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Небесная энциклопедия

Космические корабли и станции, автоматические КА и методы их проектирования, бортовые комплексы управления, системы и средства жизнеобеспечения, особенности технологии производства ракетно-космических систем

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Мониторинг СМИ

Мониторинг СМИ и социальных сетей. Сканирование интернета, новостных сайтов, специализированных контентных площадок на базе мессенджеров. Гибкие настройки фильтров и первоначальных источников.

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Поддерживает ввод нескольких поисковых фраз (по одной на строку). При поиске обеспечивает поддержку морфологии русского и английского языка
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Применить Всего найдено 3425. Отображено 100.
05-01-2012 дата публикации

Process for producing alkylated aromatic compounds and process for producing phenols

Номер: US20120004471A1
Принадлежит: Mitsui Chemicals Inc

According to a process of the invention, a ketone, an aromatic compound and hydrogen as starting materials are reacted together in a single reaction step to produce an alkylaromatic compound in high yield. A process for producing phenols in the invention includes a step of performing the above alkylation process and does not increase the number of steps compared to the conventional cumene process. The process for producing alkylated aromatic compounds includes reacting an aromatic compound such as benzene, a ketone such as acetone and hydrogen in the presence of a solid acid substance, preferably a zeolite, and a silver-containing catalyst.

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08-03-2012 дата публикации

Zeolite-palladium complex, method for producing the same, catalyst containing the complex, and method for producing a coupling compound by using the catalyst

Номер: US20120059191A1
Принадлежит: Individual

There is provided a substance having much higher catalytic activity for a Suzuki-Miyaura coupling reaction than conventional heterogenous catalysts. The present invention provides a zeolite-palladium complex including USY-zeolite and Pd supported on the USY-zeolite, the Pd having a Pd—Pd coordination number of 4 or less and an oxidation number of 0.5 or less.

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29-03-2012 дата публикации

Removal of Hydrogen From Dehydrogenation Processes

Номер: US20120078024A1
Принадлежит: Fina Technology Inc

A process and system for dehydrogenating certain hydrocarbons is disclosed. The process includes contacting a dehydrogenatable hydrocarbon with steam in the presence of a dehydrogenation catalyst to form hydrogen and a dehydrogenated hydrocarbon. Some of the hydrogen is then removed and some of the remaining dehydrogenatable hydrocarbon is dehydrogenated.

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21-06-2012 дата публикации

Methods for removing unsaturated aliphatic hydrocarbons from a hydrocarbon stream using an acidic molecular sieve

Номер: US20120157739A1
Принадлежит: UOP LLC

Disclosed is a method for removing unsaturated aliphatic compounds from a hydrocarbon feed stream by contacting the hydrocarbon feed stream with an acidic molecular sieve to produce a hydrocarbon effluent stream having a lower unsaturated aliphatic content relative to the hydrocarbon feed stream. The hydrocarbon feed stream comprises an aromatic compound, a nitrogen compound, and an unsaturated aliphatic compound.

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08-11-2012 дата публикации

Dehydrogenation Process

Номер: US20120283494A1
Принадлежит: ExxonMobil Chemical Patents Inc

In a dehydrogenation process a hydrocarbon stream comprising at least one non-aromatic six-membered ring compound and at least one five-membered ring compound is contacted with a first catalyst comprising at least one metal component and at least one support and a second catalyst. The first catalyst is utilized to convert at least a portion of the at least one non-aromatic six-membered ring compound in the hydrocarbon stream to at least one aromatic compound and the second catalyst is utilized to convert at least a portion of the at least one five-membered ring compound in the hydrocarbon stream to at least one paraffin.

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22-11-2012 дата публикации

Process for alkylation of toluene to form styrene and ethylbenzene

Номер: US20120296136A1
Автор: Sivadinarayana Chinta
Принадлежит: Fina Technology Inc

A process is disclosed for making styrene and/or ethylbenzene by reacting toluene with a C 1 source over a catalyst in at least one radial reactor to form a product stream comprising styrene and/or ethylbenzene.

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14-03-2013 дата публикации

Pre-carburized molybdenum-modified zeolite catalyst and use thereof for the aromatization of lower alkanes

Номер: US20130066126A1
Автор: Suman Kumar Jana
Принадлежит: Saudi Basic Industries Corp

The present invention relates to a method for producing a zeolite catalyst useful for aromatization of a lower alkane, a zeolite catalyst useful for aromatization of a lower alkane obtainable by said method and a process for aromatization of a lower alkane using the zeolite catalyst of the present invention.

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28-03-2013 дата публикации

Conversion of methylamine to olefin or mixture of olefins

Номер: US20130079576A1
Принадлежит: Dow Global Technologies LLC

Convert a methylamine (e.g. monomethylamine, dimethylamine and trimethylamine) to a mixture of olefins (e.g. ethylene, propylene and butylene) by placing the methylamine, optionally in a mixture with at least one of ammonia and an inert diluent, in contact with a microporous acidic silicoaluminophosphate catalyst or a microporous aluminosilicate catalyst.

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18-04-2013 дата публикации

Heavy alkylbenzene transalkylation operating cost reduction

Номер: US20130096357A1
Принадлежит: UOP LLC

A process for increasing the production of monoalkylbenzenes is presented. The process includes utilizing a transalkylation process to convert dialkylbenzenes to monoalkylbenzenes. The transalkylation process recycles a portion of the effluent stream from the transalkylation reactor back to the feed of the transalkylation reactor. The recycled dialkylbenzenes and a portion of the recycled benzene are converted to monoalkylbenzenes.

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23-05-2013 дата публикации

Production of renewable aromatic compounds

Номер: US20130130345A1
Принадлежит: JNF BIOCHEMICALS LLC

The invention provides a process for producing a variety renewable aromatic compounds such as benzene, toluene, xylenes, and cumene, as well as compounds derived from these including, for example, aniline, benzoic acid, cresol, cyclohexane, cyclohexanone, phenol and bisphenol A, toluene di-isocyanate, isophthalic acid, phthalic anhydride, terephthalic acid and dimethyl terephthalate. The invention also provides for renewable forms of these aromatic compounds.

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27-06-2013 дата публикации

Catalytic refining of terpenes of pulp origin

Номер: US20130165721A1
Принадлежит: STORA ENSO OYJ

Biobased p-cymene and methods of producing same, which can further be converted to terephtalate. Further, a method is described for converting crude sulfate turpentine recovered from chemical wood pulping into p-cymene and eventually to terephtalic acid of biological origin, and and products thereof respectively. In said method, both conversion and desulfurization is realized in one reaction step. The disclosure is also related to use of zeolite catalysts in said method.

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04-07-2013 дата публикации

"process for producing cycloalkylaromatic compounds"

Номер: US20130172514A1
Автор: Teng Xu, Wenyih F. Lai
Принадлежит: ExxonMobil Chemical Patents Inc

In a process for producing a cycloalkylaromatic compound, an aromatic compound, hydrogen and at least one diluent are supplied to a hydroalkylation reaction zone, such that the weight ratio of the diluent to the aromatic compound supplied to the hydroalkylation reaction zone is at least 1:100. The aromatic compound, hydrogen and the at least one diluent are then contacted under hydroalkylation conditions with a hydroalkylation catalyst in the hydroalkylation reaction zone to produce an effluent comprising a cycloalkylaromatic compound.

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04-07-2013 дата публикации

Supported nano sized zeolite catalyst for alkylation reactions

Номер: US20130172649A1
Принадлежит: Fina Technology Inc

A catalyst containing nanosize zeolite particles supported on a support material for alkylation reactions, such as the alkylation of benzene to form ethylbenzene, and processes using such a catalyst is disclosed.

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05-09-2013 дата публикации

Silica composite, method for producing the same, and method for producing propylene using the silica composite

Номер: US20130231515A1
Принадлежит: Asahi Kasei Chemicals Corp

The present invention provides a method for producing a silica composite by the steps of: preparing a raw material mixture containing silica and zeolite; drying the raw material mixture to obtain a dried product; and calcining the dried product, wherein the method comprising the step of allowing the raw material mixture to contain phosphoric acid and/or phosphate or bringing a solution of phosphoric acid and/or phosphate into contact with the zeolite and/or the dried product, or a combination thereof to thereby adjust a phosphorus content in the silica composite to 0.01 to 1.0% by mass based on the total mass of the silica composite.

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12-09-2013 дата публикации

Process for producing cumene

Номер: US20130237730A1

A process of producing isopropyl benzene which solves the problem of high amount of n-propyl benzene according to the prior art. The process separates the polyisopropyl benzene through a suitable rectification into two streams of relatively lighter and heavier components, wherein the content of diisopropylbenzene in the stream of relatively lighter components is controlled to be at least greater than 95 wt %, and the content of tri-isopropyl benzene in the stream of relatively heavier components is controlled to be at least greater than 0.5 wt %. Such a technical solution subjecting the two streams respectively to the transalkylation solves the problem raised from the prior art, and is useful for the industrial production of isopropyl benzene.

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31-10-2013 дата публикации

Catalyst for producing monocyclic aromatic hydrocarbon and production method of monocyclic aromatic hydrocarbon

Номер: US20130289325A1
Принадлежит: JX Nippon Oil and Energy Corp

The catalyst for producing aromatic hydrocarbon is for producing monocyclic aromatic hydrocarbon having 6 to 8 carbon number from oil feedstock having a 10 volume % distillation temperature of 140° C. or higher and a 90 volume % distillation temperature of 380° C. or lower and contains crystalline aluminosilicate and phosphorus. A molar ratio (P/Al ratio) between phosphorus contained in the crystalline aluminosilicate and aluminum of the crystalline aluminosilicate is from 0.1 to 1.0. The production method of monocyclic aromatic hydrocarbon is a method of bringing oil feedstock having a 10 volume % distillation temperature of 140° C. or higher and a 90 volume % distillation temperature of 380° C. or lower into contact with the catalyst for producing monocyclic aromatic hydrocarbon.

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27-02-2014 дата публикации

3,3',4,4'-tetraalkyl cyclohexylbenzene and method for producing same

Номер: US20140058143A1
Принадлежит: UBE Industries Ltd

The present invention relates to a 3,3′,4,4′-tetraalkyl cyclohexylbenzene represented by the general formula (1): wherein R represents an alkyl group having 1 to 4 carbon atoms, which may be easily converted into a 3,3′,4,4′-biphenyltetracarboxylic acid and a 3,3′,4,4′-biphenyltetracarboxylic dianhydride thereof, which are a starting material for a polyimide, via a 3,3′,4,4′-tetraalkylbiphenyl; and a method for producing the same.

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05-01-2017 дата публикации

CIT-10: A TWO DIMENSIONAL LAYERED CRYSTALLINE MICROPOROUS SILICATE COMPOSITION AND COMPOSITIONS DERIVED THEREFROM

Номер: US20170001872A1
Принадлежит:

This disclosure relates to a new crystalline microporous silicate solid, designated CIT-10, comprising a two dimensional layered structure, having an organic interlayer sandwiched between individual crystalline silicate layers. This CIT-10 material can be converted to a pure-silicate of RTH topology, as well as two new of pillared silicate structures, designated CIT-11 and CIT-12. This disclosure characterizes new materials and provides methods of preparing and using these new crystalline microporous solids. 1. A crystalline microporous silicate , designated CIT-10 , which exhibits a powder X-ray diffraction (XRD) pattern exhibiting at least five of the characteristic peaks at 7.6±0.2° , 8.7±0.2° , 10.3±0.2° , 18.8±0.2° , 20.3±0.2° , 21.8±0.2° , 22.4±0.2° , 22.7±0.2° , 22.9±0.2° , and 23.6±0.2° 2-theta.2. The crystalline microporous silicate of claim 1 , wherein the crystalline microporous silicate comprises a two dimensional layered structure claim 1 , having an organic material sandwiched between individual crystalline silicate layers.3. The crystalline microporous silicate of claim 2 , having a structure which is ordered along its two dimensional crystalline silicate layers claim 2 , but which exhibits disorder between its crystalline silicate layers claim 2 , as evidenced by RED (rotating electron diffraction) structure analysis.4. The crystalline microporous silicate of claim 1 , which exhibits an Si-MAS NMR spectrum having resonances at chemical shifts of −113 ppm claim 1 , −107 ppm claim 1 , and −102 ppm claim 1 , relative to tetramethylsilane (TMS).5. The crystalline microporous silicate of claim 4 , wherein the resonances at chemical shifts of −113 ppm claim 4 , −107 ppm claim 4 , and −102 ppm have relative integrated intensities of 8 claim 4 , 5 claim 4 , and 3 claim 4 , respectively.7. A crystalline microporous silicate claim 4 , designated CIT-11 claim 4 , which exhibits a powder X-ray diffraction (XRD) pattern exhibiting at least five of the ...

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04-01-2018 дата публикации

PRODUCTION OF HYDROCARBON LIQUIDS

Номер: US20180002248A1
Принадлежит:

A process to efficiently convert organic feedstock material into liquid non-oxygenated hydrocarbons in the Cto Ccarbon skeleton range is disclosed. The process can utilize gaseous, liquid or solid organic feedstocks containing carbon, hydrogen and, optionally, oxygen. The feedstock may require preparation of the organic feedstock for the process and is converted first into a synthesis gas containing carbon monoxide and hydrogen. The synthesis gas is then cleaned and conditioned and extraneous components removed, leaving substantially only the carbon monoxide and hydrogen. It is then converted via a series of chemical reactions into the desired liquid hydrocarbons. The hydrocarbons are suitable for combustion in a vehicle engine and may be regarded a replacement for petrol made from fossil fuels in the Cto Ccarbon backbone range. The process also recycles gaseous by-products back through the various reactors of the process to maximize the liquid hydrocarbon in the Cto Ccarbon skeleton range yield. 1. A process for producing a Cto Chydrocarbon fuel from organic material , comprising:a) applying a heat source to heat an organic feedstock and oxygen at substoichiometric conditions to a temperature sufficient for partial combustion of said organic feedstock to occur and then ceasing application of said heat source once partial combustion has commenced;b) partially combusting said organic feedstock so as to produce a synthesis gas stream, said synthesis gas stream containing at least carbon monoxide, carbon dioxide and hydrogen;{'sub': '10', 'c) substantially removing unwanted solid and liquid matter comprising oxides, ash and hydrocarbons having a carbon skeleton of greater than Cfrom said synthesis gas stream to produce a first cleaned synthesis gas stream containing at least carbon monoxide, carbon dioxide and hydrogen;'}d) compressing said first cleaned synthesis gas stream and substantially removing water;e) conditioning and further cleaning the first cleaned ...

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04-01-2018 дата публикации

Process for the Recovering of Paraxylene

Номер: US20180002253A1
Принадлежит:

Disclosed herein are processes for recovering paraxylene in which a first simulated moving bed adsorption unit is used to produce a paraxylene-rich extract stream that also contains a significant amount of the ethylbenzene and a paraxylene-depleted raffinate stream. Because a significant amount of the ethylbenzene is removed in the paraxylene-rich extract stream (at least enough to limit buildup in the isomerization loop), the paraxylene-depleted raffinate stream may be isomerized in the liquid phase. Avoiding vapor phase isomerization saves energy and capital, as liquid phase isomerization requires less energy and capital than the vapor phase isomerization process due to the requirement of vaporizing the paraxylene-depleted stream and the use of hydrogen, which requires an energy- and capital-intensive hydrogen recycle loop. 1. A process for recovering paraxylene , the process comprising:(a) introducing a hydrocarbon feed stream into a first simulated moving bed adsorption unit, wherein the hydrocarbon feed stream comprises a mixture of paraxylene (PX), metaxylene (MX), orthoxylene (OX), and ethylbenzene (EB);(b) introducing a desorbent stream into the first simulated moving bed adsorption unit, wherein the desorbent stream comprises desorbent;(c) withdrawing a first PX-rich extract stream from the first simulated moving bed adsorption unit, wherein the first PX-rich extract stream comprises desorbent, PX, and EB;(d) withdrawing a PX-depleted raffinate stream from the first simulated moving bed adsorption unit, wherein the PX-depleted raffinate stream comprises desorbent, MX, OX, and EB;(e) isomerizing at least a portion of the first PX-depleted raffinate stream at least partially in the liquid phase to produce an isomerized stream having a higher PX concentration than the first PX-depleted raffinate stream;(f) recycling at least a portion of the first isomerized stream to the first simulated moving bed adsorption unit; and(g) introducing the first PX-rich extract ...

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03-01-2019 дата публикации

Systems and Methods for Producing Naphthalenes and Methylnaphthalenes

Номер: US20190002367A1
Принадлежит:

A process for producing naphthalene or methylnaphthalenes from an alkane-containing stream. In an embodiment, the produce includes providing an alkane-containing feed stream to a reactor, and contacting the ethane-containing stream with an aromatization catalyst within the reactor. The aromatization catalyst comprises molecular sieve, and a dehydrogenation component. In addition, the process includes producing a reactor effluent stream from the reactor, and separating a product stream from the reactor effluent stream. The product stream comprises at least one or both of naphthalene and methylnaphthalene. 1. A process , comprising:(a) providing an alkane-containing feed stream to a reactor;(b) contacting the alkane-containing stream with an aromatization catalyst within the reactor, wherein the aromatization catalyst comprises molecular sieve, and a dehydrogenation component;(c) producing a reactor effluent stream from the reactor; and(d) separating a product stream from the reactor effluent stream, wherein the product stream comprises at least one or both of naphthalene and methylnaphthalene.2. The process of claim 1 , wherein the alkane-containing feed comprises a majority fraction of ethane.3. The process of claim 2 , wherein the molecular sieve of the aromatization catalyst comprises ZSM-5.4. The process of claim 3 , wherein the dehydrogenation component comprises gallium.5. The process of claim 4 , further comprising:(e) removing a majority of one or both of sulfur or nitrogen in the feed stream before providing the feed stream to the reactor in (a).6. The process of claim 5 , wherein the reactor effluent stream contains one or both of:less than 5 ppm sulfur; andless than 5 ppm of nitrogen.7. The process of claim 6 , wherein the contacting in (b) is carried out with a temperature of about 500° C. to about 625° C. claim 6 , a pressure of about 207 kPaa (30 psia) to about 522 kPaa (80 psia) claim 6 , and a WHSV of about 0.1 hrto about 10 hr.8. The process of claim ...

