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+ ...

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

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

METHOD FOR PRODUCING HYDROISOMERIZATION CATALYST AND METHOD FOR PRODUCING LUBRICANT BASE OIL

A method for producing a hydroisomerization catalyst according to the present invention includes: a first step of preparing a catalyst to be treated, which contains a support having a one-dimensional porous structure including a 10-membered ring and at least one metal selected from the group consisting of: group 8 to 10 metals of the periodic table, Mo, and W supported on the hydroisomerization catalyst; and a second step of producing a hydroisomerization catalyst having a carbon content of 0.4 to 2.5% by mass by subjecting the catalyst to be treated to a coking treatment by means of a carbon-containing compound. 1. A method for producing a hydroisomerization catalyst comprising:a first step of preparing a catalyst to be treated, which contains a support having a one-dimensional porous structure including a 10-membered ring and at least one metal selected from the group consisting of: group 8 to 10 metals of the periodic table, Mo, and W supported on the hydroisomerization catalyst; anda second step of producing a hydroisomerization catalyst having a carbon content of 0.4 to 2.5% by mass by subjecting the catalyst to be treated to a coking treatment by means of a carbon-containing compound.2. The method for producing a hydroisomerization catalyst according to claim 1 ,wherein in the second step, a hydroisomerization catalyst is produced, for which a volume of micropores per unit mass of the catalyst is 0.02 to 0.11 cc/g and a volume of micropores per unit mass of the zeolite contained in the catalyst is 0.04 to 0.12 cc/g.3. The method for producing a hydroisomerization catalyst according to claim 1 ,wherein the zeolite is at least one selected from the group consisting of: a ZSM-22 zeolite; a ZSM-23 zeolite; an SSZ-32 zeolite; and a ZSM-48 zeolite.4. A hydroisomerization catalyst produced by the method for producing a hydroisomerization catalyst according to .5. A method for producing lubricant base oil claim 1 ,{'claim-ref': {'@idref': 'CLM-00004', 'claim 4'}, ' ...

METHODS AND APPARATUSES FOR ISOMERIZATION OF PARAFFINS

Embodiments of methods and apparatuses for isomerization of paraffins are provided. In one example, a method comprises the steps of separating an isomerization effluent into a product stream that comprises branched paraffins and a stabilizer overhead vapor stream that comprises HCl, H, and C-hydrocarbons. C-hydrocarbons are removed from at least a portion of the stabilizer overhead vapor stream to form a HCl and H-rich stream. An isomerization catalyst is activated using at least a portion of the HCl and H-rich stream to form a chloride-promoted isomerization catalyst. A paraffin feed stream is contacted with the chloride-promoted isomerization catalyst in the presence of hydrogen for isomerization of the paraffins. 1. A method for isomerization of paraffins , the method comprising the steps of:{'b': 42', '44', '46, 'sub': 2', '6, 'separating an isomerization effluent () into a product stream () that comprises branched and un-branched paraffins and a stabilizer overhead vapor stream () that comprises HCl, H, and C-hydrocarbons;'}{'sub': 6', '2, 'b': 46', '40, 'removing C-hydrocarbons from at least a portion of the stabilizer overhead vapor stream () to form a HCl and H-rich stream ();'}{'sub': '2', 'b': '40', 'activating an isomerization catalyst using at least a portion of the HCl and H-rich stream () to form a chloride-promoted isomerization catalyst; and'}{'b': '22', 'contacting a paraffin feed stream () with the chloride-promoted isomerization catalyst in the presence of hydrogen for isomerization of the paraffins.'}2465462. The method of claim 1 , wherein the step of removing comprises separating the stabilizer overhead vapor stream () at first separation conditions effective to form a liquid stream () that comprises Chydrocarbon and a net gas stream () that comprises HCl claim 1 , H claim 1 , and C-hydrocarbons.346. The method of claim 2 , wherein the step of removing comprises separating the stabilizer overhead vapor stream () at the first separation ...

Method and Catalyst System for Improving Benzene Purity in a Xylenes Isomerization Process

A process and catalyst system is disclosed for producing para-xylene from a Chydrocarbon mixture comprising ethylbenzene and at least one xylene isomer other than para-xylene. The process modifies the conventional process by operating with a higher weight hourly space velocity, lower pressure and lower hydrogen partial pressure, which allows production of on-specification benzene product without penalty with respect to ethylbenzene conversion, para-xylene approach to equilibrium or xylene losses. The catalyst system comprises a first catalyst bed comprising a first zeolite having a constraint index from 1 to 12 and an average crystal size from 0.1 to 1 micron and a platinum hydrogenation component, and a second catalyst bed comprising a second zeolite having a constraint index ranging from 1 to 12 and an average crystal size of less than 0.1 micron and a rhenium hydrogenation component. 1. A catalyst system for producing para-xylene from a Chydrocarbon mixture comprising ethylbenzene and at least one xylene isomer other than para-xylene , the catalyst system comprising a first catalyst bed (1) and a second catalyst bed (2) , wherein:the first catalyst bed (1) comprises a first catalyst comprising a first zeolite and a hydrogenation component comprising platinum, wherein the first zeolite has a constraint index ranging from 1 to 12 and an average crystal size of at least 1 micron; andthe second catalyst bed (2) comprises a second catalyst comprising a second zeolite and a hydrogenation component comprising rhenium, wherein the second zeolite has a constraint to index ranging from 1 to 12 and an average crystal size of about 0.02-0.05 microns.2. The catalyst system of claim 1 , wherein the hydrogenation component of the first catalyst consists essentially of platinum.3. The catalyst system of claim 1 , wherein the hydrogenation component of the second catalyst consists essentially of rhenium.4. The catalyst system of claim 1 , wherein the first zeolite comprises ZSM-5 ...

METHODS AND APPARATUSES FOR PROCESSING BIO-DERIVED NORMAL NONANE

Methods for forming bio-derived fuel products, upgrading bio-derived feedstocks, and processing bio-derived normal nonane are provided. In an embodiment, a method for forming a bio-derived fuel product includes providing a bio-derived hydrocarbon stream comprising at least about 50 wt % normal nonane and having a research octane number of less than about 10. The method further includes isomerizing the bio-derived hydrocarbon stream over a non-zeolitic, non-sulfated and/or non-halogenated catalyst to form the bio-derived fuel product with a research octane number of greater than about 50. 1. A method for forming a bio-derived fuel product , the method comprising the steps of:providing a bio-derived hydrocarbon stream comprising at least about 50 wt % normal nonane and having a research octane number of less than about 10; andisomerizing the bio-derived hydrocarbon stream over a non-zeolitic, non-sulfated and/or non-halogenated catalyst to form the bio-derived fuel product with a research octane number of greater than about 50.2. The method of wherein providing the bio-derived hydrocarbon stream comprises providing the bio-derived hydrocarbon stream comprising at least about 90 wt % normal nonane and having a research octane number of less than about 5.3. The method of wherein providing the bio-derived hydrocarbon stream comprises providing the bio-derived hydrocarbon stream having a research octane number of less than about 0.4. The method of wherein isomerizing the bio-derived hydrocarbon stream comprises forming the bio-derived fuel product with a research octane number of greater than about 75.5. The method of wherein providing the bio-derived hydrocarbon stream comprises providing the bio-derived hydrocarbon stream having a research octane number of less than about 0.6. The method of wherein isomerizing the bio-derived hydrocarbon stream forms the bio-derived fuel product with a Ccontent of less than about 5 wt %.7. The method of wherein the bio-derived ...

ISOMERISATION CATALYST PREPARATION PROCESS

A process for preparing an alkylaromatics isomerisation catalyst comprising at least 0.01% wt of platinum on a carrier comprising of from 1 to 9 wt % of ZSM-12 and inorganic binder, which process comprises treating the carrier with an impregnation solution comprising a cationic platinum compound and having a pH of more than 9, and subsequently drying and calcining the impregnated carrier at a temperature of from 200 to 420° C.; and a process for the isomerisation of alkylaromatics with the help of catalyst thus obtained. 1. A process for preparing an alkylaromatics isomerisation catalyst , the process comprising at least 0.01% wt of platinum on a carrier comprising of from 1 to 9 wt % of ZSM-12 and inorganic binder , which process comprises treating the carrier with an impregnation solution comprising a cationic platinum compound and having a pH of more than 9 , and subsequently drying and calcining the impregnated carrier at a temperature of from 200 to 420° C.2. A process as claimed in in which the impregnated carrier is calcined at a temperature in the range of from 250 to 400 ° C.3. A process as claimed in in which the impregnation solution further comprises ammonium hydroxide.4. A process as claimed in in which the impregnation solution has a pH of at least 11.5. A process as claimed in in which the ZSM-12 zeolite has a silica to alumina molar ratio (SAR) in the range of from 60 to 200.6. A process as claimed in in which the catalyst comprises at least 50 wt % of an acidic inorganic binder.7. A process as claimed in in which the cationic platinum compound is a platinum hydroxide compound.8. A process for the isomerisation of alkylaromatics which process comprises contacting a hydrocarbon feed comprising alkylaromatics with a catalyst obtained in a process as claimed in . This invention relates to a zeolite-based catalyst for the isomerisation of alkylaromatics, more specifically ethylbenzene.Following fractionation or distillation of crude petroleum oil, a ...

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

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

DISPERSED NOBLE METAL-CONTAINING CATALYST FOR HYDROCARBON CONVERSION

A method for modification of pretreated acidic porous material via selective cation exchange using suitable solvent to obtain higher noble metal dispersion is described herein. The solvent system required for cation exchange should have its dielectric constant in the range of 25-45, wherein this solvent property is found to impart significant effect on cation loading and distribution, which in turn defines the stability, dispersion of the noble metals. The catalyst so obtained has higher noble metal dispersion and when used for hydroisomerization reaction, leads to higher selectivity even at significantly high conversion values. 1. A process for preparing a dispersed noble metal-containing catalyst , the process comprising;(a) contacting a pretreated acidic porous material with at least one metal ion complexed with a ligand in a solvent having dielectric constant in a range of 25-45 to obtain a metal ion exchanged acidic porous material;(b) calcining the metal ion exchanged acidic porous material at a temperature of 300-600° C. to obtain a calcined mixture;(c) incorporating the calcined mixture with a noble metal to obtain a noble metal loaded acidic porous material;(d) drying the noble metal loaded acidic porous material to obtain a dried material;(e) extruding 50% w/w to 95% w/w of the dried material with 5% w/w to 50% w/w of a binder material to obtain a extruded catalyst; and(f) calcining the extruded catalyst at 250-400° C. under constant air flow to obtain a dispersed noble metal-containing catalyst having dispersion of over 90%.2. The process as claimed in claim 1 , wherein the acidic porous material is selected from the group consisting of zeolite claim 1 , molecular sieve claim 1 , amorphous silica-alumina claim 1 , solid acids and mixtures thereof claim 1 , preferably selected from the group consisting of ZSM-5 claim 1 , ZSM-22 claim 1 , ZSM-23 claim 1 , ZSM-35 claim 1 , and ZSM-48.3. The process as claimed in claim 1 , wherein the acidic porous material ...

