EP0000812A1 - Procédé d'isomérisation de xylènes - Google Patents

Procédé d'isomérisation de xylènes Download PDF

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Publication number
EP0000812A1
EP0000812A1 EP7878300170A EP78300170A EP0000812A1 EP 0000812 A1 EP0000812 A1 EP 0000812A1 EP 7878300170 A EP7878300170 A EP 7878300170A EP 78300170 A EP78300170 A EP 78300170A EP 0000812 A1 EP0000812 A1 EP 0000812A1
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Prior art keywords
zeolite
xylene
zsm
silica
catalyst
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Granted
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EP7878300170A
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German (de)
English (en)
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EP0000812B1 (fr
Inventor
Samuel Allen Tabak
Roger Allan Morrison
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ExxonMobil Oil Corp
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Mobil Oil Corp
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively
    • B01J29/42—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively containing iron group metals, noble metals or copper
    • B01J29/46—Iron group metals or copper
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively
    • B01J29/42—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively containing iron group metals, noble metals or copper
    • B01J29/44—Noble metals
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
    • C07C5/22—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by isomerisation
    • C07C5/27—Rearrangement of carbon atoms in the hydrocarbon skeleton
    • C07C5/2729—Changing the branching point of an open chain or the point of substitution on a ring
    • C07C5/2732—Catalytic processes
    • C07C5/2737—Catalytic processes with crystalline alumino-silicates, e.g. molecular sieves
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
    • B01J2229/10—After treatment, characterised by the effect to be obtained
    • B01J2229/26—After treatment, characterised by the effect to be obtained to stabilize the total catalyst structure
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
    • B01J2229/30—After treatment, characterised by the means used
    • B01J2229/42—Addition of matrix or binder particles
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts

