Solid terephthalic acid composition

A solid terephthalic acid composition and a process for producing terephthalic acid from para-xylene are provided. The process comprises forming a mixture comprising the para-xylene, a solvent, a bromine source, and a catalyst; and oxidizing the para-xylene by contacting the mixture with an oxidizing agent at oxidizing conditions to produce a solid oxidation product comprising terephthalic acid, para-toluic acid, 4-carboxybenzaldehyde. The solvent comprises a carboxylic acid having from 1 to 7 carbon atoms and an dialkyl imidazolium ionic liquid; and the catalyst comprises at least one of cobalt, titanium, manganese, chromium, copper, nickel, vanadium, iron, molybdenum, tin, cerium, and zirconium. The solid terephthalic acid composition comprises, less than about 4,000 ppm-wt 4-carboxybenzaldehyde content, and more than about 2,000 ppm-wt a para-toluic acid.

Process for producing terephthalic acid

The invention relates to a solid terephthalic acid composition and a process for producing terephthalic acid from para-xylene. The process comprises forming a mixture comprising the para-xylene, a solvent, a bromine source, and a catalyst; and oxidizing the para-xylene by contacting the mixture with an oxidizing agent at oxidizing conditions to produce a solid oxidation product comprising terephthalic acid, para-toluic acid, 4-carboxybenzaldehyde. The solvent comprises a carboxylic acid having from 1 to 7 carbon atoms and an dialkyl imidazolium ionic liquid; and the catalyst comprises at least one of cobalt, titanium, manganese, chromium, copper, nickel, vanadium, iron, molybdenum, tin, cerium, and zirconium. The solid terephthalic acid composition comprises, less than about 4,000 ppm-wt 4-carboxybenzaldehyde content, and more than about 2,000 ppm-wt a para-toluic acid.

Process for removing metals from vacuum gas oil

A process for removing a metal from a vacuum gas oil feed includes contacting the vacuum gas oil feed comprising the metal with a VGO-immiscible ionic liquid to produce a vacuum gas oil and VGO-immiscible ionic liquid mixture, and separating the mixture to produce a vacuum gas oil effluent having a reduced metal content relative to the vacuum gas oil feed.

Process for oxidizing alkyl aromatic compounds

A process and a mixture for oxidizing an alkyl-aromatic compound are provided. The method comprises forming a mixture comprising the alkyl-aromatic compound, a solvent, a bromine source, and a catalyst; and contacting the mixture with an oxidizing agent at oxidizing conditions to produce an oxidation product comprising at least one of an aromatic aldehyde, an aromatic alcohol, an aromatic ketone, and an aromatic carboxylic acid. The solvent comprises a carboxylic acid having from 1 to 7 carbon atoms and an ionic liquid selected from the group consisting of an imidazolium ionic liquid, a pyridinium ionic liquid, a phosphonium ionic liquid, a tetra alkyl ammonium ionic liquid, and combinations thereof. The catalyst comprises at least one of cobalt, titanium, manganese, chromium, copper, nickel, vanadium, iron, molybdenum, tin, cerium, and zirconium.

Mixtures used in oxidizing alkyl aromatic compounds

A process and a mixture for oxidizing an alkyl-aromatic compound are provided. The method comprises forming a mixture comprising the alkyl-aromatic compound, a solvent, a bromine source, and a catalyst; and contacting the mixture with an oxidizing agent at oxidizing conditions to produce an oxidation product comprising at least one of an aromatic aldehyde, an aromatic alcohol, an aromatic ketone, and an aromatic carboxylic acid. The solvent comprises a carboxylic acid having from 1 to 7 carbon atoms and an ionic liquid selected from the group consisting of an imidazolium ionic liquid, a pyridinium ionic liquid, a phosphonium ionic liquid, a tetra alkyl ammonium ionic liquid, and combinations thereof. The catalyst comprises at least one of cobalt, titanium, manganese, chromium, copper, nickel, vanadium, iron, molybdenum, tin, cerium, and zirconium.

