Heavy alkylbenzene transalkylation operating cost reduction

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.

Process for the preparation of a catalyst support

Process for preparing a catalyst support which process comprises a) mixing pentasil zeolite having a bulk silica to alumina molar ratio in the range of from 20 to 150 with water, a silica source and an alkali metal salt, b) extruding the mixture obtained in step (a), c) drying and calcining the extrudates obtained in step (b), d) subjecting the calcined extrudates obtained in step (c) to ion exchange to reduce the alkali metal content, and e) drying the extrudates obtained in step (d); process for preparing a catalyst by furthermore impregnating such support with platinum in an amount in the range of from 0.001 to 0.1 wt % and tin in an amount in the range of from 0.01 to 0.5 wt %, each on the basis of total catalyst; ethylbenzene dealkylation catalyst obtainable thereby and a process for dealkylation of ethylbenzene which process comprises contacting feedstock containing ethylbenzene with such catalyst.

Process for producing cumene

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.

COMBINED HEAVY REFORMATE DEALKYLATION-TRANSALKYLATION PROCESS FOR MAXIMIZING XYLENES PRODUCTION

A method of forming mixed xylenes from a heavy reformate using a dealkylation-transalkylation system includes the step of introducing both a heavy reformate containing methyl ethyl benzenes and tri-methyl benzenes and that is sufficiently free of toluene and a hydrogen-containing material into the dealkylation stage such that the heavy reformate and the hydrogen-containing material intermingle and contact the hydrodealkylation catalyst. The dealkylation-transalkylation system includes dealkylation, non-aromatic product gas separations and transalkylation stages. 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 includes mixed xylenes. 1. A method of forming mixed xylenes from a heavy reformate using a dealkylation-transalkylation system , the method comprising the steps of:introducing both the heavy reformate and a hydrogen-containing material into a dealkylation stage of the dealkylation-transalkylation system such that the heavy reformate and the hydrogen-containing material intermingle and contact a hydrodealkylation catalyst, where the dealkylation stage contains the hydrodealkylation catalyst, where the heavy reformate comprises a significant amount of both methyl ethyl benzenes and tri-methyl benzenes and is substantially free of toluene by weight, and where the hydrogen-containing material comprises hydrogen;operating the dealkylation stage such that toluene forms from the reaction of methyl ethyl benzenes and hydrogen in the presence of the hydrodealkylation catalyst and such that a dealkylation stage product is produced, where the dealkylation stage product comprises toluene, tri-methyl benzenes and non-aromatic product gas;operating the non-aromatic ...

ZSM-5, ITS PREPARATION AND USE IN ETHYLBENZENE DEALKYLATION

A new configuration of ZSM-5 is provided whereby the crystals have a higher average silica to alumina ratio at the edges of each crystallite than in the centre as determined from a narrow slit line scan profile obtained from SEM/EDX or TEM/EDX elemental analysis. Such ZSM-5 crystals are obtained by a preparation process using L-tartaric acid. The new configuration ZSM-5 provides significantly reduced xylene losses in ethylbenzene dealkylation, especially when combined with silica as binder, and one or more hydrogenation metals selected from platinum, tin, lead, silver, copper, and nickel. 1. A ZSM-5 crystals which have a higher average SAR at the edge of each crystallite than at the centre , as determined via SEM/EDX or TEM/EDX elemental analysis.2. A ZSM-5 crystals as claimed in claim 1 , wherein the ratio of the average SAR at the edge of each crystallite to the average SAR at the centre of the crystallite is at least 1.15 claim 1 , preferably at least 1.25.3. A ZSM-5 crystals as claimed in claim 1 , wherein the ratio is at most 3 claim 1 , preferably at most 2.4. A ZSM-5 crystals as claimed in claim 1 , wherein the slope of a second order polynomial fitted to the SAR values between the two edge SAR maxima claim 1 , expressed as −y′ claim 1 , is at least 2 claim 1 , preferably at least 3.5. A ZSM-5 crystals as claimed in claim 1 , wherein the slope of a second order polynomial fitted to the SAR values between the two edge SAR maxima claim 1 , expressed as −y′ claim 1 , is at most 6 claim 1 , preferably at most 4.6. A catalyst composition comprising ZSM-5 crystals which have a higher average SAR at the edge of each crystallite than at the centre claim 1 , as determined via SEM/EDX or TEM/EDX elemental analysis claim 1 , which also contains a silica binder in an amount in the range of from 30 to 80 wt % claim 1 , based on the total of ZSM-5; and silica.7. A catalyst composition as claimed in claim 6 , which also contains a hydrogenation metal selected from platinum ...

Method of producing monocyclic aromatic hydrocarbons

A method of producing monocyclic aromatic hydrocarbons includes bringing a feedstock oil having a 10 vol % distillation temperature of 140° C. or higher and a 90 vol % distillation temperature of 380° C. or lower, into contact with a catalyst for monocyclic aromatic hydrocarbon production containing a crystalline aluminosilicate, in which a content ratio of monocyclic naphthenobenzenes in the feedstock oil is adjusted to 10 mass % to 90 mass %, by mixing a hydrocarbon oil A having a 10 vol % distillation temperature of 140° C. or higher and a 90 vol % distillation temperature of 380° C. or lower with a hydrocarbon oil B containing more monocyclic naphthenobenzenes than the hydrocarbon oil A.

Catalyst for metathesis of ethylene and 2-butene and/or double bond isomerization

A process for the double-bond isomerization of olefins is disclosed. The process may include contacting a fluid stream comprising olefins with a fixed bed comprising an activated basic metal oxide isomerization catalyst to convert at least a portion of the olefin to its isomer. The isomerization catalysts disclosed herein may have a reduced cycle to cycle deactivation as compared to conventional catalysts, thus maintaining higher activity over the complete catalyst life cycle.

MWW TYPE ZEOLITE, METHOD FOR PRODUCING SAME, AND CRACKING CATALYST

Provided are the following: an MWW type zeolite which has many Brønsted acid sites when in the form of a proton type and which is highly suitable as a cracking catalyst for cumene; a method for producing same; and an application of same. The present invention provides an MWW type zeolite in which the ratio (B/A) of the peak intensity (B) attributable to tetracoordinate aluminum relative to the peak intensity (A) attributable to hexacoordinate aluminum is 2 or more in Al MAS NMR, when measured as an ammonium type. The present invention also provides a method for producing an MWW type zeolite, the method having a step for carrying out a hydrothermal synthesis reaction in the presence of: a seed crystal of an MWW type zeolite containing no organic structure-directing agent; and a reaction mixture containing a silica source, an alumina source, an alkali source, an organic structure-directing agent, and water. The reaction mixture satisfies the following molar ratio: X/SiO<0.15 (here, X denotes the number of moles of the organic structure-directing agent). 1. An MWW-type zeolite wherein a ratio (B/A) of a peak intensity (B) attributable to tetracoordinate aluminum to a peak intensity (A) attributable to hexacoordinate aluminum is 2 or more in Al MAS NMR as measured in the form of an ammonium type.2. The MWW-type zeolite according to claim 1 , wherein an amount of Brønsted acid site with a adsorption heat of ammonia of 106 kJ/mol or more is 0.5 mmol/g or more.3. The MWW-type zeolite according to claim 1 , wherein a micropore volume is 0.07 cm/g or more and 0.2530 cm/g or less.4. The MWW-type zeolite according to claim 1 , wherein SiO/AlOmolar ratio is 17 or more and 37 or less.5. The MWW-type zeolite according to claim 1 , wherein when the MWW-type zeolite is subjected to X-ray diffraction measurement claim 1 , a peak is observed in at least one range below:2θ=6.4° to 7.4°, 13.5° to 14.5°, 24.1° to 25.1°, 24.7 to 25.7°, 27.1 to 28.1°, 28.0° to 29.0°, 28.6° to 29.6°, and ...

Systems and Methods for Producing Naphthalenes and Methylnaphthalenes

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

High Density Cyclic Fuels Derived From Linear Sesquiterpenes

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

Processes for Converting Aromatic Hydrocarbons via Alkyl-Demethylation

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+ ...

Transalkylation Processes for Converting Aromatic Hydrocarbons Comprising Alkyl-Demethylation

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.

Process for Xylenes Isomerization

A process for the isomerization of a para-xylene depleted, meta-xylene rich stream under at least partially liquid phase conditions using ZSM-23 with an external surface area of at least 75 m/g (indicating a small crystallite size), and a SiO/AlOratio between 15 and 75 that produces a higher than equilibrium amount of para-xylene, i.e., more than about 24 wt % of para-xylene, based on the total amount of xylenes. 1. A process for producing para-xylene comprising contacting a feed stream comprising meta-xylene with a catalyst comprising ZSM-23 having a SiO/AlOratio between 15 and 75 and an external surface area of at least 75 m/g under at least partially liquid phase conditions effective to produce a first isomerized stream comprising para-xylene having a para-xylene content of more than 24 wt % , based on the total amount of xylenes in the first isomerized stream.2. The process of claim 1 , wherein the catalyst comprises ZSM-23 having SiO/AlOratio between 15 and 50 and an external surface area of at least 90 m/g.3. The process of claim 1 , wherein the catalyst is self-bound.4. The process of claim 1 , wherein the feed stream consists essentially of meta-xylene.5. The process of claim 1 , wherein the liquid phase conditions comprise a temperature from 400° F. (204° C.) to 1 claim 1 ,000° F. (538° C.) claim 1 , a pressure of from 0 to 1 claim 1 ,000 psig claim 1 , a weight hourly space velocity (WHSV) of from 0.5 to 100 hr.6. The process of claim 5 , wherein the liquid phase conditions comprise a temperature from 482° F. (250° C.) to 572° F. (300° C.) claim 5 , a pressure from 350 psig (2.41 MPa) to 500 psig (3.45 MPa) claim 5 , and a weight hourly space velocity (WHSV) from 0.5 to 10 hr.7. The process of claim 1 , wherein said feed stream comprising meta-xylene is produced by:{'sub': '8', '(a) providing a Caromatic hydrocarbon mixture comprising para-xylene, ortho-xylene and meta-xylene to an ortho-xylene splitter;'}(b) recovering a first stream comprising para- ...

Catalyst System and Use in Heavy Aromatics Conversion Processes

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.

Heavy Aromatics Conversion Processes and Catalyst Compositions Used Therein

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 ...

Heavy Aromatics Conversion Processes and Catalyst Compositions Used Therein

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 ...

Xylene Production Processes and Systems

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 ...

Aromatics Production Process

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 Caromatic 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 , the process comprising:{'sub': 6+', '7−', '8', '9+, '(a1) supplying at least one feed comprising C aromatic hydrocarbons to a dividing wall distillation column to separate the feed into a Caromatic hydrocarbon-containing stream, a Caromatic hydrocarbon-containing stream and a C aromatic hydrocarbon-containing stream;'}{'sub': 8', '8, '(b1) supplying at least part of the Caromatic hydrocarbon-containing stream to a para-xylene recovery unit to recover para-xylene from the Caromatic hydrocarbon-containing stream and produce a para-xylene depleted stream;'}(c1) 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-xylene depleted stream and produce an isomerized stream; and(d1) recycling at least part of the isomerized stream to the para-xylene recovery unit.2. The process of claim 1 , wherein the at least one feed to (a1) comprises a mixture of C aromatic and aliphatic hydrocarbons produced by removing C hydrocarbons from a reformate stream.3. The process of and further ...

Transalkylation System

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.

AROMATIC TRANSFORMATION USING UZM-44 ALUMINOSILICATE ZEOLITE

A new family of aluminosilicate zeolites designated UZM-44 has been synthesized. These zeolites are represented by the empirical formula. 2. The process of wherein the microporous crystalline zeolitic catalytic composite is thermally stable up to a temperature of greater than 600° C.3. The process of wherein the microporous crystalline zeolitic catalytic composite has a micropore volume as a percentage of total pore volume of less than 60%.4. The process of wherein the microporous crystalline zeolitic catalytic composite has micropore volume of less than 0.155 mL/g.5. The process of wherein the microporous crystalline zeolitic catalytic composite has micropore volume of less than 0.150 mL/g.6. The process of wherein the microporous crystalline zeolitic catalytic composite exhibits no feature at 200-300 Å on a dV/dlog D versus pore diameter plot of differential volume of nitrogen adsorbed as a function of pore diameter.7. The process of wherein the microporous crystalline zeolitic catalytic composite exhibits adsorption occurring at greater than 450 Å on a dV/dlog D versus pore diameter plot of differential volume of nitrogen adsorbed as a function of pore diameter.8. The process of wherein the differential volume of nitrogen adsorbed by the catalytic composite at a pore diameter of 475 Å is greater than 0.1 mL N/gÅ on a dV/dlog D versus pore diameter plot of differential volume of nitrogen adsorbed as a function of pore diameter.9. The process of wherein the differential volume of nitrogen adsorbed by the catalytic composite at pore diameters greater than 475 Å is greater than 0.1 mL N/gÅ on a dV/dlog D versus pore diameter plot of differential volume of nitrogen adsorbed as a function of pore diameter.10. The process of wherein the first aromatic is benzene.11. The process of wherein the first aromatic is benzene and the second aromatic is toluene or xylene.12. The process of further comprising removing an effluent comprising the second aromatic claim 1 , ...

DISSOLVED OIL REMOVAL FROM QUENCH WATER OF GAS CRACKER ETHYLENE PLANTS

A method for removing dissolved hydrocarbons from water may comprise: cracking a mixed hydrocarbon stream in a cracking furnace to produce a cracked gas effluent; quenching the cracked gas effluent in a quench water tower with quench water to produce a quenched gas stream and a spent quench water stream comprising water, tars, heavy aromatic hydrocarbons, gasoline, dissolved oil, and dispersed oil; feeding the spent quench water stream to a liquid-liquid extraction unit wherein the liquid-liquid extraction unit removes at least a portion of the dissolved oil and produce an extracted effluent stream. 1. A method for removing dissolved hydrocarbons from water comprising:mixing a gaseous hydrocarbon stream with a clean steam stream to produce a mixed hydrocarbon stream;cracking the mixed hydrocarbon stream in a cracking furnace to produce a cracked gas effluent;quenching the cracked gas effluent in a quench water tower with quench water to produce a quenched gas stream and a spent quench water stream comprising water, tars, heavy aromatic hydrocarbons, gasoline, dissolved oil, and dispersed oil;decanting the spent quench water stream to remove at least a portion of the tars, the heavy aromatic hydrocarbons, and the gasoline from the spent quench water stream to produce a decanted spent quench water stream;feeding the decanted spent quench water stream to a dispersed oil removal unit wherein the dispersed oil removal unit removes at least a portion of the dispersed oil from the decanted spent quench water to produce a coalesced quench water stream and wherein the dispersed oil removal unit is selected from the group consisting of a filter coalescer unit, dispersed oil extractor unit, induced gas floatation unit, and combinations thereof; andfeeding the coalesced quench water stream to a liquid-liquid extraction unit wherein the liquid-liquid extraction unit removes at least a portion of the dissolved oil and produce an extracted effluent stream;feeding the extracted ...

