EP0000812B1 - Procédé d'isomérisation de xylènes - Google Patents
Procédé d'isomérisation de xylènes Download PDFInfo
- Publication number
- EP0000812B1 EP0000812B1 EP78300170A EP78300170A EP0000812B1 EP 0000812 B1 EP0000812 B1 EP 0000812B1 EP 78300170 A EP78300170 A EP 78300170A EP 78300170 A EP78300170 A EP 78300170A EP 0000812 B1 EP0000812 B1 EP 0000812B1
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- EP
- European Patent Office
- Prior art keywords
- zeolite
- xylene
- silica
- zsm
- catalyst
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
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Classifications
-
- 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 a fraction which also contains ethylbenzene.
- a process for isomerizing xylenes mixed with ethyl benzene by contact in the presence of hydrogen 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 426°C (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 426 to 538°C (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 as platinum or nickel.
- the temperature is raised to 426°C (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 C2 alkyl groups is favored since the temperature is above 426°C (800°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 smaller 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 separted 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.
- xylenes include toluene disproportionation and methylation of toluene, which are acceptable charge stocks in combination with fractions which contain ethyl benzene.
- charge stock passes by line 4 to a xylene splitter column 5.
- the bottoms from the xylene splitter, constituted by o-xylene and Cg aromatics passes by line 6 to the o-xylene tower 7 from which o-xylene is taken overhead at tine 8 and heavy ends are removed by line 9.
- the overhead from xylene splitter column 5 is transferred to conventional crystallization separation 10 through line 11.
- the crystallizer operates in the manner described in U.S. Specification 3,662,013.
- 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 stripper 19 from which light ends are passed overhead by line 20.
- the remaining liquid product constituted by C 8 + hydrocarbons 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 aluminsolicate (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 Vlll of the Periodic Table promotes a reaction course which is unique at temperatures upward of 426°C (800°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 aluminsolicate
- 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 ⁇ aromatics and take only Cg as bottoms from tower 5.
- the preferred zeolites for use according to the invention are zeolites having lattice structure of the type of the well known zeolites ZSM-5, ZSM-11, ZSM-12, ZSM-35 and ZSM-38, identified respectively in U.S. Specifications 3,702,886, 3,709,979, 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(ccPt)- 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:
- the radiation was the K-alpha doublet copper, and a scintillation counter spectrometer with a strip chart pen recorder was used.
- Table I the relative intensities are given in terms of a subjective evaluation.
- this X-ray diffraction pattern is charateristic of all the species of ZSM-5 (ccM) compositions. Ion exchange of the sodium ion with cations reveals substantially the same pattern with some minor shifts in interplanar spacing and variation in relative intensity. Other minor variations can occur depending on the silica to alumina ratio of the particular sample and the extent of thermal conditioning.
- 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 95°C to 175°C. for a period of time of from about six hours to 120 days.
- a more preferred temperature range is from about 100°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 110°C (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 538°C (1000°F), for one hour, for example, followed by base exchange with ammonium salts followed by calcination at 538°C (1 OOOOF) 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 538°C (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, dachiaridite, 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 namely constraint index, silica/alumina ratio, and crystal density, are most desired. Therefore, the preferred zeolites of this invention are those having a constraint index as defined above of 1 to 12, a silica to alumina ratio of at least 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.
- the crystal framework density may be determined by classical pyknometer 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.
- 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 ammonium form as a result of ammonium ion exchange and calcination of the ammonium form to yield the hydrogen form.
- the hydrogen form In addition to the hydrogen form, other forms of the zeolite wherein the original alkali metal has been reduced to less than about 1.5 percent by weight may be used.
- the original alkali metal of the zeolite may be replaced by ion exchange with other suitable ions of Groups IB to VIII of the Periodic Table, including, by way of example, nickel, copper, zinc, palladium, calcium or rare earth metals.
- Such matrix materials 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 montmorillonite 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-beryllia, 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 1 to 99 percent by weight and more usually in the range of 5 to 80 percent by weight of the composite.
- Zeolite ZSM-5 (ccPt) having a silica to alumina ratio of 660 and containing 0.23% by weight of platinum was prepared by heating together the following reagents:
- the product contained 0.23% platinum in ZSM-5 (cc Pt) 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 isomerizer 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 III.
- Example 3 The same charge as in Example 3 was processed over the catalyst of Example 2, with results as shown in Table III.
- 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 fractionation of catalytic reformate to separate a C a aromatics cut and solvent extraction to reject the paraffin content of the fraction. Results are shown in Table III 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.
- 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, with 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.
- platinum applied by impregnation the catalyst exhibits tendency to loss of benzene rings, apparently by hydrocracking, possibly on relatively large crystals of metal within the pores of the catalyst.
- Catalyst comprising 0.18 wt.% platinum in zeolite ZSM-5 (ccPt) 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 IV.
