Method of Improving Metal-impregnated Catalyst Performance

A method of reducing the amount of carbon monoxide present during the metal reduction step of start-up, thus, maintaining metal dispersion and improving the metal reduction and catalyst yields. Carbon monoxide formation is minimized during the start-up procedure and during the initial catalyst dryout phase in a hydrogen-containing atmosphere, gas is purged from the reactor system, either continuously at constant pressure or by a series of pressure/depressure cycles, to remove carbon monoxide. The purging is conducted at temperatures of about 30-500° C. and pressures of about −90-5,000 kPa(g) (−0.9-50 bar(g)). In this temperature range, carbon monoxide absorbed to the surface of the metal will desorb into the hydrogen-containing atmosphere and can be removed from the system along with carbon monoxide present in the atmosphere through the purging. 1. A method of desorbing carbon monoxide from metal-impregnated catalysts , the method comprising purging gas from the catalyst reactor system at about 30-500° C. and about −90 kPa(g)-5 ,000 kPa(g) while the catalyst is in the presence of hydrogen by performing at least two pressure/depressure cycles , wherein said metal comprises platinum in an amount less than about 0.05 wt % , and wherein said purging reduces the carbon monoxide concentration in the catalyst reactor system to about 1 ppm or less.2. (canceled)3. The method of wherein said hydrogen comprises about 0.3 ppm or less of carbon monoxide.4. The method of wherein said pressure/depressure cycle comprises pressurizing the catalyst reactor system to at least about 500 kPa(g) with a gas containing about 0.3 ppm or less of carbon monoxide and subsequently depressurizing the catalyst reactor system to about 200 kPa(g) or less.5. The method of wherein said gas comprises nitrogen or hydrogen.6. The method of wherein said pressure/depressure cycle is repeated four times.7. The method of wherein the catalyst reactor system is depressured to about 200 kPa(g) or less prior to ...

METHODS FOR APPLYING SOLUTION CATALYSTS TO REACTOR SURFACES

A method for treating at least one interior surface (for example, a bed wall) of a fluidized bed polymerization reactor system, including by applying a solution catalyst (preferably at least substantially uniformly and in liquid form) to each surface, and optionally (where a catalyst component of the solution catalyst comprises at least one chromium containing compound) oxidizing at least some of the applied chromium containing compound in a controlled manner. 166-. (canceled)67. A method for treating interior surfaces of a fluidized bed polymerization reactor system , said surfaces including at least one sensitive surface and at least one nonsensitive surface , said method including the steps of:(a) applying a zinc coating to at least one said sensitive surface but not to at least one said nonsensitive surface; and(b) after step (a), applying a solution catalyst at least substantially uniformly and in liquid form to each said sensitive surface and each said nonsensitive surface.68. The method of claim 67 , wherein the solution catalyst comprises a dissolved chromium containing compound.69. The method of claim 68 , wherein the chromium containing compound is chromocene.70. The method of claim 67 , wherein the solution catalyst comprises chromocene dissolved in toluene.71. The method of claim 67 , wherein the reactor system has a bed wall and step (b) includes the step of:introducing at least one spray of droplets of the solution catalyst into the reactor system under conditions such that many of the droplets neither vaporize nor sublimate before contacting the bed wall.72. The method of claim 67 , wherein step (b) includes the step of:introducing the solution catalyst into the reactor system under conditions such that the solution catalyst has a drying rate sufficiently low so as not to prevent at least substantially uniform wetting of each said each said sensitive surface and each said nonsensitive surface by the solution catalyst.73. The method of claim 67 , ...

Reactor Components

The present disclosure relates to reactor components and their use, e.g., in regenerative reactors. A process and apparatus for utilizing different wetted areas along the flow path of a fluid in a pyrolysis reactor, e.g., a thermally regenerating reactor, such as a regenerative, reverse-flow reactor, is described. 1. A hydrocarbon conversion method comprising: {'sub': v1', 'v2', 'v2', 'v1, 'the regenerative reactor has a first portion having a first plurality of flow passages with a wetted area aand a second portion having a second plurality of flow passages with a second wetted area a, wherein the ratio of the second wetted area ato the first wetted area ais ≦0.75; and'}, 'passing a first mixture comprising hydrocarbons to a regenerative reactor, wherein'}{'sub': '2', 'reacting at least a portion of the hydrocarbons within the regenerative reactor to produce a second mixture comprising Cunsaturates.'}2. The method of claim 1 , wherein the ratio of the second wetted area ato the first wetted area ais ≦0.5.3. The method of claim 1 , wherein the ratio of the second wetted area ato the first wetted area ais in the range of 0.05 to 0.75.4. The method of claim 1 , wherein the ratio of the second wetted area ato the first wetted area ais in the range of 0.1 to 0.5.5. The method of claim 1 , comprising: [{'br': None, 'i': R', '=a', '/a', '=X, 'sub': 21', 'v2', 'v1, 'sup': (T', {'sub2': '2'}, '-T', {'sub2': '1'}, ')/300}, {'sub': 21', '2', '1, 'wherein Ris the ratio, Tis the zone temperature of the second portion in units of ° C., Tis the zone temperature of the first portion in units of ° C., and the X parameter is between 0.1 and 0.9;'}], 'calculating the ratio by the following equation{'sub': '21', 'obtaining the first portion and the second portion based on the determined ratio R; and'}disposing the first portion and second portion within the regenerative reactor.6. The method of claim 5 , wherein the X parameter is in the range of 0.25 to 0.75.7. The method of claim 1 ...

Production of Olefins and Aromatics

In a process for producing olefins and aromatic hydrocarbons, a feed comprising a biomass pyrolysis oil or a fraction thereof is supplied to a steam cracking unit operating at a temperature of 600° C. to 1000° C. or a reverse flow reactor operating at a temperature of 900° C. to 1,700° C. and is thermally cracked to produce one or more hydrocarbon effluent fractions. 1. A process for producing olefins and aromatic hydrocarbons , the process comprising:(a) supplying a feed comprising a biomass pyrolysis-oil or a fraction thereof to a steam cracking unit operating at a temperature of 600° C. to 1000° C. and recovering one or more hydrocarbon effluent fractions.2. The process of claim 1 , wherein the residence time of the feed at said temperature of 600° C. to 1000° C. is less than 1 second.3. The process of claim 1 , wherein the feed to the steam cracking unit also comprises a fossil hydrocarbon feedstock.4. The process of claim 3 , wherein the fossil hydrocarbon feedstock is selected from ethane claim 3 , natural gas liquids claim 3 , natural gas condensate claim 3 , naphtha claim 3 , distillate claim 3 , gas oils claim 3 , resids claim 3 , shale oils and/or crude oils.5. The process of claim 1 , wherein the hydrocarbon effluent fractions comprise C+ olefins and C+ aromatic hydrocarbons.6. The process of claim 1 , further comprising removing CO claim 1 , CO claim 1 , HO claim 1 , and organic oxygenates from said hydrocarbon effluent fractions.7. A process for producing olefins and aromatic hydrocarbons claim 1 , the process comprising:(a) pyrolysing biomass in a reactor under conditions to convert the biomass to a vapor condensable into pyrolysis oil, non-condensable gases and solid biochar; and(b) supplying a feed comprising at least part of the condensable vapor or the condensed pyrolysis oil to a steam cracking unit operating at a temperature of 600° C. to 1000° C. and recovering one or more hydrocarbon effluent fractions.8. The process of claim 7 , wherein said ...