Process for the Production of Xylenes

In a process for producing para-xylene, a feed stream comprising C aromatic hydrocarbons is separated into a Caromatic hydrocarbon-containing stream, a Caromatic hydrocarbon-containing stream, and a C aromatic hydrocarbon-containing stream. The C aromatic hydrocarbon-containing stream is contacted with a methylating agent to convert toluene to xylenes and produce a methylated effluent stream. Ethylbenzene is removed from the Caromatic hydrocarbon-containing stream, para-xylene is recovered from the ethylbenzene-depleted Caromatic hydrocarbon-containing stream and the methylated effluent stream in a para-xylene recovery section to produce a para-xylene depleted stream, which is then contacted with a xylene isomerization catalyst under liquid phase conditions effective to isomerize xylenes in the para-xylene depleted stream and produce an isomerized stream. The C-containing stream with a transalkylation catalyst under conditions effective to convert C-aromatics to C-aromatics and produce a transalkylated stream, which is recycled together with the isomerized stream to the para-xylene recovery section.

PROCESS FOR THE PREPARATION OF A CATALYST SUPPORT

Process for preparing a catalyst support which process comprises a) mixing pentasil zeolite having a bulk silica to alumina molar ratio in the range of from 20 to 150 with water, a silica source and an alkali metal salt, b) extruding the mixture obtained in step (a), c) drying and calcining the extrudates obtained in step (b), d) subjecting the calcined extrudates obtained in step (c) to ion exchange to reduce the alkali metal content, and e) drying the extrudates obtained in step (d); process for preparing a catalyst by furthermore impregnating such support with platinum in an amount in the range of from 0.001 to 0.1 wt % and tin in an amount in the range of from 0.01 to 0.5 wt %, each on the basis of total catalyst; ethylbenzene dealkylation catalyst obtainable thereby and a process for dealkylation of ethylbenzene which process comprises contacting feedstock containing ethylbenzene with such catalyst. 1. An ethylbenzene dealkylation catalyst , containing; a) mixing pentasil zeolite having a bulk silica to alumina molar ratio in the range of from 20 to 150 with water, a silica source and an alkali metal salt;', 'b) extruding the mixture obtained in step (a);', 'c) drying and calcining the extrudates obtained in step (b);', 'd) treating the extrudates obtained in step (c) with an aqueous solution of fluorosilicate salt to provide fluorosilicate-treated extrudates;', 'e) subjecting the fluorosilicate-treated extrudates obtained in step (d) to ion exchange with an aqueous ammonium containing solution to reduce the alkali metal content; and', 'f) drying the extrudates obtained in step (e); and, 'a support obtainable by a process which comprisesplatinum in an amount in the range of from 0.001 to 0.1 wt % and tin in an amount in the range of from 0.01 to 0.5 wt %, each on the basis of total catalyst.2. An ethylbenzene dealkylation catalyst as recited in claim 1 , wherein the silica source is selected from the group consisting of powder form silica claim 1 , silica sol ...

INTEGRATED PROCESS FOR OPTIMUM PRODUCTION OF PARA-XYLENE

A method of producing p-xylene comprising the steps of separating the reformate feed in the reformate splitter to produce a benzene stream, a combined heavy stream, a xylene stream, and a toluene stream, converting the C9+ aromatic hydrocarbons in the presence of a dealkylation catalyst in the dealkylation reactor to produce a dealkylation effluent, separating the dealkylation effluent in the dealkylation splitter to produce a C9 stream and a C10+ stream, reacting the C9 stream, the toluene stream, the benzene stream, and the hydrogen stream in the presence of a transalkylation catalyst in the transalkylation reactor to produce a transalkylation effluent, separating the p-xylenes from the xylene stream in the p-xylene separation unit to produce a p-xylene product and a p-xylene depleted stream, converting the m-xylene and o-xylene in the p-xylene depleted stream in the isomerization unit to produce an isomerization effluent. 1. A system for producing para-xylene (p-xylene) from a reformate feed , the system comprising:a reformate splitter, the reformate splitter configured to separate the reformate feed, wherein the reformate feed comprises aromatic hydrocarbons, wherein the aromatic hydrocarbons are selected from the group consisting of benzene, toluene, mixed xylenes, carbon-nine plus (C9+) aromatic hydrocarbons, and combinations of the same, wherein the reformate splitter produces a light gases stream, a combined heavy stream, a benzene stream, a xylene stream, and toluene stream, wherein the C9 aromatics stream comprises C9 aromatic hydrocarbons, and wherein the xylene stream comprises mixed xylenes, wherein the mixed xylenes comprises p-xylenes, and wherein the mixed light aromatics stream comprises toluene;a dealkylation reactor fluidly connected to the reformate splitter, the dealkylation reactor configured to convert the C9+ aromatic hydrocarbons to carbon-six (C6) to carbon-eight (C8) aromatic hydrocarbons in the presence of a dealkylation catalyst to ...

MODIFIED ULTRA-STABLE Y (USY) ZEOLITE CATALYST FOR DEALKYLATION OF AROMATICS

The present disclosure relates to a process for the hydrodealkylation of aromatic rich hydrocarbon streams to produce benzene, toluene and mixed xylenes (BTX), with high selectivity towards high value xylenes. The process uses catalysts containing a framework-substituted zirconium and/or titanium and/or hafnium-modified ultra-stable Y (USY) type zeolite. 1. A process for hydrodealkylating a hydrocarbon feed to produce a dealkylated product , the process comprising the step of reacting the hydrocarbon feed with a hydrogen feed in the presence of a dealkylation catalyst , wherein the hydrocarbon feed comprises aromatic hydrocarbons with nine or more carbon atoms (C9+ aromatics; and wherein the dealkylation catalyst is a framework-substituted ultra-stable Y (USY)-type zeolite in which a portion of aluminum atoms constituting a zeolite framework thereof is substituted with zirconium atoms and/or titanium and/or hafnium atoms.2. The process according to claim 1 , further comprising the steps of:introducing a hydrocarbon feed and a hydrogen feed to a dealkylation reactor, wherein the dealkylation reactor comprises a dealkylation catalyst; andreacting the hydrocarbon feed with the hydrogen feed in the presence of the dealkylated catalyst to produce a dealkylated product.3. The process according to claim 1 , wherein the framework-substituted USY-type zeolite in the catalyst comprises zirconium atoms and titanium atoms.4. The process according to claim 1 , wherein the framework-substituted USY-type zeolite in the catalyst comprises from about 0.1 to about 5% by mass zirconium and/or titanium and/or hafnium atoms claim 1 , each calculated as the oxide basis.5. The process according to claim 1 , wherein the framework-substituted USY-type zeolite in the catalyst further includes a support comprising inorganic oxides selected from the group consisting of alumina claim 1 , silica-alumina and combinations thereof.6. The process according to claim 1 , wherein the framework- ...

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

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

SYSTEMS AND METHODS RELATED TO THE SYNGAS TO OLEFIN PROCESS

Disclosed herein is a system and method capable of producing butadiene from a product stream. 1. A method comprising the steps of:a) providing a first product stream comprising a C2-C3 hydrocarbon stream, a C4 hydrocarbon stream comprising butane and butene, and a C5+ hydrocarbon stream;b) separating at least a portion of the C2-C3 hydrocarbon stream from the first product stream;c) separating at least a portion of the C4 hydrocarbon stream comprising butane and butene from the first product stream;d) separating at least a portion of the C5+ hydrocarbon stream from the first product stream; ande) converting at least a portion of the butene in the C4 hydrocarbon stream to butadiene.2. The method of claim 1 , wherein the first product stream comprises at least about 1 wt % of the C2-C3 hydrocarbon stream.3. The method of claim 1 , wherein the first product stream comprises at least about 1 wt % of the C4 hydrocarbon stream comprising butane and butene.4. The method of claim 1 , wherein the first product stream comprises at least about 1 wt % of the C5+ hydrocarbon stream.5. The method of claim 1 , wherein the first product stream comprises from about 10 wt % to about 30 wt % of the C2-C3 hydrocarbon stream.6. The method of claim 1 , wherein the first product stream comprises from about 5 wt % to about 15 wt % of the C4 hydrocarbon stream comprising butane and butene.7. The method of claim 1 , wherein the first product stream comprises from about 30 wt % to about 50 wt % of the C5+ hydrocarbon stream.8. The method of claim 1 , wherein steps b) claim 1 , c) claim 1 , and d) occur simultaneously.9. The method of claim 1 , wherein the method further comprises prior to step e) claim 1 , the step of converting at least a portion of the butane in the C4 hydrocarbon stream to butene.10. The method of claim 1 , wherein the method further comprises after step b) the step of separating C2-C3 olefins from the C2-C3 hydrocarbon stream.11. The method of claim 1 , wherein the C5+ ...

PROCESS FOR PRODUCING BENZENE FROM C5-C12 HYDROCARBON MIXTURE

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 ...

INTEGRATED PROCESS FOR MAXIMIZING PRODUCTION OF PARA-XYLENE FROM FULL REFORMATE

A method of producing p-xylene, the method comprising the steps of converting the C9+ aromatic hydrocarbons and the hydrogen gas in the presence of a dealkylation catalyst to produce a dealkylation effluent, separating the dealkylation effluent to produce a carbon-nine (C9) aromatics stream, a xylene stream, and a toluene stream, separating the p-xylenes from the xylene stream in the p-xylene separation unit to produce a p-xylene product and a p-xylene depleted stream, converting the m-xylene and o-xylene in the p-xylene depleted stream in the isomerization unit to produce an isomerization effluent, reacting the C9 aromatics stream and the hydrogen stream in the presence of a transalkylation catalyst in the transalkylation reactor to produce a transalkylation effluent, separating the C6 to C9+ aromatic hydrocarbons in the isomerization effluent and the transalkylation effluent in the splitter column to produce a benzene recycle, a toluene recycle, a xylene recycle and a C9+ recycle. 1. A method of producing p-xylene , the method comprising the steps of:introducing a reformate feed to a dealkylation reactor, the reformate feed comprises aromatic hydrocarbons, wherein the aromatic hydrocarbons are selected from the group consisting of benzene, toluene, mixed xylenes, carbon-nine plus (C9+) aromatic hydrocarbons, and combinations of the same;introducing a hydrogen feed to the dealkylation reactor, wherein the hydrogen feed comprises hydrogen gas, wherein the dealkylation reactor is configured to convert C9+ aromatic hydrocarbons to carbon-six (C6) to carbon-eight (C8) aromatic hydrocarbons;converting the C9+ aromatic hydrocarbons and the hydrogen gas in the presence of a 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 effluent comprises aromatic hydrocarbons such that an amount ...

INTEGRATED PROCESS FOR OPTIMUM PRODUCTION OF PARA-XYLENE

A method of producing p-xylene comprising the steps of separating the reformate feed in the reformate splitter to produce a benzene stream, a combined heavy stream, a xylene stream, and a toluene stream, converting the C9+ aromatic hydrocarbons in the presence of a dealkylation catalyst in the dealkylation reactor to produce a dealkylation effluent, separating the dealkylation effluent in the dealkylation splitter to produce a C9 stream and a C10+ stream, reacting the C9 stream, the toluene stream, the benzene stream, and the hydrogen stream in the presence of a transalkylation catalyst in the transalkylation reactor to produce a transalkylation effluent, separating the p-xylenes from the xylene stream in the p-xylene separation unit to produce a p-xylene product and a p-xylene depleted stream, converting the m-xylene and o-xylene in the p-xylene depleted stream in the isomerization unit to produce an isomerization effluent. 1. A method of producing para-xylene (p-xylene) , the method comprising the steps of:introducing a reformate feed to reformate splitter, the reformate splitter configured to separate the reformate feed, the reformate feed comprises aromatic hydrocarbons, wherein the aromatic hydrocarbons are selected from the group consisting of benzene, toluene, mixed xylenes, carbon-nine plus (C9+) aromatic hydrocarbons, and combinations of the same;separating the reformate feed in the reformate splitter to produce a light gases stream, a benzene stream, a combined heavy stream, a xylene stream, and a toluene stream, wherein the combined heavy stream comprises C9+ aromatic hydrocarbons, and wherein the xylene stream comprises mixed xylenes, wherein the mixed xylenes comprises p-xylenes, and wherein the toluene stream comprises toluene;introducing the combined heavy stream to a dealkylation reactor;introducing a hydrogen feed to the dealkylation reactor, wherein the hydrogen feed comprises hydrogen gas, wherein the dealkylation reactor is configured to the ...

CATALYST COMPOSITIONS COMPRISING SMALL SIZE MOLECULAR SIEVES CRYSTALS DEPOSITED ON A POROUS MATERIAL

A catalyst composition contains an inorganic porous material with pore diameters of at least 2 nm and of crystals of molecular sieve. The crystals of molecular sieve have an average diameter, measured by scanning electron microscopy, not bigger than 50 nm. The catalyst composition has a concentration of acid sites ranges from 50 to 1200 μmol/g measured by TPD NH3 adsorption. An XRD pattern of the catalyst composition is the same as an XRD pattern of the inorganic porous material. 115-. (canceled)16. A catalyst composition comprising an inorganic porous material with pore diameters of at least 2 nm and crystals of molecular sieve;wherein the crystals of molecular sieve have an average diameter not bigger than 50 nm measured using Scanning Electron Microscopy;wherein the catalyst composition has a concentration of acid sites ranging from 50 to 1200 μmol/g measured by Temperature-Programmed Desorption of ammonia, TPD NH3; andwherein an X-ray diffraction pattern of the catalyst composition is the same as an X-ray diffraction pattern of the inorganic porous material.17. The catalyst composition according to claim 16 , further characterized in that the catalyst composition contains a Bronsted aciditic sites concentration of at least 10 μmol/g measured by pyridine desorption at 150° C.18. The catalyst composition according to claim 16 , further characterized in that the inorganic porous material is amorphous.19. The catalyst composition according to claim 16 , further characterized in that the catalyst composition contains up to 30 weight % of crystals of molecular sieve relative to a total weight of the catalyst composition.20. The catalyst composition according to claim 16 , further characterized in that the surface area is of at least 250 m/g measured using ASTM D3663.21. The catalyst composition according to claim 16 , further characterized in that the ratio V/Vis of at least 5 claim 16 , wherein Vis the total porous volume of the catalyst composition and Vis the ...