Definitions

  • This invention relates to the isomerization of xylenes in a C 8 fraction which also contains ethylbenzene.
  • a process for isomerizing xylenes mixed with ethyl benzene by contact at conversion conditions with a catalyst comprising a zeolite having a constraint index of 1 to 12, is characterized by the fact that the zeolite has a silica/alumina ratio of at least 500 and the conversion temperature is above 800°F.
  • the preferred zeolites are ZSM-5 itself and ZSM-5(ccM), particularly ZSM-5 (ccPt). They are advantageously employed in composited form,, the zeolite constituting from 1 to 99, preferably 5 to 80, weight percent of a composite with a binder.
  • the temperature range usually employed is 800 to 1000°F, and the zeolite silica/alumina mole ratio can range up to 3000.
  • the process of the invention thus uses a zeolite of low alumina content, and therefore of low acid exchange capacity, which may also contain metals such a platinum or nickel.
  • a zeolite of low alumina content and therefore of low acid exchange capacity, which may also contain metals such a platinum or nickel.
  • the temperature is raised to 800°F. or higher to effect xylene isomerization.
  • ethyl benzene reacts primarily via dealkylation to benzene and ethane rather than via disproportionation to benzene and diethyl benzene, a mechanism fairly independent of catalyst acidity.
  • a lower acidity catalyst can be used to perform the relatively easy xylene isomerization, and the amount of xylenes disproportionated is eliminated.
  • the reduction of xylene losses is important because about 75% of the xylene stream is recycled in the loop resulting in an ultimate xylene loss of 6-10 wt.% by previous processes.
  • the new process also allows greater flexibility with respect to charge stock. Since ethyl benzene conversion is relatively independent of isomerization, high ethyl benzene containing charge stocks can be processed, which means that charge stocks from thermal crackers (about 30 wt.% ethyl benzene) can be used as well as conventional stocks from reformers. In addition, dealkylation of C 2 + alkyl groups is favored since the temperature is above 800 o F. As a result, paraffins in the charge stock will not alkylate the aromatic rings, eliminating xylene loss via this mechanism. Thus, this new process can process paraffins in the charge by cracking them to lighter paraffins eliminating the need for their removal by techniques such as extraction. Finally, a small portion of the cracked fragments are recombined to form new aromatic rings which results in a net increase of aromatic rings.
  • the single figure of the drawing is a flow sheet of a typical xylene isomerization plant for processing C 8 feeds, in which the invention may be applied.
  • the charge introduced by line 4 is a mixture of eight carbon atom alkyl aromatics, namely ethyl benzene and the three xylene isomers.
  • Such charge stocks are derived from catalytic reformates, pyrolysis gasoline, etc. by distillation and solvent extraction to separate aromatic compounds from aliphatics.
  • the present process has the ability, unique among xylene isomerization processes, of converting paraffins, olefins and the like which are separated by the normal distillation facilities of an isomerization loop. This process is therefore capable of accepting charge materials which contain substantial quantities (say up to 15%) of aliphatic hydrocarbons.
  • Isomerized product from reactor 15 is cooled in heat exchanger 16 and passes to a high pressure separator 17 from which separated hydrogen can be recycled in the process.
  • the liquid product of the isomerization passes by line 18 to a strip per 19 from which light ends are passed overhead by line 20.
  • the remaining liquid product constituted by C8 + hydrocabrons is recycled in the system by line 21 to the inlet of xylene stripper column 5.
  • the system is adapted to produce maximum quantities of p-xylene from a mixed C 8 aromatic feed containing all of the xylene isomers plus ethyl benzene .
  • the key to efficient operation for that purpose is in the isomerizer which takes crystallizer effluent lean in p-xylene and converts the other xylene isomers in part to p-xylene for further recovery at the crystallizer.
  • the reactor 15 contains a crystalline aluminosilicate (zeolite) catalyst of relatively low acid activity by reason of its very high silica/alumina ratio of 500 or higher. That catalyst, which is preferably combined with a metal from Group VIII of the Periodic Table promotes a reaction course which is unique at temperatures upwards of 800 0 F. Ethyl benzene in the charge is selectively cracked to benzene and ethane at little or no conversion of xylenes. The two conversions are, as noted above, decoupled such that, for the first time, reaction severity is not a compromise to achieve effective ethyl benzene conversion at "acceptable" loss of xylene.
  • zeolite crystalline aluminosilicate