Hydrocarbon Conversion Process

The invention relates to processes for converting a mixture of hydrocarbon and oxygenate into products containing acetylene and carbon monoxide. The invention also relates to utilizing at least a portion of the acetylene and carbon monoxide for producing xylenes such as p-xylene, utilizing at least a portion of xylenes for producing polymeric fibers, and to equipment useful for these processes. 1. A hydrocarbon conversion process , comprising:(a) providing a first mixture, the first mixture comprising ≧10.0 wt. % hydrocarbon and ≧1.0 wt. % oxygenate, the weight percents being based on the weight of the first mixture;(b) exposing the first mixture a temperature ≧700° C. in a first region under pyrolysis conditions to produce a second mixture, the second mixture comprising molecular hydrogen, carbon monoxide, and ≧1.0 wt. % of acetylene based on the weight of the second mixture, wherein the second mixture has a molecular hydrogen:carbon monoxide molar ratio ≧2.0 and a carbon monoxide:acetylene molar ratio ≧0.1;(c) converting at least a portion of the second mixture's acetylene to produce a first intermediate mixture comprising ≧10.0 wt. % aromatic hydrocarbon based on the weight of the intermediate mixture;(d) reacting at least a portion of the second mixture's carbon monoxide with at least a portion of the second mixture's molecular hydrogen to produce a second intermediate mixture comprising ≧10.0 wt. % alcohol based on the weight of the second intermediate mixture; and(e) reacting at least a portion of the first intermediate mixture's aromatics with at least a portion of the second intermediate mixture's alcohol to produce a product comprising water and ≧10.0 wt. % p-xylene based on the weight of the product.2. The process of claim 1 , wherein the first mixture comprises ≧25.0 wt. % of hydrocarbon and ≧10.0 wt. % of oxygenate claim 1 , the oxygenate having an Effectiveness Factor ≧0.05 claim 1 , and further comprises ≧5.0 wt. % molecular hydrogen claim 1 , the ...

Hydrocarbon Conversion Process

The invention relates to processes for converting hydrocarbons to phthalic acids such as terephthalic acid. The invention also relates to polymerizing phthalic acid derivatives to produce, e.g., synthetic fibers.

Reactor Components

The present disclosure relates to reactor components and their use, e.g., in regenerative reactors. A process and apparatus for utilizing different wetted areas along the flow path of a fluid in a pyrolysis reactor, e.g., a thermally regenerating reactor, such as a regenerative, reverse-flow reactor, is described. 1. A hydrocarbon conversion method comprising: {'sub': v1', 'v2', 'v2', 'v1, 'the regenerative reactor has a first portion having a first plurality of flow passages with a wetted area aand a second portion having a second plurality of flow passages with a second wetted area a, wherein the ratio of the second wetted area ato the first wetted area ais ≦0.75; and'}, 'passing a first mixture comprising hydrocarbons to a regenerative reactor, wherein'}reacting at least a portion of the hydrocarbons within the regenerative reactor to produce{'sub': '2', 'a second mixture comprising Cunsaturates.'}2. The method of claim 1 , wherein the ratio of the second wetted area ato the first wetted area ais ≦0.5.3. The method of claim 1 , wherein the ratio of the second wetted area ato the first wetted area ais in the range of 0.05 to 0.75.4. The method of claim 1 , wherein the ratio of the second wetted area ato the first wetted area ais in the range of 0.1 to 0.5.5. The method of claim 1 , comprising: [{'br': None, 'i': R', '=a', '/a', '=X, 'sub': 21', 'v2', 'v1, 'sup': (T', {'sub2': '2'}, '-T', {'sub2': '1'}, ')/300}, {'sub': 21', '2', '1, 'wherein Ris the ratio, Tis the zone temperature of the second portion in units of ° C., Tis the zone temperature of the first portion in units of ° C., and the X parameter is between 0.1 and 0.9;'}], 'calculating the ratio by the following equation{'sub': '21', 'obtaining the first portion and the second portion based on the determined ratio R; and'}disposing the first portion and second portion within the regenerative reactor.6. The method of claim 5 , wherein the X parameter is in the range of 0.25 to 0.75.7. The method of claim 1 , ...

Hydrocarbon Conversion Process

The invention relates to processes for converting a mixture of hydrocarbon and sulfur-containing molecules such as mercaptan into products comprising acetylene, ethylene, and hydrogen sulfide, to processes utilizing the acetylene and ethylene resulting from the conversion, and to equipment useful for such processes. 1. A hydrocarbon conversion process , comprising:(a) providing a first mixture comprising ≧90 wt. % of hydrocarbon having a hydrogen content in the range of from 6 wt. % to 25 wt. % and ≧4.0 ppmw mercaptan based on the weight of the first mixture; and{'sup': '3', 'sub': 2', 'x, "(b) pyrolysing the first mixture in a first region under pyrolysis conditions which include exposing the first mixture to a temperature ≧1.20×10° C., to convert at least a portion of the natural gas and ≧90.0 wt. % of the first mixture's mercaptan based on the weight of mercaptan in the first mixture to produce a second mixture, the second mixture comprising ≧1.0 wt. % Cunsaturates, ≦20.0 wt. % CO, wherein x is 1 or 2, ≦1.0 ppmw mercaptan, and ≦1.0 ppmw thiophene based on the weight of the second mixture."}2. The process of claim 1 , wherein the first mixture comprises ≧20.0 wt. % methane and ≧10.0 ppmw methyl mercaptan based on the weight of the first mixture; the first mixture being obtained from a natural gas with no intervening mercaptan-removal steps claim 1 , and wherein the second mixture comprises ≦0.05 ppmw methyl mercaptan based on the weight of the second mixture.3. The process of claim 1 , wherein the first mixture further comprises hydrogen sulfide in an amount in the range of 50.0 ppmw to 5 wt. % based on the weight of the first mixture.4. The process of claim 1 , wherein the first mixture is exposed to a temperature ≧1.45×10° C. during the pyrolysing.5. The process of any of claim 1 , further comprising (c) separating hydrogen sulfide from the second mixture to produce a third mixture.6. The process of claim 5 , further comprising:(d) combining first and second ...

Production and Use of 3,4' and 4,4'-Dimethylbiphenyl Isomers

In a process for producing 3,4′ and/or 4,4′ dimethyl-substituted biphenyl compounds, a feed comprising toluene is contacted with hydrogen in the presence of a hydroalkylation catalyst under conditions effective to produce a hydroalkylation reaction product comprising (methylcyclohexyl)toluenes. At least part of the hydroalkylation reaction product is dehydrogenated in the presence of a dehydrogenation catalyst under conditions effective to produce a dehydrogenation reaction product comprising a mixture of dimethyl-substituted biphenyl isomers. The dehydrogenation reaction product is then separated into at least a first stream containing at least 50% of 3,4′ and 4,4′ dimethylbiphenyl isomers by weight of the first stream and at least one second stream comprising one or more 2,x′ (where x′ is 2′, 3′, or 4′) and 3,3′ dimethylbiphenyl isomers. 1. A process for producing 3 ,4′ and/or 4 ,4′ dimethyl-substituted biphenyl compounds , the process comprising:(a1) contacting a feed comprising toluene with hydrogen in the presence of a hydroalkylation catalyst under conditions effective to produce a hydroalkylation reaction product comprising (methylcyclohexyl)toluenes;(b1) dehydrogenating at least part of the hydroalkylation reaction product in the presence of a dehydrogenation catalyst under conditions effective to produce a dehydrogenation reaction product comprising a mixture of dimethyl-substituted biphenyl isomers; and(c1) separating the dehydrogenation reaction product into at least a first stream containing at least 50% of 3,4′ and 4,4′ dimethylbiphenyl isomers by weight of the first stream and at least one second stream comprising one or more 2,X′ (where X′ is 2′, 3′, or 4′) and 3,3′ dimethylbiphenyl isomers.2. The process of claim 1 , wherein the hydroalkylation catalyst comprises an acidic component and a hydrogenation component.3. The process of claim 2 , wherein the acidic component of the hydroalkylation catalyst comprises a molecular sieve selected from the group ...

