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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 2220. Отображено 100.
10-05-2012 дата публикации

Multiple zeolite catalyst

Номер: US20120116139A1
Автор: Katsuhiko Ishikawa, Khalid Al-Nawad, Masayuki Inui, Minoru Hatayama, Mohammad A. Ali, Muhammad A. Al-Saleh, Syed A. Ali, Tomoyuki Inui, Tsutomo Okamoto
Принадлежит: Japan Cooperation Center Petroleum (JCCP), KING FAHD UNIVERSITY OF PETROLEUM AND MINERALS

The multiple zeolite catalyst is a catalytic composition used to convert C 9+ alkylaromatic hydrocarbons to BTX, particularly commercially valuable xylenes. The catalyst is formed by mixing at least two zeolites selected from mordenite, beta zeolite, ZSM-5, ZSM-11, ZSM-12, ZSM-22, ZSM-23, MFI topology zeolite, NES topology zeolite, EU-1, MAPO-36, SAPO-5, SAPO-11, SAPO-34, and SAPO-41, and adding at least one metal component selected from Group VIB and Group VIII of the Periodic Table of the Elements. The two zeolites should have different physical and chemical characteristics, such as pore size and acidity. An exemplary catalyst includes mordenite, ZSM-5, and 3 wt. % molybdenum. The transalkylation reaction may be conducted in one or more reactors with a fixed bed, moving bed, or radial flow reactor at 200-540° C., a pressure of 1.0-5.0 MPa, and liquid hourly space velocity of 1.0-5.0 per hour.

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Номер записи: 1
21-06-2012 дата публикации

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

Номер: US20120157739A1
Автор: Deng-Yang Jan, James A. Johnson, Michael A. Schultz
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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Номер записи: 2
12-07-2012 дата публикации

Process For Producing Cyclohexylbenzene

Номер: US20120178969A1
Автор: Jane C. Cheng, Prasenjeet Ghosh, Tan-Jen Chen
Принадлежит: ExxonMobil Chemical Patents Inc

In a process for producing cyclohexylbenzene, benzene and hydrogen are contacted under hydroalkylation conditions with a catalyst system comprising a MCM-22 family molecular sieve and at least one hydrogenation metal. The conditions comprise a temperature of about 140° C. to about 175° C., a pressure of about 135 psig to about 175 psig (931 kPag to 1207 kPag), a hydrogen to benzene molar ratio of about 0.30 to about 0.65 and a weight hourly space velocity of benzene of about 0.26 to about 1.05 hr −1 .

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Номер записи: 3
01-11-2012 дата публикации

Processes for Transalkylating Aromatic Hydrocarbons

Номер: US20120277512A1
Автор: Edwin P. Boldingh
Принадлежит: UOP LLC

A process for transalkylating aromatic hydrocarbon compounds, the process comprising introducing an aromatic hydrocarbon feed stream and a sulfur source to a transalkylation zone. The feed stream contacts a catalyst in the transalkylation zone in the presence of sulfur, and produces a reaction product stream comprising benzene and xylene. The invention includes methods to control the transalkylation process.

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Номер записи: 4
18-04-2013 дата публикации

Heavy alkylbenzene transalkylation operating cost reduction

Номер: US20130096357A1
Автор: Mark G. Riley, Stephen W. Sohn
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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Номер записи: 5
23-05-2013 дата публикации

Production of renewable aromatic compounds

Номер: US20130130345A1
Автор: David A. Sikkenga, Wendy Thai, Will SCHROEDER
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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Номер записи: 6
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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Номер записи: 7
05-09-2013 дата публикации

Catalysts Useful for the Alkylation of Aromatic Hydrocarbons

Номер: US20130230450A1
Автор: Anne Mae Gaffney, Chuen Yuan Yeh, Marshall J. Margolis, Ruozhi Song, Tadeusz Langner
Принадлежит: Lummus Technology Inc

A catalyst useful for the alkylation or transalkylation of aromatic compounds is disclosed. The catalyst is an acid-treated zeolitic catalyst produced by a process including contacting an acidic zeolitic catalyst comprising surface non-framework aluminum and framework aluminum with an organic dibasic acid at a catalyst to acid weight ratio in the range from about 2:1 to about 20:1 and at a temperature in the range from about 50° C. to about 100° C. to selectively remove at least a portion of the surface non-framework aluminum. The resulting catalyst may have a measured first-order rate constant, k cum , for the alkylation of benzene with propylene to form cumene, of at least 2.0 cm 3 /s g.

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Номер записи: 8
12-09-2013 дата публикации

Process for producing cumene

Номер: US20130237730A1
Автор: Bin Zhou, HUA Fang, Huanxin Gao, Hui Yao, Ruifang Gu, Shufang Ji, Yilun Wei
Принадлежит: China Petroleum and Chemical Corp, Sinopec Shanghai Research Institute of Petrochemical Technology

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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Номер записи: 9
03-10-2013 дата публикации

Multimetal Zeolites Based Catalyst for Transalkylation of Heavy Reformate to Produce Xylenes and Petrochemical Feedstocks

Номер: US20130261364A1
Автор: Ercan Cemal, Wang Yuguo
Принадлежит: Saudi Arabian Oil Company

A transalkylation catalyst for the transalkylation of a heavy reformate is provided. The catalyst includes two solid acid zeolites having different physical and chemical properties, and at least three metals selected from the group 4 Lanthanoids, and the elements found in groups 6 and 10 of the periodic table. 1. A transalkylation catalyst for the conversion of a heavy reformate feedstock into a xylenes-rich product stream , the transalkylation catalyst comprising:at least two solid acid zeolites, wherein the first solid acid zeolite and the second solid acid zeolite are selected from the group consisting of mordenite, beta zeolite, ZSM-5, ZSM-11, ZSM-12, ZSM-22, ZSM-23, MFI topology zeolite, NES topology zeolite, EU-1, MAPO-36, SAPO-5, SAPO-11, SAPO-34, and SAPO-41, and wherein the first and second solid acid zeolite are not identical; andat least three metal selected from the Group 4 Lanthanoids, Group 6, and Group 10 of the Periodic Table of the Elements.2. The method of wherein the first and second solid acid zeolites are physically and chemically different.3. The method of wherein the acidity of the first or second solid acid zeolite is greater than the other.4. The method of wherein the first solid acid zeolite is Beta zeolite and the second solid acid zeolite is ZSM-5.5. The method of wherein the metals are nickel claim 1 , cerium and platinum.6. The method of wherein the pore size of the first and second solid acid zeolites are different.7. The method of wherein the first solid acid zeolite that is present in an amount of between about 10 and 90% by weight of the total catalyst weight.8. The method of claim 1 , wherein second solid acid zeolite that is present in an amount of between about 10 and 90% by weight of the total catalyst weight.9. The method of claim 1 , wherein the transalkylation catalyst further includes a binder selected from inorganic oxides.10. The method of claim 1 , wherein the metal components are present in an amount of between about 0. ...

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Номер записи: 10
17-10-2013 дата публикации

PARAFFIN DISPROPORTIONATION WITH ZEOLITE Y

Номер: US20130274534A1
Автор: Gill Christopher S.
Принадлежит: Phillips 66 Company

Methods relate to disproportionation of hydrocarbons utilizing a zeolite catalyst. The methods include reacting pentanes in contact with ultrastable zeolite Y having a silica to alumina ratio of less than 80 to disproportionate the pentanes into butanes and hexanes. The ultrastable zeolite Y is defined by having a sodium oxide content of less than 1% by weight. 1. A method , comprising:reacting pentanes in contact with ultrastable zeolite Y having a silica to alumina ratio of less than 80 to disproportionate the pentanes into butanes and hexanes, wherein the ultrastable zeolite Y is defined by having a sodium oxide content of less than 1% by weight.2. The method of claim 1 , wherein the ultrastable zeolite Y is in proton form containing hydrogen counter ions.3. The method of claim 1 , wherein the ultrastable zeolite Y has a silica to alumina ratio of less than 10.4. The method of claim 1 , wherein the ultrastable zeolite Y has a silica to alumina ratio of 5.2.5. The method of claim 1 , wherein the ultrastable zeolite Y is rare earth element exchanged.6. The method of claim 1 , wherein the ultrastable zeolite Y is lanthanum exchanged.7. The method of claim 1 , wherein the reacting is at a temperature between 100° C. and 400° C. and at a pressure between 1 claim 1 ,500 kilopascals and 4 claim 1 ,250 kilopascals.8. The method of claim 1 , wherein the reacting is at 250° C. and at 2859 kilopascals.9. The method of claim 1 , wherein the reacting has a selectivity that is defined as mass of the butanes and the hexanes divided by total non-pentane product mass and is at least 89%.10. The method of claim 1 , wherein the reacting converts at least 20% of the pentanes.11. The method of claim 1 , wherein a mol ratio of the butanes to the hexanes produced by the reacting is less than 1.12. The method of claim 1 , wherein over 90% of the butanes produced by the reacting are isobutane.13. The method of claim 1 , wherein the reacting converts at least 20% of the pentanes claim 1 , ...

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Номер записи: 11
05-12-2013 дата публикации

Hydrocarbon Conversion Process Using a High Throughpout Process for Manufacturing Molecular Sieves

Номер: US20130324760A1
Автор: Ivy D. Johnson, Wenyih Frank Lai
Принадлежит: ExxonMobil Chemical Patents Inc

A method of crystallizing a crystalline molecular sieve having a pore size in the range of from about 2 to about 19 Å, said method comprising the steps of (a) providing a mixture comprising at least one source of ions of tetravalent element (Y), at least one hydroxide source (OH − ), and water, said mixture having a solid-content in the range of from about 15 wt. % to about 50 wt. %; and (b) treating said mixture to form the desired crystalline molecular sieve with stirring at crystallization conditions sufficient to obtain a weight hourly throughput from about 0.005 to about 1 hr −1 , wherein said crystallization conditions comprise a temperature in the range of from about 200° C. to about 500° C. and a crystallization time less than 100 hr.

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Номер записи: 12
10-04-2014 дата публикации

Low pressure transalkylation process

Номер: US20140100403A1
Автор: David S. Lafyatis, Edwin P. Boldingh, Marc R. Schreier, Naiyl A. Rashid, Raymond Shih
Принадлежит: UOP LLC

A process for transalkylation is described. The process operates at a lower pressure than a typical transalkylation processes, and provides higher benzene purity with comparable or lower ring loss compared to the typical transalkylation process. The xylene selectivity is comparable to or higher than the standard process, and the ethyl benzene selectivity is comparable to or lower than the standard process.

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Номер записи: 13
05-01-2017 дата публикации

ALKANE METATHESIS CATALYST, METHODS OF USE AND THE PREPARATION THEREOF

Номер: US20170001184A1
Автор: ABOU-HAMAD Edy, Basset Jean-Marie Maurince, Callens Emmanuel, Riache Nassima, Samantaray Manoja Kumar
Принадлежит: KING ABDULLAH UNIVERSITY OF SCIENCE AND TECHNOLOGY

The invention concerns an alkane metathesis catalyst, its production and use. The catalyst comprises a Group V, VI or VII metal alkyl with the metal in its highest oxidation state, preferably Ta or W, and the alkyl of C1-C4, preferably together with alkylidene and/or alkylidyne ligands, in particular -Me, ═CH2 and ≡CH, on a metal oxide support, preferably silica partially dehydroxylated at 200 or 700° C. Substrates include cycloalkanes, preferably cyclooctane. 1. A catalyst comprising an oxide support and a supported metal alkyl species bound to the oxide support , wherein the supported metal alkyl species is a group V , VI or a group VII metal in its highest oxidation state and the alkyl group is a C1-C4 alkyl.2. The catalyst of claim 1 , wherein the oxide support includes an oxide of silicon claim 1 , an oxide of titanium claim 1 , an oxide of aluminum claim 1 , a mixed silica-alumina claim 1 , or an aminated oxide of silicon.3. The catalyst of claim 1 , wherein the supported metal alkyl species bound to the oxide support includes a moiety having a formula of (≡Si—O)M(R)(R) claim 1 , wherein ≡Si—O is a surface Si—O group claim 1 , wherein Ris a C1-C4 alkylidene group or a C1-C4 alkylidyne group claim 1 , wherein each R claim 1 , independently claim 1 , is a halogen or C1-C4 alkyl group claim 1 , wherein x is 1 claim 1 , 2 or 3 claim 1 , y is 0 or 1 claim 1 , and z is 1 claim 1 , 2 claim 1 , 3 claim 1 , 4 or 5 claim 1 , and wherein M is a group VI metal claim 1 , such that x+2y+z is 6 when Ris a C1-C4 alkylidene group or each of two Rgroups is a C1-C4 alkylidene group claim 1 , and that x+3y+z is 6 when Ris a C1-C4 alkylidyne group.4. The catalyst of claim 3 , wherein M is tungsten or molybdenum.5. (canceled)6. The catalyst of claim 3 , wherein Ris methylidyne.7. The catalyst of claim 3 , wherein Ris methyl.8. The catalyst of claim 3 , wherein x is 1 and y is 0.9. The catalyst of claim 3 , wherein x is 1 and y is 1.10. The catalyst of claim 3 , wherein x is 2 and y ...

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Номер записи: 14
03-01-2019 дата публикации

CATALYST AND HYDROCARBON CONVERSION PROCESS UTILIZING THE CATALYST

Номер: US20190002372A1
Автор: JANTHARASUK Amnart, JAREEWATCHARA Wuttithep, SURIYE Kongkiat
Принадлежит: SMH Co., Ltd

The present invention relates to a hydrocarbon conversion catalyst comprising i) a catalyst, in oxidic form, metals M1, M2, M3 and M4, wherein: M1 is selected from Si, Al, Zr, and mixtures thereof; M2 is selected from Pt, Cr, and mixtures thereof; M3 is selected from W, Mo, Re and mixtures thereof; M4 is selected from Sn, K, Y, Yb and mixtures thereof; and ii) a hydrogen scavenger selected from at least one alkali and/or alkaline earth metal derivative, preferably in metallic, hydride, salt, complex or alloy form; as well as a hydrocarbon conversion process utilizing this catalyst. 1. Hydrocarbon conversion catalyst comprising , M1 is selected from Si, Al, Zr, and mixtures thereof;', 'M2 is selected from Pt, Cr, and mixtures thereof;', 'M3 is selected from W, Mo, Re and mixtures thereof;', 'M4 is selected from Sn, K, Y, Yb, and mixtures thereof; wherein', 'the mass fraction of M1 is in the range of 0.1 to 0.8;', 'the mass fraction of M2 is in the range of 0.001 to 0.2;', 'the mass fraction of M3 is in the range of 0.001 to 0.2;', 'the mass fraction of M4 is in the range of 0.0001 to 0.2; and', 'the mass fraction of oxygen is in the range of 0.1 to 0.8;', 'and, 'i) a catalyst in oxidic form, comprising metals M1, M2, M3 and M4, whereinii) a hydrogen scavenger selected from at least one alkali and/or alkaline earth metal derivative.2. Hydrocarbon conversion catalyst according to claim 1 , wherein the at least one alkali and/or alkaline earth metal is selected from Li claim 1 , Na claim 1 , K claim 1 , Mg claim 1 , Ca claim 1 , and mixtures thereof.3. Hydrocarbon conversion catalyst according to claim 1 , wherein weight ratio of catalyst i) and hydrogen scavenger ii) is from 1-99 to 99-1.4. Hydrocarbon conversion catalyst according to claim 1 , wherein M2 is Pt and M3 is W.5. Process for conversion of a hydrocarbon feed comprising saturated hydrocarbon compounds to olefin products comprising contacting a hydrocarbon feed stream with the hydrocarbon conversion catalyst ...

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Номер записи: 15
01-01-2015 дата публикации

CATALYTIC DISPROPORTIONATION OF PARAFFINS USING IONIC LIQUIDS

Номер: US20150005543A1
Автор: Bhattacharyya Alakananda, Smith Stuart
Принадлежит:

Processes for the disproportionation and isomerization of a hydrocarbon feed using a liquid catalyst comprising an ionic liquid and a carbocation promoter are described. The ionic liquid is unsupported, and the reactions occur at temperatures below about 200° C. 1. A hydrocarbon conversion process comprising:{'sub': n', 'n+', 'n, 'disproportionating a hydrocarbon feed comprising one or more Calkanes, wherein n=5-12, by contacting the hydrocarbon feed with a liquid catalyst in a reaction zone under disproportionation conditions to form a disproportionation product mixture comprising at least about 3 wt % C alkanes in 1 hr based on the Calkanes in the hydrocarbon feed, wherein the liquid catalyst comprises an unsupported ionic liquid and a carbocation promoter, and wherein a mass ratio of the ionic liquid to the hydrocarbon feed is less than 0.75:1.'}2. The process of wherein the ionic liquid comprises an organic cation and an anion.4. The process of wherein the anion is derived from halides claim 2 , sulfates claim 2 , bisulfates claim 2 , nitrates claim 2 , sulfonates claim 2 , fluoroalkanesulfonates claim 2 , or combinations thereof.5. The process of wherein the anion is selected from the group consisting of AlCl claim 2 , AlCl claim 2 , AlCl claim 2 , AlClBr claim 2 , AlClBr claim 2 , AlClBr claim 2 , AlBr claim 2 , AlBr claim 2 , AlBr claim 2 , GaCl claim 2 , GaCl claim 2 , GaCl claim 2 , GaClBr claim 2 , GaClBr claim 2 , GaClBr claim 2 , CuCl claim 2 , CuCl claim 2 , CuCl claim 2 , ZnCl claim 2 , FeCl claim 2 , FeCl claim 2 , FeCl claim 2 , PF claim 2 , and BF.6. The process of wherein the carbocation promoter comprises halo-alkanes claim 1 , mineral acids claim 1 , or combinations thereof.7. The process of further comprising stirring the hydrocarbon feed and the liquid catalyst while contacting the hydrocarbon feed with the liquid catalyst.8. The process of wherein the carbocation promoter comprises 2-chloro-2-methylpropane claim 1 , 2-chloropropane claim 1 , 2 ...

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Номер записи: 16
01-01-2015 дата публикации

CATALYTIC DISPROPORTIONATION OF HEPTANE USING IONIC LIQUIDS

Номер: US20150005544A1
Автор: Bhattacharyya Alakananda, Smith Stuart
Принадлежит:

Processes for the disproportionation and isomerization of a Chydrocarbon feed using a liquid catalyst comprising an ionic liquid and a carbocation promoter are described. The ionic liquid is unsupported, and the reactions occur at temperatures below about 200° C. 1. A hydrocarbon conversion process comprising:{'sub': 7', '8+', '7, 'disproportionating a hydrocarbon feed comprising Calkanes by contacting the hydrocarbon feed with a liquid catalyst in a reaction zone under disproportionation conditions to form a product mixture comprising at least about 3 wt % C alkanes in 1 hr based on the Calkanes in the hydrocarbon feed, wherein the liquid catalyst comprises an unsupported ionic liquid and a carbocation promoter, and wherein a mass ratio of the liquid catalyst to the hydrocarbon feed is less than 0.75:1.'}2. The process of wherein the ionic liquid comprises an organic cation and an anion.4. The process of wherein the anion is derived from halides claim 2 , sulfates claim 2 , bisulfates claim 2 , nitrates claim 2 , sulfonates claim 2 , fluoroalkanesulfonates claim 2 , or combinations thereof.5. The process of wherein the anion is selected from the group consisting of AlCl claim 2 , AlCl claim 2 , AlCl claim 2 , AlClBr claim 2 , AlClBr claim 2 , AlClBr claim 2 , AlBr claim 2 , AlBr claim 2 , AlBr claim 2 , GaCl claim 2 , GaCl claim 2 , GaCl claim 2 , GaClBr claim 2 , GaClBr claim 2 , GaClBr claim 2 , CuCl claim 2 , CuCl claim 2 , CuCl claim 2 , ZnCl claim 2 , FeCl claim 2 , FeCl claim 2 , FeCl claim 2 , PF claim 2 , and BF.6. The process of wherein the carbocation promoter comprises halo-alkanes claim 1 , mineral acids claim 1 , or combinations thereof.7. The process of further comprising stirring the hydrocarbon feed and the liquid catalyst while contacting the hydrocarbon feed with the liquid catalyst.8. The process of wherein the carbocation promoter comprises 2-chloro-2-methylpropane claim 1 , 2-chloropropane claim 1 , 2-chlorobutane claim 1 , 2-chloro-2- ...

