem Verfahren hergestellten Katalysators

Basen-Lösungsmittel-System

Catalyseur d'hydrogénation sélective et procédé de préparation dudit catalyseur

Catalyseur utilisable pour l'hydrogénation sélective d'hydrocarbures

Process for the preparation of organic complexes of transition metals

СПОСОБ ПОЛУЧЕНИЯ ПОЛИГИДРО[60]ФУЛЛЕРЕНОВ

Изобретение относится к области химии и может быть использовано в органическом синтезе производных фуллерена С60 и в водородной энергетике. Полигидро[60]фуллерены формулы (С60Н2n; n=11-17) получают в растворе толуола путем взаимодействия фуллерена С60 с борогидридом натрия в присутствии 18-краун-6 и железного купороса (FeSO4 × 7H2O). Изобретение обеспечивает увеличение выхода продукта до 93-97 % и упрощение процесса.

Способ получения гидрогенизированных углеводородов

Изобретение относится к способам превращения природного газа в высшие гидрогенизированные углеводороды. Способ включает предварительную обработку природного газа на катализаторе при высокой температуре и последующую гидрогенизацию полученной смеси циклических и/или ароматических углеводородов. Предложенный способ полезен для конверсии природного газа, особенно в случае нефтяных месторождений с попутным газом или газовых месторождений вблизи нефтяных месторождений, для сбора, отделения и транспортировки продукта.

СПОСОБ ПОЛУЧЕНИЯ КОБАЛЬТОВЫХ КАТАЛИЗАТОРОВ НА НОСИТЕЛЕ ИЗ ДИОКСИДА ТИТАНА

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

ПОЛИВАЛЕНТНЫЙ БИФУНКЦИОНАЛЬНЫЙ КАТАЛИЗАТОР И ЕГО ПРИМЕНЕНИЕ

... 1. Поливалентный бифункциональный катализатор, состоящий из оксида металла или смеси оксидов металлов MO2, где M выбирают из группы, состоящей из молибдена и вольфрама, при этом указанный оксид или смесь оксидов наносят на TiO2носитель, отличающийся тем, что как металлический, так и кислотный характер катализатору придает MO2фаза, получаемая на месте восстановлением соответствующего MO3 оксида, который осаждают в виде атомных слоев, в количестве от 1 до 8, предпочтительно равном 5, на указанном TiO2 носителе, процесс восстановления осуществляют при температуре от 380 до 550°C, в частности при температуре около 400°C в случае чистого MoO2и при температуре около 510°C в случае чистого WO2 , в газообразном потоке, содержащем, по меньшей мере, водород, при этом процесс восстановления не влияет на указанное число слоев. 2. Катализатор по п.1, отличающийся тем, что оксид металла MO3 , который восстанавливают до MO2, осаждают на носителе TiO2, который в свою очередь осажден на субстрате, имеющем ...

CATALYSTS, CONTAINING METALS ON MATERIALS CARRIER BASED ON HYDRO TALTsITA, AND METHOD FOR THEIR PRODUCTION

Combined technological and comprehensive utilizing method in C5 prodn. splitting process

This invention relates to a combined technology for cracking C5 fraction to produce methyl tert-amyl ether (TAME) by utilizing ethylene and use it for rich n-pentane-contained parafins of ethylene-cracked raw material. It features that decyclized pentadiene, selective hydrogenation, etherization reaction and saturated hydrogenation technique are organicly combined to decrease hydrogen consumptionto the maximum extent, and an ideal harmonious ingredient without lead and containing oxygen and high octane number gasoline-TAME is obtained. Catalstic-distilled etherization reaction is used, tert-amy ethylene reaches deep transformation; the saturated-hydrogenated C5 paraffins contain rich n-pentane used as ethylene-cracked raw material or gasoline ingredient; crude cyclic tert-amyl diene can be produced in combination, and after further refining, it can be used as raw material for fine chemical industry.

Benzene class solvent production purification device

High unsaturated hydrocarbon selective hydrogenation method in cracking gas

The invention discloses a method for selective hydrogenation of highly unsaturated hydrocarbons in cracked gas. The invention belongs to the technical field of the selective hydrogenation of unsaturated hydrocarbons. In order to solve the problems of the prior art that liquid phase flow in a mixed phase hydrogenation reaction chamber contains a large amount of C3, C4, C5 components and can not fully play a role in flushing the reaction chamber; in addition, the liquid phase flow repeatedly enters a front depropanization tower so as to bring about high energy consumption, large device dimensions, high operating cost and adverse effects on the improvement of C3 selectivity, the invention provides the method which comprises the following steps: carrying out the selective hydrogenation of C2 to C10 highly unsaturated hydrocarbons (acetylene hydrocarbons and diolefin) at the upstream of the front depropanization tower of an olefin production device first, then removing the C5 component, and ...

Method for removing poisonous, hazardous, polychlorine biphenyl compounds

Hydrogenizing process of unsaturated hydrocarbons

BIMETALLIC CATALYST SUPPORTS COMPRISING A STRONG INTERACTION BETWEEN UNMETAL OF GROUP VIII AND THE TIN AND ITS USE IN A PROCESS OF REFORMAGECATALYTIQUE

Method of preparation of mono-olefinic hydrocarbons alicyclic

Polycyclic compositions

HYDROGENATION CATALYST

METHOD OF PREPARATION OF JET FUEL FROM MOLECULES RESULTING FROM THE BIOMASS.

L'invention concerne un procédé de préparation de jet fuel ou de précurseurs de jet fuel lequel comprend le traitement d'une charge issue de la biomasse, ladite charge comprenant au moins un composé choisi parmi les terpènes de formule [CH2=C(CH3)CH=CH2]n, où n est un entier, dont la chaîne carbonée est linéaire, cyclique ou ramifiée, ou les terpènes tels que définis précédemment modifiés chimiquement par oxydation et/ou réarrangement du squelette carboné, cycliques ou ramifiés, ledit procédé comprenant une étape (i) de cycloaddition suivie d'une étape (ii) de craquage et d'hydrogénation.

PROCESS FOR PREPARING A CRYSTALLINE ALUMINOSILICATE HYDROCONVERSION CATALYST

Hydrotreating catalyst composition, manufacturing method and use thereof

Optimizing method for selective hydrogenation of acetylene

SELECTIVE HYDROGENATION CATALYST AND METHOD FOR PREPARING SAME

SELF-HYDROGENATION PROCESS

NOUVEAU PROCEDE D'HYDROGENATION DE COMPOSES ORGANIQUES INSATURES

CATALYST FOR THE HYDROGENATION OF UNSATURATED HYDROCARBONS AND PROCESS FOR ITS PREPARATION

The present invention relates to a catalyst for the hydrogenation of unsaturated hydrocarbons, in particular aromatics with a broad molecular weight range, a process for the production thereof and a process for hydrogenating unsaturated hydrocarbons.

METHOD OF PRODUCING A FUEL ADDITIVE

A method of producing a fuel additive includes passing a feed stream comprising C4 hydrocarbons through a hydrogenation unit producing a hydrogenated stream; passing the hydrogenated stream through a distillation unit producing a first stream and a second stream; producing an isobutylene stream by passing the first stream through a molecular sieve unit; passing the isobutylene stream to a hydration unit as a feedstock for the fuel additive; and forming the fuel additive in the hydration unit.

METHOD OF PRODUCING A FUEL ADDITIVE

A method of producing a fuel additive includes producing a first product stream comprising butadiene by passing a feed stream comprising C4 hydrocarbons through a steam cracker; transforming greater than or equal to 90 weight % of the butadiene in the first product stream into a second product stream by passing the first product stream through a first hydrogenation unit, wherein the second product stream comprises 1-butene, 2-butene, n-butane, isobutylene, isobutane, or a combination thereof; and converting the second product stream into the fuel additive by passing the second product stream through a fuel additive synthesis unit with an acid catalyst.

PROCESSES AND SYSTEMS FOR THE CONVERSION OF ACYCLIC HYDROCARBONS TO CYCLOPENTADIENE

This invention relates to processes and systems for converting acyclic hydrocarbons to alkenes, cyclic hydrocarbons and/or aromatics, for example converting acyclic C5 hydrocarbons to cyclopentadiene in a reactor system. The process includes heating an electrically-conductive reaction zone by applying an electrical current to the first electrically-conductive reaction zone; and contacting a feedstock comprising acyclic hydrocarbons with a catalyst material in the electrically-conductive reaction zone under reaction conditions to convert at least a portion of the acyclic hydrocarbons to an effluent comprising alkenes, cyclic hydrocarbons, and/or aromatics.

PROCESS FOR CONVERTING 1,1,2-TRICHLOROETHANE TO VINYL CHLORIDE AND/OR ETHYLENE

A process for the catalytic conversion of 1,1, 2-trichloroethane to reaction products including one or both of ethylene and vinyl chloride in a commercially substantial proportion, in which 1,1,2-trichloroethane is reacted with hydrogen in the presence of a catalyst including a Group VIII metal such as platinum in elemental or compound form, and a Group IB metal such as copper in elemental or compound form.

Composite catalyst for the selective oligomerization of lower alkenes and the production of high octane products

The present invention relates to a) a catalytic composite comprising a support structure and a catalytic species that is deposited on the support structure, b) a process for the selective oligomerization of lower alkenes and mixtures of alkenes, which process comprises contacting the lower alkenes with the catalytic composite in a catalytic distillation apparatus and under catalytic distillation conditions, and c) a process for producing high octane products, which process comprises hydrogenating one or more catalytic distillation apparatus and under catalytic distillation conditions.

Molecular sieve compositions

Crystalline molecular sieves having three-dimensional microporous framework structures of ELO2, AlO2, SiO2 and PO2 framework oxide units are disclosed. The molecular sieves have an empirical chemical composition on an anhydrous basis expressed by the formula: mR: (ELw Alx Py Siz)O22 wherein "R" represents at least one organic templating agent present in the intracrystalline pore system; "m" represents the molar amount of "R" present per mole of (ELw Alx Py Siz)O2 ; "EL" represents at least one element capable of forming a framework oxide unit; and "w", "x", "y" and "z" represent the mole fractions of element(s) "EL", aluminum, phosphorus and silicon, respectively, present as framework oxides. Their use as adsorbents, catalysts, etc. is also disclosed.

CONTINUOUS LIQUID PHASE HYDROGENATION PROCESS USING EXCESS HYDROGEN

Arsenic-aluminum-phosphorus-silicon-oxide molecular sieve compositions

Molecular sieve compositions having three-dimensional microporous framework structures of AsO2, AlO2, PO2 and SiO2 tetrahedral oxide units are disclosed. These molecular sieves have an empirical chemical composition on an anhydrous basis expressed by the formula: mR: (AswAlxPySiz)O2 wherein "R" represents at least one organic templating agent present in the intracrystalline pore system; "m" represents the molar amount of "R" present per mole of (AswAlxPySiz)O2; and "w", "x", "y" and "z" represent the mole fractions of arsenic, aluminum, phosphorus and silicon, respectively, present as tetrahedral oxides. Their use as adsorbents, catalysts, etc. is also disclosed.