  • paraffins in the charge are hydrocracked to lighter paraffins, including ethane, which will come off separator 17 with the recycle hydrogen in much greater quantity than that resulting from conversion of ethyl benzene. This requires modification of the usual techniques for maintaining concentration of the recycle hydrogen stream by withdrawal of a drag stream, not shown in the drawing.
  • splitter tower 5 is operated to take o-xylene overhead with the other C 8 aromatics and take only Cg+ as bottoms from tower 5.
  • the preferred zeolites for use according to the invention are the well known zeolites ZSM-5, ZSM-11, ZSM-12, ZSM-35 and ZSM-38, described respectively in U.S. Specifications 3,702,886, 3,709,949, 3,970,544, 4,016,245 and 4,046,859.
  • a particularly preferred form of zeolite ZSM-5 is obtained by crystallization of the zeolite from a solution containing metal ions.
  • Such ZSM-5 variants obtained by co-crystallization of metal and zeolite -which we designate ZSM-5(ccM)- have proven particularly effective in the process of the invention where the variant is one -ZSM-5(ocPt)- containing 0.2 to 0.8 Wt.% platinum.
  • zeolite ZSM-5(ccM) The x-ray diffraction pattern of zeolite ZSM-5(ccM) manifests the following significant d-spacings:
  • ZSM-5(ccM) can be prepared from a reaction mixture having a composition, in terms of mole ratios of oxides, falling within the following ranges:
  • Typical reaction conditions consist of heating the foregoing reaction mixture to a temperature of from . about 100°C to 175°C. for a period of time of from aboutsix hours to 120 days.
  • a more preferred temperature range is from about 95°C. to 175°C. with the amount of time at a temperature in such range being from about 12 hours to 8 days.
  • the digestion of the gel particles is carried out until crystals form.
  • the solid product is separated from the reaction medium, as by cooling the whole to room temperature, filtering and water washing.
  • the foregoing product is dried, e.g. at 230°F., for from about 8 to 24 hours.
  • milder conditions may be employed if desired, e.g. room temperature under vacuum.
  • the specific zeolites described, when prepared in the presence of organic cations, are catalytically inactive, possibly because the intracrystalline free space is occupied by organic cations from the forming . solution. They may be activated by heating in an inert atmosphere at 1000°F. for one hour, for example, followed by base exchange with.ammonium salts followed by calcination at 1000°F. in air.
  • the presence of organic cations in the forming solution may not be absolutely essential to the formation of this type zeolite; however, the presence of these cations does appear to favor the formation of this special type of zeolite. More generally, it is desirable to activate this type catalyst by base exchange with ammonium salts followed by calcination in air at about 1000°F. for from about 15 minutes to about 24 hours.
  • Natural zeolites may sometimes be converted to this type zeolite catalyst by various activation procedures and other treatments such as base exchange, steaming, alumina extraction and calcination, in combinations.
  • Natural minerals which may be so treated include ferrierite, brewsterite, stilbite, dachiardite, epistilbite, heulandite, and clinoptilolite.
  • the zeolites hereof are selected as those having a crystal framework density, in the dry hydrogen form, of not substantially below about 1'.6 grams per cubic centimeter. It has been found that zeolites which satisfy all three of these criteria are most desired. Therefore, the preferred zeolites of this invention are those having a constraint index as defined above of about 1 to about 12, a silica to alumina ratio of at least about 500 and a dried crystal density of not less than about 1.6 grams per cubic centimeter.
  • the dry density for known structures may be calculated from the number of silicon plus aluminum atoms per 1000 cubic Angstroms, as given, e.g. on page 19 of the article on Zeolite Structure by W. M. Meier.
  • the crystal framework density may be determined by classical pykometer techniques. For example, it may be determined by immersing the dry hydrogen form of the zeolite in an organic solvent which is not sorbed by the crystal. It is possible that the unusual sustained activity and stability of this class of zeolites is associated with its high crystal anionic framework density of not less than about 1.6 grams per cubic centimeter. The high density, of course, must be associated with a relatively small amount of free space within the crystal, which might be expected to result in more stable structures. This free space, however, is important as the locus of catalytic activity.
  • Crystal framework densities of some typical zeolites are:
  • the zeolite When synthesized in the alkali metal form, the zeolite is conveniently converted to the hydrogen form, generally by intermediate formation of the aammonium form as a result of amonium ion exehange and calcination of the ammonium form to yield the hydrogen form.
  • the original alkali metal of the zeolite may be replaced by ion exchange with other suitable ions of Groups IB to VIII of the periodie Table, including, by way of example, nickel, copper, zinc, palladium, calcium or rare earth metals.