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Номер записи: 17
01-01-2015 дата публикации

CATALYTIC DISPROPORTIONATION OF PENTANE USING IONIC LIQUIDS

Номер: US20150005545A1
Автор: Bhattacharyya Alakananda, Smith Stuart
Принадлежит:

Processes for the disproportionation and isomerization of a Chydrocarbon feed using a liquid catalyst comprising an ionic liquid and a carbocation promoter are described. The ionic liquid is unsupported, and the reactions occur at temperatures below about 200° C. 1. A hydrocarbon conversion process comprising:{'sub': 5', '4−', '6+', '5, 'disproportionating a hydrocarbon feed comprising Calkanes by contacting the hydrocarbon feed with a liquid catalyst in a reaction zone under disproportionation conditions to form a product mixture comprising at least about 5 wt % C alkanes, and at least about 5 wt % C alkanes in 30 min based on the Calkanes in the hydrocarbon feed, wherein the liquid catalyst comprises an unsupported ionic liquid and a carbocation promoter, and wherein a mass ratio of the liquid catalyst to the hydrocarbon feed is less than 0.75:1.'}2. The process of wherein the ionic liquid comprises an organic cation and an anion.4. The process of wherein the anion is derived from halides claim 2 , sulfates claim 2 , bisulfates claim 2 , nitrates claim 2 , sulfonates claim 2 , fluoroalkanesulfonates claim 2 , or combinations thereof.5. The process of wherein the anion is selected from the group consisting of AlCl claim 2 , AlCl claim 2 , AlCl claim 2 , AlClBr claim 2 , AlClBr claim 2 , AlClBr claim 2 , AlBr claim 2 , AlBr claim 2 , AlBr claim 2 , GaCl claim 2 , GaCl claim 2 , GaCl claim 2 , GaClBr claim 2 , GaClBr claim 2 , GaClBr claim 2 , CuCl claim 2 , CuCl claim 2 , CuCl claim 2 , ZnCl claim 2 , FeCl claim 2 , FeCl claim 2 , FeCl claim 2 , PF claim 2 , and BF.6. The process of wherein the carbocation promoter comprises halo-alkanes claim 1 , mineral acids claim 1 , or combinations thereof.7. The process of further comprising stirring the hydrocarbon feed and the liquid catalyst while contacting the hydrocarbon feed with the liquid catalyst.8. The process of wherein the carbocation promoter comprises 2-chloro-2-methylpropane claim 1 , 2-chloropropane claim 1 , ...

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Номер записи: 18
01-01-2015 дата публикации

CATALYTIC ISOMERIZATION OF HEXANES USING IONIC LIQUIDS

Номер: US20150005546A1
Автор: Bhattacharyya Alakananda, Martin Susie C., Smith Stuart, Sullivan Dana K.
Принадлежит:

Processes for the disproportionation and isomerization of a hydrocarbon feed using a liquid catalyst comprising an ionic liquid and a carbocation promoter are described. The ionic liquid is unsupported, and the reactions occur at temperatures below the decomposition temperature of the ionic liquid, typically below about 250° C. The process includes isomerizing a hydrocarbon feed comprising normal Calkane or branched Calkane by contacting the hydrocarbon feed with a liquid catalyst in a reaction zone to form a product mixture. Isomerization reaction mixtures are also described. 1. A hydrocarbon conversion process comprising:{'sub': 6', '6', '6', '6', '6', '6', '6', '6, 'isomerizing a hydrocarbon feed comprising normal Calkane or branched Calkane by contacting the hydrocarbon feed with a liquid catalyst in a reaction zone under isomerization conditions to form a product mixture comprising at least about 5 wt % branched Calkanes if the hydrocarbon feed was the normal Calkane or at least about 2 wt % normal Calkanes if the hydrocarbon feed was the branched Calkane in 1 hr based on the normal Calkane or branched Calkane in the hydrocarbon feed, wherein the liquid catalyst comprises an unsupported ionic liquid and a carbocation promoter comprising a haloalkane, and wherein a mass ratio of liquid catalyst to hydrocarbon feed is less than 0.75:1.'}2. The process of wherein the ionic liquid comprises an organic cation and an anion.4. The process of wherein the anion is derived from halides claim 2 , sulfates claim 2 , bisulfates claim 2 , nitrates claim 2 , sulfonates claim 2 , fluoroalkanesulfonates claim 2 , or combinations thereof.5. The process of wherein the anion is selected from the group consisting of AlCl claim 2 , AlCl claim 2 , AlCl claim 2 , AlClBr claim 2 , AlClBr claim 2 , AlClBr claim 2 , AlBr claim 2 , AlBr claim 2 , AlBr claim 2 , GaCl claim 2 , GaCl claim 2 , GaCl claim 2 , GaClBr claim 2 , GaClBr claim 2 , GaClBr claim 2 , CuCl claim 2 , CuCl claim 2 , ...

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Номер записи: 19
01-01-2015 дата публикации

CATALYTIC ISOMERIZATION OF BUTANE USING IONIC LIQUIDS

Номер: US20150005554A1
Автор: Bhattacharyya Alakananda, Smith Stuart
Принадлежит: UOP LLC

Processes for the disproportionation and isomerization of a Chydrocarbon feed using a liquid catalyst comprising an ionic liquid and a carbocation promoter are described. The ionic liquid is unsupported, and the reactions occur at temperatures below about 300° C. 1. A hydrocarbon conversion process comprising:{'sub': 4', '4', '4', '4, 'isomerizing a hydrocarbon feed comprising normal Calkane or branched Calkane by contacting the hydrocarbon feed with a liquid catalyst in a reaction zone under isomerization conditions to form a product mixture having a ratio of branched Calkane to normal Calkane of at least about 0.3:1 in 1 hr, wherein the liquid catalyst comprises an unsupported ionic liquid and a carbocation promoter, and wherein a mass ratio of liquid catalyst to hydrocarbon feed is less than 0.75:1.'}3. The process of wherein the ionic liquid comprises an organic cation and an anion and wherein the anion is derived from halides claim 1 , sulfates claim 1 , bisulfates claim 1 , nitrates claim 1 , sulfonates claim 1 , fluoroalkanesulfonates claim 1 , or combinations thereof.4. The process of wherein the ionic liquid comprises an organic cation and an anion and wherein the anion is selected from the group consisting of AlCl claim 1 , AlCl claim 1 , AlCl claim 1 , AlClBr claim 1 , AlClBr claim 1 , AlClBr claim 1 , AlBr claim 1 , AlBr claim 1 , AlBr claim 1 , GaCl claim 1 , GaCl claim 1 , GaCl claim 1 , GaClBr claim 1 , GaClBr claim 1 , GaClBr claim 1 , CuCl claim 1 , CuCl claim 1 , CuCl claim 1 , ZnCl claim 1 , FeCl claim 1 , FeCl claim 1 , FeCl claim 1 , PF claim 1 , and BF.5. The process of wherein the carbocation promoter comprises a haloalkane claim 1 , a mineral acid claim 1 , or combinations thereof.6. The process of wherein the haloalkane comprises 2-chloro-2-methylpropane claim 5 , 2-chloropropane claim 5 , 2-chlorobutane claim 5 , 2-chloro-2-methylbutane claim 5 , 2-chloropentane claim 5 , 1-chlorohexane claim 5 , 3-chloro-3-methylpentane claim 5 , or ...

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Номер записи: 20
01-01-2015 дата публикации

CATALYTIC DISPROPORTIONATION OF BUTANE USING IONIC LIQUIDS

Номер: US20150005555A1
Автор: Bhattacharyya Alakananda, Smith Stuart
Принадлежит: UOP LLC

Processes for the disproportionation and isomerization of a Chydrocarbon feed using a liquid catalyst comprising an ionic liquid and a carbocation promoter are described. The ionic liquid is unsupported, and the reactions occur at temperatures below about 300° C. 1. A hydrocarbon conversion process comprising:{'sub': 4', '4', '3−', '5+', '4, 'disproportionating a hydrocarbon feed comprising normal Calkane or branched Calkane by contacting the hydrocarbon feed with a liquid catalyst in a reaction zone under disproportionation conditions to form a product mixture comprising at least about 0.2 wt % C alkanes and C alkanes in 1 hr based on the Calkanes in the hydrocarbon feed, wherein the liquid catalyst comprises an unsupported ionic liquid and a carbocation promoter, and wherein a mass ratio of liquid catalyst to hydrocarbon feed is less than 0.75:1.'}2. The process of wherein the ionic liquid comprises an organic cation and an anion.4. The process of wherein the anion is derived from halides claim 2 , sulfates claim 2 , bisulfates claim 2 , nitrates claim 2 , sulfonates claim 2 , fluoroalkanesulfonates claim 2 , or combinations thereof.5. The process of wherein the anion is selected from the group consisting of AlCl claim 2 , AlCl claim 2 , AlCl claim 2 , AlClBr claim 2 , AlClBr claim 2 , AlClBr claim 2 , AlBr claim 2 , AlBr claim 2 , AlBr claim 2 , GaCl claim 2 , GaCl claim 2 , GaCl claim 2 , GaClBr claim 2 , GaClBr claim 2 , GaClBr claim 2 , CuCl claim 2 , CuCl claim 2 , CuCl claim 2 , ZnCl claim 2 , FeCl claim 2 , FeCl claim 2 , FeCl claim 2 , PF claim 2 , and BF.6. The process of wherein the carbocation promoter comprises a haloalkane claim 1 , a mineral acid claim 1 , or combinations thereof.7. The process of wherein the carbocation promoter comprises the haloalkane claim 6 , and wherein the haloalkane comprises 2-chloro-2-methylpropane claim 6 , 2-chloropropane claim 6 , 2-chlorobutane claim 6 , 2-chloro-2-methylbutane claim 6 , 2-chloropentane claim 6 , 1- ...

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Номер записи: 21
01-01-2015 дата публикации

CATALYTIC REVERSE DISPROPORTIONATION OF PARAFFINS USING IONIC LIQUIDS

Номер: US20150005556A1
Автор: Abrevaya Hayim, Bhattacharyya Alakananda, Smith Stuart, Walenga Joel T.
Принадлежит:

A reverse disproportionation reaction of two hydrocarbon feeds allows production of a reaction mixture containing products with intermediate carbon numbers. The amount of at least one of the products with intermediate carbon numbers is equal to or greater than the amount formed from disproportionation of the hydrocarbon alone. A reverse disproportionation reaction mixture is also described. 1. A hydrocarbon conversion process comprising:{'sub': n', 'm', 'n+1', 'm−1', 'n+1', 'm−1', 'n+1', 'm−1', 'n', 'm, 'reverse disproportionating two hydrocarbon feeds, the first hydrocarbon feed comprising one or more Calkanes and the second hydrocarbon feed comprising one or more Calkanes, where n=1-198, m=3-200, and m−n=2 or more, by contacting the first and second hydrocarbon feeds with a liquid catalyst in a reaction zone under reverse disproportionation conditions to form a product mixture comprising at least one Cto Calkanes, wherein an amount of at least one of the Cto Calkanes in the product mixture is equal to or greater than an amount of the at least one Cto Calkanes formed from disproportionating the Calkane or Calkane alone, wherein the liquid catalyst comprises an ionic liquid and carbocation promoter.'}2. The process of wherein n=1-4 claim 1 , m=5-12 claim 1 , and the product mixture comprises at least one Calkane where n Подробнее

Номер записи: 22
01-01-2015 дата публикации

METHOD FOR TUNING PRODUCT COMPOSITION BASED ON VARYING TYPES AND RATIOS OF FEED

Номер: US20150005560A1
Автор: Bhattacharyya Alakananda, Coughlin Peter K., Smith Stuart
Принадлежит:

A process of tuning a hydrocarbon product composition is described. The process involves selecting paraffins for reaction. The equilibrium constants for reactions of the selected paraffins can be used to select appropriate feed ratios, or an equilibrium composition as function of C/H molar ratio. A selected feed is reacted to obtain the product. Equilibrium product compositions and non-equilibrium product compositions can be obtained using the process. 1. A process of tuning a hydrocarbon product composition comprising:selecting a range of paraffins;determining a series of equilibrium constants for reactions of the selected range of paraffins;selecting a desired product composition based on an equilibrium composition;{'sub': 'n', 'selecting a hydrocarbon feed based on the desired product composition, the selected hydrocarbon feed comprising at least one Calkane where n=1-200determining a feed ratio based on the selected hydrocarbon feed and the desired product composition;reacting the selected hydrocarbon feed by contacting the selected hydrocarbon feed with a liquid catalyst in the determined feed ratio in a reaction zone under tuning conditions to form the desired product composition, the liquid catalyst comprising an ionic liquid and a carbocation promoter; andrecovering the desired product composition.2. The process of further comprising:selecting a C/H molar ratio which yields the desired product composition as determined from the series of equilibrium constants;wherein selecting the desired product composition based on the equilibrium composition comprises selecting the desired product composition based on the equilibrium composition at the selected C/H molar ratio;wherein determining the feed ratio based on the selected hydrocarbon feed and the desired product composition comprises determining the feed ratio based on the selected hydrocarbon feed, the desired product composition, and the selected C/H molar ratio.3. The process of wherein the C/H molar ratio ...

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Номер записи: 23
03-02-2022 дата публикации

PROCESS FOR PREPARING LINEAR ALKYL BENZENE

Номер: US20220033323A1
Автор: Aduri Pavankumar, Chafle Romal, Dhawade Rahul Mahadeo, Dhukande Vibhuti, Goyal Gordhan Das, Iyengar Suresh, Kotra Viswanath, Kumbhar Rahul, Ratnaparkhi Uday Meghashyam, Sakhalkar Mangesh Raghunath, Uppara Parasuveera
Принадлежит: RELIANCE INDUSTRIES LIMITED

The present disclosure relates to a process for preparing linear alkyl benzne (LAB). The process comprises alkylation of benzene with an alkylating agent in the presence of an ionic liquid to obtain a first product mixture comprising a first organic phase and a first aqueous phase comprising first partially spent ionic liquid. The first organic phase is deacidified and fractionally distilled to obtain a fraction comprising LAB and a fraction comprising HAB. The fraction comprising HAB is transalkylated with benzene in the presence of the ionic liquid to obtain a second product mixture comprising a second organic phase comprising LAB and a second aqueous phase comprising second partially spent ionic liquid. The partially spent ionic liquids are regenerated, and reused in the steps of alkylation or transalkylation for at least 6 cycles. 1. A process for preparing linear alkyl benzene by alkylation of benzene , said process comprising the following steps:a) alkylating benzene with an alkylating agent in the presence of an ionic liquid to obtain a first product mixture;b) allowing the first product mixture to settle to obtain a first biphasic mixture comprising a first organic phase and a first aqueous phase, wherein the first organic phase comprises linear alkyl benzene (LAB), heavier alkyl benzene (HAB) and unreacted benzene, and the first aqueous phase comprises first partially spent ionic liquid;c) deacidifying the first organic phase to obtain a deacidified first organic phase;d) fractionally distlling the deacidified first organic phase to obtain a fraction comprising unreacted benzene, a fraction comprising LAB and a fraction comprising HAB;e) transalkylating the fraction comprising HAB with benzene in the presence of the ionic liquid at a temperature in the range of 70° C. to 120° C. to obtain a second product mixture;f) allowing the second product mixture to settle to obtain a second biphasic mixture comprising a second organic phase and a second aqueous phase; ...

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Номер записи: 24
17-01-2019 дата публикации

Process for producing ethylbenzene

Номер: US20190016647A1
Автор: Brian Maerz, Chung-Ming Chi, Raghavender Bhoomi
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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Номер записи: 25
21-01-2021 дата публикации

Processes for Converting Aromatic Hydrocarbons via Alkyl-Demethylation

Номер: US20210017102A1
Автор: Brody John F., Levin Doron, Molinier Michel, Nair Hari, Rungta Meha, Salciccioli Michael, Weigel Scott J.
Принадлежит:

Alkyl-demethylation of C2+-hydrocarbyl substituted aromatic hydrocarbons can be utilized to treat one or more of a heavy naphtha reformate stream, a hydrotreated SCN stream, a C8 aromatic hydrocarbon isomerization feed stream, a C9+ aromatic hydrocarbon transalkylation feed stream, and similar hydrocarbon streams to produce additional quantity of xylene products. 1. A process for making xylenes , the process comprising:(I) providing a C6+ aromatic hydrocarbon-containing stream comprising a C2+-hydrocarbyl-substituted aromatic hydrocarbon, wherein the C2+-hydrocarbyl-substituted aromatic hydrocarbon has (i) a C2+ alkyl substitute attached to an aromatic ring therein and/or (ii) an aliphatic ring annelated to an aromatic ring therein;(II) optionally contacting the C6+ aromatic hydrocarbon-containing stream with a first alkyl-demethylation catalyst in a first alkyl-demethylation zone under a first set of alkyl-demethylation conditions to convert at least a portion of the C2+-hydrocarbyl-substituted aromatic hydrocarbon to an alkyl-demethylated aromatic hydrocarbon to obtain an optional first alkyl-demethylated effluent exiting the first alkyl-demethylation zone;(III) separating at least a portion of the C6+ aromatic hydrocarbon-containing stream and/or the first alkyl-demethylated effluent in a first separation apparatus to obtain a C6-C7 hydrocarbons-rich stream and a first C8+ aromatic hydrocarbons-rich stream;(IV) optionally contacting the first C8+ aromatic hydrocarbons-rich stream with a second alkyl-demethylation catalyst in a second alkyl-demethylation zone under a second set of alkyl-demethylation conditions to convert at least a portion of the C2+-hydrocarbyl-substituted aromatic hydrocarbon, if any, contained in the first C8+ aromatic hydrocarbons-rich stream to an alkyl-demethylated aromatic hydrocarbon to obtain an optional second alkyl-demethylated effluent exiting the second alkyl-demethylation zone;(V) separating at least a portion of the first C8+ ...

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Номер записи: 26
16-01-2020 дата публикации

CONVERSION OF WASTE PLASTIC THROUGH PYROLYSIS TO HIGH VALUE PRODUCTS LIKE BENZENE AND XYLENES

Номер: US20200017773A1
Автор: GANAPATHY BHOTLA Venkata Ramanarayanan, GANJI Santosh, Narayanaswamy Ravichander, Ramamurthy Krishna Kumar, STANISLAUS Alexander
Принадлежит:

A process for producing benzene and xylenes comprising introducing hydrocarbon liquid stream to hydroprocessor to yield first gas stream and hydrocarbon product (C+); optionally introducing hydrocarbon product to first aromatics separating unit to produce saturated hydrocarbons (C+) and first aromatics stream (C+); feeding hydrocarbon product and/or saturated hydrocarbons to reformer to produce reformer product, second gas stream, and hydrogen stream; introducing reformer product to second aromatics separating unit to produce a non-aromatics recycle stream and second aromatics stream comprising C+ aromatics; recycling non-aromatics recycle stream to reformer; introducing first aromatics stream and/or second aromatics stream to third aromatics separating unit to produce first Caromatics (benzene), Caromatics (toluene), Caromatics (xylenesðylbenzene), C 1. A process for producing benzene and xylenes comprising:{'sub': '5', '(a) contacting a hydrocarbon liquid stream with a hydroprocessing catalyst in the presence of hydrogen in a hydroprocessing unit to yield a hydrocarbon product and a first gas stream, wherein the hydrocarbon product comprises C+ hydrocarbons;'}{'sub': 5', '6, '(b) optionally introducing at least a portion of the hydrocarbon product to a first aromatics separating unit to produce a saturated hydrocarbons stream and a first aromatics stream, wherein the saturated hydrocarbons stream comprises C+ saturated hydrocarbons, and wherein the first aromatics stream comprises C+ aromatic hydrocarbons;'}{'sub': 6', '8', '6', '8, '(c) feeding at least a portion of the hydrocarbon product and/or at least a portion of the saturated hydrocarbons stream to a reforming unit to produce a reforming unit product, a second gas stream, and a hydrogen stream, wherein the reforming unit comprises a reforming catalyst, and wherein an amount of Cto Caromatic hydrocarbons in the reforming unit product is greater than an amount of Cto Caromatic hydrocarbons in the saturated ...

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Номер записи: 27
01-02-2018 дата публикации

Catalyst System and Use in Heavy Aromatics Conversion Processes

Номер: US20180029025A1
Автор: Christine N. Elia, Hari Nair, Robert G. TINGER, Shifang L. Luo, Wenyih F. Lai
Принадлежит: ExxonMobil Chemical Patents Inc

Disclosed are a catalyst system and its use in a process for the conversion of a feedstock containing C 8 + aromatic hydrocarbons to produce light aromatic products, comprising benzene, toluene and xylene. The catalyst system comprises (a) a first catalyst bed comprising a first catalyst composition, said first catalyst composition comprising a zeolite having a constraint index of 3 to 12 combined (i) optionally with at least one first metal of Group 10 of the IUPAC Periodic Table, and (ii) optionally with at least one second metal of Group 11 to 15 of the IUPAC Periodic Table; and (b) a second catalyst bed comprising a second catalyst composition, said second catalyst composition comprising (i) a meso-mordenite zeolite, combined (ii) optionally with at least one first metal of Group 10 of the IUPAC Periodic Table, and (iii) optionally with at least one second metal of Group 11 to 15 of the IUPAC Periodic Table, wherein said meso-mordenite zeolite is synthesized from TEA or MTEA and having a mesopore surface area of greater than 30 m 2 /g and said meso-mordenite zeolite comprises agglomerates composed of primary crystallites, wherein said primary crystallites have an average primary crystal size as measured by TEM of less than 80 nm and an aspect ratio of less than 2.