METHODS AND APPARATUSES FOR ISOMERIZING HYDROCARBONS

Methods and apparatuses are provided for isomerizing a hydrocarbon stream. The method includes isomerizing a hydrocarbon stream in a reactor to produce an intermediate isomerized stream. The intermediate isomerized stream is fractionated to produce an off gas stream and a heavy isomerized stream, where the off gas stream includes an off gas recycle stream. The off gas recycle stream is dried in an off gas dryer to produce a hydrogen recycle stream, where the off gas drier includes an off gas dryer membrane separating the off gas recycle stream from an off gas purge stream. The off dryer membrane includes a perfluorosulfonated ionomer. The hydrogen recycle stream is then fed into the reactor. 1. A method of isomerizing hydrocarbons , the method comprising the steps of:isomerizing a hydrocarbon stream in a reactor to produce an intermediate isomerized stream;fractionating the intermediate isomerized stream to produce an off gas stream and a heavy isomerized stream, wherein the off gas stream comprises an off gas recycle stream;drying the off gas recycle stream in an off gas dryer to produce a hydrogen recycle stream, wherein the off gas dryer comprises an off gas dryer membrane separating the off gas recycle stream from an off gas purge stream, and wherein the off gas dryer membrane comprises a perfluorosulfonated ionomer; andfeeding the hydrogen recycle stream into the reactor.3. The method of wherein drying the off gas recycle stream further comprises drying the off gas recycle stream in the off gas dryer comprising the off gas dryer membrane claim 1 , wherein the off gas dryer membrane comprises a copolymer of tetrafluoroethylene and perfluoro-3 claim 1 ,6-dioxa-4-methyl-7-octene-sulfonic acid.4. The method of wherein drying the off gas recycle stream further comprises drying the off gas recycle stream in the off gas dryer comprising the off gas dryer membrane claim 3 , wherein the off gas dryer membrane comprises the copolymer of tetrafluoroethylene and perfluoro- ...

INTEGRATED PERCHLOROETHYLENE DECOMPOSITION REACTOR DESIGN FOR C4 AND C5-6 ISOMERIZATION UNITS

Processes incorporating a common organic chloride decomposition reactor and chloride treater to be used by both the Cand Cisomerization reaction zones are described. A portion of the Cisomerization reaction zone off gas is routed to the CHCl absorber, which provides about 85% of the HCl requirement for the Cisomerization reaction zone. A small amount of the Cisomerization reaction zone off gas is mixed with the Cisomerization reaction zone off gas portion going to the CHCl absorber. 1. An integrated process for Cisomerization and Cisomerization comprising:{'sub': 5-6', '5-6', '5-6', '5-6, 'passing a Cfeed stream comprising normal pentane and normal hexane to a CHCl absorber forming a Cabsorber bottoms stream comprising normal pentane, normal hexane and HCL, and a Cabsorber overhead stream comprising a trace amount of HCl;'}passing a first hydrogen rich gas stream and a chloride feed stream containing an organic chloride compound to an organic chloride decomposition reactor containing a chloride decomposition catalyst to decompose the organic chloride compound to form a chloride effluent stream comprising hydrogen, hydrocarbon, and HCl;{'sub': 5-6', '5-6', '5-6', '5-6', '5-6, 'passing the Cabsorber bottoms stream and the chloride effluent stream to a Cisomerization reaction zone under Cisomerization conditions in the presence of a Cisomerization catalyst to convert a portion of the normal pentane and normal hexane to iso-pentane and iso-hexane forming a Cisomerization effluent comprising normal pentane, normal hexane, iso-pentane, iso-hexane, and gases;'}{'sub': 5-6', '5-6', '5-6', '5-6, 'separating the Cisomerization effluent in a Cstabilizer column into at least a Cproduct stream comprising the normal pentane, normal hexane, iso-pentane, and iso-hexane, and a Coff gas stream;'}{'sub': 4', '4', '4', '4, 'passing a Cfeed stream comprising normal butane to a CHCl absorber forming a Cabsorber bottoms stream comprising normal butane and HCL, and a Cabsorber overhead ...

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

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

CONVERSION OF LIPIDS

A process is described for producing a hydrocarbon product. In examples, the process comprising contacting a feedstock with a catalyst composition in the presence of hydrogen, the feedstock including a lipid, and the catalyst composition being active for conversion of the lipid to the hydrocarbon product in a single step. The catalyst composition comprises an M1-8 Sup] catalyst, where M1 is an active metal and [Sup] comprises an acidic support. In examples described, the process is used in the production of diesel-range fuel and/or jet fuel from lipid having a high yield of C-Cbranched alkanes with high cetane value and low freeing point. In examples, the hydrocarbon product includes greater than 70% measured by weight of C-Calkanes based on the weight of the lipid, and the content of branched alkanes of the C-Calkanes is greater than 60% measured by weight of branched C-Calkanes based on the weight of the C-Calkanes. 142-. (canceled)43. A process for producing a hydrocarbon product , the process comprising contacting a feedstock with a catalyst composition in the presence of hydrogen , the feedstock including a lipid , and the catalyst composition being active for conversion of the lipid to the hydrocarbon product in a single step , the catalyst composition comprising an M1-[Sup] catalyst , where M1 is an active metal and [Sup] comprises an acidic support , wherein the hydrocarbon product includes greater than 70% measured by weight of C-Calkanes based on the weight of the lipid , and the content of branched alkanes of the C-Calkanes is greater than 60% measured by weight of branched C-Calkanes based on the weight of the C-Calkanes.44. A process according to claim 43 , wherein the catalyst composition effects hydrogenation claim 43 , deoxygenation and hydroisomerization of the lipid.45. A process according to claim 43 , wherein the weight ratio of Calkanes to Calkanes in the hydrocarbon product is greater than one claim 43 , where Calkanes comprise an odd number of ...

Isomerization process using feedstock containing dissolved hydrogen

A process and system is provided including hydroisomerization reaction zone for production of high octane gasoline blending components that provide high selectivity for producing high octane isomers of light paraffins. A light paraffin feed is enriched by incorporation of dissolved hydrogen, thereby permitting a reaction phase that is liquid or substantially liquid to produce high octane gasoline blending components. Accordingly, a substantially two phase isomerization reactor system is provided, with a hydrogen-enriched liquid feedstock phase and a solid phase catalyst.

ISOMERIZATION PROCESS USING FEEDSTOCK CONTAINING DISSOLVED HYDROGEN

A process and system is provided including hydroisomerization reaction zone for production of high octane gasoline blending components that provide high selectivity for producing high octane isomers of light paraffins. A light paraffin feed is enriched by incorporation of dissolved hydrogen, thereby permitting a reaction phase that is liquid or substantially liquid to produce high octane gasoline blending components. Accordingly, a substantially two phase isomerization reactor system is provided, with a hydrogen-enriched liquid feedstock phase and a solid phase catalyst. 1. A process for isomerization of a gasoline pool feedstock comprising:mixing the feedstock and hydrogen gas to produce a mixture of hydrogen-enriched feedstock reactants;contacting the hydrogen-enriched feedstock reactants with solid isomerization catalyst for hydroisomerization in a substantially two-phase liquid-solid isomerization reaction zone under conditions that minimize cracking reactions and that are effective to isomerize paraffins in the gasoline pool feedstock into branched paraffins; andrecovering an isomerate effluent stream.2. The process of claim 1 , wherein an excess of hydrogen gas is used claim 1 , wherein the mixture comprises hydrogen-enriched feedstock reactants and undissolved hydrogen gas claim 1 , the process further comprising separating the mixture of hydrogen-enriched feedstock and undissolved hydrogen into undissolved hydrogen and hydrogen-enriched feedstock reactants.3. The process of claim 1 , wherein the step of mixing is carried out in a mixing zone.4. The process of claim 3 , wherein the mixing zone comprises one or more gas-liquid distributor vessels.5. The process of claim 3 , wherein the mixing zone comprises in-line apparatus within one or more conduits upstream of the flashing zone.6. The process of claim 1 , wherein the feedstock has a RON of 60 or less.7. The process of claim 6 , wherein the isomerized product has a RON of at least 80.8. The process of claim ...

Processes for Producing Xylenes

A process for making p-xylene comprising co-feeding toluene with C8 aromatics into a vapor phase isomerization unit can improve xylenes loss and benzene selectivity in ethylbenzene conversion

XYLENE ISOMERIZATION

A process for producing xylenes, in particular para-xylene that is less energy intensive than conventional processes is provided. In an embodiment the process comprises contacting a feed mixture in an isomerization zone with a catalyst at isomerization conditions and producing an isomerized product comprising a higher proportion of p-xylene than in the feed mixture, wherein the catalyst comprises an acidic sulfonated catalytic membrane. Xylene isomerization can also be coupled with a p-xylene extraction process, where the raffinate (p-xylene deprived stream) from the extraction process is fed to an isomerization reactor to produce p-xylene. In an embodiment, the process can comprise: a) providing a feed stream comprising a mixture of xylene isomers including p-xylene; b) extracting p-xylene from the feed stream using a separator to separate the feed stream into a p-xylene rich stream and a p-xylene deprived stream; and c) delivering the p-xylene deprived stream to an isomerization unit, the isomerization unit including an acidic sulfonated catalytic membrane, and using the isomerization unit to produce an isomerized product comprising a higher proportion of p-xylene than in the p-xylene deprived stream delivered to the isomerization unit. In any one or more aspects, the isomerization unit can be operated at a temperature in the range of less than 350°, for example about 20° C. to about 200° C. 1. A process for removing p-xylene from a feed stream , comprising the steps of:a) providing a feed stream comprising a mixture of xylene isomers including p-xylene;b) extracting p-xylene from the feed stream using an extractor to separate the feed stream into a p-xylene rich stream and a p-xylene deprived stream;c) delivering the p-xylene deprived stream to an isomerization unit, the isomerization unit including an acidic sulfonated catalytic membrane, and using the isomerization unit to produce an isomerized product comprising a higher proportion of p-xylene than in the p- ...