  • Such matrix matarials include synthetic or naturally occurring substances as well as inorganic materials such as clay, silica and/or metal oxides.
  • the latter may be either naturally occurring or in the form of gelatinous precipitates or gels including mixtures of silica and metal oxides.
  • Naturally occurring clays which can be composited with the zeolite include those of the montmorillcnite and kaolin families, which families include the sub-bentonites and the kaolins commonly known as dixie, McNamee-Georgia and Florida clays or others in which the main mineral constituent is halloysite, kaolinite, dickite, nacrite or anauxite.
  • Such clays can be used in the raw state as originally mined or initially subjected to calcination, acid treatment or chemical modification.
  • the zeolites employed herein may be composited with a porous matrix material, such as alumina, silica-alumina, silica-magnesia, silica-zirconia, silica-thoria, silica-berylia, silica-titania as well as ternary compositions, such as silica-alumina-thoria,silica-alumina-zirconia, silica-alumina-magnesia and silica-magnesia-zirconia.
  • the matrix may be in the form of a cogel.
  • the relative proportions of zeolite component and inorganic oxide gel matrix may vary widely with the zeolite content ranging from between about 1 to about 99 percent by weight and more usually in the range of about 5 to about 80 percent by weight of the composite.
  • Zeolite ZSM-5 (ecPt) having a silica to alumina ratio of 660 and containing 0.23x by weight of platinum was prepared by heating together the following reagents:
  • the product contained 0.23% platinum in ZSM-41 of 660 silica/alumina.
  • Zeolite ZSM-5 (ccPt) having a silica to alumina ratio of 1041 and containing 0.76% by weight of platinum was prepared by heating together the following reagents:
  • the resultant catalyst had a silica/alumina ratio of 1041 and contained 0.76 wt.% platinum.
  • a mixture of hydrocarbons was prepared which simulates charge to the isomer 15 in an operation charging at line 4 of the drawing, a fraction prepared by distillation from catalytic reformate to include the C 8 aromatics.
  • the simulated charge contained 6.9% n-nonane, 30.7% ethyl benzene and 62.4% of a mixture of xylenes poor in p-xylene, viz. 73.3% m-xylene, 17.8% o-xylene and 8.9% p-xylene. That mixture was reacted over the catalyst of Example 1. Reaction conditions and products of the reaction are tabulated in Table V.
  • Example 3 The same charge as in Example 3 was processed over the catalyst of Example 2, with results as shown in Table V.
  • a simulated charge was prepared by blending 9.8% ethyl benzene with 90.2% of mixed xylenes having the composition set out in Example 3. That charge approximates the isomerizer feed in a system supplied with fresh feed prepared by fracticnation of catalytic reformate to sepaRATE A C 8 aromatics cut and solvent extraction to reject the paraffin content of the fraction. Results are shown in Table 7 on processing the simulated charge over the catalyst of Example 2.
  • the reaction is found to proceed in the direction indicated with metal free high silica zeolite, but is less selective than when the zeolite is associated with a metal of Group VIII. Also shorter catalyst life is to be expected with metal-free zeolite catalyst, Particularly preferred are the noble metals of Group VIII, namely platinum, palladium, osmium, iridium, ruthenium and rhodium.
  • the other Group VIII metals, such as nickel exhibit the advantages of the invention to less extent, in some cases by minor increase of xylene loss at conditions to promote increased ethyl benzene conversion, some apparent coupling of the reactions.
  • the metal should be a minor component of the catalyst, say 0.05 to 2.0 weight percent and is preferably highly dispersed.
  • the catalyst is preferably of the ZSM-5(ccM) variety wherein the metal is present in the forming solution from which the zeolite is synthesized.
  • the quantity of metal should be relatively low, say up to 0.2 weight percent. At moderate to high metal content, e.g.
  • the metal-bearing zeolite is of the ZSM-5 (ccM) variety and all the metal « content is derived from metal compounds in the synthesis liquor.
  • Catalyst comprising 0.18 wt.% platinum in zeolite ZSM-5(cePt) of 2000 silica/alumina ratio was prepared from the reaction mixture:
  • Zeolite HZSM-5 of 1000 silica/alumina ratio was prepared from the following mixture:
  • a further ZSM-5 catalyst was prepared by impregnation of zeolite having 1600 silica/alumina ratio with 4.0 weight percent nickel, blending with 35 weight percent alumina and extrusion.
  • Catalyst prepared according to Example 6 and 7 were employed in processing ethyl benzene mixed with xylene in which the distribution of isomers was as described in Example 3. Conditions and results obtained are summarized in Table VI.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
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EP78300170A 1977-07-22 1978-07-20 Procédé d'isomérisation de xylènes Expired EP0000812B1 (fr)