PROCESS FOR SELECTIVELY DEALKYLATING AROMATIC COMPOUNDS

A process for selectively dealkylating aromatic compounds includes providing a coal tar stream comprising aromatic compounds and hydrotreating the coal tar stream to reduce a concentration of one or more of organic sulfur, nitrogen, and oxygen in the coal tar stream, and to hydrogenate at least a portion of the aromatic compounds in the coal tar stream. The process further includes hydrocracking the hydrotreated coal tar stream to further hydrogenate the aromatic compounds and to crack at least one ring of multi-ring aromatic compounds to form single-ring aromatic compounds. The single-ring aromatic compounds present in the hydrocracked stream are then dealkylated to remove alkyl groups containing two or more carbon atoms. 1. A process for selectively dealkylating aromatic compounds , comprising:providing a coal tar stream comprising aromatic compounds;hydrotreating the coal tar stream to reduce a concentration of one or more of organic sulfur, nitrogen, and oxygen in the coal tar stream, and to hydrogenate at least a portion of the aromatic compounds in the coal tar stream;hydrocracking the hydrotreated coal tar stream to further hydrogenate the aromatic compounds and to crack at least one ring of multi-ring aromatic compounds to form single-ring aromatic compounds; anddealkylating the single-ring aromatic compounds to remove alkyl groups containing two or more carbon atoms.2. The process of claim 1 , wherein hydrotreating the coal tar stream comprises:contacting the coal tar stream with a hydrotreating catalyst comprising one or more of nickel, molybdenum, cobalt, and tungsten.3. The process of claim 2 , wherein hydrotreating the coal tar stream takes place at a hydrogen partial pressure in the range of about 4 claim 2 ,100 kPa (595 psi) to about 17 claim 2 ,250 kPa (2 claim 2 ,502 psi).4. The process of claim 1 , wherein hydrocracking the hydrotreated the coal tar stream comprises:contacting the hydrotreated coal tar stream with a catalyst comprising:amorphous ...

SYSTEMS AND METHODS RELATED TO SYNGAS TO OLEFIN PROCESS

Disclosed herein is a system and method capable of producing benzene from a product stream. 1. A method comprising the steps of:a) providing a first product stream produced from a Fischer-Tropsch process converting syngas to olefins comprising a C2-C3 hydrocarbon stream and a C4+ hydrocarbon stream;b) separating at least a portion of the C2-C3 hydrocarbon stream from the first product stream;c) converting at least a portion of the butene in the C4+ hydrocarbon stream to BTX; andd) converting at least a portion of the toluene or xylene or combination thereof in the BTX to benzene.2. The method of claim 1 , wherein the first product stream comprises at least about 1 wt % of the C2-C3 hydrocarbon stream.3. The method of claim 1 , wherein the first product stream comprises at least about 1 wt % of the C4+ hydrocarbon stream.4. The method of claim 1 , wherein the first product stream comprises from about 1 wt % to about 30 wt % of the C2-C3 hydrocarbon stream.5. The method of claim 1 , wherein the first product stream comprises from about 1 wt % to about 50 wt % of the C4+ hydrocarbon stream.6. The method of claim 1 , wherein the step of converting at least a portion of the toluene or xylene or combination thereof in the BTX to benzene comprises hydroalkylting at least a portion of the toluene or xylene or combination thereof in the BTX.7. The method of claim 1 , wherein steps b) and c) occur simultaneously.8. The method of claim 1 , wherein the method further comprises after step b) the step of separating C2-C3 olefins from the C2-C3 hydrocarbon stream.9. The method of claim 1 , wherein the C4+ hydrocarbon stream is a C4-C12 hydrocarbon stream.10. The method of claim 1 , wherein the C4+ hydrocarbon stream is a C6-C8 hydrocarbon stream.11. The method of claim 1 , wherein the step of converting at least a portion of the C4+ hydrocarbon stream to BTX further produces C2-C4 hydrocarbons claim 1 , wherein the C2-C4 hydrocarbons are recycled back into the first product stream ...

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

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 ...

Conversion of Lignin to Fuels and Aromatics

Methods are provided for converting lignin-containing biomass into compounds that are more readily processed to form fuel and/or chemical products. The methods can allow for removal of at least a portion of the oxygen in lignin, either during or after depolymerization of lignin to single ring aromatic compounds, while optionally reducing or minimizing aromatic saturation performed on the aromatic compounds. The methods can include use of quench solvent to control reactions within the product stream from a pyrolysis process and/or use of a solvent to assist with hydroprocessing of lignin, lignin-containing biomass, or a pyrolysis oil. 1. A method of converting lignin to aromatic compounds , comprising:processing a lignin-containing feed under effective depolymerization conditions to form a depolymerized effluent containing monolignols;mixing the depolymerized effluent with a solvent to form a mixture of depolymerized effluent and solvent, the solvent having a T5 boiling point of at least about 240° C. and comprising at least about 50 wt % of aromatic compounds; andexposing at least a portion of the depolymerized effluent and solvent to a deoxygenation catalyst under effective deoxygenation conditions to form at least a deoxygenated effluent.2. The method of claim 1 , wherein processing a lignin-containing feed under effective depolymerization conditions comprises processing the lignin-containing feed under effective pyrolysis conditions in a pyrolysis reaction zone to form a pyrolysis effluent claim 1 , the pyrolysis effluent exiting the pyrolysis reaction zone at an exit temperature.3. The method of claim 2 , wherein mixing the depolymerized effluent with a solvent to form a mixture of depolymerized effluent and solvent comprises:mixing the pyrolysis effluent with a quench solvent, the quench solvent being at a quench solvent temperature and the pyrolysis effluent being at a mixing temperature that is less than about 100° C. different than the exit temperature; ...

Catalyst for Converting Alkylaromatic Hydrocarbon and Preparation Method Thereof

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 ...

HEAT INTEGRATION IN DISPROPORTIONATION OR TRANSALKYLATION PROCESSES

Toluene disproportionation and C9/C10 transalkylation are a significant source of xylenes in a modern aromatics complex. Methods and apparatuses for improving the energy efficiency of these disproportionation and transalkylation processes are provided. 1. A process comprising the steps of:(a) reacting, in a reactor, a reactor feed stream comprising toluene, C9 aromatics, C10 aromatics, and hydrogen over a catalyst to produce a reactor effluent stream comprising benzene and xylenes;(b) cooling the reactor effluent stream to form a first two-phase mixture;(c) separating the first two-phase mixture into a first liquid stream and a first vapor stream;(d) providing at least a portion of the first liquid stream to a benzene column, wherein the portion of the first liquid stream provided to the benzene column bypasses a stabilizer column; and(e) recovering benzene from the first condensed liquid stream in the benzene column.2. The process of claim 1 , further comprising the steps of:(f) cooling the first vapor stream to form a second two-phase mixture; and(g) separating the second two-phase mixture into a second liquid stream and a second vapor stream.3. The process of claim 2 , further comprising providing the second liquid stream to the stabilizer column.4. The process of claim 1 , wherein the first liquid stream is substantially free of light hydrocarbons.5. The process of claim 1 , further comprising using the reactor effluent stream to heat the reactor feed stream.6. The process of claim 1 , further comprising using the first vapor stream to heat the reactor feed stream.7. The process of claim 1 , wherein the reactor feed stream is heated to within about 50 degrees Celsius of the reactor effluent stream.8. The process of claim 1 , wherein the step of cooling the reactor effluent stream to form the first two-phase mixture is performed at between about ambient temperature and the reactor temperature.9. The process of claim 2 , wherein the step of cooling the first vapor ...

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

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 ...

METHOD OF HYDROGENOLYSIS FOR IMPROVED PRODUCTION OF PARAXYLENE

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 ...

Process for producing btx from a c5-c12 hydrocarbon mixture

The present invention relates to a process for producing chemical grade BTX from a mixed feedstream comprising C5-C12 hydrocarbons by contacting said feedstream in the presence of hydrogen with a catalyst having hydrocracking/hydrodesulphurisation activity. Particularly, a process for producing BTX from a feedstream comprising C5-C12 hydrocarbons is provided comprising the steps of: (a) contacting said feedstream in the presence of hydrogen with a combined hydrocracking/hydrodesulphurisation catalyst to produce a hydrocracking product stream comprising BTX; and (b) separating the BTX from the hydrocracking product stream. The hydrocracking/hydrodesulphurisation catalyst comprises 0.1-1 wt-% hydrogenation metal in relation to the total catalyst weight. The hydrocracking/hydrodesulphurisation catalyst further comprises a zeolite having a pore size of 5-8 Å and a silica (SiO 2 ) to alumina (Al 2 O 3 ) molar ratio of 5-200. The hydrocracking/hydrodesulphurisation conditions include a temperature of 450-580° C., a pressure of 300-5000 kPa gauge and a Weight Hourly Space Velocity of 0.1-10 h −1 .

METHODS AND APPARATUSES FOR PROCESSING HYDROCARBONS

Methods and apparatuses for processing hydrocarbons are provided. In one embodiment, a method for processing hydrocarbons includes fractionating a feed stock to form a C6-C10 naphtha stream and a C11hydrocarbon stream. The method reforms the C6-C10 naphtha stream. Further, the method cracks the C11hydrocarbon stream to form a stream of C6-C10 hydrocarbons and extracts aromatics from the stream of C6-C10 hydrocarbons to form an extract stream. The method includes combining the C6-C10 naphtha stream and the extract stream containing the aromatics. Also, the method includes processing the C6-C10 naphtha stream and the extract stream in an aromatics complex to form selected aromatic products. Further, the embodiment may include reforming raffinate streams. 1. A method for processing hydrocarbons , the method comprising the steps of:{'sup': '+', 'fractionating a feed stock to form a C6-C10 naphtha stream and a C11stream;'}reforming the C6-C10 naphtha stream;{'sup': '+', 'cracking the C11stream to form a stream of C6-C10 hydrocarbons;'}extracting aromatics from the stream of C6-C10 hydrocarbons to form an extract stream;combining the C6-C10 naphtha stream and the extract stream containing the aromatics; andprocessing the C6-C10 naphtha stream and the extract stream in an aromatics complex to form selected aromatic products.2. The method of comprising combining the C6-C10 naphtha stream and the extract stream containing the aromatics after reforming the C6-C10 naphtha stream.3. The method of comprising combining the C6-C10 naphtha stream and the extract stream containing the aromatics before reforming the C6-C10 naphtha stream claim 1 , and wherein reforming the C6-C10 naphtha stream comprises reforming the C6-C10 naphtha stream and the extract stream containing the aromatics.4. The method of further comprising hydrotreating the C6-C10 naphtha stream before reforming the C6-C10 naphtha stream.5. The method of further comprising:selectively hydrotreating the stream of C6- ...

Process for Xylenes Isomerization

A process for the isomerization of a para-xylene depleted, meta-xylene rich stream under at least partially liquid phase conditions using ZSM-23 with an external surface area of at least 75 m/g (indicating a small crystallite size), and a SiO/AlOratio between 15 and 75 that produces a higher than equilibrium amount of para-xylene, i.e., more than about 24 wt % of para-xylene, based on the total amount of xylenes. 1. A process for producing para-xylene from a Caromatic hydrocarbon mixture , the process comprising:{'sub': '8', '(a) providing a Caromatic hydrocarbon mixture comprising para-xylene, ortho-xylene and meta-xylene to an ortho-xylene splitter to produce a first stream comprising para-xylene and meta-xylene and a second stream comprising ortho-xylene;'}(b) passing the first stream comprising para-xylene and meta-xylene to a para-xylene recovery unit to recover a para-xylene product stream and produce a para-xylene-depleted stream comprising meta-xylene;(c) contacting the para-xylene-depleted stream comprising meta-xylene with a catalyst under at least partially liquid phase conditions effective to produce a first isomerized stream having a para-xylene content of more than 24 wt %, based on the total amount of xylenes in the first isomerized stream; and(d) recycling at least a portion of the first isomerized stream back to the para-xylene recovery unit.2. The process of claim 1 , wherein the catalyst of step (c) comprises ZSM-23 with a SiO/AlOratio between 15 and 75 and an external surface area of at least 75 m/g.3. The process of claim 2 , wherein the catalyst in step (c) comprises ZSM-23 having SiO/AlOratio between 15 and 50 and an external surface area of at least 90 m/g.4. The process of claim 1 , wherein the catalyst in step (c) is self-bound.5. The process of claim 1 , wherein the para-xylene-depleted stream produced in step (b) consists essentially of meta-xylene.6. The process of claim 1 , wherein at least a portion of the first isomerized stream is ...

Combined heavy reformate dealkylation-transalkylation process for maximizing xylenes production

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.

Heavy Aromatics Conversion Processes and Catalyst Compositions Used Therein

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 ...