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Номер записи: 28
29-01-2015 дата публикации

PROCESSES AND APPARATUSES FOR PREPARING AROMATIC COMPOUNDS

Номер: US20150031928A1
Автор: Kokayeff Peter, Noe Jason L.
Принадлежит: UOP LLC

Processes and apparatuses for preparing aromatic compounds are provided herein. In an embodiment, a process for preparing aromatic compounds includes providing a first stream that includes an aromatic component, a non-aromatic component, and a sulfur-containing component. The aromatic component and the sulfur-containing component are separated from the non-aromatic component of the first stream to form a separated aromatic stream and a raffinate stream. The separated aromatic stream includes the aromatic component and the sulfur-containing component. The raffinate stream includes the non-aromatic component. The separated aromatic stream is concurrently transalkylated and desulfurized in the presence of a catalyst that includes acid function and metal function to produce a transalkylated aromatic stream and a sulfur-containing gas stream that is separate from the transalkylated aromatic stream. 1. A process for preparing aromatic compounds , the process comprising the steps of:providing a first stream comprising an aromatic component, a non-aromatic component, and a sulfur-containing component;separating the aromatic component and the sulfur-containing component from the non-aromatic component of the first stream to form a separated aromatic stream comprising the aromatic component and the sulfur-containing component and a raffinate stream comprising the non-aromatic component;concurrently transalkylating and desulfurizing the separated aromatic stream in the presence of a catalyst that includes acid function and metal function to produce a transalkylated aromatic stream and a sulfur-containing gas stream separate from the transalkylated aromatic stream.2. The process of claim 1 , wherein providing the first stream comprises fractionating a full boiling range naphtha stream comprising the sulfur-containing component into a fractionation overhead stream comprising compounds having 5 or less carbon atoms claim 1 , a fractionation bottoms stream comprising compounds ...

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Номер записи: 29
30-01-2020 дата публикации

Heavy Aromatics Conversion Processes and Catalyst Compositions Used Therein

Номер: US20200031737A1
Автор: Bai Chuansheng, Cutler Joshua I., Elias Christine N., Lai Wenyih F., Nair Hari, Rollman Nicholas S.
Принадлежит:

Disclosed are processes for conversion of a feedstock comprising C aromatic hydrocarbons to lighter aromatic products in which the feedstock and optionally hydrogen are contacted in the presence of the catalyst composition under conversion conditions effective to dealkylate and transalkylate said C aromatic hydrocarbons to produce said lighter aromatic products comprising benzene, toluene and xylene. The catalyst composition comprises a zeolite, a first metal, and a second metal, and is treated with a source of sulfur and/or a source of steam. 125.-. (canceled)26. A process for conversion of a feedstock comprising Caromatic hydrocarbons to lighter aromatic products , the process comprising the step of contacting said feedstock and optionally hydrogen in the presence of a catalyst composition under conversion conditions effective to dealkylate and transalkylate said Caromatic hydrocarbons to produce said lighter aromatic products comprising benzene , toluene and xylene ,wherein said catalyst composition is treated with a source of sulfur and/or steam and comprises:(i) at least one zeolite selected from the group consisting of zeolite beta, ZSM-4, ZSM-5, ZSM-11, ZSM-12, ZSM-20, ZSM-22, ZSM-23, ZSM-35, ZSM-48, ZSM-50, ZSM-57, ZSM-58, MCM-68, a faujasite zeolite, a mordenite zeolite, a MCM-22 family material, or a mixture thereof,(ii) 0.001 wt. % to 20.0 wt. % of at least one first metal, said first metal being in Group 6 of the Periodic Table, based on the weight of said catalyst composition, and(iii) 0.001 wt. % to 20.0 wt. % of at least one second metal, said second metal being in Group 9 or Group 10 of the Periodic Table, based on the weight of said catalyst composition.27. The process of claim 26 , wherein said catalyst composition is treated with said source of sulfur in one or more steps at temperatures in the range 204° C. (400° F.) up to about 480° C. (900° F.).28. The process of claim 27 , wherein said source of sulfur is one or more of hydrogen sulfide claim ...

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Номер записи: 30
30-01-2020 дата публикации

Heavy Aromatics Conversion Processes and Catalyst Compositions Used Therein

Номер: US20200031740A1
Автор: Bai Chuansheng, Cutler Joshua I., Elias Christine N., Lai Wenyih F., Nair Hari, Rollman Nicholas S.
Принадлежит:

Disclosed are processes for conversion of a feedstock comprising C aromatic hydrocarbons to lighter aromatic products in which the feedstock and optionally hydrogen are contacted in the presence of a first and a second catalyst composition under conversion conditions effective to produce said lighter aromatic products comprising benzene, toluene and xylene. In the process, the C aromatic hydrocarbons are dealkylated to form C-Caromatic hydrocarbon and the C olefins formed are saturated. The remaining C aromatic hydrocarbons are transalkylated with the C-Caromatic hydrocarbon. The first and second catalyst compositions each comprise a zeolite, a first metal, and optionally a second metal, and are treated with a source of sulfur and/or a source of steam. 125.-. (canceled)27. The process of claim 26 , wherein said first catalyst composition and/or said second catalyst composition is treated with said source of sulfur in one or more stages at temperatures in the range 204° C. (400° F.) up to about 480° C. (900° F.).28. The process of claim 26 , wherein said source of sulfur is one or more of hydrogen sulfide claim 26 , carbon disulfide and alkylsulfides which are selected from the group consisting of methylsulfide claim 26 , dimethylsulfide claim 26 , dimethyldisulfide claim 26 , diethylsulfide claim 26 , dibutyl sulfide claim 26 , and mixtures of two or more thereof.29. The process of claim 26 , wherein said first zeolite and/or said second zeolite are treated with a source of steam.30. The process of claim 26 , wherein said source of steam comprises up to about 100% steam at temperatures in the range of about 260° C. (500° F.) to about 649° C. (1200° F.) and said treatment is in one or more temperature stages.31. The process of claim 26 , wherein said first metal of Group 6 is selected from the group consisting of chromium claim 26 , molybdenum claim 26 , tungsten and mixtures of two or more thereof.32. The process of claim 26 , wherein said second metal of Group 9 is ...

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Номер записи: 31
30-01-2020 дата публикации

PROCESS FOR MAKING XYLENES AND PHENOL FROM COAL DERIVED LIQUIDS

Номер: US20200031741A1
Автор: Zhang Shuguang, Zhou Lubo
Принадлежит:

Processes and apparatus for making xylenes and phenol are described. Phenol and alkyl phenols are separated from coal derived liquid. The phenol is separated from the alkyl phenols. The alkyl phenols can be reacted with aromatics such as benzene and toluene to make xylenes. The xylenes and other aromatics are then separated from the phenol and alkyl phenols. Para-xylene is separated and recovered using a xylene separation process, and meta-xylene and ortho-xylene are optionally converted to para-xylene through an isomerization reaction. 1. A process for making xylenes and phenol comprising:providing a first phenols stream comprising phenol and alkyl phenols from a coal derived liquid;separating the first phenols stream into at least a phenol product stream comprising phenol, and a cresols stream comprising cresols in a phenols separation zone;transalkylating the cresols stream with a first aromatics stream comprising toluene, benzene, or both in a cresols transalkylation reaction zone in the presence of a cresols transalkylating catalyst to form a first effluent stream comprising aromatics, phenol, and alkyl phenols;separating the first effluent stream into at least a second aromatics stream comprising aromatics and a second phenols stream comprising phenol and alkyl phenols in a phenols and aromatics separation zone;separating the second aromatics stream into at least the first aromatics stream and a first xylenes stream comprising para-xylene, ortho-xylene, and meta-xylene in an aromatics separation zone; andintroducing the second phenols stream into the phenols separation zone.2. The process of wherein separating the first phenols stream into at least the phenol product stream claim 1 , and the cresols stream comprises separating the first phenols stream into at least the phenol product stream claim 1 , the cresols stream claim 1 , and a xylenols stream comprising xylenols; wherein the first aromatics stream comprises toluene; and wherein separating the second ...

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Номер записи: 32
04-02-2021 дата публикации

Xylene Production Processes and Systems

Номер: US20210032182A1
Автор: Levin Doron, Molinier Michel, Nair Hari, Salciccioli Michael, Weigel Scott J.
Принадлежит:

A process and related system for producing para-xylene (PX). In an embodiment, the process includes (a) separating a feed stream comprising C aromatic hydrocarbons into a toluene containing stream and a C hydrocarbon containing stream and (b) contacting at least part of the toluene containing stream with a methylating agent in a methylation unit to convert toluene to xylenes and produce a methylated effluent stream. In addition, the process includes (c) recovering PX from the methylated effluent stream in (b) to produce a PX depleted stream and (d) transalkylating the PX depleted stream to produce a transalkylation effluent stream. The transalkylation effluent stream includes a higher concentration of toluene than the PX depleted stream. Further, the process includes (e) converting at least some ethylbenzene (EB) within the C hydrocarbon containing stream into toluene and (f) flowing the toluene converted in (e) to the contacting in (b). 1. A process for producing para-xylene (PX) , the process comprising:{'sub': 6+', '8+, '(a) separating a feed stream comprising C aromatic hydrocarbons into at least a toluene containing stream and a C hydrocarbon containing stream;'}(b) contacting at least part of the toluene containing stream with a methylating agent in a methylation unit under conditions effective to convert toluene to xylenes and produce a methylated effluent stream;(c) recovering PX from the methylated effluent stream in (b) to produce a PX depleted stream;(d) transalkylating the PX depleted stream to produce a transalkylation effluent stream, wherein the transalkylation effluent stream includes a higher concentration of toluene than the PX depleted stream;{'sub': '8+', '(e) converting at least some ethylbenzene (EB) within the C hydrocarbon containing stream into toluene; and'}(f) flowing the toluene converted in (e) to the contacting in (b).2. The process of claim 1 , further comprising:{'sub': 7', '8+, '(g) separating from the transalkylation effluent stream ...

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Номер записи: 33
05-02-2015 дата публикации

SYSTEMS AND METHODS OF PRODUCING AROMATIC PRODUCTS

Номер: US20150038752A1
Автор: Noe Jason L., Prudhom Jon Eric
Принадлежит: UOP LLC

Systems and methods for producing aromatic products are provided. An aromatic stream is provided with aromatic compounds and olefins. The olefins are reacted with aromatic compounds to form colored bodies, and the aromatic stream is distilled to produce an overhead stream and reboiler stream. The colored bodies are in the reboiler stream, and the reboiler stream is passed through an absorbent to remove the colored bodies. 1. A method of producing toluene , the method comprising the steps of:processing a feed naphtha stream with a naphtha processing unit to produce a processed naphtha stream;separating the processed naphtha stream into an aromatic stream and a non-aromatic stream, wherein the aromatic stream primarily comprises toluene and benzene;reacting olefins remaining in the aromatic stream to produce colored bodies;distilling the aromatic stream to produce an overhead stream and a reboiler stream, wherein the reboiler stream comprises toluene and colored bodies; andremoving the colored bodies from the reboiler stream by passing the reboiler stream through an absorbent, wherein the absorbent selectively absorbs colored bodies over toluene.2. A method of producing aromatic products , the method comprising the steps of:providing an aromatic stream, where the aromatic stream comprises aromatic compounds and olefins;reacting the olefins with the aromatic compounds in the aromatic stream to form colored bodiesdistilling the aromatic stream to produce an overhead stream and a reboiler stream, wherein the reboiler stream comprises the colored bodies; andpassing the reboiler stream through an absorbent to remove the colored bodies.3. The method of where providing the aromatic stream further comprises providing an aromatic stream primarily comprising benzene and toluene.4. The method of wherein providing the aromatic stream further comprises processing a feed naphtha stream with a reforming process claim 3 , wherein aromatic compounds are produced in the reforming ...

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Номер записи: 34
24-02-2022 дата публикации

Selective catalyst for hydrogenolysis of ethyl-aromatics by conserving methyl-aromatics

Номер: US20220056350A1
Автор: Alexandre Jouve, Anne-Claire Dubreuil, Denis Uzio, Vincent Coupard
Принадлежит: IFP Energies Nouvelles IFPEN

The present invention relates to a hydrogenolysis process wherein a hydrocarbon-based feedstock comprising aromatic compounds having at least 8 carbon atoms is treated by means of a hydrogen feed and in the presence of a catalyst, in order to convert C2+ alkyl chains of said aromatic compounds into methyl groups and to produce a hydrogenolysis effluent enriched in methyl-substituted aromatic compounds, wherein the catalyst comprises a support, comprising at least one refractory oxide, and an active phase comprising nickel and molybdenum, wherein: the nickel content being between 0.1 and 25% by weight relative to the total weight of the catalyst; the molybdenum content being between 0.1 and 20% by weight relative to the total weight of the catalyst; and the catalyst comprising a molar ratio of molybdenum to nickel of between 0.2 and 0.9. The present invention also relates to said catalyst and to the process for preparing said catalyst.

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Номер записи: 35
06-02-2020 дата публикации

Methods and Systems of Upgrading Heavy Aromatics Stream to Petrochemical Feedstock

Номер: US20200039898A1
Автор: HODGKINS Robert, KOSEOGLU Omer Refa
Принадлежит: Saudi Arabian Oil Company

Provided here are systems and methods that integrate a hydrodearylation process and a transalkylation process into an aromatic recovery complex. Various other embodiments may be disclosed and claimed. 1. A system for conversion of alkyl-bridged non-condensed alkyl multi-aromatic compounds to alkyl mono-aromatic compounds , the system comprising:{'sub': 9', '10, 'a first separator adapted to receive a feed stream containing one or more of heavy alkyl aromatic compounds and one or more alkyl-bridged non-condensed alkyl multi-aromatic compounds having at least two benzene rings connected by an alkyl bridge group with at least two carbons and the benzene rings being connected to different carbons of the alkyl bridge group, and produces a first product stream containing Cand Ccompounds and a second product stream containing one or more of heavy alkyl aromatic compounds and alkyl-bridged non-condensed alkyl multi-aromatic compounds;'}a hydrodearylation reactor fluidly coupled to the first separator and adapted to receive a hydrogen stream and the second product stream and to produce a third product stream in presence of a catalyst, the third product stream containing one or more alkyl mono-aromatic compounds; and{'sub': 8', '9+, 'a second separator fluidly coupled to the hydrodearylation reactor and adapted to receive the third product stream and to produce a benzene-containing stream, a toluene-containing stream, a C-rich stream, and a bottoms C stream.'}2. The system of claim 1 , further comprising:{'sub': '9+', 'a transalkylation unit fluidly coupled to the second separator and adapted to receive the first product stream and one or more of the benzene-containing stream, the toluene-containing stream, and the bottoms C stream, and to produce alkyl mono-aromatic compounds.'}3. The system of claim 1 , further comprising:{'sub': '8', 'a para-xylene unit fluidly coupled to the second separator and adapted to receive the C-rich stream and to produce a para-xylene-rich stream ...

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Номер записи: 36
12-02-2015 дата публикации

PROCESS FOR PROMOTING DISPROPORTIONATION REACTIONS AND RING OPENING REACTIONS WITHIN AN ISOMERIZATION ZONE

Номер: US20150045602A1
Автор: Funk Gregory, Lapinski Mark P.
Принадлежит:

A process for increasing disproportionation and ring opening reactions an isomerization zone which converts iso-paraffins to normal paraffins. In order to promote these reactions, the amount of Ccyclic hydrocarbons entering the isomerization zone is reduced. Disproportionation reaction selectivity is observed which produces valuable Chydrocarbons and Chydrocarbons. Also, a higher ring opening conversion of Ccyclic hydrocarbons is observed. Conversion of iChydrocarbons, iChydrocarbons, and iChydrocarbons may occur in the same isomerization zone. 1. A process for increasing a conversion of iChydrocarbons and iChydrocarbons from a naphtha stream , the process comprising:{'sub': '5', 'isomerizing iChydrocarbons to normal pentane, under isomerization conditions in the presence of a catalyst, in an isomerization zone;'}{'sub': '6', 'simultaneously isomerizing iChydrocarbons to normal hexane, under isomerization conditions in the presence of a catalyst, in the isomerization zone; and,'}{'sub': '6', 'promoting disproportionation reactions within the isomerization zone by reducing an amount of C+ cyclic hydrocarbons entering into the isomerization zone.'}2. The process of wherein the disproportionation reactions produce at least one of: Chydrocarbons; Chydrocarbons; and claim 1 , Chydrocarbons.3. The process of wherein at least a portion of the Chydrocarbons claim 2 , Chydrocarbons claim 2 , or both are non-normal paraffins.4. The process of further comprising:{'sub': 4', '7, 'isomerizing a portion of the non-normal paraffins portion of the Chydrocarbons and Chydrocarbons to normal paraffins in the isomerization zone.'}5. The process of further comprising:{'sub': 5', '6, 'promoting a ring opening of Ccyclic hydrocarbons in the isomerization zone by reducing an amount of Ccyclic hydrocarbons entering into the isomerization zone.'}6. The process of wherein a conversion of iChydrocarbons is greater in the isomerization zone with the reduced amount of Ccyclic hydrocarbons than a ...

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Номер записи: 37
18-02-2021 дата публикации

Process for Transalkylation of Aromatic Fluids

Номер: US20210047249A1
Автор: Abichandani Jeevan S., Chen Tan-Jen, Ide Matthew S., Lai Wenyih F., Loveless Brett T.
Принадлежит:

Systems and methods are provided for an improved transalkylation process that better tolerates the presence of Caromatics and may be conducted substantially in the liquid phase. The transalkylation feedstock may comprise alkyl-substituted benzenes and naphthalene and the transalkylation effluent comprises alkyl-substituted naphthalene and benzene, toluene, and/or xylenes. 1. A method for liquid phase transalkylation of aromatic compounds , comprising:exposing an aromatic feedstock comprising at least about 1.0 wt % naphthalene and alkyl-substituted benzene to a transalkylation catalyst under effective transalkylation conditions to form a transalkylation effluent comprising an alkyl-substituted naphthalene and benzene;wherein a mole fraction of aromatic compounds in the liquid phase, relative to the total amount of aromatic compounds in the feedstock, is at least about 0.01 under the effective transalkylation conditions; and a first molecular sieve having an MWW framework with an n value of about 2 to about 50;', 'a second molecular sieve corresponding to a Beta polymorph with an n value of about 10 to about 60; and', 'a third molecular sieve having a FAU framework with an n value of about 2 to about 400;', {'sub': 2', '2', '3, 'where n is a molar ratio YOover XOin the framework of the first, second, and third molecular sieves, X is a trivalent element, and Y is a tetravalent element.'}], 'wherein the transalkylation catalyst comprises at least one of the following2. The method of claim 1 , wherein the transalkylation catalyst further comprises 0.01 wt % to 5 wt % of a metal from Groups 5-11 and 14 supported on the transalkylation catalyst.3. The method of claim 2 , wherein the metal from Groups 5-11 and 14 is selected from the group consisting of Pd claim 2 , Pt claim 2 , Ni claim 2 , Rh claim 2 , Sn claim 2 , or a combination thereof.4. The method of claim 1 , wherein the MWW framework of the first molecular sieve is selected from the group consisting of MCM-22 ...

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Номер записи: 38
03-03-2022 дата публикации

COUPLING OF UNIT FOR EXTRACTING METHYL-SUBSTITUTED AROMATICS WITH UNIT FOR HYDROGENOLYSING ALKYL-AROMATICS

Номер: US20220064086A1
Автор: COUPARD Vincent, PAGOT Alexandre, VINCENT-GENOD Vanessa
Принадлежит: IFP ENERGIES NOUVELLES

The present invention relates to a device and a process for converting aromatic compounds, wherein: methyl-substituted aromatic compounds are extracted from a hydrocarbon feedstock () comprising aromatic compounds having at least 8 carbon atoms in an extraction unit (), to produce at least one effluent enriched in methyl-substituted aromatic compounds (A, B) and an effluent depleted in methyl-substituted aromatic compounds (); and C2+ alkyl chains of the aromatic compounds of the depleted effluent () are converted into methyl groups in a hydrogenolysis unit () placed downstream of the extraction unit (), to produce a hydrogenolysis effluent enriched in methyl-substituted aromatic compounds ().