Amorphous alloy catalyst containing boron, its preparation and use

The present invention discloses an amorphous alloy catalyst containing boron, which is composed of a porous carrier, a Q-B amorphous alloy, and a metal additive (M), the content of Q-B amorphous alloy together with metal additive is from 0.1 to 60 wt %, based on the total weight of the catalyst, in which the atomic ratio (Q+M)/B is 0.5-10, and the Q/M atomic ratio is 0.1-1000; wherein Q represents an metal selected from group VIII and B represents boron; and said metal additive (M) refers to those one or more metal elements which can be reduced to its/their elemental states from the corresponding salts by a solution containing BH4- with the exception that M is not the one which is used as Q. Said catalyst exhibits high catalytic hydrogenation activity.

ZERO-VALENT METAL CATALYSTS AND A PROCESS FOR PREPARING THEM

Reactor for carrying out reactions having a high enthalpy change

The invention relates to a reactor for carrying out reactions having a high enthalpy change containing catalyst particles between cooled dividing walls. According to the invention, the cooled dividing walls are formed by metal plates/metallic components in which hollow or intermediate spaces in the form of channels are provided in the metal plates/components for accommodating and conveying a cooling medium so as to cool the reactor. The reactor can be used for carrying out strongly exothermic catalytic reactions, for example for the selective hydrogenation of acetylene to ethylene.

High density fuels from oxygenated terpenoids

A method for the efficient synthesis of useful deoxygenated terpenoids from an abundant renewable source, using catalytic conversion of oxygenated terpenoids. Oxygenated terpenoids such as 1,4-cineole and 1,8-cineole are, for example, major components of turpentine and essential oils. These oxygenated terpenoids can also be produced from sugars via a biosynthetic approach. Catalytic deoxygenation of these substrates can be used to efficiently generate commercially important chemicals and high density fuels for turbine or diesel propulsion.

Process for preparing a C4-olefin mixture by selective hydrogenation and metathesis process for using this stream

A C4-olefin mixture having a 1,3-butadiene content of from 100 to 500 ppm and a content of 1,2-dienes of less than 10 ppm is described. The present invention further provides a process for preparing this C4-olefin mixture and provides for its use in a metathesis reaction for preparing 2-pentene and/or 3-hexene.

Crystalline silicoaluminophosphates

USE OF CELL MEMBRANE-BOUND SIGNALING FACTORS

Disclosed herein are compositions comprising complexes of cyclodextrins and lipidmodified stem cell proteins. Also disclosed are topical compositions the complexes. Methods of using the compositions for the therapeutic purposes are also disclosed as well as methods of producing the compositions.

ENANTIOPURE BASE-METAL CATALYSTS FOR ASYMMETRIC CATALYSIS AND BIS(IMINO)PYRIDINE IRON ALKYL COMPLEXES FOR CATALYSIS

Disclosed herein are iron, nickel, or cobalt compounds having tridentate ligands, which can have at least one chiral moiety in the molecular structure thereof and the use of these compounds for the hydrogenation and transformation of olefins (preferably prochiral) and alkynes. 2. The transition metal-containing compound according to claim 1 , wherein M represents an iron atom.3. The transition metal-containing compound according to claim 1 , wherein M represents a cobalt atom.4. The transition metal-containing compound according to claim 1 , wherein M represents a nickel atom.5. The transition metal-containing compound according to claim 1 , wherein each of X claim 1 , X claim 1 , and Xrepresents a nitrogen atom.6. The transition metal-containing compound according to claim 1 , wherein M represents a cobalt atom and each of X claim 1 , X claim 1 , and Xrepresents a nitrogen atom.7. The transition metal-containing compound according to claim 1 , wherein one of Zand Zrepresents a chiral group represented by formula (II) claim 1 , Ror Rrepresents a tert-butyl group or a cyclohexyl group and the other of Rand Rrepresents a methyl group.8. The transition metal-containing compound according to claim 1 , wherein one of Zand Zrepresents a chiral group represented by formula (II) claim 1 , Ror Rrepresents a tert-butyl group and the other of Rand Rrepresents a methyl group.9. The transition metal-containing compound according to claim 1 , wherein one of Zand Zrepresents a chiral group represented by formula (II) claim 1 , Ror Rrepresents a cyclohexyl group and the other of Rand Rrepresents a methyl group.10. The transition metal-containing compound according to claim 1 , wherein M represents a cobalt atom; each of X claim 1 , X claim 1 , and Xrepresents a nitrogen atom; one of Zand Zrepresents a chiral group represented by formula (II); Ror Rrepresents a tert-butyl group or a cyclohexyl group; and the other of Rand Rrepresents a methyl group.11. The transition metal- ...

CATALYST AND METHOD OF CATALYST MANUFACTURE

The catalyst of the invention is a particulate catalyst in the form of particles having a minimum dimension of at least 0.8 mm, including a transition metal or a compound thereof dispersed on a porous support material, characterised in that said catalyst particles comprise at least 35% w/w total transition metal; and the transition metal surface area of said catalyst is at least 110 mper gram of transition metal and the tapped bulk density of a bed of the catalyst particles is at least 0.7 g/ml. The method of making a catalyst includes multiple steps of impregnation of a porous support with a metal ammine solution followed by drying, calcination and reduction of the dried material. The catalyst is useful in hydrogenation reactions. 1. A particulate catalyst in the form of particles having a minimum dimension of at least 0.8 mm , comprising a transition metal or a compound thereof dispersed on a porous support material , wherein said catalyst particles comprise at least 35% w/w total transition metal; and the transition metal surface area of said catalyst is at least 110 mper gram of transition metal and the tapped bulk density of a bed of the catalyst particles is at least 0.7 g/ml.2. A catalyst according to claim 1 , n wherein the porous support comprises a transition alumina.3. A catalyst according to claim 1 , wherein the porous support material has a bimodal pore size distribution.4. A catalyst according to claim 3 , wherein the porous support material has a pore size distribution claim 3 , as measured by mercury porosimetry claim 3 , in which at least 20% of the total pore volume is contained in pores having a diameter of from 100 nm-700 nm and at least 30% of the total pore volume is contained in pores having a diameter of from 5 nm-20 nm5. A catalyst according to claim 1 , wherein the porous support material has a pore volume of at least 1.0 ml/g.6. A catalyst according to claim 1 , wherein the porous support is in the form of extruded cylinders or lobed ...

PROCESS FOR SELECTIVE HYDROGENATION IN THE PRESENCE OF A CATALYST BASED ON A METAL FROM GROUP VIII PREPARED USING AT LEAST ONE CYCLIC OLIGOSACCHARIDE

Selective hydrogenation of a polyunsaturated hydrocarbon feed containing at least 2 carbon atoms per molecule and having an end point of 250° C. or less, by contacting said feed with a catalyst having an active phase of at least one metal from group VIII deposited on a support formed by at least one oxide, said catalyst being prepared using a process involving at least: 1. A process for the selective hydrogenation of a polyunsaturated hydrocarbon feed containing at least 2 carbon atoms per molecule and having an end point of 250° C. or less , said process consisting of bringing said feed into contact with at least one catalyst the active phase of which comprises at least one metal from group VIII deposited on a support formed by at least one oxide , said catalyst being prepared using a process comprising at least:i) at least one step for bringing at least said support into contact with at least one solution containing at least one precursor of at least said metal from group VIII;ii) at least one step for bringing at least said support into contact with at least one organic compound formed from at least one cyclic oligosaccharide composed of at least 6α-(1,4)-bonded glucopyranose subunits;iii) at least one calcining step to obtain at least said metal from said group VIII in the oxide form;the steps i) and ii) possibly being carried out separately, in any order, or simultaneously.2. A selective hydrogenation process according to claim 1 , in which said polyunsaturated hydrocarbon feed is selected from the C2 steam cracked cut claim 1 , the C3 steam cracked cut claim 1 , the C4 steam cracked cut claim 1 , the C5 steam cracked cut and steam cracked gasolines.3. A selective hydrogenation process according to claim 2 , in which said polyunsaturated hydrocarbon feed is a steam cracked gasoline.4. A selective hydrogenation process according to claim 3 , carried out at a temperature in the range 20° C. to 200° C. claim 3 , at a pressure in the range 0.4 to 5 MPa and at an ...

METHOD FOR PRODUCING RENEWABLE FUELS

According to the present invention, organic material is converted to biogas through anaerobic digestion and the biogas is purified to yield a combustible fluid feedstock comprising methane. A fuel production facility utilizes or arranges to utilize combustible fluid feedstock to generate renewable hydrogen that is used to hydrogenate crude oil derived hydrocarbons in a process to make liquid transportation or heating fuel. The renewable hydrogen is combined with crude oil derived hydrocarbons that have been desulfurized under conditions to hydrogenate the hydrocarbons with the renewable hydrogen. 1. A method of transforming waste organic material to produce a liquid transportation or heating fuel comprising:(a) subjecting waste organic material to anaerobic digestion by microorganisms in a biogas production facility that incorporates apparatus to collect the microbially generated biogas;(b) collecting an amount of crude biogas from the biogas production facility;(c) removing impurities from the crude biogas to yield a combustible fluid feedstock;(d) introducing a first amount of combustible fluid feedstock from step (b) or (c) to apparatus for delivering a combustible fluid feedstock to a fuel production facility;(e) withdrawing for use at a fuel production facility a second amount of combustible fluid feedstock approximately equal to the first amount of combustible fluid feedstock;(f) processing at the fuel production facility the second amount of combustible fluid feedstock to produce renewable hydrogen; and(g) producing a third amount of liquid transportation or heating fuel by a process that comprises combining renewable hydrogen derived from the second amount of combustible fluid feedstock with a desulfurized, crude oil derived liquid hydrocarbon in a reactor under conditions to hydrogenate the liquid hydrocarbon with the renewable hydrogen.2. The method of claim 1 , wherein the biogas production facility is a landfill claim 1 , a sewage treatment facility or a ...

THE METHOD FOR PRODUCING VALUABLE AROMATICS AND LIGHT PARAFFINS FROM HYDROCARBONACEOUS OILS DERIVED FROM OIL, COAL OR WOOD

This invention relates to a method of producing aromatics and light paraffins from hydrocarbonaceous oils derived from oil, coal or wood, including partially saturating and hydrocracking the oils derived from oil in a hydrogenation and reaction area, separating them depending on the number of carbons, recirculating heavy oils having 11 or more carbons to the hydrogenation and reaction area, feeding oils suitable for producing BTX to an aromatic separation process and a transalkylation process to recover aromatics, and feeding hydrocarbonaceous components having 5 or fewer carbons to a light separation process, thus obtaining light paraffins. 1. A method of producing aromatics and light paraffins , comprising:(a) introducing oils derived from oil, coal or wood into a hydrogenation and reaction area, so that polycyclic aromatic components are partially saturated and cracked;(b) separating components obtained in (a) into hydrocarbonaceous components having 11 or more carbons, hydrocarbonaceous components having 6-10 carbons, and hydrocarbonaceous components having 5 or fewer carbons; and(c) recirculating the hydrocarbonaceous components having 11 or more carbons separated in (b) to (a), feeding the hydrocarbonaceous components having 6-10 carbons to an aromatic separation process and a transalkylation process so that at least a portion of aromatics is recovered, and feeding the hydrocarbonaceous components having 5 or fewer carbons to a light separation process thus obtaining paraffins.2. The method of claim 1 , wherein the hydrocarbonaceous components having 6-10 carbons are separated in (b) and are transferred to the aromatic separation process so that they are separated into benzene claim 1 , toluene claim 1 , xylene and hydrocarbonaceous components having 9 or more carbons claim 1 , and a portion of the hydrocarbonaceous components is then fed to the transalkylation process to thus obtain a mixture comprising benzene claim 1 , toluene claim 1 , xylene and ...