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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)
- Catalysts (AREA)
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Claims (6)
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US81817177A | 1977-07-22 | 1977-07-22 | |
US818171 | 1997-03-14 |
Publications (2)
Publication Number | Publication Date |
---|---|
EP0000812A1 EP0000812A1 (fr) | 1979-02-21 |
EP0000812B1 true EP0000812B1 (fr) | 1981-09-02 |
Family
ID=25224859
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP78300170A Expired EP0000812B1 (fr) | 1977-07-22 | 1978-07-20 | Procédé d'isomérisation de xylènes |
Country Status (9)
Country | Link |
---|---|
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) |
Families Citing this family (47)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
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 |
AU540104B2 (en) * | 1980-01-10 | 1984-11-01 | Mobil Oil Corp. | Calytic reforming |
US4312790A (en) * | 1980-04-14 | 1982-01-26 | Mobil Oil Corporation | Aromatics processing catalysts |
JPS5732735A (en) * | 1980-08-04 | 1982-02-22 | Teijin Yuka Kk | Regenerating method for catalyst |
EP0054385B1 (fr) * | 1980-12-12 | 1985-08-14 | Exxon Research And Engineering Company | Isomérisation de xylènes |
US4427577A (en) * | 1980-12-12 | 1984-01-24 | Exxon Research & Engineering Co. | Composite zeolite |
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 |
FR2529100B1 (fr) * | 1982-06-23 | 1986-10-03 | Inst Francais Du Petrole | Nouveau catalyseur a base de mordenite fortement desaluminee |
US4665269A (en) * | 1984-06-13 | 1987-05-12 | Mobil Oil Corporation | Conversion of oxygenates over novel catalyst composition |
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 |
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 |
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 |
US4873387A (en) * | 1987-10-13 | 1989-10-10 | Uop | Process for the isomerization of aromatics |
US5043512A (en) * | 1988-10-06 | 1991-08-27 | Mobil Oil Corp. | Alkylaromatic isomerization process |
US5030787A (en) * | 1990-01-24 | 1991-07-09 | Mobil Oil Corp. | Catalytic disproportionation/transalkylation utilizing a C9+ aromatics feed |
US5028573A (en) * | 1990-01-29 | 1991-07-02 | Mobil Oil Corp. | Dual function catalyst and isomerization therewith |
US5082984A (en) * | 1990-01-29 | 1992-01-21 | Mobil Oil Corp. | Dual function catalyst and isomerization therewith |
US5001296A (en) * | 1990-03-07 | 1991-03-19 | Mobil Oil Corp. | Catalytic hydrodealkylation of aromatics |
US5043513A (en) * | 1990-03-07 | 1991-08-27 | Mobil Oil Corp. | Catalytic hydrodealkylation of aromatics |
US5689027A (en) * | 1994-11-18 | 1997-11-18 | Mobil Oil Corporation | Selective ethylbenzene conversion |
US5705726A (en) * | 1994-11-18 | 1998-01-06 | Mobil Oil Corporation | Xylene isomerization on separate reactors |
US5516956A (en) * | 1994-11-18 | 1996-05-14 | Mobil Oil Corporation | Dual bed xylene isomerization |
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 |
CN1088450C (zh) * | 1996-01-25 | 2002-07-31 | 埃克森研究工程公司 | 使用膜的分离方法 |
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 |
ES2458100T3 (es) | 2010-02-26 | 2014-04-29 | Georg Fischer Jrg Ag | Disposición de filtrado de lavado a contracorriente |
MX2015012209A (es) * | 2013-03-15 | 2015-12-01 | Bp Corp North America Inc | Tamices moleculares de aluminosilicato de mfi y metodos para su uso para isomerizacion de xileno. |
SG11201802653RA (en) * | 2015-10-28 | 2018-05-30 | Bp Corp Nurth America Inc | Improved catalyst for ethylbenzene conversion in a xylene isomerrization process |
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 |
Family Cites Families (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3856872A (en) * | 1973-09-13 | 1974-12-24 | Mobil Oil Corp | Xylene isomerization |
JPS5341658B2 (fr) * | 1973-09-13 | 1978-11-06 | ||
US3856873A (en) * | 1973-09-13 | 1974-12-24 | Mobil Oil Corp | Xylene isomerization |
US3856871A (en) * | 1973-09-13 | 1974-12-24 | Mobil Oil Corp | Xylene isomerization |
-
1978
- 1978-06-05 US US05/912,681 patent/US4163028A/en not_active Expired - Lifetime
- 1978-07-15 IN IN783/CAL/78A patent/IN149484B/en unknown
- 1978-07-17 CA CA307,504A patent/CA1096890A/fr not_active Expired
- 1978-07-20 EP EP78300170A patent/EP0000812B1/fr not_active Expired
- 1978-07-20 DE DE7878300170T patent/DE2861001D1/de not_active Expired
- 1978-07-20 JP JP53087828A patent/JPS6024772B2/ja not_active Expired
- 1978-07-21 IT IT26000/78A patent/IT1099583B/it active
- 1978-07-21 ES ES471957A patent/ES471957A1/es not_active Expired
- 1978-07-21 ZA ZA784167A patent/ZA784167B/xx unknown
Also Published As
Publication number | Publication date |
---|---|
JPS5424834A (en) | 1979-02-24 |
JPS6024772B2 (ja) | 1985-06-14 |
EP0000812A1 (fr) | 1979-02-21 |
DE2861001D1 (en) | 1981-11-26 |
CA1096890A (fr) | 1981-03-03 |
IT1099583B (it) | 1985-09-18 |
US4163028A (en) | 1979-07-31 |
IN149484B (fr) | 1981-12-26 |
IT7826000A0 (it) | 1978-07-21 |
ZA784167B (en) | 1980-02-27 |
ES471957A1 (es) | 1979-02-01 |
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