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.

Composição catalisadora ativada e processo para preparar a mesma

Activation of platinum group metal catalysts

Preparation of silica-alumina composites for use in the hydrocracking of hydrocarbons

Intercalated clay compositions

This invention relates to clay compositions intercalated with inorganic oxide particles and the process from preparing them.

PROCESS FOR THE PREPARATION OF CLAYED ARGILES, CLAYS PREPARED BY THIS METHOD AND APPLICATIONS OF SAID CLAYS

L'INVENTION CONCERNE UN PROCEDE DE PREPARATION D'ARGILES PONTEES. SELON L'INVENTION, ON EFFECTUE LA DIALYSE D'UN MELANGE D'UNE SOLUTION AQUEUSE D'AU MOINS UN HYDROXYDE D'UN METAL ET D'UNE SUSPENSION AQUEUSE D'ARGILE. CES ARGILES PEUVENT SERVIR DE CATALYSEURS OU DE SUPPORTS CATALYSEURS POUR LA CONVERSION D'HYDROCARBURES PARAFFINIQUES OU OLEFINIQUES. THE INVENTION RELATES TO A PROCESS FOR PREPARING PONTED CLAYS. ACCORDING TO THE INVENTION, DIALYSIS OF A MIXTURE OF AN AQUEOUS SOLUTION OF AT LEAST ONE HYDROXIDE OF A METAL AND AN AQUEOUS CLAY SUSPENSION. THESE CLAYS CAN BE USED AS CATALYSTS OR SUPPORTS FOR THE CONVERSION OF PARAFFINIC OR OLEFINIC HYDROCARBONS.

Process for the preparation of catalytically active cross-linked metal silicates

Highly active and selective hydroisomerization catalysts are prepared by heating to 300 DEG -450 DEG C. at subatmospheric pressure, a mixture of nickel synthetic mica montmorillonite (Ni-SMM) with a hydroxy aluminum polymeric solution. The resulting pillared Ni-SMM catalyst, preferably Pd-loaded, is especially useful in hydroisomerizing C4-C7 paraffins.

Method of preparing bridged clays

L'invention concerne un procédé de préparation d'argiles pontées. Selon l'invention, on effectue la dialyse d'un mélange d'une solution aqueuse d'au moins un hydroxyde d'un métal et d'une suspension aqueuse d'argile. Ces argiles peuvent servir de catalyseurs ou de supports de catalyseurs pour la conversion d'au moins un hydroxyde d'un métal et d'une suspension aqueuse d'argile. Ces argiles peuvent servir de catalyseurs ou de supports de catalyseurs pour la conversion d'hydrocarbures paraffiniques ou oléofiniques. The invention relates to a process for the preparation of bridged clays. According to the invention, dialysis is carried out on a mixture of an aqueous solution of at least one hydroxide of a metal and an aqueous suspension of clay. These clays can serve as catalysts or catalyst supports for the conversion of at least one hydroxide of a metal and an aqueous suspension of clay. These clays can serve as catalysts or catalyst supports for the conversion of paraffinic or oleofinic hydrocarbons.

Process for the preparation of bridged clays, clays prepared by said process, and uses for said clays

In a process for the preparation of bridged clays, a mixture of an aqueous solution of at least one metal hydroxide and aqueous clay suspension is subjected to dialysis. Said clays are suited for use as catalysts or as supports for catalysts for the conversion of paraffinic or olefinic hydrocarbons.

A process for isomerisation or alkylation a hydrocarbon

Werkwijze voor het bereiden van mordeniet.

Hydrocarbon isomerization with increased temperature and lowered hydrogen/hydrocarbon ratio

In a process for isomerizing light hydrocarbons with a catalyst system comprising a halogenated alumina or platinum alumina when hydrogen is utilized to sustain the catalyst activity, the ratio of hydrogen to hydrocarbon in the feed is decreased and the temperature increased after a substantial period of operation. This results in an improved conversion and selectivity which allows for increasing the total catalyst life.

METHOD FOR THE PREPARATION OF A CATALYST COMPOSITION FOR THE ISOMERIZATION OF HYDROCARBONS.

Se prepara una composición que contiene cloro y metales del Grupo VIII (efectiva como un catalizador de isomerización de alcano/cicloalcano),mediante un método que comprende mezclar tricloruro de aluminio con un material sólido que contiene al menos un metal del Grupo VIII (Pt y/o Pd y/o Ni) yalúmina, calentar la mezcla obtenida en un gas inerte a aproximadamente 450-750°C, y luego tratar la mezcla con un gas que contiene cloruro dehidrógeno a aproximadamente 300-700°C. A composition containing chlorine and Group VIII metals (effective as an alkane / cycloalkane isomerization catalyst) is prepared by a method comprising mixing aluminum trichloride with a solid material containing at least one Group VIII metal (Pt and / or Pd and / or Ni) yalumina, heat the obtained mixture in an inert gas to approximately 450-750 ° C, and then treat the mixture with a gas containing hydrogen chloride at approximately 300-700 ° C.

Liquid-phase olefin alkylation process

FIELD: petrochemical synthesis. SUBSTANCE: alkylation of olefin having at least 3 carbon atoms with isoalkane having at least 4 carbon atoms in presence of (i) Lewis acid-based complex catalyst is distinguished by that complex catalyst is product of reaction of at least Lewis acid with general formula R(m-2-z)MX(2+z) wherein M is 3a, 5a, or 5b group metal, X halide, R is C 4 -C 12 -hydrocarbyl, m integer equal to highest oxidation degree of M, Z is equal to 1, 2 or m-2; (ii) hydrogen halide; and (iii) organic compound with up to 12 carbon atoms. EFFECT: simplified process. 15 cl, 4 dwg, 2 tbl, 13 ex УЗ Гс ПЫ ГЭ РОССИЙСКОЕ АГЕНТСТВО ПО ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ (19) (51) МПК ВИ “” 2438 471 Сл С 07С 2/58, В 01 4 31/22 12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ РОССИЙСКОЙ ФЕДЕРАЦИИ (21), (22) Заявка: 94039538/04, 13.12.1993 (30) Приоритет: 21.12.1992 1$ 07/993,601 19.07.1993 1$ 08093,463 19.07.1993 4$ 08094,520 (46) Дата публикации: 21.09.1999 (56) Ссылки: 4$ 3873635 А, 25.03.75. ЗЦ 400075 А, 03.10.73. $Ц 1172916 А, 08.07.93. (86) Заявка РСТ: Ц$ 93/12087 (13.12.93) (87) Публикация РСТ: \/О 94/14734 (07.07.94) (98) Адрес для переписки: 103735, Москва, ул.Ильинка 5/2, Союзпатент, Патентному поверенному Лебедевой Н.Г. (71) Заявитель: Керр-МакДжи Корпорейшн (ЦЗ) (72) Изобретатель: Ларри Г.Шерман (13), Уилльям А.Юйлл (ЦЗ) (73) Патентообладатель: Керр-МакДжи Корпорейшн (ЦЗ) (54) СПОСОБ ЖИДКОФАЗНОГО АЛКИЛИРОВАНИЯ ОЛЕФИНА (57) Реферат: Описывается способ алкилирования олефина, имеющего по меньшей мере 3 атома углерода, изоалканом, имеющим по меньшей мере 4 атома углерода, в присутствии углеводородного комплексного катализатора на основе кислоты Льюиса, отличающийся тем, что — используют комплексный катализатор, включающий продукт реакции по меньшей мере кислоты Льюиса К(т-2-2)МХ(2+2), где М - металл групп За, 5а или 5в Периодической системы элементов; Х - галогенид; К - гидрокарбильный радикал, имеющий от 1 до 12 атомов углерода; т - целое число, равное наибольшей степени окисления М ...

Process for obtaining catalysts for the conversion of hydrocarbons

Способ изомеризации С5-С8 парафинового углеводородного сырья

А 2001130402 ко РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) “А (11) . М \ & (51) МК’ С 07С 5/22 7 222 2 02? А 7 р РР #_# 7 722 2, 7 77 й 2 \Х ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ, ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ (12 ИЗВЕЩЕНИЯ К ЗАЯВКЕ НА ИЗОБРЕТЕНИЕ (21), (22) Заявка: 2001130402/04, 13.11.2001 (71) Заявитель(и): ХАЛЬДОР ТОПСЕЭ А/С (ОК) (43) Дата публикации заявки: 20.08.2003 (72) Автор(ы): Адрес для переписки: Васина Тамара Владимировна (КИ), 103064, Москва, ул. Казакова, 16, НИИР Кустов Леонид Модестович (КЦ), Канцелярия "Патентные поверенные Квашнин, Ксенофонтов Владислав Анатольевич (ВЦ), Сапельников и Партнеры", В.П. Квашнину Зубарев Юрий Егорович (ВИ), ХОУЖВИЧКА Индржих (ОК), ЗАВИЛЛА Джон (ОК) (74) Патентный поверенный: Квашнин Валерий Павлович (54) Способ изомеризации С5-С8 парафинового углеводородного сырья ГАЭА - Признание заявок на изобретение отозванными в связи с непредставлением в установленный срок дополнительных материалов или запрашиваемых документов Дата отзыва заявки: 23.06.2006 Извещение опубликовано: 10.08.2006 БИ: 22/2006 Страница: 1 па СООО ОС А"

증류 범위 탄화수소 공급원료의 파라핀 이성화법

내용없음.

Hydrocarbon conversion catalyst comprising a halogen component combined with a support containing alumina and finely divided crystalline aluminosilicate particles

Hydrocarbon conversion process with a catalyst activated with an organic chloride and oxygen

A HYDROCARBON CONVERSION PROCESS IN WHICH A HYDROCARBON IS CONTACTED AT CONVERSION CONDITIONS WITH A CATALYST COMPRISING ALUMINA AND CHLORINE WHEREIN AT LEAST A PORTION OF SAID CHLORINE IS INTRODUCED INTO SAID CATALYST BY CONTACTING SAID ALUMINA AT ELEVATED TEMPERATURE WITH A SELECTED ORGANIC CHLORINE IN THE PRESENCE OF AN AMOUNT OF OXYGEN SUFFICIENT TO CONVERT ALL OF THE CARBON IN SAID ORGANIC CHLORIDE TO CARBON DIOXIDE. IN ADDITION, THE CATALYST MAY CONTAIN A METAL SELECTED FROM THE GROUP CONSISTING OF RUTHENIUM, RHODIUM, PALLADIUM AND PLATINUM. THE CATALYST SO PREPARED IS USEFUL IN HYDROCARBON CONVERSION PROCESSES AS ISOMERIZATION, HYDROCRACKING, ALKYLATION, HYDROGENATION, AND POLYMERIZATION.