PROCESS FOR PRODUCING TEREPHTHALIC ACID

A solid terephthalic acid composition and a process for producing terephthalic acid from para-xylene. The process comprises forming a mixture comprising the para-xylene, a solvent, a bromine source, and a catalyst; and oxidizing the para-xylene by contacting the mixture with an oxidizing agent at oxidizing conditions to produce a solid oxidation product comprising terephthalic acid, para-toluic acid, 4-carboxybenzaldehyde. The solvent comprises a carboxylic acid having from 1 to 7 carbon atoms and an dialkyl imidazolium ionic liquid; and the catalyst comprises at least one of cobalt, titanium, manganese, chromium, copper, nickel, vanadium, iron, molybdenum, tin, cerium, and zirconium. The solid terephthalic acid composition comprises, less than about 4,000 ppm-wt 4-carboxybenzaldehyde content, and more than about 2,000 ppm-wt a para-toluic acid. 1. A process for producing terephthalic acid from para-xylene , the process comprising:forming a mixture comprising the para-xylene, a solvent, a bromine source, a catalyst and optionally ammonium acetate; andoxidizing the para-xylene by contacting the mixture with an oxidizing agent at oxidizing conditions to produce a solid oxidation product, the solid oxidation product comprising terephthalic acid, 4-carboxybenzaldehyde, and para-toluic acid;wherein the solvent comprises a carboxylic acid having from 1 to 7 carbon atoms, a dialkyl imidazolium ionic liquid, and optionally water; and the catalyst comprises at least one of cobalt, titanium, manganese, chromium, copper, nickel, vanadium, iron, molybdenum, tin, cerium, and zirconium.2. The process of wherein the carboxylic acid comprises acetic acid.3. The process of wherein the oxidizing agent is a gas comprising oxygen.4. The process of wherein the solvent has a ratio of ionic liquid to carboxylic acid ranging from about 1:10 to about 10:1 by weight.5. The process of wherein the oxidizing conditions comprise a pressure ranging from about 0 MPa(g) to about 6 MPa(g).6. The ...

SOLID TEREPHTHALIC ACID COMPOSITION

A solid terephthalic acid composition and a process for producing terephthalic acid from para-xylene. The process comprises forming a mixture comprising the para-xylene, a solvent, a bromine source, and a catalyst; and oxidizing the para-xylene by contacting the mixture with an oxidizing agent at oxidizing conditions to produce a solid oxidation product comprising terephthalic acid, para-toluic acid, 4-carboxybenzaldehyde. The solvent comprises a carboxylic acid having from 1 to 7 carbon atoms and an dialkyl imidazolium ionic liquid; and the catalyst comprises at least one of cobalt, titanium, manganese, chromium, copper, nickel, vanadium, iron, molybdenum, tin, cerium, and zirconium. The solid terephthalic acid composition comprises, less than about 4,000 ppm-wt 4-carboxybenzaldehyde content, and more than about 2,000 ppm-wt a para-toluic acid. 1. A solid terephthalic acid composition comprising terephthalic acid , para-toluic acid , and 4-carboxybenzaldehyde; wherein the composition has a 4-carboxybenzaldehyde content of less than about 4 ,000 ppm-wt , and a para-toluic acid content of more than about 2 ,000 ppm-wt.2. The solid terephthalic acid composition of wherein the composition has a terephthalic acid content of at least about 80 wt %.3. The solid terephthalic acid composition of wherein the para-toluic acid content is more than about 4 claim 1 ,000 ppm-wt.4. The solid terephthalic acid composition of wherein the para-toluic acid content ranges from about 2 claim 1 ,000 ppm-wt to about 14 wt %.5. The solid terephthalic acid composition of wherein the para-toluic acid content is at least 15 times greater than the 4-carboxybenzaldehyde content on a weight basis.6. The solid terephthalic acid composition of wherein the 4-carboxybenzaldehyde content is less than about 3 claim 1 ,000 ppm-wt.7. The solid terephthalic acid composition of wherein the para-toluic acid content is more than about 4 claim 6 ,000 ppm-wt.8. The solid terephthalic acid composition of ...

Process for ProducingTerephthalic Acid

A solid terephthalic acid composition and a process for producing terephthalic acid from para-xylene. The process comprises forming a mixture comprising the para-xylene, a solvent, a bromine source, and a catalyst; and oxidizing the para-xylene by contacting the mixture with an oxidizing agent at oxidizing conditions to produce a solid oxidation product comprising terephthalic acid, para-toluic acid, 4-carboxybenzaldehyde. The solvent comprises a carboxylic acid having from 1 to 7 carbon atoms and an dialkyl imidazolium ionic liquid; and the catalyst comprises at least one of cobalt, titanium, manganese, chromium, copper, nickel, vanadium, iron, molybdenum, tin, cerium, and zirconium. The solid terephthalic acid composition comprises, less than about 4,000 ppm-wt 4-carboxybenzaldehyde content, and more than about 2,000 ppm-wt a para-toluic acid. 1. A process for producing terephthalic acid from para-xylene , the process comprising:forming a mixture comprising the para-xylene, a solvent, a bromine source, a catalyst and optionally ammonium acetate; andoxidizing the para-xylene by contacting the mixture with an oxidizing agent at oxidizing conditions to produce a solid oxidation product, the solid oxidation product comprising terephthalic acid, 4-carboxybenzaldehyde, and para-toluic acid;wherein the solvent comprises a carboxylic acid having from 1 to 7 carbon atoms, a dialkyl imidazolium ionic liquid, and optionally water; and the catalyst comprises at least one of cobalt, titanium, manganese, chromium, copper, nickel, vanadium, iron, molybdenum, tin, cerium, and zirconium.2. The process of wherein the carboxylic acid comprises acetic acid.3. The process of wherein the oxidizing agent is a gas comprising oxygen.4. The process of wherein the solvent has a ratio of ionic liquid to carboxylic acid ranging from about 1:10 to about 10:1 by weight.5. The process of wherein the oxidizing conditions comprise a pressure ranging from about 0 MPa(g) to about 6 MPa(g).6. The ...