GAS TREATMENT PROCESS

The present invention relates to a process for treating a gas containing from 10 ppm by volume to 0.5 volume % of at least one of the compounds COS and CSand from 30 ppm by volume to 5 volume % of unsaturated hydrocarbon compounds, the said process comprising the following stages: 1. Process for treating a gas containing from 10 ppm by volume to 0.5 volume % of at least one of the compounds COS and CSand from 30 ppm by volume to 5 volume % of unsaturated hydrocarbon compounds , the said process comprising the following stages:a) a hydrogenation (1) of the unsaturated hydrocarbon compounds to paraffins is carried out by contacting the said gas with a hydrogenation catalyst in the presence of hydrogen at a temperature between 100 and 400° C., so as to provide a gaseous effluent depleted in unsaturated hydrocarbon compounds, the hydrogenation catalyst comprising at least one metal selected from palladium, platinum, nickel and cobalt deposited on a porous support,{'sub': 2', '2, 'b) a catalytic hydrolysis (2) of COS and/or CSpresent in the gaseous effluent from stage a) is carried out in the presence of water so as to provide a gaseous effluent rich in HS by contacting the said gaseous effluent from stage a) with a hydrolysis catalyst, the hydrolysis catalyst comprising alumina or titanium oxide.'}2. Process according to claim 1 , in which the hydrogenation catalyst contains platinum claim 1 , expressed as metal claim 1 , in an amount between 0.02 wt. % and 4 wt. % with respect to the weight of the catalyst.3. Process according to claim 1 , in which the hydrogenation catalyst contains palladium claim 1 , expressed as metal claim 1 , in an amount between 0.05 wt. % and 5 wt. % with respect to the weight of the catalyst.4. Process according to claim 1 , in which the hydrogenation catalyst contains nickel in an amount claim 1 , expressed as oxide claim 1 , between 0.5 wt. % and 15 wt. % with respect to the weight of the catalyst.5. Process according to claim 1 , in which ...

Hydrogen recycle and hydrogen cloride recovery in an alkylation process

We provide an alkylation process, comprising: separating and recycling a hydrogen gas and a hydrogen chloride from an offgas of a hydrogenation reactor; wherein the hydrogen gas is recycled to the hydrogenation reactor; and wherein the hydrogen chloride is recycled to an alkylation reactor. We also provide an alkylation process unit for performing this process.

Renewable High-Density, High-Octane Fuels

A method/fuels for making high-density, high-octane fuels, the high-density, high-octane including, dimerizirig terpene monomer(s), crude mixture of terpene(s), and/or oxygenated terpenoid(s) with at least one heterogeneous dimerization acid catalyst at temperatures ranging from about 25° C. to about 160° C. to produce a mixture of residual/isomerized monomer(s) cymene(s), and terpene dimer(s), hydrogenating the mixture of residual/isomerized monomer(s), p-cymene(s), and terpene dimer(s) with at least one heterogenous catalyst(s) under a hydrogen atmosphere to produce a hydrogenated mixture of cymene(s), saturated cyclic molecules of terpene(s), other aromatic(s), and/or saturated terpene dimer(s), and isolating the hydrogenated mixture of cymene(s), saturated cyclic terpene(s), other aromatic(s), and saturated terpene dimer(s) by fractional distillation to yield a high boiling fraction composed of terpene dimers and mixture low boiling fraction composed of hydrogenated monomer(s) and cymenes. 1. A method for making a high-density , high-octane fuel , comprising:dimerizing terpene monomer(s), crude mixture of terpene(s), and/or oxygenated terpenoid(s) with at least one heterogeneous dimerization acid catalyst at temperatures ranging from about 25° C. to about 170° C. to produce a mixture of residual/isomerized monomer(s), cymene(s), and terpene dimer(s);hydrogenating said mixture of residual/isomerized monomer(s), cymene(s), and terpene dimer(s) with at least one catalyst under a hydrogen atmosphere to produce a hydrogenated mixture of cymene(s), saturated cyclic molecules of terpene(s), other aromatic(s), and/or saturated terpene dimer(s); andisolating said hydrogenated mixture of cymene(s), saturated cyclic terpene(s), other aromatic(s), and saturated terpene dimer(s) by fractional distillation to yield a high boiling fraction composed of terpene dimers and boiling between about 280 and 350° C. under standard conditions, and a low boiling fraction composed of ...

PROCESS FOR THE PRODUCTION OF PARA-XYLENE

A reforming process using a medium pore zeolite under conditions to facilitate the conversion of Cparaffinic compounds to para-xylene is provided. Para-xylene is produced at greater than thermodynamic equilibrium concentrations using the process. 1. A process for producing para-xylene comprising the steps of:(a) contacting a hydrocarbonaceous feed wherein at least 50 wt. % of said feed boils above 550° F., in a first reaction zone comprising a hydrocracking catalyst under hydrocracking conditions to form an effluent;{'sub': 8', '8, '(b) separating the effluent into at least a Ccontaining fraction comprising at least 10 wt. % Cparaffinic hydrocarbons;'}{'sub': '8', '(c) providing the Ccontaining fraction to a second reaction zone;'}{'sub': '8', '(d) contacting the Ccontaining fraction under reforming reaction conditions with a reforming catalyst comprising a medium pore zeolite having a silica to alumina molar ratio of at least 200, a crystallite size of less than 10 microns and an alkali content of less than 5000 ppm in a second reaction zone to produce a product stream comprising para-xylene and meta-xylene wherein the para-xylene to meta-xylene ratio is at least 0.9; and'}(e) separating the para-xylene from the product stream.2. The process of claim 1 , wherein the reforming catalyst comprises silicalite.3. The process of claim 1 , where the medium pore zeolite is selected from the group consisting of ZSM-5 claim 1 , ZSM-11 claim 1 , ZSM-12 claim 1 , ZSM-22 claim 1 , ZSM-23 claim 1 , ZSM-35 claim 1 , ZSM-38 claim 1 , ZSM-48 claim 1 , MCM-22 claim 1 , SSZ-20 claim 1 , SSZ-25 claim 1 , SSZ-32 claim 1 , SSZ-35 claim 1 , SSZ-37 claim 1 , SSZ-44 claim 1 , SSZ-45 claim 1 , SSZ-47 claim 1 , SSZ-58 claim 1 , SSZ-74 claim 1 , SUZ-4 claim 1 , EU-1 claim 1 , NU-85 claim 1 , NU-87 claim 1 , NU-88 claim 1 , IM-5 claim 1 , TNU-9 claim 1 , ESR-10 claim 1 , TNU-10 claim 1 , and combinations thereof.4. The process of claim 3 , wherein the medium pore zeolite is selected from the ...

Highly Branched Hydrocarbon Isomerization for an Aromatization Reaction

A process for aromatizing hydrocarbons comprises: converting at least a portion of highly branched hydrocarbons in a feed stream into selectively convertible components, and aromatizing the selectively convertible components to produce an aromatization reactor effluent. The aromatization reactor effluent comprises an aromatic product. Converting at least the portion of the highly branched hydrocarbons into the selectively convertible components may include contacting the feed stream with an isomerization catalyst in an isomerization reaction system under isomerization reaction conditions; and isomerizing the portion of the highly branched hydrocarbons in the feed stream into the selectively convertible components. 1. A process for aromatizing hydrocarbons comprising:concentrating highly branched hydrocarbons in a hydrocarbon stream to yield a highly branched hydrocarbon rich stream, wherein the highly branched hydrocarbons comprise hydrocarbons having six or seven carbon atoms with an internal quaternary carbon or hydrocarbons having six carbon atoms and two adjacent internal tertiary carbons, or mixtures thereof;converting at least a portion of the highly branched hydrocarbons in the highly branched hydrocarbon rich stream into selectively convertible components by contacting the highly branched hydrocarbons with an isomerization catalyst and isomerizing at least the portion of the highly branched hydrocarbons into the selectively convertible components; andaromatizing the selectively convertible components to produce an aromatization reactor effluent comprising an aromatic product.2. The process of claim 1 , wherein the isomerization catalyst comprises platinum.3. The process of claim 1 , wherein the isomerization catalyst comprises a platinum alumina catalyst with or without a Friedel-Crafts halide claim 1 , platinum molecular sieve catalyst claim 1 , or platinum sulfate metal oxide catalyst.4. The process of claim 1 , wherein the isomerization catalyst comprises ...

METHOD FOR PRODUCING LUBRICATING-OIL BASE OIL

A method for producing a lubricant base oil which comprises a first step of carrying out isomerization dewaxing by contacting, in the presence of hydrogen, a hydrocarbon oil containing normal paraffin having a boiling point of 360° C. or higher, with a hydroisomerization catalyst under conditions such that a cracking rate defined in the following formula (1) is 10 mass % or less, and a second step of carrying out the above isomerization dewaxing by temporarily switching the above conditions to conditions such that the cracking rate is 13 mass % or more. 2. The method for producing a lubricant base oil according to claim 1 , whereinthe hydroisomerization catalyst is a catalyst containing a zeolite having a one-dimensional porous structure including a 10-membered ring, a support containing a binder, and platinum and/or palladium supported on the support;a carbon content of the catalyst is 0.4 to 3.5% by mass;the zeolite is derived from an ion-exchanged zeolite obtained by ion-exchanging an organic template-containing zeolite containing an organic template and having a one-dimensional porous structure including a 10-membered ring in a solution containing ammonium ions and/or protons4. The method for producing a lubricant base oil according to claim 1 , wherein while performing the first step continuously claim 1 , the second step is temporarily carried out at predetermined intervals. The present invention relates to a method for producing a lubricant base oil.Among petroleum products, for example, lubricant oils, gas oils, jet fuels, and the like are products in which cold flow property is regarded as important. For this reason, it is desirable that base oils used for these products be such that waxy components such as normal paraffins or slightly branched isoparaffins, which are responsible for deteriorating the cold flow property, have been completely or partially removed, or converted to components other than waxy components.An example of a known dewaxing technique ...