Catalyst for hydrocarbon conversion

A METHOD FOR PREPARING A HYDROCARBON CONVERSION CATALYST COMPOSED OF ALUMINA AND CHLORINE OR BROMINE BY CONTACTING ALUMINA WITH AN ACTIVATOR SYSTEM COMPRISING CHLORINE OR BROMINE AND AN INORGANIC SULFUR COMPOUND SELECTED FROM THE GROUP HYDROGEN SULFIDE AND COMPOUNDS CORROESPONDING TO THE FORMULA SMX2. THE CATAYST MAY ADDITIONALLY INCLUDE A METAL SUCH AS APLATINUM, PALLADIUM, RUTHENIUM OR RHODIUM. THE CATALYSTS SO PREPARED ARE USEFUL IN SUCH HYDROCARBON CONVERSION PROCESSES AS ISOMERIZATION, CRACKING, HYDROCRACKING, REFORMING, ALKYLATION, DEHYDROGENATION, DISPROPORTIONATION AND POLYMERIZATION.

Fluorided metal-alumina catalysts

A METHOD FOR PREPARING A HYDROCARBON CONVERSION CATALYST BY PROVIDING A COMPOSITE COMPOSED OF ALUMINA HAVING ASSOCIATED THEREWITH A GROUP VI-B, VII-B OR VIII METAL OR COMPOUND AND CONTACTING THE COMPOSITE WITH AN ACTIVATOR SYSTEM COMPRISING HYDROGEN AND SULFURYL FLUORIDE OR THIONYL FLUORIDE. THE CATALYSTS SO PREPARED ARE USEFUL IN SUCH HYDROCARBON CONVERSION PROCESSES AS ISOMERIZATION, HYDROCRACKING, REFORMING, ALKYLATION, DISPROPORTIONATION, POLYMERIZATION AND HYDROGENATION.

Fluorided composite alumina catalysts

A method for preparing a hydrocarbon conversion catalyst by providing a composite composed of alumina having associated therewith a Group VIB or VIII metal or compound and contacting the composite with an activator system comprising hydrogen and an organic fluoride compound having from two to 16 carbon atoms. The catalysts so prepared are useful in such hydrocarbon conversion processes as isomerization, hydrocracking, reforming, alkylation, disproportionation, polymerization and hydrogenation.

Supported superacidic catalysts based on C10 to C18 perfluorinated alkanesulfonic acids

The present invention relates to supported superacidic catalysts comprising C 4 -C 18 , preferentially C 6 to C 12 , perfluorinated alkanesulfonic acid absorbed on suitable supports, such as fluorinated alumina, alumina silica and other chalcides having bonded thereto subsequently a Lewis acid compound selected from the higher valency fluorides of the elements of Groups IIA, IIIA, IVB, VA or VIB of the Periodic Table. The invention includes a process for catalytic transformation of hydrocarbons.

Boron, aluminum and gallium perfluoro alkanesulfonate and resinsulfonate catalysts

Boron, aluminum and gallium C 1 -C 18 perfluoroalkanesulfonates (CF 3 (CF 2 ) n SO 3 ) 3 M (M=B, A1, Ga; n=0-17) as well as perfluororesin sulfonates such as Nafionates are new, highly effective Friedel-Crafts catalysts. In contrast to volatile aluminum and boron trihalides, the Group III-B perfluoroalkanesulfonates are generally of low or no volatility and, except for boron triflate and some of its homologs, only sparingly soluble incommon organic solvents. This allows their use as solid or supported Friedel-Crafts catalysts of wide utility and scope in continuous heterogenous catalytic processes. At the same time, boron triflate and related lower perfluoroalkanesulfonates are particularly efficient soluble catalysts in solution reactions.

Boron aluminum and gallium perfluoro alkanesulfonate and resinsulfonate catalysts

Boron, aluminum and gallium C 1 -C 18 perfluoroalkane-sulfonates (CF 3 (CF 2 ) n SO 3 ) 3 M (M=B, A1, Ga; n=0-17) as well as perfluororesin sulfonates such as Nafionates are new, highly effective Friedel-Crafts catalysts. In contrast to volatile aluminum and boron trihalides, the Group III-B perfluoroalkanesulfonates are generally of low or no volatility and, except for boron triflate and some of its homologs, only sparingly soluble incommon organic solvents. This allows their use as solid or supported Friedel-Crafts catalysts of wide utility and scope in continuous heterogenous catalytic processes. At the same time, boron triflate and related lower perfluoroalkanesulfonates are particularly efficient soluble catalysts in solution reactions.

Catalyst for hydrocarbon conversion

A METHOD FOR PREPARING A HYDROCARBON CONVERSION CATALYST BY PROVIDING A COMPOSITE COMPOSED OF ALUMINA HAVING ASSOCIATED THEREWITH A GROUP VI-B, VII-B OR VIII METAL OR COMPOUND AND CONTACTING THE COMPOSITE WITH AND ACTIVATOR SYSTEM COMPRISING CARBON MONOXIDE AND SULFUR HEXAFLUORIDE. THE CATALYSTS SO PREPARED ARE USEFUL IN SUCH HYDROCARBON CONVERSION PROCESSES AS ISOMERIATION, HYDROCRACKING, REFORMING, ALKYLATION, DISPROPORTIONATION, POLYMERIZATION AND HYDROGENERATION.

Catalyst for hydrocarbon conversion

A METHOD FOR PREPARING A HYDROCARBON CONVERSION CATALYST BY PROVIDING A COMPOSITE COMPOSED OF ALUMINA HAVING ASSOCIATED THEREWITH A GROUP VI-B, VII-B OR VIII METAL OR COMPOUND AND CONTACTING THE COMPOSITE WITH AN ACTIVATOR SYSTEM COMPRISING CARBON MONOXIDE AND SULFURYL FLUORIDE OR THIONYL FLUORIDE. THE CATALYSTS SO PREPARED ARE USEFUL IN SUCH HYDROCARBON CONVERSION PROCESSES AS ISOMERIZATION, HYDROCRACKING, REFORMING, ALKYLATION DISPROPORTIONATION, POLYMERIZATION AND HYDROGENERATION.

Fluorided composite alumina catalysts

A METHOD FOR PREPARING A HYDROCARBON CONVERSION CATALYST BY PROVIDING A COMPOSITE COMPOUND OF ALUMINA HAVING ASSOCIATED THEREWITH A GROUP VI-B, VII-B OR VIII METAL OR COMPOUND AND CONTACTING THE COMPOSITE WITH AN ACTIVATOR SYSTEM COMPRISING HYDROGEN AND SULFUR HEXAFLUORIDE. THE CATALYSTS SO PREPARED ARE USEFUL IN SUCH HYDROCARBON CONVERSION PROCESSES AS ISOMERIZATION, HYDROCRACKING, REFORMING, ALKYLATION, DISPROPORTIONATION, POLYMERIZATION AND HYDROGENTATION.

SUPERACCED CATALYST FOR THE HYDROISOMERIZATION OF N-PARFINES, THE USE OF SUCH CATALYZER AND HYDROISOMERIZATION PROCEDURE OF N-PARFINES MAKING USE OF THE SAME.

Se describe un catalizador superacido, basado en sulfato de circonio, optativamente que contiene un metal noble, con una porosidad del rango de 0,1 a 0,30cm2/g, consistente de por lo menos un 70% de poros con un diámetro de rango desde 1 a 4 nmprepa rado como sigue (a) hidrolisis en un medio alcalino de uncompuesto hidrolizable de circonio en presencia de un tetra-alquilamonio hidroxido (TAA), ácido sulfurico acetilacetona; (b) secar el producto resultante ycalcinarlo a una temperaturaentre 25 0s a 650sC; (c) posible tratamiento del producto resultante de la etapa (b) con una solucion acuosa de un compuesto de unmetal noble, secado y calcinado. Estos materiales son activos en las reacciones catalizadoras ácidas y en lahidroisomerizacion d e n-parafinas. Elprocedimiento de hidroisomerizacion empleando dicho catalizador incluye poner en contacto una n-parafina o su mezcla, en condiciones de hidroisomerizacion ,con un catalizador superácido que contiene un metalnoble, del tipo arriba ci tado. A superacid catalyst based on zirconium sulfate is described, optionally containing a noble metal, with a porosity of the range of 0.1 to 0.30cm2 / g, consisting of at least 70% of pores with a range diameter from 1 to 4 times as follows (a) hydrolysis in an alkaline medium of a zirconium hydrolyzable compound in the presence of a tetra-alkylammonium hydroxide (TAA), acetylacetone sulfuric acid; (b) drying the resulting product and calcining it at a temperature between 25 0s at 650sC; (c) possible treatment of the product resulting from step (b) with an aqueous solution of a noble metal compound, dried and calcined. These materials are active in acid catalyst reactions and in the dehydroisomerization of n-paraffins. The hydroisomerization process using said catalyst includes contacting an n-paraffin or its mixture, under hydroisomerization conditions, with a super-acid catalyst containing a metalnoble, of the above-mentioned type.

Zeolite SSZ-25

A crystalline zeolite SSZ-25 is prepared using an adamantane quaternary ammonium ion as a template.