Production and Use of 3,4' and 4,4'-Dimethylbiphenyl Isomers

In a process for producing 3,4′ and/or 4,4′ dimethyl-substituted biphenyl compounds, a feed comprising toluene is contacted with hydrogen in the presence of a hydroalkylation catalyst under conditions effective to produce a hydroalkylation reaction product comprising (methylcyclohexyl)toluenes. At least part of the hydroalkylation reaction product is dehydrogenated in the presence of a dehydrogenation catalyst under conditions effective to produce a dehydrogenation reaction product comprising a mixture of dimethyl-substituted biphenyl isomers. The dehydrogenation reaction product is then separated into at least a first stream containing at least 50% of 3,4′ and 4,4′ dimethylbiphenyl isomers by weight of the first stream and at least one second stream comprising one or more 2,x′ (where x′ is 2′, 3′, or 4′) and 3,3′ dimethylbiphenyl isomers. 1. A process for producing 3 ,4′ and/or 4 ,4′ dimethyl-substituted biphenyl compounds , the process comprising:(a2) contacting a feed comprising benzene with hydrogen in the presence of a hydroalkylation catalyst under conditions effective to produce a hydroalkylation reaction product comprising cyclohexylbenzenes;(b2) dehydrogenating at least part of the hydroalkylation reaction product in the presence of a dehydrogenation catalyst under conditions effective to produce a dehydrogenation reaction product comprising biphenyl;(c2) reacting at least part of the dehydrogenation reaction product with a methylating agent in the presence of an alkylation catalyst under conditions effective to produce a methylation reaction product comprising a mixture of dimethyl-substituted biphenyl isomers; and(d2) separating the methylation reaction product into at least a first stream containing at least 50% of 3,4′ and 4,4′ dimethylbiphenyl isomers by weight of the first stream and at least one second stream comprising one or more 2,X′ (where X′ is 2′, 3′, or 4′) and 3,3′ dimethylbiphenyl isomers.2. The process of claim 1 , wherein the ...

Method and Apparatus for Managing Hydrogen Content Through The Conversion of Hydrocarbons Into Olefins

An apparatus and method are provided for processing hydrocarbon feeds. The method enhances the conversion of hydrocarbon feeds into conversion products, such as ethylene and propylene. In particular, the present techniques combine a first hydrocarbon feed with a second hydrocarbon feed and a hydrogen (H 2 ) containing stream to manage the hydrogen content of the feed provided to a pyrolysis reactor. The mixture is then exposed to high-severity operating conditions in a pyrolysis reactor and further processing into desired olefins.

Activation of Dehydrogenation Catalysts

In a process for dehydrogenating cyclohexylbenzene and/or alkyl-substituted cyclohexylbenzene compounds, a dehydrogenation catalyst comprising at least one Group 10 metal compound on a support is heated in the presence of hydrogen from a first temperature from 0° C. to 200° C. to a second, higher temperature from 60° C. to 500° C. at a ramp rate no more than 100° C./hour. The dehydrogenation catalyst is contacted with hydrogen at the second temperature for a time from 3 to 300 hours to produce an activated dehydrogenation catalyst. A feed comprising cyclohexylbenzene and/or an alkyl-substituted cyclohexylbenzene compound is then contacted with hydrogen in the presence of the activated dehydrogenation catalyst under conditions effective to produce a dehydrogenation reaction product comprising biphenyl and/or an alkyl-substituted biphenyl compound. 1. A process for dehydrogenating cyclohexylbenzene and/or alkyl-substituted cyclohexylbenzene compounds , the process comprising:(a) providing a dehydrogenation catalyst comprising at least one Group 10 metal compound on a support;(b) heating the dehydrogenation catalyst in the presence of hydrogen from a first temperature from 0° C. to 200° C. to a second, higher temperature from 60° C. to 500° C. at a ramp rate no more than 100° C./hour;(c) contacting the dehydrogenation catalyst with hydrogen at the second temperature for a time from 3 to 300 hours to produce an activated dehydrogenation catalyst; and(d) contacting a feed comprising cyclohexylbenzene and/or an alkyl-substituted cyclohexylbenzene compound with hydrogen in the presence of the activated dehydrogenation catalyst under conditions effective to produce a dehydrogenation reaction product comprising biphenyl and/or an alkyl-substituted biphenyl compound.2. The process of claim 1 , wherein the at least one Group 10 metal comprises platinum.3. The process of claim 1 , wherein the dehydrogenation catalyst comprises from 0.1 to 5% wt % of elemental platinum.4. The ...

HYDROCARBON CONVERSION PROCESS

The invention relates to processes for converting a mixture of hydrocarbon and sulfur-containing molecules such as mercaptan into products comprising acetylene, ethylene, and hydrogen sulfide, to processes utilizing the acetylene and ethylene resulting from the conversion, and to equipment useful for such processes. 1. A hydrocarbon conversion process , comprising:(a) providing a first mixture comprising ≧0.5 wt. % hydrocarbon and ≧4.0 ppmw mercaptan based on the weight of the first mixture; and{'sup': '3', 'sub': 2', 'x, "(b) exposing a first mixture to a temperature ≧1.20×10° C. in a first region under pyrolysis conditions to convert at least a portion of the hydrocarbon and ≧90.0 wt. % of the first mixture's mercaptan based on the weight of mercaptan in the first mixture to produce a second mixture, the second mixture comprising ≧1.0 wt. % Cunsaturates, ≦20.0 wt. % CO, wherein x is 1 or 2, and ≦1.0 ppmw thiophene based on the weight of the second mixture."}2. The process of claim 1 , wherein the first mixture comprises ≧20.0 wt. % methane and ≧10.0 ppmw methyl mercaptan based on the weight of the first mixture; the first mixture being obtained from a natural gas with no intervening mercaptan-removal steps claim 1 , and wherein second mixture comprises ≦0.05 ppmw methyl mercaptan based on the weight of the second mixture.3. The process of claim 1 , wherein the first mixture further comprises hydrogen sulfide in an amount in the range of 50.0 ppmw to 5 wt. % based on the weight of the first mixture.4. The process of claim 1 , wherein the first mixture is exposed to a temperature ≧1.45×10° C. during the pyrolysis.5. The process of any of claim 1 , further comprising (c) separating hydrogen sulfide from the second mixture to produce a third mixture.6. The process of claim 5 , further comprising:(d) combining first and second reactants in a second region to produce a fourth mixture, the first and second regions being at least partially coextensive; and (i) the ...

Process to Produce Terephthalic Acid

This invention relates to the production of terephthalic acid by 1) cycloaddition of 2,5 substituted furan (such as 2,5-bis hydroxymethylfuran or 5-hydroxymethylfurfural) and ethylene, and 2) the subsequent oxidation of the dehydrated cycloaddition product to terephthalic acid. The invention relates more particularly to overall biobased pathways for making terephthalic acid from carbohydrates such as hexoses (e.g., glucose or fructose). 2. The process of claim 1 , wherein the cycloaddition reaction conditions include a temperature from about 100° C. to about 300° C.3. The process of claim 1 , wherein the catalyst comprises activated carbon claim 1 , silica claim 1 , alumina claim 1 , a zeolitic molecular sieve claim 1 , or a non-zeolitic molecular sieve.4. The process of claim 3 , wherein the catalyst comprises activated carbon.5. The process of claim 4 , wherein the activated carbon is acid washed.6. The process of claim 1 , wherein at least 6 of the carbon atoms of the terephthalic acid are derived from one or more renewable feedstocks.7. The process of claim 1 , wherein the substituted furan is obtained from conversion of glucose or fructose.8. The process of claim 1 , wherein the substituted furan comprises 5-hydroxymethylfurfural.9. The process of claim 1 , wherein the substituted furan comprises 2 claim 1 ,5-bis hydroxymethylfuran.10. The process of claim 7 , wherein the substituted furan is obtained from conversion of glucose or fructose to 5-hydroxymethylfurfural.11. The process of claim 10 , wherein the 5-hydroxymethylfurfural is not converted to 2 claim 10 ,5-dimethylfuran prior to cycloaddition with ethylene.15. The process of claim 1 , wherein the substituted furan comprises 2 claim 1 ,5-bis hydroxymethylfuran and the 2 claim 1 ,5-bis hydroxymethylfuran is combined with an acid to produce a diester prior to the cycloaddition step.16. The process of claim 14 , wherein the acid is acetic acid.17. The process of claim 15 , wherein less than 1.5 moles of ...