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Номер записи: 39
13-02-2020 дата публикации

PROCESS FOR THE PRODUCTION OF HIGH PURITY PARA-XYLENE AND HIGH PURITY TOLUENE

Номер: US20200048167A1
Автор: Corradi Jason T., Miller Ryan D.
Принадлежит:

A process for the production of high purity toluene and para-xylene is described. More specifically, the process involves the production of high purity toluene produced via a light-desorbent selective adsorption process for para-xylene production, such as light desorbent para-xylene extraction, without the need for dedicated solvent extraction or olefin removal from the toluene stream. 1. A process for producing high purity toluene and para-xylene in a para-xylene complex comprising:separating an extract stream comprising para-xylene and toluene from an adsorbent chamber into an overhead stream comprising C6− compounds and a bottoms stream comprising para-xylene and toluene in a first para-xylene fractionation column;separating the bottoms stream from the first para-xylene fractionation column in a second para-xylene fractionation column into a sidedraw stream comprising high purity para-xylene, an overhead stream comprising toluene, and a bottoms stream comprising C9+ aromatics;recovering the sidedraw stream as a high purity para-xylene stream; andrecovering at least a portion of the overhead stream from the second para-xylene fractionation column as a high purity toluene product stream.2. The process of wherein the overhead stream from the second para-xylene fractionation column comprises high purity toluene.3. The process of further comprising;separating the overhead stream from the second para-xylene fractionation column in a toluene fractionation column into an overhead stream comprising high purity toluene and a bottom stream comprising xylenes, and wherein the high purity toluene product stream comprises the overhead stream from the toluene fractionation column.4. The process of further comprising:introducing a mixed xylenes stream and a toluene stream into the adsorption chamber comprising a para-xylene selective adsorbent; andseparating the mixed xylenes stream and the toluene stream into the extract stream and a stream comprising ortho-xylene, meta-xylene, ...

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Номер записи: 40
23-02-2017 дата публикации

Energy Efficient Fractionation Process for Separating the Reactor Effluent from TOL/A9+ Transalkylation Processes

Номер: US20170050901A1
Автор: Jeffrey AMELSE
Принадлежит: BP Corp North America Inc

Processes and apparatus are disclosed for the energy efficient separation of the effluent from a TOL/A9+ transalkylation reactor. The apparatus includes a reboiled prefractionation column and a sidedraw tower that produces: 1) an overhead stream including unreacted toluene, 2) a stream including unreacted C9+ aromatics, a portion of which stream may be recycled to the reactor; and 3) a sidedraw stream including C8 aromatics that may be directed to a crystallization or selective adsorption paraxylene separation unit for recovery o a paraxylene product.

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Номер записи: 41
22-02-2018 дата публикации

Transalkylated Cyclohexylbenzyl and Biphenyl Compounds

Номер: US20180050971A1
Автор: Chen Tan-Jen, de Smit Emiel, Kheir Ali A., Pavlish Aaron B., Salciccioli Michael, Sangar Neeraj
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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Номер записи: 42
10-03-2022 дата публикации

Product By Integrated Process for Producing Propylene Polymers and Copolymers with Reduced Greenhouse Gas Emission

Номер: US20220073655A1
Автор: Fowler James Nicholas, Lawrence Deborah, McHaney Stephen Craig
Принадлежит:

A product made by a substantially zero-carbon-emission (ZCE) process for making propylene polymers and copolymers including: converting alkanes to the olefin monomers ethylene, propylene, and butene or combinations thereof, using renewable electric power and scrubbing the stack gases from any fired heaters or boilers to remove carbon dioxide, in an oxidative-coupling of methane plant including the steps of passing alkanes through an ethylene plant while adding oxygen, passing a portion of the polymerization grade ethylene through a 2-butene plant, and passing the 2-butene stream and a portion of the polymerization grade ethylene stream through a propylene plant. The polymerization grade propylene is polymerized to produce isotactic homopolymer polypropylene, or ethylene-propylene random copolymer, or impact-grade polypropylene containing ethylene-propylene rubber. 1. A product comprising isotactic polypropylene homopolymers or copolymers produced by a substantially zero carbon dioxide emissions process comprising: i. providing an ethylene plant comprising an oxidation reactor and a first fractionation train and converting natural gas and oxygen in the oxidation reactor to produce an oxidation reactor effluent comprising ethylene and passing the oxidation reactor effluent to the first fractionation train to recover a first ethylene stream, a second ethylene stream, and a third ethylene stream;', 'ii. providing a 2-butene plant comprising a dimerization unit and a second fractionation train and converting a portion of the first ethylene stream in the dimerization unit to produce a dimerization unit effluent comprising 2-butene and passing the dimerization unit effluent to the second fractionation train to produce a 2-butene stream;', 'iii. providing a propylene plant comprising a metathesis reactor and a third fractionation train and converting the 2-butene stream and a portion of the second ethylene stream in the metathesis reactor to produce a metathesis reactor ...

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Номер записи: 43
01-03-2018 дата публикации

PROCESSES AND COMPOSITIONS FOR TOLUENE METHYLATION IN AN AROMATICS COMPLEX

Номер: US20180057420A1
Автор: AITANI Abdullah Mohammed, Al-Khattaf Sulaiman Saleh, ARUDRA Palani, Fayad Elie Jean, Fazal Atif, JAHEL Ali, Negiz Antoine
Принадлежит:

This present disclosure relates to processes and compositions for toluene methylation in an aromatics complex for producing paraxylene. More specifically, the present disclosure relates to a process for producing paraxylene which includes alkylating a toluene stream and a methanol stream in a toluene methylation zone operating under toluene methylation conditions in the presence of a catalyst comprising a MFI crystal to produce a toluene methylation product stream. 1. A process for producing paraxylene comprising alkylating a toluene stream and a methanol stream in a toluene methylation zone operating under toluene methylation conditions in the presence of a catalyst comprising an MFI crystal , alone or bound to any another material , to produce a toluene methylation product stream.2. The process according to claim 1 , wherein the catalyst includes MFI crystals with a framework silica to alumina ratio of about 50 to about 10 claim 1 ,000 claim 1 , more preferably about 100 to about 6 claim 1 ,000 claim 1 , or even more preferably about 500 to about 3 claim 1 ,000.3. The process according to claim 1 , wherein the toluene methylation conditions include a temperature of about 250° C. to about 750° C. claim 1 , more preferably between about 350° C. and about 650° C. claim 1 , even more preferably between about 400° C. and about 600° C.4. The process according to claim 1 , wherein the toluene methylation conditions include a pressure of about 1 Barg to about 100 Barg claim 1 , more preferably between about 1 Barg to about 50 Barg claim 1 , even more preferably between 2 Barg to about 30 Barg.5. The process according to claim 1 , wherein the toluene methylation product stream has a benzene to total xylene molar ratio of less than 1 claim 1 , or preferably less than 0.5 claim 1 , or more preferably less than 0.16. The process according to claim 2 , wherein the catalyst includes MFI crystals with a framework silica to alumina ratio of 2000.7. The process according to claim ...

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Номер записи: 44
15-05-2014 дата публикации

Alkylated Aromatics Production

Номер: US20140135548A1
Автор: Brian Maerz, Maruti Bhandarkar, Matthew J. Vincent, Terry E. Helton, Vijay Nanda
Принадлежит: ExxonMobil Chemical Patents Inc, Technip Process Technology Inc

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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Номер записи: 45
28-02-2019 дата публикации

PROCESS FOR XYLENE PRODUCTION WITH ENERGY OPTIMIZATION

Номер: US20190062241A1
Автор: ABUDAWOUD RAED, JAZZAR Ahmad A., XU QI, Zhang Zhonglin
Принадлежит: Saudi Arabian Oil Company

A method for producing xylenes from a heavy reformate feed includes the steps of introducing the heavy reformate feed and a hydrogen feed to a dealkylation reactor, reacting the heavy reformate feed with the hydrogen gas in the presence of the dealkylation catalyst in the dealkylation reactor to produce a dealkylation effluent, introducing the dealkylation effluent to a splitter unit, separating the dealkylation effluent into a light gas stream, a toluene stream, a benzene stream, a C9 aromatics stream, a C10+ aromatics stream, and a mixed xylene stream in the splitter unit, introducing the toluene stream, the C9 aromatics stream, and a hydrogen stream into a transalkylation reactor, reacting the toluene stream and the C9 aromatics stream in the presence of the transalkylation catalyst to produce a transalkylation effluent, introducing the transalkylation effluent to the splitter unit, and separating the transalkylation effluent in the splitter unit. 1. A method for producing mixed xylenes from a heavy reformate feed , the method comprising the steps of:introducing the heavy reformate feed to a feed exchanger to produce a hot feed stream, wherein the feed exchanger increases the temperature of the heavy reformate feed, wherein the heavy reformate comprises aromatic hydrocarbons with nine or more carbon atoms (C9+ aromatics), wherein the hydrogen feed comprises hydrogen gas;mixing the hot feed stream and a hydrogen feed to produce a mixed feed;increasing a temperature of the mixed feed in a feed-effluent exchanger to produce a hot mixed feed, wherein a temperature of the hot mixed feed is between 324 deg C. and 344 deg C.;increasing the temperature of the hot mixed feed in a feed fired heater to produce a hot reactor feed, wherein a temperature of the hot reactor feed is between 380 deg C. and 400 deg C.;introducing the hot reactor feed to a dealkylation reactor, wherein the dealkylation reactor comprises a dealkylation catalyst;reacting the heavy reformate feed with ...

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Номер записи: 46
17-03-2022 дата публикации

PROCESS FOR MAKING PHENOL AND XYLENES

Номер: US20220081382A1
Автор: Zhang Shuguang, Zhou Lubo
Принадлежит:

Processes for making phenol and xylenes from a phenols-containing feed are described. The processes involve transalkylation of alkylphenols to form phenol and alkylbenzenes. The phenol is separated from the alkylbenzenes, and the alkylbenzenes may be separated into benzene, toluene, xylenes, and heavy alkylbenzene streams. The benzene stream may be recycled to the transalkylation reaction zone. The toluene may be sent to a disproportionation reaction zone, and the product is sent back to the aromatic separation zone. The toluene can also be recycled to the transalkylation zone. The xylenes are separated into a p-xylene stream and a mixed xylene stream comprising m-xylene and o-xylene. The mixed xylene stream is isomerized and the isomerized product is sent back to the aromatic separation zone. The heavy alkylbenzenes are dealkylated and separated, with the aromatic stream being recycled to the aromatic separation zone. 1. A process for producing one or more of phenol , and xylenes comprising:introducing a phenols containing feed stream into a feed separation zone;separating the phenols containing feed stream in the feed separation zone into at least a phenol stream comprising phenol, and an alkylphenol stream comprising alkylphenols;transalkylating the alkylphenol stream and a reactant stream comprising one or more of benzene or toluene in a transalkylation reaction zone under transalkylation reaction conditions to produce a transalkylation effluent stream comprising phenols, and alkylbenzenes;separating the transalkylation effluent stream in a phenol separation zone into a phenol recycle stream comprising phenols, and an aromatic stream comprising benzene, toluene, xylenes, and heavy alkylbenzenes;separating the aromatic stream in an aromatic separation zone into at least a recycle stream comprising one or more of benzene or toluene, a heavy alkylbenzene stream comprising heavy alkylbenzenes, and a mixed xylene stream comprising mixed xylenes;separating the mixed ...

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Номер записи: 47
28-02-2019 дата публикации

PROCESSES FOR REFORMING AND TRANSALKYLATING HYDROCARBONS

Номер: US20190062644A1
Автор: Bambal Ashish S., Cheng Linda S., Montalbano Joseph A.
Принадлежит:

Processes for reforming and transalkylating hydrocarbons are disclosed. A method for processing a hydrocarbon stream includes the steps of separating para-xylene from a first mixed-xylene and ethylbenzene-containing stream to produce a first non-equilibrium xylene and ethylbenzene stream and isomerizing the first non-equilibrium xylene and ethylbenzene stream to produce additional para-xylene. The method further includes transalkylating a toluene stream to produce a second mixed-xylene and ethylbenzene-containing stream, separating para-xylene from the second mixed-xylene and ethylbenzene-containing stream to produce a second non-equilibrium xylene and ethylbenzene stream, and isomerizing the second non-equilibrium xylene and ethylbenzene stream using a liquid phase isomerization process to produce additional para-xylene. 1. A process for processing a hydrocarbon stream comprising the steps of:separating para-xylene from the first mixed-xylene and ethylbenzene-containing stream to produce a first non-equilibrium xylene and ethylbenzene stream;isomerizing the first non-equilibrium xylene and ethylbenzene stream to produce additional para-xylene;transalkylating a toluene stream to produce a second mixed-xylene and ethylbenzene-containing stream;separating para-xylene from the second mixed-xylene and ethylbenzene-containing stream to produce a second non-equilibrium xylene and ethylbenzene stream; andisomerizing the second non-equilibrium xylene and ethylbenzene stream using a liquid phase isomerization process to produce additional para-xylene.2. The process of claim 1 , wherein the first mixed-xylene and ethylbenzene-containing stream comprises a greater proportion of ethylbenzene than does the second mixed-xylene and ethylbenzene-containing stream.3. The process of claim 1 , further comprising reforming a naphtha-containing hydrocarbon stream to produce the first mixed-xylene and ethylbenzene-containing stream and the toluene stream.4. The process of claim 3 , ...

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Номер записи: 48
17-03-2016 дата публикации

In-situ Trim Coke Selectivation of Toluene Disproportionation Catalyst

Номер: US20160074845A1
Автор: Detjen Todd E., Tinger Robert G., Zheng Xiaobo
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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Номер записи: 49
17-03-2016 дата публикации

Transalkylation System

Номер: US20160075618A1
Автор: Robert G. TINGER, Timothy P. Bender, Todd E. DETJEN, Xiaobo Zheng
Принадлежит: ExxonMobil Chemical Patents Inc

The invention relates to a transalkylation system to convert feedstreams containing benzene and/or toluene (C7− aromatic hydrocarbons) and feedstreams containing C9+ aromatic hydrocarbons into a product stream comprising xylenes.

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Номер записи: 50
18-03-2021 дата публикации

SYSTEM FOR CONVERSION OF CRUDE OIL TO PETROCHEMICALS AND FUEL PRODUCTS INTEGRATING VACUUM GAS OIL HYDROTREATING AND STEAM CRACKING

Номер: US20210079305A1
Автор: AL-GHAMDI Mohammed Saeed
Принадлежит:

Process scheme configurations are disclosed that enable conversion of crude oil feeds with several processing units in an integrated manner into petrochemicals. The designs utilize minimum capital expenditures to prepare suitable feedstocks for the steam cracker complex. The integrated process for converting crude oil to petrochemical products including olefins and aromatics, and fuel products, includes mixed feed steam cracking and gas oil steam cracking. Feeds to the mixed feed steam cracker include light products and naphtha from hydroprocessing zones within the battery limits, recycle streams from the C3 and C4 olefins recovery steps, and raffinate from a pyrolysis gasoline aromatics extraction zone within the battery limits. Feeds to the gas oil steam cracker include hydrotreated gas oil range intermediates from vacuum gas oil hydrotreating. 121.-. (canceled)22. An integrated system for producing petrochemicals and fuel products comprising:an atmospheric distillation unit (ADU) operable to receive and separate a feed, and discharge a first ADU fraction comprising naphtha, a second ADU fraction comprising at least a portion of middle distillates from the feed, and a third ADU fraction comprising atmospheric residue;a vacuum distillation unit (VDU) operable to receive and separate the third ADU fraction, and discharge a first VDU fraction comprising vacuum gas oil;a distillate hydroprocessing (DHP) zone operable to receive and convert middle distillates from the second ADU fraction into a first DHP fraction and a second DHP fraction, wherein the first DHP fraction comprises naphtha and the second DHP fraction is used for diesel fuel production;a gas oil hydrotreating (GOHT) zone operable to receive and treat vacuum gas oil from the first VDU fraction and produce a first GOHT fraction containing naphtha range components, and a hydrotreated gas oil fraction;a steam cracking zone comprising (a) a mixed feed steam cracking (MFSC) zone operable to receive and ...

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Номер записи: 51
22-03-2018 дата публикации

PROCESS FOR INCREASING XYLENE ISOMER TO BENZENE RATIO

Номер: US20180079701A1
Автор: Gattupalli Rajeswar R., Rashid Naiyl A., Shakur Mohamed S. M.
Принадлежит:

Apparatuses and processes are provided for regulating C7 and C8 feed to an aromatics complex to increase the ratio of a selected xylene isomer to benzene ratio. Reformate may be split into three cuts in a splitter column. A side cut stream comprises predominantly C7 hydrocarbons and a bottoms steam from the splitter column comprises predominantly C8+ hydrocarbons. The relative proportion of the C7 and C8+ hydrocarbon streams sent to the aromatics complex are metered to determine the resulting ratio of a selected xylene isomer to benzene produced by the aromatics complex. 1. A process for preparing a feed for an aromatics complex comprising:fractionating a naphtha stream to provide a C7 stream and a C8+ aromatics stream;feeding a first C7 stream taken from the C7 stream to the aromatics complex;feeding a first C8+ aromatics stream taken from the C8+ aromatics stream to the aromatics complex; andfeeding a second C7 stream taken from the C7 stream away from the aromatics complex; orfeeding a second C8+ aromatics stream taken from the C8+ aromatics stream away from the aromatics complex.2. The process of comprising feeding the first C7 stream taken from the C7 stream to an aromatics extraction unit in the aromatics complex to extract a C7 raffinate stream from a toluene stream.3. The process of comprising feeding the C7 raffinate stream to a gasoline pool.4. The process of comprising calculating a selected xylene isomer to benzene ratio and changing a flow rate of the second C7 stream and/or the second C8+ aromatics stream in response to the calculated selected xylene isomer to benzene ratio.5. The process of comprising fractionating said C8+ aromatics stream to provide said first stream of the C8+ aromatics stream comprising C8 aromatics and said second stream of the C8+ aromatics stream comprising C9 aromatics.6. The process of comprising fractionating the toluene stream to separate a benzene stream from a concentrated toluene stream.7. The process of comprising ...

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Номер записи: 52
12-03-2020 дата публикации

CATALYST COMPOSITION

Номер: US20200078777A1
Автор: LI Hong-Xin, MAUER Richard Berend, SABATER PUJADAS Gisela
Принадлежит:

A catalyst composition comprising (a) carrier comprising (i) 5 to 95 wt % mordenite type zeolite having a mean crystallite length parallel to the direction of the 12-ring channels of 60 nm or less and a mesopore volume of at least 0.10 cc/gram, (ii) 5 to 95 wt % ZSM-5 type zeolite; and (iii) 10 to 60 wt % inorganic binder; and (b) 0.001 to 10 wt % of one or more catalytically active metals, wherein the inorganic binder comprises titania, its preparation and its use in alkylaromatic conversion. 1. A catalyst composition comprising(a) a carrier comprising (i) mordenite type zeolite having a mean crystallite length parallel to the direction of the 12-ring channels of 60 nm or less and a mesopore volume of at least 0.10 cc/gram in an amount in the range of from 5 to 95 wt %, based on total weight of carrier, (ii) ZSM-5 type zeolite in an amount of from 5 to 95 wt %, based on total weight of carrier; and (iii) an inorganic binder in an amount in the range of from 10 to 60 wt %, based on total weight of carrier; and(b) of from 0.001 to 10 wt % of one or more catalytically active metals, wherein the inorganic binder comprises titania.2. The catalyst composition according to claim 1 , in which the carrier comprises mordenite type zeolite in an amount in the range of from 20 to 90 wt % claim 1 , based on total weight of carrier.3. The catalyst composition according to claim 1 , in which the carrier comprises ZSM-5 type zeolite in an amount of from 10 to 70 wt % claim 1 , based on total weight of carrier.4. The catalyst composition according to claim 1 , wherein the ZSM-5 type zeolite has a silica to alumina molar ratio in the range of from 15 to 40.5. The catalyst composition according to claim 1 , wherein the ZSM-5 type zeolite has a number average crystal size in the range of from 25 to 200 nm claim 1 , as determined by X-ray diffraction.6. The catalyst composition according to claim 1 , wherein the ZSM-5 type zeolite has a number average.7. A crystal size in the range of ...

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Номер записи: 53
31-03-2022 дата публикации

Production of aromatics by reverse water gas shift, fermentation and recycling to pyrolysis.

Номер: US20220098624A1
Автор: Frederic Feugnet, Jean-Francois Joly
Принадлежит: IFP Energies Nouvelles IFPEN

Device and process for the conversion of a feedstock of aromatic compounds, in which the feedstock is treated notably by means of a fractionation train (4-7), a xylene separation unit (10) and an isomerization unit (11), and in which a pyrolysis unit (13) treats a second hydrocarbon feedstock, produces a pyrolysis effluent feeding the feedstock, and produces a pyrolysis gas comprising CO, CO2 and H2; a reverse water gas shift RWGS reaction section (50) treats the pyrolysis gas and produces an RWGS gas enriched in CO and in water; a fermentation reaction section (52) treats the RWGS gas enriched in CO and in water, to produce ethanol and recycle the ethanol to the inlet of the pyrolysis unit.