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01-01-2015 дата публикации

Catalyst used in the production of ethylene and propylene from methanol and/or dimethyl ether, method for preparing the same and method for using the same

Номер: US20150005559A1

The application provides a catalyst for producing ethylene and propylene from methanol and/or dimethyl ether, and a preparation and application thereof. In the present application, a molecular sieve catalyst co-modified by rare earth metals and silanization is utilized. First, the material containing methanol and/or dimethyl ether reacts on the catalyst to generate hydrocarbons. The hydrocarbons are separated into a C 1 -C 5 component and a C 6 + component. Then the C 6 + component is recycled to the feeding port and fed into the reactor after mixing with methanol and/or dimethyl ether. The above steps are repeated, to finally generate C 1 -C 5 products, in which the selectivity for ethylene and propylene can reach more than 90 wt % in the C 1 -C 5 component, so that the maximal yield can be achieved in the production of ethylene and propylene from methanol and/or dimethyl ether.

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08-01-2015 дата публикации

CATALYTIC CONVERSION OF ALCOHOLS HAVING AT LEAST THREE CARBON ATOMS TO HYDROCARBON BLENDSTOCK

Номер: US20150011813A1
Принадлежит:

A method for producing a hydrocarbon blendstock, the method comprising contacting at least one saturated acyclic alcohol having at least three and up to ten carbon atoms with a metal-loaded zeolite catalyst at a temperature of at least 100° C. and up to 550° C., wherein the metal is a positively-charged metal ion, and the metal-loaded zeolite catalyst is catalytically active for converting the alcohol to the hydrocarbon blendstock, wherein the method directly produces a hydrocarbon blendstock having less than 1 vol % ethylene and at least 35 vol % of hydrocarbon compounds containing at least eight carbon atoms. 1. A method for producing a hydrocarbon blendstock , the method comprising contacting at least one saturated acyclic alcohol having at least three and up to ten carbon atoms with a metal-loaded zeolite catalyst at a temperature of at least 100° C. and up to 550° C. , wherein said metal is a positively-charged metal ion , and said metal-loaded zeolite catalyst is catalytically active for converting said alcohol to said hydrocarbon blendstock , wherein said method directly produces a hydrocarbon blendstock having less than 1 vol % ethylene and at least 35 vol % of hydrocarbon compounds containing at least eight carbon atoms.2. The method of claim 1 , wherein said at least one saturated acyclic alcohol is a straight-chained alcohol.3. The method of claim 2 , wherein said straight-chained alcohol is selected from n-propanol claim 2 , n-butanol claim 2 , n-pentanol claim 2 , n-hexanol claim 2 , n-heptanol claim 2 , n-octanol claim 2 , n-nonanol claim 2 , and n-decanol.4. The method of claim 1 , wherein said at least one saturated acyclic alcohol is a branched alcohol.5. The method of claim 4 , wherein said branched alcohol is selected from isopropanol claim 4 , isobutanol claim 4 , sec-butanol claim 4 , t-butanol claim 4 , isopentanol claim 4 , 2-pentanol claim 4 , 3-pentanol claim 4 , neopentyl alcohol claim 4 , isohexanol claim 4 , 2-hexanol claim 4 , 3-hexanol ...

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09-01-2020 дата публикации

Methods of Preparing an Aromatization Catalyst

Номер: US20200010384A1
Автор: Wu An-Hsiang
Принадлежит:

A method of preparing a bound zeolite support comprising: contacting a zeolite powder with a binder and water to form a paste; shaping the paste to form an wet extruded base; removing excess water from the wet extruded base to form an extruded base; contacting the extruded base with a fluorine-containing compound to form a fluorinated extruded base; calcining the extruded base to form a calcined fluorinated extruded base; washing the calcined fluorinated extruded base to form a washed calcined fluorinated extruded base; drying the washed calcined fluorinated extruded base to form a dried washed calcined fluorinated extruded base; and calcining the dried washed calcined fluorinated extruded base to form a bound zeolite support. 1. A method of preparing a bound zeolite support comprising:calcining an extruded base to form a calcined extruded base, wherein the extruded base comprises a KL-zeolite;contacting the calcined extruded base with a fluorine-containing compound to form a fluorinated calcined extruded base;washing the fluorinated calcined extruded base to form a washed fluorinated calcined extruded base;drying the washed fluorinated calcined extruded base to form a dried washed fluorinated calcined extruded base;calcining the dried washed fluorinated calcined extruded base to form a bound zeolite support; andcontacting the bound zeolite support with a Group VIII metal.2. The method of claim 1 , further comprising:contacting a KL-zeolite powder with a binder and water to form a paste;shaping the paste to form an wet extruded base; andremoving excess water from the wet extruded base to form the extruded base.3. The method of claim 2 , wherein the binder comprises synthetic or naturally-occurring zeolites claim 2 , alumina claim 2 , silica claim 2 , clays claim 2 , refractory oxides of metals of Groups IVA and IVB of the Periodic Table of the Elements; oxides of silicon claim 2 , titanium claim 2 , zirconium; or combinations thereof.4. The method of claim 2 , ...

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18-01-2018 дата публикации

Treatment of Aromatic Alkylation Feedstock

Номер: US20180016207A1
Принадлежит: ExxonMobil Chemical Patents Inc

In a process and system for treatment of feed stocks comprising alkylating agent and metal salts, the metal salts are removed from the feedstock by an efficient combination of separations processes. The processes may take place in one or more stages, each stage taking place in one or more vessels. Such treatment processes may remove 99.9% or more of metal salts from a feedstock, while recovering 99.9% or more of the alkylating agent from the feedstock for use in an alkylation reaction, especially of aromatics such as toluene and benzene. Preferred alkylating agents include methanol and mixtures of carbon monoxide and hydrogen, for methylation of toluene and/or benzene. The methylation proceeds over an aluminosilicate catalyst and preferably yields para-xylene with 75% or greater selectivity.

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15-01-2015 дата публикации

Catalyst activation method for fischer-tropsch synthesis

Номер: US20150018438A1

The present invention relates to: a catalyst activation method for Fischer-Tropsch synthesis; a catalyst regeneration method for Fischer-Tropsch synthesis; and a method for producing a liquid or solid hydrocarbon by using the Fischer-Tropsch synthesis reaction. The temperatures required for a metal carbide producing and activating reaction is markedly lower than existing catalyst activation temperatures, and the catalyst can be activated under conditions that are the same as Fischer-Tropsch synthesis reaction conditions, and thus there is no need for separate reduction equipment in the reactor, and a Fischer-Tropsch synthesis catalyst which has been used for a long time can be regenerated within the reactor without the catalyst being isolated or extracted from the reactor.

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15-01-2015 дата публикации

CATALYST FOR CONVERSION OF HYDROCARBONS, PROCESS OF MAKING AND PROCESS OF USING THEREOF - GE ZEOLITE

Номер: US20150018590A1
Принадлежит: SAUDI BASIC INDUSTRIES CORPORATION

In an embodiment a catalyst comprises a medium or large pore zeolite having germanium incorporated into the zeolite framework. The zeolite can have a pore structure that is one dimensional, two dimensional or three dimensional. A metal selected from Group 10 can be deposited on the zeolite. In an embodiment, a process for synthesizing the zeolite comprises preparing a medium pore zeolite containing germanium in the framework of the zeolite and calcining the zeolite. In an embodiment, the catalyst can be used in a process for the conversion of hydrocarbons comprising contacting a hydrocarbon stream containing alkanes, olefins, or mixtures thereof having 2 to 12 carbon atoms per molecule with the catalyst and recovering the product. 1. A process for the conversion of hydrocarbons comprising:a) contacting a hydrocarbon stream containing alkanes, olefins or mixtures thereof having 2 to 12 carbon atoms per molecule with a medium or large pore zeolite-based catalyst wherein the zeolite contains germanium incorporated into the zeolite framework and wherein a metal selected from Group 10 has been deposited on the zeolite; andb) recovering the product.2. The process of claim 1 , wherein zeolite is a medium pore zeolite and the metal deposited on the medium pore is platinum.3. The process of claim 1 , wherein the zeolite is non-acidic and is MFI claim 1 , MEL claim 1 , BEA claim 1 , MWW claim 1 , MTW claim 1 , ZSM-48 claim 1 , or FER.4. The process of claim 1 , wherein the zeolite is non-acidic and is MEL claim 1 , BEA claim 1 , MWW claim 1 , MTW claim 1 , ZSM-48 claim 1 , or FER.5. The process of claim 1 , wherein the alkanes or the olefins are straight claim 1 , branched claim 1 , cyclic or mixtures thereof.6. The process of claim 1 , wherein the germanium is present in the zeolite in a range of 0.1 to 10 wt. %.7. The process of claim 1 , wherein the germanium is present in the zeolite in a range of 0.1 to 5 wt. %.8. The process of claim 1 , wherein the noble metal is ...

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15-01-2015 дата публикации

Method of Converting Oxygenates to Olefins

Номер: US20150018591A1
Принадлежит:

A method of converting an oxygenate comprising feedstock to olefins comprising: feeding an oxygenate comprising feedstock into a reactor containing an oxygenate to olefins conversion catalyst; contacting the feedstock with the catalyst at oxygenate conversion conditions to produce olefins; removing an effluent comprising the olefins from the reactor; passing the effluent through a compression section to form a compressed effluent; and adding methane to the compression section. 1. A method of converting an oxygenate comprising feedstock to olefins comprising:a. feeding an oxygenate comprising feedstock into a reactor containing an oxygenate to olefins conversion catalyst;b. contacting the feedstock with the catalyst at oxygenate conversion conditions to produce olefins;c. removing an effluent comprising the olefins from the reactor;d. passing the effluent through a compression section to form a compressed effluent;e. separating the effluent into several products including methane; andf. adding methane to the compression section.2. The method of wherein the feedstock comprises methanol.3. The method of wherein the compression section comprises multiple stages of compression and cooling.4. The method of wherein the methane is added to the first or second stage of the compression section.5. The method of wherein the methane is passed across a letdown valve or expander before being fed to the compression section.6. The method of wherein the methane is obtained from one or more separation steps downstream of the compression section.7. The method of wherein the methane is introduced from an external source of methane.8. The method of further comprising:g. separating the compressed effluent into a heavy stream comprising a majority of the C3 and higher hydrocarbons and a light stream comprising a majority of the C2 and lighter hydrocarbons and hydrogen;h. passing the light stream through a refrigeration section to form a cooled light stream;i. passing the cooled light ...

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17-01-2019 дата публикации

Process for producing ethylbenzene

Номер: US20190016647A1
Принадлежит: BADGER LICENSING LLC

A process for producing ethylbenzene is described in which benzene and ethylene are supplied to an alkylation reaction zone. Also added to the alkylation reaction zone is a C 3+ olefin in an amount of at least 200 ppm by weight of the ethylene supplied to the alkylation reaction zone. The benzene, ethylene and C 3+ olefin are contacted with an alkylation catalyst in the alkylation reaction zone to alkylate at least part of the benzene and produce an alkylation effluent comprising ethylbenzene, polyethylated benzene and at least one mono-C 3+ alkyl benzene. The alkylation effluent is separated into a first product fraction comprising ethylbenzene and a second fraction comprising polyethylated benzene and the at least one mono-C 3+ alkyl benzene. The second fraction is then contacted with benzene in the presence of a transalkylation catalyst to convert at least part of the polyethylated benzene to ethylbenzene and produce a transalkylation effluent.

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21-01-2021 дата публикации

Olefin aromatization catalyst, preparation method and use thereof, and low-carbon olefin aromatization process

Номер: US20210016261A1

The present discloses an aromatization catalyst, preparation process and application thereof and a low-carbon olefin aromatization process. The aromatization catalyst comprises a microporous material, a binder and a modifier; the microporous material is a zeolite molecular sieve, the binder is alumina, the modifier is phosphorus, and the molar ratio of the aluminum element in the binder to the phosphorus element is more than or equal to 1 and less than 5; the ratio of the acidity of the strongly acidic sites to the acidity of the weakly acidic sites of the olefin aromatization catalyst is less than 1.

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16-01-2020 дата публикации

METHODS FOR FORMING LIGHT OLEFINS BY CRACKING

Номер: US20200017426A1
Автор: Liu Yu, Pretz Matthew T.
Принадлежит: Dow Global Technologies LLC

According to one or more embodiments presently disclosed, light olefins may be formed by a method that may comprise introducing a feed stream into a reactor, reacting the feed stream with a cracking catalyst in the reactor to form a product stream, and processing the cracking catalyst. The reactor may comprise an upstream reactor section and a downstream reactor section. The upstream reactor section may be positioned below the downstream reactor section. The upstream reactor section may have an average cross-sectional area that is at least 150% of the average cross-sectional area of the downstream reactor section. 1. A method for forming light olefins , the method comprising:introducing a feed stream into a reactor, the reactor comprising an upstream reactor section and a downstream reactor section, the upstream reactor section positioned below the downstream reactor section, and the upstream reactor section having an average cross-sectional area that is at least 150% of the average cross-sectional area of the downstream reactor section;reacting the feed stream with a cracking catalyst in the reactor to from a product stream; and passing the catalyst from the reactor to a combustor;', 'burning a supplemental fuel source in the combustor to heat the catalyst; and', 'passing the heated catalyst from the combustor to the reactor., 'processing the cracking catalyst, the processing of the cracking catalyst comprising2. The method of claim 1 , wherein the feed stream comprises one or more of naphtha or butane.3. The method of claim 1 , wherein the product stream comprises one or more of ethylene claim 1 , propylene claim 1 , or butene.4. The method of claim 1 , wherein the upstream reactor section operates as a fast fluidized claim 1 , turbulent claim 1 , or bubbling bed upflow reactor.5. The method of claim 1 , wherein the downstream reactor section operates as a dilute phase riser reactor.6. The method of claim 1 , wherein weight hour space velocity in the reactor is ...

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28-01-2016 дата публикации

OLEFIN CONVERSION PROCESS

Номер: US20160023964A1
Принадлежит: LUMMUS TECHNOLOGY INC.

A process for the production of Colefins, which may include: contacting a hydrocarbon mixture comprising alpha-pentenes with an isomerization catalyst to form an isomerization product comprising beta-pentenes; contacting ethylene and the beta-pentenes with a first metathesis catalyst to form a first metathesis product comprising butenes and propylene, as well as any unreacted ethylene and Colefins; and fractionating the first metathesis product to for an ethylene fraction, a propylene fraction, a butene fraction, and a Cfraction. 1. A system for the production of Colefins , the system comprising:an isomerization reaction zone for contacting a hydrocarbon mixture comprising alpha-pentenes with an isomerization catalyst to form an isomerization product comprising beta-pentenes;{'sub': '5', 'a first metathesis reaction zone for contacting ethylene and the beta-pentenes with a first metathesis catalyst to form a first metathesis product comprising butenes and propylene, as well as any unreacted ethylene and Colefins;'}{'sub': '5', 'a separation system for fractionating the first metathesis product to form an ethylene fraction, a propylene fraction, a butene fraction, and a Cfraction; and'}a second metathesis reaction zone for contacting the propylene with a second metathesis catalyst, which may be the same or different than the first metathesis catalyst, to convert at least a portion of the propylene to ethylene and 2-butene and form a second metathesis product.2. The system of claim 1 , further comprising a flow conduit for feeding the first metathesis product and the second metathesis product to a common fractionation system.3. The system of claim 2 , further comprising a flow conduit for withdrawing a propylene product stream.4. The system of claim 3 , further comprising a control system for adjusting a rate of withdrawing the propylene product stream to produce a selected ratio of butene to propylene product.5. The system of claim 1 , further comprising one or more ...

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26-01-2017 дата публикации

Catalyzed Alkylation, Alkylation Catalysts, and Methods of Making Alkylation Catalysts

Номер: US20170022126A1
Принадлежит:

Improved alkylation catalysts, alkylation methods, and methods of making alkylation catalysts are described. The alkylation method comprises reaction over a solid acid, zeolite-based catalyst and can be conducted for relatively long periods at steady state conditions. The alkylation catalyst comprises a crystalline zeolite structure, a Si/Al molar ratio of 20 or less, less than 0.5 weight percent alkali metals, and further having a characteristic catalyst life property. Some catalysts may contain rare earth elements in the range of 10 to 35 wt %. One method of making a catalyst includes a calcination step following exchange of the rare earth element(s) conducted at a temperature of at least 575° C. to stabilize the resulting structure followed by an deammoniation treatment. An improved method of deammoniation uses low temperature oxidation. 1. A method of alkylating isobutane , comprising:passing a feed mixture consisting of excess isobutane and C2 to C5 olefins into a reaction chamber;wherein the reaction chamber comprises a crystalline zeolite catalyst;wherein the crystalline zeolite catalyst comprises sodalite cages and supercages, a Si/Al molar ratio of 20 or less, less than 0.5 weight percent alkali metals; and up to 5 wt % of Pt, Pd and or Nickel,wherein, at steady state, at least 90% of the butenes (or at least 90% of the C2 to C5 olefins) are converted to products and wherein the Research Octane Number (RON) remains above 92; and conducting the process for a catalyst age of 2.5 or greater over the same catalyst; andwherein steady state means that the selectivity to C8 isomers changes by 10% or less over the entire period that the catalyst age is determined.2. (canceled)3. (canceled)4. The method of wherein the catalyst is regenerated in a flowing gas stream that is essentially hydrogen at a temperature of at least 250° C.; and wherein the catalyst comprises 0.1 wt % to 5 wt % of an element selected from the group consisting of Pt claim 1 , Pd claim 1 , Ni ...

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25-01-2018 дата публикации

Hydrocarbon Dehydrocyclization in the Presence of Carbon Dioxide

Номер: US20180022667A1
Принадлежит: ExxonMobil Chemical Patents Inc

The invention relates to converting non-aromatic hydrocarbon in the presence of CO 2 to produce aromatic hydrocarbon. CO 2 methanation using molecular hydrogen produced during the aromatization increases aromatic hydrocarbon yield. The invention also relates to equipment and materials useful in such upgrading, to processes for carrying out such upgrading, and to the use of such processes for, e.g., natural gas upgrading.

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17-04-2014 дата публикации

Method for Providing a Co-Feed in the Coupling of Toluene with a Carbon Source

Номер: US20140107384A1
Принадлежит: Fina Technology Inc

A process for making styrene is disclosed that includes reacting toluene with a C 1 source and a co-feed in the presence of a catalyst in a reactor to form a first product stream comprising styrene, ethylbenzene, carbon monoxide, and hydrogen; separating the hydrogen and carbon monoxide from the first product stream to form a second stream; separating the hydrogen from the second stream to form a third stream comprising hydrogen and a fourth stream comprising carbon monoxide; wherein the fourth stream is recycled to the reactor and forms at least a portion of the co-feed.