Preparation method of bio-based isomeric tridecanol

本发明涉及一种生物基异构十三醇的制备方法，该方法以天然月桂醇为原料，在酸催化下脱水制备十二碳烯，十二碳烯经异构、氢甲酰化和加氢制备异构十三醇产品。该方法使用天然脂肪醇为原料制备异构十三醇，减少了石化原料的消耗，为异构十三醇的生产提供了全新的可再生生物来源。

The method of processing hydrocarbon raw materials

Method of hydrocarbon isomerisation

FIELD: chemistry. ^ SUBSTANCE: invention relates to method of polymerisation of raw material flow containing C5-C6 hydrocarbons, which includes: loading of hydrogen and raw material, containing at least, normal C5-C6 hydrocarbons into isomerisation zone and contacting of hydrogen and raw material with isomerisation catalyst in conditions that favour increase of degree of hydrocarbons branching in raw material flow and ensuring formation of outgoing flow from isomerisation zone, which contains, at least, butane, normal pentane, normal hexane, methylbutane, dimethylbutane, methylpentanes and hydrocarbons which have seven or more carbon atoms, isomerisation conditions including temperature from 40 to 235C and pressure 70 kPa abs. to 7000 kPa abs; passing outgoing flow from isomerisation zone through deisohexanizer zone in order to divide it into four flows, flow outgoing from upper part of deisohexaniser zone, containing, at least, butane, first side flow from deisohexaniser zone, containing, at least, methylbutane and dimethylbutanes, second side flow from deisohexaniser zone, containing, at least, methylpentanes and normal hexane, and lower flow from deisohexaniser zone, containing, at least, hydrocarbons, consisting of seven and more carbon atoms; and supply of first side flow from deisohexaniser zone into zone of isomerizate stripping in order to separate upper flow from isomerisate desorber which contains, at least, butane, from product flow from zone of isomerisate stripping, containing methylbutane and dimethylbutanes. ^ EFFECT: application of claimed method allows to reduce capital outlays and reduce cost of energy supply due to excluding of column-stabiliser. ^ 9 cl, 4 dwg (19) РОССИЙСКАЯ ФЕДЕРАЦИЯ RU (11) 2 364 582 (13) C2 (51) МПК C07C C07C 5/22 9/16 (2006.01) (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ, ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (21), (22) Заявка: 2007137662/04, 02.03.2006 (24) Дата начала отсчета ...

Nitrogen resistant paraffin hydroisomerization catalysts

The present invention includes a process and catalyst composition for paraffinic isomerization of a hydrocarbon feedstock which has a paraffin content having no more than 20 carbon atoms per molecule. The feedstock is contacted with a crystalline aluminosilicate zeolite catalyst having pore openings defined by: (1) a ratio of sorption of n-hexane to o-xylene, on a volume percent basis, of greater than about 3, which sorption is determined at a P/P o of 0.1 and at a temperature of 50° C. for n-hexane and 80° C. for o-xylene and (2) by the ability of selectively cracking 3-methylpentane (3MP) in preference to the doubly branched 2,3-dimethylbutane (DMB) at 1000° F. and 1 atmosphere pressure from a 1/1/1 weight ratio mixture of n-hexane/3-methyl-pentane/2,3-dimethylbutane, with the ratio of rate constants k 3MP/ k DMB determined at a temperature of 1000° F. being in excess of about 2, e.g., ZSM-22, ZSM-23, AXM-35 and mixtures thereof, in combination with a Group VIII metal, and having a zeolite SiO 2 /Al 2 O 3 ratio of at least about 20:1 at a temperature and pressure suitable for isomerization.

Isomerization process

Long chain (C 7+ ) paraffins are isomerized over a large pore, highly siliceous zeolite catalyst such as zeolite Y or ZSM-20 having a structural silica:alumina ratio of at least 10:1. The use of the highly siliceous zeolite inhibits the degree of cracking and also permits weaker hydrogenation components such as palladium to be used in the catalyst.

Isomerization process

Long chain (C 7+ ) paraffins are isomerized over a large pore, highly siliceous zeolite catalyst such as zeolite Y or ZSM-20 having a structural silica:alumina ratio of at least 10:1. The use of the highly siliceous zeolite inhibits the degree of cracking and also permits weaker hydrogenation components such as palladium to be used in the catalyst.

SOLID STRONG ACID CATALYST.

Process for the preparation of mordenite

A method of preparing mordenite by hydrothermal treatment of a silica-alumina cogel prepared by precipitation of alumina on a silica gel (as opposed to a coprecipitate) in which the cogel is heated in an alkali solution having excess alkali (calculated basis the alkali-metal oxide), the total amount of alkali being equal to AX/102+BY/1000, where A is the molecular weight of the alkali oxide, x is the weight of alumina in the cogel, in grams; y is the weight of water in the total solution, in grams; and b is the weight, in milligrams, of excess alkali (basis a molar alkali-alumina ratio of 1 per gram of water and is in a range between 7-30 milligrams per gram of water.

Method of producing catalyst for isomerizing c4-c7-normal paraffin hydrocarbons

A process for the preparation of a catalyst suitable for the isomerization of normal paraffins by mixing 1) an amorphous material consisting substantially of one or more oxides of metals of the groups II, III and IV, onto which one or more noble metals of group VIII have been deposited and 2) mordenite which has been treated with a solution prepared by incorporating potassium and/or sodium ions in an aqueous acid solution with a normality of at least 0.5 and at most 3.0, in an amount which, expressed in g/l, is at least ten times the normality of the aqueous acid solution, and subsequently with an aqueous solution of an ammonium compound, and subjecting the mixture obtained to shaping under high pressure.

METHOD FOR ISOMERIZING CARBON FRACTIONS C5 / C6 WITH RECIRCULATION OF CHLORINE-CONTAINING COMPOUNDS

РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2015 143 021 A (51) МПК C07C 5/27 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21)(22) Заявка: 2015143021, 08.10.2015 (71) Заявитель(и): АКСЕНС (FR) Приоритет(ы): (30) Конвенционный приоритет: 20.10.2014 FR 1460090 Адрес для переписки: 129090, Москва, ул. Б. Спасская, 25, стр. 3, ООО "Юридическая фирма Городисский и Партнеры" Стр.: 1 A 2 0 1 5 1 4 3 0 2 1 R U A (57) Формула изобретения 1. Способ изомеризации углеводородного сырья, содержащего углеводородные соединения С5 и/или С6, причем указанный способ включает использование контура рециркуляции по меньшей мере одного хлорсодержащего соединения, и причем согласно указанному способу: a) подают на установку изомеризации (1) по меньшей мере одну жидкую фракцию указанного углеводородного сырья и осуществляют изомеризацию в присутствии хлорсодержащего. катализатора; b) подают на стабилизационную установку (20), содержащую по меньшей мере одну стабилизационную колонну (2), поток, выходящий из установки изомеризации (1), и осуществляют в указанной стабилизационной установке (2) разделение на: - газовый поток, содержащий по меньшей мере одно хлорсодержащее соединение, - жидкий поток, имеющий концентрацию СА соединений С5+, и - жидкий поток, содержащий по меньшей мере один продукт изомеризации углеводородного сырья; c) реализуют в абсорбционной установке (7), содержащей по меньшей мере одну абсорбционную колонну (3): - первый контакт между газовым потоком, выходящим с этапа b), и промывочным раствором, причем указанный промывочный раствор выбран из жидкой фракции, комплементарной указанному углеводородному сырью, и/или из по меньшей мере части указанного жидкого потока, полученного на этапе b), содержащего по меньшей мере один продукт изомеризации углеводородного сырья; причем указанный промывочный раствор имеет концентрацию СВ соединений С5+ такую, что СА<СВ; - второй контакт между газовым потоком, полученным в результате указанного ...

Hydrocarbon isomerization method

Manufacture of catalyst for isomerizing normal paraffine

Isomerisation catalyst preparation process

1 내지 9 중량% 의 ZSM-12 및 무기 결합제를 포함하는 담체 상에 백금을 0.01 중량% 이상 포함하는 알킬방향족 이성질화 촉매의 제조 방법으로서, 상기 방법이 상기 담체를, 양이온성 백금 화합물을 포함하고 pH 가 9 초과인 함침 용액으로 처리한 후, 함침된 담체를 200 내지 420 ℃ 의 온도에서 건조 및 소성시키는 것을 포함하는 방법; 및 이와 같이 수득된 촉매의 도움에 의한 알킬방향족의 이성질화 방법.

Process method for producing m-xylene by mixing carbon octa-arene

本发明涉及一种用于混合碳八芳烃生产间二甲苯的工艺方法。本发明采用高效液相异构化催化反应和择形吸附分离工艺技术的结合匹配，实现以混合碳八芳烃原料生产高纯的间二甲苯产品。利用择形吸附剂分子筛孔道对各个二甲苯异构体分子间差异的高选择性分子识别，通过吸附分离获得高纯度的间二甲苯；利用高选择性/高活性的液相异构化催化反应催化剂进行二甲苯异构化反应，将对二甲苯/邻二甲苯分子转化为间二甲苯分子；将上述的异构化催化反应工艺和择形吸附分离工艺的结合匹配，从而形成了以混合碳八芳烃为原料高选性地生产高纯间二甲苯的工艺技术方法。本发明具有高活性与选择性、反应温度低、间二甲苯产品收率高的优点，而择形吸附工艺具有分离效率高、所需设备简单、原料适用范围广、吸附剂用量少的特点。

Process for preparing catalyst composition for hydrocarbon isomerization

Ⅷ족 금속 및 클로라이드-함유 조성물(알칸/시클로알칸 이성화 촉매로서 효과적임)은 삼염화 알루미늄을 적어도 하나의 Ⅷ족 금속(Pt 및/또는 Pd 및/또는 Ni) 및 알루미나를 함유하는 고체 물질과 혼합하고, 얻어진 혼합물을 불활성 가스내 약 450 내지 750℃에서 가열시킨 다음, 혼합물을 약 300 내지 700℃에서 염화수소-함유 가스로 처리함으로써 제조된다.

CATALYST AND METHOD OF ISOMERIZATION

1. Катализатор изомеризации алкилароматических соединений, который содержит: ! по меньшей мере 50 мас.% кислого неорганического связующего; ! по меньшей мере 0,01 мас.% металла VIII группы; и ! 1-9 мас.% цеолита ZSM-12; ! причем цеолит ZSM-12 имеет молярное отношение окиси Si к окиси Al (SAR) от 60 до 200. ! 2. Катализатор по п.1, который представляет собой экструдат. ! 3. Катализатор по п.1 или 2, в котором пористость неорганического связующего составляет по меньшей мере 0,6 см3/г. ! 4. Катализатор по п.1 или 2, котором объемная плотность составляет менее 0,3 г/см3. ! 5. Катализатор по п.1 или 2, котором значение SAR составляет от 70 до 150. ! 6. Катализатор по п.1 или 2, который содержит 1-7 мас.% цеолита. ! 7. Катализатор по п.1 или 2, в котором цеолит ZSM-12 имеет средний размер кристаллов от 30 до 70 нм. ! 8. Катализатор по п.1 или 2, в котором кристалличность цеолита ZSM-12 составляет более 94%. ! 9. Способ изомеризации алкилароматических соединений для получения реакционной смеси, который включает контактирование потока углеводородов содержащего алкилароматические соединения, с катализатором по любому из пп.1-8. ! 10. Способ по п.9, в котором углеводородная фракция содержит по меньшей мере 5 мас.% этилбензола. РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2011 103 935 (13) A (51) МПК B01J 29/74 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (71) Заявитель(и): ШЕЛЛ ИНТЕРНЭШНЛ РИСЕРЧ МААТСХАППИЙ Б.В. (NL) (21)(22) Заявка: 2011103935/04, 24.06.2009 Приоритет(ы): (30) Конвенционный приоритет: 04.07.2008 EP 08159696.7 R U (54) КАТАЛИЗАТОР И СПОСОБ ИЗОМЕРИЗАЦИИ (57) Формула изобретения 1. Катализатор изомеризации алкилароматических соединений, который содержит: по меньшей мере 50 мас.% кислого неорганического связующего; по меньшей мере 0,01 мас.% металла VIII группы; и 1-9 мас.% цеолита ZSM-12; причем цеолит ZSM-12 имеет молярное отношение окиси Si к окиси Al (SAR) от 60 до 200. 2. Катализатор по п.1, который представляет собой ...