CONVERSION OF POLYESTER-CONTAINING FEEDSTOCKS INTO HYDROCARBON PRODUCTS

Provided herein are methods of processing polyester-containing feedstocks to provide hydrocarbon products. Exemplary feedstocks include those containing estolide compounds, which may be processed under thermal and/or catalytic conditions to provide at least one hydrocarbon product. 196-. (canceled)97. A method comprising:providing a feedstock comprising at least one estolide compound; andconverting the at least one estolide compound into at least one hydrocarbon product.98. The method according to claim 97 , wherein converting the at least one estolide compound comprises deoxygenating the at least one estolide compound.99. The method according to claim 98 , wherein the deoxygenating comprises decarboxylation.100. The method according to claim 98 , wherein the deoxygenating comprises thermal decarboxylation.101. The method according to claim 98 , wherein the deoxygenating comprises decarbonylation.102. The method according to claim 98 , wherein the deoxygenating comprises hydrodeoxygenation.103. The method according to claim 98 , wherein converting the at least one estolide compound is conducted in the presence of water.104. The method according to claim 98 , wherein converting the at least one estolide compound is conducted in the presence of hydrogen.105. The method according to claim 98 , wherein converting the at least one estolide compound comprises contacting said at least one estolide compound with at least one catalyst.106. The method according to claim 105 , wherein the at least one catalyst comprises a transition metal.107. The method according claim 98 , wherein converting the at least one estolide compound is conducted at a temperature of at least 100° C.108. The method according to claim 107 , wherein converting the at least one estolide compound is conducted at a temperature of about 200° C. to about 500° C.109. The method according to claim 98 , wherein converting the at least one estolide compound is conducted at a pressure that is greater than 1 atm ...

Methods and apparatuses for selective hydrogenation of olefins

Methods and apparatuses for selective hydrogenation of olefins are provided. The method for selective hydrogenation of olefins comprises reacting a hydrocarbonaceous feedstock comprising olefins and aromatic compounds with hydrogen in a reaction zone. The reaction contains a catalyst producing a reaction zone product stream comprising aromatic compounds. The reaction zone product stream is passed to a flash vessel, recovering a first product stream and a second product stream from the flash vessel. The first product stream is passed to a liquid jet eductor, whereas the second product stream comprising aromatic compounds having a reduced concentration of olefins is subsequently recovered.

METHOD FOR PRODUCING MONOCYCLIC AROMATIC HYDROCARBONS

The present method for producing monocyclic aromatic hydrocarbons is a method for producing monocyclic aromatic hydrocarbons having 6 to 8 carbon atoms. This method includes a cracking and reforming reaction step of bringing oil feedstock into contact with a catalyst to cause a reaction and obtain a product containing monocyclic aromatic hydrocarbons having 6 to 8 carbon atoms and a heavy fraction having 9 or more carbon atoms, a purification and recovery step of purifying and recovering the monocyclic aromatic hydrocarbons having 6 to 8 carbon atoms separated from the product formed by the cracking and reforming reaction step, and a first returning step of returning at least a portion of toluene obtained by the purification and recovery step to the cracking and reforming reaction step. 1. A method for producing monocyclic aromatic hydrocarbons having 6 to 8 carbon atoms from oil feedstock having a 10 vol % distillation temperature of 140° C. or higher and a 90 vol % distillation temperature of 380° C. or lower , comprising:a cracking and reforming reaction step of bringing the oil feedstock into contact with a catalyst for producing monocyclic aromatic hydrocarbons containing a crystalline aluminosilicate to cause a reaction and obtain a product containing monocyclic aromatic hydrocarbons having 6 to 8 carbon atoms and a heavy fraction having 9 or more carbon atoms;a purification and recovery step of purifying and recovering the monocyclic aromatic hydrocarbons having 6 to 8 carbon atoms separated from the product formed by the cracking and reforming reaction step; anda first returning step of returning at least a portion of toluene obtained by the purification and recovery step to the cracking and reforming reaction step.2. The method for producing monocyclic aromatic hydrocarbons according to claim 1 , further comprising a second returning step of returning the heavy fraction having 9 or more carbon atoms separated from the product formed by the cracking and ...

THERMAL CRACKING OF IMPURITIES IN TRIGLYCERIDE MIXTURES

A heated petroleum-derived hydrocarbon is contacted with a triglyceride feed in a thermal cracking zone to decompose and remove impurities prior to hydrotreating the mixture to fuel range hydrocarbon. This process allows the use of a variety of low cost triglyceride feeds while reducing fouling of process equipment and catalyst. The process also reduces the use of chemicals required for conventional degumming of triglyceride feeds. 1. A process comprising:a) obtaining a petroleum-derived hydrocarbon feed that comprises hydrocarbon compounds having a boiling point from about 25° C. to about 760° C.;b) heating the petroleum-derived hydrocarbon feed to a temperature ranging from about 100° C. to about 540° C. to produce a heated hydrocarbon feed;c) conveying the heated hydrocarbon feed to a thermal cracking zone;d) contacting a triglyceride feed with the heated hydrocarbon feed in the thermal cracking zone at a temperature ranging from about 100° C. to about 540° C. to form a thermally treated feed, wherein the contacting results in the thermal cracking of at least one contaminant derived from the triglyceride feed to form a decomposed contaminant, wherein the contaminant is selected from phospholipids, proteins, gums, metal containing compound and any combination thereof, wherein the metal containing compound is selected from alkali metals, alkaline earth metals, and any combination thereof;e) conveying the thermally treated feed to a hydrotreating zone;f) hydrotreating the thermally treated feed with a hydrotreating catalyst in the hydrotreating zone at a temperature in the range of from about 260° C. to about 430° C. and a pressure ranging from 0 psig to about 2000 psig to produce a product containing diesel boiling range hydrocarbons.2. The process of claim 1 , wherein the sole source of heat for the thermal cracking zone is the heated hydrocarbon feed.3. The process of claim 1 , wherein the triglyceride feed is maintained at a temperature that does not permit ...

METHODS AND SYSTEMS FOR CONVERTING HYDROCARBONS

Methods and systems for converting hydrocarbons including exposing a portion of a hydroperoxide-containing feed including tert-butyl hydroperoxide to a solid deperoxidation catalyst under decomposition conditions to form an oxidation effluent comprising tert-butyl alcohol, wherein the solid deperoxidation catalyst comprises a manganese oxide octahedral molecular sieve, are provided herein. Further methods and systems for converting the oxidation effluent to an alkylation product are also provided herein. 1. A method for converting hydrocarbons , comprising:an oxidizing step comprising exposing a portion of a hydroperoxide-containing feed comprising tert-butyl hydroperoxide to a solid deperoxidation catalyst under decomposition conditions to form an oxidation effluent comprising tert-butyl alcohol,wherein the solid deperoxidation catalyst comprises a manganese oxide octahedral molecular sieve.2. The method of claim 1 , wherein the decomposition conditions comprise a temperature of about 50° C. to about 170° C. and a pressure of about 10 psig to about 500 psig.3. The method of claim 1 , wherein at least about 70% of the tert-butyl hydroperoxide is converted to tert-butyl alcohol and/or the solid deperoxidation catalyst has a selectivity of at least about 70% for conversion of tert-butyl hydroperoxide to tert-butyl alcohol.4. The method of claim 1 , wherein at least about 90% of the tert-butyl hydroperoxide is converted to tert-butyl alcohol and/or the solid deperoxidation catalyst has a selectivity of at least about 90% for conversion of tert-butyl hydroperoxide to tert-butyl alcohol.5. The method of claim 1 , wherein the manganese oxide octahedral molecular sieve comprises MnOoctahedra which share edges to form a tunnel structure.6. The method of claim 5 , wherein the tunnel structure is 2×2 tunnel structure or 3×3 tunnel structure.7. The method of claim 1 , wherein the solid deperoxidation catalyst is selected from the group consisting of OMS-2 claim 1 , Nb-OMS-2 ...

NICKEL HYDROGENATION CATALYST

The invention relates to a catalyst comprising nickel and a solid silica support, to a process for preparing such a catalyst and to a process for the hydrogenation of an unsaturated fatty material. According to the invention there is provided a catalyst comprising nickel on a solid silica support, wherein said catalyst has a specific pore volume of at least 0.4 ml/g and a TPR peak maximum within the range of 360-420° C.

PROCESSES FOR UPGRADING ALGAE OILS AND PRODUCTS THEREOF

Algae oil feeds comprise a wide range of molecular species forming a complex mixture of molecules having varying sizes and therefore varying boiling points, comprise high nitrogen, oxygen, and fatty acid content, but comprise low sulfur, saturated hydrocarbons, and triglycerides. The wide range of molecular species in the algae oil feeds, very unusual compared to conventional refinery feedstocks and vegetable oils, may be upgraded into fuels by conventional refining approaches such as thermal and/or catalytic-hydroprocessing. Hydrotreating at high pressure over large-pore catalyst, and optionally followed by FCC cracking, has shown a beneficial product slate including coke yield. Thermal treatment prior to hydrotreating may improve hydrotreating feedstock quality. Unusual behavior of the algae oils in thermal treatment and/or hydroprocessing, including cracking to lower boiling range compounds, may provide a high quality product slate with the flexibility to adjust the product slate due to the cracking behavior exhibited by these algae oils.

METHOD FOR PRODUCING BASE LUBRICATING OIL FROM OILS RECOVERED FROM COMBUSTION ENGINE SERVICE

A method for producing ILSAC GF5 or higher compatible oils from used oil, comprising separating material having a boiling point less than about 350° F. from recovered oil to produce de-volatized oil fraction and light oil fraction. Separating material with a boiling point greater than about 350° F. and less than about 650° F. from the de-volatized oil fraction to produce fuel oil fraction and heavy oil fraction. Separating material with a boiling point greater than about 1200° F. from the heavy oil fraction to produce partially purified oil fraction and residual fraction. Treating the partially purified oil fraction to separate it into purified oil fraction and contaminant fraction. Hydrogenating the contaminant fraction to remove predetermined compounds, further saturating the fraction and thereby creating a saturated oil fraction. Fractionating the saturated oil stream to produce one or more of naphtha fraction, diesel oil fraction and base oil fraction.

Aromatization reactors with hydrogen removal and related reactor systems

The present invention discloses aromatization reactor vessels with hydrogen membrane tubes, and associated aromatization reactor vessel systems. Also disclosed are processes for conducting aromatization reactions utilizing these reactor vessels and systems. 1. An aromatization reactor vessel comprising:(a) a reactor wall;(b) a catalyst bed positioned within the reactor vessel;(c) an outer annulus positioned between the reactor wall and an outer particle barrier, the outer particle barrier and the outer annulus surrounding the catalyst bed;(d) a reactor inlet for a feed stream; 'wherein a flow path for the feed stream begins at the reactor inlet, continues to the outer annulus, through the outer particle barrier and the catalyst bed, into the center pipe, and to the reactor outlet; and', '(e) a reactor outlet connected to a center pipe, the center pipe positioned in the reactor vessel and surrounded by the catalyst bed;'}{'sub': '2', '(f) a membrane tube configured to remove H, the membrane tube positioned in the center pipe or the outer annulus, the membrane tube having an inner permeate side and an outer process side.'}2. The vessel of claim 1 , wherein the membrane tube is positioned in the center pipe claim 1 , and wherein the outer process side faces the center pipe.3. (canceled)4. The vessel of claim 1 , wherein the membrane tube is positioned in the outer annulus claim 1 , and wherein the outer process side faces the outer annulus.5. The vessel of claim 1 , wherein the membrane tube is configured for an operating temperature in a range from about 260° C. to about 600° C.6. The vessel of claim 1 , wherein the membrane tube comprises palladium.7. The vessel of claim 1 , wherein the center pipe and the catalyst bed are positioned concentrically.8. The vessel of claim 1 , wherein the aromatization reactor vessel is configured for a catalytic conversion of a non-aromatic hydrocarbon to an aromatic hydrocarbon comprising benzene claim 1 , toluene claim 1 , xylene ...