Method and Apparatus for Converting Hydrocarbons Into Olefins

An apparatus and method are provided for processing hydrocarbon feeds. The method enhances the conversion of hydrocarbon feeds into conversion products, such as ethylene. In particular, the present techniques utilize a high-severity thermal pyrolysis reactor that exposes a feed at a peak pyrolysis gas temperature ≧1540° C. to produce a reactor product comprising ethylene and acetylene and has a C to acetylene weight ratio ≦0.5. Then, the method separates a product comprising tars and/or solids from at least a portion of the reactor product and converts at least a portion of the remaining reactor product into a conversion product, such as ethylene. 1. A hydrocarbon conversion method comprising:{'sub': '3', 'exposing a pyrolysis feed to thermal pyrolysis high-severity operating conditions including a peak pyrolysis gas temperature ≧1540.0° C. to produce a reactor product that comprises ethylene and acetylene and that has an Cto acetylene weight ratio ≦0.5;'}removing from the reactor product a first product comprising tars and/or solids; andconverting at least a portion of the reactor product's acetylene to ethylene, wherein the converting is downstream of the removing.2. The method of claim 1 , wherein the pyrolysis feed (i) comprises ≧50.0 wt. % hydrocarbons based on the weight of the pyrolysis feed and (ii) has a hydrogen to carbon (H/C) ratio in the range of 0.1 to 5.0.3. The method of claim 1 , further comprising polymerizing at least a portion of the ethylene.4. The method of claim 1 , further comprising compressing at least a portion of the reactor product upstream of the converting.5. The method of claim 1 , further comprising separating hydrogen from the reactor product upstream of the converting.6. The method of claim 1 , further comprising separating hydrogen downstream of the converting.7. The method of claim 5 , wherein the hydrogen is separated via one or more of a hydrogen membrane claim 5 , pressure swing adsorption claim 5 , electrochemical claim 5 , ...

Hydrocarbon Conversion Process

The invention relates to processes for converting a mixture of hydrocarbon and sulfur-containing molecules such as mercaptan into products comprising acetylene, ethylene, and hydrogen sulfide, to processes utilizing the acetylene and ethylene resulting from the conversion, and to equipment useful for such processes. 1. A hydrocarbon conversion process , comprising:(a) providing a first mixture comprising ≧0.5 wt. % hydrocarbon and ≧4.0 ppmw mercaptan based on the weight of the first mixture; and{'sup': '3', 'sub': 2', 'N, "(b) exposing a first mixture to a temperature ≧1.20×10° C. in a first region under pyrolysis conditions to convert at least a portion of the hydrocarbon and ≧90.0 wt. % of the first mixture's mercaptan based on the weight of mercaptan in the first mixture to produce a second mixture, the second mixture comprising ≧1.0 wt. % Cunsaturates, ≦20.0 wt. % CO, wherein x is 1 or 2, and ≦1.0 ppmw thiophene based on the weight of the second mixture."}2. The process of claim 1 , wherein the first mixture comprises ≧20.0 wt. % methane and ≧10.0 ppmw methyl mercaptan based on the weight of the first mixture; the first mixture being obtained from a natural gas with no intervening mercaptan-removal steps claim 1 , and wherein second mixture comprises ≦0.05 ppmw methyl mercaptan based on the weight of the second mixture.3. The process of claim 1 , wherein the first mixture further comprises hydrogen sulfide in an amount in the range of 50.0 ppmw to 5 wt. % based on the weight of the first mixture.4. The process of claim 1 , wherein the first mixture is exposed to a temperature ≧1.45×10° C. during the pyrolysis.5. The process of claim 1 , further comprising (c) separating hydrogen sulfide from the second mixture to produce a third mixture.6. The process of claim 5 , further comprising:(d) combining first and second reactants in a second region to produce a fourth mixture, the first and second regions being at least partially coextensive; and (i) the pyrolysis and ...

Transalkylation of Heavy Aromatic Hydrocarbon Feedstocks

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

Process for Making Para-Xylene

Disclosed is a process for making para-xylene from toluene and/or benzene comprising (i) converting toluene and/or benzene to a first product mixture comprising mixed xylenes, (ii) obtaining a xylene mixture from the first product mixture, (iii) separating para-xylene from the xylene mixture, and (iv) transalkylating meta-xylene and/or ortho-xylene with toluene and/or benzene. 1. A process for making para-xylene , the process comprising:(A) feeding a first feed comprising toluene and/or benzene to a first reactor;(B) conducting reactions in the first reactor to produce a first product mixture comprising toluene and mixed xylenes, and optionally benzene;(C) separating the first product mixture in a first separation device to obtain a first toluene-rich stream and a first xylene-rich stream;(D) separating the first xylene-rich stream in a second separation device to obtain a para-xylene-rich product stream, and a meta-xylene-rich stream;(E) feeding a third feed comprising benzene and at least a portion of the meta-xylene-rich stream to a second reactor; and(F) conducting transalkylation reactions in the second reactor in the presence of a transalkylation catalyst under transalkylation conditions to obtain a second reaction product mixture comprising benzene, toluene, and mixed xylenes.2. The process of claim 1 , further comprising:(G) separating the second reaction product mixture in a third separation device to obtain a second toluene-rich stream and a second xylene-rich stream comprising mixed xylenes.3. The process of claim 2 , further comprising:(H) feeding at least a portion of the second xylene-rich stream into the second separation device in step (D).4. The process of claim 2 , further comprising:(I) feeding at least a portion of the second xylene-rich stream into the second reactor.5. The process of claim 4 , wherein at least 50 wt % the second xylene-rich stream is fed to the second reactor;wherein (A) further comprises feeding a second feed comprising a ...

Pyrolysis Reactor Materials and Methods

In one aspect, the invention includes a reactor apparatus for pyrolyzing a hydrocarbon feedstock, the apparatus including: a reactor component comprising a refractory material in oxide form, the refractory material having a melting point of at least 2060° C. and which remains in oxide form when exposed to a gas having an oxygen partial pressure of 10bar, a carbon partial pressure above the carbon partial pressure of the zirconium carbide and zirconium oxide phase transition at the same temperature, and at temperatures below the temperature of the zirconium triple point at the oxygen partial pressure of 10bar; and ii) when exposed to a gas having an oxygen partial pressure of 10bar and at temperatures above the zirconium triple point at the oxygen partial pressure of 10bar. In some embodiments, the reactor comprises a regenerative pyrolysis reactor apparatus and in other embodiments it includes a reverse flow regenerative reactor apparatus. In other aspects, this invention includes a method for pyrolyzing a hydrocarbon feedstock using a pyrolysis reactor system comprising the step of providing in a heated region of a pyrolysis reactor system for pyrolyzing a hydrocarbon feedstock, apparatus comprising the above refractory material. 119-. (canceled)21. The method of claim 20 , wherein the refractory material remains in oxide form when exposed to a gas having a carbon partial pressure of 10bar claim 20 , an oxygen partial pressure of 10bar claim 20 , at a temperature of 2050° C.22. The method of claim 20 , wherein the refractory material remains in the oxide form when exposed to a gas having a carbon partial pressure of 10bar claim 20 , an oxygen partial pressure of 10bar claim 20 , and at a temperature over the full range of from 1800° C. to 2100° C.23. The method of claim 20 , wherein the refractory material exhibits a cubic crystalline structure when exposed to a temperature in the range of from 1250° C. to 2200° C.24. The method of wherein the refractory material ...

Pyrolysis Reactor Materials and Methods

In one aspect, the invention includes a reactor apparatus for pyrolyzing a hydrocarbon feedstock, the apparatus including: a reactor component comprising a refractory material in oxide form, the refractory material having a melting point of at least 2060° C. and which remains in oxide form when exposed to a gas having an oxygen partial pressure of 10bar, a carbon partial pressure above the carbon partial pressure of the zirconium carbide and zirconium oxide phase transition at the same temperature, and at temperatures below the temperature of the zirconium triple point at the oxygen partial pressure of 10bar; and ii) when exposed to a gas having an oxygen partial pressure of 10bar and at temperatures above the zirconium triple point at the oxygen partial pressure of 10bar. In some embodiments, the reactor comprises a regenerative pyrolysis reactor apparatus and in other embodiments it includes a reverse flow regenerative reactor apparatus. In other aspects, this invention includes a method for pyrolyzing a hydrocarbon feedstock using a pyrolysis reactor system comprising the step of providing in a heated region of a pyrolysis reactor system for pyrolyzing a hydrocarbon feedstock, apparatus comprising the above refractory material. 119-. (canceled)21. The method of claim 20 , wherein the refractory material remains in oxide form when exposed to a gas having a carbon partial pressure of 10bar claim 20 , an oxygen partial pressure of 10bar claim 20 , at a temperature of 2050° C.22. The method of claim 20 , wherein the refractory material remains in the oxide form when exposed to a gas having a carbon partial pressure of 10bar claim 20 , an oxygen partial pressure of 10bar claim 20 , and at a temperature over the full range of from 1800° C. to 2100° C.23. The method of claim 20 , wherein the refractory material exhibits a cubic crystalline structure when exposed to a temperature in the range of from 1250° C. to 2200° C.24. The method of wherein the refractory material ...