C 8 Aromatic hydrocarbon separation and conversion process and system

本发明公开了一种C 8 芳烃分离转化工艺及系统，包括：C 8 芳烃原料进入二甲苯塔进行分馏，塔顶物流经换热送至吸附分离塔，得到的富对二甲苯抽出液经换热器进入抽出液分馏塔，贫对二甲苯抽余液进入抽余液塔，上部侧线物料经换热，经异构化反应加热炉加热后进行异构化反应，反应产物经换热后，进入加氢反应器脱除烯烃，进入异构化产物分馏塔，所述的异构化产物分馏塔为分壁塔形式；塔顶物料为C 7 以下轻烃和氢气，侧线物料与吸附分离进料混合，塔底出料为C 9 + 芳烃。针对现有技术的不足，本发明优化了换热网络，大幅降低了能耗，同时解决了白土失活较快、吸附能力有限导致吸附效率差、废白土需要经常更换且对环境造成污染等问题，提高了社会和经济效益。

PSA process with reaction for reversible reactions

A process is disclosed for the production of a high octane product from a feed mixture comprising C 5 -C 6 normal paraffins in which an equilibrium reaction to produce mono and dimethyl branched paraffins is achieved by conducting the reaction and the product separation in a pressure swing adsorption and reaction zone containing a uniformly distributed adsorbent for the selective adsorption of normal paraffins and a catalyst for the equilibrium conversion of normal paraffins to mono and dimethyl branched paraffins. More specifically, the process achieves the isomerization of the normal paraffins by the reaction of the normal paraffins in the presence of hydrogen with the simultaneous removal of the mono and dimethyl branched paraffin product at the same temperature and pressure. In one embodiment, the passing of the feed mixture to the bed is terminated and the bed is purged with one of the reactants which in turn further reacts to displace heavier paraffin and enhance the overall product octane. The advantage of the present invention over the conventional process is the higher octane of the product produced and that this higher octane can be achieved at lower severity since the product is removed from the reaction zone as soon as it is produced. The lower operating severity provides longer catalyst life, and reduces the amount of heavy paraffins lost to side reactions such as cracking.

PSA process with reaction for reversible reactions

A process is disclosed for the production of methanol from a synthesis gas stream comprising hydrogen and carbon dioxide in which an equilibrium reaction to methanol is achieved by conducting the reaction and the product separation in a pressure swing adsorption and reaction zone containing a uniformly distributed adsorbent for the selective adsorption of methanol and a catalyst for the equilibrium conversion of the synthesis gas to methanol. More specifically, the process achieves the production of methanol by the reaction of the hydrogen and the carbon oxide with the simultaneous adsorption of the product at the same temperature and pressure. The passing of the synthesis stream to the bed is terminated and the bed is purged and depressurized to desorb the methanol product. In one embodiment, the bed is cocurrently purged with at least a portion of an effluent stream prior to depressurizing the bed. In further embodiments, the pressure swing adsorption and reaction zone is employed in a methanol synthesis loop both with and without a secondary reforming step to provide a lean synthesis gas with a stoichiometric ratio of carbon to hydrogen. The use of the pressure swing adsorption and reaction zone results in a higher conversion of the synthesis gas to methanol and significantly reduces the capital and operation costs in the production of methanol by reducing compressor requirements.

Method for producing isobutene by combining hydroisomerization reaction distillation, distillation and skeletal isomerization

Catalyst for conversion of hydrocarbons

FIELD: oil processing, particular, production of catalysts for conversion of hydrocarbons. SUBSTANCE: catalyst for conversion of hydrocarbons has zeolite NU-87 whose content is on anhydrous base in molar ratio of oxides: 100XO 2 less or equal to 10 Y203: less or equal to 20 R2/nO, where R is one or more cations with valency n, at least, partially hydrogen: X is silicon and/or germanium; Y is one or more elements from the group including aluminum, iron, gallium, boron and titanium, and having in hydrogen form the X-ray diffraction pattern with lines presented in Table 2. Preferably catalyst contains in form of X silicon, and in form of Y aluminum. It is desirable to replace hydrogen partially or fully with metal taken from the group including platinum, gallium and nickel. EFFECT: higher efficiency. 3 cl, 7 dwg, 10 tbl 7012190сС ПЧ Го РОССИЙСКОЕ АГЕНТСТВО ПО ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ (19) ВИ” 2 067 024 ' (51) МПК 13) СЛ 01 34 29/70, 101:20, 101:50, 103:24, 103:30, 103:36, 103:60) В 01 4 29/70, С 01 В 39/02/(В 12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ РОССИЙСКОЙ ФЕДЕРАЦИИ (21), (22) Заявка: 4742706/04, 21.12.1989 (30) Приоритет: 22.12.1988 СВ 8829923.5 (46) Дата публикации: 27.09.1996 (56) Ссылки: Европейский патент М 42226, кл.С 01 В 33/28, 1981. (71) Заявитель: Империал Кемикал Индастриз ПЛС (СВ) (72) Изобретатель: Джон Леонелло Каски[СВ], Иван Джеймс Сэмюель Лейк! СВ], Тимоти Робин Мэберли[СВ] (73) Патентообладатель: Империал Кемикал Индастриз ПЛС (СВ) (54) КАТАЛИЗАТОР ДЛЯ ПРЕВРАЩЕНИЯ УГЛЕВОДОРОДОВ (57) Реферат: Использование. нефтепереработка, в частности производство катализаторов для превращения углеводородов. Сущность изобретения: катализатор содержит цеолит МУ-87, имеющий состав, выраженный на безводной основе в молярном отношении окислов: 100 х О2: меньше или равно 10 У 203: меньше или равно 20 Кто, где К - один или более катионов с валентностью "п" по меньшей мере; частично водород; Х - кремний и/или германий; У - один или более элементов из алюминия, железа, ...

Modified solid oxidation catalyst and preparation method thereof

본 발명의 촉매는 그룹 VIB 금속의 옥시음이온으로 그룹 IVB 금속 산화물을 개질시켜 생성된 산성의 고체 생성물에 침착되는 귀금속과 같은 수소화/탈수소화 성분을 포함한다. 본 촉매의 예는 텡스테이트로 개질된 지르코니아에 침착된 백금이다. 촉매는 예로, C 4 내지 C 8 파라핀 화합물을 이성질화하는데 사용될 수 있다. The catalyst of the present invention comprises a hydrogenation / dehydrogenation component such as a noble metal which is deposited on the acidic solid product produced by modifying the group IVB metal oxide with an oxyanion of the group VIB metal. An example of this catalyst is platinum deposited on zirconia modified with wetstate. The catalyst can be used to, for example, isomerize C 4 to C 8 paraffinic compounds.

Method for converting loads from renewable sources using a catalyst including an Nu-10 zeolite and a silica-alumina

Converting a paraffinic feedstock constituted of 9-25C hydrocarbons using a catalyst comprising a hydro-dehydrogenated metal consisting of group VIB metals and/or VIII group metals and a support comprising a zeolite Nu-10 and silica alumina, is claimed. The paraffinic feedstock is produced from renewable resources, and is obtained by Fischer-Tropsch process. The method is carried out: at a temperature of 150-500[deg] C, a pressure of 0.1-15 MPa and a hourly space velocity of 0.1-10 h->1>; and in presence of hydrogen. The ratio between hydrogen and feedstock is 70-2000 Nm3>/m3>.

Method for converting loads from renewable sources using a catalyst including an Nu-10 zeolite and a ZSM-48 zeolite

Converting a paraffinic feedstock constituted of 9-25C hydrocarbons using a catalyst comprising a hydro-dehydrogenated metal consisting of group VIB metals and/or VIII group metals and a support comprising a zeolite Nu-10 and ZSM-48, is claimed. The paraffinic feedstock is produced from renewable resources, and is obtained by Fischer-Tropsch process. The method is carried out: at a temperature of 150-500[deg] C, a pressure of 0.1-15 MPa and a hourly space velocity of 0.1-10 h->1>; and in presence of hydrogen. A ratio of hydrogen and feedstock is 70-2000 Nm3>/m3>.

Solid acid catalyst, method of production of such catalyst and its application

FIELD: solid catalyst easily separated from reagents for re-use in alkylation, etherification and isomerization reactions. SUBSTANCE: method includes (a) production of carrier containing fraction of zirconium dioxide and/or hydrated zirconium dioxide and fraction of aluminum oxide and/or hydrated aluminum oxide at peak of diameter between 0.05 and 1 mcm on diameter distribution curve of pores from 0.05 to 10 mcm and application of sulfur-containing component on carrier; (2) obtaining of carrier containing fraction of zirconium dioxide and/or hydrated zirconium dioxide and fraction of aluminum oxide or hydrated aluminium oxide at volume of pores at diameter no less than 0.05 mcm and no more than 1 mcm at 0.05 to 0.5 ml/g and volume of pores at diameter higher than 1 mcm and no more than 10 mcm below 0.05 ml/g followed by application of sulfur-containing component on carrier. Invention describes also solid acid catalyst and method of performing reaction catalyzed by acid and method of carbon isomerization. EFFECT: enhanced activity, handling and mechanical strength of catalyst; application for many reactions in presence of organic compounds. 16 cl, 3 tbl, 21 dwg 906 с ПЧ сэ (19) 13) ВО `” 2190 465” С2 5 МК” В 014 4 24/04, 24/06, 27/02, 27/04, 37/04, С 07 С 5/22, 9/16, 9/15, 6/10, 49/813, 45/28, С 07 В 61/00 РОССИЙСКОЕ АГЕНТСТВО ПО ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ 12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ РОССИЙСКОЙ ФЕДЕРАЦИИ (21), (22) Заявка: 2000125097/04, 26.02.1999 (71) Заявитель: ДЖАПЭН ЭНЕРДЖИ КОРПОРЕЙШН (/Р) (24) Дата начала действия патента: 26.02.1999 (72) Изобретатель: МАЦУЗАВА Кендзи (+Р), (30) Приоритет: 04.03.1998 Р 10/67614 АИМОТО Кохдзиро (4Р), СЕКИ Казухиро (/Р) (46) Дата публикации: 10.10.2002 (73) Патентообладатель: ЖАПЭН ЭНЕРДЖИ КОРПОРЕЙШН (/Р (56) Ссылки: УР 61153140 А, 11.07.1986. КЦ д д (УР) 2100067 СЛ, 2Г.12.1997. КЦ 2103059 СЛ, (74) Патентный поверенный: 21.01.1998. КЦ 2050976 СЛ, 21.12.1935. $9 Фомичева Тамара Семеновна 806104 СЛ, 25.02.1981. КЦ 2171827 СЛ ...