Catalyst Compositions Comprising Small Size Molecular Sieves Crystals Deposited on a Porous Material

Catalyst compositions comprising an inorganic porous material with pore diameters of at least 2 nm and of crystals of molecular sieve, characterized in that the crystals of molecular sieve have an average diameter, measured by scanning electron microscopy, not bigger than 50 nm, and in that the catalyst composition presents a concentration of acid sites ranges from 50 to 1200 μmol/g measured by TPD NH3 adsorption; and the XRD pattern of said catalyst composition is the same as the X ray diffraction pattern of said inorganic porous material. 115-. (canceled)17. The process according to claim 16 , further characterized in that the steps e) to g) are repeated at least two times prior to performing step h).18. The process according to claim 17 , wherein the maturation of the solution is conducted for at least 30 min and at most 100 h each time.19. The process according to claim 18 , wherein the steps e) to g) are performed once and maturation of the solution is conducted for at most 50 h.20. The process according to claim 16 , further comprising claim 16 , after step h) claim 16 , performing one or more of the following steps:introducing phosphorous by impregnation of the catalyst composition by a solution containing phosphorous, said step being optionally followed by further steps of calcinations and/or steaming;adding at least one metal selected from the group consisting of: B, Cr, Co, Ga, Fe, Li, Mg, Ca, Mn, La, Ti, Mo, W, Ni, Ag, Sn or Zn, Pt, Pd, Ru, Re, Os, Au, and combinations thereof, by impregnation of the catalyst composition by a solution containing the at least one metal;adding at least one binder selected from the group consisting of: silica, silica alumina, metal silicates, metal oxides and/or metals, amorphous alumophophate or silica alumophosphates, gels including mixtures of silica and metal oxides, and combinations thereof, by spray drying or extrusion;shaping of the catalyst composition by extrusion.21. A process comprising using a catalyst ...

Production of Neopentane

Disclosed herein are processes for producing neopentane. The processes generally relate to demethylating neohexane and/or neoheptane to produce neopentane. The neohexane and/or neoheptane may be provided by the isomerization of C-Cparaffins. 1. A process for producing neopentane , the process comprising:{'sub': 6', '7, '(a) providing a feed stream including C-Cparaffins;'}{'sub': 6', '7, '(b) isomerizing the C-Cparaffins to produce an isomerization product including neohexane and/or neoheptane; and'}(c) demethylating the neohexane and/or neoheptane to produce a demethylation product including at least 40 wt % neopentane based on the weight of the demethylation product.2. The process of claim 1 , wherein at least part of the neohexane and/or neoheptane is separated from the isomerization product prior to demethylation.3. The process of claim 2 , wherein separating the neohexane and/or neoheptane from the isomerization product comprises distillation.4. The process of claim 3 , wherein the isomerization product is separated into fractions comprising (1) a C− hydrocarbon fraction (2) a first C-Chydrocarbon fraction comprising neohexane and/or neoheptane and (3) a second C-Chydrocarbon fraction comprising non-neo isomers.5. The process of claim 4 , wherein the isomerization is carried out in a reaction vessel claim 4 , and wherein the second C-Chydrocarbon fraction is recycled to the reaction vessel.6. The process of claim 1 , wherein the feed stream comprises light virgin naphtha.7. The process of claim 1 , wherein the isomerization comprises contacting the feed stream with hydrogen in the presence of a catalyst (A).8. The process of claim 7 , wherein the catalyst (A) comprises at least one member selected from the group consisting of Pd claim 7 , Pt claim 7 , Rh claim 7 , Ru claim 7 , Os claim 7 , Ir claim 7 , Au claim 7 , Ag claim 7 , Cu claim 7 , Ni claim 7 , Co claim 7 , Fe claim 7 , Re claim 7 , combinations thereof claim 7 , compounds thereof claim 7 , and ...

ALIPHATIC CRACKING AND DEALKYLATION WITH HYDROGEN DILUENT

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

PROCESS FOR THE PREPARATION OF A CATALYST SUPPORT

Process for preparing a catalyst support which process comprises a) mixing pentasil zeolite having a bulk silica to alumina molar ratio in the range of from 20 to 150 with water, a silica source and an alkali metal salt, b) extruding the mixture obtained in step (a), c) drying and calcining the extrudates obtained in step (b), d) subjecting the calcined extrudates obtained in step (c) to ion exchange to reduce the alkali metal content, and e) drying the extrudates obtained in step (d); process for preparing a catalyst by furthermore impregnating such support with platinum in an amount in the range of from 0.001 to 0.1 wt % and tin in an amount in the range of from 0.01 to 0.5 wt %, each on the basis of total catalyst; ethylbenzene dealkylation catalyst obtainable thereby and a process for dealkylation of ethylbenzene which process comprises contacting feedstock containing ethylbenzene with such catalyst. 1. A process for preparing a catalyst , which process comprises:a) mixing pentasil zeolite having a bulk silica to alumina molar ratio in the range of from 20 to 150 with water, a silica source and an alkali metal salt;b) extruding the mixture obtained in step (a);c) drying and calcining the extrudates obtained in step (b);d) treating the extrudates obtained in step (c) with an aqueous solution of fluorosilicate salt to provide fluorosilicate-treated extrudates;e) subjecting the fluorosilicate-treated extrudates obtained in step (d) to ion exchange with an aqueous ammonium containing solution to reduce the alkali metal content;f) drying the extrudates obtained in step (e); andg) impregnating the catalyst support with platinum in an amount in the range of from 0.001 to 0.1 wt % and tin in an amount in the range of from 0.01 to 0.5 wt %, each on the basis of total catalyst.2. A process as recited in claim 1 , wherein the silica source is selected from the group consisting of powder form silica claim 1 , silica sol claim 1 , and mixtures of powder form silica and ...

Production of Neopentane

Disclosed herein are processes for producing neopentane. The processes generally relate to demethylating diisobutylene to produce neopentane. The diisobutylene may be provided by the dimerization of isobutylene. 1. A process for producing neopentane , the process comprising:(a) providing a feed stream including isobutylene;(b) dimerizing the isobutylene to produce a dimerization product including diisobutylene; and(c) demethylating the diisobutylene to produce a demethylation product including at least 10 wt % neopentane based on the weight of the demethylation product.2. The process of claim 1 , wherein at least part of the diisobutylene is separated from the dimerization product prior to demethylation.3. The process of claim 2 , wherein separating the diisobutylene from the dimerization product comprises distillation.4. The process of claim 3 , wherein the dimerization product is separated into fractions comprising (1) a Chydrocarbon fraction (2) a diisobutylene fraction and (3) a C+ hydrocarbon fraction.5. The process of claim 1 , wherein the feed stream comprises a raffinate stream obtained from cracking a naphtha stream.6. The process of claim 5 , wherein the feed stream comprises from about 5 wt % to about 60 wt % isobutylene based on the weight of the feed stream.7. The process of claim 1 , wherein the feed stream is provided at a temperature ranging from about 50° C. to about 350° C. and wherein the dimerization is performed in the presence of catalyst (A).8. The process of claim 7 , wherein the catalyst (A) comprises at least one member selected from the group consisting of acidic ion-exchange resin claim 7 , acidic clay claim 7 , aluminosilicate claim 7 , supported phosphoric acid claim 7 , acidic metal oxide claim 7 , acidic mixed metal oxide claim 7 , zeolites claim 7 , and mixtures thereof.9. The process of claim 1 , wherein the dimerization is carried out within an adiabatic reaction vessel.10. The process of claim 1 , further comprising contacting the ...

Catalysts And Processes For The Production Of Aromatic Compounds From Lignin

Hydrotreating catalysts and processes useful for the conversion of methoxylated aromatic compounds to simple aromatic compounds are provided. The catalysts comprise transition metal selected from the group consisting of Group 8 metals, Group 9 metals, Group 10 metals, Group 11 metals, and mixtures thereof, and catalyst support selected from the group consisting of shape-selective zeolite, silica, titania, zirconia, and mixtures thereof. 1. A process for converting methoxylated aromatic compounds and compositions comprising methoxylated aromatic compounds to simple aromatic compounds comprising:a. contacting said methoxylated aromatic compounds and said compositions comprising methoxylated aromatic compounds with a catalyst and hydrogen in a reactor; andb. removing simple aromatic compounds from said reactor; i. a transition metal selected from the group consisting of Group 8 metals, Group 9 metals, Group 10 metals, Group 11 metals, and mixtures thereof; and', 'ii. a catalyst support selected from the group consisting of silica, titania, zirconia, shape-selective zeolite, and mixtures thereof., 'wherein said catalyst comprises2. The process of claim 1 , wherein said catalyst support is a shape-selective zeolite claim 1 , and further claim 1 , wherein the shape-selective zeolite comprises ferrierite zeolite.3. The process of claim 1 , wherein said catalyst support is a shape-selective zeolite claim 1 , and further claim 1 , wherein the shape-selective zeolite comprises H-ZSM-5 zeolite.4. The process of claim 1 , wherein said transition metal is selected from the group consisting of Fe claim 1 , Ru claim 1 , Co claim 1 , Rh claim 1 , Ni claim 1 , Pd claim 1 , Pt claim 1 , Cu claim 1 , and mixtures thereof.5. The process of claim 4 , wherein said transition metal is selected from the group consisting of Ni claim 4 , Pd claim 4 , Pt claim 4 , Cu claim 4 , and mixtures thereof.6. The process of claim 1 , wherein said transition metal comprises less than about 20 wt % of ...

Integrated Process for the Production of Benzene and Xylenes from Heavy Aromatics

Systems and processes for maximizing the production of benzene and para-xylene from heavy reformate are provided. An integrated process and system may include a C9 dealkylation reactor, a transalkylation reactor, and a C10+ dealkylation reactor. The integrated process and system for producing benzene and para-xylene may be configured to additionally produce alkanes in the presence of hydrogen or olefins in the absence of hydrogen. The transalkylation reactor may perform transalkylation of product from the C9 dealkylation reactor and xylene isomerization. 1. A heavy reformate processing system for producing benzene and para-xylene from a heavy reformate , the heavy reformate processing system comprising:a reformate splitter operable to receive a feed stream, the feed stream comprising heavy reformate, the reformate splitter further operable to produce benzene, toluene, and a C8+ aromatics product, the C8+ aromatics product provided to a xylene splitter;a para-xylene separator operable to receive a C8 aromatic product from the xylene splitter and produce a first xylene product comprising para-xylene and a second xylene product comprising ortho-xylene and meta-xylene; produce alkanes from the C10+ aromatics product and hydrogen, or', 'produce olefins from the C10+ aromatic product in the absence of hydrogen;, 'a first dealkylation reactor operable to receive a C10+ aromatics product from the xylene splitter and produce the first dealkylation product, the first dealkylation reactor further operable to produce alkanes from the C9 aromatics product and hydrogen; or', 'produce olefins from the C9 aromatic product in the absence of hydrogen. a transalkylation reactor operable to receive the second dealkylation product from the second dealkylation reactor and produce the transalkylation product, the transalkylation reactor further operable to:', 'produce alkanes from the second dealkylation product and hydrogen; or', 'produce olefins from the second dealkylation product in ...

PENTASIL-TYPE ZEOLITE, AND METHOD FOR MANUFACTURING SAME

[Problem] The purpose of the present invention is to provide: a pentasil-type zeolite that combines a higher BET specific surface area and a higher acid amount than previously; and a method for manufacturing said pentasil-type zeolite. 1. A pentasil-type zeolite comprising a BET specific surface area of 450 m/g or more and an acid amount measured by an ammonia-TPD method of 0.38 mmol/g or more.2. The pentasil-type zeolite according to claim 1 , wherein the pentasil-type zeolite comprises a pore volume being 0.60 mL/g or less.3. The pentasil-type zeolite according to claim 1 , wherein the pentasil-type zeolite comprises a molar ratio of silica to alumina being less than 150.4. The pentasil-type zeolite according to claim 1 , wherein the pentasil-type zeolite comprises a molar ratio of tetra-coordinated aluminum to the sum of the tetra-coordinated aluminum and hexa-coordinated aluminum in a crystal being 90% or more.5. The pentasil-type zeolite according to claim 1 , wherein the pentasil-type zeolite comprises an alkali metal claim 1 , with a molar ratio of the alkali metal to aluminum being 0.5 or less.6. The pentasil-type zeolite according to claim 1 , wherein primary particles do not regularly aggregate.7. The pentasil-type zeolite according to claim 1 , wherein secondary particles has a diameter of aggregate of 0.3 to 50 μm.8. The pentasil-type zeolite according to claim 1 , wherein the pentasil-type zeolite comprises phosphorus.9. The pentasil-type zeolite according to claim 8 , wherein the pentasil-type zeolite comprises a molar ratio of phosphorus to silicon and aluminum being 0.0005 or more.10. The pentasil-type zeolite according to claim 1 , wherein the acid amount measured by an ammonia-TPD method is 0.45 mmol/g or more.11. A method for manufacturing the pentasil-type zeolite according to any one of claim 1 , comprising a crystallization step of crystallizing a mixture containing tetrabutylphosphonium cations claim 1 , a silica source claim 1 , an alumina ...

Process for Producing Cyclohexylbenzene

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.

MOLECULAR SIEVE SCM-15, SYNTHESIS METHOD THEREFOR AND USE THEREOF

The invention relates to a molecular sieve SCM-15, a preparation process and use thereof. The molecular sieve comprises a schematic chemical composition of a formula of “SiO.GeO”, wherein the molar ratio of silicon and germanium satisfies SiO/GeO≥1. The molecular sieve has unique XRD diffraction data and can be used as an adsorbent or a catalyst. 3. The molecular sieve SCM-15 according to claim 1 , characterized in that the molecular sieve has a schematic chemical composition of formula “SiO.GeO” claim 1 , wherein the molar ratio of silicon to germanium satisfies SiO/GeO≥1 claim 1 , preferably 1≤SiO/GeO≤15 claim 1 , more preferably 2≤SiO/GeO≤10 claim 1 , or more preferably 2.5≤SiO/GeO≤5.4. The molecular sieve SCM-15 according to claim 3 , characterized in that not more than 10% of the Ge atoms in the molecular sieve are substituted by atoms of at least one element other than silicon and germanium.5. The molecular sieve SCM-15 according to claim 4 , characterized in that the element other than silicon and germanium is at least one selected from the group consisting of boron claim 4 , aluminum claim 4 , tin claim 4 , zirconium and titanium.7. The process of preparing molecular sieve SCM-15 according to claim 6 , characterized in that the silicon source is at least one selected from the group consisting of silicic acid claim 6 , silica gel claim 6 , silica sol claim 6 , tetraalkyl orthosilicate and water glass; the germanium source is at least one selected from the group consisting of germanium oxide claim 6 , germanium nitrate and tetraalkoxygermanium;{'sub': 2', '2, 'and the molar ratio of the silicon source (calculated by SiO), the germanium source (calculated by GeO), the fluorine source (calculated by F), the organic template agent and water is 1:(0-1):(0.1-2.0): (0.1-2.0):(3-30); preferably 1:( 1/15-1.5):(0.2-1.5):(0.2-1.5):(4-25); more preferably 1:(0.1-0.5):(0.4-1.2):(0.4-1.2):(5-20); more preferably 1:(0.2-0.4):(0.6-1.0):(0.6-1.0):(5-15).'}8. The process of ...