Applications Claiming Priority (2)

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US81817177A 1977-07-22 1977-07-22
US818171 1997-03-14

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EP0000812A1 true EP0000812A1 (fr) 1979-02-21
EP0000812B1 EP0000812B1 (fr) 1981-09-02

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US (1) US4163028A (fr)
EP (1) EP0000812B1 (fr)
JP (1) JPS6024772B2 (fr)
CA (1) CA1096890A (fr)
DE (1) DE2861001D1 (fr)
ES (1) ES471957A1 (fr)
IN (1) IN149484B (fr)
IT (1) IT1099583B (fr)
ZA (1) ZA784167B (fr)

Cited By (7)

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Publication number Priority date Publication date Assignee Title
EP0038141A2 (fr) * 1980-04-14 1981-10-21 Mobil Oil Corporation Préparation de catalyseur pour le traitement d'aromatiques, catalyseur ainsi obtenu, et son utilisation pour l'isomérisation du xylène
EP0097552A1 (fr) * 1982-06-23 1984-01-04 Institut Français du Pétrole Nouveau catalyseur à base de mordénite fortement désaluminée
EP0032414B1 (fr) * 1980-01-10 1986-08-13 Mobil Oil Corporation Amélioration de réformats
US4700012A (en) * 1986-12-30 1987-10-13 Teijin Petrochemical Industries, Ltd. Process for isomerizing xylene
US4723050A (en) * 1986-09-03 1988-02-02 Cosden Technology, Inc. Xylene isomerization process
WO2011104220A1 (fr) 2010-02-26 2011-09-01 Georg Fischer Jrg Ag Agencement de filtre lavable à contre-courant
CN112023978A (zh) * 2019-06-04 2020-12-04 中国石油化工股份有限公司 一种二甲苯异构化催化剂及其制备方法与应用

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US4218573A (en) * 1978-06-12 1980-08-19 Mobil Oil Corporation Xylene isomerization
US4371721A (en) * 1978-12-14 1983-02-01 Mobil Oil Corporation Selective cracking of disubstituted benzenes having polar substituents
JPS55129232A (en) * 1979-03-29 1980-10-06 Teijin Yuka Kk Isomerization of xylenes
US4224141A (en) * 1979-05-21 1980-09-23 Mobil Oil Corporation Manufacture of aromatic compounds
US4231955A (en) * 1979-07-13 1980-11-04 Mobil Oil Corporation Synthesis of alkyl and alkylaminonitriles
JPS5732735A (en) * 1980-08-04 1982-02-22 Teijin Yuka Kk Regenerating method for catalyst
EP0055044B1 (fr) * 1980-12-12 1985-09-18 Exxon Research And Engineering Company Composé de zéolite
ATE14869T1 (de) * 1980-12-12 1985-08-15 Exxon Research Engineering Co Xylol-isomerisierung.
JPS62228031A (ja) * 1981-06-03 1987-10-06 Toray Ind Inc 芳香族炭化水素の変換方法
JPS5877828A (ja) * 1981-11-02 1983-05-11 Toray Ind Inc エチルベンゼンを含むキシレン類の変換方法
US4482773A (en) * 1982-02-25 1984-11-13 Mobil Oil Corporation Catalyst for xylene isomerization
US4469909A (en) * 1982-06-18 1984-09-04 Mobil Oil Corporation Heavy aromatics process
US4563435A (en) * 1982-06-23 1986-01-07 Mobil Oil Corporation Catalytic composition from reaction of high silica zeolites with binder
US4665265A (en) * 1984-06-13 1987-05-12 Mobil Oil Corporation Conversion of olefins and paraffins over novel catalyst composition
US4665253A (en) * 1984-06-13 1987-05-12 Mobil Oil Corporation Conversion of aromatics over novel catalyst composition
US4665269A (en) * 1984-06-13 1987-05-12 Mobil Oil Corporation Conversion of oxygenates over novel catalyst composition
US4681747A (en) * 1984-11-16 1987-07-21 The Standard Oil Company Process for the preparation of metallosilicates of tetravalent lanthanide and actinide series metals using heterpoly metallates
US4899011A (en) * 1986-01-15 1990-02-06 Mobil Oil Corporation Xylene isomerization process to exhaustively convert ethylbenzene and non-aromatics
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US5043512A (en) * 1988-10-06 1991-08-27 Mobil Oil Corp. Alkylaromatic isomerization process
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US5028573A (en) * 1990-01-29 1991-07-02 Mobil Oil Corp. Dual function catalyst and isomerization therewith
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US6342649B1 (en) * 1995-05-10 2002-01-29 Denim Engineering, Inc Method for removing ethylbenzene from a para-xylene feed stream
US5958217A (en) * 1995-11-15 1999-09-28 Chevron Chemical Company Llc Two-stage reforming process that enhances para-xylene yield and minimizes ethylbenzene production
JP3868000B2 (ja) * 1996-01-25 2007-01-17 エクソン・リサーチ・アンド・エンジニアリング・カンパニー 膜を用いる分離法
US6051744A (en) * 1998-12-17 2000-04-18 Chevron Chemical Company Llc Low pressure hydrodealkylation of ethylbenzene and xylene isomerization
US6398947B2 (en) 1999-09-27 2002-06-04 Exxon Mobil Oil Corporation Reformate upgrading using zeolite catalyst
TWI240716B (en) 2000-07-10 2005-10-01 Bp Corp North America Inc Pressure swing adsorption process for separating paraxylene and ethylbenzene from mixed C8 aromatics
TWI263630B (en) * 2003-07-08 2006-10-11 Toray Industries Conversion catalyst for ethylbenzene containing xylenes and process for converting ethylbenzene containing xylenes by using catalyst
US7247762B2 (en) * 2003-09-12 2007-07-24 Exxonmobil Chemical Patents Inc. Process for xylene isomerization and ethylbenzene conversion
US7439204B2 (en) * 2004-03-15 2008-10-21 Exxonmobil Chemical Patents Inc. Process for producing catalysts with reduced hydrogenation activity and use thereof
US7271118B2 (en) * 2004-07-29 2007-09-18 Exxonmobil Chemical Patents Inc. Xylenes isomerization catalyst system and use thereof
RU2015142878A (ru) * 2013-03-15 2017-04-19 Бп Корпорейшн Норс Америка Инк. Бороалюмосиликатные молекулярные сита и способы их применения при изомеризации ксилола
RU2727190C2 (ru) * 2015-10-28 2020-07-21 Бипи Корпорейшен Норт Америка Инк. Улучшенный катализатор превращения этилбензола в способе изомеризации ксилола