Transalkylation of Heavy Aromatic Hydrocarbon Feedstocks

A process for producing xylene comprises contacting a first feed comprising C 9+ aromatic hydrocarbons, at least one C 6 -C 7 aromatic hydrocarbon and hydrogen with a first catalyst composition to dealkylate at least part of the C 9+ aromatic hydrocarbons containing C 2+ alkyl groups and to saturate the resulting C 2+ olefins to produce a second feed. The second feed is then contacted with a second catalyst composition under conditions effective to transalkylate at least part of the C 9+ aromatic hydrocarbons with at least part of the C 6 -C 7 aromatic hydrocarbon to produce a first product comprising xylene. Each of the first and second catalyst compositions is substantially free of amorphous alumina.

Methods for applying solution catalysts to reactor surfaces

A method for treating at least one interior surface (for example, a bed wall) of a fluidized bed polymerization reactor system, including by applying a solution catalyst (preferably at least substantially uniformly and in liquid form) to each surface, and optionally (where a catalyst component of the solution catalyst comprises at least one chromium containing compound) oxidizing at least some of the applied chromium containing compound in a controlled manner.

Process for feeding ethylene to polymerization reactors

A process for feeding ethylene into a polymerization system includes providing a low-pressure ethylene stream, one or more low-pressure C 3 to C 20 monomer streams, an optional low-pressure inert solvent/diluent stream, and one or more reactors; metering the low-pressure ethylene stream, the one or more low-pressure C 3 to C 20 monomer streams, and the optional low-pressure inert solvent/diluent stream; blending the metered low-pressure ethylene stream, the metered one or more low-pressure C 3 to C 20 monomer streams, and the metered low-pressure optional inert solvent/diluent stream to form an ethylene-carrying low-pressure blended liquid feed stream; pressurizing the ethylene-carrying low-pressure blended liquid feed stream to the polymerization system pressure with one or more high-pressure pumps to thrm an ethylene-carrying high-pressure blended reactor feed stream; and feeding the ethylene-carrying high-pressure blended reactor feed stream to the one or more reactors.

Gas phase polymerization and distributor plate passivation treatment

Apparatus and methods for gas phase polymerization are provided. The method can include polymerizing one or more olefins at gas phase conditions in a reactor comprising one or more process exposed surfaces in the presence of a catalyst system; and treating at least a portion of the one or more process exposed surfaces prior to injecting the catalyst system to reduce the number of surface hydroxyls or access of the catalyst system to the surface hydroxyls on the process exposed surfaces.

Methods and devices for polymerization

A method of treating a gas phase fluidized bed reactor and a method of polymerizing olefins in a gas phase fluidized bed reactor in the presence of a catalyst prone to cause sheeting by introducing a chromium-containing compound into the reactor and forming a high molecular weight polymer coating on the walls of the reactor. Furthermore, a device for and method of introducing the chromium-containing compound into the fluidized bed reactor at a plurality of locations in proximity to a lower section of a bed section wall of the fluidized bed reactor, and forming a high molecular weight polymer coating on the bed section wall.

Method and apparatus for managing for hydrogen content through the conversion of hydrocarbons into olefins

An apparatus and method are provided for processing hydrocarbon feeds. The method enhances the conversion of hydrocarbon feeds into conversion products, such as ethylene and propylene. In particular, the present techniques combine a first hydrocarbon feed with a second hydrocarbon feed and a hydrogen (¾) containing stream to manage the hydrogen content of the feed provided to a pyrolysis reactor. The mixture is then exposed to high-severity operating conditions in a pyrolysis reactor and further processing into desired olefins.

Method and apparatus for converting hydrocarbons into olefins

An apparatus and method are provided for processing hydrocarbon feeds. The method enhances the conversion of hydrocarbon feeds into conversion products, such as ethylene. In particular, the present techniques utilize a high-severity thermal pyrolysis reactor that exposes a feed at a peak pyrolysis gas temperature ≥ 1540 °C to produce a reactor product comprising ethylene and acetylene and has a C 3 + to acetylene weight ratio ≤ 0.5. Then, the method separates a product comprising tars and/or solids from at least a portion of the reactor product and converts at least a portion of the remaining reactor product into a conversion product, such as ethylene.

Gas Phase Polymerization And Distributor Plate Passivation Treatment

Apparatus and methods for gas phase polymerization are provided. The method can include polymerizing one or more olefins at gas phase conditions in a reactor comprising one or more process exposed surfaces in the presence of a catalyst system; and treating at least a portion of the one or more process exposed surfaces prior to injecting the catalyst system to reduce the number of surface hydroxyls or access of the catalyst system to the surface hydroxyls on the process exposed surfaces.

Methods and devices for polymerization

A method of treating a gas phase fluidized bed reactor and a method of polymerizing olefins in a gas phase fluidized bed reactor in the presence of a catalyst prone to cause sheeting by introducing a chromium-containing compound into the reactor and forming a high molecular weight polymer coating on the walls of the reactor. Furthermore, a device for and method of introducing the chromium-containing compound into the fluidized bed reactor at a plurality of locations in proximity to a lower section of a bed section wall of the fluidized bed reactor, and forming a high molecular weight polymer coating on the bed section wall.

Methods for applying solution catalysts to reactor surfaces

A method for treating at least one interior surface (for example, a bed wall) of a fluidized bed polymerization reactor system, including by applying a solution catalyst (preferably at least substantially uniformly and in liquid form) to each surface, and optionally (where a catalyst component of the solution catalyst comprises at least one chromium containing compound) oxidizing at least some of the applied chromium containing compound in a controlled manner.

Methods and devices for polymerization

A method of treating a gas phase fluidized bed reactor and a method of polymerizing olefins in a gas phase fluidized bed reactor in the presence of a catalyst prone to cause sheeting by introducing a chromium-containing compound into the reactor and forming a high molecular weight polymer coating on the walls of the reactor. Furthermore, a device for and method of introducing the chromium-containing compound into the fluidized bed reactor at a plurality of locations in proximity to a lower section of a bed section wall of the fluidized bed reactor, and forming a high molecular weight polymer coating on the bed section wall.

Methods for applying solution catalysts to reactor surfaces

A method for treating at least one interior surface (for example, a bed wall) of a fluidized bed polymerization reactor system, including by applying a solution catalyst (preferably at least substantially uniformly and in liquid form) to each surface, and optionally (where a catalyst component of the solution catalyst comprises at least one chromium containing compound) oxidizing at least some of the applied chromium containing compound in a controlled manner.

Methods for applying solution catalysts to reactor surfaces

A method for treating at least one interior surface (for example, a bed wall) of a fluidized bed polymerization reactor system, including by applying a solution catalyst (preferably at least substantially uniformly and in liquid form) to each surface, and optionally (where a catalyst component of the solution catalyst comprises at least one chromium containing compound) oxidizing at least some of the applied chromium containing compound in a controlled manner.

Methods and devices for polymerization

A method of treating a gas phase fluidized bed reactor and a method of polymerizing olefins in a gas phase fluidized bed reactor in the presence of a catalyst prone to cause sheeting by introducing a chromium-containing compound into the reactor and forming a high molecular weight polymer coating on the walls of the reactor. Furthermore, a device for and method of introducing the chromium-containing compound into the fluidized bed reactor at a plurality of locations in proximity to a lower section of a bed section wall of the fluidized bed reactor, and forming a high molecular weight polymer coating on the bed section wall.

Hydrocarbon formation process and catalyst useful therein

Hydrocarbon conversion process and catalyst useful therein.

Hydrokarbon omdannelsesprosess og katalysator som er nyttig for denne

Gas phase polymerization and disbributor plate passivation treatment

Apparatus and methods for gas phase polymerization are provided. The method can include polymerizing one or more olefins at gas phase conditions in a reactor comprising one or more process exposed surfaces in the presence of a catalyst system; and treating at least a portion of the one or more process exposed surfaces prior to injecting the catalyst system to reduce the number of surface hydroxyls or access of the catalyst system to the surface hydroxyls on the process exposed surfaces.