MOLECULAR SIEVE SCM-14, A PREPARATION PROCESS AND USE THEREOF

The invention relates to a molecular sieve SCM-14, a preparation process and use thereof. The molecular sieve has a schematic chemical composition of a formula of “SiO.1/nGeO” or a formula of “kF.mQ.SiO.1/nGeO.pHO”, wherein the molar ratio of silicon to germanium, n, satisfies n≤30, and other values and symbols are defined in the specification. The molecular sieve has unique XRD diffraction data and can be used as an adsorbent or a catalyst. 3. The molecular sieve SCM-14 according to claim 1 , characterized in that the molecular sieve in the calcined form has a schematic chemical composition of formula “SiO.1/nGeO” claim 1 , wherein the molar ratio of silicon to germanium claim 1 , n claim 1 , satisfies n≤30 claim 1 , preferably 0.5≤n≤20 claim 1 , more preferably 1≤n≤10 claim 1 , or more preferably 1≤n≤5.5. The molecular sieve SCM-14 according to claim 1 , characterized in that not more than 10% of the Ge atoms in the molecular sieve are replaced by atoms of at least one element other than silicon and germanium.6. The molecular sieve SCM-14 according to claim 5 , characterized in that the element other than silicon and germanium is at least one selected from the group consisting of boron claim 5 , aluminum claim 5 , tin claim 5 , zirconium and titanium claim 5 , preferably at least one selected from the group consisting of boron and titanium.8. The process of preparing molecular sieve SCM-14 according to claim 7 , characterized in that the silicon source is at least one selected from the group consisting of silicic acid claim 7 , silica gel claim 7 , silica sol claim 7 , tetraalkyl orthosilicate and water glass; the germanium source is at least one selected from the group consisting of germanium oxide claim 7 , germanium nitrate and tetraalkoxygermanium;{'sub': 2', '2, 'the molar ratio of the silicon source (calculated as SiO), the germanium source (calculated as GeO), the fluorine source (calculated as F), the organic template agent and water is 1:(1/30 to ∞):(0.1 ...

Dealkylation and Transalkylation of Heavy Aromatic Hydrocarbons

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 ...

CATALYST COMPOSITION, ITS PREPARATION AND USE

A catalyst composition which comprises 1. A process for preparation of a catalyst composition , wherein said process comprises:{'sup': '+', 'forming a carrier by combining from 30 wt % to 80 wt % silica binder comprising a powder form silica and silica sol in a weight ratio of powder form to sol in the range of from 1:1 to 10:1, and 20 wt % to 70 wt % of a pentasil zeolite, having an average crystallite size in the range of from 1 to 10 μm and a bulk silica-to-alumina (SAR) ratio in the range of from 20 to 150 and being in its H form, with all percentages being on the basis of total carrier;'}{'sub': 2/b', '6, 'providing a surface-modified carrier by subjecting said carrier to a dealumination treatment by contacting said carrier with either an aqueous solution of fluorosilicate salt of formula (A)SiF, wherein A is a metallic or non-metallic cation other than H+ having valence b and b is the valence of A, or an aqueous solution of hexaflurorosilicate salt or dicarboxylic acid;'}incorporating platinum onto said surface-modified carrier in an amount in the range of from 0.001 to 0.1 wt % of the weight of said catalyst composition; andincorporating tin onto said surface-modified carrier in an amount in the range of from 0.01 to 0.5 wt % of the weight of said catalyst composition.2. A process as recited in claim 1 , wherein said dealumination treatment of said carrier includes subjecting said carrier to said dealumination treatment with ammonium hexaflurorosilicate.3. A process as recited in claim 2 , wherein said pentasil zeolite is one having an MFI configuration.4. A process as recited in claim 3 , wherein said pentasil zeolite having said MFI configuration is ZSM-5.5. A process as recited in claim 4 , wherein the ZSM-5 has a SAR in the range of from 20 to 50 and is present in said carrier in an amount in the range of from 20 wt % to 50 wt %.6. A process as recite in claim 5 , wherein said powder form silica has a mean particle size in the range of from 2 to 60 μm.7. ...

Catalyst Compositions and Use in Heavy Aromatics Conversion Processes

Disclosed is a catalyst composition and its use in a process for the conversion of a feedstock containing C+ aromatic hydrocarbons to produce light aromatic products, comprising benzene, toluene and xylene. The catalyst composition comprises a mordenite zeolite synthesized from TEA or MTEA, optionally at least one first metal of Group 10 of the IUPAC Periodic Table, and optionally at least one second metal of Group 11 to 15 of the IUPAC Periodic Table, wherein said mordenite zeolite has a mesopore surface area of greater than 30 m/g and said 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. 1. A catalyst composition for conversion of Caromatic hydrocarbons to lighter aromatic products , said catalyst composition comprising (i) a mordenite zeolite synthesized from tetraethylammonium cation (TEA) or methyltriethylammonium cation (MTEA) , wherein said mordenite zeolite has a mesopore surface area of greater than 30 m/g and said 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 2.2. The catalyst composition of claim 1 , said catalyst composition further comprising 0.005 to 5.0 wt. % of at least one first metal of Group 10 of the IUPAC Periodic Table claim 1 , based on the weight of said catalyst composition.3. The catalyst composition of claim 2 , said catalyst composition further comprising 0.01 to 5.0 wt. % of at least one second metal of Group 11 to 15 of the IUPAC Periodic Table claim 2 , based on the weight of said catalyst composition.4. The catalyst composition of claim 2 , wherein said at least first metal of Group 10 is selected from the group consisting of nickel claim 2 , platinum claim 2 , palladium and mixtures thereof.5. The ...

Catalyst System and Use in Heavy Aromatics Conversion Processes

Disclosed are a catalyst system and its use in a process for the conversion of a feedstock containing C+ 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/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. 1. A catalyst system for conversion of Caromatic hydrocarbons to lighter aromatic products , said catalyst system comprising:(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; and{'sup': '2', '(b) a second catalyst bed comprising a second catalyst composition, said second catalyst composition comprising (i) a meso-mordenite zeolite, wherein said meso-mordenite zeolite is synthesized from tetraethylammonium cation (TEA) or methyltriethylammonium cation (MTEA) and has a mesopore surface area of greater than 30 m/g and comprises agglomerates of primary crystallites, wherein said primary crystallites have an ...

Transalkylation of Heavy Aromatic Hydrocarbon Feedstocks

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.

Process for the production of gasoline blending components and aromatic hydrocarbons from lower alkanes

An integrated process for producing gasoline blending components and aromatic hydrocarbons which comprises: (a) contacting a lower alkane feed with an aromatic hydrocarbon conversion catalyst to produce an aromatic reaction product mixture which is comprised of benzene and/or toluene and/or xylene, C 9 aromatic products, C 10 aromatic products including naphthalene and, optionally, C 11+ aromatic products, (b) separating and recovering the aromatic reaction product mixture, (c) separating and recovering benzene, (d) optionally separating recovering toluene and/or xylene, and (e) separating and recovering the C 9 aromatic products and the C 10 aromatic products which boil at a lower temperature than naphthalene from the naphthalene and the C 10 aromatic reaction products which boil at a higher temperature than naphthalene and any C 11+ aromatic products.

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

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-containing products from a feed stream comprising C9 aromatic components , comprising:a. hydrodealkylating the feed stream to remove C2 and higher alkyl groups from the aromatic components of the feed stream as their corresponding alkanes;b. transalkylating the feed stream to rearrange the distribution of methyl groups among the aromatic components of the feed stream;c. after steps a and b, recovering a TMB-rich product.2. The method of in which the feed stream includes lower paraffins claim 1 , which method further includes hydrocracking the paraffins.3. The method of which further includes introducing into the feed stream supplemental methylated aromatics.4. The method of in which the methylated aromatics comprise a stream of C7 and higher methylated aromatics.5. The method of in which the methylated aromatics comprise a recycle stream of C7 and higher methylated aromatics obtained during the method.6. The method of in which the HDA and TA are performed in the same reaction vessel.7. The method of which further includes introducing a recycle stream of C7 and higher methylated aromatics obtained during the method into the feed stream prior to steps a and b.8. The method of in which the HDA of step a is performed first and then the TA of step b is performed separately.9. The method of which further includes introducing a recycle stream of C7 and higher ...

PROCESS FOR PRODUCING BTX FROM A C5-C12 HYDROCARBON MIXTURE

The invention relates to a process for producing benzene comprising the steps of: (a) providing a hydrocracking feed stream comprising C-Chydrocarbons, (b) contacting the hydrocracking feed stream in the presence of hydrogen with a hydrocracking catalyst under process conditions including a temperature of 425-580° C., a pressure of 300-5000 kPa gauge and a Weight Hourly Space Velocity of 3-30 hto produce a hydrocracking product stream comprising BTX and (c) separating the BTX from the hydrocracking product stream, wherein the hydrocracking catalyst comprises a shaped body comprising a zeolite and a binder and a hydrogenation metal deposited on the shaped body, wherein the amount of the hydrogenation metal is 0.010-0.30 wt-% with respect to the total catalyst and wherein the zeolite is ZSM-5 having a silica (SiO) to alumina (AlO) molar ratio of 25-75. 1. A process for producing benzene comprising the steps of:{'sub': 5', '12, '(a) providing a hydrocracking feed stream comprising C-Chydrocarbons,'}{'sup': '−1', '(b) contacting the hydrocracking feed stream in the presence of hydrogen with a hydrocracking catalyst under process conditions including a temperature of 425-580° C., a pressure of 300-5000 kPa gauge and a Weight Hourly Space Velocity of 3-30 hto produce a hydrocracking product stream comprising BTX and'}(c) separating the BTX from the hydrocracking product stream,wherein the hydrocracking catalyst comprises a shaped body comprising a zeolite and a binder and a hydrogenation metal deposited on the shaped body,wherein the amount of the hydrogenation metal is 0.010-0.30 wt % with respect to the total catalyst andwherein the zeolite is ZSM-5 having a silica to alumina molar ratio of 25-75.2. The process according to claim 1 , wherein the zeolite has a silica to alumina molar ratio of 30-65.3. The process according to claim 1 , wherein the amount of the hydrogenation metal is 0.015-0.095 wt % with respect to the total catalyst.4. The process according to claim 1 ...

PROCESS FOR THE PREPARATION OF AROMATIC COMPOUNDS

A process for the preparation of small aromatic compounds from black liquor comprising: 1. A process for the preparation of small aromatic compounds from black liquor comprising:providing black liquor that derives from alkaline treatment of wood chips;subjecting the black liquor to a pyrolysis treatment to yield a pyrolysed black liquor gas and a solid mass comprising char and salts in a first reactor, wherein the salts substantially derive from the treatment of black liquor;contacting at least part of the pyrolysed black liquor gas with a catalyst in a second reactor, which is different from the first reactor to provide a conversion treatment to yield a conversion product; andrecovering small aromatic compounds from the conversion product.2. The process according to claim 1 , wherein the pyrolysis treatment is carried out without the addition of a catalyst.3. The process according to claim 1 , wherein the wood chips are derived from hardwood.4. The process according to claim 1 , wherein the pyrolysis treatment of black liquor is carried out at a temperature of 350° C. to 700° C. at a pressure of between 0.1 to 6 bara.5. The process according to claim 1 , wherein at least a part of the solid mass is collected and heated to a temperature that is sufficiently high to recover the salt in the solid mass.6. The process according to claim 1 , wherein the conversion treatment involves the conversion of complex aromatic compounds to small aromatic compounds claim 1 , the conversion of oxygen containing aromatic and oxygen containing aliphatic compounds to small aromatic compounds without oxygen atoms claim 1 , and/or the conversion of hydrocarbons claim 1 , such as olefins into small aromatic compounds.7. The process according to claim 1 , wherein the conversion treatment occurs at a temperature between 200° C. and 1000° C.8. The process according to claim 1 , wherein in the conversion treatment the catalyst is present in a weight ratio of pyrolysed black liquor gas to ...

Process for selectively dealkylating aromatic compounds

A process for selectively dealkylating aromatic compounds includes providing a coal tar stream comprising aromatic compounds and hydrotreating the coal tar stream to reduce a concentration of one or more of organic sulfur, nitrogen, and oxygen in the coal tar stream, and to hydrogenate at least a portion of the aromatic compounds in the coal tar stream. The process further includes hydrocracking the hydrotreated coal tar stream to further hydrogenate the aromatic compounds and to crack at least one ring of multi-ring aromatic compounds to form single-ring aromatic compounds. The single-ring aromatic compounds present in the hydrocracked stream are then dealkylated to remove alkyl groups containing two or more carbon atoms.

Purge Streams in Paraxylene Production

In a process for producing para-xylene, a hydrocarbon feed comprising xylenes and ethylbenzene is supplied to a para-xylene extraction system, where a para-xylene-rich stream is recovered from the feed to leave at least one para-xylene-depleted stream. At least a portion of the para-xylene-depleted stream is isomerized at least partially in the liquid phase to produce an isomerized stream having a higher para-xylene concentration than the para-xylene-depleted stream. At least a portion of the isomerized stream is then recycled to the para-xylene extraction system. To control ethylbenzene build-up in the process, a purge stream is removed from the para-xylene-depleted stream and/or the isomerized stream and is subjected to one or more chemical processing steps to produce benzene and/or para-xylene. 1. A process for producing para-xylene , the process comprising:(a) supplying a hydrocarbon feed comprising xylenes and ethylbenzene to a para-xylene extraction system;(b) recovering a para-xylene-rich stream from said feed in said para-xylene extraction system to leave at least one para-xylene-depleted stream;(c) isomerizing at least a portion of said para-xylene-depleted stream at least partially in the liquid phase to produce an isomerized stream having a higher para-xylene concentration than said para-xylene-depleted stream;(d) recycling at least a portion of the isomerized stream to said para-xylene extraction system;(e) removing a purge stream from said para-xylene-depleted stream and/or said isomerized stream; and (i) isomerizing ethylbenzene to produce para-xylene;', '(ii) deethylating ethylbenzene to produce benzene;', '(iii) deethylating ethylbenzene to produce benzene and isomerizing xylenes to produce para-xylene;', '(iv) deethylating ethylbenzene to produce benzene and methylating said benzene to form toluene and para-xylene; and', '(v) methylating ethylbenzene to form methylated ethylbenzene and/or polymethylated ethylbenzene, deethylating said methylated ...