Zeolite ssz-41 and method of preparation thereof

FIELD: hydrocarbon conversion catalysts. SUBSTANCE: invention provides novel crystalline zeolite SSZ-41 including oxides of silicon or silicon-germanium mixture and zinc oxide, the latter being present in amounts (calculated for metal) from ca. 2 to ca. 5% based on total weight of metals in zeolite. Zeolite is characterized by x-ray diffraction corresponding to standard pattern and adsorption capacity with regard to argon at least about 0.06 cu.cm/g at 87 K. Invention also provides preparation and use of zeolite for conversion of hydrocarbons. EFFECT: increased adsorption capacity. 11 cl, 6 tbl, ex 659 с ПЧ сэ (19) РОССИЙСКОЕ АГЕНТСТВО ПО ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ ВИ” 2 153 397. (51) МПК? 13) С2 В 01 + 29/70, С 01 В 39/48, С 10 С 47/16 12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ РОССИЙСКОЙ ФЕДЕРАЦИИ (21), (22) Заявка: 97102114/04, 21.06.1995 (24) Дата начала действия патента: 21.06.1995 (30) Приоритет: 11.07.1994 Ш$ 08/273,068 (46) Дата публикации: 21.01.2000 (56) Ссылки: Ц$ 4910006 А, 20.03.1990. МО 89/09185 АЛ, 05.10.1989. (85) Дата перевода заявки РСТ на национальную фазу: 11.02.1997 (86) Заявка РСТ: 1$ 95/07884 (21.06.1995) (87) Публикация РСТ: М/О 96/01688 (25.01.1996) (98) Адрес для переписки: 129010, Москва, ул. Большая Спасская 25, стр.3, ООО "Городисский и Партнеры", Томской Е.В. (71) Заявитель: . ШЕВРОН Ю.ЭС.ЭИ.ИНК. (43) (72) Изобретатель: Стейси И. ЗОУНЗ (ЦЭ), Дональд С. САНТИЛЛИ (4$) (73) Патентообладатель: ШЕВРОН Ю.ЭС.ЭЙ.ИНК. (4$) (54) ЦЕОЛИТ $$7-41 И СПОСОБ ЕГО ПОЛУЧЕНИЯ (57) Изобретение относится к новому кристаллическому цеолиту $$/-41. Описывается цеолит $$/-41, включающий оксиды (1) кремния или смеси кремния и германия и (2) цинка, причем указанный цинк присутствует в количестве примерно 2 - 5 вес.% металлического цинка по отношению к общему весу металлов в указанном цеолите и указанный цеолит имеет линии дифракции рентгеновских лучей из Таблицы 1 и адсорбционную емкость по отношению к аргону не менее примерно 0,06 см3/г аргона при 87’ К Также описываются ...

A kind of solid acid catalyst and normal butane-iso-butane isomerization method for isomerization reaction

本发明涉及一种用于异构化反应的固体酸催化剂以及正丁烷‑异丁烷异构化方法，属于烷基异构化技术领域。本发明利用模板法制备得到的纳米棒状AlOOH作为催化剂载体，其具有比表面积大、活性中心负载量大的优点，在其表面负载活性Pb和W作为催化活性中心，具有烷基异构化反应转化率高、选择性好、催化剂使用寿命长势优点。

Highly active isomerisation catalyst and isomerisation method

Изобретение относится к катализатору и способу для селективного повышения качества парафинового сырья с целью получения обогащенного изопарафинами продукта в качестве компонента бензина. Описан катализатор, включающий носитель из сульфатированного оксида или гидроксида из металла группы IVB (IUPAC 4), первый компонент из, по меньшей мере, одного лантанидного элемента или иттриевого компонента, которым преимущественно является иттербий, и, по меньшей мере, один металл платиновой группы, которым преимущественно является платина, и огнеупорное оксидное связующее, на котором диспергирован, по меньшей мере, один металл платиновой группы. Описан способ приготовления указанного выше катализатора, включающий сульфатирование оксида или гидроксида из металла группы IVB, нанесение первого компонента, смешение сульфатированного носителя с огнеупорным неорганическим оксидным носителем, прокаливание, нанесение второго компонента и последующее прокаливание. Описан способ конверсии углеводородов путем контактирования сырья с описанным выше катализатором. Технический эффект - селективное повышение качества парафинового сырья. 3 н. и 9 з.п. ф-лы, 2 табл., 2 ил. ÐÎÑÑÈÉÑÊÀß ÔÅÄÅÐÀÖÈß RU (19) (11) 2 329 099 (13) C1 (51) ÌÏÊ B01J 27/053 B01J 23/63 B01J 21/06 B01J 23/89 B01J 37/00 ÔÅÄÅÐÀËÜÍÀß ÑËÓÆÁÀ C07C 5/22 ÏÎ ÈÍÒÅËËÅÊÒÓÀËÜÍÎÉ ÑÎÁÑÒÂÅÍÍÎÑÒÈ,C07C 5/13 ÏÀÒÅÍÒÀÌ È ÒÎÂÀÐÍÛÌ ÇÍÀÊÀÌ (12) (2006.01) (2006.01) (2006.01) (2006.01) (2006.01) (2006.01) (2006.01) ÎÏÈÑÀÍÈÅ ÈÇÎÁÐÅÒÅÍÈß Ê ÏÀÒÅÍÒÓ (21), (22) Çà âêà: 2007102047/04, 15.06.2005 (24) Äàòà íà÷àëà îòñ÷åòà ñðîêà äåéñòâè ïàòåíòà: 15.06.2005 (30) Êîíâåíöèîííûé ïðèîðèòåò: 21.06.2004 US 10/872.581 (45) Îïóáëèêîâàíî: 20.07.2008 Áþë. ¹ 20 (73) Ïàòåíòîîáëàäàòåëü(è): ÞÎÏ ËËÊ (US) 2 3 2 9 0 9 9 (56) Ñïèñîê äîêóìåíòîâ, öèòèðîâàííûõ â îò÷åòå î ïîèñêå: US 6706659 A, 16.03.2004. RU 2176233 C1, 27.11.2001. RU 2196124 Ñ1, 10.01.2003. US 4241036 A, 23.12.1980. US 6359179 A, 19.03.2002. (85) Äàòà ïåðåâîäà çà âêè PCT íà íàöèîíàëüíóþ ôàçó: 22.01.2007 (86) Çà âêà ...

Method for alkylation of isomerization of hydrocarbon

Дискретный катализатор образуют путем контактирования в условиях текучей среды, гомогенной текучей среды, содержащей углеводород парафинового ряда, имеющий от 4 до 12 углеродных атомов, с кислотной парой кислота Льюиса (кислота Бренстеда/182) и, по желанию, с переходным металлом, для получения дискретного каталитического комплекса, который растворим в текучей среде. Дискретный катализатор является реакционным продуктом кислотной пары и алканов и включает углеводородные лиганды с ограниченной длиной цепи, делающие его растворимым в текучей среде. Катализатор является активным для изомеризации алканов и олефинов и алкилирования изоалканов при гомогенном состоянии текучей среды.

Superacid Catalyst for hydroisomerization of N-paraffins and process for its preparation

描述了一种基于硫酸氧化锆的超强酸催化剂,其可还含有一种贵金属,特征在于在0.1至0.3cm 2 /g范围内的孔隙度由至少70%直径在1至4nm的孔构成。还描述了上述催化剂的制备,其在酸催化反应中的活性和在正链烷烃的脱氢异构化中的应用。

PROCESS FOR VALUING C4 OLEFINIC CUTS

Patent FR1582423A

HYDROCARBON CONVERSION PROCESS, CATALYST FOR ITS IMPLEMENTATION AND PREPARATION PROCESS OF THIS CATALYST

Process for the catalytic transformation of hydrocarbons and catalyst used

Patent FR2347096B1

METHOD FOR CONVERTING CHARGES FROM RENEWABLE SOURCES USING A CATALYST COMPRISING A NU-10 ZEOLITE AND AN ALUMINA SILICA

PROCESS FOR VALUING C4 OLEFINIC CUTS

Patent FR2006803B1

NOVEL HETEROPOLYANION CONTAINING CATALYSTS FOR USE IN PARAFFIN CONVERSION PROCESSES

CATALYTIC COMPOSITION FOR THE VERSION OF HYDROCARBONS AND PROCEDURE FOR THE DEHYDRATION OF PERFLUOROALCANSOLPHONIC ACIDS INTENDED TO BE PART OF THE COMPOSITION

Tri:metallic catalyst for reforming, etc. - contains a platinum group metal, indium, and manganese, molybdenum or technetium on e.g. alumina

A catalyst comprises (in wt.% w.r.t. the support): 0.05-0.6 (esp. 0.1-0.5) wt.% of a noble metal of the Pt family; 0.05-4 (esp. 0.2-0.8) In; 0.005-3 of one or more of Mn, Mo and Tc (esp. 0.2-0.5 of Mn and/or Tc); 0.1-15 of a halogen; and a support. Also claimed is the use of the catalyst in isomerisation of aromatics and paraffins, hydrocracking, hydrodealkylation and steam dealkylation of aromatics, and esp. in reforming and aromatics prodn. from gasolines. The catalyst is pref. used as a moving bed. Catalyst activity and life are increased. Under the severe conditions of reforming to high -octane gasoline (min. index 102, clear), hydrogenolysis is reduced.