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22-01-2015 дата публикации

Production of Monoalkyl Aromatic Compounds

Номер: US20150025286A1
Принадлежит: ExxonMobile Chemical Patents Inc.

The present disclosure relates to a process for production of a monoalkyl aromatic compound by alkylation of alkylatable aromatic compounds with an alkylating agent in a reactor comprising at least a first and a second series-connected alkylation reaction zones and a cooler disposed between the first and the second series-connected alkylation reaction zones. The process comprising a step of cooling at least a portion of an effluent withdrawn from the first alkylation reaction zone before being introduced into the second alkylation reaction zone. 1. A process for production of ethylbenzene in a reactor having at least a first and a second series-connected alkylation reaction zone , each reaction zone having an alkylation catalyst , the process comprising the steps of:a) introducing a first feed comprising benzene and a second feed comprising ethylene into said first alkylation reaction zone;b) operating said first alkylation reaction zone under at least partly liquid phase conditions sufficient to cause alkylation of said benzene by said ethylene in the presence of said alkylation catalyst to produce a first effluent comprising said ethylbenzene and unreacted to benzene;c) withdrawing said first effluent from said first reaction zone;d) cooling at least a portion of said first effluent to form a cooled first effluent;e) supplying said cooled first effluent and the rest of said first effluent, and optionally a third feed comprising additional said ethylene to said second alkylation reaction zone;f) operating said second alkylation reaction zone under at least partly liquid phase conditions sufficient to cause alkylation of said unreacted benzene by said ethylene in the presence of said alkylation catalyst to produce a second effluent comprising additional said ethylbenzene and unreacted benzene;g) withdrawing a reactor effluent which comprises at least said first and second effluents from said reactor; andh) recycling a portion of said reactor effluent to said first ...

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28-01-2021 дата публикации

HYDRODESULFURIZATION CATALYST WITH A ZEOLITE-GRAPHENE MATERIAL COMPOSITE SUPPORT AND METHODS THEREOF

Номер: US20210024436A1

A hydrodesulfurization catalyst, which includes (i) a catalyst support including a zeolite doped with 0.1 to 0.5 wt. % of a graphene material, based on a total weight of the catalyst support, (ii) 5 to 20 wt. % of molybdenum, based on a total weight of the hydrodesulfurization catalyst, and (iii) 1 to 6 wt. % of a promoter selected from the group consisting of cobalt and nickel, based on a total weight of the hydrodesulfurization catalyst. The molybdenum and the promoter are homogeneously disposed on the catalyst support. A method of producing the hydrodesulfurization catalyst via incipient wetness impregnation techniques, and a method for desulfurizing a hydrocarbon feedstock with the hydrodesulfurization catalyst are also provided. 1: A hydrodesulfurization catalyst , comprising:a catalyst support comprising a zeolite doped with 0.1 to 0.5 wt. % of a graphene material, based on a total weight of the catalyst support;5 to 20 wt. % of molybdenum, based on a total weight of the hydrodesulfurization catalyst; and1 to 6 wt. % of a promoter selected from the group consisting of cobalt and nickel, based on a total weight of the hydrodesulfurization catalyst;wherein the molybdenum and the promoter are homogeneously disposed on the catalyst support.2: The hydrodesulfurization catalyst of claim 1 , wherein the zeolite is a Y-zeolite.3: The hydrodesulfurization catalyst of claim 1 , wherein the graphene material is present in the catalyst support in an amount of 0.3 to 0.4 wt. % claim 1 , based on a total weight of the catalyst support.4: The hydrodesulfurization catalyst of claim 1 , wherein the graphene material is graphene oxide.5: The hydrodesulfurization catalyst of claim 1 , wherein molybdenum is present in an amount of 14 to 16 wt. % claim 1 , and the promoter is present in an amount of 4 to 6 wt. % claim 1 , each based on a total weight of the hydrodesulfurization catalyst.6: The hydrodesulfurization catalyst of claim 1 , wherein the catalyst support consists of the ...

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28-01-2021 дата публикации

PROCESS FOR THE OLIGOMERIZATION OF OLEFINS

Номер: US20210024437A1
Принадлежит: TOTAL MARKETING SERVICES

A process for preparing a hydrocarbon fluid includes a step of oligomerising an initial hydrocarbon composition which contains, in relation to the total weight of said initial hydrocarbon composition, at least 2% by weight of 3-methyl-but-1-ene, at least 5% by weight of 2-methyl-but-2-ene and at least 5% by weight of 2-methyl-but-1-ene. 1. Process A process for preparing a hydrocarbon fluid , comprising an oligomerization step of an initial hydrocarbon composition comprising at least 2% wt. of 3-methyl-but-1-ene , at least 5% wt. of 2-methyl-but-2-ene and at least 5% wt. of 2-methyl-but-1-ene relative to the total weight of the initial hydrocarbon composition.2. The process according to claim 1 , wherein the initial hydrocarbon composition is derived from biomass.3. The process according to claim 1 , wherein the initial hydrocarbon composition is obtained via dehydration of alcohol(s).4. The process according to claim 1 , wherein the initial hydrocarbon composition comprises at least 20% wt. claim 1 , of branched olefins having 5 carbon atoms selected from among 3-methyl-but-1-ene claim 1 , 2-methyl-but-2-ene and 2-methyl-but-1-ene claim 1 , relative to the total weight of the initial composition.5. The process according to claim 1 , wherein the initial hydrocarbon composition comprises at least 20% wt. claim 1 , of 2-methyl-but-2-ene claim 1 , relative to the total weight of the composition.6. The process according to claim 5 , wherein the initial hydrocarbon composition comprises 3-methyl-but-1-ene in a weight proportion such that the 3-methyl-but-1-ene represents the olefin having 5 carbon atoms present in majority amount in the initial hydrocarbon composition.7. The process according to claim 1 , wherein the oligomerization step is conducted in the presence of a catalyst selected from among alumina and aluminosilicates.8. The process according to claim 1 , wherein the catalyst is an aluminosilicate and the SiO/AlOmolar ratio of the catalyst ranges from 10 to 80. ...

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01-02-2018 дата публикации

LEWIS ACID CATALYSTS FOR PRODUCING TOLUENE AND METHOD FOR MANUFACTURING TOLUENE USING THE SAME

Номер: US20180029959A1
Принадлежит:

Disclosed is a Lewis acid catalyst for preparation of toluene from 2-methylfuran and a method for preparing toluene from 2-methylfuran by using the same. The catalyst is a zeolite catalyst ion-exchanged with a metal or a metal halide catalyst. The catalyst accelerates the cycloaddition of 2-methylfuran with ethylene and inhibits oligomerization as a side reaction, and thus allows production of toluene from 2-methylfuran with high yield and high selectivity. 1. A catalyst for use in the preparation of toluene from 2-methylfuran ,wherein the catalyst is a Lewis acid catalyst; andwherein the catalyst is a zeolite catalyst ion-exchanged with at least one metal.2. The catalyst for use in the preparation of toluene according to claim 1 , wherein the zeolite catalyst is ion-exchanged with at least one metal selected from the group consisting of alkali metals claim 1 , transition metals and post-transition metals.3. The catalyst for use in the preparation of toluene according to claim 2 , wherein the zeolite catalyst is ion-exchanged with at least one alkali metal.4. The catalyst for use in the preparation of toluene according to claim 3 , wherein the zeolite catalyst is ion-exchanged with Li or Na.5. The catalyst for use in the preparation of toluene according to claim 1 , wherein the zeolite catalyst is a Y-zeolite catalyst having an FAU structure.6. A catalyst for use in the preparation of toluene from 2-methylfuran claim 1 ,wherein the catalyst is a Lewis acid catalyst; andwherein the catalyst is a metal halide catalyst.7. The catalyst for use in the preparation of toluene according to claim 6 , wherein the metal halide catalyst comprises: at least one cation selected from the group consisting of transition metals and post-transition metals; and at least one halogen anion.8. The catalyst for use in the preparation of toluene according to claim 7 , wherein the metal halide catalyst is a metal chloride.9. The catalyst for use in the preparation of toluene according to ...

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31-01-2019 дата публикации

A Process for Preparing Perhydrofluorene or Alkyl-Substituted Perhydrofluorene

Номер: US20190031576A1
Принадлежит: TIANJIN UNIVERSITY

The present invention discloses a process for preparing perhydrofluorene or alkyl-substituted perhydrofluorene, comprising the steps of: (1) reacting a phenolic compound or an aromatic hydrocarbon compound or an aromatic ketone compound or an aromatic ether compound with a benzyl compound to carry out an alkylation reaction in the presence of a first catalyst, thereby to produce substituted or unsubstituted diphenyl methane, wherein the first catalyst is an acidic catalyst; and (2) reacting the substituted or unsubstituted diphenyl methane with hydrogen gas to carry out an hydrogenation reaction or a hydrodeoxygenation reaction, thereby to produce perhydrofluorene or alkyl-substituted perhydrofluorene, wherein the second catalyst is a physical mixture of a metal catalyst and an acidic catalyst or a metal catalyst loaded on an acidic catalyst.

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31-01-2019 дата публикации

CONVERSION OF SHALE GAS TO AROMATICS

Номер: US20190031578A1
Автор: Mamedov Aghaddin Kh.
Принадлежит:

A method for converting shale gas to aromatic hydrocarbons includes passing a feedstock comprising ethane gas and methane gas to an aromatization reactor; converting a portion of the methane gas and ethane gas in the feedstock to liquid aromatic hydrocarbons with a zeolite based catalyst at a temperature of 750 C to 900 C; separating unconverted methane gas from liquid aromatic hydrocarbons; separating unconverted methane gas from the unconverted ethane gas; recycling the separated methane gas to the aromatization reactor; recovering aromatic hydrocarbons in a product stream after separation and removal from the aromatization reactor. Less than or equal to 95% of the ethane is converted to aromatic hydrocarbons. 1. A method for converting shale gas to aromatic hydrocarbons , comprising:passing a feedstock comprising ethane gas and methane gas to an aromatization reactor;converting a portion of the methane gas and ethane gas in the feedstock to liquid aromatic hydrocarbons with a zeolite based catalyst at a temperature of 750° C. to 900° C.;separating unconverted methane gas from liquid aromatic hydrocarbons;separating unconverted methane gas from the unconverted ethane gas;recycling the separated methane gas to the aromatization reactor;recovering aromatic hydrocarbons in a product stream after separation and removal from the aromatization reactor;wherein less than or equal to 95% of the ethane is converted to aromatic hydrocarbons.2. The method of claim 1 , wherein the feedstock is a shale gas feedstock.3. The method of claim 1 , wherein the feedstock further comprises propane claim 1 , butane claim 1 , pentane claim 1 , carbon dioxide claim 1 , oxygen claim 1 , nitrogen claim 1 , hydrogen sulfide claim 1 , or a combination comprising at least one of the foregoing.4. The method of claim 1 , wherein the feedstock comprises 75-85 mol % methane.5. The method of claim 1 , wherein the feedstock comprises 10-25 mol % ethane.6. The method of claim 1 , wherein less than or ...

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30-01-2020 дата публикации

PROCESS FOR OLIGOMERIZATION OF BUTENE WITH DETERMINATION OF THE PROPORTION OF ACIDIC CATALYSIS

Номер: US20200031732A1
Принадлежит: EVONIK DEGUSSA GmbH

The invention provides a process for oligomerization of n-butenes using a nickel-containing aluminosilicate catalyst to produce a product mixture whose ratio of 4,4-dimethylhexene to 3,4-dimethylhexene is determined and monitored. The invention further relates to a process for determining the ratio of the amount of the formed 4,4-dimethylhexene or of the formed 3-ethyl-2-methylpentene to the amount of the formed 3,4-dimethylhexene. 1. A process for oligomerization of n-butenes using a mesoporous , nickel-containing aluminosilicate catalyst over which a reactant stream containing the n-butenes is passed to form a product mixture , wherein the ratio of the amount of the formed 4 ,4-dimethylhexene to the amount of the formed 3 ,4-dimethylhexene in the product mixture is monitored and the catalyst is replaced upon exceedance of a threshold value for the ratio (amount of 4 ,4-dimethylhexene/amount of 3 ,4-dimethylhexene) ,wherein the threshold value for the ratio (amount of 4,4-dimethylhexene/amount of 3,4-dimethylhexene) is not more than 0.05.2. The process according to claim 1 , wherein the process for oligomerization is performed at a temperature in the range from 50° C. to 200° C.3. The process according to claim 1 , wherein the process for oligomerization is performed at a pressure in the range from 10 bar to 70 bar.4. The process according to claim 1 , wherein the mesoporous nickel-containing aluminosilicate catalyst employed in the process for oligomerization contains nickel claim 1 , calculated as nickel oxide NiO claim 1 , in an amount of 0.1% to 51% by weight based on the total composition of the mesoporous nickel-containing aluminosilicate catalyst.5. The process according to claim 1 , wherein the mesoporous nickel-containing aluminosilicate catalyst employed in the process for oligomerization has an Si/Al ratio of 1 to 100.6. The process according to claim 1 , wherein the mesoporous nickel-containing aluminosilicate catalyst contains no titanium dioxide and/ ...

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30-01-2020 дата публикации

Catalyzed Alkylation, Alkylation Catalysts, and Methods of Making Alkylation Catalysts

Номер: US20200031733A1
Принадлежит: Exelus Inc

Improved alkylation catalysts, alkylation methods, and methods of making alkylation catalysts are described. The alkylation method comprises reaction over a solid acid, zeolite-based catalyst and can be conducted for relatively long periods at steady state conditions. The alkylation catalyst comprises a crystalline zeolite structure, a Si/Al molar ratio of 20 or less, less than 0.5 weight percent alkali metals, and further having a characteristic catalyst life property. Some catalysts may contain rare earth elements in the range of 10 to 35 wt %. One method of making a catalyst includes a calcination step following exchange of the rare earth element(s) conducted at a temperature of at least 575° C. to stabilize the resulting structure followed by an deammoniation treatment. An improved method of deammoniation uses low temperature oxidation.

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11-02-2016 дата публикации

Treatment of Aromatic Alkylation Catalysts

Номер: US20160038928A1
Принадлежит:

The present disclosure relates to a method for treating a catalyst that is useful for producing mono-alkylaromatic compounds, the method comprises the steps of (a) contacting the untreated catalyst with water to produce water-contacted catalyst, and (b) drying the water-contacted catalyst with a drying gas without steam being formed at a temperature of less than 300° C. to produce a treated catalyst. The treatment is effective to improve the activity and catalyst selectivity. A process for producing a mono-alkylaromatic compound comprising such a catalyst treatment is also disclosed. 1. A process for producing an alkylated aromatic compound , comprising the step of contacting an alkylatable aromatic compound and an alkylating agent with a treated catalyst under alkylation or transalkylation conditions to produce the alkylated aromatic compound , wherein the treated catalyst was treated by the method comprising the steps of:(a) contacting an untreated catalyst with water to produce a water-contacted catalyst, and(b) drying the water-contacted catalyst with a drying gas with minimal steam being formed at a temperature of less than about 300° C. to produce a treated catalyst.2. The process of claim 1 , wherein the water-contacted catalyst of drying step (b) is dried at a deposit height of less than about 10 centimeters.3. The process of claim 1 , wherein the drying gas flows along the direction of the catalyst deposit height through the water-contacted catalyst.4. The process of claim 1 , wherein the drying gas flows in a direction vertical to the catalyst deposit height.5. The process of claim 1 , wherein the drying step (b) is conducted at a temperature of from about 50° C. to about 250° C.6. (canceled)7. The method of claim 1 , wherein drying step (b) is conducted for a period of from about 1 minute to about 96 hours.8. The process of claim 1 , wherein the catalyst comprises a fresh catalyst claim 1 , and at least partially deactivated catalyst claim 1 , or ...

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11-02-2016 дата публикации

Process for Starting Up a Fluidized Catalytic Reaction Apparatus Used for Producing Lower Olefins

Номер: US20160039725A1
Принадлежит:

Disclosed is a process for starting up fluidized reaction apparatus which are used for producing lower olefins from methanol or/and dimethyl ether. Said process includes after heating the catalyst bed of circulating fluidized catalytic reaction apparatus to above 200° C. or 300° C. by using a starting-up auxiliary heat source, feeding methanol or dimethyl ether raw materials to a reactor, whereby heat released by the reaction makes the temperature of the reaction system apparatus increase quickly to a designed temperature, consequently making the system reach the normal operation state rapidly. Said process is suitable for starting up an exothermic fluidized catalytic reaction apparatus and can simplify the apparatus and operation, accordingly lowering the cost. 1. A process for starting up a fluidized catalytic reaction apparatus for producing lower olefins , in which methanol or a mixture of methanol and dimethyl ether is taken as raw material , and said reaction apparatus includes a reactor having a catalyst bed and a regenerator having a regeneration bed , the method including the steps of:1) heating the catalyst bed of the reactor in the circulating fluidized catalytic reaction apparatus to a temperature of 200° C. or above, and heating the regeneration bed of the regenerator to a temperature of 300° C. or above, by using a starting up auxiliary heat source;2) circulating the catalyst between the reactor and regenerator with a circulation rate as low as possible, wherein the catalyst circulation rate is higher than zero and lower than half of the normal catalyst circulation rate, wherein the normal catalyst circulation rate=catalyst inventory in the catalyst bed of the reactor divided by the normal catalyst residence time in the reactor, wherein the normal catalyst residence time is 45 minutes;3) feeding the raw material to the catalyst bed of the reactor in the fluidized catalytic reaction apparatus, whereby the catalyst bed of the reactor is further heated to ...

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24-02-2022 дата публикации

APPARATUS AND METHOD FOR PRODUCING HYDROCARBONS

Номер: US20220055967A1
Принадлежит: FURUKAWA ELECTRIC CO., LTD.

An apparatus and method for producing hydrocarbons including aromatic hydrocarbons and/or lower olefins including propylene from CO Hwhile inhibiting reduction in catalyst activity and enhancing selectivity. The apparatus produces hydrocarbons including aromatic hydrocarbons having 6-10 carbon atoms and/or lower olefins including propylene, and is provided: a first supply unit which supplies a raw material gas containing CO and H; and a hydrocarbon production unit to which the raw material gas is supplied from the first supply unit, and which produces the hydrocarbons from CO and Hcontained in the raw material gas while heating a catalyst structure at a temperature of 150° C. or more and less than 300° C. or at a temperature of 350° C. or more and less than 550° C., the catalyst structure includes supports having a porous structure and including a zeolite-type compound, and a metal fine particle present in the supports, the supports have channels communicating with outside the supports, and a portion of the channels have an average inner diameter of 0.95 nm or less. 1. An apparatus for producing hydrocarbons including at least one compound selected from lower olefins including propylene and aromatic hydrocarbons having six or more and ten or less carbon atoms , the apparatus comprising:a first supply unit that supplies a raw material gas comprising carbon monoxide and hydrogen; anda hydrocarbon production unit that comprises a catalyst structure, receives supply of the raw material gas from the first supply unit, and produces, from carbon monoxide and hydrogen in the raw material gas, hydrocarbons including at least one compound selected from lower olefins including propylene and aromatic hydrocarbons having six or more and ten or less carbon atoms while heating the catalyst structure at a first temperature of 150° C. or more and less than 300° C. or at a second temperature of 350° C. or more and less than 550° C., whereinthe catalyst structure includes supports ...