PREPARATION OF A ZSM-5-BASED CATALYST; USE IN ETHYLBENZENE DEALKYLATION PROCESS

A process of preparing a catalyst composition which process comprises the steps of (a) treating ZSM-5 zeolite with an alkaline solution having a pH of at least (8) followed by ion exchange to obtain a treated zeolite, (b) extruding a mixture of the treated zeolite and binder and contacting the zeolite with a fluorocompound containing solution, (c) increasing the temperature of the extrudates obtained in step (b) to at least 200° C., and (d) combining the extrudates obtained in step (c) with one or more metals selected from the group consisting of Group (10) and (11) of the IUPAC Periodic Table of Elements and a process for the conversion of an aromatic hydrocarbons containing feedstock using a catalyst composition prepared by such process. 1. A process of preparing a catalyst composition which process comprises the steps of:(a) treating ZSM-5 zeolite with an alkaline solution having a pH of at least 8 followed by ion exchange to obtain a treated zeolite,(b) extruding a mixture of the treated zeolite and a binder and contacting the zeolite with a fluorocompound containing solution,(c) increasing the temperature of the extrudates obtained in step (b) to at least 200° C., and(d) combining the extrudates obtained in step (c) with one or more metals selected from the group consisting of Group 10 and 11 of the IUPAC Periodic Table of Elements.2. The process according to in which step (b) comprises extruding a mixture of the treated zeolite and silica binder claim 1 , and subsequently treating the extrudates with a fluorocompound containing solution.3. The process according to in which step (b) comprises treating the extrudates with a solution comprising a fluorosilicate.4. The process according to in which the metal is selected from the group consisting of platinum and palladium.5. The process according to in which the extrudate is further combined with one or more metal chosen from the group consisting of tin and rhenium.6. The process according to in which the ZSM-5 ...

ALKYLAROMATIC CONVERSION CATALYST

Alkylaromatic conversion catalyst which comprises a) a carrier which comprises of from 20 to 70 wt % of a refractory oxide binder, of from 30 to 80 wt % of ZSM-5 having a mesopore volume of from 0.1 to 1.0 ml/g, a crystallite size of from 3 to 100 nm and a silica to alumina molar ratio in the range of from 20 to 200, all percentages being on the basis of total catalyst; b) an amount of from 0.001 to 5 wt % of one or more metals chosen from the group consisting of Groups 6, 9 and 10; and c) optionally a metal chosen from Group 14 in an amount up to 0.5 wt %, on the basis of total catalyst, and a process for the preparation of such catalyst. 1. The alkylaromatic conversion catalyst which comprisesa) a carrier which comprises of from 20 to 70 wt % of a refractory oxide binder; of from 30 to 80 wt % of ZSM-5 having a mesopore volume of from 0.1 to 1.0 ml/g, a crystallite size of from 3 to 100 nm and a silica to alumina molar ratio in the range of from 20 to 200, all percentages being on the basis of total catalyst;b) an amount of from 0.001 to 5 wt % of one or more metals chosen from the group consisting of Groups 6, 9 and 10; and c) optionally a metal chosen from Group 14 in an amount up to 0.5 wt %, on the basis of total catalyst.2. An alkylaromatic conversion catalyst as claimed in claim 1 , wherein the refractory oxide binder is chosen from the group consisting of silica claim 1 , zirconia and titania.3. An alkylaromatic conversion catalyst as claimed in claim 1 , wherein the carrier is composed of in the range of from 25 to 60 wt % silica claim 1 , and in the range of from 40 to 75 wt % ZSM-5.4. An alkylaromatic conversion catalyst as claimed in claim 1 , wherein the ZSM-5 has a mesopore volume of from 0.20 to 0.90 ml/g and a crystallite size of from 5 to 80 nm.5. An alkylaromatic conversion catalyst as claimed in claim 1 , wherein the ZSM-5 has a SAR in the range of from 20 to 150.6. An alkylaromatic conversion catalyst as claimed in claim 1 , wherein the binder ...

METHOD FOR CONVERSION OF AROMATIC HYDROCARBONS

A method of converting hydrocarbons requires contacting a hydrocarbon stream containing alkylated aromatic hydrocarbons with a catalyst of a phosphorus-containing pentasil zeolite in a reactor. The phosphorus-containing pentasil zeolite having a phosphorus content of 7.5% or less by weight of zeolite, a pore volume of at least 0.2 ml/g, and a Al MAS NMR spectrum characterized by a peak at or near 50 ppm that is greater than any other peak in said spectrum. A benzene-enriched output stream is recovered from the reactor. 1. A method of converting hydrocarbons comprising: i. a phosphorus content of 7.5% or less by weight of zeolite;', 'ii. a pore volume of at least 0.2 ml/g; and', {'sup': '27', 'iii. a Al MAS NMR spectrum characterized by a peak at or near 50 ppm that is greater than any other peak in said spectrum; and'}], 'a. contacting a hydrocarbon stream containing alkylated aromatic hydrocarbons with a catalyst of a first phosphorus-containing pentasil zeolite in a reactor, said phosphorus-containing pentasil zeolite havingb. recovering a benzene-enriched output stream from the reactor.2. The method of claim 1 , wherein the hydrocarbon stream contains benzene in an amount of less than 15% by weight of the feed and at least one of toluene claim 1 , Caromatics claim 1 , and C aromatics in an amount totaling 50% or more by weight of the hydrocarbon stream.3. The method of claim 2 , further comprising separating benzene from the benzene-enriched output stream to form a benzene product stream and a second output stream.4. The method of claim 3 , further comprising contacting said second output stream with a xylene-selective catalyst in a second reactor to form a xylene-enriched output stream.5. The method of claim 4 , further comprising separating xylene from the said xylene-enriched output stream to form a xylene product stream.6. The method of claim 4 , wherein said xylene selective catalyst is a second phosphorus-containing zeolite that is bound with an inorganic ...

Production of Paraxylene

The process concerns ethylbenzene conversion and xylene isomerization with a catalyst pretreated by sulfiding.

PROCESSES AND APPARATUSES FOR TOLUENE METHYLATION IN AN AROMATICS COMPLEX

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 ...

METHODS OF HEAVY REFORMATE CONVERSION INTO AROMATIC COMPOUNDS

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 ...

INTEGRATED PROCESS FOR MAXIMIZING PRODUCTION OF PARA-XYLENE FROM FULL REFORMATE

A method of producing p-xylene, the method comprising the steps of converting the C9+ aromatic hydrocarbons and the hydrogen gas in the presence of a dealkylation catalyst to produce a dealkylation effluent, separating the dealkylation effluent to produce a carbon-nine (C9) aromatics stream, a xylene stream, and a toluene stream, separating the p-xylenes from the xylene stream in the p-xylene separation unit to produce a p-xylene product and a p-xylene depleted stream, converting the m-xylene and o-xylene in the p-xylene depleted stream in the isomerization unit to produce an isomerization effluent, reacting the C9 aromatics stream and the hydrogen stream in the presence of a transalkylation catalyst in the transalkylation reactor to produce a transalkylation effluent, separating the C6 to C9+ aromatic hydrocarbons in the isomerization effluent and the transalkylation effluent in the splitter column to produce a benzene recycle, a toluene recycle, a xylene recycle and a C9+ recycle. 1. A system for producing p-xylene , the system comprising:a dealkylation reactor, the dealkylation reactor is configured to convert carbon-nine plus (C9+) aromatic hydrocarbons in the presence of hydrogen gas to produce a dealkylation effluent, the dealkylation reactor comprising a dealkylation catalyst, wherein the dealkylation reactor is at a dealkylation temperature, wherein the dealkylation reactor is at a dealkylation pressure, wherein a reformate feed comprises aromatic hydrocarbons, wherein the aromatic hydrocarbons are selected from the group consisting of benzene, toluene, mixed xylenes, carbon-nine plus (C9+) aromatic hydrocarbons, and combinations of the same, wherein a hydrogen feed comprises the hydrogen gas, wherein the dealkylation effluent comprises aromatic hydrocarbons such that an amount of C9+ aromatic hydrocarbons in the dealkylation effluent is less than the amount of C9+ aromatic hydrocarbons in the reformate feed;a reformate splitter fluidly connected to the ...

Dealkylation Process

In a process for dealkylating a poly-alkylated aromatic compound, a feed comprising at least one poly-alkylated aromatic compound selected from polypropylbenzene, polybutylbenzene, and polycyclohexylbenzene is introduced into a reaction zone. The feed is then contacted in the reaction zone with an acid catalyst under conditions effective to dealkylate at least a portion of the poly-alkylated aromatic compound and produce a first reaction product comprising at least one mono-alkylated aromatic compound. 1. A process for dealkylating a poly-alkylated aromatic compound , the process comprising:(a) introducing a feed comprising at least one poly-alkylated aromatic compound selected from polypropylbenzene, polybutylbenzene, and polycyclohexylbenzene into a reaction zone; and(b) contacting the feed in the reaction zone with an acid catalyst under conditions effective to dealkylate at least a portion of the poly-alkylated aromatic compound to produce a first reaction product comprising (i) a first compound comprising at least one mono-alkylated aromatic compound and (ii) a second compound comprising at least one compound selected from an alkane and alkene.2. The process of claim 1 , wherein the poly-alkylated aromatic compound is selected from di-isopropylbenzene claim 1 , tri-isopropylbenzene claim 1 , and mixtures thereof and the first reaction product comprises (i) cumene and (ii) propylene and/or propane.3. The process of claim 1 , wherein the poly-alkylated aromatic compound is selected from di-sec-butylbenzene claim 1 , tri-sec-butylbenzene claim 1 , and mixtures thereof and the first reaction product comprises (i) sec-butylbenzene and (ii) butene and/or butane.4. The process of claim 1 , wherein the poly-alkylated aromatic compound is selected from di-cyclohexylbenzene claim 1 , tri-cyclohexylbenzene claim 1 , and mixtures thereof and the first reaction product comprises (i) cyclohexylbenzene and (ii) cyclohexene and/or cyclohexane.5. The process of any preceding ...

PROCESSES FOR PRODUCING LINEAR ALKYLBENZENES

One or more process for the production of a linear alkylbenzenes which can be used to produce surfactants. The linear hydrocarbon and the aromatic hydrocarbon are both produced from a renewable feedstock. The linear hydrocarbon may be produced by deoxygenating a natural oil and dehydrogenating the resulting hydrocarbon to provide an olefinic hydrocarbon. The aromatic hydrocarbon may be produced from the pyrolysis of a biomass and the deoxygenation of a pyrolysis oil. 1. A process for generating an alkylbenzene product comprising:producing a linear hydrocarbon from a renewable triglyceride feedstock;producing an aromatic hydrocarbon from a biomass feedstock;reacting the linear hydrocarbon produced from the renewable triglyceride feedstock and the aromatic hydrocarbon produced from the biomass feedstock to produce an alkylbenzene product.2. The process of wherein the linear hydrocarbon is produced by deoxygenating the renewable triglyceride feedstock to provide a deoxygenated linear hydrocarbon.3. The process of wherein the deoxygenated linear hydrocarbon is dehydrogenated to provide a linear olefin hydrocarbon claim 2 , and wherein the linear olefin hydrocarbon is reacted with the aromatic hydrocarbon to produce the alkylbenzene product.4. The process of wherein the linear hydrocarbon comprises a linear olefin hydrocarbon.5. The process of wherein the aromatic hydrocarbon is produced from the biomass feedstock by pyrolysis.6. The process of wherein the pyrolysis produces a pyrolysis oil.7. The process of wherein the pyrolysis oil is deoxygenated under conditions to maintain aromatic hydrocarbons and to provide a benzene rich aromatic stream.8. The process of wherein the benzene rich aromatic stream is reacted with the linear hydrocarbon produced from the renewable feedstock.9. A process for generating an alkylbenzene product from renewable resources claim 7 , the process comprising:deoxygenating a renewable triglyceride feedstock in a deoxygenation zone having a ...

Methods of producing composite zeolite catalysts for heavy reformate conversion into xylenes

A method of forming a composite zeolite catalyst includes combining a silicon source and an aqueous organic structure directing agent having a polyamino cation compound to form a silica intermediary gel, introducing an aluminum precursor to the silica intermediary gel to form a catalyst precursor gel, evaporating water in the catalyst precursor gel to form a catalyst gel, and heating the catalyst gel to form a composite zeolite catalyst particle having an intergrowth region with a mixture of both Beta crystals and ZSM-5 crystals. An associated method of making xylene includes feeding heavy reformate to a reactor, the reactor containing the composite zeolite catalyst, and producing xylene by simultaneously performing dealkylation and transalkylation of the heavy reformate in the reactor, where each composite zeolite catalyst particle is able to catalyze both the dealkylation and transalkylation reactions.

METHODS OF PRODUCING COMPOSITE ZEOLITE CATALYSTS FOR HEAVY REFORMATE CONVERSION INTO XYLENES

A method of forming composite zeolite catalyst particles includes combining a silicon source, an aqueous organic structure directing agent having a polyquaternary ammonium compound, water and an aluminum source to form a catalyst gel. The method also includes heating the catalyst gel to form the composite zeolite catalyst particle having an intergrowth region with a mixture of both Mordenite crystals and ZSM-5 crystals. An associated method of making xylene includes feeding heavy reformate to a reactor, the reactor containing the composite zeolite catalyst particles, and producing xylene by simultaneously performing dealkylation and transalkylation of the heavy reformate in the reactor, where each composite zeolite catalyst particle is able to catalyze both the dealkylation and transalkylation reactions. 2. The method of where the silicon source comprises a silica gel claim 1 , silicon oxide claim 1 , silicon halide claim 1 , tetraalkyl orthosilicate claim 1 , silicic acid claim 1 , fumed silica claim 1 , sodium silicate claim 1 , colloidal silica claim 1 , or combinations thereof.3. The method of where the silicon source is a silica gel and the silica gel is a 20 to 60 wt. % suspension of silica in water.4. The method of where the polyquaternary ammonium compound is a diquaternary ammonium compound.5. The method of where claim 1 ,X is a halogen selected from Cl, Br, I, or combinations thereof,{'sub': '18-22', 'R1 is a substituted or an unsubstituted Calkyl group;'}{'sub': '6', 'R2 is a substituted or an unsubstituted Calkyl group; and'}{'sub': '6-8', 'R3 is a substituted or an unsubstituted Calkyl group or an alkenyl group.'}6. The method of where the aluminum source comprises NaAlO.7. The method of where the aluminum source claim 1 , the silicon source claim 1 , the organic structure directing agent claim 1 , and the water are further combined with NaOH to form the catalyst gel.8. The method of where the heating of the catalyst gel is conducted in a sealed vessel ...