Iron, cobalt and/or nickel containing ALPO bound SAPO molecular sieve catalyst for producing olefins

An aluminophosphate bound silicoaluminophosphate catalyst contains iron, cobalt and/or nickel is useful in a method of making a product including an olefin from a feedstock containing an oxygenate. The method includes contacting an oxygenate feedstock with the catalyst, which is an aluminophosphate bound silicoaluminophosphate catalyst containing iron, cobalt and/or nickel and which does not contain a significant amount of amorphous binder, in its activated state under conditions effective to produce an olefin product.

Methods and devices for polymerization

A method of treating a gas phase fluidized bed reactor and a method of polymerizing olefins in a gas phase fluidized bed reactor in the presence of a catalyst prone to cause sheeting by introducing a chromium-containing compound into the reactor and forming a high molecular weight polymer coating on the walls of the reactor. Furthermore, a device for and method of introducing the chromium-containing compound into the fluidized bed reactor at a plurality of locations in proximity to a lower section of a bed section wall of the fluidized bed reactor, and forming a high molecular weight polymer coating on the bed section wall.

Methods for applying solution catalysts to reactor surfaces

Process for producing catalysts with reduced hydrogenation activity and use thereof

A process for controlling the hydrogenation activity of a catalyst comprised of a crystalline molecular sieve and at least one hydrogenation metal selected from the group consisting of a Group VIIB metal, a Group VIII metal, and mixtures thereof. The process is carried out by contacting the catalyst with hydrogen under sufficient conditions of temperature and pressure and for sufficient time to reduce the hydrogenolysis activity of the catalyst. The catalyst prepared by the process finds application in the catalytic conversion of organic compounds, such as ethylbenzene dealkylation, xylenes isomerization, and the transalkylation of polyalkylaromatic hydrocarbons.

Hydrocarbon conversion process and catalyst useful therein

Method of Producing a Polymeric Product in a Fluid Bed Polymerization Reactor System

Methods for applying solution catalysts to reactor surfaces

A method for treating at least one interior surface (for example, a bed wall) of a fluidized bed polymerization reactor system, including by applying a solution catalyst (preferably at least substantially uniformly and in liquid form) to each surface, and optionally (where a catalyst component of the solution catalyst comprises at least one chromium containing compound) oxidizing at least some of the applied chromium containing compound in a controlled manner.

Methods for applying solution catalysts to reactor surfaces

A method for treating at least one interior surface (for example, a bed wall) of a fluidized bed polymerization reactor system, including by applying a solution catalyst (preferably at least substantially uniformly and in liquid form) to each surface, and optionally (where a catalyst component of the solution catalyst comprises at least one chromium containing compound) oxidizing at least some of the applied chromium containing compound in a controlled manner.

METHODS FOR APPLYING CATALYZERS IN REACTOR SURFACE SOLUTION.

Gas phase polymerization and disbributor plate passivation treatment

Apparatus and methods for gas phase polymerization are provided. The method can include polymerizing one or more olefins at gas phase conditions in a reactor comprising one or more process exposed surfaces in the presence of a catalyst system; and treating at least a portion of the one or more process exposed surfaces prior to injecting the catalyst system to reduce the number of surface hydroxyls or access of the catalyst system to the surface hydroxyls on the process exposed surfaces.

Ethylbenzene conversion catalyst and process

An ethylbenzene conversion catalyst is described which comprises a molecular sieve and a hydrogenation metal, wherein the catalyst exhibits a benzene hydrogenation activity at 100° C. of less than about 100 and a metal dispersion, as measured by hydrogen chemisorption, greater than 0.4 and wherein the molecular sieve is steamed to an alpha value of less than 400 prior to incorporation of the palladium with the molecular sieve.

Methylation of toluene to para-xylene

A process is provided for the production of paraxylene by the methylation of toluene in the presence of a zeolite bound zeolite catalyst. The catalyst comprises first zeolite crystals which are bound together by second zeolite crystals. When used to methylate toluene to para-xylene, the zeolite bound zeolite catalyst has a para-xylene selectivity greater than thermodynamic equilibrium. This selectivity can be enhanced by selectivating the catalyst.

Aromatic conversion processes and zeolite catalyst useful therein

Synthesis of large crystal zeolites

Large crystal zeolites are prepared by heating a zeolite synthesis mixture under agitation to a temperature equal to or less than the effective nucleation temperature of the zeolite synthesis mixture and thereafter the zeolite synthesis mixture is heated without agitation to a temperature equal to or greater than the effective nucleation temperature of the zeolite synthesis mixture.

Zeolite catalyst and its use in hydrocarbon conversion

There is provided a zeolite bound zeolite catalyst which can be tailored to optimize its performance and a process for converting hydrocarbons utilizing the zeolite bound zeolite catalyst. The zeolite bound zeolite catalyst comprises a first zeolite and a binder comprising a second zeolite. The structure type of the second zeolite is different from the structure type of the first zeolite. The zeolite bound zeolite catalyst finds particular application in hydrocarbon conversion process, e.g., catalytic cracking, alkylation, disproportionation of toluene, isomerization, and transalkylation reactions.

Metal-containing macrostructures of porous inorganic oxide, preparation thereof, and use

There is provided a catalyst containing porous macrostructures comprised of: (a) a three-dimensional network of particles of porous inorganic material; and, (b) at least one metal. The particles of the at least one macrostructur e occupy less than 75 % of the total volume of the at least one macrostructure and are jointed together to form a three-dimensional interconnected network. The three-dimensional interconnected network will usually be comprised of pores having diameters greater than about 20 .ANG.. The macrostructures can be made by forming an admixture containing a porous organic ion exchanger and a synthesis mixture capable of forming the porous inorganic material and the a t least one metal; converting the synthesis mixture to the porous inorganic material; and removing the porous organic ion exchanger from the organic material. The metal-containing macrostructures find application in hydrocarb on conversion and in the reduction of emissions.

Method of improving metal-impregnated catalyst performance

A method of reducing the amount of carbon monoxide present during the metal reduction step of start-up, thus, maintaining metal dispersion and improving the metal reduction and catalyst yields. Carbon monoxide formation is minimized during the start-up procedure and during the initial catalyst dryout phase in a hydrogen-containing atmosphere, gas is purged from the reactor system, either continuously at constant pressure or by a series of pressure/depressure cycles, to remove carbon monoxide. The purging is conducted at temperatures of about 30- 500?C and pressures of about -90-5,000 kPa(g) (-0.9-50 bar(g)). In this temperature range, carbon monoxide absorbed to the surface of the metal will desorb into the hydrogen-containing atmosphere and can be removed from the system along with carbon monoxide present in the atmosphere through the purging.

Process for isomerization of alkylaromatic hydrocarbons

A process for isomerizating a feed containing alkylaromatic hydrocarbons, e.g., monocyclic alkylaromatic hydrocarbons and/or bicyclic alkylaromatic hydrocarbons. The process is carried out by contacting the feed under conversion conditions with a zeolite bound zeolite catalyst which comprises first crystals of an intermediate pore size first zeolite and a binder which comprises second crystals of a second zeolite. The process finds particular application in isomerizing a feed containing ethylbenzene and less than equilibrium amounts of xylenes with ethylbenzene and can produce a product containing above equilibrium quantities of para-xylene with low aromatics ring loss and xylene loss.

Method and apparatus for managing hydrogen content through the conversion of hydrocarbons into olefins

An apparatus and method are provided for processing hydrocarbon feeds. The method enhances the conversion of hydrocarbon feeds into conversion products, such as ethylene and propylene. In particular, the present techniques combine a first hydrocarbon feed with a second hydrocarbon feed and a hydrogen (H 2 ) containing stream to manage the hydrogen content of the feed provided to a pyrolysis reactor. The mixture is then exposed to high-severity operating conditions in a pyrolysis reactor and further processing into desired olefins.