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18-02-2016 дата публикации

PROCESS FOR MAKING LINEAR LONG-CHAIN ALKANES FROM RENEWABLE FEEDSTOCKS USING CATALYSTS COMPRISING HETEROPOLYACIDS

Номер: US20160046541A1
Принадлежит:

A hydrodeoxygenation process for producing a linear alkane from a feedstock comprising a saturated or unsaturated Coxygenate that comprises an ester group, carboxylic acid group, carbonyl group and/or alcohol group is disclosed. The process comprises contacting the feedstock with a catalyst composition comprising a metal catalyst and a heteropolyacid or heteropolyacid salt, at a temperature between about 240° C. to 280° C. and a hydrogen gas pressure of at least 300 psi. The metal catalyst comprises copper in certain embodiments. By contacting the feedstock with the catalyst composition under these temperature and pressure conditions, the Coxygenate is hydrodeoxygenated to a linear alkane that has the same carbon chain length as the Coxygenate. 1. A hydrodeoxygenation process for producing a linear alkane from a feedstock comprising a saturated or unsaturated Coxygenate comprising a moiety selected from the group consisting of an ester group , carboxylic acid group , carbonyl group , and alcohol group , wherein the process comprises:{'sub': 10-18', '10-18, 'a) contacting said feedstock with a catalyst composition at a temperature between about 240° C. to about 280° C. and a hydrogen gas pressure of at least about 300 psi, wherein said catalyst composition comprises (i) a metal catalyst and (ii) a heteropolyacid or heteropolyacid salt, wherein the Coxygenate is hydrodeoxygenated to a linear alkane, and wherein the linear alkane has the same carbon chain length as the Coxygenate; and'}b) optionally, recovering the linear alkane produced in step (a).2. The hydrodeoxygenation process of claim 1 , wherein said Coxygenate is a fatty acid or a triglyceride.3. The hydrodeoxygenation process of claim 1 , wherein said feedstock comprises a plant oil or a fatty acid distillate thereof.4. The hydrodeoxygenation process of claim 3 , wherein said feedstock comprises:(i) a plant oil selected from the group consisting of soybean oil, palm oil and palm kernel oil; or(ii) a palm ...

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18-02-2021 дата публикации

High severity fluidized catalytic cracking systems and processes for producing olefins from petroleum feeds

Номер: US20210047573A1
Принадлежит: Saudi Arabian Oil Co

Systems and processes are disclosed for producing petrochemical products, such as ethylene, propene and other olefins from crude oil in high severity fluid catalytic cracking (HSFCC) units. Processes include separating a crude oil into a light fraction and a heavy fraction, cracking the light fraction and heavy fraction in separation cracking reaction zones, and regenerating the cracking catalysts in a two-zone regenerator having a first regeneration zone for the first catalyst (heavy fraction) and a second regeneration zone for the second catalyst (light fraction) separate from the first regeneration zone. Flue gas from the first catalyst regeneration zone is passed to the second regeneration zone to provide additional heat to raise the temperature of the second catalyst of the light fraction side. The disclosed systems and processes enable different catalysts and operating conditions to be utilized for the light fraction and the heavy fraction of a crude oil feed.

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03-03-2022 дата публикации

Enantiomerically enriched, polycrystalline molecular sieves

Номер: US20220062875A1

This disclosure describes enantiomerically enriched chiral molecular sieves and methods of making and using the same. In some embodiments, the molecular sieves are silicates or germanosilicates of STW topology.

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19-02-2015 дата публикации

METHOD FOR PRODUCING LUBRICATING-OIL BASE OIL

Номер: US20150051429A1
Принадлежит: JX NIPPON OIL & ENERGY CORPORATION

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 ...

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22-02-2018 дата публикации

PRODUCTION OF PROPYLENE IN A FLUID CATALYTIC CRACKING UNIT

Номер: US20180050969A1
Принадлежит:

A process and apparatus for catalytic cracking of hydrocarbon feedstock employing circulating fluidized bed reactor-regenerator configuration for maximizing the yield of propylene (C3 olefin) is disclosed. The apparatus comprises two reaction zones operating under different temperature and weight hourly space velocity (WHSV), one primary zone for cracking of hydrocarbon feedstock and other as secondary zone for cracking of C4 fraction produced from the cracking of hydrocarbon feedstock in the primary reaction zone, optionally admixed with C4 stream from external source. Two dedicated conduits equipped with valves for control of catalyst flow rate are provided to supply the hot catalyst from a common catalyst regeneration zone wherein the catalyst flowing though conduit connected to the secondary reaction zone is cooled employing a heat exchanging device. The lower temperature achieved in secondary reaction zone on account of exchange of heat along with lower weight hourly space velocity (WHSV) selectively promotes oligomerisation of C4 fraction before being cracked to produce C3 olefin in the subsequent portion of the reaction zone (primary). 1. A process for enhancing the yield of C3 olefin in fluid catalytic cracking of hydrocarbon feedstock , the process comprising:a) contacting a hydrocarbon feedstock in a primary reaction zone of a riser in the presence of a fluidizable solid micro-spherical cracking catalyst to produce cracked hydrocarbon products and spent catalyst;b) separating the spent catalyst from the cracked hydrocarbon products and stripping the spent catalyst with steam to remove the hydrocarbons entrapped inside the pores;c) separating a C4 hydrocarbon fraction of the cracked hydrocarbon products to obtain a recycle C4 hydrocarbon fraction;d) burning off the coke deposited on the spent catalyst in a catalyst regenerator to obtain a hot regenerated catalyst;e) recycling a part of the hot regenerated catalyst into the primary reaction zone and ...

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22-02-2018 дата публикации

Transalkylated Cyclohexylbenzyl and Biphenyl Compounds

Номер: US20180050971A1
Принадлежит:

Processes for selectively alkylating and/or dealkylating one ring of cyclohexylbenzyl and/or biphenyl compounds are provided. Such selective alkylation and/or dealkylation takes place through a transalkylation reaction between the cyclohexylbenzyl compound and a substituted or unsubstituted benzene, which replaces the phenyl moiety of the cyclohexylbenzyl compound. The transalkylated cyclohexylbenzyl may be dehydrogenated to give a corresponding biphenyl compound. The same reaction steps can be utilized with respect to biphenyl compounds by first partially hydrogenating one phenyl ring of the biphenyl compound, thereby obtaining a corresponding cyclohexylbenzyl compound, which may undergo the transalkylation and, optionally, subsequent dehydrogenation. Combinations of any two or more of partial hydrogenation, transalkylation, and dehydrogenation enable targeted substitution (or de-substitution) of only one ring of cyclohexylbenzyl and/or biphenyl compounds, thereby providing superior control in designing the synthesis of these compounds. 5. The process of wherein R-Rare each H.6. The process of claim 5 , wherein R-Rare each H.7. The process of claim 1 , wherein one of R-Ris a C-Calkyl group claim 1 , and the rest of R-Rare each H; and further wherein R-Rare each H.8. The process of claim 1 , wherein the substituted or unsubstituted benzene and the additional substituted or unsubstituted benzene are each independently selected from the group consisting of toluene claim 1 , xylene claim 1 , and ethylbenzene.9. The process of claim 1 , wherein R*-R* and R*-R* each comprise the same five substitutions.10. The process of claim 3 , wherein the transalkylation catalyst and the second transalkylation catalyst are each independently selected from molecular sieves having a large pore molecular sieve having a Constraint Index less than 2.11. The process of claim 3 , wherein a single catalyst composition is both the transalkylation catalyst and the second transalkylation ...

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26-02-2015 дата публикации

PROCESS FOR THE MANUFACTURE OF DIESEL RANGE HYDROCARBONS

Номер: US20150057476A1
Принадлежит: NESTE OIL OYJ

The invention relates to a process for the manufacture of diesel range hydrocarbons wherein a feed is hydrotreated in a hydrotreating step and isomerised in an isomerisation step, and a feed comprising fresh feed containing more than 5 wt % of free fatty acids and at least one diluting agent is hydrotreated at a reaction temperature of 200-400° C., in a hydrotreating reactor in the presence of catalyst, and the ratio of the diluting agent/fresh feed is 5-30:1. 1. A process for the manufacture of diesel range hydrocarbons comprising the following steps:introducing a feedstock comprising bio oil and/or fat from renewable sources to a hydrotreatment step in which hydrocarbons are formed,isomerizing the formed hydrocarbons in an isomerization step,whereingas phase impurities formed in the hydrotreatment step are removed from the stream comprising hydrocarbons prior to contacting the hydrocarbons with the isomerization catalyst.2. The process according to claim 1 , further comprising a step of purifying the feedstock prior to the hydrotreatment step so as to remove impurities.3. The process according to claim 1 , wherein the gas phase impurities formed in the hydrotreatment step comprise propane claim 1 , water claim 1 , CO claim 1 , HS claim 1 , NHor mixtures thereof.4. The process according to claim 1 , wherein the removal of the gas phase impurities formed in the hydrotreatment step is performed in a stripping step upstream of the isomerization catalyst.5. The process according to claim 4 , wherein the stripping step is performed by stripping with water vapor or a suitable gas comprising light hydrocarbon claim 4 , nitrogen or hydrogen.6. The process according to claim 4 , wherein the stripping step is carried out in a counter-current manner.7. The process according to claim 1 , wherein the feedstock comprises more than 10 wt % of free fatty acids.8. The process according to claim 1 , wherein the feedstock contains less than 10 w-ppm alkaline and alkaline earth metals ...

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26-02-2015 дата публикации

ZSM-22 ZEOLITE, HYDROISOMERIZATION CATALYST AND METHOD FOR PRODUCING SAME, AND METHOD FOR PRODUCING HYDROCARBON

Номер: US20150057478A1
Принадлежит: JX NIPPON OIL & ENERGY CORPORATION

A method for producing a hydroisomerization catalyst includes a first step of preparing a support precursor by heating a mixture containing an ion-exchanged zeolite and a binder, the ion-exchanged zeolite being prepared by ion-exchanging an organic template-containing zeolite which contains an organic template and has a one-dimensional pore structure including a 10-membered ring in a solution containing ammonium ions and/or protons, at a temperature of 250 to 350° C. under Natmosphere, and a second step of preparing a hydroisomerization catalyst, which is prepared by calcining a catalyst precursor, the catalyst precursor being prepared based on the support precursor containing a platinum salt and/or a palladium salt, at a temperature of 350 to 400° C. in an atmosphere containing molecular oxygen, the hydroisomerization catalyst containing a support which includes a zeolite and carries platinum and/or palladium. 1. A method for producing a hydroisomerization catalyst comprising:{'sub': '2', 'a first step of preparing a support precursor by heating a mixture containing an ion-exchanged zeolite and a binder, the ion-exchanged zeolite being prepared by ion-exchanging an organic template-containing zeolite which contains an organic template and has a one-dimensional pore structure including a 10-membered ring in a solution containing ammonium ions and/or protons, at a temperature of 250 to 350° C. under Natmosphere; and'}a second step of preparing a hydroisomerization catalyst, which is prepared by calcining a catalyst precursor, the catalyst precursor being prepared based on the support precursor containing a platinum salt and/or a palladium salt, at a temperature of 350 to 400° C. in an atmosphere containing molecular oxygen, the hydroisomerization catalyst containing a support which includes a zeolite and carries platinum and/or palladium.2. The method for producing a hydroisomerization catalyst according to claim 1 ,wherein the organic template-containing zeolite is ...

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26-02-2015 дата публикации

METHOD FOR DEHYDRATING AND ISOMERISING ALCOHOLS USING A NON-ZEOLITE ALUMINOSILICATE SOLID

Номер: US20150057481A1
Принадлежит: IFP ENERGIES NOUVELLES

Process for simultaneous dehydration and skeletal isomerization of a feedstock that comprises at least one Cmonoalcohol and that contains between 0.5 and 50% water, for the purpose of producing Calkenes, with said process operating at a temperature of between 250 and 550° C., under a pressure of between 0.1 and 1 MPa, with an hourly volumetric flow rate of between 0.1 and 10 h, characterized in that it uses a catalyst that comprises at least one non-zeolitic aluminosilicate-type solid. 2. Process according to claim 1 , such that said feedstock for the most part comprises isobutanol.3. Process according to claim 1 , such that said silicic compound used in said stage a) is selected from among silicic acid claim 1 , the sols of silicic acid claim 1 , the water-soluble alkaline silicates claim 1 , and the cationic salts of silicon claim 1 , taken by itself or in a mixture.4. Process according to claim 1 , such that said aluminum compound used in said stage a) is selected from among boehmite claim 1 , pseudo-boehmite and the amorphous or essentially amorphous alumina gels claim 1 , taken by itself or in a mixture.5. Process according to claim 1 , such that said aluminosilicate-type solid has a silica content by mass of between 4 and 25% by weight of said solid.6. Process according to claim 5 , such that said aluminosilicate-type solid has a silica content by mass of between 4 and 15% by weight of said solid.7. Process according to claim 1 , such that said aluminosilicate-type solid has a silica content by mass of between 35 and 95% by weight of said solid.8. Process according to claim 7 , such that said aluminosilicate-type solid has a silica content by mass of between 35 and 50% by weight of said solid.9. Process according to claim 1 , such that said aluminosilicate-type solid has a cationic impurities content by mass that is less than 0.1% by weight of the catalyst.10. Process according to claim 1 , such that said aluminosilicate-type solid has an anionic impurities ...

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03-03-2016 дата публикации

Treatment of Off-Gas in the Production of Para-Xylene by the Methylation of Toluene and/or Benzene

Номер: US20160060187A1
Принадлежит:

A process for removing contaminants from an off-gas stream generated by the methylation of toluene and/or benzene by methanol to produce para-xylene. The treated off-gas stream, which contains C hydrocarbons, may be further processed in an olefins plant/process to yield valuable light alkanes and olefins. 1. A process for producing para-xylene , the process comprising:{'sub': '4', '(a) contacting toluene and/or benzene with methanol in the presence of an alkylation catalyst under conditions effective to produce an alkylation effluent comprising xylenes and a by-product mixture comprising water, dimethyl ether, C− hydrocarbons, and contaminants;'}(b) separating the alkylation effluent into a first fraction containing xylenes and a second fraction containing the by-product mixture;(c) recovering para-xylene from the first fraction; and(d) treating the second fraction to remove the contaminants.2. The process of claim 1 , wherein the para-xylene is recovered by fractional crystallization or selective adsorption.3. The process of claim 1 , wherein the treating (d) is accomplished by counter-currently contacting the second fraction with a C-Chydrocarbon absorbent in an absorber demethanizer.4. The process of claim 3 , wherein the absorbent consists essentially of a Cor Chydrocarbon or a mixture thereof.5. The process of claim 3 , wherein the absorbent consists essentially of a Chydrocarbon or a mixture thereof.6. The process of claim 3 , wherein the treating (d) produces an overhead stream comprising hydrogen claim 3 , methane and contaminants and a bottoms stream comprising C hydrocarbons and absorbent claim 3 , and further comprising:{'sub': '2+', '(e) separating the absorbent from the differing C hydrocarbons.'}7. The process of claim 6 , wherein the absorbent recovered in the separating (e) is recirculated to the treating (d).8. The process of claim 6 , wherein the separating (e) is accomplished by a single fractionation column.9. The process of claim 1 , further ...

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15-05-2014 дата публикации

Alkylated Aromatics Production

Номер: US20140135548A1

Disclosed is a process for the production of alkylated aromatics by contacting a feed stream comprising an alkylatable aromatic, an alkylating agent and trace amounts of water and impurities in the presence of a first catalyst and an alkylation catalyst wherein such water and impurities are removed in order to improve the cycle length of such alkylation catalysts. Water and at least a portion of impurities are removed in a dehydration zone. A reaction zone having a first catalyst which, in some embodiments is a large pore molecular sieve, acts to remove another portion of impurities, such as nitrogenous and other species. An alkylation zone having an alkylation catalyst which, in some embodiments is a medium pore molecular sieve or a MCM-22 family material, acts to remove additional impurities, and to alkylate the alkylatable aromatic compound.

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02-03-2017 дата публикации

SEPARATION OF CATALYST AND INERT HEAT PARTICLE AFTER AROMATIZATION OF A METHANE CONTAINING GAS STREAM

Номер: US20170057887A1
Принадлежит:

Implementations of the disclosed subject matter provide a process for the aromatization of a methane-containing gas stream may include contacting the methane-containing gas stream in a reaction zone comprising an aromatization catalyst particulate and an inert heat carrier particulate under methane-containing gas aromatization reaction conditions to produce a product stream comprising aromatics in the reaction zone. The inert heat carrier particulate may be separated from the aromatization catalyst particulate in a separation zone under separation conditions. The aromatization catalyst particulate may have a first minimum fluidization velocity and the inert heat carrier particulate may have a second minimum fluidization velocity which may be greater than the first minimum fluidization velocity. The ratio of the second minimum fluidization velocity to the first minimum fluidization velocity may be less than 200 and may be more than 15. 1. A process for the aromatization of a methane-containing gas stream comprising:contacting the methane-containing gas stream in a reaction zone comprising an aromatization catalyst particulate and an inert heat carrier particulate under methane-containing gas aromatization reaction conditions to produce a product stream comprising aromatics in the reaction zone;separating the inert heat carrier particulate from the aromatization catalyst particulate in a separation zone under separation conditions;wherein the aromatization catalyst particulate has a first minimum fluidization velocity and the inert heat carrier particulate has a second minimum fluidization velocity, wherein the second minimum fluidization velocity is greater than the first minimum fluidization velocity, and wherein the ratio of the second minimum fluidization velocity to the first minimum fluidization velocity is less than 200 and the ratio of the second minimum fluidization velocity to the first minimum fluidization velocity is more than 15.2. The process of claim 1 ...