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Номер записи: 54
21-03-2019 дата публикации

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

Номер: US20190083962A1
Автор: BOAL BEN W., Davis Mark E., Kang Jong Hun, SCHMIDT JOEL E.
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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Номер записи: 55
16-04-2015 дата публикации

PROCESSES USING MOLECULAR SIEVE SSZ-96

Номер: US20150104364A1
Автор: Elomari Saleh Ali
Принадлежит: Chevron U.S.A. INC.

The present disclosure is directed to processes using a new crystalline molecular sieve designated SSZ-96, which is synthesized using a 1-butyl-1-methyl-octahydroindolium cation as a structure directing agent. 2. The process of claim 1 , wherein the molecular sieve has a mole ratio of at least 10 of (1) silicon oxide to (2) and oxide selected from boron oxide claim 1 , aluminum oxide claim 1 , gallium oxide claim 1 , indium oxide claim 1 , and mixtures thereof.4. The process of claim 3 , wherein T is selected from the group consisting of Si claim 3 , Ge claim 3 , and mixtures thereof.5. The process of claim 4 , wherein T is Si.6. The process of claim 3 , wherein X is selected from the group consisting of B claim 3 , Al claim 3 , Ga claim 3 , In claim 3 , and mixtures thereof.7. The process of claim 3 , wherein T is Si and X is Al.8. The process of claim 1 , wherein the process is a process selected from the group consisting of hydrocracking claim 1 , dewaxing claim 1 , catalytic cracking claim 1 , aromatics formation claim 1 , isomerization claim 1 , alkylation and transalkylation claim 1 , conversion of paraffins to aromatics claim 1 , isomerization of olefins claim 1 , xylene isomerization claim 1 , oligomerization claim 1 , condensation of alcohols claim 1 , methane upgrading and polymerization of 1-olefins.9. The process of claim 8 , wherein the process is a dewaxing process comprising contacting the catalyst with a hydrocarbon feedstock under dewaxing conditions.10. The process of claim 1 , wherein the process is a process for producing a C lube oil from a C olefin feed comprising isomerizing the olefin feed under isomerization conditions over the catalyst. The present disclosure relates to processes using a new molecular sieve designated SSZ-96, wherein the molecular sieve is synthesized using a 1-butyl-1-methyl-octahydroindolium cation as a structure directing agent (“SDA”).Because of their unique sieving characteristics, as well as their catalytic properties ...

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Номер записи: 56
04-05-2017 дата публикации

PROCESS FOR PRODUCING BENZENE FROM C5-C12 HYDROCARBON MIXTURE

Номер: US20170121239A1
Автор: Farrokhpanah Sonia, FICKEL Dustin, Hall Stephen, Prashant Kumar, Van Iersel Maikel
Принадлежит:

The present invention relates to a process for producing benzene comprising the steps of: a) separating a source feedstream comprising C5-C12 hydrocarbons including benzene and alkylbenzenes into a first feedstream comprising a higher proportion of benzene than the source feedstream and a second feedstream comprising a lower proportion of benzene than the source feedstream and subsequently, b) contacting the first feedstream in the presence of hydrogen with a first hydrocracking catalyst comprising 0.01-1 wt-% hydrogenation metal in relation to the total catalyst weight and a zeolite having a pore size of 5-8 Å and a silica (SiO2) to alumina (Al2O3) molar ratio of 5-200 under first process conditions to produce a first product stream comprising benzene, wherein the first process conditions include a temperature of 425-580° C., a pressure of 300-5000 kPa gauge and a Weight Hourly Space Velocity of 0.1-15 h, and c) contacting the second feedstream with hydrogen under second process conditions to produce a second product stream comprising benzene, wherein i) the second process conditions are suitable for hydrocracking and step (c) involves contacting the second feedstream in the presence of hydrogen with a second hydrocracking catalyst comprising 0.01-1 wt-% hydrogenation metal in relation to the total catalyst weight and a zeolite having a pore size of 5-8 Å and a silica (SiO2) to alumina (Al2O3) molar ratio of 5-200 under the second process conditions which include a temperature of 300-600° C., a pressure of 300-5000 kPa gauge and a Weight Hourly space Velocity of 0.1-15 h, ii) the second process conditions are suitable for toluene disproportionation and involve contracting the second feedstream with a toluene disproportionation catalyst, or iii) the second process conditions are suitable for hydrodealkylation. 1. A process for producing benzene comprising the steps of:(a) separating a source feedstream comprising C5-C12 hydrocarbons including benzene and ...

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Номер записи: 57
11-05-2017 дата публикации

Scm-11 molecular sieve, process for producing same and use thereof

Номер: US20170128918A1
Автор: Bin Zhang, Hongmin Sun, Weimin Yang, YI LUO, Zhendong Wang
Принадлежит: China Petroleum and Chemical Corp, Sinopec Shanghai Research Institute of Petrochemical Technology

The present invention relates to an SCM-11 molecular sieve, a process for producing same and use thereof. The molecular sieve has an empirical chemical composition as illustrated by the formula “the first oxide·the second oxide”, wherein the ratio by molar of the first oxide to the second oxide is more than 2, the first oxide is silica, the second oxide is at least one selected from the group consisting of germanium dioxide, alumina, boron oxide, iron oxide, gallium oxide, titanium oxide, rare earth oxides, indium oxide and vanadium oxide. The molecular sieve has specific XRD pattern, and can be used as an adsorbent or a catalyst for converting an organic compound.

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Номер записи: 58
03-06-2021 дата публикации

Transalkylation with Reduced Ring Loss

Номер: US20210163379A1
Автор: Andrews Jeffrey L., Molinier Michel, Podsiadlo Paul
Принадлежит:

A transalkylation process co-feeds benzene at a relatively high proportion with C9+ aromatics in a feed stream to a transalkylation reactor. At lower proportions (≤5 wt %) of benzene, ring loss is greater for benzene than toluene and ring loss is increased by increasing the proportion of benzene in the feed stream. When the benzene is co-fed in a proportion sufficiently greater than 5 weight percent of the feed stream, ring loss is unexpectedly reduced. 1. A transalkylation process comprising:(a) supplying a molecular hydrogen stream and a feed stream, the feed stream comprising C9+ heavy aromatics and optionally further comprising toluene, to a transalkylation reactor comprising therein a catalyst comprising a zeolite and at least one metal, to produce C8 aromatics; and(b) co-feeding benzene in the feed stream in a proportion of the feed stream sufficiently high to reduce ring loss relative to a reference stream at same transalkylation conditions of pressure, WHSV, inlet temperature, and molecular hydrogen to hydrocarbon molar ratio, where benzene in the feed stream is replaced with an equal weight of toluene in the reference stream.2. A transalkylation process comprising:(a) supplying a molecular hydrogen stream and a feed stream, the feed stream comprising C9+ heavy aromatics and optionally further comprising toluene, to a transalkylation reactor comprising therein a catalyst comprising a zeolite and at least one metal, to produce C8 aromatics; and(b) co-feeding benzene in the feed stream, wherein a proportion of co-fed benzene in the feed stream is not less than 10 weight percent of the total weight of aromatics in the feed stream.3. The transalkylation process of claim 1 , wherein a proportion of co-fed benzene in the feed stream is in a range from 10 to 50 weight percent of the total weight of aromatics in the feed stream.4. The transalkylation process of claim 1 , wherein the feed stream comprises a weight ratio of benzene to toluene of at least 1:1 claim 1 , ...

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Номер записи: 59
09-05-2019 дата публикации

TREATING C8- C10 AROMATIC FEED STREAMS TO PREPARE AND RECOVER TRIMETHYLATED BENZENES

Номер: US20190135716A1
Автор: "DAcosta Chris", Hoch Robert, Miller Jeffery
Принадлежит:

Methods are provided for the treatment of a feed stream containing C9 aromatic components to produce mesitylene-containing products. The methods include hydrodealkylating the feed stream to remove C2 and higher alkyl groups from the aromatic components and transalkylating the feed stream to rearrange the distribution of methyl groups among the aromatic components. Disclosed methods also include the treatment of a hydrocarbon feedstock by hydrodealkylation and/or transalkylation in order to produce a hydrocarbon product having an increased mass percentage of mesitylene. 1. A method for the production of mesitylene from an aromatic composition comprising aromatic components including methyl benzenes and Cand/or higher alkyl benzenes , comprising:{'sub': '2', 'a. hydrodealkylating the aromatic components to convert the Cand/or higher alkyl benzenes to the corresponding alkanes and dealkylated aromatics while retaining the methyl benzenes;'}b. transalkylating the methyl benzenes to redistribute the methyl groups among the methyl benzenes to form trimethylbenzenes and other methylated benzenes;c. isomerizing the trimethylbenzenes to increase the amount of mesitylene in the aromatic composition; andd. recovering a TMB-rich product from the aromatic composition.2. The method of in which said recovering a TMB-rich product is by distillation.3. The method of in which said hydrodealkylating is performed in the presence of a suitable hydrodealkylating catalyst claim 1 , and the transalkylating is performed in the presence of a suitable transalkylating catalyst.4. The method of and which further includes combining elemental hydrogen with the feed stream for hydrodealkylating.5. The method of which further includes combining one or more of nitrogen claim 4 , methane claim 4 , ethane and propane with the feed stream for hydrodealkylating.6. The method of which includes removing elemental hydrogen claim 1 , methane claim 1 , ethane and propane from the dealkylated product and ...

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Номер записи: 60
10-06-2021 дата публикации

Liquid Phase Transalkylation Process

Номер: US20210171422A1
Автор: "ONeil Brandon J", Chen Tan-Jen, Cheng Jane C., Deetjen Todd E, Lacy Darryl D, Seigel Scott J
Принадлежит:

Methods and corresponding catalysts are provided for transalkylation of 1-ring (C) aromatic compounds, such as transalkylation to form para-xylene and/or other xylenes. Suitable catalysts include molecular sieves having a 3-D 12-member ring framework structure, molecular sieves having a 1-D 12-member ring framework structure, acidic microporous materials with a pore channel size of at least 6.0 Angstroms, and/or molecular sieves having a MWW framework structure. The methods include performing transalkylation where at least a portion of the feed to the transalkylation process is in the liquid phase. Optionally, the transalkylation conditions can correspond to conditions where a continuous liquid phase is present within the reaction environment. Some embodiments include liquid phase transalkylation processes for naphthalene-containing feedstock streams. 1. A method for liquid phase transalkylation of aromatic compounds , comprising:{'sub': '9+', 'exposing an aromatic feedstock comprising C aromatics and at least one of benzene and toluene to a transalkylation catalyst under effective transalkylation conditions to form a transalkylation effluent;'}wherein the mole fraction of aromatic compounds in the liquid phase in the feedstock, relative to the total amount of aromatic compounds in the feedstock, is at least about 0.01 under the effective transalkylation conditions;{'sub': '8', 'wherein the transalkylation effluent has a higher weight percentage of Caromatics than the feedstock; and'} a molecular sieve with a 3-dimensional 12-member ring or larger pore network;', 'a molecular sieve with a 1-dimensional 12-member ring or larger pore network, wherein the 1-dimensional channel has a pore channel size of at least 6.0 Angstroms;', 'an acidic microporous material with a pore channel size of at least 6.0 Angstroms; and', 'a molecular sieve having a MWW framework., 'wherein the catalyst comprises at least one of the following2. The method of claim 1 , wherein the molecular ...

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Номер записи: 61
17-06-2021 дата публикации

Catalyst for Converting Alkylaromatic Hydrocarbon and Preparation Method Thereof

Номер: US20210178372A1
Автор: Cheon Young Eun, Lee Ji Hoon, LEE Sang Il
Принадлежит:

Disclosed are a bifunctional catalyst and a preparation method therefor, the bifunctional catalyst being suitable to produce high-value aromatic hydrocarbons by subjecting alkylaromatic hydrocarbons to a disproportionation/transalkylation/dealkylation reaction while suppressing aromatic loss or subjecting C8 aromatic hydrocarbons to an isomerization reaction while suppressing xylene loss. 1. A method for preparing a catalyst for converting aromatic hydrocarbons , the method comprising:a) supporting a precursor of a first metal having hydrogenation activity on a refractory inorganic oxide binder to prepare a first metal precursor-supported binder;b) combining a first zeolite and/or a second zeolite with the first metal precursor-supported binder to prepare a shaped body; andc) calcining the shaped body to form a catalyst, in which the first metal is supported on a mixed support containing the first zeolite and/or the second zeolite and the binder,wherein the first zeolite has a silica-alumina ratio (SAR) of 5 to 300 and a 10-membered ring pore structure, and the second zeolite has a silica-alumina ratio (SAR) of 5 to 300 and a 12-membered ring pore structure with a pore diameter of 6 to 9 Å, andwherein the first metal is selectively supported on the refractory inorganic oxide binder in the mixed support, the amount of the first metal supported being in the range of 0.01 to 5 wt % on the basis of the weight of the mixed support.2. The method of claim 1 , wherein the refractory inorganic oxide is at least one selected from the group consisting of alumina claim 1 , silica claim 1 , aluminum phosphate claim 1 , titania claim 1 , zirconia claim 1 , bentonite claim 1 , kaolin claim 1 , clinoptilolite claim 1 , and montmorillonite.3. The method of claim 1 , wherein the first zeolite is at least one selected from the group consisting of ZSM-5 claim 1 , ZSM-11 claim 1 , ZSM-23 claim 1 , ZSM-48 claim 1 , ZSM-57 claim 1 , EU-2 claim 1 , TNU-9 claim 1 , and MCM-22.4. The method ...

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Номер записи: 62
17-06-2021 дата публикации

APPARATUS AND PROCESS FOR CONVERTING AROMATIC COMPOUNDS BY BENZENE ALKYLATION WITH ETHANOL

Номер: US20210179513A1
Автор: Feugnet Frederic, JOLY Jean-Francois
Принадлежит: IFP ENERGIES NOUVELLES

Apparatus and process for converting aromatic compounds, comprising/using: a fractionating train (-) suitable for extracting at least one benzene-comprising fraction (), one toluene-comprising fraction () and one fraction () comprising xylenes and ethylbenzene from the feedstock (); a xylene separating unit () suitable for treating the fraction comprising xylenes and ethylbenzene and producing a para-xylene-comprising extract () and a raffinate () comprising ortho-xylene, meta-xylene and ethylbenzene; an isomerizing unit () for treating the raffinate and producing a para-xylene-enriched isomerizate (), which is sent to the fractionated train; and an alkylating reaction section () for treating at least part of the benzene-comprising fraction with an ethanol source () and producing an alkylation effluent () comprising ethylbenzene, which is sent to the isomerizing unit. 12. Apparatus for converting a feedstock () of aromatic compounds , comprising:{'b': 4', '7', '22', '23', '24', '2, 'a fractionating train (-) suitable for extracting at least one fraction comprising benzene (), one fraction comprising toluene () and one fraction comprising xylenes and ethylbenzene () from the feedstock ();'}{'b': 10', '24', '39', '40, 'a xylene separating unit () suitable for treating the fraction comprising xylenes and ethylbenzene () and for producing an extract () comprising para-xylene and a raffinate () comprising ortho-xylene, meta-xylene and ethylbenzene;'}{'b': 11', '40', '42', '4', '7, 'an isomerizing unit () suitable for treating the raffinate () and producing a para-xylene-enriched isomerizate (), which is sent to the fractionating train (-); and'}{'b': 13', '22', '30', '31', '11, 'an alkylating reaction section () suitable for treating at least part of the fraction comprising benzene () with an ethanol source () and producing an alkylating effluent () comprising ethylbenzene, which is sent to the isomerizing unit ().'}214313247. Conversion apparatus according to claim 1 , ...

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Номер записи: 63
09-06-2016 дата публикации

DISPROPORTIONATION OF HYDROCARBONS USING SOLID ACID CATALYSTS

Номер: US20160159710A1
Автор: Barger Paul T., Bhattacharyya Alakananda, KALNES TOM N., Smith Stuart, Wier Mary
Принадлежит:

A hydrocarbon disproportionation process is described. The process includes contacting a hydrocarbon feed in a disproportionation reaction zone with a disproportionation catalyst in the presence of hydrogen and an added chloride promoter under disproportionation conditions including to obtain disproportionation products, wherein the disproportionation catalyst comprises a solid catalyst comprising a refractory inorganic oxide having a metal halide dispersed thereon. 1. A hydrocarbon disproportionation process comprising:contacting a hydrocarbon feed in a disproportionation reaction zone with a disproportionation catalyst in the presence of hydrogen and an added chloride promoter under disproportionation conditions to obtain disproportionation products, wherein the disproportionation catalyst comprises a solid catalyst comprising a refractory inorganic oxide having a metal halide dispersed thereon.2. The process of wherein the disproportionation catalyst further comprises a Group VIII metal component dispersed thereon.3. The process of wherein the hydrogen is present in a mole ratio of hydrogen to hydrocarbon feed of greater than 0:1 to about 0.5:1.4. The process of wherein the chloride concentration from the added chloride promoter is in a range of greater than 0 to about 5000 ppm and a mole ratio of hydrogen to chloride from the added chloride promoter is in a range of greater than 0:1 to about 5000:1.5. The process of wherein a selectivity for disproportionation is at least about 25%.6. The process of wherein the hydrocarbon feed comprises alkanes having 4 to 7 carbon atoms.7. The process of wherein the disproportionation conditions include at least one of: a temperature in a range of about 100° C. to about 250° C. claim 1 , a pressure in a range of about 0 MPa (g) to about 13.8 MPa (g) claim 1 , and a liquid hourly space velocity of about 0.25 hrto about 10 hr.8. The process of wherein the added chloride promoter comprises carbon tetrachloride claim 1 , ...

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Номер записи: 64
09-06-2016 дата публикации

Flexible unit for isomerization and disproportionation of hydrocarbons using solid acid catalysts

Номер: US20160159711A1
Автор: Alakananda Bhattacharyya, Mary Wier, Stuart Smith, Tom N. Kalnes
Принадлежит: UOP LLC

A flexible hydrocarbon conversion process utilizing the same reaction zone for isomerization and disproportionation is described. The feed and type of products are selected. The hydrocarbon feed is contacted with a catalyst and in the presence of hydrogen and an added chloride promoter. The catalyst comprises a solid catalyst comprising a refractory inorganic oxide having a metal halide dispersed thereon. The operating conditions are varied depending on whether isomerization or disproportionation is desired.

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Номер записи: 65
07-06-2018 дата публикации

TREATING C8-C10 AROMATIC FEED STREAMS TO PREPARE AND RECOVER TRANSMETHYLATED BENZENES

Номер: US20180155257A1
Автор: "DAcosta Chris", Hoch Robert, Miller Jeffery
Принадлежит: Swift Fuels, LLC

Methods are provided for the treatment of a feed stream containing C9 aromatic components to produce mesitylene-containing products. The methods include hydrodealkylating the feed stream to remove C2 and higher alkyl groups from the aromatic components and transalkylating the feed stream to rearrange the distribution of methyl groups among the aromatic components. Disclosed methods also include the treatment of a hydrocarbon feedstock by hydrodealkylation and/or transalkylation in order to produce a hydrocarbon product having an increased mass percentage of mesitylene. 1. A method for the production of mesitylene from an aromatic composition comprising aromatic components including methyl benzenes and Cand/or higher alkyl benzenes , comprising:{'sub': '2', 'a. hydrodealkylating the aromatic components to convert the Cand/or higher alkyl benzenes to the corresponding alkanes and dealkylated aromatics while retaining the methyl benzenes;'}b. transalkylating the methyl benzenes to redistribute the methyl groups among the methyl benzenes to form trimethylbenzenes and other methylated benzenes;c. isomerizing the trimethylbenzenes to increase the amount of mesitylene in the aromatic composition; andd. recovering a TMB-rich product from the aromatic composition.2. The method of in which said recovering a TMB-rich product is by distillation.3. The method of in which said hydrodealkylating is performed in the presence of a suitable hydrodealkylating catalyst claim 1 , and the transalkylating is performed in the presence of a suitable transalkylating catalyst.4. The method of and which further includes combining elemental hydrogen with the feed stream for hydrodealkylating.5. The method of which further includes combining one or more of nitrogen claim 4 , methane claim 4 , ethane and propane with the feed stream for hydrodealkylating.6. The method of which includes removing elemental hydrogen claim 1 , methane claim 1 , ethane and propane from the dealkylated product and ...