CO-PRODUCTION OF MTBE AND ALKYLATE

Processes for co-production of methyl tertiary-butyl ether (MTBE) and alkylate is disclosed. The process includes comprising passing a hydrocarbon feed stream comprising Chydrocarbons to a dehydrogenation unit to generate a dehydrogenation effluent comprising Colefins. The dehydrogenation effluent is passed to a MTBE unit to provide a mixed stream comprising Colefins and MTBE. The mixed stream is separated to provide an MTBE product stream and a fractionator overhead stream comprising olefins. The fractionator overhead stream is passed to an alkylation unit to produce an alkylation product stream comprising an alkylate. 1. A process for co-production of a tertiary-butyl ether compound and alkylate , comprising:{'sub': 4', '4, 'passing a hydrocarbon feed stream comprising Chydrocarbons to a dehydrogenation unit to generate a dehydrogenation effluent comprising Colefins;'}{'sub': '4', 'passing the dehydrogenation effluent to a tertiary-butyl ether unit to provide a mixed stream comprising Colefins and a tertiary-butyl ether compound;'}separating the mixed stream to provide a tertiary-butyl ether product stream and a fractionator overhead stream comprising olefins; andpassing the fractionator overhead stream to an alkylation unit to produce an alkylation product stream comprising an alkylate.2. The process of claim 1 , wherein the tertiary-butyl ether compound is one of methyl tertiary-butyl ether (MTBE) or ethyl tertiary-butyl ether (ETBE).3. The process of further comprising:passing the alkylation product stream to a de-isobutanizer column to generate a de-isobutanizer overhead stream and a de-isobutanizer bottoms stream; andpassing the de-isobutanizer bottoms stream to a debutanizer column to generate a debutanizer overhead stream and the alkylate.4. The process of further comprising:passing a first portion of the debutanizer overhead stream to an isomerization unit to generate an isomerate stream; andpassing the isomerate stream to the de-isobutanizer column.5. The ...

IONIC LIQUID ALKYLATION OF 1-BUTENE TO PRODUCE 2,5-DIMETHYLHEXANE

A process for producing dimethylhexanes (DMH) is provided. The DMH can be used to produce p-xylene. The process involves the alkylation of isobutane and 1-butene using an ionic liquid to produce naphtha that is rich in DMH. The DMH is then converted in high selectivity to xylene, including p-xylene, by dehydrocyclization. 1. A process for producing dimethylhexane comprising:introducing a stream comprising isobutane and a stream comprising 1-butene or a stream comprising isobutane and 1-butene to an alkylation reaction zone to form a reaction mixture, the stream comprising 1-butene or the stream comprising isobutane and 1-butene containing less than about 50 wt % total of 2-butene and isobutene; andalkylating the isobutane and the 1-butene in the alkylation reaction zone in the presence of a haloaluminate ionic liquid catalyst under alkylation conditions to form a stream rich in dimethylhexane, the stream rich in dimethylhexane having a ratio of dimethylhexane to trimethylpentane of at least about 2:1.2. The process of wherein the haloaluminate ionic liquid catalyst comprises a chloroaluminate ionic liquid catalyst claim 1 , a bromoaluminate ionic liquid catalyst claim 1 , or combinations thereof.4. The process of wherein the stream rich in dimethylhexane comprises at least about 25 wt % 2 claim 1 ,5-dimethylhexane based on a total weight of dimethylhexane claim 1 , or at least about 25 wt % 2 claim 1 ,4-dimethylhexane based on a total weight of dimethylhexane claim 1 , or both.5. The process of wherein a ratio of isobutane to 1-butene is in a range of about 1:1 to about 50:1.6. The process of wherein the alkylation conditions include a temperature in a range of about −20° C. to about 100° C. claim 1 , and a pressure in a range of about 0.101 MPa to about 8.0 MPa.7. The process of wherein a ratio of catalyst to olefins is in a range of about 0.1:1 to about 10:1.8. The process of claim further comprising stirring the reaction mixture and the acidic ionic liquid ...

System and Method for Reducing Fouling Rate In A Hydrogenation Reactor

Fouling rate inhibition for a hydrogenation reactor. A hydrocarbon hydrogenation method comprises passing a liquid feedstream through a magnetic field to separate magnetically susceptible particles, and introducing the magnetically lean stream into a fixed catalyst bed under hydrogenation conditions to saturate carbon-carbon double bonds in the hydrocarbon. Also, a hydrogenation reactor system comprises a magnetic conditioning zone, an inlet flow path to introduce a magnetically lean stream from the magnetic conditioning zone into a fixed catalyst bed and an outlet flow path from an outlet end of the catalyst bed to withdraw reactor effluent. 1. A hydrogenation reactor system , comprising:a magnetic conditioning zone to pass a liquid hydrocarbon feedstream through a magnetic field to separate magnetically susceptible particles from the hydrocarbon and form a magnetically lean stream;an inlet flow path to introduce the magnetically lean stream from the magnetic conditioning zone into a fixed catalyst bed; andan outlet flow path from an outlet end of the catalyst bed to withdraw reactor effluent.2. The hydrogenation reactor system of claim 1 , wherein the magnetic conditioning zone comprises a rare earth magnet.3. The hydrogenation reactor system of claim 1 , wherein the magnetic conditioning zone comprises a magnetic grate.4. The hydrogenation reactor system of claim 1 , further comprising filter media disposed in the inlet flow path between the magnetic conditioning zone and the fixed catalyst bed.5. The hydrogenation reactor system of claim 4 , wherein the filter media comprises a fabric sock filter.6. The hydrogenation reactor system of claim 4 , further comprising a magnet disposed in a sock of the fabric sock filter.7. The hydrogenation reactor system of claim 1 , wherein the liquid hydrocarbon feedstream comprises an unsaturated hydrocarbon resin claim 1 , and wherein the catalyst bed comprises metal oxide or metal sulfide hydrogenation catalyst.8. The ...

Aromatization Reactors with Hydrogen Removal and Related Reactor Systems

The present invention discloses aromatization reactor vessels with hydrogen membrane tubes, and associated aromatization reactor vessel systems. Also disclosed are processes for conducting aromatization reactions utilizing these reactor vessels and systems. 120-. (canceled)21. An aromatization process comprising:{'sub': '2', 'claim-text': (a) a reactor wall;', '(b) a catalyst bed positioned within the reactor vessel;', '(c) an outer annulus positioned between the reactor wall and an outer particle barrier, the outer particle barrier and the outer annulus surrounding the catalyst bed;', '(d) a reactor inlet for the feed stream;', 'wherein a flow path for the feed stream begins at the reactor inlet, continues to the outer annulus, through the outer particle barrier and the catalyst bed, into the center pipe, and to the reactor outlet; and', '(e) a reactor outlet connected to a center pipe, the center pipe positioned in the reactor vessel and surrounded by the catalyst bed;'}, {'sub': '2', '(f) a membrane tube configured to remove H, the membrane tube positioned in the center pipe or the outer annulus, the membrane tube having an inner permeate side and an outer process side;'}], '(i) introducing a feed stream comprising Hand a non-aromatic hydrocarbon into an aromatization reactor vessel, the aromatization reactor vessel comprising(ii) contacting the feed stream with the catalyst bed comprising an aromatization catalyst;{'sub': '2', '(iii) catalytically converting at least a portion of the non-aromatic hydrocarbon within the aromatization reactor vessel to produce an aromatic hydrocarbon and H;'}{'sub': 2', '2, '(iv) removing a portion of the Hfrom the center pipe or the outer annulus via the membrane tube to reduce a partial pressure of Hin the process; and'}(v) discharging a reactor effluent comprising the aromatic hydrocarbon from the aromatization reactor vessel via the reactor outlet.22. The process of claim 21 , wherein:the aromatic hydrocarbon comprises benzene ...

PURIFYING ORGANOPHOSPHORUS COMPOUNDS CONTAMINATED WITH CHLORINE

The invention relates to a process for the purification of a contaminated organophosphorus product which comprises at least one organophosphorus compound and, as contaminant, at least one chlorine compound. It is based on the object of indicating a purification method in which the chlorine content of an organophosphorus product which comprises at least one organophosphorus compound and at least one chlorine compound as contaminant, can be reduced from originally 1000 to 100 000 ppm to a total chlorine content between 10 ppm and 10 000 ppm. This is achieved by a process with the steps: 115-. (canceled)16. A process for the purification of a contaminated organophosphorus product which comprises at least one organophosphorus compound and , as contaminant , at least one chlorine compound , having the following steps:a) providing the contaminated organophosphorus product;b) completing dissolution of the contaminated organophosphorus product in a solvent to give a contaminated solution;c) separating the contaminated solution by means of a filter and/or by means of a membrane separation unit to give a purified solution;d) removing the solvent from the purified solution to give a purified organophosphorus product.17. The process according to claim 16 , in which the stepsa) providing the contaminated organophosphorus product;andb) completing dissolution of the contaminated organophosphorus product in a solvent to give a contaminated solution;take place in one operation by providing the contaminated organophosphorus product completely dissolved in the contaminated solution.18. The process according to claim 16 , wherein the total chlorine content of the purified solution is less than that of the total chlorine content of the contaminated solution.19. The process according to claim 18 , wherein the total chlorine content of the contaminated organophosphorus product is between 1000 ppm and 100 claim 18 ,000 ppm claim 18 , and that the total chlorine content of the purified ...

Procedimento di idrogenazione selettiva in fase gassosa di composti plurinsaturi

Selective hydrogenation in gaseous phase of cyclopentadiene or a mixture of ethylene and acetylene using a palladium zinc catalyst deactivated with ammonia, ammonium chloride, steam, or their mixtures

In a process for the selective hydrogenation of polyunsaturated compounds, by means of a catalyst system, the hydrogenation is carried out in gaseous phase in the presence of a catalyst of a metal of the eight group of the Periodical Table, partially deactivated by a deactivating system.

Hydrogen recycle and hydrogen chloride recovery in an alkylation process

We provide an alkylation process, comprising: separating and recycling a hydrogen gas and a hydrogen chloride from an offgas of a hydrogenation reactor; wherein the hydrogen gas is recycled to the hydrogenation reactor; and wherein the hydrogen chloride is recycled to an alkylation reactor. We also provide an alkylation process unit for performing this process.

Alkylation process unit comprising a fractionation unit for separating hydrogen gas and hydrogen chloride

We provide an alkylation process, comprising: separating and recycling a hydrogen gas and a hydrogen chloride from an offgas of a hydrogenation reactor; wherein the hydrogen gas is recycled to the hydrogenation reactor; and wherein the hydrogen chloride is recycled to an alkylation reactor. We also provide an alkylation process unit for performing this process.