METHOD FOR CONVERTING CHARGES FROM RENEWABLE SOURCES USING A CATALYST COMPRISING A NU-10 ZEOLITE AND ZSM-48 ZEOLITE

L'invention concerne un procédé de conversion d'une charge paraffinique constituée par des hydrocarbures ayant un nombre d'atomes de carbone compris entre 9 et 25, ladite charge paraffinique étant produite à partir de ressources renouvelables, mettant en œuvre un catalyseur comprenant au moins un métal hydro-déshydrogénant choisi dans le groupe formé par les métaux du groupe VIB et du groupe VIII de la classification périodique, pris seuls ou en mélange et un support comprenant au moins une zéolithe Nu-10 et au moins une zéolithe ZSM-48, ledit procédé opérant à une température comprise entre 150 et 500°C, à une pression comprise entre 0,1 MPa et 15 MPa, à une vitesse spatiale horaire comprise entre 0,1 et 10 h-1 et en présence d'une quantité totale d'hydrogène mélangée à la charge telle que le ratio hydrogène/charge soit compris entre 70 et 2000 Nm3/m3 de charge. The invention relates to a process for converting a paraffinic feed consisting of hydrocarbons having a number of carbon atoms between 9 and 25, said paraffinic feed being produced from renewable resources, using a catalyst comprising at least a hydro-dehydrogenating metal chosen from the group formed by metals from group VIB and group VIII of the periodic table, taken alone or as a mixture and a support comprising at least one Nu-10 zeolite and at least one ZSM-48 zeolite, said process operating at a temperature between 150 and 500 ° C, at a pressure between 0.1 MPa and 15 MPa, at an hourly space velocity between 0.1 and 10 h-1 and in the presence of a total quantity of hydrogen mixed with the feed such that the hydrogen / feed ratio is between 70 and 2000 Nm3 / m3 of feed.

USE OF ZEOLITE IZM-2 CATALYST AND EUO ZEOLITE CATALYST FOR ISOMERIZING C8 AROMATIC CUTTING

On décrit un procédé d'isomérisation d'une coupe aromatique comprenant au moins un composé aromatique à huit atomes de carbone par molécule, ledit procédé mettant en œuvre l'utilisation successive de deux catalyseurs d'isomérisation à base de zéolithe IZM-2 (A) puis à base de zéolithe EUO (B). An isomerization process of an aromatic section comprising at least one aromatic compound with eight carbon atoms per molecule, said process involving the successive use of two isomerization catalysts based on zeolite IZM-2 (A) is described. ) then based on EUO zeolite (B).

Patent JPS568080B1

Process for the manufacture of synthetic saponites

A B S T R A C T PROCESS FOR THE MANUFACTURE OF SYNTHETIC SAPONITES Process for the preparation of synthetic saponites according to the general formula (II) wherein A represents any metal ion having basic or amphoteric properties, M represents a bivalent metal ion having an ionic radius between 0.050 and 0.085 nm or lithium, Z represents a fluoride moiety, n represents the valency of A, x represents a number between 0.05 and 1.5, y represents a number from 0 to 2.95, and z = y when M = lithium and zero when M represents a bivalent metal ion as defined hereinabove, by reacting under solid state conditions a silica source, an alumina source, a magnesia source, a sodium and/or lithium source, a fluoride source and optionally a further source containing A and/or M metal ions and/or a chloride source, at a temperature between the lowest melting point of any alkali fluoride or chloride which is either present as such or which could be formed under solid state synthesis conditions and a temperature not more than 200 °C below said temperature. The saponites (constituting novel materials when M represents Ni, Co or Cu) can be used as (catalyst) carriers, e.g. in the (hydro)-isomerisation of hydrocarbons.

METHOD OF HYDROISOMERIZING A FISCHER-TROPSCH SYNTHESIS LOAD USING A CATALYST COMPRISING A NU-10 ZEOLITE AND AN ALUMINUM SILICA

L'invention concerne un procédé d'hydroisomérisation d'une charge paraffinique bouillant à une température comprise entre 150 et 370°C, ladite charge paraffinique étant produite par synthèse Fischer-Tropsch, ledit procédé d'hydroisomérisation mettant en œuvre un catalyseur comprenant au moins un métal hydro-déshydrogénant choisi dans le groupe formé par les métaux du groupe VIB et du groupe VIII de la classification périodique, pris seuls ou en mélange et un support comprenant au moins une zéolithe Nu-10 et au moins une silice alumine, ledit procédé d'hydroisomérisation étant effectué à une température comprise entre 150 et 400°C, à une pression comprise entre 0,1 MPa et 7 MPa, à une vitesse spatiale horaire comprise entre 0,1 et 10 h-1 et en présence d'une quantité totale d'hydrogène mélangée à la charge telle que le ratio hydrogène/charge soit compris entre 70 et 2000 Nm3/m3 de charge. The invention relates to a process for hydroisomerization of a paraffinic filler boiling at a temperature between 150 and 370 ° C, said paraffinic filler being produced by Fischer-Tropsch synthesis, said hydroisomerization process using a catalyst comprising at least a hydro-dehydrogenating metal selected from the group consisting of Group VIB metals and Group VIII of the Periodic Table, taken alone or as a mixture and a support comprising at least one Nu-10 zeolite and at least one silica-alumina, said process hydroisomerization being carried out at a temperature of between 150 and 400 ° C., at a pressure of between 0.1 MPa and 7 MPa, at a space velocity of between 0.1 and 10 h -1 and in the presence of a total amount of hydrogen mixed with the feed such that the hydrogen / feed ratio is between 70 and 2000 Nm3 / m3 of feedstock.

Hydrocarbon conversion process

NOVEL HETEROPOLYANION-CONTAINING CATALYSTS FOR USE IN PARAFFIN CONVERSION PROCESSES

De nouveaux catalyseurs contenant des hétéropolyanions de l'acide 12-tungstophosphorique ou de l'acide 12-tungstomolybdique et, pour certains, au moins un métal du groupe VIII, et déposés sur des supports développant une surface spécifique et un volume poreux élevés, tels que l'oxyde de zirconium (ZrO2 ), des silices, des silices-alumines ou des alumines, sont utilisés notamment en isomérisation des coupes paraffiniques contenant en majeure partie des n-paraffines ayant par exemple de 4 à 8 atomes de carbone par molécule et en alkylation aliphatique des isoparaffines (par exemple de l'isobutane et/ ou de l'isopentane) par au moins une oléfine comprenant par exemple de 2 à 6 atomes de carbone par molécule (C2 à C6 ). New catalysts containing heteropolyanions of 12-tungstophosphoric acid or 12-tungstomolybdic acid and, for some, at least one group VIII metal, and deposited on supports developing a high specific surface and a high pore volume, such as that zirconium oxide (ZrO2), silicas, silica-aluminas or aluminas, are used in particular in the isomerization of paraffinic cuts containing for the most part n-paraffins having for example from 4 to 8 carbon atoms per molecule and in aliphatic alkylation of isoparaffins (for example isobutane and/or isopentane) by at least one olefin comprising for example from 2 to 6 carbon atoms per molecule (C2 to C6).

Patent JPH0226541B2

Process for preparing a catalyst which can be used for the conversion of hydrocarbons

METHOD FOR CONVERTING CHARGES FROM RENEWABLE SOURCES USING A CATALYST COMPRISING A NU-10 ZEOLITE AND ZSM-48 ZEOLITE

L'invention concerne un procédé de conversion d'une charge paraffinique constituée par des hydrocarbures ayant un nombre d'atomes de carbone compris entre 9 et 25, ladite charge paraffinique étant produite à partir de ressources renouvelables, mettant en œuvre un catalyseur comprenant au moins un métal hydro-déshydrogénant choisi dans le groupe formé par les métaux du groupe VIB et du groupe VIII de la classification périodique, pris seuls ou en mélange et un support comprenant au moins une zéolithe Nu-10 et au moins une zéolithe ZSM-48, ledit procédé opérant à une température comprise entre 150 et 500°C, à une pression comprise entre 0,1 MPa et 15 MPa, à une vitesse spatiale horaire comprise entre 0,1 et 10 h-1 et en présence d'une quantité totale d'hydrogène mélangée à la charge telle que le ratio hydrogène/charge soit compris entre 70 et 2000 Nm3/m3 de charge. The invention relates to a process for converting a paraffinic feedstock consisting of hydrocarbons having a carbon number of between 9 and 25, said paraffinic feed being produced from renewable resources, using a catalyst comprising at least a hydro-dehydrogenating metal selected from the group consisting of Group VIB metals and Group VIII of the Periodic Table, taken alone or as a mixture and a carrier comprising at least one Nu-10 zeolite and at least one ZSM-48 zeolite, said process operating at a temperature between 150 and 500 ° C, at a pressure of between 0.1 MPa and 15 MPa, at a space velocity of between 0.1 and 10 h -1 and in the presence of a total amount of of hydrogen mixed with the feed such that the hydrogen / feed ratio is between 70 and 2000 Nm3 / m3 of feedstock.

Hydrocarbon conversion catalysts, esp. for reforming - contg. platinum-group metal, hafnium and group=iib metal

New catalysts comprise 100 pts. wt. of a support, 0.05-0.6 (pref. 0.1-0.5) pts. wt. of a Pt-gp. metal (M), 0.005-5 (pref. 0.01-3, esp. 0.05-0.4) pts. wt. of Hf, 0.005-5 (pref. 0.05-3, esp. 0.08-1) pts. wt. of at least one metal (M') selected from Zn, Cd and Hg, and 0.1-15 pts. wt. of a halogen. The support is pref. alumina. M is pref. Pt or Ir and M' is pref. Cd or Zn. The catalysts can be prepd. by impregnation in one or more stages, e.g. by impregnation with an aq. soln. contg. HCl, H2PtCl6, HfOCl2 and M'Cl2. The catalysts are esp. useful for reforming or aromising, but can also be used for hydrocracking, isomerisation of alkyl- aromatics, hydroisomerisation of 4-7C paraffins, or hydro- or steam-dealkylation of alkylaromatics. Incorporation of both Hf and M' increases the selectivity of the catalysts, esp. when used for continuous high-severity reforming (to RON = 102+) in a series of at least 2 mobile-bed reactors.

METHOD FOR ACTIVATION OF A CATALYST FOR ISOMERIZATION OF NORMAL PARAFFINS