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02-03-2017 дата публикации

SEPARATION OF CATALYST AND HYDROGEN ACCEPTOR AFTER AROMATIZATION OF A METHANE CONTAINING GAS STREAM

Номер: US20170057888A1
Принадлежит:

Implementations of the disclosed subject matter provide a process for the aromatization of a methane-containing gas stream including contacting the methane-containing gas stream in a reaction zone comprising an aromatization catalyst particulate and a hydrogen acceptor particulate under methane-containing gas aromatization reaction conditions to produce reaction products comprising aromatics and gaseous hydrogen. At least a portion of the gaseous hydrogen produced is bound by the hydrogen acceptor particulate in the reaction zone and removed from the reaction products in the reaction zone. Further, the hydrogen acceptor particulate may be separated from the aromatization catalyst particulate in a separation zone under separation conditions. 1. A process for the aromatization of a methane-containing gas stream comprising:contacting the methane-containing gas stream in a reaction zone comprising an aromatization catalyst particulate and a hydrogen acceptor particulate under methane-containing gas aromatization reaction conditions to produce reaction products comprising aromatics and gaseous hydrogen, wherein at least a portion of the gaseous hydrogen produced is bound by the hydrogen acceptor particulate in the reaction zone and removed from the reaction products in the reaction zone, andseparating the hydrogen acceptor particulate from the aromatization catalyst particulate in a separation zone under separation conditions.2. The process of claim 1 , wherein the aromatization catalyst particulate has a first set of physical properties comprising a first minimum fluidization velocity claim 1 , and wherein the hydrogen acceptor particulate has a second set of physical properties comprising a second minimum fluidization velocity claim 1 , and wherein the first minimum fluidization velocity is different from the second minimum fluidization velocity.3. The process of claim 2 , wherein the ratio of the second minimum fluidization velocity to the first minimum fluidization ...

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08-03-2018 дата публикации

Acidic Aromatization Catalyst with Improved Activity and Stability

Номер: US20180065115A1
Принадлежит:

Methods for producing supported catalysts containing a transition metal and a bound zeolite base are disclosed. These methods employ a step of impregnating the bound zeolite base with the transition metal, fluorine, and high loadings of chlorine. The resultant high chlorine content supported catalysts have improved catalyst activity in aromatization reactions. 1. A supported catalyst comprising:a bound zeolite base;from about 0.3 wt. % to about 3 wt. % of a transition metal;from about 1.8 wt. % to about 4 wt. % of chlorine; andfrom about 0.4 wt. % to about 1.5 wt. % of fluorine, based on the total weight of the supported catalyst;wherein the supported catalyst is characterized by a peak reduction temperature on a Temperature Programmed Reduction curve in a range from about 580° F. to about 800° F.2. The catalyst of claim 1 , wherein the bound zeolite base comprises from about 5 wt. % to about 30 wt. % of a binder claim 1 , based on the total weight of the bound zeolite base.3. The catalyst of claim 1 , wherein:the bound zeolite base comprises a silica-bound K/L-zeolite;the transition metal comprises platinum; anda weight ratio of chlorine:fluorine is in a range from about 2:1 to about 5:1.4. The catalyst of claim 1 , wherein the supported catalyst comprises:from about 0.5 wt. % to about 2 wt. % of platinum;from about 2.2 wt. % to about 3.4 wt. % of chlorine; andfrom about 0.5 wt. % to about 1.1 wt. % of fluorine.5. The catalyst of claim 4 , wherein the supported catalyst is characterized by a peak reduction temperature on a Temperature Programmed Reduction curve in a range from about 600° F. to about 720° F.6. The catalyst of claim 1 , wherein the supported catalyst has a total nitrogen content that is greater than that of a catalyst having from 0.3 wt. % to 1.5 wt. % chlorine claim 1 , under the same catalyst preparation conditions.7. The catalyst of claim 1 , wherein the supported catalyst is characterized by a Temperature Programmed Reduction curve comprising a ...

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11-03-2021 дата публикации

CATALYTIC HYDROCARBON DEHYDROGENATION

Номер: US20210069683A1
Принадлежит:

A catalyst for dehydrogenation of hydrocarbons includes a support including zirconium oxide and Linde type L zeolite (L-zeolite). A concentration of the zirconium oxide in the catalyst is in a range of from 0.1 weight percent (wt. %) to 20 wt. %. The catalyst includes from 5 wt. % to 15 wt. % of an alkali metal or alkaline earth metal. The catalyst includes from 0.1 wt. % to 10 wt. % of tin. The catalyst includes from 0.1 wt. % to 8 wt. % of a platinum group metal. The alkali metal or alkaline earth metal, tin, and platinum group metal are disposed on the support. 1. A catalyst for dehydrogenation of hydrocarbons , the catalyst comprising:a support comprising zirconium oxide and Linde type L zeolite (L-zeolite), wherein a concentration of the zirconium oxide in the catalyst is in a range of from 0.1 weight percent (wt. %) to 20 wt. %;from 5 wt. % to 15 wt. % of an alkali metal or alkaline earth metal, the alkali metal or alkaline earth metal disposed on the support;from 0.1 wt. % to 10 wt. % of tin, the tin disposed on the support; andfrom 0.1 wt. % to 8 wt. % of a platinum group metal, the platinum group metal disposed on the support.2. The catalyst of claim 1 , wherein the alkali metal or alkaline earth metal is selected from the group consisting of lithium claim 1 , sodium claim 1 , potassium claim 1 , rubidium claim 1 , cesium claim 1 , beryllium claim 1 , magnesium claim 1 , calcium claim 1 , and barium.3. The catalyst of claim 2 , wherein the alkali metal is potassium or cesium.4. The catalyst of claim 2 , wherein the platinum group metal is selected from the group consisting of platinum claim 2 , ruthenium claim 2 , iridium claim 2 , rhodium claim 2 , and palladium.5. The catalyst of claim 2 , wherein the catalyst is configured to dehydrogenate hydrocarbons including 3 to 6 carbon atoms at an operating temperature in a range of from about 500 degrees Celsius (° C.) to about 800° C. and an operating pressure in a range of from about 0.01 bar to about 10 bar.6. ...

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12-03-2015 дата публикации

PROCESS AND SYSTEM FOR EXTRACTION OF A FEEDSTOCK

Номер: US20150071850A1
Автор: Rhodey William George
Принадлежит:

The present invention relates to a method and system for recovering aromatics from a naphtha feedstock obtained from a crude petroleum, natural gas condensate, or petrochemical feedstock. The method and system comprise the steps of recovering an aromatics fraction from the feedstock prior to reforming. 127.-. (canceled)28. A method of recovering aromatics comprising the steps of:{'sub': 6', '11, '(a) providing a Cto Chydrocarbon fraction;'}{'sub': 6', '11, '(b) recovering from the Cto Chydrocarbon fraction an aromatics fraction, an aromatics precursors fraction and a raffinate fraction in an aromatics extraction unit;'}(c) converting aromatics precursors in the aromatics precursors fraction to aromatics; and(d) recovering aromatics from step (c) in an aromatics extraction unit;{'sub': 6', '11, 'wherein the Cto Chydrocarbon fraction provided in step (a) is subjected to step (b) without having been subjected to a reforming or a dehydrogenation process.'}29. The method according to claim 28 , wherein the Cto Chydrocarbon fraction is obtained by separation from a naphtha feedstock.30. The method according to claim 28 , wherein the Cto Chydrocarbon fraction is obtained by separation from a Cfraction of a naphtha feedstock.31. The method according to claim 28 , further comprising recovering from step (d) any unreacted aromatics precursors and returning them to step (c) for conversion to aromatics.32. The method according to claim 28 , wherein benzene claim 28 , toluene claim 28 , xylenes claim 28 , or a combination thereof claim 28 , are recovered claim 28 , and the aromatics precursors fraction comprises Cto Cnaphthenes and paraffins.33. The method according to claim 32 , wherein the aromatics precursors fraction is further fractionated by fractional distillation to selectively concentrate C claim 32 , C claim 32 , or Cnaphthenes claim 32 , or a combination thereof claim 32 , in the aromatics precursors fraction claim 32 , with C claim 32 , Cor Cnormal paraffins claim 32 ...

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11-03-2021 дата публикации

Multistage Nanoreactor Catalyst and Preparation and Application Thereof

Номер: US20210070672A1
Принадлежит:

The present disclosure discloses a multistage nanoreactor catalyst and preparation and application thereof, belonging to the technical field of synthesis gas conversion. The catalyst consists of a core of an iron-based Fischer-Tropsch catalyst, a transition layer of a porous oxide or porous carbon material, and a shell layer of a molecular sieve having an aromatization function. The molecular sieve of the shell layer can be further modified by a metal element or a non-metal element, and the outer surface of the molecular sieve is further modified by a silicon-oxygen compound to adjust the acidic site on the outer surface and the aperture of the molecular sieve, thereby inhibiting the formation of heavy aromatic hydrocarbons. According to the disclosure, the shell layer molecular sieve with a transition layer and a shell layer containing or not containing auxiliaries, and with or without surface modification can be prepared by the iron-based Fischer-Tropsch catalyst through multiple steps. The catalyst can be used for direct preparation of aromatic compounds, especially light aromatic compounds, from synthesis gas; the selectivity of light aromatic hydrocarbons in hydrocarbons can be 75% or above, and the content in the liquid phase product is not less than 95%; and the catalyst has good stability and good industrial application prospect. 1. A multistage nanoreactor catalyst , comprising a structure of a core , a shell body and a core-shell transition layer; wherein the core layer is an iron-based catalyst having Fischer-Tropsch activity , weight of the core layer being 0.1% to 80% of total weight of the catalyst; wherein the shell body is a molecular sieve , the weight of the shell body being 0.1% to 80% of the total weight of the catalyst; and wherein the core-shell transition layer is a porous oxide or porous carbon material , the weight of the transition layer being 0.01% to 35% of the total weight of the catalyst.2. The multistage nanoreactor catalyst according ...

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12-03-2015 дата публикации

LINEAR ALKYLBENZENES FROM NATURAL OILS AND METHODS OF PRODUCING

Номер: US20150072916A1
Принадлежит: UOP LLC

The production of linear alkylbenzene from a natural oil is provided. A method comprises the step of deoxygenating the natural oils to form a stream comprising paraffins. The paraffins are dehydrogenated to provide mono-olefins. Then, benzene is alkylated with the mono-olefins under alkylation conditions to provide an alkylation effluent comprising alkylbenzenes and benzene. Thereafter, the alkylbenzenes are isolated to provide the alkylbenzene product. 1. A method for generating an alkylbenzene product from a natural oil comprising:deoxygenating feedstock comprising natural oil having less than about 3 wt. ppm of nitrogen contained in nitrogen containing compounds to form a stream comprising paraffins;dehydrogenating at least a portion of the paraffins to provide mono-olefins;alkylating benzene with the mono-olefins under alkylation conditions to provide an alkylation effluent comprising alkylbenzenes and benzene;separating the alkylbenzenes to provide the alkylbenzene product comprising alkylbenzenes having an alkyl group of about n carbon atoms where n is from 12 to about 13 and wherein the alkyl group is a linear alkyl group for for at least 80 mass % of the alkylbenzenes having an alkyl group of about n carbon atoms.2. The alkylbenzene product produced by the method of .31. The method of further comprising claim 1 , sulfonating the alkylbenzene product to form a linear alkylbenzene sulfonate product.4. The linear alkylbenzene sulfonate product produced by the method of .5. The method of further comprising where n is expanded to include from 8 to 15.6. The method of further comprising where n is expanded to include from 10 to 13.7. The method of further comprising where n is expanded to include from 9 to 14.8. The method of wherein a hydrogen stream results from dehydrogenating the paraffins claim 1 , and wherein the method further comprises recycling the hydrogen stream to the deoxygenating step.9. The method of further comprising separating a second portion of ...

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12-03-2015 дата публикации

HIGH TEMPERATURE CCR PROCESS WITH INTEGRATED REACTOR BYPASSES

Номер: US20150073189A1
Принадлежит:

A process is presented for increasing the aromatics content in a reformate process stream. The process modifies existing processes to change the operation without changing the reactors or heating units. The process includes bypasses to utilize heating capacity of upstream heating units, and passes the excess capacity of the upstream heating units to downstream process streams. 1. A process for increasing the aromatic content of a hydrocarbon stream , comprising:passing the hydrocarbon stream through a series of reforming reactors and reactor feed heaters, wherein the reactors feed heaters generate a heated stream and at least one of the heated streams is split into a first portion and a second portion, with the first portion passed to a reforming reactor to generate a reforming reactor effluent stream; andwherein the second portion of the heated stream is combined with a downstream reforming reactor effluent stream and the combined stream is passed to a downstream reactor feed heater, to generate a reactor product stream with increased aromatic content.2. The process of wherein the first reactor is operated at a first temperature claim 1 , and the subsequent reactors are operated at a second temperature and the second temperature is greater than the first temperature.3. The process of further comprising:splitting at least one reactor effluent stream into a first portion and a second portion;passing the first portion of the effluent stream with the second portion of the heated stream to a reactor interheater; andcombining the second portion of the effluent stream with a downstream heated feedstream to a downstream reactor.4. The process of wherein the downstream reactor is the next reactor in the series of reactors.5. The process of wherein the downstream reactor is the reactor after the next reactor in the series of reactors.6. The process of wherein the first reaction temperature is between 400° C. and 500° C.7. The process of wherein there are at least two ...

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12-03-2015 дата публикации

Methods of Regenerating Aromatization Catalysts

Номер: US20150073190A1
Автор: Wu An-Hsiang
Принадлежит:

Methods for treating or rejuvenating a spent catalyst are disclosed. Such methods can employ a step of halogenating the spent catalyst, followed by decoking the halogenated spent catalyst. The halogenation step can utilize fluorine and chlorine together, or fluorine and chlorine can be applied sequentially. 120-. (canceled)21. A method of treating a spent catalyst comprising a transition metal and a catalyst support , the method comprising:(1) contacting the spent catalyst with a chlorine-containing stream comprising a chlorine-containing compound to produce a chlorinated spent catalyst;(2) contacting the chlorinated spent catalyst with a fluorine-containing stream comprising a fluorine-containing compound to produce a chlorinated-fluorinated spent catalyst; and(3) contacting the chlorinated-fluorinated spent catalyst with a decoking gas stream comprising oxygen;wherein the spent catalyst comprises from about 0.1 wt. % to about 10 wt. % transition metal, based on the weight of the spent catalyst excluding carbon.22. The method of claim 21 , wherein the spent catalyst comprises:platinum on a KL-zeolite;a support matrix comprising alumina, silica, a mixed oxide thereof, or a mixture thereof;from about 0.025 wt. % to about 5 wt. % chlorine; andfrom about 0.025 wt. % to about 5 wt. % fluorine.23. The method of claim 22 , wherein step (1) is conducted at a chlorination temperature in a range from about 25° C. to about 250° C.24. The method of claim 22 , wherein a concentration of chlorine (Cl) in the chlorine-containing stream is in a range from about 50 to about 25 claim 22 ,000 ppm by volume.25. The method of claim 22 , wherein the chlorine-containing stream comprises Cland nitrogen claim 22 , and is substantially free of oxygen-containing compounds.26. The method of claim 22 , wherein step (2) is conducted at a fluorination temperature in a range from about 10° C. to about 100° C.27. The method of claim 22 , wherein a concentration of fluorine (F) in the fluorine- ...

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12-03-2015 дата публикации

CATALYSTS FOR PETROCHEMICAL CATALYSIS

Номер: US20150073192A1
Принадлежит:

Metal oxide catalysts comprising various dopants are provided. The catalysts are useful as heterogenous catalysts in a variety of catalytic reactions, for example, the oxidative coupling of methane to C2 hydrocarbons such as ethane and ethylene. Related methods for use and manufacture of the same are also disclosed. 185-. (canceled)86. A method for the preparation of ethane , ethylene or combinations thereof , the method comprising contacting a catalyst with a gas comprising methane , the catalyst comprising:{'sub': 4-x', 'x', '6, 'the formula Ln1Ln2O, wherein Ln1 and Ln2 are each independently a different lanthanide element, and x is a number ranging from greater than 0 to less than 4; and'}at least one doping element from groups 1-16, lanthanides, actinides or combinations thereof,{'sub': '2', 'wherein the catalyst further comprises a Cselectivity of greater than 50% and a methane conversion of greater than 20% when the catalyst is employed as a heterogeneous catalyst in the oxidative coupling of methane at a temperature of 750° C. or less.'}87. The method of claim 86 , wherein the at least one doping element is selected from groups 1-4 claim 86 , 8 claim 86 , 13 claim 86 , 14 claim 86 , lanthanides claim 86 , actinides and combinations thereof.88. The method of claim 86 , wherein the at least one doping element is selected from groups 1-6 claim 86 , 8 claim 86 , 11 claim 86 , 13-15 claim 86 , lanthanides claim 86 , actinides and combinations thereof.89. The method of claim 86 , wherein the at least one doping element is a rare earth element.90. The method of claim 86 , wherein the at least one doping element is Na claim 86 , Mg claim 86 , Ca claim 86 , Sr claim 86 , Ga claim 86 , Sc claim 86 , Y claim 86 , Zr claim 86 , In claim 86 , Nd claim 86 , Eu claim 86 , Sm claim 86 , Ce claim 86 , Gd claim 86 , Hf claim 86 , Ho claim 86 , Tm claim 86 , W claim 86 , La claim 86 , K claim 86 , Dy claim 86 , In claim 86 , Cs claim 86 , S claim 86 , Zn claim 86 , Rb claim 86 ...

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12-03-2015 дата публикации

Process for Nitrile Removal from Hydrocarbon Feeds

Номер: US20150073193A1
Принадлежит: ExxonMobil Chemical Patents Inc

A process is described, such process comprising i) contacting a hydrocarbon feed with a heterogeneous catalyst under conditions suitable to hydrolyze nitriles present in the feed to form a nitrile hydrolysis product comprising ammonia, carboxylic acid and carboxylate salts or a mixture thereof; and ii) removing the nitrile hydrolysis product from the feed. In an embodiment, the hydrocarbon feed comprises olefins and is intended for use in an olefin oligomerization process.

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12-03-2015 дата публикации

Oxygenates-Free C8-C12 Aromatic Hydrocarbon Stream and a Process for Preparing the Same

Номер: US20150073197A1
Принадлежит: Reliance Industries Ltd

The present disclosure provides a process for separating oxygenates present in an aromatic hydrocarbon stream to obtain an oxygenates-free aromatic hydrocarbon stream. The process involves selectively removing oxygenates from the aromatic hydrocarbon stream by passing said stream through at least one zeolite based adsorbing material.