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Номер записи: 66
14-05-2020 дата публикации

METHOD OF HYDROGENOLYSIS FOR IMPROVED PRODUCTION OF PARAXYLENE

Номер: US20200148611A1
Автор: DUBREUIL Anne-Claire, JOLY Jean-Francois, PAGOT Alexandre, Uzio Denis
Принадлежит: IFP ENERGIES NOUVELLES

The invention relates to a selective hydrogenolysis method for treating a feed rich in aromatic compounds having more than 8 carbon atoms, comprising transforming at least one alkyl group with at least two carbon atoms (ethyl, propyl, butyl, isopropyl, etc.) attached to a benzene ring into at least one methyl group. The invention also relates to the integration of the hydrogenolysis unit into an aromatic complex. 1- A selective hydrogenolysis process in which a feedstock rich in aromatic compounds having more than 8 carbon atoms is treated and which consists in converting one or more alkyl group(s) having at least two carbon atoms (ethyl , propyl , butyl , isopropyl and the like) attached to a benzene nucleus into one or more methyl group(s) , said process being carried out in the presence of a catalyst comprising at least one metal from Group VIII of the Periodic Table , preferably nickel or platinum , and a porous support comprising at least one crystalline or noncrystalline refractory oxide , having or not having structured porosity , the reaction taking place:at a temperature of between 300° C. and 550° C., preferentially of between 350° C. and 500° C., and more preferentially still of between 370° C. and 450° C.,at a pressure of between 1 and 30 bar, preferentially of between 2 and 20 bar, and more preferentially still of between 2 and 10 bar,{'sub': '2', 'with a H/HC molar ratio of between 1 and 10, and preferentially of between 1.5 and 6,'}{'sup': −1', '−1', '−1, 'with an HSV of between 0.1 and 50 h, preferentially between 1 and 30 hand more preferentially still between 3 and 20 h.'}2- The selective hydrogenolysis process as claimed in claim 1 , in which the reactor used in said process is of fixed bed type and the catalyst support is provided in the form of extrudates.3- The selective hydrogenolysis process as claimed in claim 1 , in which the reactor used in said process is of moving bed type and the catalyst support is provided in the form of approximately ...

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Номер записи: 67
24-06-2021 дата публикации

PROCESS FOR MAKING MODIFIED SMALL-CRYSTAL MORDENITE, TRANSALKYLATION PROCESS USING SAME, AND MODIFIED SMALL-CRYSTAL MORDENITE

Номер: US20210187486A1
Автор: Abrams Martha Leigh, Cox Pelin, Jan Deng-Yang, Jeroro Eseoghene, Moscoso Jaime G.
Принадлежит:

A modified UZM-14 zeolite is described. The modified UZM-14 zeolite has a Modification Factor of 6 or more. The modified UZM-14 zeolite may have one or more of: a Si/Alratio of 14 to 30; a total pore volume in a range of 0.5 to 1.0 cc/g; at least 5% of a total pore volume being mesopores having a diameter of 10 nm of less; a cumulative pore volume of micropores and mesopores having a diameter of 100 Å or less of 0.25 cc/g or more; or a Collidine IR Bronsted acid site distribution greater than or equal to an area of 3/mg for a peak in a range of 1575 to 1700 cmafter desorption at 150° C. Processes of making the modified UZM-14 zeolite and transalkylation processes using the modified UZM-14 zeolite are also described. 1. A catalyst suitable for the conversion of aromatic hydrocarbons comprising:a modified UZM-14 zeolite having a Modification Factor of 6 or more, wherein the modified UZM-14 zeolite is an ion exchanged, caustic washed, acid washed UZM-14 zeolite.2. The catalyst of wherein the modified UZM-14 zeolite has a Si/Alratio of 14 to 30.3. The catalyst of wherein the modified UZM-14 zeolite has a total pore volume in a range of 0.5 to 1.0 cc/g.4. The catalyst of wherein the modified UZM-14 zeolite has at least 5% of a total pore volume being mesopores having a diameter of 10 nm of less.5. The catalyst of wherein the modified UZM-14 zeolite has a cumulative pore volume of micropores and mesopores having a diameter of 100 Å or less of 0.25 cc/g or more.6. The catalyst of wherein the modified UZM-14 zeolite has a Collidine IR Bronsted acid site distribution greater than or equal to an area of 3/mg for a peak in a range of 1575 to 1700 cm-1 after desorption at 150° C.7. The catalyst of wherein the catalyst further comprises an additional zeolitic component selected from one or more of MFI claim 1 , MEL claim 1 , EUO claim 1 , FER claim 1 , MFS claim 1 , MTT claim 1 , MTW claim 1 , TON and FAU.8. The catalyst of wherein the catalyst further comprises a binder ...

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Номер записи: 68
16-06-2016 дата публикации

INTEGRATED PROCESS FOR NORMAL PARAFFIN ALKYLATION

Номер: US20160168053A1
Автор: Bhattacharyya Alakananda, KALNES TOM N., Smith Stuart, Wier Mary
Принадлежит:

An integrated alkylation and disproportionation process and apparatus are described. n-Cand n-Care routed to a disproportionation reaction zone for conversion to iso-Cand C isoparaffin-rich product. The iso-Cis routed to an alkylation reaction zone and reacted with refinery propylene and butenes to produce alkylate product. The C isoparaffin-rich product and alkylate product are recovered. Unconverted iso-Cand/or olefins are recycled to the alkylation reaction zone, and unconverted n-Cand n-Care recycled to the disproportionation reaction zone. 1. A process for normal paraffin alkylation comprising:{'sub': 4', '5', '4', '6+', '4', '5, 'introducing a feed comprising n-Cand n-Cparaffins to a disproportionation reaction zone in the presence of a disproportionation catalyst under disproportionation reaction conditions to form a disproportionation mixture comprising iso-Cand C disproportionation products and unreacted n-Cand n-Cparaffins;'}{'sub': 4', '6+', '4', '5, 'separating the disproportionation mixture in a disproportionation separation zone into at least an iso-C-rich stream, a C isoparaffin-rich stream, and a stream rich in unreacted n-Cand n-Cparaffins;'}{'sub': 4', '4, 'introducing the iso-C-rich stream and an olefin feed stream comprising at least one of ethylene, propylene, and butenes into an alkylation reaction zone in the presence of an alkylation catalyst under alkylation reaction conditions to produce an alkylation mixture comprising alkylate and unreacted iso-Cparaffins;'}{'sub': '4', 'separating the alkylation mixture in an alkylation separation zone into at least an alkylate-rich stream, and a stream rich in unreacted iso-Cparaffins;'}{'sub': 4', '5, 'recycling the stream rich in unreacted n-Cand n-Cparaffins from the disproportionation separation zone to the disproportionation reaction zone;'}{'sub': '4', 'recycling the stream rich in unreacted iso-Cparaffins from the alkylation separation zone to the alkylation reaction zone; and'}{'sub': '6+', ' ...

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Номер записи: 69
16-06-2016 дата публикации

INTEGRATED PROCESS FOR GASOLINE PRODUCTION

Номер: US20160168054A1
Автор: Bhattacharyya Alakananda, Glover Bryan K., KALNES TOM N., Martins Susie C., Nafis Douglas A., Smith Stuart
Принадлежит:

An integrated process for gasoline production is described. The process includes introducing a feed comprising n-Chydrocarbons into a disproportionation reaction zone in the presence of a disproportionation catalyst to form a disproportionation mixture comprising iso-Cand Cdisproportionation products and unreacted n-Chydrocarbons. An iso-Chydrocarbon stream and an olefin feed are introduced into an alkylation reaction zone in the presence of an alkylation catalyst to produce an alkylation mixture comprising alkylate and unreacted iso-Cparaffins. The disproportionation mixture and the alkylation mixture are combined, and the combined mixture is separated into at least a stream comprising the alkylate product, an iso-Cstream, and an unreacted n-Chydrocarbon stream. The iso-Cstream is recycled to the alkylation reaction zone, and the unreacted n-Chydrocarbon stream is recycled to the disproportionation reaction zone. The stream comprising the alkylate product is recovered. 1. An integrated process for gasoline production comprising:{'sub': 5', '4', '6+', '5, 'introducing a feed comprising n-Chydrocarbons to a disproportionation reaction zone in the presence of a disproportionation catalyst under disproportionation reaction conditions to form a disproportionation mixture comprising iso-Cand Cdisproportionation products and unreacted n-Chydrocarbons;'}{'sub': 4', '4, 'introducing an iso-Chydrocarbon stream and an olefin feed stream comprising at least one of ethylene, propylene, and butenes into an alkylation reaction zone in the presence of an alkylation catalyst under alkylation reaction conditions to produce an alkylation mixture comprising alkylate product and unreacted iso-Cparaffins;'}combining the disproportionation mixture and the alkylation mixture to form a combined mixture;{'sub': 4', '4', '4,', '5, 'separating the combined mixture into at least a stream comprising the alkylate product, an iso-Cstream comprising the iso-Cdisproportionation product and the ...

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Номер записи: 70
25-06-2015 дата публикации

Combined heavy reformate dealkylation-transalkylation process for maximizing xylenes production

Номер: US20150175504A1
Автор: Raed Abudawoud
Принадлежит: Saudi Arabian Oil Co

The present invention relates to a method of forming mixed xylenes from a heavy reformate using a dealkylation-transalkylation system that includes the step of introducing a heavy reformate containing methyl ethyl benzenes and tri-methyl benzenes and sufficiently free of toluene into the dealkylation stage with a hydrogen-containing material such that the heavy reformate and the hydrogen-containing material intermingle and contact a hydrodealkylation catalyst. The dealkylation-transalkylation system includes dealkylation stages, non-aromatic product gas separations and transalkylation stages. The BTEX component toluene forms from the reaction of methyl ethyl benzenes and hydrogen in the presence of the hydrodealkylation catalyst. The method also includes the step of introducing a dealkylated heavy reformate into the transalkylation stage such that the dealkylated heavy reformate contacts a transalkylation catalyst, forming a transalkylation stage product mixture that includes mixed xylenes.

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Номер записи: 71
01-07-2021 дата публикации

Heavy Aromatics Conversion Processes and Catalyst Compositions Used Therein

Номер: US20210198165A1
Автор: Bai Chuansheng, Cutler Joshua I., Elia Christine N., Lai Wenyih F., Nair Hari, Rollman Nicholas S.
Принадлежит:

Disclosed are processes for conversion of a feedstock comprising C aromatic hydrocarbons to lighter aromatic products in which the feedstock and optionally hydrogen are contacted in the presence of the catalyst composition under conversion conditions effective to dealkylate and transalkylate said C aromatic hydrocarbons to produce said lighter aromatic products comprising benzene, toluene and xylene. The catalyst composition comprises a zeolite, a first metal, and a second metal, and is treated with a source of sulfur and/or a source of steam. 125.-. (canceled)26. A catalyst composition comprising (i) one or more zeolites selected from zeolite beta , ZSM-5 , ZSM-12 and mordenite zeolites synthesized from TEA or MTEA , said mordenite zeolites having a mesopore surface area of greater than 30 m/g and said mordenite zeolites comprising agglomerates composed of primary crystallites , wherein said primary crystallites have an average primary crystal size as measured by TEM of less than 80 nm and an aspect ratio of less than 2 , (ii) 0.001 wt. % to 20.0 wt. % of at least one first metal comprising molybdenum or tungsten , based on the weight of the catalyst composition , and (iii) 0.001 wt. % to 20.0 wt. % of at least one second metal comprising cobalt or nickel , based on the weight of the catalyst composition ,wherein said catalyst composition is treated with a source of sulfur in one or more steps at temperatures in the range 204° C. (400° F.) up to about 480° C. (900° F.) or treated with a source of steam which comprises up to about 100% steam at temperatures in the range of about 260° C. (500° F.) to about 649° C. (1200° F.).27. The catalyst composition of claim 26 , wherein said source of sulfur is one or more of hydrogen sulfide claim 26 , carbon disulfide and alkylsulfides which are selected from the group consisting of methylsulfide claim 26 , dimethylsulfide claim 26 , dimethyldisulfide claim 26 , diethylsulfide and dibutyl sulfide claim 26 , and mixtures of two ...

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Номер записи: 72
23-06-2016 дата публикации

Transalkylation Process

Номер: US20160176787A1
Автор: Hari Nair, Jeffrey L. Andrews, Michel Molinier
Принадлежит: ExxonMobil Chemical Patents Inc

Disclosed is a transalkylation process for making an aromatic material between a light aromatic material and a heavier aromatic material in the presence of hydrogen and a transalkylation catalyst comprising a hydrogenation component and a transalkylation component. The process comprises conducting the transalkylation reaction under conditions conducive to reducing the amount of cyclic compounds in the transalkylation reaction mixture in the beginning phase of the operation that is different from the conditions after the beginning phase. The invention is useful, e.g., in transalkylation between toluene and C9+ aromatic feed materials to produce xylenes and/or benzene.

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Номер записи: 73
08-07-2021 дата публикации

UZM-54 AND TRANSALKYLATION PROCESS USING SAME

Номер: US20210205795A1
Автор: Abrams Martha Leigh, Cox Pelin, Jan Deng-Yang, Jeroro Eseoghene, Moscoso Jaime G.
Принадлежит:

A catalyst suitable for the conversion of aromatic hydrocarbons is described. The catalyst comprises UZM-54 zeolite; a mordenite zeolite; a binder comprising alumina, silica, or combinations, thereof; and a metal selected from one or more of: Groups VIB(6) VIIB(7), VIII(8-10) and IVA(14) of the Periodic Table. A process for transalkylation using the catalyst is also described. 1. A catalyst suitable for the conversion of aromatic hydrocarbons comprising:UZM-54 zeolite;a mordenite zeolite;a binder comprising alumina, silica, or combinations, thereof; anda metal selected from one or more of: Groups VIB(6) VIIB(7), VIII(8-10) and IVA(14) of the Periodic Table.2. The catalyst of wherein the catalyst comprises about 20 to about 60 wt % of the UZM-54 zeolite claim 1 , about 20 to about 60 wt % of the mordenite zeolite claim 1 , about 10 to about 40 wt % of the binder claim 1 , and about 0.1 to about 10 wt % of the metal.3. The catalyst of wherein the UZM-54 zeolite has less than about 500 wppm Na.4. The catalyst of wherein the binder comprises alumina.5. The catalyst of wherein the metal comprises one or more of: Mo claim 1 , Ni claim 1 , Re claim 1 , Pt claim 1 , or Pd.6. The catalyst of wherein the catalyst comprisesabout 20 to about 60 wt % of the UZM-54 zeolite;about 20 to about 60 wt % of the mordenite zeolite;about 10 to about 40 wt % of the binder; and,about 0.1 to about 10 wt % of the metal wherein the metal comprises one or more of: Mo, Ni, Re, Pt, or Pd.7. The catalyst of wherein the UZM-54 zeolite has less than about 500 wppm Na.8. The catalyst of wherein the binder comprises alumina.9. A process for transalkylation of a feedstream comprising one or more of C claim 6 , C claim 6 , Cand C aromatics to obtain a transalkylation product stream having an increased concentration of Caromatics relative to that of the feedstream claim 6 , comprising contacting the feedstream at transalkylation conditions with a catalyst comprising:UZM-54 zeolite;a mordenite zeolite;a ...

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Номер записи: 74
08-07-2021 дата публикации

SYSTEM FOR CONVERSION OF CRUDE OIL TO PETROCHEMICALS AND FUEL PRODUCTS INTEGRATING VACUUM GAS OIL HYDROTREATING AND STEAM CRACKING

Номер: US20210207044A9
Автор: AL-GHAMDI Mohammed Saeed
Принадлежит:

Process scheme configurations are disclosed that enable conversion of crude oil feeds with several processing units in an integrated manner into petrochemicals. The designs utilize minimum capital expenditures to prepare suitable feedstocks for the steam cracker complex. The integrated process for converting crude oil to petrochemical products including olefins and aromatics, and fuel products, includes mixed feed steam cracking and gas oil steam cracking. Feeds to the mixed feed steam cracker include light products and naphtha from hydroprocessing zones within the battery limits, recycle streams from the C3 and C4 olefins recovery steps, and raffinate from a pyrolysis gasoline aromatics extraction zone within the battery limits. Feeds to the gas oil steam cracker include hydrotreated gas oil range intermediates from vacuum gas oil hydrotreating. 121.-. (canceled)22. An integrated system for producing petrochemicals and fuel products comprising:an atmospheric distillation unit (ADU) operable to receive and separate a feed, and discharge a first ADU fraction comprising naphtha, a second ADU fraction comprising at least a portion of middle distillates from the feed, and a third ADU fraction comprising atmospheric residue;a vacuum distillation unit (VDU) operable to receive and separate the third ADU fraction, and discharge a first VDU fraction comprising vacuum gas oil;a distillate hydroprocessing (DHP) zone operable to receive and convert middle distillates from the second ADU fraction into a first DHP fraction and a second DHP fraction, wherein the first DHP fraction comprises naphtha and the second DHP fraction is used for diesel fuel production;a gas oil hydrotreating (GOHT) zone operable to receive and treat vacuum gas oil from the first VDU fraction and produce a first GOHT fraction containing naphtha range components, and a hydrotreated gas oil fraction;a steam cracking zone comprising (a) a mixed feed steam cracking (MFSC) zone operable to receive and ...

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Номер записи: 75
30-06-2016 дата публикации

HYDROCARBON PROCESSING APPARATUSES AND PROCESSES FOR PRODUCING N-PENTANE AND ISOBUTANE

Номер: US20160185688A1
Автор: Lapinski Mark Paul, Lippmann Matthew, Lowry David, Shecterle David James
Принадлежит:

Hydrocarbon processing apparatuses and processes for producing n-pentane and isobutane are provided herein. In an embodiment, a process for producing n-pentane and isobutane includes providing a hydrocarbon feed stream that includes C4 and C5 hydrocarbons. A recycle stream that includes C4+ hydrocarbons and the hydrocarbon feed stream is combined to produce a combined feed stream. The combined feed stream is separated to produce an iC4 product stream, an nC5+ product stream, and an iC5/nC4 feed stream. The iC5/nC4 feed stream is simultaneously disproportionated and isomerized in an isomerization zone to produce an intermediate stream that includes C3-C6 hydrocarbons. The C3-C6 hydrocarbons in the intermediate stream are separated to produce a C3− stream and the recycle stream that includes C4+ hydrocarbons. 1. A process for producing n-pentane and isobutane , wherein the process comprises:providing a hydrocarbon feed stream comprising C4 and C5 hydrocarbons;combining a recycle stream comprising C4+ hydrocarbons and the hydrocarbon feed stream to produce a combined feed stream;{'b': '30', 'separating the combined feed stream to produce an iC4 product stream, an nC5 product stream, and an iC5/nC4 feed stream;'}simultaneously disproportionating and isomerizing the iC5/nC4 feed stream in an isomerization zone to produce an intermediate stream comprising C3-C6 hydrocarbons; andseparating the C3-C6 hydrocarbons in the intermediate stream to produce a C3− stream and the recycle stream comprising C4+ hydrocarbons.2. The process of claim 1 , wherein simultaneously disproportionating and isomerizing the iC5/nC4 feed stream comprises simultaneously disproportionating and isomerizing the iC5/nC4 feed stream substantially in the absence of water.3. The process of claim 2 , wherein simultaneously disproportionating and isomerizing the iC5/nC4 feed stream comprises simultaneously disproportionating and isomerizing the iC5/nC4 feed stream in the presence of hydrogen and an ...

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Номер записи: 76
28-06-2018 дата публикации

PROCESS FOR COMPOUND TRANSFORMATION

Номер: US20180179126A1
Автор: BASSET Jean-Marie Maurice, Callens Emmanuel, Riache Nassima
Принадлежит:

Embodiments of the present disclosure provide for methods of using a catalytic system to chemically transform a compound (e.g., a hydrocarbon). In an embodiment, the method does not employ grafting the catalyst prior to catalysis. In particular, embodiments of the present disclosure provide for a process of hydrocarbon (e.g., C1 to C20 hydrocarbon) metathesis (e.g., alkane, olefin, or alkyne metathesis) transformation, where the process can be conducted without employing grafting prior to catalysis. 1. A method of hydrocarbon metathesis , comprising:contacting a partially dehydroxylated metal oxide, an organometallic compound, and one or more hydrocarbons sufficient to achieve hydrocarbon metathesis.2. The method of claim 1 , wherein the hydrocarbon is selected from the group consisting of a saturated hydrocarbon claim 1 , a unsaturated fatty acid ester claim 1 , an olefin claim 1 , a functionalized olefin claim 1 , and a combination thereof.3. The method of claim 1 , wherein the organometallic compound is selected from: Wilkinson dWMeor Schrock type dW metal alkylidyne complex.4. The method of claim 1 , wherein the metal in the organometallic compound is a transition metal or mixture thereof.5. The method of claim 4 , wherein the transition metal is selected from the group consisting of: Ti claim 4 , Zr claim 4 , Hf claim 4 , Ta claim 4 , Nb claim 4 , V claim 4 , Cr claim 4 , Mo claim 4 , W claim 4 , Re claim 4 , and their mixtures.6. The method of claim 1 , wherein the organometallic compound containing a chloride or an aryl oxide is associated with an alkylating agent.7. The method of claim 6 , wherein the alkylating agent is MeLi or MeZn.8. The method of claim 1 , wherein the metal oxide is selected from the group consisting of: silica claim 1 , silica-alumina claim 1 , γ-alumina claim 1 , mesoporous silica claim 1 , zeolite claim 1 , metal organic frameworks (MOF) claim 1 , organic-inorganic mixed oxides claim 1 , carbon black claim 1 , carbon nanotubes claim 1 ...