Microdispersant for droplets generation

FIELD: micro dispersing agents. SUBSTANCE: invention relates to micro dispersers in which micro droplets of mainly spherical shape of nanoliter and sub-nanolitre volume are generated, and then generated droplets can be used in chemical, pharmaceutical and other technologies, including for mass-exchange processes and chemical reactions between reagents dissolved in drops, or dissolved in drops and in a solid medium, as well as for subsequent application of biologically active substances on the surface of formed drops. Essence of the invention lies in the fact that in the microdispersant for generation of drops of one liquid in another with a narrow disperse composition, comprising a housing in the form of a channel of an extended shape, a nozzle for input of the disperse phase coaxially attached to the housing, and connected to side surface of housing one or more branch pipes for input of solid phase, channel cross-section from branch pipe branch for disperse phase input is made periodically varying, wherein inner size h of narrow part of channel is made in accordance with design formula where d is average size of drops, which need to be generated in microdispersant, m; Q 1 is flow rate of disperse phase, m 3 /s; Q 2 is flow rate of continuous phase, m 3 /s, and internal size H of wide part of channel is made in accordance with design formula: , wherein spatial period λ between adjacent waves in periodically varying structure of housing is made in accordance with design formula . Number of waves in the periodically varying body structure in the microdispersant ranges from 3 to 7. Device enables to form in a liquid in micro channels spherical drops (microspheres) with dimensions distributed in a sufficiently narrow range, as well as provide an equal distance between adjacent drops, which will prevent their collision and subsequent coalescence. EFFECT: technical result consists in improvement of universality of the device and possibility of its applicability for ...

Catalyst

Selective Hydrogenation Catalyst based on Nickel-Zirconia and Its Use for Selective Hydrogenation of Di-olefins

본 발명은 선택적 수소화 반응에 유용한 정방정계상 구조를 갖는 니켈/지르코니아계 촉매 및 이를 이용한 탄화수소 혼합물 중에 함유된 디-올레핀 화합물로부터 모노-올레핀으로의 선택적 수소화 공정에 관한 것으로서, 더욱 상세하게는 지르코니아 그 자체 또는 알칼리 토금속, 란탄족 금속, IIIB족 금속, IVB족 금속 중의 한성분으로 수식된 지르코니아 담체상에 니켈 또는 니켈과 함께 팔라듐, 백금, 은, 구리, 몰리브데늄, 붕소 및 인 중에서 선택된 조촉매를 졸겔법 또는 공침법에 의해 제조된 것으로, 담체로 사용된 지르코니아 격자내에 니켈 산화물의 일부가 결합하여 고용체를 형성하고 있고, 이러한 고용체는 지르코니아 담체 표면에 고르게 분산되어 있어 탄화수소 혼합물 중에 함유된 디-올레핀 탄화수소를 동일 탄소수의 모노-올레핀 탄화수소로 선택적으로 전환시킬 수 있는 디-올레핀 화합물의 선택적 수소화 반응에 촉매로 사용되는 정방정계(tetragonal)상 구조의 니켈/지르코니아 촉매에 관한 것이다. 또한, 상기 촉매를 환원한 후 탄소수 8개에서 15개 범위의 지방족 디-올레핀의 수소화 반응에 적용할 때 동일 탄소수의 모노-올레핀으로 선택적으로 전환시킬 수 있는 특성을 나타낸다. The present invention relates to a nickel / zirconia-based catalyst having a tetragonal phase structure useful for selective hydrogenation, and to a selective hydrogenation process from a di-olefin compound to a mono-olefin contained in a hydrocarbon mixture using the same. Cocatalyst selected from palladium, platinum, silver, copper, molybdenum, boron and phosphorus together with nickel or nickel on zirconia carriers modified on their own or as constituents of alkaline earth metal, lanthanide metal, group IIIB metal, group IVB metal Prepared by the sol-gel method or coprecipitation method, a part of nickel oxide is combined in the zirconia lattice used as a carrier to form a solid solution, which is dispersed evenly on the surface of the zirconia carrier to Olefin hydrocarbons to mono-olefin hydrocarbons of the same carbon number It relates to a tetragonal phase nickel / zirconia catalyst used as a catalyst for the selective hydrogenation of di-olefin compounds which can be selectively converted. In addition, after the reduction of the catalyst, when applied to the hydrogenation of aliphatic di-olefin of 8 to 15 carbon atoms, it exhibits a property that can be selectively converted to a mono-olefin of the same carbon number.

Hydrogenating catalyst of unsaturated hydrocarbon by hydrogen and its production

(57)【要約】本公報は電子出願前の出願データであるた め要約のデータは記録されません。

Method of producing trans-1-alkenyl(chlorodiisopropylamino)boranes

FIELD: chemistry. SUBSTANCE: invention relates to a method of producing trans-1-alkenyl(chlorodiisopropylamino)-boranes of general formula (1a-d): (1a-d), where (a) R = para -Me, (b) R = meta- Me, (c) R = ortho- Me, (d) R = H. Method involves reacting aromatic α-olefin ( para- methylstyrene, or meta- methylstyrene, or ortho- methylstyrene, or styrene) with i-Pr 2 NBCl 2 while cooling to 0 °C for 1 h in presence of Mg (powder) and catalyst Cp 2 TiCl 2 in molar ratio of i-Pr 2 NBCl 2 : α-olefin : Mg : Cp 2 TiCl 2 = (10÷14) : 10 : 20 : (1.5÷2.5) in tetrahydrofuran in an inert atmosphere and further stirring at room temperature (~22–25 °C) for 6–8 hours. EFFECT: novel organoboron compounds which can be used in organic chemistry as substrates in cross-coupling reactions are obtained. 1 cl, 1 tbl, 4 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 734 345 C1 (51) МПК C07F 5/02 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК C07C 5/02 (2020.05); C07F 5/027 (2020.05) (21)(22) Заявка: 2019142061, 16.12.2019 (24) Дата начала отсчета срока действия патента: Дата регистрации: 15.10.2020 (45) Опубликовано: 15.10.2020 Бюл. № 29 2 7 3 4 3 4 5 (54) СПОСОБ ПОЛУЧЕНИЯ ТРАНС-1-АЛКЕНИЛ(ХЛОРДИИЗОПРОПИЛАМИНО)БОРАНОВ (57) Реферат: Изобретение относится к способу получения орто-метилстирол, или стирол) с i-Pr2NBCl2 при транс-1-алкенил(хлордиизопропиламино)охлаждении до 0°С в течение 1 ч в присутствии боранов общей формулы (1а-г): Mg (порошок) и катализатора Cp2TiCl2 при R U (56) Список документов, цитированных в отчете о поиске: EUZENAT L. et al, Stereospecific palladium-catalyzed borylation reaction of 1alkenyl halides with diispropylaminoborane, J. Organomet. Chem., 2005, v. 690, no. 11, p. 27212724. IWADATE N. et al, Rhodium-catalyzed Dehydroborylation of Styrenes with Naphthalene1,8-diaminatoborane [(dan)BH]: New Synthesis of Masked β-Borylstyrenes as New (см. прод.) где (a) R = пара-Ме, (б) R = мета-Ме, (в) R = орто-Ме, (г) R = Н. ...

Hydrogenation of unsaturated hydrocarbons

Process for reaction of organic compounds and catalyst therefor

(57)【要約】 【課題】 担体に適用された、活性金属としてルテニウ ムを単独か又は少なくとも１種のＩｂ、ＶＩＩｂ又はＶ ＩＩＩｂ族金属と一緒に、触媒の全重量に対して、０． ０１〜３０重量％の量で包含する触媒の存在で有機化合 物を反応させ、非常に高い収率又は殆ど定量的変換率が 達成される方法および触媒そのものを提供する。 【解決手段】 担体の細孔容積の１０〜５０％が５０ｎ ｍ〜１００００ｎｍの範囲内の孔径を有するマクロ細孔 からなり、担体の細孔容積の５０〜９０％が２〜５０ｎ ｍの範囲内の孔径を有するメソ細孔からなり、該細孔容 積の和は１００％である。 【効果】 反応、好ましくは水素化の間副生成物又は分 解生成物の最小含量しか形成せず、反応生成物は高い純 度で得られる。

Process for the selective hydrogenation of poly-unsaturated hydrocarbons in hydrocarbon mixtures

In c>3 gas streams, alkynes, alkadienes, and alkenynes are selectively hydrogenated to the corresponding monoenes by liq. -phase hydrogenation (1-3.0 MPa at 5-75≰C) over 0.5% Pd/Al2O3 in the presence of stoichiometric or twice-stoichiometric H and <10.0 ppm CO with no alkene isomerization or other side reactions. Thus, a C4 stream containing 48.2% 1-butene and butadiene 5140, butyne 52, and butenyne 12 ppm, was hydrogenated at 21≰C and 1.3 MPa in the presence of near-stoichiometric H and 1.8 ppm CO to yield a stream containing 48.4% 1-butene, 2 ppm butadiene, and <1 ppm each butyne and butenyne

Method for producing once unsaturated hydrocarbons c3-c5

Изобретение касаетс  нефтехимического производства алифатических не- насьщенных углеводородов, в частности способа получени  однократно не насыщенных углеводородов С,-Cj гидрированием исходной смеси, содержащей Cj-Cj-aTOMOB углерода углеводородов с одной двойной св зью, с сопр женными и/или кумулированными двойными св з ми, и/или ацетиленовыми тройными св з ми на катализаторе, содержащем 0,1-2,0 мас.%. паллади  на окиси алюмини  или активном угле в присутствии окиси углерода. С целью повышени  выхода целевого продукта (за счет предотвращени  изомеризации двойной св зи) используют исходную смесь, содержащую 0,00004-0,001 мас.% растворенной окиси углерода и 1,01- 1,98-кратное (стехиометрическое) количество растворенного водорода, и гидрирование провод т при 0-75 С и давлении, обеспечивающем нахождение исходной смеси в гомогенной жидкой фазе. При гидрировании исходной смеси , содержащей 48,2 мас.% бутена-1 и бутадиена, бутина и бутенина соответственно в количествах 5140, 56 и . 12 ч/млн, получают продукт с содержанием бутена-1 48,4 мас.% и бутадиена , бутина и бутенина соответственно 4, 1 и 1 ч/млн. 10 табл. СО СА) О О см The invention relates to the petrochemical production of aliphatic unsaturated hydrocarbons, in particular, the method of producing once-saturated hydrocarbons C, -Cj by hydrogenating a feed mixture containing Cj-Cj-aTOMOB carbon hydrocarbons with one double bond, conjugated and / or cumulated double bonds mi and / or acetylenic triple bonds on a catalyst containing 0.1-2.0 wt.%. palladium on alumina or active carbon in the presence of carbon monoxide. In order to increase the yield of the target product (by preventing the isomerization of a double bond), an initial mixture containing 0.00004-0.001% by weight of dissolved carbon monoxide and 1.01-1.98-fold (stoichiometric) amount of dissolved hydrogen is used, and hydrogenation carried out at 0-75 ° C and pressure, ensuring that the initial mixture is in the homogeneous liquid phase. When ...

The method of obtaining anthracene or its derivatives

Method for producing aromatic hydrocarbon

Method of producing cyclopentenes or ethylene

In a process for the selective hydrogenation of polyunsaturated compounds, by means of a catalyst system, the hydrogenation is carried out in gaseous phase in the presence of a catalyst of a metal of the eight group of the Periodical Table, partially deactivated by a deactivating system.