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17-03-2016 дата публикации

In-situ Trim Coke Selectivation of Toluene Disproportionation Catalyst

Номер: US20160074845A1
Принадлежит: ExxonMobil Chemical Patents Inc.

The invention relates to treating a molecular sieve prepared by at least one in situ selectivation sequence wherein graphitic coke is adhered to said molecular sieve, which is useful in a toluene disproportionation process. 1. A method for modifying a molecular sieve comprising:treating a molecular sieve prepared by at least one ex situ silicon selectivation sequence to at least one in situ trim coke selectivation sequence to provide a modified silicon selectivated molecular sieve, wherein graphitic coke is adhered to said molecular sieve by said in situ trim coke selectivation sequence.2. The method of claim 1 , wherein said ex situ silicon selectivation sequence comprises:contacting said molecular sieve with a silicon-containing selectivating agent comprising silicones or silicone polymers, to provide a silicon-treated molecular sieve;calcining said silicon-treated molecular sieve to provide a calcined silicon selectivated molecular sieve;optionally steam treating said calcined silicon selectivated molecular sieve.3. The method of claim 1 , wherein said molecular sieve has been modified by between two and six ex situ silicon selectivation sequences and including at least one steam-treating.4. The method of claim 1 , wherein said molecular sieve has been modified by two ex situ silicon selectivation sequences.5. The method of any one of the preceding claims claim 1 , wherein said molecular sieve has been modified by three ex situ silicon selectivation sequences.6. The method of claim 1 , wherein the in situ trim coke selectivation conditions comprise a reactor temperature of about 260-593° C. claim 1 , for about 0.1 hour to about 3 weeks claim 1 , operating at a WHSV of about 0.1-20 hr claim 1 , and a hydrogen partial pressure of about 0.0689-2.07 Mpa-a claim 1 , with a reactor pressure of about 1.72-2.41 Mpa-g.7. The method of claim 6 , wherein the in situ trim coke selectivation conditions comprise a reactor temperature of about 454-510° C. claim 6 , operating at ...

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19-03-2015 дата публикации

Production and Use of 3,4' and 4,4'-Dimethylbiphenyl Isomers

Номер: US20150080546A1
Принадлежит:

In a process for producing 3,4′ and/or 4,4′ dimethyl-substituted biphenyl compounds, a feed comprising toluene is contacted with hydrogen in the presence of a hydroalkylation catalyst under conditions effective to produce a hydroalkylation reaction product comprising (methylcyclohexyl)toluenes. At least part of the hydroalkylation reaction product is dehydrogenated in the presence of a dehydrogenation catalyst under conditions effective to produce a dehydrogenation reaction product comprising a mixture of dimethyl-substituted biphenyl isomers. The dehydrogenation reaction product is then separated into at least a first stream containing at least 50% of 3,4′ and 4,4′ dimethylbiphenyl isomers by weight of the first stream and at least one second stream comprising one or more 2,x′ (where x′ is 2′, 3′, or 4′) and 3,3′ dimethylbiphenyl isomers. 1. A process for producing 3 ,4′ and/or 4 ,4′ dimethyl-substituted biphenyl compounds , the process comprising:(a2) contacting a feed comprising benzene with hydrogen in the presence of a hydroalkylation catalyst under conditions effective to produce a hydroalkylation reaction product comprising cyclohexylbenzenes;(b2) dehydrogenating at least part of the hydroalkylation reaction product in the presence of a dehydrogenation catalyst under conditions effective to produce a dehydrogenation reaction product comprising biphenyl;(c2) reacting at least part of the dehydrogenation reaction product with a methylating agent in the presence of an alkylation catalyst under conditions effective to produce a methylation reaction product comprising a mixture of dimethyl-substituted biphenyl isomers; and(d2) separating the methylation reaction product into at least a first stream containing at least 50% of 3,4′ and 4,4′ dimethylbiphenyl isomers by weight of the first stream and at least one second stream comprising one or more 2,X′ (where X′ is 2′, 3′, or 4′) and 3,3′ dimethylbiphenyl isomers.2. The process of claim 1 , wherein the ...

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14-03-2019 дата публикации

CATALYSTS FOR PETROCHEMICAL CATALYSIS

Номер: US20190077728A1
Принадлежит:

Metal oxide catalysts comprising various dopants are provided. The catalysts are useful as heterogenous catalysts in a variety of catalytic reactions, for example, the oxidative coupling of methane to C2 hydrocarbons such as ethane and ethylene. Related methods for use and manufacture of the same are also disclosed. 140-. (canceled)41. A catalyst comprising a mixed oxide of a lanthanide and tungsten , wherein the catalyst further comprises a sodium dopant and at least one doping element from groups 2 , 4-15 , lanthanides or combinations thereof , wherein the catalyst comprises a Cselectivity of greater than 50% and a methane conversion of greater than 20% when the catalyst is employed as a heterogeneous catalyst in the oxidative coupling of methane at a temperature of 750° C. or less.42. The catalyst of claim 41 , wherein the lanthanide is Ce claim 41 , Pr claim 41 , Nd claim 41 , La claim 41 , Eu claim 41 , Sm or Yb.43. The catalyst of claim 41 , wherein the at least one doping element is Fe claim 41 , Co claim 41 , Mn claim 41 , Cu claim 41 , Ni claim 41 , Sr claim 41 , Ga claim 41 , Zr claim 41 , Pb claim 41 , Zn claim 41 , Cr claim 41 , Pt claim 41 , Al claim 41 , Nb claim 41 , La claim 41 , Ba claim 41 , Bi claim 41 , Sn claim 41 , In claim 41 , Ru claim 41 , P or combinations thereof.44. A catalyst comprising a rare earth oxide and two or more dopants claim 41 , wherein the catalyst comprises a Cselectivity of greater than 50% and a methane conversion of greater than 20% when the catalyst is employed as a heterogeneous catalyst in the oxidative coupling of methane at a temperature of 750° C. or less claim 41 , and wherein the dopant comprises Eu/Na claim 41 , Sr/Na claim 41 , Na/Zr/Eu/Ca claim 41 , Mg/Na claim 41 , Sr/Sm/Ho/Tm claim 41 , Sr/W claim 41 , Mg/La/K claim 41 , Na/K/Mg/Tm claim 41 , Na/Dy/K claim 41 , Na/La/Dy claim 41 , Na/La/Eu claim 41 , Na/La/Eu/In claim 41 , Na/La/K claim 41 , Na/La/Li/Cs claim 41 , K/La claim 41 , K/La/S claim 41 , K/Na claim ...

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24-03-2016 дата публикации

PROCESS FOR CONVERSION OF LIGHT ALIPHATIC HYDROCARBONS TO AROMATICS

Номер: US20160083313A1
Принадлежит:

A process is disclosed for the aromatization and alkylation of light aliphatic hydrocarbons, such as propane or propylene, into aromatic hydrocarbons. The process provides increased aromatics production and decreases methane and ethane production. This improvement for the aromatization and alkylation of light aliphatic hydrocarbons is achieved by adding a benzene stream to the light paraffin feed components. 1. A method of hydrocarbon conversion comprising:feeding a vapor phase feed stream comprising a light aliphatic hydrocarbon stream and a light aromatic stream to a reaction zone comprising a catalyst and contacting the feed stream with the catalyst to form a reaction zone effluent stream comprising an aromatic product.2. The method of wherein the light aliphatic hydrocarbon stream is rich in at least one of Chydrocarbons claim 1 , Chydrocarbons claim 1 , or a combination thereof.3. The method of wherein the light aliphatic hydrocarbon stream is rich in Chydrocarbons.4. The method of wherein feeding the vapor phase feed stream comprising light aliphatic hydrocarbons to the reaction zone comprises feeding at least a portion of the reaction zone effluent stream comprising light aliphatic hydrocarbons claim 1 , at least a portion of the reaction zone effluent stream comprising light aromatic hydrocarbons claim 1 , and a fresh feed stream comprising light aliphatic and light aromatic hydrocarbons to the reaction zone.5. The method of wherein the reaction zone comprises at least one reactor.6. The method of claim 1 , wherein the pressure of the reaction zone is between about 17 to about 200 Psig.7. The method of wherein the catalyst comprises a zeolite.8. The method of wherein the catalyst comprises at least one active metal.9. The method of wherein the catalyst comprises less than 1.5% gallium.10. The method of claim 1 , wherein the reaction zone effluent stream comprises benzene claim 1 , toluene claim 1 , xylenes claim 1 , and heavier aromatics.11. The method of ...

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12-03-2020 дата публикации

PROCESS FOR SELECTIVE PRODUCTION OF LIGHT OLEFINS AND AROMATIC FROM CRACKED LIGHT NAPHTHA

Номер: US20200080006A1
Принадлежит:

The present invention provides a process for a production of light olefins and aromatics from cracked light naphtha by selective cracking. The present invention thus provides a process for up grading cracked olefinic naphtha to high value petrochemical feed stocks. This process is based on catalytic cracking in which the catalyst activity is optimized by depositing coke for production of light olefins and aromatics. The proposed process has high flexibility and can be operated either in maximizing olefins as reflected from the PIE ratio or in maximizing aromatics (BTX) at different modes of operation depending upon the product requirement. 1. A process for selective production of light olefins and aromatics , the process comprising:a) feeding a mixed olefinic cracked naphtha feedstock into a reactor; (i) wherein under olefinic mode of operation, the mixed olefinic cracked naphtha is catalytically cracked by contacting with a zeolite catalyst for a residence time ranging between 35-65 minutes and at a pressure ranging between 1-2 bar to obtain a cracked product comprising light olefins in the range of 30-50 wt % and obtaining the light olefins as a gaseous product with a propylene to ethylene ratio (PIE) in the range of 1-5;', '(ii) wherein under aromatic mode of operation, the mixed olefinic cracked naphtha is catalytically cracked by contacting with a zeolite catalyst for a residence time ranging between 20-35 minutes and at a pressure ranging between 5-7 bar to obtain a cracked product comprising aromatics in the range of 10-25 wt % and obtaining the aromatics as a liquid product; and, 'b) catalytic cracking of the mixed olefinic cracked naphtha in the reactor under olefinic mode or aromatic mode of operation,'}c) recovering spent catalyst from the reactor and feeding the spent catalyst to a regenerator to obtain a regenerated catalyst and recycling the regenerated catalyst to the reactor.2. The process as claimed in claim 1 , wherein the mixed olefinic cracked ...

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21-03-2019 дата публикации

Crystalline Germanosilicate Materials Of New CIT-13 Topology And Methods Of Preparing The Same

Номер: US20190083962A1
Принадлежит:

The present disclosure is directed to the use of novel crystalline germanosilicate compositions in affecting a range of organic transformations. In particular, the crystalline germanosilicate compositions are extra-large-pore compositions, designated CIT-13 possessing 10- and 14-membered rings. 2. The process of comprising:(c) cracking, hydrocracking, or dehydrogenating a hydrocarbon;(d) dewaxing a hydrocarbon feedstock;(d) converting paraffins to aromatics:(e) isomerizing or disproportionating an aromatic feedstock;(f) alkylating an aromatic hydrocarbon;(g) oligomerizing an alkene;(i) separating and sorbing a lower alkane from a hydrocarbon feedstock;(j) isomerizing an olefin;(k) producing a higher molecular weight hydrocarbon from lower molecular weight hydrocarbon; or(l) reforming a hydrocarbon.3. The process of comprising converting synthesis gas containing hydrogen and carbon monoxide to a hydrocarbon stream using a catalyst comprising the crystalline microporous germanosilicate composition and a Fischer-Tropsch catalyst.4. The process of comprising reducing the concentration of an organic halide in an initial hydrocarbon product claim 1 , the initial hydrocarbon product containing an undesirable level of the organic halide claim 1 , the process comprising contacting at least a portion of the initial hydrocarbon product with a composition comprising the crystalline microporous germanosilicate composition claim 1 , under organic halide absorption conditions to reduce the halogen concentration in the hydrocarbon.6. The process of claim 1 , wherein the crystalline microporous germanosilicate composition exhibits a powder X-ray diffraction (XRD) pattern exhibiting at least seven of the characteristic peaks at 6.45±0.2 claim 1 , 7.18±0.2 claim 1 , 12.85±0.2 claim 1 , 18.26±0.2 claim 1 , 18.36±0.2 claim 1 , 18.63±0.2 claim 1 , 20.78±0.2 claim 1 , 21.55±0.2 claim 1 , 23.36±0.2 claim 1 , 24.55±0.2 claim 1 , 26.01±0.2 claim 1 , and 26.68±0.2 degrees 2-θ.7. The process ...

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31-03-2016 дата публикации

Methods and apparatus for producing jet-range hydrocarbons

Номер: US20160090333A1
Принадлежит: UOP LLC

Methods and apparatus are provided for producing jet-range hydrocarbons from biorenewable sources, such as oligomerizing C 3 -C 8 biorenewable olefins, for example, derived from C 3 -C 8 alkanol products of fermentation of biomass. Production of jet-range hydrocarbons is increased by employing an additional oligomerization zone for oligomerizing naphtha separated from the effluent of a primary oligomerization zone wherein the C 3 -C 8 biorenewable olefins were first subjected to oligomerization.

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31-03-2016 дата публикации

METHODS FOR PRODUCING ALKYLAROMATICS

Номер: US20160090338A1
Принадлежит:

Disclosed is a method for process for transalkylation of aromatic compounds comprising introducing a feed stream comprising aromatic hydrocarbon compounds to the transalkylation zone; introducing a water source to the transalkylation zone; contacting the feed stream with a zeolitic transalkylation catalyst; and producing an ethylbenzene product stream. This method increases ethylbenzene yield while improving the selectivity of the catalyst. 1. A process for transalkylation of aromatic compounds comprising:introducing a feed stream comprising aromatic hydrocarbon compounds to the transalkylation zone;introducing a water source to the transalkylation zone;contacting the feed stream with a transalkylation catalyst; andproducing an ethylbenzene product stream.2. The process of wherein the feed stream introduced to the transalkylation zone comprises benzene and polyethylbenzene.3. The process of claim 1 , wherein the water source is introduced to the transalkylation zone in an amount to provide between 100 ppm-wt and 500 ppm-wt of water based upon the mass of the feed stream.4. The process of claim 1 , wherein the zeolitic transalkylation catalyst comprises a modified Y zeolite catalyst.5. The process of claim 1 , wherein the transalkylation zone comprises at least one transalkylator.6. The process of claim 1 , wherein the ethylbenzene yield is 99.5 to 99.9% by weight.7. A process for transalkylation of aromatic compounds comprising:introducing a feed stream comprising aromatic hydrocarbon compounds to the transalkylator;introducing a water source to the transalkylator;contacting the feed stream with a zeolitic transalkylation catalyst in the presence of water; andproducing an ethylbenzene product stream.8. The process of wherein the feed stream introduced to the transalkylator comprises benzene and polyethylbenzene.9. The process of claim 7 , wherein the water source is introduced to the transalkylator in an amount to provide between 100 ppm-wt and 500 ppm-wt of water ...

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30-03-2017 дата публикации

Hydrocarbon Dehydrocyclization in the Presence of Carbon Dioxide

Номер: US20170088486A1
Принадлежит:

The invention relates to converting non-aromatic hydrocarbon in the presence of COto produce aromatic hydrocarbon. COmethanation using molecular hydrogen produced during the aromatization increases aromatic hydrocarbon yield. The invention also relates to equipment and materials useful in such upgrading, to processes for carrying out such upgrading, and to the use of such processes for, e.g., natural gas upgrading. 1. A hydrocarbon conversion process , comprising:{'sub': 2+', '2, '(a) providing a feed comprising ≧1 wt. % of C non-aromatic hydrocarbon and ≧0.1 wt. % of CO;'} the first catalyst includes (i) ≧0.005 wt. % of a dehydrogenation component which comprises one or more of Ga, Zn, Mo, W, La, Pt, and Pd, and (ii) ≧10 wt. % of a molecular sieve component, the molecular sieve component comprising at least one molecular sieve having a Constraint Index in the range of from 1 to 12, and', {'sub': '2', 'the second catalyst includes ≧0.005 wt. % of a COconversion component which comprises one or more of Ru, Rh, Ni, Co, and Fe;'}], '(b) providing first and second catalysts, wherein'}{'sub': 2+', '2, "(c) exposing the feed to the first catalyst under conversion conditions effective for (i) converting ≧10 wt. % of the feed's C non-aromatic hydrocarbon to aromatic hydrocarbon and molecular hydrogen and (ii) increasing aromatic hydrocarbon yield by reacting ≧1 wt. % of the feed's COwith at least a portion of the molecular hydrogen in the presence of the second catalyst to produce methane and water."}2. The process of claim 1 , wherein the feed comprises ≧1 wt. % of CO; 10 wt. % to 40 wt. % ethane; 20 wt. % to 50 wt. % propane claim 1 , and 20 wt. % to 50 wt. % butanes claim 1 , and further comprises 1 wt. % to 40 wt. % methane and ≦1 wt. % of aromatic hydrocarbon.3. The process of claim 1 , wherein the COreaction of step (c) has a greater selectivity for methane than CO.4. The process of claim 1 , wherein (i) the first catalyst includes (i) ≧0.01 wt. % of the ...

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30-03-2017 дата публикации

Hydrocarbon Conversion

Номер: US20170088487A1
Принадлежит:

The invention relates to the conversion of light hydrocarbon to higher-value hydrocarbon, such as aromatic hydrocarbon, to equipment and materials useful in such conversion, and to the use of such conversion for, e.g., natural gas upgrading. The conversion can be carried out in two stages, with each stage containing a dehydrocyclization catalyst comprising at least one dehydrogenation component and at least one molecular sieve. 1. A hydrocarbon conversion process , comprising:(a) providing a feed comprising ≧1 wt. % of non-aromatic hydrocarbon,(b) providing first and second catalysts, wherein (i) the first catalyst comprises ≧10 wt. % of a first molecular sieve component and ≧0.005 wt. % of a first dehydrogenation component and (ii) the second catalyst comprises ≧10 wt. % of a second molecular sieve component and ≧0.005 wt. % of a second dehydrogenation component;{'sub': '1', '(c) contacting the feed with the first catalyst under catalytic dehydrocyclization conditions including a temperature Tin the range of from 400° C. to 630° C. to produce a first product comprising ≧1 wt. % aromatic hydrocarbon; and'}{'sub': 2', '1', '2, "(d) contacting ≧50 wt. % of the first product, including ≧50 wt. % of the first product's aromatic hydrocarbon, with the second catalyst under catalytic dehydrocyclization conditions including a temperature Tin the range of from 450° C. to 700° C., to produce a second product comprising ≧1 wt. % of additional aromatic hydrocarbon, wherein T≦0.9·T."}2. The process of claim 1 , wherein (i) the first and second molecular sieve components each comprise (i) one or more of MCM-22 claim 1 , ZSM-5 claim 1 , ZSM-11 claim 1 , ZSM-12 claim 1 , ZSM-22 claim 1 , ZSM-23 claim 1 , ZSM-35 claim 1 , and ZSM-48 and/or (ii) the first and second dehydrogenation components each comprise one or more of Ga claim 1 , Zn claim 1 , Cu claim 1 , Re claim 1 , Mo claim 1 , W claim 1 , La claim 1 , Fe claim 1 , Ag claim 1 , Pt claim 1 , and Pd.3. The process of claim 1 , ...