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GB1444481A (en) * 1973-09-13 1976-07-28 Mobil Oil Corp Xylene isomerization

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0032414B1 (fr) * 1980-01-10 1986-08-13 Mobil Oil Corporation Amélioration de réformats
EP0038141A2 (fr) * 1980-04-14 1981-10-21 Mobil Oil Corporation Préparation de catalyseur pour le traitement d'aromatiques, catalyseur ainsi obtenu, et son utilisation pour l'isomérisation du xylène
EP0038141A3 (en) * 1980-04-14 1981-12-02 Mobil Oil Corporation Preparation of aromatics processing catalyst, catalyst so prepared, and xylene isomerisation therewith
EP0097552A1 (fr) * 1982-06-23 1984-01-04 Institut Français du Pétrole Nouveau catalyseur à base de mordénite fortement désaluminée
US4723050A (en) * 1986-09-03 1988-02-02 Cosden Technology, Inc. Xylene isomerization process
US4700012A (en) * 1986-12-30 1987-10-13 Teijin Petrochemical Industries, Ltd. Process for isomerizing xylene
WO2011104220A1 (fr) 2010-02-26 2011-09-01 Georg Fischer Jrg Ag Agencement de filtre lavable à contre-courant
CN112023978A (zh) * 2019-06-04 2020-12-04 中国石油化工股份有限公司 一种二甲苯异构化催化剂及其制备方法与应用
CN112023978B (zh) * 2019-06-04 2023-06-09 中国石油化工股份有限公司 一种二甲苯异构化催化剂及其制备方法与应用

Also Published As

Publication number Publication date
CA1096890A (fr) 1981-03-03
EP0000812B1 (fr) 1981-09-02
JPS6024772B2 (ja) 1985-06-14
ES471957A1 (es) 1979-02-01
IT7826000A0 (it) 1978-07-21
JPS5424834A (en) 1979-02-24
DE2861001D1 (en) 1981-11-26
ZA784167B (en) 1980-02-27
US4163028A (en) 1979-07-31
IN149484B (fr) 1981-12-26
IT1099583B (it) 1985-09-18

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