Patent JPS5019521B1

Process for the preparation of high purity paraffin compounds

본 발명은 고순도 파라핀 화합물의 제조방법에 관한 것으로서, 더욱 상세하게는 올레핀화합물과 디메틸에테르 등과 같은 극성화합물을 함유하는 파라핀 화합물의 원료를 수소화 반응 시켜서 파라핀 화합물로 정제한 후 이를 활성화된 고체산 촉매를 이용하여 극성화합물을 흡착제거 시켜서 특히 고분자 중합용 용매 등에 유용한 고순도의 파라핀 화합물을 제조하는 방법에 관한 것이다. The present invention relates to a method for producing a high-purity paraffin compound, and more particularly, a raw material of a paraffin compound containing a polar compound such as an olefin compound and a dimethyl ether is hydrogenated to purify the paraffin compound, and then to activate the solid acid catalyst. The present invention relates to a method for preparing a high purity paraffin compound, which is particularly useful for solvents for polymer polymerization by adsorption and removal of polar compounds.

Method for producing butadiene from n-butane

The invention relates to a method for producing butadiene from n-butane comprising the following steps: A) provision of a feed gas stream (a) containing n-butane; B) introduction of the feed gas stream (a) containing n-butane into at least one first dehydrogenation zone and the non-oxidative catalytic dehydrogenation of n-butane to obtain a product gas stream (b) containing n-butane, 1-butene, 2-butene, butadiene, hydrogen, low-boiling minor constituents, optionally carbon oxides and optionally water vapour; C) introduction of the product gas stream (b) of the non-oxidative catalytic dehydrogenation and a gas containing oxygen into at least a second dehydrogenation zone and the oxidative dehydrogenation of n-butane, 1-butene and 2-butene to obtain a product gas stream (c) containing n-butane, 2-butene, butadiene, low-boiling minor constituents, carbon oxides and water vapour, said stream having a higher butadiene content than the product gas (b); D) isolation of the low-boiling minor constituents and the water vapour to obtain a C4 product gas stream (d), which essentially consists of n-butane, 2-butene and butadiene; E) separation of the C4 product gas stream (d) into a stream (e1), which essentially consists of n-butane and 2-butene and a useful product stream (e2), which essentially consists of butadiene, by extractive distillation; F) return of the stream (e1) to the first dehydrogenation zone.

Prepn of partially saturated hydrocarbons

A monomeric unsatd. cpd. is polymerised in pres. of a homogeneous catalyst contg. a metal or metallic cpd. and the crude reactn. product contg. residual catalyst is subjected to hydrogenation. The catalyst contg. Ni, Ti or Co. By this process, a normal 2-stage process is converted into a single stage process using a homogeneous catalyst with an increase in yield.

Production of anthracene from 2-methyl diphenyl methanes in presence of sulfur

IN THE PREPARATION OF ANTHRACENES BY THE THERMAL CONVERSION OF A 2-METHYL DIPHENYL METHANE, THE IMPROVEMENT WHICH COMPRISES EFFECTING THE THERMAL CONVERSION IN THE PRESENCE OF A SMALL AMOUNT OF SULFUR IN ELEMENTARY OR COMBINED FORM. THE TEMPERATURE IS PREFERABLY ABOUT 400 TO 800* C. AND THE SULFUR MAY BE ORGANIC OR INORGANIC E.G. SULFUR VAPOR OR CARBON DISULFIDE.

GAS SELECTIVE HYDROGENATION PROCESS OF POLYUNSATURATED COMPOUNDS

CATALYST FOR HYDROGENATION BY HYDROGEN OF UNSATURATED HYDROCARBONS AND METHOD FOR PREPARING THE SAME

LE CATALYSEUR POUR L'HYDROGENATION PAR L'HYDROGENE D'HYDROCARBURES NON SATURES EST UNE MEMBRANE REALISEE EN ALLIAGE A 80-95 MASSIQUES DE PALLADIUM ET A 5-20 MASSIQUES DE RUTHENIUM OU DE RHODIUM ET COMPOSEE D'UNE COUCHE NON POREUSE ET D'UNE COUCHE POREUSE DISPOSEE SUR UNE FACE OU SUR LES DEUX FACES DE LA PREMIERE COUCHE; LA SURFACE POREUSE COMPORTE 150-820 CM DE PORES AU CM DE LA SURFACE DE LA MEMBRANE, LE RAPPORT DE L'EPAISSEUR DE LA COUCHE POREUSE A L'EPAISSEUR DE LA COUCHE NON POREUSE ETANT DE 1(5-1000), RESPECTIVEMENT. LE PROCEDE DE PREPARATION DU CATALYSEUR CONSISTE A APPLIQUER A LA SURFACE DE LA MEMBRANE REALISEE EN ALLIAGE SUSDIT, SUR UNE FACE OU SUR DEUX FACES, DU CUIVRE OU DU MERCURE, A ABANDONNER LA MEMBRANE AVEC LE CUIVRE APPLIQUE DESSUS A 300-800 C, ET AVEC LE MERCURE APPLIQUE DESSUS A UNE TEMPERATURE DE - 10 A 150 C, ET A REALISER L'EXTRACTION CHIMIQUE DU CUIVRE OU DU MERCURE. THE CATALYST FOR HYDROGENATION WITH HYDROGENES OF NON-SATURATED HYDROCARBONS IS A MEMBRANE MADE OF PALLADIUM MASS 80-95 MASS AND 5-20 MASS OF RUTHENIUM OR RHODIUM AND COMPOSED OF A NON-POROUS LAYER AND A POROUS LAYER DISPOSED ON ONE OR THE BOTH SIDES OF THE FIRST LAYER; THE POROUS SURFACE HAS 150-820 CM OF PORES AT THE CM OF THE SURFACE OF THE MEMBRANE, THE RATIO OF THE THICKNESS OF THE POROUS LAYER TO THE THICKNESS OF THE NON-POROUS LAYER BEING 1 (5-1000), RESPECTIVELY. THE PROCESS FOR PREPARING THE CATALYST CONSISTS OF APPLYING TO THE SURFACE OF THE MEMBRANE MADE OF ALLOY SUSENDED ON ONE OR ON TWO SIDES OF COPPER OR MERCURY, ABANDONING THE MEMBRANE WITH COPPER APPLIED ON AT 300-800 C, AND WITH MERCURY APPLIED TO A TEMPERATURE OF -10 TO 150 C, AND TO ACHIEVE THE CHEMICAL EXTRACTION OF COPPER OR MERCURY.

Process for obtaining aromatic hydrocarbons

Process for preparing aromatic hydrocarbons

HYDROGENATION OF FATTY ESTERS.

L'invention a pour objet un procédé d'hydrogénation d'esters gras en alcools en utilisant un catalyseur de cuivre/zinc. On maintient l'activité du catalyseur par traitement à la vapeur d'eau par exemple en incorporant 1,0 à 1,8% en poids d'eau dans l'alimentation d'ester. Préservation de l'activité du catalyseur pendant une longue période. The subject of the invention is a process for the hydrogenation of fatty esters into alcohols using a copper / zinc catalyst. The activity of the catalyst is maintained by treatment with steam, for example, by incorporating 1.0 to 1.8% by weight of water in the ester feed. Preservation of catalyst activity for a long time.

CATALYST FOR HYDROGENATION BY HYDROGEN OF UNSATURATED HYDROCARBONS AND PROCESS FOR THE PREPARATION THEREOF

Selective hydrogenation catalysts and their method of preparation

Patent FR2127310A5

Hydrogenation of unsatd cpds - in a homogeneous then a heterogenous catalytic process

Hydrogenation is effected as in FR 6922455, where 99-99.9% of the cpd. is converted in the first step with a homogenous catalyst (pref. based on Ni or Co) and reaction continued in a heterogenous second step. Pref. dodecatriene is reduced to dodecane. Yield is raised by minimising damage by exothermic heat of second step.

A process for the selective hydrogenation of olefins

올레핀 및 방향족 화합물을 포함하는 탄화수소계 공급물에 함유되어 있는 올레핀의 선택적 수소화 방법. A process for selective hydrogenation of olefins contained in a hydrocarbon-based feed comprising olefins and aromatic compounds. 올레핀, 방향족 화합물, 선택적 수소화 Olefins, aromatics, selective hydrogenation

Process for the destructive hydrogenation of distillable carbonaceous materials

Gp vi metal carboxyaltes - from sublimable reactants in solvents of different boiling pts

Org. derivs. of metals (esp. carboxylates) are produced from sublimable reactants (esp. gp VI metal carbonyls) in the presence of >=2 solvents of different b.pts. Reaction is rapid gives high yields and does not entrain troublesome solvents. Products (esp. Mo carboxylates) are very active hydrogenation catalysts. used in conjunction with organo Al hydrides.

Methane procuding apparatus and controlling method thereof

본 발명은 메탄 생성 장치 및 이의 제어 방법에 관한 것이다. 구체적으로, 본 발명의 실시예에 따르면, 수소와 이산화탄소를 포함하는 원료가스를 공급받아서 메탄을 생성하고, 상기 원료가스로부터 메탄을 생성하는 반응을 위한 촉매가 내부에 충진된 촉매 튜브가 내부에 제공되는 제1 반응기, 상기 제1 반응기와 연결되어 냉매를 공급하는 냉매 공급 탱크, 상기 제1 반응기와 상기 냉매 공급 탱크를 연결하는 냉매 공급 라인 상에 제공되는 유량 조절 밸브, 상기 냉매 공급 탱크에 연결되어 상기 냉매 공급 탱크 내에서 상기 냉매가 증발되어 발생된 기체를 상기 냉매 공급 탱크의 외부로 배출하는 기체 배출 라인 상에 제공되는 압력 조절 밸브, 상기 제1 반응기의 후단에 제공되고, 상기 원료가스가 상기 촉매와 반응하여 생성된 메탄을 포함하는 1차 전환가스의 온도를 측정하는 온도 센서, 및 상기 온도 센서에서 측정된 온도에 따라 상기 유량 조절 밸브 및 상기 압력 조절 밸브를 제어하는 제어부를 포함하는, 메탄 생성 장치 및 이를 제어하는 방법이 제공될 수 있다.

FOERFARANDE FOER SELEKTIV HYDRERING AV MAONGFALDIGT OMAETTADE KOLVAETEN I KOLVAETEBLANDNINGAR

Method for making organic compound reaction under condition of existence of ruthenium catalyst on carrier

一种使有机化合物在催化剂存在下反应的方法，所述的催化剂包含占催化剂总重量的0.01至30wt%的、涂敷于载体的、单独或与至少一种IB、VIIB或VIIIB族金属一起作为活性金属的钌，所述的载体中，孔径在50nm至10,000nm范围的大孔占载体孔体积10至50%，且孔径为2至50nm的中孔占载体孔体积的50至90%，所述的孔体积之和为100%。

Method for making organic compound reaction under condition of existence of ruthenium catalyst on carrier

一种使有机化合物在催化剂存在下反应的方法,所述的催化剂包含占催化剂总重量的0.01至30wt%的、涂敷于载体的、单独或与至少一种ⅠB、ⅦB或ⅧB族金属一起作为活性金属的钌,所述的载体中,孔径在50nm至10,000nm范围的大孔占载体孔体积10至50%,且孔径为2至50nm的中孔占载体孔体积的50至90%,所述的孔体积之和为100%。

Process for the selective hydrogenation of polyunsaturated hydrocarbons in hydrocarbon mixtures

Process for the production of aromatic hydrocarbons by catalytic aromatization of diisobutylene and / or triisobutylene and / or their hydrogenation products

Crystalline ferroaluminophosphates

Novel class of crystalline microporous ferroaluminophosphate compositions containing as lattice constituents in addition to AlO 2 and PO 2 structural units, ferric and/or ferrous iron in tetrahedral coordination with oxygen atoms. These compositions are prepared hydrothermally using organic templating agents and are suitably employed as catalysts or adsorbents.