Methods of heavy reformate conversion into aromatic compounds

Method of making BTX compounds including benzene, toluene, and xylene, including feeding heavy reformats to a reactor containing a composite zeolite catalyst. The composite zeolite catalyst includes a mixture of nanocrystalline Beta zeolite (Nano-Beta) comprising crystal size in the range of 10 to 40 nm and ZSM-5. The Nano-Beta, 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.

HYDROCRACKING CATALYST FOR PREPARING LIGHT AROMATIC HYDROCARBON, METHOD FOR PREPARING SAME AND METHOD FOR PREPARING LIGHT AROMATIC HYDROCARBON BY USING SAME

The present disclosure relates to a hydrocracking catalyst for preparing a C-Clight aromatic hydrocarbons having an increased BTX content from a polycyclic aromatic hydrocarbon, a method for preparing the same and a method for preparing a C-Clight aromatic hydrocarbons having an increased BTX content by using the same. More specifically, an effect of obtaining a C-Clight aromatic hydrocarbons having an increased BTX content with a high yield from the byproducts of oil refining and petrochemical processes, which contain polycyclic aromatic hydrocarbons such as naphthalene, alkylnaphthalene, etc., can be achieved by using a catalyst in which one or more metal selected from group VIII and one or more metal selected from group VIB are supported on a composite zeolite support of zeolite beta and zeolite ZSM-5. 1. A hydrocracking catalyst for preparing a C-Clight aromatic hydrocarbons , comprising:(i) a composite zeolite of zeolite beta and zeolite ZSM-5;(ii) a group VIII metal; and(iii) a group VIB metal.2. The hydrocracking catalyst for preparing a C-Clight aromatic hydrocarbons according to claim 1 , which further comprises pseudoboehmite.3. The hydrocracking catalyst for preparing a C-Clight aromatic hydrocarbons according to claim 1 , wherein the group VIII metal is one or more selected from Ni and Co claim 1 , and the group VIB metal is one or more selected from Mo and W.4. The hydrocracking catalyst for preparing a C-Clight aromatic hydrocarbons according to claim 1 , wherein the group VIII metal and the group VIB metal are in the form of sulfides.5. The hydrocracking catalyst for preparing a C-Clight aromatic hydrocarbons according to claim 1 , wherein the content of the composite zeolite is 50-95 wt % based on the total weight of the hydrocracking catalyst.6. The hydrocracking catalyst for preparing a C-Clight aromatic hydrocarbons according to claim 1 , wherein the content of the zeolite ZSM-5 is 5-50 wt % based on based on the total weight of the composite ...

METHODS OF HEAVY REFORMATE CONVERSION INTO AROMATIC COMPOUNDS

Methods of making BTX compounds including benzene, toluene, and xylene include feeding heavy reformate to a reactor containing a composite zeolite catalyst. The composite zeolite catalyst includes a mixture of SSZ-33 and ZSM-5. The SSZ-33, the ZSM-5, or both comprise 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 method of making BTX compounds including benzene , toluene , and xylene , the method comprising:feeding heavy reformate to a reactor, the reactor containing a composite zeolite catalyst comprising a mixture of SSZ-33 and ZSM-5, where the SSZ-33, the ZSM-5, or both comprise one or more impregnated metals; andproducing the BTX compounds by simultaneously performing transalkylation and dealkylation of the heavy reformate in the reactor, where the composite zeolite catalyst is able to simultaneously catalyze both the transalkylation and dealkylation reactions.2. The method of claim 1 , where the heavy reformate comprises at least 15 wt. % methylethvlbenzene (MEB) and at least 50 wt. % trimethylbenzene (TMB).3. The method 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.4. The method of claim 1 , where the one or more impregnated metals comprise rhenium.5. The method of claim 1 , where the SSZ-33 claim 1 , the ZSM-5 claim 1 , or both the SSZ-33 and ZSM-5 comprise 0.01 wt. % to 20 wt. % of the one or more impregnated metals.6. The method of claim 1 , where the composite zeolite catalyst comprises a mixture of SSZ-33 and ...

Methods of heavy reformate conversion into aromatic compounds

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.

CATALYST FOR CONVERTING HEAVY REFORMATE TO PRODUCE BTX COMPOUNDS

A method of making BTX (benzene, toluene, xylene) compounds by feeding a heavy reformate stream to a reactor, where the reactor includes a composite zeolite catalyst, that contains a mixture of a desilicated mesoporous mordenite and ZSM-5, and in which the desilicated mesoporous mordenite, the ZSM-5, or both, comprise one or more impregnated metals. The composite zeolite catalyst is able to catalyze the transalkylation reaction and the dealkylation reaction simultaneously to produce the BTX compounds. 1. A method of making BTX compounds comprising benzene , toluene , and xylene , the method comprising: where the composite zeolite catalyst comprises a mixture of a desilicated mesoporous mordenite and ZSM-5, and', 'the desilicated mesoporous mordenite, the ZSM-5, or both, comprise one or more impregnated metals; and, 'feeding a heavy reformate stream to a reactor, the reactor comprising a composite zeolite catalyst,'}producing the BTX compounds by simultaneously performing a transalkylation reaction and a dealkylation reaction of the heavy reformate stream in the reactor, where the composite zeolite catalyst is able to catalyze the transalkylation reaction and the dealkylation reaction simultaneously.2. The method of claim 1 , where the heavy reformate stream comprises at least 15 weight percent (wt. %) methylethylbenzene (MEB) and at least 50 wt. % trimethylbenzene (TMB) claim 1 , based on the total weight of the heavy reformate stream.3. The method of claim 1 , where the one or more impregnated metals are selected from Group VI and Group VII according to IUPAC nomenclature claim 1 , in which the metal in the zeolite catalyst is from 0.05 to 10 wt. % claim 1 , based on the total weight of the zeolite catalyst.4. The method of claim 1 , where the composite zeolite catalyst has a weight ratio of ZSM-5 to desilicated mesoporous mordenite of from greater than 0 to 1.0.5. The method of claim 1 , where the composite zeolite catalyst comprises a mixture of ZSM-5 and ...

METHOD FOR PRODUCING 2,4-DIENAL ACETAL COMPOUND AND 2,4-DIENAL COMPOUND

Methods of producing a 2,4-dienal acetal compound and a 2,4-dienal compound useful as synthesis intermediates of a sex pheromone compound having a conjugated diene structure or a conjugated triene structure. More specifically, a method produces a 2,4-dienal acetal compound of Formula (2): RCH═CH—CH═CH—CH(OR)(OR), including a step of subjecting a 2-enal acetal compound having a leaving group X at position C5 and being expressed by Formula (1): RCHX—CH—CH═CH—CH(OR)(OR) to an elimination reaction in the presence of a base to obtain the 2,4-dienal acetal compound (2); and a method for producing a 2,4-dienal compound of Formula (3): RCH═CH—CH═CH—CHO, further including a step of deprotecting the 2,4-dienal acetal compound (2) to obtain the 2,4-dienal compound (3). 2. The method for producing a 2 claim 1 ,4-dienal acetal compound according to claim 1 , wherein the base is selected from the group consisting of a metal alkoxide claim 1 , an organometallic reagent claim 1 , a metal amide claim 1 , a metal hydride claim 1 , and an amine.3. The method for producing a 2 claim 1 ,4-dienal acetal compound according to claim 1 , wherein the Ris a hydrogen atom.5. The method for producing a 2 claim 4 ,4-dienal compound according to claim 4 , wherein the base is selected from the group consisting of a metal alkoxide claim 4 , an organometallic reagent claim 4 , a metal amide claim 4 , a metal hydride claim 4 , and an amine.6. The method for producing a 2 claim 4 ,4-dienal compound according to claim 4 , wherein the Ris a hydrogen atom.7. The method for producing a 2 claim 2 ,4-dienal acetal compound according to wherein the Ris a hydrogen atom.8. The method for producing a 2 claim 5 ,4-dienal compound according to claim 5 , wherein the Ris a hydrogen atom. The invention relates to methods of producing a 2,4-dienal acetal compound and a 2,4-dienal compound useful as synthesis intermediates of the sex pheromone of an insect.A sex pheromone of insect is a usually bioactive substance ...

PROCESS FOR PRODUCING BENZENE AND LPG2

The invention is directed to a process for producing benzene and LPG comprising the steps of: (a) reacting a source feed stream comprising monoaromatic compounds of formula (I), wherein R1-R5 are the same or different and are chosen from hydrogen or a linear alkyl group of 1-10 carbon atoms, and methanol in an alkylation reactor comprising a basic catalyst to obtain an alkylation product stream and subsequently (b) contacting the alkylation product stream in the presence of hydrogen in a hydrocracking reactor with a 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 to produce a hydrocracking product stream comprising benzene and LPG under process conditions including a temperature of 425-580° C., a pressure of 300-5000 kPa gauge and a Weight Hourly Space Velocity of 0.1-15 h. 2. The process according to claim 1 , wherein step (b) involves further feeding in the hydrocracking reactor a second feed stream comprising C5-C12 hydrocarbons.3. The process according to claim 1 , wherein the monoaromatic compounds comprise toluene claim 1 , xylene and/or 1 claim 1 ,3 claim 1 ,5-trimethyl benzene.4. The process according to claim 1 , wherein the source feed stream comprises C5-C12 hydrocarbons.5. The process according to claim 1 , wherein the second feed stream comprises pyrolysis gasoline claim 1 , straight run naphtha claim 1 , light coker naphtha and coke oven light oil or mixtures thereof.6. The process according to claim 1 , further comprising the step of separating the hydrocracking product stream into benzene claim 1 , LPG and optionally a stream comprising alkyl monoaromatic compounds.7. The process according to claim 6 , wherein the source feed stream comprises the stream comprising the alkyl monoaromatic compounds separated from the hydrocracking product stream and fed back to the alkylation reactor.8. The ...

CATALYST SYSTEM AND PROCESS FOR CONVERSION OF A HYDROCARBON FEED UTILIZING THE CATALYST SYSTEM

The present invention relates to a catalyst system comprising: i. a first layer of a hydrocarbon conversion catalyst, the hydrocarbon conversion catalyst comprising: a first composition comprising a platinum group metal on a solid support; and a second composition comprising a transition metal on an inorganic support; ii. a second layer comprising a cracking catalyst; and to a process for conversion of a hydrocarbon feed utilizing this catalyst system. 1. A catalyst system comprising: a first composition comprising a dehydrogenation active metal on a solid support; and', 'a second composition comprising a transition metal on an inorganic support; and, 'i. a first layer of a hydrocarbon conversion catalyst, the hydrocarbon conversion catalyst comprisingii. a second layer comprising a cracking catalyst.2. The catalyst system according to claim 1 , wherein the cracking catalyst comprises a molecular sieve.3. The catalyst system according to claim 2 , wherein the molecular sieve is zeolite and/or silicalite.4. The catalyst system according to claim 3 , wherein the zeolite is selected from ZSM-5 claim 3 , ZSM-11 claim 3 , SAPO-11 claim 3 , and mixtures thereof.5. The catalyst system according to claim 1 , wherein a weight ratio of the first layer to the second layer is from 50:1 to 1:20.6. The catalyst system according to claim 1 , wherein the dehydrogenation active metal is selected from platinum claim 1 , palladium claim 1 , iridium claim 1 , chromium claim 1 , and mixtures thereof.7. The catalyst system according to claim 1 , wherein the solid support is selected from aluminium oxide claim 1 , silicon dioxide claim 1 , zirconium dioxide claim 1 , titanium dioxide claim 1 , magnesium oxide claim 1 , calcium oxide claim 1 , and mixtures thereof.8. The catalyst system according to claim 1 , wherein the transition metal is selected from molybdenum claim 1 , tungsten claim 1 , rhenium claim 1 , and mixtures thereof.9. The catalyst system according to claim 1 , wherein the ...

METHODS FOR PRODUCING AROMATICS AND OLEFINS

The presently disclosed subject matter provides methods for producing olefins and/or aromatics from coker naphtha. In a non-limiting embodiment, a method for producing aromatics includes hydrogenating the coker naphtha stream in the presence of a first catalyst to remove diolefins and sulfur, if any, to obtain a hydrogenated stream and subjecting the hydrogenated stream to aromatization in the presence of a second catalyst to produce an aromatic-rich stream that includes benzene, toluene and xylene. In certain embodiments, a method for producing olefins includes hydrogenating the coker naphtha stream in the presence of a first catalyst to remove diolefins and sulfur, if any, to obtain a hydrogenated stream and subjecting the hydrogenated stream to catalytic cracking in the presence of a second catalyst to produce an olefin-rich stream that includes ethylene, propylene and aromatics. 1. A method for producing aromatics from a coker naphtha stream , the method comprising:(a) hydrogenating the coker naphtha stream in the presence of a first catalyst to remove diolefins and sulfur, if any, to obtain a hydrogenated stream; and(b) subjecting the hydrogenated stream to aromatization in the presence of a second catalyst to produce an aromatic-rich stream comprising benzene, toluene, and xylene.2. The method of claim 1 , further comprising removing silica and particulates claim 1 , if any claim 1 , from the coker naphtha stream prior to hydrogenation.3. The method of claim 1 , wherein the second catalyst has a metal oxide loading of about 0.2 to about 1.5 weight % and is selected from the group consisting of Ga/Nd/ZSM-5 claim 1 , Ga/Pt/Ge/ZSM-5 claim 1 , Pt/Ga/ZSM-5 claim 1 , Pt/Ge/ZSM-5 and Ni—W/Ga/Z SM-5.4. The method of claim 1 , wherein the aromatic-rich stream comprises at least about 40% of aromatic compounds.5. The method of claim 1 , further comprising hydrodealkylating the aromatic-rich stream in the presence of a third catalyst and hydrogen to produce a benzene- ...