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Номер записи: 77
18-09-2014 дата публикации

HYDROCARBON TRANSFORMATIONS USING CARBOCATALYSTS

Номер: US20140275684A1
Автор: Bielawski Christopher W., Dreyer Daniel R., Miller Richard
Принадлежит: GRAPHEA, INC.

The disclosure relates to catalytically active carbocatalysts, e.g., a graphene oxide or graphite oxide catalyst suitable for use in a variety of high value chemical transformations. 1. A process for converting(a) an alkane starting material to an alkene product (dehydrogenation);(b) an alkane starting material to one or more higher molecular weight alkane products (coupling);(c) an alkane starting material to one or more metathesis products (metathesis);(d) a higher alkane starting material to one or more lower alkane products (cracking);(e) a cycloalkane starting material to an alkane product or an alkene product or a combination thereof (cracking);or any combination thereof;comprising contacting any starting material in (a)-(e) with a catalytically active surface-modified graphene oxide or graphite oxide to provide the corresponding product in (a)-(e).2. The process of claim 1 , wherein the catalytically active surface-modified graphene oxide or graphite oxide is catalytically active surface-modified graphene oxide.3. The process of claim 1 , wherein the catalytically active surface-modified graphene oxide or graphite oxide is catalytically active surface-modified graphite oxide.4. The process of claim 1 , wherein the catalytically active surface-modified graphene oxide or graphite oxide is characterized by one or more FT-IR features at about 3150 cm claim 1 , 1685 cm claim 1 , 1280 cm claim 1 , or 1140 cm.5. The process of claim 1 , wherein the catalytically active surface-modified graphene oxide or graphite oxide has a surface modification comprising one or more of a hydrogen peroxide-terminated surface claim 1 , an epoxide-terminated surface claim 1 , a ketone-terminated surface claim 1 , a diketone terminated surface claim 1 , an aldehyde terminated surface claim 1 , a carboxyl terminated surface claim 1 , a hydroxyl terminated surface claim 1 , an alcohol terminated surface claim 1 , an ether terminated surface claim 1 , a dioxirane terminated surface claim ...

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Номер записи: 78
11-06-2020 дата публикации

Catalyst Compositions and Their Use in Aromatic Alkylation Processes

Номер: US20200179913A1
Автор: Ide Matthew S., Johnson Ivy D., Lai Wenyih F., Levin Doron, Loveless Brett T., Weigel Scott J.
Принадлежит:

Catalyst composition which comprises a first zeolite having a BEA* framework type and a second zeolite having a MOR framework type and a mesopore surface area of greater than 30 m/g is disclosed. These catalyst compositions are used to remove catalyst poisons from untreated feed streams having one or more impurities which cause deactivation of the downstream catalysts employed in hydrocarbon conversion processes, such as those that produce mono-alkylated aromatic compounds. 1. A catalyst composition comprising a first zeolite having a BEA* framework type and a second zeolite having a MOR framework type and a mesopore surface area of greater than 30 m/g as measured by BET.2. The catalyst composition of claim 1 , wherein said first zeolite is zeolite beta.3. The catalyst composition of claim 1 , wherein said second zeolite is EMM-34.4. The catalyst composition of claim 3 , wherein said second zeolite comprising agglomerates of primary crystallites claim 3 , wherein said primary crystallites have an average primary crystal size of less than 80 nm in each of the a claim 3 , b and c crystal vectors as measured by X-ray diffraction and an aspect ratio of less than 2 claim 3 , wherein the aspect ratio is defined as the longest dimension of the crystallite divided by the width of the crystallite claim 3 , wherein said width of the crystallite is defined as the dimension of the crystallite in the middle of that longest dimension in a direction orthogonal to that longest dimension claim 3 , as measured by TEM.5. The catalyst composition of claim 4 , wherein said EMM-34 has a ratio of the mesopore surface area to the total surface area of greater than 0.05.6. The catalyst composition of claim 5 , wherein said second zeolite is synthesized from TEA or MTEA.7. The catalyst composition of claim 6 , wherein the Si/Almolar ratio of said second zeolite is in the range of 10 to 60.8. The catalyst composition claim 7 , wherein said catalyst composition has a collidine uptake in the ...

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Номер записи: 79
23-07-2015 дата публикации

Process for Producing Cyclohexylbenzene

Номер: US20150203419A1
Автор: Charles Morris Smith, Christopher L. Becker, Francisco M. Benitez, Ryan A. Sothen
Принадлежит: ExxonMobil Chemical Patents Inc

In a process for producing cyclohexylbenzene, benzene is reacted with cyclohexene under alkylation conditions effective to produce an alkylation effluent comprising cyclohexylbenzene and a polycyclohexylbenzene. A first feed comprising at least a portion of the alkylation effluent is then fed to a first separation device, where the first feed is separated into at least a first fraction containing cyclohexylbenzene and a second fraction containing the polycyclohexylbenzene, the second fraction also comprising an oxygenated hydrocarbon. At least a portion of the oxygenated hydrocarbon is removed from at least a portion of the second fraction in a second separation device to obtain a second feed. The second feed may then be reacted in a transalkylation or dealkylation reactor to convert at least part of the polycyclohexylbenzene to additional cyclohexylbenzene.

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Номер записи: 80
27-06-2019 дата публикации

PROCESS FOR MAXIMIZING PRODUCTION OF XYLENES FROM HEAVY REFORMATE WITHOUT PURGE

Номер: US20190194095A1
Автор: ABUDAWOUD RAED, XU QI
Принадлежит: Saudi Arabian Oil Company

A method for producing xylenes from a heavy reformate feed includes the steps of introducing the heavy reformate feed and a hydrogen feed to a dealkylation reactor, reacting the heavy reformate feed with the hydrogen gas in the presence of the dealkylation catalyst in the dealkylation reactor to produce a dealkylation effluent, introducing the dealkylation effluent to a splitter unit, separating the dealkylation effluent into a light gas stream, a toluene stream, a benzene stream, a C9 aromatics stream, a C10+ aromatics stream, and a mixed xylene stream in the splitter unit, introducing the toluene stream, the C9 aromatics stream, and a hydrogen stream into a transalkylation reactor, reacting the toluene stream and the C9 aromatics stream in the presence of the transalkylation catalyst to produce a transalkylation effluent, introducing the transalkylation effluent to the splitter unit, and separating the transalkylation effluent in the splitter unit. 1. A method for producing mixed xylenes from a heavy reformate feed , the method comprising the steps of:introducing the heavy reformate feed and a hydrogen feed to a dealkylation reactor, wherein the dealkylation reactor comprises a dealkylation catalyst, wherein the heavy reformate feed comprises aromatic hydrocarbons with nine or more carbon atoms (C9+ aromatics), wherein the hydrogen feed comprises hydrogen gas;reacting the heavy reformate feed with the hydrogen feed in the presence of the dealkylation catalyst in the dealkylation reactor to produce a dealkylation effluent, wherein the dealkylation reactor is at a dealkylation temperature, wherein the dealkylation reactor is at a dealkylation pressure, wherein the dealkylation reactor has a liquid hourly space velocity;introducing the dealkylation effluent to a splitter unit, where the dealkylation effluent comprises light gases, toluene, benzene, mixed xylenes, and C9+ aromatics;separating the dealkylation effluent into a light gas stream, a toluene stream, a ...

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Номер записи: 81
29-07-2021 дата публикации

Dealkylation and Transalkylation of Heavy Aromatic Hydrocarbons

Номер: US20210230083A1
Автор: Abichandani Jeevan S., Detjen Todd E.
Принадлежит:

A process for producing xylene from Caromatic hydrocarbons comprises contacting a first feedstock comprising Caromatic hydrocarbons with a first catalyst in the presence of hydrogen under effective vapor phase dealkylation conditions to dealkylate part of the Caromatic hydrocarbons and produce a first product comprising benzene and unreacted Caromatic hydrocarbons. A second feedstock comprising toluene is contacted with a second catalyst in the presence of hydrogen under effective vapor phase toluene disproportionation conditions to disproportionate at least part of the toluene and produce a second product comprising para-xylene. A third feedstock comprising Caromatic hydrocarbons and benzene and/or toluene is contacted with a third catalyst in the presence of hydrogen under effective liquid phase Ctransalkylation conditions to transalkylate at least part of the Caromatic hydrocarbons and produce a third product comprising xylenes. 1. A process for producing xylene from Caromatic hydrocarbons , the process comprising:{'sub': 9+', '9+', '9+, '(a) contacting a first feedstock comprising Caromatic hydrocarbons with a first catalyst in the presence of 0 wt. % or more of hydrogen under effective vapor phase dealkylation conditions to dealkylate part of the Caromatic hydrocarbons and produce a first product comprising benzene and unreacted Caromatic hydrocarbons;'}(b) contacting a second feedstock comprising toluene with a second catalyst in the presence of hydrogen under effective vapor phase toluene disproportionation conditions to disproportionate at least part of the toluene and produce a second product comprising para-xylene; and{'sub': 9+', '9+, '(c) contacting a third feedstock comprising C9+ aromatic hydrocarbons and benzene and/or toluene with a third catalyst in the presence of hydrogen under effective liquid phase Ctransalkylation conditions to transalkylate at least part of the Caromatic hydrocarbons and produce a third product comprising xylenes.'}2. The ...

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Номер записи: 82
25-06-2020 дата публикации

CATALYST, DEVICE FOR MANUFACTURING CONJUGATED DIENE, AND METHOD FOR MANUFACTURING CONJUGATED DIENE

Номер: US20200199045A1
Автор: MIYAMA Toshihito, NISHIYAMA Haruka, Watanabe Shinsuke, YAGIHASHI Noritoshi
Принадлежит: Sekisui Chemical Co., Ltd.

A catalyst for synthesizing a conjugated diene from a raw material including an alcohol, which includes at least Ce and Zn as metal elements constituting the catalyst. An apparatus for producing a conjugated diene, including: a reaction tube () provided with the catalyst; a supply means for supplying a raw material gas containing the raw material into the reaction tube (); and an outlet means for releasing a product from the reaction tube (). A method for producing a conjugated diene, including contacting a raw material gas containing a raw material with the catalyst to obtain a conjugated diene. The amount of the raw material is preferably 10 to 50% by volume (in terms of gas volume) with respect to 100% by volume (in terms of gas volume) of the raw material gas. 1. A catalyst for synthesizing a conjugated diene from a raw material comprising an alcohol , which comprisesat least Ce and Zn as metal elements constituting the catalyst.2. The catalyst according to claim 1 , which further comprises at least one metal element A selected from metal elements belonging to Group 4 of the periodic table as metal element constituting the catalyst.3. The catalyst according to claim 1 , wherein the metal element A is Hf.4. The catalyst according to claim 1 , wherein the alcohol is ethanol.5. The catalyst according to claim 1 , which is a catalyst for synthesizing a conjugated diene.6. The catalyst according to claim 1 , wherein the raw material further comprises acetaldehyde.7. The catalyst according to claim 1 , wherein the metal elements are supported on a carrier.8. The catalyst according to claim 1 , which satisfies formula (I):{'br': None, 'AxZnyCez \u2003\u2003(I)'} x is 0 to 10,', 'y is from 0.1 to 5, and', 'z is 0.5 to 20., 'wherein A represents a metal element A belonging to Group 4 of the periodic table, and x, y, and z are numbers representing mass ratios of the metal elements A, Zn, and Ce, respectively, provided that9. The catalyst according to claim 8 , wherein in ...

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Номер записи: 83
04-08-2016 дата публикации

Process for Preparing a Molecular Sieve

Номер: US20160221832A1
Автор: Guang Cao, Nicholas S. ROLLMAN, Wenyih F. Lai
Принадлежит: ExxonMobil Chemical Patents Inc

The present invention provides a mordenite zeolite having a mesopore surface area of greater than 30 m 2 /g and an average primary crystal size as measured by TEM of less than 80 nm, and methods of making the mordenite zeolite.

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Номер записи: 84
04-08-2016 дата публикации

Transalkylation of Heavy Aromatic Hydrocarbon Feedstocks

Номер: US20160221897A1
Автор: Christine N. Elia, Gary D. Mohr, Jeevan S. Abichandani, Robert G. TINGER, Shifang L. Luo, Wenyih F. Lai, Xiaobo Zheng
Принадлежит: ExxonMobil Chemical Patents Inc

A process for producing xylene comprises contacting a first feed comprising C 9+ aromatic hydrocarbons and hydrogen with a first catalyst composition comprising a first molecular sieve having a Constraint Index of 3 to 12 and at least one hydrogenation component. The first catalyst composition dealkylates at least part of the C 9+ aromatic hydrocarbons containing C 2+ alkyl groups and to saturate the resulting C 2+ olefins to produce a second feed. The second feed is then contacted with a second catalyst composition under conditions effective to transalkylate at least part of the C 9+ aromatic hydrocarbons in the second feed to produce a product comprising xylene. The second catalyst composition comprises a second molecular sieve having a Constraint Index less than 3 and a third molecular sieve having a Constraint Index of 3 to 12.

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Номер записи: 85
19-08-2021 дата публикации

TOLUENE DISPROPORTIONATION USING AN ENHANCED UZM-39 ALUMINOSILICATE ZEOLITE

Номер: US20210253497A1
Автор: Abrams Martha Leigh, Boldingh Edwin P., Nicholas Christopher P.
Принадлежит:

Toluene disproportionation processes utilizing treated UZM-39 zeolites are described. The processes produce effluent streams comprising para-xylene and benzene. The molar ratio of benzene to xylene (Bz/X) in the effluent stream can be in a range of about 1.00 to about 1.14, the molar ratio of para-xylene to xylene (pX/X) in the effluent stream can be in a range of about 0.80 to about 1.0, and the conversion of toluene can be about 20% to about 40%. 1. A toluene disproportionation process comprising contacting a feed comprising toluene with a catalyst comprising a microporous crystalline zeolite at disproportionation conditions to produce an effluent stream comprising para-xylene and benzene , wherein a molar ratio of benzene to xylene in the effluent stream is in a range of about 1.00 to about 1.14 , wherein a molar ratio of para-xylene to xylene in the effluent stream is in a range of about 0.80 to about 1.0 , and wherein a conversion of toluene is about 20% to about 40%; andwherein the zeolite has been enhanced with at least one enhancement selected from treatment for deposition of carbon, treatment for deposition of silica, or both.2. The process of wherein the molar ratio of benzene to xylene is in the range of about 1.00 to about 1.08.4. (canceled)5. The process of wherein the at least one enhancement treatment step comprises at least one treatment to incorporate silica.6. The process of wherein the catalyst is steamed after the at least one enhancement treatment step.7. The process of wherein the molar ratio of benzene to xylene is in the range of about 1.00 to about 1.08 and wherein the range of the molar ratio of para-xylene to xylene is in the range of about 0.80 to about 0.95.8. The process of wherein a selectivity to xylenes is greater than 52% when the molar ratio of para-xylene to xylene is in the range of about 0.80 to about 0.90.9. The process of wherein a selectivity to light ends is less than about 3.5% when the molar ratio of para-xylene to xylene ...

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Номер записи: 86
19-08-2021 дата публикации

TOLUENE DISPROPORTIONATION USING AN ENHANCED UZM-44 ALUMINOSILICATE ZEOLITE

Номер: US20210253498A1
Автор: Abrams Martha Leigh, Boldingh Edwin P., Nicholas Christopher P.
Принадлежит:

Toluene disproportionation processes utilizing treated UZM-44 zeolites are described. The processes produce effluent streams comprising para-xylene and benzene. The molar ratio of benzene to xylene (Bz/X) in the effluent stream can be in a range of about 1.00 to about 1.14, the molar ratio of para-xylene to xylene (pX/X) in the effluent stream can be in a range of about 0.80 to about 1.0, and the conversion of toluene can be about 20% to about 40%. 1. A toluene disproportionation process comprising contacting a feed comprising toluene with a catalyst comprising a microporous crystalline zeolite at disproportionation conditions to produce an effluent stream comprising para-xylene and benzene , wherein the zeolite is UZM-44 , wherein a molar ratio of benzene to xylene in the effluent stream is in a range of about 1.00 to about 1.14 , wherein a molar ratio of para-xylene to xylene in the effluent stream is in a range of about 0.80 to about 1.0 , wherein a conversion of toluene is about 20% to about 40%; andwherein the catalyst has been enhanced with at least one enhancement treatment step selected from treatment for deposition of carbon, treatment for deposition of silica, or both.2. The process of wherein the molar ratio of benzene to xylene is in the range of about 1.00 to about 1.08.4. (canceled)5. The process of wherein the at least one enhancement treatment step comprises at least one treatment to incorporate silica.6. The process of wherein the catalyst is steamed after the at least one enhancement treatment step.7. The process of wherein the molar ratio of benzene to xylene is in the range of about 1.00 to about 1.08 and wherein the molar ratio of para-xylene to xylene is in the range of about 0.80 to about 0.95.8. The process of wherein a selectivity to xylenes is greater than 52% when the molar ratio of para-xylene to xylene is in the range of about 0.80 to about 0.90.9. The process of wherein a selectivity to light ends is less than about 3.5% when the molar ...

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Номер записи: 87
23-08-2018 дата публикации

Aromatic Compositions and Methods for Obtaining Them

Номер: US20180237361A1
Автор: DAVIS STEPHEN M., Xu Teng
Принадлежит:

Aromatic compositions useful in various applications, such as aromatic fluid solvents and high temperature heat transfer fluids, are provided herein. Also provided are advantageous methods for obtaining the aromatic compositions, utilizing hydroalkylation of precursor aromatic hydrocarbons such as benzene, toluene, xylene, and the like. Particularly preferred aromatic compositions include one or more of cycloalkylaromatic, dicycloalkylaromatic, biphenyl, terphenyl, and diphenyl oxide compounds. The aromatic compositions may be blended with an aromatic solvent or other aromatic fluid comprising one or more of alkylnaphthalenes, alkylbenzenes, and naphthalene, e.g., to form a useful aromatic fluid solvent, or the aromatic compositions may be utilized as high temperature heat transfer fluids (with or without additional blend components). 1. A process comprising:(a) obtaining a first aromatic composition from one or more precursor aromatic hydrocarbons, wherein the first aromatic composition comprises one or more of: (i) one or more cycloalkylaromatic compounds; (ii) one or more dicycloalkylaromatic compounds; (iii) one or more biphenyl compounds; and (iv) one or more terphenyl compounds; wherein obtaining the first aromatic composition comprises one of:', '(a-1) contacting a hydroalkylation feed comprising the one or more aromatic hydrocarbons with hydrogen in the presence of a hydroalkylation catalyst so as to produce a hydroalkylation reaction effluent comprising (i) the one or more cycloalkylaromatic compounds and (ii) the one or more dicycloalkylaromatic compounds; and', '(a-2) contacting a transalkylation feed comprising the one or more aromatic hydrocarbons with a precursor cycloalkylaromatic compound in the presence of a transalkylation catalyst so as to produce a transalkylation reaction effluent comprising the one or more cycloalkylaromatic compounds and the one or more dicycloalkylaromatic compounds., '(b) blending the first aromatic composition with a second ...