Process for the selective hydrogenation of polyunsaturated hydrocarbons in mixtures of hydrocarbons

Purifying organophosphorus compounds contaminated with chlorine

The invention relates to a process for the purification of a contaminated organophosphorus product which comprises at least one organophosphorus compound and, as contaminant, at least one chlorine compound. It is based on the object of indicating a purification method in which the chlorine content of an organophosphorus product which comprises at least one organophosphorus compound and at least one chlorine compound as contaminant, can be reduced from originally 1000 to 100 000 ppm to a total chlorine content between 10 ppm and 10 000 ppm. This is achieved by a process with the steps: a) provision of the contaminated organophosphorus product; b) complete dissolution of the contaminated organophosphorus product in a solvent to give a contaminated solution; c) separation of the contaminated solution by means of a filter and/or by means of a membrane separation unit to give a purified solution; d) removal of the solvent from the purified solution to give a purified organophosphorus product.

Method for producing butadiene from n-butane

本发明涉及一种从正丁烷制备丁二烯的方法，该方法包括以下步骤：A)提供含有正丁烷的进料气流(a)；B)将含有正丁烷的进料气流(a)加入至少一个第一脱氢区域，并使正丁烷进行非氧化性催化脱氢，得到含有正丁烷、1－丁烯、2－丁烯、丁二烯、氢气和低沸点次级组分的产物气流(b)，其中有或没有碳氧化物和有或没有水蒸气；C)将非氧化性催化脱氢的产物气流(b)和含氧气体加入至少一个第二脱氢区域，并使正丁烷、1－丁烯和2－丁烯进行氧化脱氢，得到含有正丁烷、2－丁烯、丁二烯、低沸点次级组分、碳氧化物和水蒸气的产物气流(c)，所述产物气流(c)具有的丁二烯含量高于产物气流(b)；D)除去低沸点次级组分和水蒸气，得到基本含有正丁烷、2－丁烯和丁二烯的C 4 产物气流(d)；E)通过萃取蒸馏将C 4 产物气流(d)分离成基本含有正丁烷和2－丁烯的料流e1以及基本含有丁二烯的有价值产物料流e2；F)将料流e1循环到第一脱氢区域中。

Patent JPS5910258B2

Process for preparing aromatic hydrocarbons

Hydrogen recycle and hydrogen chloride recovery in an alkylation process.

Se proporciona un proceso de alquilación que comprende: separar y reciclar un gas de hidrógeno y un cloruro de hidrógeno de un gas de escape de un reactor de hidrogenación; donde el gas de hidrógeno se recicla al reactor de hidrogenación y donde el cloruro de hidrógeno se recicla a un reactor de alquilación. También se proporciona una unidad de proceso de alquilación para llevar a cabo este proceso.

Process for the production of phenanthrene.

Hydrocarbon aromatization process

Manufacture of polycyclic hydrocarbons

PROCESS FOR THE CATALYTIC CONVERSION OF HYDROCARBONS WITH RECOVERY AND RECIRCULATION OF PART OF THE REGENERATED CATALYST.

Catalyst for the selective hydrogenation of olefins and acetylene compounds

Method of producing aromatic hydrocarbons

Titanium-aluminum-silicon-oxide molecular sieve compositions

Titanium-aluminum-silicon-oxide molecular sieves having three-dimensional micoporous crystalline framework structures of tetrahedral oxide units TiO2, AlO2 and SiO2 are disclosed having use as molecular sieves and as catalyst compositions in hydrocarbon conversion and other processes.

Catalyst and process for the selective hydrogenation of multi-unsaturated organic compounds

Catalyst for the selective hydrogenation of multi-unsaturated organic compounds, in particular of diolefins and dienes in mixtures with other hydrocarbons; the catalyst is characterized by (A) a metal component from one or more elements of Group VIII of the Periodic Table on (B) a support material on the basis (b1) of one or more n-semiconducting oxides of one or more elements from the Subgroups IVb, Vb and VIb of the Periodic Table or of thorium or cerium, or respectively on the basis (b2) of one or more n-semiconducting mixed oxide systems of the formula Me2Me1(0)x, where Me1 is an element of the group defined in (b1), Me2 an alkaline earth metal or an element different from Me1 or the group defined in (b1), and x signifies the number of oxygen atoms required for the saturation of Me1 and Me2 to the range of an n-semiconducting state; the hydrogen chemisorption capacity, expressed as the atomic ratio between chemisorbed hydrogen atoms and metal atoms of the metal component (A) present on the surface of the metal particles, (H/MeA), being at least 0.6:1.

process for preparing butadiene from n-butane

PROCESSO PARA PREPARAR BUTADIENO A PARTIR DE N-BUTANO. A invenção refere-se a um processo para produzir butadieno a partir de n-butano compreendendo as seguintes etapas: A) provisão de uma corrente gasosa de alimentação (a) contendo n-butano; B) introdução da corrente gasosa de alimentação (a) contendo n-butano em pelo menos uma primeira zona de desidrogenação e a desidrogenação catalítica não-oxidativa de n-butano para obter uma corrente gasosa de produto (b) contendo n-butano, 1 -buteno, 2-buteno, butadieno, hidrogênio, constituintes menores de ebulição baixa, opcionalmente óxidos de carbono e opcionalmente vapor; C) introdução da corrente gasosa de produto (b) da desidrogenação catalítica não-oxidativa e um gás contendo oxigênio em pelo menos uma segunda zona de desidrogenação e a desidrogenação oxidativa de n-butano, 1 -buteno e 2-buteno para obter uma corrente gasosa de produto (c) contendo n-butano, 2- butano, butadieno, constituintes menores de ebulição baixa, óxidos de carbono e vapor, a citada corrente possuindo um conteúdo de butadieno maior do que o gás produto (b); D) isolamento dos constituintes menores de ebulição baixa e vapor para obter uma corrente gasosa de produto C~ 4~ (d), que essencialmente consiste de n-butano, 2-buteno e butadieno; E) separação da corrente gasosa de produto C~ 4~ (d) em uma corrente (ei), que essencialmente consiste de n-butano e 2-buteno e uma corrente de produto bruto (e2), que essencialmente consiste de butadieno, por destilação extrativa; F) retomo da corrente (ei) para a primeira zona de desidrogenação. PROCESS FOR PREPARING BUTDIENE FROM N-BUTANE. The invention relates to a process for producing butadiene from n-butane comprising the following steps: A) providing a supply gas stream (a) containing n-butane; B) introducing the n-butane-containing feed stream (a) into at least a first dehydrogenation zone and the non-oxidative catalytic de-hydrogenation of n-butane to obtain a n-butane-containing product (b) stream, 1 - ...

PROCEDURE FOR SELECTIVE HYDROGENATION IN GAS PHASE OF POLYUMAATED CARBON HYDRODES

PROCESS FOR THE SELECTIVE HYDROGENATION OF MULTIPLE UNSATURIZED COMPOUNDS IN THE GAS PHASE

Patent GB1264255A

1,264,255. Two-stage hydrogenation. INSTITUT FRANCAIS DU PETROLE DES CARBURANTS ET LUBRIFIANTS. 26 June, 1970 [2 July, 1969], No. 31237/70. Heading C5E. Unsaturated hydrocarbons are hydrogenated in two stages, 20-99% of the hydrocarbons being converted in liquid phase in the first stage in the presence of a catalyst in homogeneous phase; and the conversion being completed in a second stage in the presence of a fixed bed of catalyst in heterogeneous phase. The first stage catalyst may be obtained by reaction of a transition metal compound with a compound containing Al-H bonds. Preferred catalysts are the reaction products of LiAlH(OtBu) 3 or AlH(OtBu) 2 with cobalt naphthenate. The second stage catalyst may be a Group VIII metal e.g. Pt, Pd or Ni supported on a carrier. The product of the first stage may be passed though a bed of absorbent e.g. Al 2 O 3 or SiO 2 before the second stage. The feedstock may be monodi- or tri-olefins, acyclic or cyclic. Examples describe the hydrogenation of cyclododecatriene to cyclododecane, cyclopentadiene to cyclopentane, and cyclooctadiene to cyclooctane.

Patent FR2180104B1

Hydrocarbon conversion

Conversion of diolefin hydrocarbons to aromatic hydrocarbons

Hydrogen storage materials comprising naphtalene group and the method for hydrogen storage and release using the same

Proposed are a naphthalene-based hydrogen storage material including a naphthalene group, the naphthalene-based hydrogen storage material being capable of being used as a hydrogen storage media for supplying hydrogen to a device using hydrogen such as a fuel cell and a hydrogen combustion device, and to a method of storing and releasing hydrogen using the same. The hydrogen storage material can exhibit a significantly high hydrogen capacity, and can have excellent cost competitiveness with the use of a low-cost organic compound which is commercially available in the art.

Process for the production of high alcohols by catalytic hydrogenation of alkyl esters of carboxylic acids

Process for hydrogenating unsaturated organic compounds

THIS INVENTION RELATES TO A TWO-STEP PROCESS FOR HYDROGENATING UNSATURATED ORGANIC COMPOUNDS, THE FIRST STEP BEING CONDUCTED IN HOMOGENEOUS PHASE AND THE SECOND STEP IN HETEROGENEOUS PHASE.

Process for the production of alkyl aryl hydrocarbons

Dehydrocyclization process

Process for selective hydrogenation of hydrocarbons

A kind of efficient aromatization method of non-aromatic lighter hydrocarbons

本发明公开了一种非芳轻烃的高效芳构化方法，将非芳轻烃原料与稀释氢气混合脱水后进入反应系统进行芳构化反应；产物进入气液分离器I进行气液分离，气相物料增压后，进入气液分离器II进行气液分离，气相物料部分作为稀释氢气返回或排入氢气回收系统；气液分离器I所得液相物料进入脱戊烷塔分离，塔顶物料与气液分离器II所得液相物料进入脱丁烷塔分离，塔底物料进入芳烃抽提塔分离；抽提塔塔顶物料进入脱二甲基丁烷塔；脱二甲基丁烷塔塔顶和塔底物料作为汽油调和组分回收，侧线采出物料返回反应系统；从芳烃抽提塔底部得到芳烃；该方法大幅提高了轻烃原料的芳构化利用率，解决了轻重组分在系统内的累积问题。

Process for the reaction of an organic compound in the presence of a supported ruthenium catalyst

Manufacture of aromatic hydrocarbons

Low surface acidity platinum-group metal catalysts for hydrogenation- and dehydrogenation reactions