Manufacture of xylenes by reactive distillation of reformate

Pyrolysis reactor materials and methods

In one aspect, the invention includes a reactor apparatus for pyrolyzing a hydrocarbon feedstock, the apparatus including: a reactor component comprising a refractory material in oxide form, the refractory material having a melting point of at least 20600C and which remains in oxide form when exposed to a gas having an oxygen partial pressure of 10" 15 bar, a carbon partial pressure above the carbon partial pressure of the zirconium carbide and zirconium oxide phase transition at the same temperature, and at temperatures below the temperature of the zirconium triple point at the oxygen partial pressure of 10" 15 bar; and ii) when exposed to a gas having an oxygen partial pressure of 10"15 bar and at temperatures above the zirconium triple point at the oxygen partial pressure of 10"15 bar. In some embodiments, the reactor comprises a regenerative pyrolysis reactor apparatus and in other embodiments it includes a reverse flow regenerative reactor apparatus. In other aspects, this invention includes a method for pyrolyzing a hydrocarbon feedstock using a pyrolysis reactor system comprising the step of providing in a heated region of a pyrolysis reactor system for pyrolyzing a hydrocarbon feedstock, apparatus comprising the above refractory material.

Process for producing aromatic compounds from aliphatic hydrocarbons

Synthesis of large crystal zeolites

Zeolite catalyst and use for hydrocarbon conversion

There is provided a zeolite bound zeolite catalyst which can be tailored to optimize its performance and a process for converting hydrocarbons utilizing the zeolite bound zeolite catalyst. The zeolite bound zeolite catalyst comprises a first zeolite and a binder comprising a second zeolite. The structure type of the second zeolite is different from the structure type of the first zeolite. The zeolite bound zeolite finds particular application in hydrocarbon conversion process, e.g., catalytic cracking, alkylation, disproportional of toluene, isomerization, and transalkylation reactions.

Zeolite catalyst and its use in hydrocarbon conversion

There is provided a zeolite bound zeolite catalyst which can be tailored to optimize its performance and a process for converting hydrocarbons utilizing the zeolite bound zeolite catalyst. The zeolite bound zeolite catalyst comprises a first zeolite and a binder comprising a second zeolite. The structure type of the second zeolite is different from the structure type of the first zeolite. The zeolite bound zeolite catalyst finds particular application in hydrocarbon conversion process, e.g., catalytic cracking, alkylation, disproportionation of toluene, isomerization, and transalkylation reactions.

Reforming process for manufacture of para-xylene

A process for selectively producing para-xylene from a feedstock enriched in C 8 isoalkanes and/or isoalkenes is disclosed. The feed is contacted with Group VIII metal loaded molecular sieve catalyst of low acidity under dehydrocyclization conditions wherein the molecular sieve has a channel size ranging from about 5-8 Angstroms and a 10 to 12 membered ring structure containing at least two elements selected from the group consisting of Si, Al, P, Ge, Ga and Ti.

Hydrocarbon conversion process

The invention relates to processes for converting a mixture of hydrocarbon and sulfur- containing molecules such as mercaptan into products comprising acetylene, ethylene, and hydrogen sulfide, to processes utilizing the acetylene and ethylene resulting from the conversion, and to equipment useful for such processes.

Preparation of high silica zeolites bound by zeolite and use thereof

Catalyst comprising a zeolite partially coated with a second zeolite, its use for hydrocarbon conversion

There is provided a coated zeolite catalyst in which the accessiblility of the acid sites on the external surfaces of the zeolite is controlled and a process for converting hydrocarbons utilizing the coated zeolite catalyst. The zeolite catalyst comprises core crystals of a first zeolite and a discontinuous layer of smaller size second crystals of a second zeolite which cover at least a portion of the external surface of the first crystals. The coated zeolite catalyst finds particular application in hydrocarbon conversion processes where catalyst activity in combination with zoelite structure are important for reaction selectivity, e.g., catalytic cracking, alkylation, disproportional of toluene, isomerization, and transalkylation reactions.

Zeolite catalyst and its use in hydrocarbon conversion

There is provided a zeolite bound zeolite catalyst which can be tailored to optimize its performance and a process for converting hydrocarbons utilizing the zeolite bound zeolite catalyst. The zeolite bound zeolite catalyst comprises a first zeolite and a binder comprising a second zeolite. The structure type of the second zeolite is different from the structure type of the first zeolite. The zeolite bound zeolite catalyst finds particular application in hydrocarbon conversion process, e.g., catalytic cracking, alkylation, disproportionation of toluene, isomerization, and transalkylation reactions.

Pyrolysis reactor materials and methods

In one aspect, the invention includes a reactor apparatus for pyrolyzing a hydrocarbon feedstock, the apparatus including: a reactor component comprising a refractory material in oxide form, the refractory material having a melting point of at least 20600C and which remains in oxide form when exposed to a gas having an oxygen partial pressure of 10"15 bar, a carbon partial pressure above the carbon partial pressure of the zirconium carbide and zirconium oxide phase transition at the same temperature, and at temperatures below the temperature of the zirconium triple point at the oxygen partial pressure of 10"15 bar; and ii) when exposed to a gas having an oxygen partial pressure of 10"15 bar and at temperatures above the zirconium triple point at the oxygen partial pressure of 10"15 bar. In some embodiments, the reactor comprises a regenerative pyrolysis reactor apparatus and in other embodiments it includes a reverse flow regenerative reactor apparatus. In other aspects, this invention includes a method for pyrolyzing a hydrocarbon feedstock using a pyrolysis reactor system comprising the step of providing in a heated region of a pyrolysis reactor system for pyrolyzing a hydrocarbon feedstock, apparatus comprising the above refractory material.

Reactor components

The present disclosure relates to reactor components and their use, e.g., in regenerative reactors. A process and apparatus for utilizing different wetted areas along the flow path of a fluid in a pyrolysis reactor, e.g., a thermally regenerating reactor, such as a regenerative, reverse-flow reactor, is described.

Pyrolysis reactor materials and methods

In one aspect, the invention includes a reactor apparatus for pyrolyzing a hydrocarbon feedstock, the apparatus including: a reactor component comprising a refractory material in oxide form, the refractory material having a melting point of at least 20600C and which remains in oxide form when exposed to a gas having an oxygen partial pressure of 10" 15 bar, a carbon partial pressure above the carbon partial pressure of the zirconium carbide and zirconium oxide phase transition at the same temperature, and at temperatures below the temperature of the zirconium triple point at the oxygen partial pressure of 10" 15 bar; and ii) when exposed to a gas having an oxygen partial pressure of 10"15 bar and at temperatures above the zirconium triple point at the oxygen partial pressure of 10"15 bar. In some embodiments, the reactor comprises a regenerative pyrolysis reactor apparatus and in other embodiments it includes a reverse flow regenerative reactor apparatus. In other aspects, this invention includes a method for pyrolyzing a hydrocarbon feedstock using a pyrolysis reactor system comprising the step of providing in a heated region of a pyrolysis reactor system for pyrolyzing a hydrocarbon feedstock, apparatus comprising the above refractory material.

Methylation of toluene to para-xylene

Methylation of toluene to para-xylene

A process is provided for the production of paraxylene by the methylation of toluene in the presence of a zeolite bound zeolite catalyst. The catalyst comprises first zeolite crystals which are bound together by second zeolite crystals. When used to methylate toluene to para-xylene, the zeolite bound zeolite catalyst has a para-xylene selectivity greater than thermodynamic equilibrium. This selectivity can be enhanced by selectivating the catalyst.

PREPARATION OF ELEVATED ZEOLITES CONTAINED IN SILICE THAT ARE UNITED BY ZEOLITE AND ITS USE.

Un procedimiento para la preparación de zeolita de elevado contenido en sílice unida por zeolita que no contiene cantidades significativas de aglomerante no zeolítico y que contiene cristales de zeolita de elevado contenido en sílice y cristales de aglomerante de zeolita, comprendiendo dicho procedimiento: (a) proporcionar una mezcla de zeolita de elevado contenido en sílice en la forma de hidrógeno, agua, y sílice para proporcionar una masa capaz de ser extruída; (b) extruir dicha masa capaz de ser extruída para formar un artículo extruído de zeolita de elevado contenido en sílice unida por sílice; y (c) convertir la sílice del aglomerante de dicho artículo extruído en un aglomerante de zeolita.