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Номер записи: 88
09-09-2021 дата публикации

SYSTEMS AND PROCESSES FOR DIRECT CRUDE OIL UPGRADING TO HYDROGEN AND CHEMICALS

Номер: US20210277318A1
Автор: Abba Ibrahim, BOURANE Abdennour, Harale Aadesh, Jamal Aqil, KHOWAITER Ahmad, Younes Mourad
Принадлежит: Saudi Arabian Oil Company

Systems and methods for direct crude oil upgrading to hydrogen and chemicals including separating an inlet hydrocarbon stream into a light fraction and a heavy fraction comprising diesel boiling point temperature range material; producing from the light fraction syngas comprising Hand CO; reacting the CO produced; producing from the heavy fraction and separating CO, polymer grade ethylene, polymer grade propylene, Ccompounds, cracking products, light cycle oils, and heavy cycle oils; collecting and purifying the COproduced from the heavy fraction; processing the Ccompounds to produce olefinic oligomerate and paraffinic raffinate; separating the cracking products; oligomerizing a light cut naphtha stream; hydrotreating an aromatic stream; hydrocracking the light cycle oils to produce a monoaromatics product stream; gasifying the heavy cycle oils; reacting the CO produced from gasifying the heavy cycle oils; collecting and purifying the CO; and processing and separating produced aromatic compounds into benzene and para-xylene. 1. A method for hydrocarbon separation and upgrading , the method comprising the steps of:separating an inlet hydrocarbon stream into a light fraction comprising naphtha boiling point temperature range material and a heavy fraction comprising diesel boiling point temperature range material;{'sub': '2', 'producing from the light fraction syngas comprising Hand CO;'}reacting the CO produced from the light fraction via at least one reaction selected from the group consisting of: carbonylation, polymerization, and water-gas shift;{'sub': 2', '4, 'producing from the heavy fraction and separating CO, polymer grade ethylene, polymer grade propylene, Ccompounds, cracking products comprising naphtha boiling point temperature range products with olefins and aromatics, light cycle oils, and heavy cycle oils;'}{'sub': '2', 'collecting and purifying the COproduced from the heavy fraction;'}{'sub': '4', 'processing the Ccompounds to produce olefinic ...

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Номер записи: 89
06-09-2018 дата публикации

Transalkylation Processes and Catalyst Compositions Used Therein

Номер: US20180251413A1
Автор: Benedict Daniel J., Henao Juan D., Ide Matthew S., Keville Kathleen M., Loveless Brett T.
Принадлежит:

Disclosed are selectivated transalkylation catalyst compositions and methods of making the same. The selectivated transalkylation catalyst compositions have a zeolite framework structure of MWW, FAU, BEA*, or MOR, or mixtures thereof, and are selectivated with a selectivating solution. The selectivating solution includes a dissolved ion of at least one element in Group 1, Group 2, Group 15, Group 16, or Group 17 of the Periodic Table. Also disclosed are processes of producing ethylbenzene and cumene using the selectivated transalkylation catalyst compositions. 1. A process for producing ethylbenzene comprising the steps of:(a) providing a selectivated transalkylation catalyst composition;(b) providing a stream comprising poly-alkylated benzene and a stream comprising benzene, wherein said poly-alkylated benzene stream comprises di-ethylbenzene; and(c) contacting said poly-alkylated benzene stream with said benzene stream in the presence of a selectivated transalkylation catalyst composition under at least partially liquid phase transalkylation conditions to produce a transalkylation effluent stream comprising said ethylbenzene,wherein said selectivated transalkylation catalyst composition is made by the method comprising the step:(i) contacting an untreated transalkylation catalyst composition with a selectivating solution to form said selectivated transalkylation catalyst, said transalkylation catalyst composition comprising a zeolite in acid form and having a framework structure selected from the group consisting of FAU, BEA*, MOR, MWW and mixtures thereof, said selectivating solution comprises water and a cation or an anion of an element in Group 1, Group 2, Group 15, Group 16, or Group 17 of the Periodic Table, wherein said selectivated transalkylation catalyst composition has a higher selectivity to ethylbenzene than the selectivity of said transalkylation catalyst composition that has not been contacted with said selectivating solution when the catalysts are ...

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Номер записи: 90
04-12-2014 дата публикации

Rhenium Promoted Catalyst

Номер: US20140357916A1
Автор: Callum Bailey, Darek Wachowicz, James Butler, Olga Khabashesku
Принадлежит: Fina Technology Inc

A group V metal/rhenium-modified molecular sieve catalyst can be used in hydrocarbon conversion reactions. Embodiments can provide a toluene conversion of at least 30 wt % with selectivity to benzene above 40 wt % and to xylenes above 40 wt % and non-aromatics selectivity of less than 2.0 wt %.

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Номер записи: 91
22-08-2019 дата публикации

PROCESS FOR XYLENE PRODUCTION WITH ENERGY OPTIMIZATION

Номер: US20190256444A1
Автор: ABUDAWOUD RAED, JAZZAR Ahmad A., XU QI, Zhang Zhonglin
Принадлежит: Saudi Arabian Oil Company

A method for producing xylenes from a heavy reformate feed includes the steps of introducing the heavy reformate feed and a hydrogen feed to a dealkylation reactor, reacting the heavy reformate feed with the hydrogen gas in the presence of the dealkylation catalyst in the dealkylation reactor to produce a dealkylation effluent, introducing the dealkylation effluent to a splitter unit, separating the dealkylation effluent into a light gas stream, a toluene stream, a benzene stream, a C9 aromatics stream, a C10+ aromatics stream, and a mixed xylene stream in the splitter unit, introducing the toluene stream, the C9 aromatics stream, and a hydrogen stream into a transalkylation reactor, reacting the toluene stream and the C9 aromatics stream in the presence of the transalkylation catalyst to produce a transalkylation effluent, introducing the transalkylation effluent to the splitter unit, and separating the transalkylation effluent in the splitter unit. 1. A system for producing mixed xylenes from a heavy reformate feed , the system comprising:a feed exchanger, the feed exchanger configured to transfer heat from a mixed xylene stream to the heavy reformate feed to increase a temperature of the heavy reformate feed to produce a hot feed stream, wherein the feed exchanger is a cross process exchanger, wherein the heavy reformate comprises aromatic hydrocarbons with nine or more carbon atoms (C9+ aromatics), wherein the hydrogen feed comprises hydrogen gas, wherein a temperature of the mixed xylene stream is reduced to produce a cooled mixed stream;a mixing point fluidly connected to the feed exchanger, the mixing point configured to mix the hot feed stream and a hydrogen feed to produce a mixed feed;a feed-effluent exchanger fluidly connected to the mixing point, the feed-effluent exchanger configured to transfer heat from a dealkylation effluent to the mixed feed to increase a temperature of the mixed feed to produce a hot mixed feed, wherein the feed-effluent exchanger ...

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Номер записи: 92
13-08-2020 дата публикации

Zeolite composite catalysts for conversion of heavy reformate to xylenes

Номер: US20200254428A1
Автор: Abdullah Mohammed Aitani, BALASAMY RABINDRAN JERMY, Raed Hasan Abudawoud, Sulaiman Saleh Al-Khattaf, Syed Ahmed Ali
Принадлежит: KING FAHD UNIVERSITY OF PETROLEUM AND MINERALS, Saudi Arabian Oil Co

Embodiments of zeolite composite catalysts and methods of producing the zeolite composite catalysts are provided, where the methods comprise dissolving in an alkaline solution a catalyst precursor comprising at least one mesoporous zeolite while heating, stirring, or both to yield a dissolved zeolite solution, where the mesoporous zeolite has a molar ratio of SiO 2 /Al 2 O 3 of at least 30, where the mesoporous zeolite comprises zeolite beta, adjusting the pH of the dissolved zeolite solution, aging the pH adjusted dissolved zeolite solution to yield solid zeolite composite from the dissolved zeolite solution, and calcining the solid zeolite composite to produce the zeolite composite catalyst, where the zeolite composite catalyst has a mesostructure comprising at least one disordered mesophase and at least one ordered mesophase, and where the zeolite composite catalyst has a surface area defined by the Brunauer-Emmett-Teller (BET) analysis of at least 600 m 2 /g.

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Номер записи: 93
20-09-2018 дата публикации

Process for Preparing a Molecular Sieve

Номер: US20180265369A1
Автор: Cao Guang, Lai Wenyih F., Rollman Nicholas S.
Принадлежит:

The present invention provides a mordenite zeolite having a mesopore surface area of greater than 30 m/g and an average primary crystal size as measured by TEM of less than 80 nm, and methods of making the mordenite zeolite. 114.-. (canceled)15. A process for converting a feedstock comprising an organic compound to a conversion product which comprises the step of contacting said feedstock at organic compound conversion conditions with a catalyst comprising a mordenite zeolite , the mordenite zeolite comprising a structure directing agent (SDA) selected from the group consisting of TEA , MTEA and mixtures thereof within its pores , having a mesopore surface area of greater than 30 m/g and comprising agglomerates composed of primary crystallites , wherein the primary crystallites have an average primary crystal size as measured by TEM of less than 80 nm.16. The process of claim 15 , wherein the primary crystallites have an average primary crystal size of less than 80 nm in each of the a claim 15 , b and c crystal vectors as measured by X-ray diffraction.17. The process of claim 15 , wherein at least 90% by number of the primary crystallites have a primary crystal size of less than 80 nm as measured by TEM.18. The process of claim 15 , wherein said primary crystallites have an aspect ratio of less than 2 claim 15 , wherein the aspect ratio is defined as the longest dimension of the crystallite divided by the width of the crystallite claim 15 , where the width of the crystallite is defined as the dimension of the crystallite in the middle of that longest dimension in a dimension orthogonal to that longest dimension claim 15 , as measured by TEM.19. The process of claim 15 , wherein the mordenite zeolite has a mesopore surface area of greater than 40 m/g.20. The process of claim 15 , wherein the ratio of mesopore surface area to the total surface area is greater than 0.05.21. The process of claim 15 , wherein the mordenite zeolite is a calcined mordenite zeolite prepared ...

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Номер записи: 94
20-09-2018 дата публикации

PROCESSES AND APPARATUSES FOR TOLUENE METHYLATION IN AN AROMATICS COMPLEX

Номер: US20180265429A1
Автор: Krimsky David S., Larson Robert B.
Принадлежит:

This present disclosure relates to processes and apparatuses for toluene methylation in an aromatics complex for producing paraxylene. More specifically, the present disclosure relates to processes and apparatuses wherein a toluene methylation zone is integrated within an aromatics complex for producing paraxylene thus allowing no benzene byproduct to be produced. This may be accomplished by incorporating a toluene methylation process into the aromatics complex and recycling the benzene to the transalkylation unit the aromatics complex. 1. A process for producing paraxylene with no benzene byproduct , comprising:{'sub': 9', '10, 'a) passing a lighter aromatic stream containing benzene and a heavier aromatic stream containing C-Caromatic compounds to a transalkylation zone;'}{'sub': '8', 'b) subjecting the lighter aromatic stream and the heavier aromatic stream in the transalkylation zone to transalkylation conditions including the presence of a first catalyst to provide a transalkylation product stream having a greater concentration of toluene to Caromatics;'}{'sub': 8', '9+, 'c) separating by fractionation from the transalkylation product stream a first boiling fraction comprising benzene, a second boiling fraction comprising toluene, a third boiling fraction comprising Caromatics and a fourth boiling fraction comprising Caromatics;'}d) recycling at least a portion of the benzene from the transalkylation product stream back to the transalkylation zone;e) passing at least a portion of the second boiling fraction from steps c, g and i and a methanol stream to a toluene methylation zone operating under toluene methylation conditions to produce a toluene methylation product stream;f) separating by fractionation from the toluene methylation product stream the same fractions described in step c;{'sub': 8', '8, 'g) subjecting at least a portion of the third boiling fraction comprising Caromatics of steps c, g and i to a separation zone to selectively remove a para-xylene ...

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Номер записи: 95
20-09-2018 дата публикации

PROCESSES AND APPARATUSES FOR OLEFIN SATURATION IN AN AROMATICS COMPLEX

Номер: US20180265791A1
Автор: Kalra Jalesh, Noe Robert J. L.
Принадлежит:

Process and apparatuses for producing benzene and para-xylene from a reformate stream is provided. The process comprises separating the reformate stream to provide a first stream comprising Cand lighter hydrocarbons and a second stream comprising aromatic hydrocarbons. The second steam is provided to a reformate splitter to provide a reformate bottoms stream comprising C aromatic hydrocarbons and a reformate overhead stream comprising C aromatic hydrocarbons. The reformate overhead stream is passed to an aromatics extraction unit to provide an aromatics extract stream comprising benzene and toluene and a raffinate stream comprising non-aromatic hydrocarbons. The reformate bottoms stream and one of the first stream and the raffinate stream is passed to an olefin reduction zone, wherein the reformate bottoms stream and one of the first stream and the raffinate stream are contacted with an olefin saturation catalyst under olefin saturation conditions to produce an olefin-treated reformate stream. 1. A process for producing benzene and para-xylene from a reformate stream , wherein the process comprises:{'sub': '4', 'a) separating the reformate stream to provide a first stream comprising Cand lighter hydrocarbons and a second stream comprising aromatic hydrocarbons;'}{'sub': 8+', '7−, 'b) providing the second steam to a reformate splitter to provide a reformate bottoms stream comprising C aromatic hydrocarbons and a reformate overhead stream comprising C aromatic hydrocarbons;'}c) passing the reformate overhead stream to an aromatics extraction unit to provide an aromatics extract stream comprising benzene and toluene and a raffinate stream comprising non-aromatic hydrocarbons; andd) passing the reformate bottoms stream and one of the first stream and the raffinate stream to an olefin reduction zone, wherein the reformate bottoms stream and one of the first stream and the raffinate stream are contacted with an olefin saturation catalyst under olefin saturation conditions ...

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Номер записи: 96
04-11-2021 дата публикации

METHODS OF HEAVY REFORMATE CONVERSION INTO AROMATIC COMPOUNDS

Номер: US20210340080A1
Автор: Abudawoud Raed Hasan, Al-Zahrani Ibrahim M., Benavent Vicente J. Margarit, Canos Avelino Corma, Ovejero M. Teresa Portilla, Sanchez M. Cristina Martinez, Villalba M. Teresa Navarro
Принадлежит:

Method of making BTX compounds including benzene, toluene, and xylene, including feeding heavy reformate to a reactor containing a composite zeolite catalyst. The composite zeolite catalyst includes a mixture of layered mordenite (MOR-L) comprising a layered or rod-type morphology with a layer thickness less than 30 nm and ZSM-5. The MOR-L, the ZSM-5, or both include one or more impregnated metals. The method further includes producing the BTX compounds by simultaneously performing transalkylation and dealkylation of the heavy reformate in the reactor. The composite zeolite catalyst is able to simultaneously catalyze both the transalkylation and dealkylation reactions. 1. A composite zeolite catalyst ,the composite zeolite catalyst comprising a mixture of layered mordenite (MOR-L) and ZSM-5, where:the MOR-L or both the MOR-L and ZSM-5 comprise one or more impregnated metals,the MOR-L comprises a rod morphology with a smallest dimension less than 28 nm,{'sup': '2', 'the MOR-L without the impregnated metals comprises an external surface area greater than 120 m/g, and'}the MOR-L has a molar ratio of silicon to aluminum (Si/Al) from 4:1 to 8:1.2. The composite zeolite catalyst of claim 1 , where the one or more impregnated metals are selected from the group consisting of molybdenum claim 1 , chromium claim 1 , platinum claim 1 , nickel claim 1 , tungsten claim 1 , palladium claim 1 , ruthenium claim 1 , gold claim 1 , rhenium claim 1 , rhodium claim 1 , or combinations thereof and their respective oxides.3. The composite zeolite catalyst of claim 1 , where the one or more impregnated metals comprises rhenium.4. The composite zeolite catalyst of claim 1 , where the MOR-L claim 1 , the ZSM-5 claim 1 , or both the MOR-L and ZSM-5 comprise up to 20 wt. % of the one or more impregnated metals.5. The composite zeolite catalyst of claim 1 , where the MOR-L is impregnated with 0.25 to 0.5 wt. % rhenium.6. The composite zeolite catalyst of claim 1 , where the ZSM-5 is ...

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Номер записи: 97
28-09-2017 дата публикации

Aromatics Production Process

Номер: US20170275218A1
Автор: Cao Chunshe J., Claudel Stephane, Fernandez Celia, Knob Kevin J., LEFLOUR Thierry, Molinier Michel, Pigourier Jerome, Prevost Isabelle, Rault Jacques, Stanley Dennis J., Vander Pol Terri S., Zheng Xiaobo
Принадлежит: ExxonMobil Chemical Patents Inc.

In a process for producing para-xylene, at least one feed comprising C aromatic hydrocarbons is supplied to a dividing wall distillation column to separate the feed into a C aromatic hydrocarbon-containing stream, a Caromatic hydrocarbon-containing stream and a C aromatic hydrocarbon-containing stream. At least part of the Caromatic hydrocarbon-containing stream is then supplied to a para-xylene recovery unit to recover para-xylene from the Caromatic hydrocarbon-containing stream and produce a para-xylene depleted stream. The para-xylene depleted stream is contacted with a xylene isomerization catalyst in a xylene isomerization zone under conditions effective to isomerize xylenes in the para-xylene depleted stream and produce an isomerized stream, which is then at least partially recycled to the para-xylene recovery unit. 1. A process for producing para-xylene and benzene , the process comprising:{'sub': 6+', '7−', '8', '9+, '(a2) supplying a feed comprising a mixture of C aliphatic and aromatic hydrocarbons to a dividing wall distillation column to separate the feed into a C hydrocarbon-containing stream, a Chydrocarbon-containing stream and a C hydrocarbon-containing stream;'}{'sub': 7−', '7−, '(b2) removing at least part of the aliphatic hydrocarbons from the C hydrocarbon-containing stream to produce a C aromatic hydrocarbon-enriched stream;'}{'sub': 7−', '7−, '(c2) supplying at least part of the C aromatic-enriched stream to a separation unit to separate the C aromatic-enriched stream into a benzene-containing stream and a toluene-containing stream;'}{'sub': 8', '8, '(d2) supplying at least part of the Chydrocarbon-containing stream to a para-xylene recovery unit to recover para-xylene from the Chydrocarbon-containing stream and produce apara-xylene depleted stream;'}(e2) contacting at least part of the para-xylene depleted stream with a xylene isomerization catalyst in a xylene isomerization zone under conditions effective to isomerize xylenes in the para- ...

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Номер записи: 98
27-09-2018 дата публикации

PROCESSES FOR INCREASING THE OVERALL AROMATICS AND XYLENES YIELD IN AN AROMATICS COMPLEX

Номер: US20180273444A1
Автор: Couch Keith A., Frey Stanley J., Whitchurch Patrick C.
Принадлежит:

The present subject matter describes processes for increasing overall aromatics and xylenes yield in an aromatics complex. More specifically, the process for increasing overall aromatics and xylenes yield in an aromatics complex accomplishes the increased yields by incorporating an A-Aisomerization step into the aromatics complex. This isomerization integration increases the para-xylene. 1. A process for increasing overall xylenes yield in an aromatics complex , the process comprising the steps of:{'sub': 7', '8', '10', '10, 'separating an aromatics-rich reformate into a first hydrocarbon stream comprising C− hydrocarbons, a second hydrocarbon stream comprising C-Caromatics, and a third hydrocarbon stream comprising C+ aromatics;'}{'sub': 8', '10', '8', '10, 'isomerizing the second hydrocarbon stream comprising C-Caromatics to produce a C-Cisomerization product stream;'}{'sub': 8', '10, 'passing the C-Cisomerization product stream to a napthene dehydrogenation zone to produce a napthene dehydrogenation zone product stream;'}{'sub': 7', '8, 'separating the napthene dehydrogenation zone product stream into a first napthene dehydrogenation zone product stream comprising C− hydrocarbons and a second naphthene dehydrogenation zone product stream comprising C+ aromatics; and'}{'sub': '8', 'passing the second napthene dehydrogenation zone product stream comprising C+ aromatics to a xylenes recovery section or transalkylation zone.'}2. The process of claim 1 , wherein the step of isomerizing comprises using an isomerization catalyst comprising a 12-member ring zeolite or 10-member ring zeolite claim 1 , a binder claim 1 , and a platinum-group metal component.3. The process of claim 1 , wherein the step of isomerizing comprises a temperature range of about 250° C. to about 450° C.4. The process of claim 1 , wherein the step of isomerizing comprises a pressure range of about 3 bar to about 15 bar.5. The process of claim 1 , wherein the napthene dehydrogenation zone comprises ...

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Номер записи: 99
18-12-2014 дата публикации

Process of Producing Cyclohexylbenzene

Номер: US20140371498A1
Автор: Christopher L. Becker, James R. Lattner, Jihad M. Dakka, Keith H. Kuechler, Tan-Jen Chen
Принадлежит: ExxonMobil Chemical Co

In a process for producing cyclohexylbenzene, benzene is contacted with hydrogen under hydroalkylation conditions effective to form a first effluent stream comprising cyclohexylbenzene, cyclohexane, methylcyclopentane, and unreacted benzene. At least a portion of the first effluent stream is contacted with a dehydrogenation catalyst under dehydrogenation conditions to convert at least a portion of the cyclohexane to benzene thereby forming a second effluent stream. The amount of methylcyclopentane in the second effluent stream is different by no more than 65% of the total amount of the portion of the first effluent stream, said amounts being on a weight basis. A methylcyclopentane-containing stream is removed from either the first or the second effluent stream and at least a portion of the second effluent stream containing benzene is recycled to the hydroalkylation step.

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Номер записи: 100