Transalkylation of Heavy Aromatic Hydrocarbon Feedstocks

A process for producing xylene comprises contacting a first feed comprising C 9+ aromatic hydrocarbons, at least one C 6 -C 7 aromatic hydrocarbon and hydrogen with a first catalyst composition to dealkylate 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 with at least part of the C 6 -C 7 aromatic hydrocarbon to produce a first product comprising xylene. Each of the first and second catalyst compositions is substantially free of amorphous alumina.

Method of increasing alpha-olefin content

Implementations described herein generally relate to methods for purifying alpha-olefins. The alpha-olefins may be used to form drag reducing agents for improving flow of hydrocarbons through conduits, particularly pipelines. In one implementation, a method of increasing alpha-olefin content is provided. The method includes providing an olefin feedstock composition having an alpha-mono-olefin and at least one of a diolefin having an equal number of carbon atoms to the alpha-mono-olefin and/or a triolefin having an equal number of carbon atoms to the alpha-mono-olefin. The method further includes contacting the olefin feedstock composition with ethylene in the presence of a catalyst composition including an olefin metathesis catalyst. The method further includes reacting the olefin feedstock composition and ethylene at metathesis reaction conditions to produce an alpha-olefin product comprising the alpha-mono-olefin and alpha-olefins having fewer carbon atoms than the alpha-mono-olefin.

Process for the Production of Xylenes

In a process for producing para-xylene, a feed stream comprising C 6+ aromatic hydrocarbons is separated into a C 7− aromatic hydrocarbon-containing stream, a C 8 aromatic hydrocarbon-containing stream, and a C 9+ aromatic hydrocarbon-containing stream. The C 7− aromatic hydrocarbon-containing stream is contacted with a methylating agent to convert toluene to xylenes and produce a methylated effluent stream. Ethylbenzene is removed from the C 8 aromatic hydrocarbon-containing stream, para-xylene is recovered from the ethylbenzene-depleted C 8 aromatic hydrocarbon-containing stream and the methylated effluent stream in a para-xylene recovery section to produce a para-xylene depleted stream, which is then contacted with a xylene isomerization catalyst under liquid phase conditions effective to isomerize xylenes in the para-xylene depleted stream and produce an isomerized stream. The C 9+ -containing stream with a transalkylation catalyst under conditions effective to convert C 9+ -aromatics to C 8− -aromatics and produce a transalkylated stream, which is recycled together with the isomerized stream to the para-xylene recovery section.

A Method of Co-Processing Fluidized Catalytic Cracking Naphtha and Pyrolysis Gasoline

An integrated process for forming a combined feedstock stream comprising catalytically cracking a first hydrocarbon feedstock to form a full range cracked full naphtha stream and a first light olefins stream, steam cracking a second hydrocarbon feedstock to form a pyrolysis gasoline stream and a second light olefins stream mixing at least a portion of each of the full range cracked naphtha stream and the pyrolysis gasoline stream to form a combined stream, hydro-processing the combined stream to form a hydro-processed combined stream splitting the hydro-processed combined stream into a C/Cstream, and a first aromatic rich stream, splitting the first aromatic rich stream into a second aromatic rich stream and a heavy oil stream. 1. An integrated process for forming a combined feedstock stream comprising a pyrolysis gasoline stream and a full range cracked naphtha stream to produce a plurality of olefin streams and a plurality of aromatic hydrocarbon streams , comprising:catalytically cracking a first hydrocarbon feedstock to form a full range cracked naphtha stream and a first light olefins stream wherein the first light olefins stream comprises ethylene, propylene, butadiene and/or any combination thereof;steam cracking a second hydrocarbon feedstock to form a heavy pyrolysis oil stream, a pyrolysis gasoline stream and a second light olefins stream wherein the second light olefins stream comprises ethylene, propylene, butadiene and/or any combination thereof;mixing at least a portion of the full range cracked naphtha stream and at least a portion of the pyrolysis gasoline stream to form a combined stream;hydro-processing the combined stream to form a hydro-processed combined stream and a light pyrolysis oil stream; [{'sub': 5', '6, 'a C/Cstream; and'}, {'sub': 6', '7', '8', '9, 'a first aromatic rich stream comprising Cmolecules, Cmolecules, Cmolecules, Cmolecules and/or any combination thereof; and'}], 'splitting the hydro-processed combined stream into a second ...

Transalkylation of Heavy Aromatic Hydrocarbons

A process for producing xylene from C 9+ aromatic hydrocarbons comprises contacting a first feedstock comprising C 9+ aromatic 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 C 9+ aromatic hydrocarbons and produce a first product comprising benzene, toluene and residual C 9+ aromatic hydrocarbons. A second feedstock comprising C 9+ aromatic hydrocarbons and benzene and/or toluene is contacted with a second catalyst under effective liquid phase C 9+ transalkylation conditions to transalkylate at least part of the C 9+ aromatic hydrocarbons and produce a second product comprising xylenes.

CATALYST COMPOSITION, ITS PREPARATION AND PROCESS USING SUCH COMPOSITION

Catalyst composition comprising a carrier and one or more Group 10 metal components, wherein the carrier comprises (i) 20 to 90 wt % mordenite having a silica to alumina molar ratio in the range of from 10 to 60; (ii) 10 to 70 wt % ZSM-5 type zeolite having a silica to alumina molar ratio in the range of from 5 to 50 and an average particle size in the range of from 5 to 50 nm; and (iii) 10 to 50 wt % of binder; a process for preparing the catalyst, and a process for the conversion of an aromatic hydrocabons-containing feedstock using the catalyst. 1. A catalyst composition which comprises a carrier and one or more metal components supported on the carrier , wherein the carrier comprises (i) mordenite in an amount in the range of from 20 to 90 wt % , based on total weight of carrier , the mordenite having a silica to alumina molar ratio in the range of from 10 to 60; (ii) ZSM-5 type zeolite in an amount of from 10 to 70 wt % , based on total weight of carrier , the ZSM-5 type zeolite having a silica to alumina molar ratio in the range of from 5 to 50 and an average particle size in the range of from 5 to 50 nm; and (iii) an inorganic binder in an amount in the range of from 10 to 50 wt % , based on total weight of carrier; and wherein the one or more metal components comprise a group 10 metal.2. The catalyst composition according to claim 1 , wherein the mordenite is present in an amount in the range of from 30 to 70 wt % claim 1 , based on total weight of carrier.3. The catalyst composition according to claim 1 , wherein the ZSM-5 type zeolite is present in an amount in the range of from 15 to 60 wt % claim 1 , based on total weight of carrier.4. The catalyst composition according to claim 1 , wherein the inorganic binder is present in an amount in the range of from 10 to 40 wt % claim 1 , based on total weight of carrier material.5. The catalyst composition according to claim 1 , wherein the ZSM-5 type zeolite has a number average particle size in the range of ...

Catalysts and Processes for Making Catalysts for Producing Neopentane

Catalysts and processes for producing catalysts for neopentane production are provided herein. A process includes reducing a catalyst precursor comprising a transition metal and an inorganic support at a temperature less than 500° C. to produce a catalyst. Also provided herein are processes to produce neopentane using the catalysts described herein and neopentane compositions produced therefrom. 1. A process for making a demethylation catalyst , the process comprising reducing a catalyst precursor comprising a transition metal and an inorganic support at a temperature less than 500° C. to produce the demethylation catalyst.2. The process of claim 1 , wherein the catalyst precursor is reduced at a temperature less than 450° C.3. The process of claim 1 , wherein the catalyst precursor is reduced at a temperature from 375° C. to 425° C.4. The process of claim 1 , wherein the catalyst precursor is reduced in the presence of a reducing agent.5. The process of claim 4 , wherein the reducing agent is hydrogen.6. The process of claim 1 , wherein the catalyst precursor is reduced in the presence of 100 to 500 standard cubic centimeters per minute of hydrogen.7. The process of claim 1 , wherein the catalyst precursor is reduced in the presence of at least 250 standard cubic centimeters per minute of hydrogen.8. The process of claim 1 , wherein the catalyst precursor is reduced at a temperature less than 450° C. and in the presence of 100 to 500 standard cubic centimeters per minute of hydrogen.9. The process of claim 1 , further comprising impregnating the inorganic support with the transition metal.10. The process of claim 1 , further comprising precipitating the catalyst precursor from a solution including the transition metal claim 1 , the inorganic support claim 1 , and a precipitating agent.11. The process of claim 10 , wherein the precipitating agent comprises urea.12. The process of claim 1 , wherein the transition metal comprises iron claim 1 , cobalt claim 1 , nickel ...

Processes to Make Neopentane Using Shell and Tube Reactors

Processes for producing neopentane are disclosed herein. Processes comprise demethylating a C-Calkane within a shell and tube reactor to produce a demethylation product including at least 10 wt % neopentane based on the weight of the demethylation product. 1. A process for producing neopentane , the process comprising demethylating a C-Calkane within a shell and tube reactor to produce a demethylation product including at least 10 wt % neopentane based on the weight of the demethylation product.2. The process of claim 1 , wherein the shell and tube reactor includes a tube having a diameter from 10 mm to 100 mm.3. The process of claim 1 , wherein the diameter is from 40 mm to 60 mm.4. The process of claim 1 , wherein the C-Calkane comprises isooctane.5. The process of further comprising dimerizing isobutylene to produce a dimerization product including diisobutylene and hydrogenating the diisobutylene to produce the isooctane.6. The process of further comprising contacting isobutane with butylenes under alkylation conditions effective to produce an alkylation product including the isooctane.7. The process of claim 1 , wherein the C-Calkane comprises neohexane claim 1 , neoheptane claim 1 , or a combination thereof.8. The process of further comprising isomerizing C-Cparaffins to produce an isomerization product including the neohexane claim 7 , neoheptane claim 7 , or the combination thereof.9. The process of claim 1 , wherein demethylating the C-Calkane comprises contacting the C-Calkane with a catalyst.10. The process of claim 9 , wherein contacting the C-Calkane with the catalyst is carried out at a temperature of about 200° C. to about 500° C.11. The process of claim 9 , wherein contacting the C-Calkane with the catalyst is carried out at a temperature of about 220° C. to about 300° C.12. The process of claim 9 , wherein contacting the C-Calkane with the catalyst is carried out in the presence of hydrogen.13. The process of claim 12 , wherein contacting the C- ...

METHOD AND SYSTEM FOR PRODUCING BENZENE

A method () is proposed for the manufacture of benzene, in which a first feedstock mixture is formed, which contains alkylated aromatics and hydrogen, and in which the alkylated aromatics contained in the first feedstock mixture are partially converted with the hydrogen contained in the first feedstock mixture to the benzene through hydrodealkylation (), thereby obtaining a first product mixture, wherein the first product mixture contains the benzene, the unconverted alkylated aromatics, alkanes with one to three carbon atoms formed in the conversion of the alkylated aromatics to the benzene, and the unconverted hydrogen, and wherein at least a part of the alkanes with one to three carbon atoms and of the hydrogen are separated from the first product mixture, thereby obtaining a light-gas fraction. It is proposed that the hydrogen contained in the first feedstock mixture is provided at least in part with the use of a low-temperature separation (), to which at least a part of a second product mixture is supplied, wherein the second product mixture is formed at least in part through steam cracking () of a second feedstock mixture, and that the light-gas fraction is also supplied at least in part to the low-temperature separation (). A corresponding plant also forms the subject matter of the invention. 1. A method for the manufacture of benzene , in which a first feedstock mixture is formed , which contains alkylated aromatics and hydrogen , and in which the alkylated aromatics contained in the first feedstock mixture are partially converted with the hydrogen contained in the first feedstock mixture to the benzene through hydrodealkylation , thereby obtaining a first product mixture , wherein the first product mixture contains the benzene , the unconverted alkylated aromatics , alkanes with one to three carbon atoms formed in the conversion of the alkylated aromatics to the benzene , and the unconverted hydrogen , and wherein at least a part of the alkanes with one to ...

Heterogeneous catalyst process

HETEROGENEOUS CONVERSION CATALYSTS ARE PREPARED BY FORMING, IN AN INERT ATMOSPHERE, COMPLEXES BETWEEN A REDUCED TRANSITION METAL AND A SUPPORT, THE COMPLEX IS THEN STABILIZED BY HEATING. THE CATALYSTS SO FORMED MAY BE USED FOR THE CONVERSION OF ORGANIC FEED COMPOUNDS IN THE PRESENCE OF HYDROGEN.

Process for the preparation of aromatic compounds by dealkylation

Improved method for reacting hydrocarbons on a catalyst in the presence of steam

The invention relates to a method for producing benzene by dealkylating alkyl-mono- and polysubstituted benzenes having 7 to 12 carbon atoms in the presence of a heterogeneous catalyst and steam.

Method for producing aromatics, in particular benzol, by the aromatisation of non-aromatics using water vapour and the subsequent dealkylation of alkyl-substituted aromatic hydrocarbons using hydrogen

The invention relates to a method for the dealkylation of alkyl-substituted aromatic hydrocarbons. According to said method, in step (I), non-aromatic hydrocarbons comprising 6 or more carbon atoms are aromatised in the presence of water vapour and a catalyst and in step (II) at least part of the product stream obtained in step (I), said stream containing alkyl-substituted aromatic hydrocarbons, is converted with the aid of hydrogen, optionally in the presence of a catalyst, dealkylating the alkyl-substituted aromatic hydrocarbons.

Method for the aromatisation of non-aromatics and the subsequent dealkylation of alkyl-substituted aromatic hydrocarbons using water vapour

The invention relates to a method for dealkylating alkyl-substituted aromatic hydrocarbons. According to said method, in step (I) non-aromatic hydrocarbons comprising 6 or more carbon atoms are aromatised in the presence of water vapour and a catalyst and in step (II) at least part of the product stream obtained in step (I), said stream containing alkyl-substituted aromatic hydrocarbons, is converted with the aid of water vapour in the presence of a catalyst, dealkylating the alkyl-substituted aromatic hydrocarbons.