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30-03-2017 дата публикации

Hydrocarbon Conversion

Номер: US20170088490A1
Принадлежит:

The invention relates to the conversion of paraffinic hydrocarbon to oligomers of greater molecular weight and/or to aromatic hydrocarbon. The invention also relates to equipment and materials useful in such conversion, and to the use of such conversion for, e.g., natural gas upgrading. Corresponding olefinic hydrocarbon is produced from the paraffinic hydrocarbon in the presence of a dehydrogenation catalyst containing a catalytically active carbonaceous component. The corresponding olefinic hydrocarbon is then converted by oligomerization and/or dehydrocyclization in the presence of at least one molecular sieve catalyst. 1. A process for producing aromatics , comprising:{'sub': n+', 'm−, '(a) providing a feed which comprises ≧1 wt. % of a first hydrocarbon and further comprises a second hydrocarbon, wherein (i) the first hydrocarbon comprises C paraffinic hydrocarbon, (ii) the second hydrocarbon comprises C hydrocarbon, (iii) n is a positive integer ≧2 and m is a positive integer ≦n−1, and (iv) the feed has a first hydrocarbon:second hydrocarbon molar ratio in the range of from 0.001 to 100;'}{'sup': '2', '(b) providing a first multi-component catalyst, the first catalyst having dehydrogenation functionality and comprising (i) ≧10 wt. % of at least one inorganic oxide component having a surface area ≧10 m/g and a pore volume ≧0.1 ml/g, (ii) ≧0.01 wt. % of at least one catalytically active carbonaceous component, and (iii) ≧0.05 wt. % of at least one element selected from Groups 5-11 of the Periodic Table;'}(c) providing a second multi-component catalyst, the second catalyst having dehydrocyclization functionality and comprising ≧10 wt. % of a molecular sieve component and ≧0.005 wt. % of a dehydrogenation component comprising at least one element selected from Groups 3 to 13 of the Periodic Table;{'sub': n+', 'm−, "(d) reacting the feed in the presence of the first catalyst under catalytic dehydrogenation conditions effective for dehydrogenating ≧10 wt. % of the C ...

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30-03-2017 дата публикации

Hydrocarbon Dehydrocyclization

Номер: US20170088491A1
Принадлежит:

The invention relates to hydrocarbon dehydrocyclization to produce products such as aromatic hydrocarbon, to equipment and materials useful for dehydrocyclization, to processes for carrying out dehydrocyclization, and to the use of dehydrocyclization for, e.g., natural gas upgrading. The dehydrocyclization is carried out in a catalytic reaction zone of a reverse-flow reactor. 1. A hydrocarbon dehydrocyclization process , the process comprising:{'sub': '2+', '(a) providing a feed comprising C non-aromatic hydrocarbon;'}(b) providing an oxidant and a gaseous fuel; (i) a pre-heated reaction zone, and', '(ii) a dehydrocyclization catalyst located in the reaction zone, the dehydrocyclization catalyst comprising a molecular sieve component and a dehydrogenation component;, '(c) providing a reverse-flow reactor, the reverse-flow reactor including'} (i) establishing a forward flow of the feed to the reaction zone,', '(ii) transferring heat from the reaction zone to the feed to produce a heated feed and a cooled reaction zone,', {'sub': '2+', "(iii) reacting at least a portion of the heated feed flow's C non-aromatic hydrocarbon in the presence of the dehydrocyclization catalyst under dehydrocyclization conditions which include a temperature a temperature ≧400° C. and a pressure ≧0 psi gauge (psig) (101 kPa) to produce a forward flow of a reaction product comprising molecular hydrogen and aromatic hydrocarbon,"}, '(iv) depositing coke on or proximate to the dehydrocyclization catalyst,', '(v) conducting the forward flow of reaction product from the reaction zone and away from the reverse-flow reactor, and', '(vi) decreasing the feed flow to the reaction zone; and, '(d) during a first time interval,'} (i) establishing a reverse flow of the fuel and a reverse flow of the oxidant toward the reverse-flow reactor, the oxidant flow comprising first and second portions of the oxidant,', '(ii) combusting the first portion of the oxidant flow under combustion conditions with at least ...

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30-03-2017 дата публикации

Hydrocarbon Conversion

Номер: US20170088492A1
Принадлежит:

The invention relates to the hydrocarbon upgrading to produce aromatic hydrocarbon, to equipment and materials useful in such upgrading, and to the use of such upgrading for, e.g., producing aromatic hydrocarbon natural gas. The upgrading can be carried out in the presence of a dehydrocyclization catalyst comprising at least one dehydrogenation component and at least one molecular sieve. 1. A hydrocarbon conversion process , comprising:{'sub': 1', '1, '(a) providing a feed comprising Awt. % ethane, Abeing at least 1;'}(b) providing first and second catalysts, wherein (i) the first catalyst comprises at least 10 wt. % of a first molecular sieve component and at least 0.005 wt. % of a first dehydrogenation component and (ii) the second catalyst comprises at least 10 wt. % of a second molecular sieve component and at least 0.005 wt. % of a second dehydrogenation component;{'sub': 1', '1', '2', '2', '1, '(c) contacting the feed with the first catalyst under catalytic dehydrocyclization conditions, including a temperature Tin the range of from 400° C. to 630° C. and a pressure P, to produce a first product comprising (i) at least 1 wt. % of aromatic hydrocarbon, (ii) molecular hydrogen, (iii) Awt. % ethane, Abeing at least 0.75•A;'}{'sub': 3', '3', '2, "(d) producing a raffinate by removing from the first product an extract comprising at least 50 wt. % of the first product's aromatic hydrocarbon, wherein the raffinate comprises ethane in an amount Awt. %, Abeing greater than A; and"}{'sub': 2', '2', '4', '1', '2', '2', '1', '4', '3', '4', '3', '2', '1, '(e) contacting at least a portion of the raffinate with the second catalyst under catalytic dehydrocyclization conditions, including a temperature Tin the range of from 450° C. to 700° C., and a pressure P≦35 psia (241.3 kPa), to produce a second product comprising at least 0.5 wt. % of additional aromatic hydrocarbon and ethane in an amount Awt. %, wherein Tdoes not exceed 0.90•T, Pis less than P, Ais less than A, and (A ...

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05-05-2022 дата публикации

Methods of Preparing an Aromatization Catalyst

Номер: US20220134319A1
Принадлежит: Chevron Phillips Chemical Co LP

Catalysts and method of preparing the catalysts are disclosed. One of the catalysts includes a zeolite support, a Group VIII metal on the zeolite support, and at least two halides bound to the zeolite support, to the Group VIII metal, or to both, and can have an average crush strength greater than 11.25 lb based on at least two samples of pellets of the catalyst measured in accordance with ASTM D4179.

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19-03-2020 дата публикации

PROCESS TO PREPARE PROPYLENE

Номер: US20200087228A1
Автор: FLETCHER RAYMOND PAUL
Принадлежит: GASOLFIN B.V.

The invention is directed to a process to prepare propylene from a hydrocarbon feed comprising pentane by contacting the hydrocarbon feed with a heterogeneous cracking catalyst as present in one or more fixed beds thereby obtaining a cracked effluent. The heterogeneous catalyst comprises a matrix component and a molecular sieve comprising framework alumina, framework silica and a framework metal selected from the group of Zn, Fe, Ce, La, Y, Ga and/or Zr. Propylene is isolated from the cracked effluent. 1. A process to prepare propylene from a hydrocarbon feed comprising pentane by contacting the hydrocarbon feed with a heterogeneous cracking catalyst as present in one or more fixed beds thereby obtaining a cracked effluent ,wherein the heterogeneous catalyst comprises a matrix component and a molecular sieve comprising framework alumina, framework silica and a framework metal selected from the group of Zn, Fe, Ce, La, Y, Ga and/or Zr andwherein propylene is isolated from the cracked effluent.2. The process according to claim 1 , wherein the framework metal is selected from the group of Fe or Ga3. The process according to claim 2 , wherein the framework metal is Fe.4. The process according to claim 1 , wherein the atomic ratio between framework Al and framework metal is between 1:0.05 and 1:0.55. A process to prepare propylene from a hydrocarbon feed comprising pentane by contacting the hydrocarbon feed with a heterogeneous cracking catalyst as present in one or more fixed beds thereby obtaining a cracked effluent claim 1 ,{'sub': '3', 'wherein the heterogeneous catalyst comprises a matrix component and a modified molecular sieve comprising framework alumina and framework silica and wherein the catalyst is obtainable by (i) crystallization of a synthesis gel comprising FeClthereby obtaining a molecular sieve product comprising of framework Al, Si and Fe, (ii) calcining, (iii) mixing with the matrix and (iv) calcined until the molecular sieve had a framework Fe to ...

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28-03-2019 дата публикации

Modified Y-Zeolite/ZSM-5 Catalyst For Increased Propylene Production

Номер: US20190091669A1
Принадлежит: ALBEMARLE EUROPE SPRL

Provided is a Fluid Catalytic Cracking catalyst composition having increased propylene production with respect to other Fluid Catalytic Cracking catalysts (measured at constant conversion). The catalyst composition comprises a particulate which comprises (a) non-rare earth metal exchanged Y-zeolite in an amount in the range of about 5 to about 50 wt %, based upon the weight of the particulate; and (b) ZSM-5 zeolite in an amount in the range of about 2 to about 50 wt %, based upon the weight of the particulate.

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12-05-2022 дата публикации

Catalyzed Alkylation, Alkylation Catalysts, and Methods of Making Alkylation Catalysts

Номер: US20220144724A1
Принадлежит:

Improved alkylation catalysts, alkylation methods, and methods of making alkylation catalysts are described. The alkylation method comprises reaction over a solid acid, zeolite-based catalyst and can be conducted for relatively long periods at steady state conditions. The alkylation catalyst comprises a crystalline zeolite structure, a Si/Al molar ratio of 20 or less, less than 0.5 weight percent alkali metals, and further having a characteristic catalyst life property. Some catalysts may contain rare earth elements in the range of 10 to 35 wt %. One method of making a catalyst includes a calcination step following exchange of the rare earth element(s) conducted at a temperature of at least 575° C. to stabilize the resulting structure followed by an deammoniation treatment. An improved method of deammoniation uses low temperature oxidation. 140-. (canceled)41. An alkylation catalyst , comprising:a zeolite structure comprising sodalite cages and supercages, a Si/Al molar ratio of 20 or less, less than 0.5 weight percent alkali metals, rare earth elements in the range of 10 to 35 wt % (or a molar ratio of rare earth elements to (Si and Al) in the range of 0.06 to 0.20), and, optionally up to 5 wt % Pt and/or Pd; and/or Nickel; andcharacterizable by a Catalyst Lifetime of 2 or greater (or 2.5 or greater, or between 2.5 and 3.5) where the Catalyst Lifetime parameter is defined as the catalyst age when the olefin conversion falls below 90% (or, in some preferred embodiments below 95%) using a test where the solid-acid catalyst is loaded in a fixed-bed reactor such that the dT/dP>10 (diameter of tube to diameter of catalyst particles) and L/dP>50 (length of catalyst bed to diameter of catalyst particles) and exposed to a flow comprising a) a feed of 10:1 molar ratio of isobutane:n-butenes at 60° C. and 300 psig with a recycle ratio (R=volumetric flow rate of recycle stream/volumetric flow rate of feed stream) of 50, where VS/VC is 7 (the ratio of system volume to catalyst ...

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28-03-2019 дата публикации

RENEWABLE HYDROCARBON COMPOSITION

Номер: US20190093020A1
Принадлежит:

The present invention provides a composition comprising 10-40 mass % of Clinear alkanes, up to 20 mass % of Caromatic hydrocarbons, at least 90 mass % of which are monoaromatic, and no more than 1 mass % in total of oxygen-containing compounds; wherein the total amount of Calkanes in the composition is 50-95 mass %, and the total amount of Calkanes, Caromatic hydrocarbons and Ccycloalkanes is at least 95 mass %; wherein the composition comprises 45-90 mass % in total of Ccycloalkanes and Cbranched alkanes; and wherein the amounts are based on the mass of the composition. Also provided is a method of producing the composition comprising the step of hydroprocessing a biological feedstock using a catalyst and the step of fractionating the product of the hydroprocessing step. 1. A composition comprising 10-40 mass % of Clinear alkanes , up to 20 mass % of Caromatic hydrocarbons , at least 90 mass % of which are monoaromatic , and no more than 1 mass % in total of oxygen-containing compounds;{'sub': 8-30', '8-30', '7-20', '8-30, 'wherein the total amount of Calkanes in the composition is 50-95 mass %, and the total amount of Calkanes, Caromatic hydrocarbons and Ccycloalkanes is at least 95 mass %;'}{'sub': 8-30', '8-30, 'wherein the composition comprises 45-90 mass % in total of Ccycloalkanes and Cbranched alkanes; and'}wherein the amounts are based on the mass of the composition.2. The composition according to claim 1 , wherein the amount of Clinear alkanes is 20-40 mass %.3. The composition according to claim 1 , wherein the amount of Caromatic hydrocarbons is 0.1-15 mass %.4. The composition according to claim 1 , which comprises 45-80 mass % in total of Ccycloalkanes and Cbranched alkanes.5. The composition according to claim 1 , which comprises 10-30 mass % of Ccycloalkanes.6. The composition according to claim 1 , wherein the alkanes are Calkanes.7. The composition according to claim 1 , wherein the aromatic hydrocarbons are Caromatic hydrocarbons.8. The ...

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16-04-2015 дата публикации

PROCESS FOR THE AROMATIZATION OF A METHANE-CONTAINING GAS STREAM

Номер: US20150105597A1
Принадлежит:

A process is disclosed for making styrene and/or ethylbenzene by reacting toluene with a Csource over a catalyst in at least one radial reactor to form a product stream comprising styrene and/or ethylbenzene. 1. A process for making styrene comprising:{'sub': '1', 'reacting toluene with a Csource over a catalyst in at least one radial reactor to form a product stream comprising styrene.'}2. The process of claim 1 , wherein the Csource is selected from the group consisting of methanol claim 1 , formaldehyde claim 1 , formalin claim 1 , trioxane claim 1 , methylformcel claim 1 , paraformaldehyde claim 1 , methylal claim 1 , dimethyl ether claim 1 , and combinations thereof.3. The process of claim 1 , wherein the reaction pressure in the radial reactor is in the range of 0.1 atm to 70 atm.4. The process of claim 1 , wherein the reaction pressure in the radial reactor is in the range of about 0.1 atm to about 10 atm.5. The process of claim 1 , wherein the radial reactor comprises a reaction zone comprising the catalyst claim 1 , wherein the process is conducted such that the average residence time in the reaction zone of the reactants is less than about 10 minutes.6. The process of claim 1 , wherein the radial reactor comprises a reaction zone comprising the catalyst claim 1 , wherein the process is conducted such that the average residence time in the reaction zone of the reactants is less than about 5 minutes.7. The process of claim 1 , wherein the radial reactor comprises a reaction zone comprising the catalyst claim 1 , wherein the process is conducted such that the average residence time in the reaction zone of the reactants is less than about 30 seconds.8. The process of claim 1 , wherein the catalyst is based on a zeolite selected from the group consisting of faujasites.9. The process of claim 8 , wherein the catalyst is based on an X-type zeolite.10. The process of claim 1 , wherein the catalyst is promoted with a promoter selected from the group consisting of ...

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13-04-2017 дата публикации

Processes for Producing Aromatic Hydrocarbon, p-Xylene and Terephthalic Acid

Номер: US20170101353A1
Принадлежит:

The present invention relates to a process for preparing an aromatic hydrocarbon, and processes for producing p-xylene and terephthalic acid. The process for producing said aromatic hydrocarbon comprises a step of contacting an olefin with a diene in the presence of a catalyst to produce an aromatic hydrocarbon, which is characterized in that, at least a part of said olefin is substituted with dienophile. The reaction pressure can be reduced and the xylene selectivity can be increased with the improvement of the present invention. 2. The process according to claim 1 , wherein said catalyst is a molecular sieve claim 1 , and said molecular sieve is one or more selected from ZSM-type molecular sieve (preferably one or more selected from ZSM-5 claim 1 , ZSM-11 claim 1 , ZSM-22 claim 1 , ZSM-23 and ZSM-38) claim 1 , Y-type molecular sieve claim 1 , beta-type molecular sieve and MCM-type molecular sieve (preferably one or more selected from MCM-22 and MCM-41); preferably one or more selected from ZSM-5 claim 1 , Y-type molecular sieve claim 1 , beta-type molecular sieve and MCM-41; more preferably ZSM-5.3. The process according to claim 2 , wherein said ZSM-type molecular sieve (preferably ZSM-5 or ZSM-22) has a SiO2/Al2O3 molar ratio of 10-500 claim 2 , preferably 15-200; said Y-type molecular sieve has a SiO2/Al2O3 molar ratio of 2-80 claim 2 , preferably 3-50; said beta-type molecular sieve has a SiO2/Al2O3 molar ratio of 10-150 claim 2 , preferably 15-65; said MCM-type molecular sieve (preferably MCM-22 or MCM-41) has a SiO2/Al2O3 molar ratio of 20-250 claim 2 , preferably 40-150.4. The process according to claim 1 , wherein the ratio of the mole of said diene to the total mole of said dienophile and said olefin is 0.1-10 claim 1 , preferably 0.5-2.5. The process according to claim 1 , wherein said contacting step is conducted at a reaction temperature of 80 to 400° C. claim 1 , preferably 160 to 350° C. claim 1 , under a reaction pressure of 0.5 to 10 MPa claim 1 , ...