Aromatic conversion processes and zeolite catalyst useful therein

A process is provided for the alkylation, transalkylation, or isomerization of aromatic hydrocarbons. The process comprises contacting aromatic hydrocarbons under conversion conditions with a zeolite bound zeolite catalyst. The zeolite bound zeolite catalyst comprises first crystals of a first large pore zeolite which are bound together by second crystals of a second zeolite.

Process for the production of aromatic compounds from aliphatic hydrocarbons

Methods and devices for polymerization

Pyrolysis reactor materials and methods

In one aspect, the invention includes a reactor apparatus for pyrolyzing a hydrocarbon feedstock, the apparatus including: a reactor component comprising a refractory material in oxide form, the refractory material having a melting point of at least 20600C and which remains in oxide form when exposed to a gas having an oxygen partial pressure of 10"15 bar, a carbon partial pressure above the carbon partial pressure of the zirconium carbide and zirconium oxide phase transition at the same temperature, and at temperatures below the temperature of the zirconium triple point at the oxygen partial pressure of 10"15 bar; and ii) when exposed to a gas having an oxygen partial pressure of 10"15 bar and at temperatures above the zirconium triple point at the oxygen partial pressure of 10"15 bar. In some embodiments, the reactor comprises a regenerative pyrolysis reactor apparatus and in other embodiments it includes a reverse flow regenerative reactor apparatus. In other aspects, this invention includes a method for pyrolyzing a hydrocarbon feedstock using a pyrolysis reactor system comprising the step of providing in a heated region of a pyrolysis reactor system for pyrolyzing a hydrocarbon feedstock, apparatus comprising the above refractory material.

Metallenthaltende makrostrukturen von porösen anorganischen partikeln, deren herstellung und anwendung

Kohlenwasserstoffumwandlungsverfahren und hierbei anwendbarer katalysator

Verfahren zur herstellung von durch zeolith gebundenen zeolithen mit hohem sio2-gehalt und ihre verwendung

Catalyst conversion of hydrocarbons and its

３，４’與４，４’－二甲基聯苯異構物之製造與用途

一種用於製造3,4’和/或4,4’二甲基取代的聯苯化合物之方法，令包含甲苯之進料與氫在氫烷化反應觸媒存在下，在有效製造包含(甲基環己基)甲苯之氫烷化反應產物的條件下接觸。在脫氫反應觸媒存在下，在有效製造包含經二甲基取代的聯苯異構物之混合物之脫氫反應產物的條件下，令氫烷化反應產物的至少一部分脫氫。之後，將脫氫反應產物至少分離成第一流和至少一個第二流，其中第一流包含以第一流重量計為至少50%之3,4’和4,4’-二甲基聯苯異構物，第二流包含一或更多種2,x’(其中x’是2’，3’或4’)和3,3’-二甲基聯苯異構物。

Hydrocarbon conversion process

The invention relates to processes for converting a mixture of hydrocarbon and sulfur-containing molecules such as mercaptan into products comprising acetylene, ethylene, and hydrogen sulfide, to processes utilizing the acetylene and ethylene resulting from the conversion, and to equipment useful for such processes.

Method of improving metal-impregnated catalyst performance

A method of reducing the amount of carbon monoxide present during the metal reduction step of start-up, thus, maintaining metal dispersion and improving the metal reduction and catalyst yields. Carbon monoxide formation is minimized during the start-up procedure and during the initial catalyst dryout phase in a hydrogen-containing atmosphere, gas is purged from the reactor system, either continuously at constant pressure or by a series of pressure/depressure cycles, to remove carbon monoxide. The purging is conducted at temperatures of about 30-500° C. and pressures of about −90-5,000 kPa(g) (−0.9-50 bar(g)). In this temperature range, carbon monoxide absorbed to the surface of the metal will desorb into the hydrogen-containing atmosphere and can be removed from the system along with carbon monoxide present in the atmosphere through the purging.

Activation of dehydrogenation catalysts

In a process for dehydrogenating cyclohexylbenzene and/or alkyl-substituted cyclohexylbenzene compounds, a dehydrogenation catalyst comprising at least one Group 10 metal compound on a support is heated in the presence of hydrogen from a first temperature from 0° C. to 200° C. to a second, higher temperature from 60° C. to 500° C. at a ramp rate no more than 100° C./hour. The dehydrogenation catalyst is contacted with hydrogen at the second temperature for a time from 3 to 300 hours to produce an activated dehydrogenation catalyst. A feed comprising cyclohexylbenzene and/or an alkyl-substituted cyclohexylbenzene compound is then contacted with hydrogen in the presence of the activated dehydrogenation catalyst under conditions effective to produce a dehydrogenation reaction product comprising biphenyl and/or an alkyl-substituted biphenyl compound.

Method and apparatus for converting hydrocarbons into olefins

An apparatus and method are provided for processing hydrocarbon feeds. The method enhances the conversion of hydrocarbon feeds into conversion products, such as ethylene. In particular, the present techniques utilize a high-severity thermal pyrolysis reactor that exposes a feed at a peak pyrolysis gas temperature ≧1540° C. to produce a reactor product comprising ethylene and acetylene and has a C 3 + to acetylene weight ratio ≦0.5. Then, the method separates a product comprising tars and/or solids from at least a portion of the reactor product and converts at least a portion of the remaining reactor product into a conversion product, such as ethylene.

Hydrocarbon conversion process

The invention relates to processes for converting a mixture of hydrocarbon and sulfur-containing molecules such as mercaptans into products comprising acetylene, ethylene, and hydrogen sulfide, to processes utilizing the acetylene and ethylene resulting from the conversion, and to equipment useful for such processes.

Hydrocarbon conversion process

The invention relates to processes for converting a mixture of hydrocarbon and sulfur-containing molecules such as mercaptan into products comprising acetylene, ethylene, and hydrogen sulfide, to processes utilizing the acetylene and ethylene resulting from the conversion, and to equipment useful for such processes.

Hydrocarbon conversion process

The invention relates to processes for converting a mixture of hydrocarbon and oxygenate into products containing acetylene and carbon monoxide. The invention also relates to utilizing at least a portion of the acetylene and carbon monoxide for producing xylenes such as p-xylene, utilizing at least a portion of xylenes for producing polymeric fibers, and to equipment useful for these processes.

Production and use of 3,4' and 4,4'-dimethylbiphenyl isomers

In a process for producing 3,4′ and/or 4,4′ dimethyl-substituted biphenyl compounds, a feed comprising toluene is contacted with hydrogen in the presence of a hydroalkylation catalyst under conditions effective to produce a hydroalkylation reaction product comprising (methylcyclohexyl)toluenes. At least part of the hydroalkylation reaction product is dehydrogenated in the presence of a dehydrogenation catalyst under conditions effective to produce a dehydrogenation reaction product comprising a mixture of dimethyl-substituted biphenyl isomers. The dehydrogenation reaction product is then separated into at least a first stream containing at least 50% of 3,4′ and 4,4′ dimethylbiphenyl isomers by weight of the first stream and at least one second stream comprising one or more 2,x′ (where x′ is 2′, 3′, or 4′) and 3,3′ dimethylbiphenyl isomers.

Pyrolysis reactor materials and methods

In one aspect, the invention includes a reactor apparatus for pyrolyzing a hydrocarbon feedstock, the apparatus including: a reactor component comprising a refractory material in oxide form, the refractory material having a melting point of at least 2060° C. and which remains in oxide form when exposed to a gas having an oxygen partial pressure of 10 −15 bar, a carbon partial pressure above the carbon partial pressure of the zirconium carbide and zirconium oxide phase transition at the same temperature, and at temperatures below the temperature of the zirconium triple point at the oxygen partial pressure of 10 −15 bar; and ii) when exposed to a gas having an oxygen partial pressure of 10 −15 bar and at temperatures above the zirconium triple point at the oxygen partial pressure of 10 −15 bar. In some embodiments, the reactor comprises a regenerative pyrolysis reactor apparatus and in other embodiments it includes a reverse flow regenerative reactor apparatus. In other aspects, this invention includes a method for pyrolyzing a hydrocarbon feedstock using a pyrolysis reactor system comprising the step of providing in a heated region of a pyrolysis reactor system for pyrolyzing a hydrocarbon feedstock, apparatus comprising the above refractory material.