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23-04-2015 дата публикации

Activated eu-2 zeolite and use thereof

Номер: US20150112110A1
Принадлежит: SK Innovation Co Ltd, SK Lubricants Co Ltd

Disclosed herein is an activated EU-2 zeolite, including: pores having a diameter of 30 to 40 Å while maintaining the crystal structure of the EU-2 zeolite; and pores having a diameter of 40 to 200 Å, wherein the volume of the pores having a diameter of 30 to 40 Å is 0.01 to 0.06 cc/g, and the volume of the pores having a diameter of 40 to 200 Å is 0.07 to 0.4 cc/g.

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11-04-2019 дата публикации

PROCESS FOR MINIMIZING BENZENE, TOLUENE, AND A RECYCLE LOOP IN A ZERO BENZENE AROMATICS COMPLEX

Номер: US20190106368A1
Принадлежит:

The present invention relates to minimizing benzene, toluene, and an A9/A10 recycle loop in a zero benzene aromatics complex. More specifically, the present invention relates to a minimizing benzene, toluene, and an A9/A10 recycle loop in a zero benzene aromatics complex wherein the aromatic feed has a low methyl to phenyl ratio, and where the aromatic feed has a high methyl to phenyl ratio. 1. A process for reducing benzene production in an aromatics complex , comprising:passing an aromatics stream having a methyl to phenyl ratio above 1.0 to a benzene column to produce a benzene column overhead stream and a benzene column bottoms stream;passing the benzene column overhead stream to a trans-alkylation unit and transalkylating aromatics having 9+ carbons with benzene to produce a benzene trans-alkylation product stream;passing the benzene column bottoms stream to a toluene column which produces a toluene column overhead stream and a toluene column bottoms stream;passing a first portion of the toluene column overhead stream to the trans-alkylation unit and transalkylating aromatics having 9+ carbons with toluene to produce a toluene transalkylation product stream;passing a second portion of the toluene column overhead stream to a toluene methylation unit to produce a toluene methylation unit product stream, wherein the toluene methylation unit produces an effluent containing xylenes with para-xylene selectivity preferably between 20% and 99.9% within the xylene fraction;passing the toluene column bottoms stream to a fractionation zone to produce an overhead stream, a bottoms stream, and a middle boiling fraction;passing the middle boiling fraction from the fractionation zone to the trans-alkylation unit of aromatics having 9+ carbons with benzene and toluene;recycling the benzene trans-alkylation product stream to the benzene column; and,recycling the toluene methylation unit product stream to the benzene column.2. The process of claim 1 , wherein the toluene ...

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28-04-2016 дата публикации

Method for Upgrading Hydrocarbon Using C4, C5 and C6 Streams

Номер: US20160115093A1
Принадлежит:

The present disclosure relates to a method for upgrading hydrocarbon using C4, C5 and C6 streams, and more specifically, to a method for upgrading hydrocarbons using C4, C5 and C6 streams. The method includes the steps of: preparing C4, C5 and C6 streams, which are the products of naphtha catalytic cracking (NCC) process, heavy oil upgrading process, thermal cracking process, or fluidized catalytic cracking (FCC or RFCC) process; oligomerizing the C4, C5 and C6 streams with a catalyst to produce branched unsaturated hydrocarbons; and fractional distillating the branched unsaturated hydrocarbons to separate into C14-18 products or C32-40 products. 1. A method for upgrading hydrocarbons using C4 , C5 and C6 streams , comprising:preparing C4, C5 and C6 streams;oligomerizing the C4, C5 and C6 streams with a catalyst to produce branched unsaturated hydrocarbons; andfractional distillating the branched unsaturated hydrocarbons to separate into C14-18 products or C32-40 products.2. The method of claim 1 , wherein the oligomerization is carried out at reaction temperature of 80 to 200° C. and under pressure of 10 to 60 bars claim 1 , and the method further comprises separating C4 claim 1 , C5 and C6 saturated hydrocarbons produced by the oligomerization reaction claim 1 , partially dehydrogenating the separated C4 claim 1 , C5 and C6 saturated hydrocarbons to produce C4 claim 1 , C5 and C6 unsaturated hydrocarbons claim 1 , and mixing the C4 claim 1 , C5 and C6 unsaturated hydrocarbons with C4 claim 1 , C5 and C6 streams again.3. The method of claim 1 , wherein the C14-18 products are subjected to an aromatic alkylation reaction.4. The method of claim 3 , wherein the aromatic alkylation reaction is carried out at a temperature of 170 to 300° C. and under pressure of 1 to 50 bars.5. The method of claim 1 , wherein the oligomerization reaction is carried out at a temperature of 200 to 300° C. and under pressure of 10 to 90 bars claim 1 , and the method further comprises ...

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09-06-2022 дата публикации

Acidic aromatization catalysts with improved activity and selectivity

Номер: US20220176356A1
Принадлежит: Chevron Phillips Chemical Co LP

Methods for producing supported catalysts containing a transition metal and a bound zeolite base are disclosed. These methods employ a step of impregnating the bound zeolite base with the transition metal, fluorine, and high loadings of chlorine. The resultant high chlorine content supported catalysts have improved catalyst activity in aromatization reactions.

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30-04-2015 дата публикации

HYDROCARBON CONVERSION PROCESS

Номер: US20150119544A1
Принадлежит:

The invention relates to processes for converting a mixture of hydrocarbon and sulfur-containing molecules such as mercaptan into products comprising acetylene, ethylene, and hydrogen sulfide, to processes utilizing the acetylene and ethylene resulting from the conversion, and to equipment useful for such processes. 1. A hydrocarbon conversion process , comprising:(a) providing a first mixture comprising ≧0.5 wt. % hydrocarbon and ≧4.0 ppmw mercaptan based on the weight of the first mixture; and{'sup': '3', 'sub': 2', 'x, "(b) exposing a first mixture to a temperature ≧1.20×10° C. in a first region under pyrolysis conditions to convert at least a portion of the hydrocarbon and ≧90.0 wt. % of the first mixture's mercaptan based on the weight of mercaptan in the first mixture to produce a second mixture, the second mixture comprising ≧1.0 wt. % Cunsaturates, ≦20.0 wt. % CO, wherein x is 1 or 2, and ≦1.0 ppmw thiophene based on the weight of the second mixture."}2. The process of claim 1 , wherein the first mixture comprises ≧20.0 wt. % methane and ≧10.0 ppmw methyl mercaptan based on the weight of the first mixture; the first mixture being obtained from a natural gas with no intervening mercaptan-removal steps claim 1 , and wherein second mixture comprises ≦0.05 ppmw methyl mercaptan based on the weight of the second mixture.3. The process of claim 1 , wherein the first mixture further comprises hydrogen sulfide in an amount in the range of 50.0 ppmw to 5 wt. % based on the weight of the first mixture.4. The process of claim 1 , wherein the first mixture is exposed to a temperature ≧1.45×10° C. during the pyrolysis.5. The process of any of claim 1 , further comprising (c) separating hydrogen sulfide from the second mixture to produce a third mixture.6. The process of claim 5 , further comprising:(d) combining first and second reactants in a second region to produce a fourth mixture, the first and second regions being at least partially coextensive; and (i) the ...

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30-04-2015 дата публикации

ALKYLATING PROCESS FOR ALKYL BENZENES

Номер: US20150119618A1
Принадлежит:

This invention relates to an alkylating process for alkyl benzenes, including the steps of: a) an alkyl benzene and a first stream of alkylating agent being fed into a first reaction zone, contacting with a catalyst A, to produce a process stream I; b) the process stream I and a second stream of alkylating agent being fed into at least one second reaction zone, contacting with a catalyst B, to produce a process stream II; and c) the process stream II being fed into at least one third reaction zone, contacting with a catalyst C, to produce a process stream III containing an alkylate. The present alkylating process can improve the utilization efficiency of the alkylating agent. 2. The alkylating process according to claim 1 , wherein in the first reaction zone claim 1 , the reaction temperature is 320-400 degrees centigrade claim 1 , the weight hourly space velocity (WHSV) is 2-4 h-1 claim 1 , the reaction pressure is 0-0.5 MPa (gage pressure); in the second reaction zone claim 1 , the reaction temperature is 380-420 degrees centigrade claim 1 , the weight hourly space velocity (WHSV) is 2-4 h-1 claim 1 , the reaction pressure is 0-0.5 MPa (gage pressure); in the third reaction zone claim 1 , the reaction temperature is 400-450 degrees centigrade claim 1 , the weight hourly space velocity (WHSV) is 2-4 h-1 claim 1 , the reaction pressure is 0-0.5 MPa (gage pressure); the ratio by molar of the alkyl benzene to the first stream of alkylating agent is greater than 1 but not greater than 6 claim 1 , and the ratio by molar of the alkyl benzene contained in the process stream I to the second stream of alkylating agent is 1-5.3. The alkylating process according to claim 2 , wherein the reaction temperature in the first reaction zone is less than the reaction temperature in the third reaction zone.4. The alkylating process according to claim 2 , wherein the ratio by molar of the alkyl benzene to the first stream of alkylating agent is greater than the ratio by molar of the ...

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09-06-2022 дата публикации

Catalytic conversion process and system with increased propylene production

Номер: US20220177390A1
Принадлежит:

A catalytic conversion process for producing propylene includes the steps of: 1) providing a starting material comprising olefin(s) having 4 or more carbon atoms; 2) pretreating the starting material to obtain a propylene precursor comprising olefin(s) having 3×2carbon atoms, wherein n is an integer greater than or equal to 1; and 3) subjecting the propylene precursor to a catalytic cracking reaction to obtain a reaction product comprising propylene. 1. A process for producing propylene , comprising the steps of:1) providing a starting material comprising olefin(s) having 4 or more carbon atoms;{'sup': 'n', '2) pretreating the starting material to obtain a propylene precursor comprising olefin(s) having 3×2carbon atoms, wherein n is an integer greater than or equal to 1, preferably 1-3, more preferably 1-2; and'}3) subjecting the propylene precursor to a catalytic cracking reaction to obtain a reaction product comprising propylene,wherein the pretreating of step 2) comprises one or both of:{'sup': 'n', 'sub': 4', '5', '7', '8, '2a) separating the starting material to obtain a first propylene precursor comprising olefin(s) having 3×2carbon atoms, and/or one or more of the following fractions: a fraction comprising Colefin, a fraction comprising Colefin, a fraction comprising Colefin, and a fraction comprising Colefin; and'}{'sup': 'm', '2b) subjecting the starting material or a fraction thereof to an olefin oligomerization reaction, and optionally separating the resulting oligomerization product, to obtain a second propylene precursor comprising olefin(s) having 3×2carbon atoms, wherein m is an integer greater than or equal to 2, preferably 2 to 3.'}2. The process according to claim 1 , wherein the oligomerization step 2b) comprises one or more of:{'sub': 4', '12, 'b1) subjecting the fraction comprising Colefin of the starting material to an olefin oligomerization reaction, and optionally separating the resulting oligomerization product, to obtain the second ...

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27-04-2017 дата публикации

Process of Making Olefins or Alkylate by Reaction of Methanol and/or DME or by Reaction of Methanol and/or DME and Butane

Номер: US20170113981A1
Принадлежит:

Methods of simultaneously converting butanes and methanol to olefins over Ti-containing zeolite catalysts are described. The exothermicity of the alcohols to olefins reaction is matched by endothermicity of dehydrogenation reaction of butane(s) to light olefins resulting in a thermo-neutral process. The Ti-containing zeolites provide excellent selectivity to light olefins as well as exceptionally high hydrothermal stability. The coupled reaction may advantageously be conducted in a staged reactor with methanol/DME conversion zones alternating with zones for butane(s) dehydrogenation. The resulting light olefins can then be reacted with iso-butane to produce high-octane alkylate. The net result is a highly efficient and low cost method for converting methanol and butanes to alkylate. 1. A method of producing alkylate , comprising:passing methanol and/or dimethylether (DME) into a reaction chamber;passing butane into the reaction chamber;{'sub': 4', '4, 'wherein the reactor comprises a catalyst that is a crystalline zeotype material in which tetrahedral [TiO] and [SiO] units are arranged in a MFI structure with a three-dimensional system of channels having a molecular dimension of 4.9 to 5.9 A, preferably 5.1-5.6 Å, and at least 0.5 mass % Ti, more preferably at least 1% Ti, in some embodiments in the range of 1 to 5 mass %Ti;'}reacting the methanol and/or DME and the butane in the reaction chamber in the presence of the catalyst to make olefins under steady state conditions where the reaction is adiabatic or nearly adiabatic such that +/−200 kJ/(kg olefin produced) or less is transferred from the reaction chamber (preferably +/−100 or less, more preferably +/−50, and preferably +/−10 kJ/(kg olefin produced) or less is transferred from the reaction chamber; andreacting the olefins with iso-butane to form alkylate in a separate reactor.2. The method of where reaction chamber further comprises a second catalyst comprising at least 1 claim 1 , or at least 2 claim 1 , or ...

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05-05-2016 дата публикации

METHOD FOR PRODUCING AN AROMATIC HYDROCARBON WITH AN OXYGENATE AS RAW MATERIAL

Номер: US20160122256A1
Принадлежит:

A method for producing an aromatic hydrocarbon with an oxygenate as raw material, includes: i) reacting an oxygenate in at least one aromatization reactor to obtain an aromatization reaction product; ii) separating the aromatization reaction product to obtain a gas phase hydrocarbons flow X and a liquid phase hydrocarbons flow Y; iii) after removing gas and/or a part of the oxygenate from the gas phase hydrocarbons flow X, a hydrocarbons flow X containing a non-aromatic hydrocarbon is obtained; or after removing gas and/or a part of the oxygenate from the gas phase hydrocarbons flow X, a reaction is conducted in another aromatization reactor and a separation is conducted to obtain a flow X containing a non-aromatic hydrocarbon and a flow X containing an aromatic hydrocarbon. The flows are further treated. 1. A method for producing an aromatic hydrocarbon with an oxygenate as raw material , comprisingi) reacting an oxygenate in at least one aromatization reactor to obtain an aromatization reaction product;ii) separating the aromatization reaction product through a separation unit A, to obtain a gas phase hydrocarbons flow X and a liquid phase hydrocarbons flow Y;{'b': '1', 'iii) after removing gas and/or a part of the oxygenate from the gas phase hydrocarbons flow X through a separation unit B, a hydrocarbons flow X containing a non-aromatic hydrocarbon is obtained; or'}after removing gas and/or a part of the oxygenate from the gas phase hydrocarbons flow X through a separation unit B,{'b': 2', '3, 'a reaction is conducted in another aromatization reactor and a separation is conducted through a separation unit A, to obtain a flow X containing a non-aromatic hydrocarbon and a flow X containing an aromatic hydrocarbon;'}{'b': '3', 'iv) after combining the liquid phase hydrocarbons flow Y and optionally the flow X containing an aromatic hydrocarbon, a mixed hydrocarbons flow M of an aromatic hydrocarbon having less than or equal to 7 carbon numbers and a flow N of the ...

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07-05-2015 дата публикации

Delaminated Zeolite Catalyzed Aromatic Alkylation

Номер: US20150126789A1
Принадлежит:

Provided is a method of alkylating an aromatic compound comprising contacting an aromatic compound and an alkylating agent in the presence of UCB-3 as a catalyst under reaction conditions suitable for aromatic alkylation. The aromatic compound preferably comprises benzene or toluene and the alkylation agent preferably comprises an olefin or alcohol. Lower temperature ranges can be used for the reaction, for example in the range of from 100 to 300° C. 1. A method of alkylating an aromatic compound comprising contacting an aromatic compound and an alkylating agent in the presence of UCB-3 as a catalyst under reaction conditions suitable for aromatic alkylation.2. The method of claim 1 , wherein the aromatic compound comprises benzene claim 1 , toluene claim 1 , or a mixture thereof.3. The method of claim 1 , wherein the aromatic compound comprises toluene.4. The method of claim 1 , wherein the alkylation agent comprises an alkane claim 1 , olefin or an alcohol.5. The method of claim 4 , wherein the alkylating agent comprises an olefin.6. The method of claim 5 , wherein the olefin comprises ethylene or propylene.7. The method of claim 3 , wherein the alkylating agent comprises propylene.8. The method of claim 4 , wherein the alkylating agent comprises an alcohol.9. The method of claim 8 , wherein the alkylating agent comprises methanol.10. The method of claim 3 , wherein the alkylating agent comprises methanol.11. The method of claim 8 , wherein the alkylating agent comprises isopropanol.12. The method of claim 3 , wherein the alkylating agent comprises isopropanol.13. The method of claim 1 , wherein the contacting is at a temperature in the range of 0° to 500° C.14. The method of claim 13 , wherein the contacting is at a temperature in the range of 150 to 250° C.15. The method of claim 13 , wherein the contacting is at a pressure in the range of 0.2 to 250 atm.16. The method of claim 1 , wherein the aromatic compound comprises benzene.17. The method of claim 16 , ...

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16-04-2020 дата публикации

PROCESS FOR THE MANUFACTURE OF DIESEL RANGE HYDROCARBONS

Номер: US20200115636A1
Принадлежит: Neste Oyj

The invention relates to a process for the manufacture of diesel range hydrocarbons wherein a feed is hydrotreated in a hydrotreating step and isomerised in an isomerisation step, and a feed comprising fresh feed containing more than 5 wt % of free fatty acids and at least one diluting agent is hydrotreated at a reaction temperature of 200-400° C., in a hydrotreating reactor in the presence of catalyst, and the ratio of the diluting agent/fresh feed is 5-30:1. 1. A process for the manufacture of diesel range hydrocarbons comprising the following steps:introducing a feedstock comprising bio oil and/or fat from renewable sources to a hydrotreatment step in which hydrocarbons are formed,isomerizing the formed hydrocarbons in an isomerization step,whereingas phase impurities formed in the hydrotreatment step are removed from the stream comprising hydrocarbons prior to contacting the hydrocarbons with the isomerization catalyst.2. The process according to claim 1 , further comprising a step of purifying the feedstock prior to the hydrotreatment step so as to remove impurities.3. The process according to claim 1 , wherein the gas phase impurities formed in the hydrotreatment step comprise propane claim 1 , water claim 1 , CO claim 1 , HS claim 1 , NHor mixtures thereof.4. The process according to claim 1 , wherein the removal of the gas phase impurities formed in the hydrotreatment step is performed in a stripping step upstream of the isomerization catalyst.5. The process according to claim 4 , wherein the stripping step is performed by stripping with water vapor or a suitable gas comprising light hydrocarbon claim 4 , nitrogen or hydrogen.6. The process according to claim 4 , wherein the stripping step is carried out in a counter-current manner.7. The process according to claim 1 , in the feedstock comprises more than 10 wt % of free fatty acids.8. The process according to claim 1 , wherein the feedstock contains less than 10 w-ppm alkaline and alkaline earth metals ...

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