PROCESS FOR HYDROTREATING A COAL TAR STREAM

A process for hydrotreating a coal tar stream is described. A coal tar stream is provided, and the coal tar stream is expanded with an inert gas stream to provide an expanded liquid coal tar stream. The expanded liquid coal tar stream is hydrotreated. The coal tar stream can be reacted with a hydrocarbon solvent before it is expanded. 1. A process comprising:providing a coal tar stream;expanding the coal tar stream with an inert gas stream to provide an expanded liquid coal tar stream; andhydrotreating the expanded liquid coal tar stream.2. The process of wherein hydrotreating the expanded liquid coal tar stream comprises subjecting the expanded liquid coal tar stream to hydrodesulfurization claim 1 , or hydrodenitrogenation claim 1 , or both.3. The process of further comprising:processing the hydrotreated stream by one or more of hydrocracking, fluid catalytic cracking, alkylation, transalkylation, oxidation, and hydrogenation to provide at least one product.4. The process of wherein the inert gas is selected from the group consisting of carbon dioxide claim 1 , nitrogen claim 1 , and light hydrocarbons.5. The process of claim 1 , wherein the hydrotreating takes place at a temperature range of about 260° C. (about 500° F.) to about 370° C. (about 700° F.).6. The process of claim 1 , wherein the hydrotreating takes place at a pressure range of about 4.8 MPa (about 700 psi) to about 8.3 MPa (about 1200 psi).7. The process of claim 1 , wherein the hydrotreating takes place in the presence of a catalyst.8. The process of further comprising:feeding the coal tar stream and a hydrocarbon solvent into a reaction zone;reacting the coal tar stream and the hydrocarbon solvent in the reaction zone to provide a liquid coal tar stream; andwherein expanding the coal tar stream comprises expanding the liquid coal tar stream.9. The process of wherein the hydrocarbon solvent comprises an aromatic hydrocarbon.10. The process of wherein the coal tar stream and the hydrocarbon solvent ...

PROCESS FOR PYROLYSIS AND GASIFICATION OF A COAL FEED

A process for gasifying and pyrolyzing coal is described. A first coal feed is pyrolyzed into a coal tar stream and a coke stream in a pyrolysis zone. A second coal feed is gasified in a gasification zone to produce an effluent stream. Contaminants are removed from the effluent stream to provide a purified effluent stream. The purified effluent stream is introduced to the pyrolysis zone. 1. A process comprising:pyrolyzing a first coal feed into a coal tar stream and a coke stream in a pyrolysis zone;gasifying a second coal feed in a gasification zone to produce an effluent stream;removing contaminants from the effluent stream to provide a purified effluent stream; andintroducing the purified effluent stream to said pyrolysis zone.2. The process of wherein the gasification zone is selected from the group consisting of a moving bed gasifier claim 1 , a fluidized bed gasifier claim 1 , and an entrained flow gasifier.3. The process of wherein the second coal feed is pulverized and dry-fed into the gasification zone.4. The process of wherein gasifying the second coal feed takes place at a temperature between about 800° C. and about 1 claim 1 ,400° C.5. The process of wherein the effluent stream comprises hydrogen claim 1 , carbon monoxide claim 1 , carbon dioxide claim 1 , hydrogen sulfide claim 1 , steam claim 1 , or a combination.6. The process of wherein removing contaminants from the effluent stream comprises filtering particulate matter from the effluent stream.7. The process of wherein removing contaminants from the effluent stream comprises removing one or more of carbon dioxide claim 1 , hydrogen sulfide claim 1 , arsenic claim 1 , and mercury.8. The process of wherein removing contaminants comprises performing a water shift gas reaction to generate hydrogen and carbon dioxide from carbon monoxide and steam in the effluent stream.9. The process of further comprising:fractionating the coal tar stream to provide at least a hydrocarbon stream.10. The process of ...

PROCESS FOR PYROLYSIS OF COAL

A process for pyrolyzing a coal feed is described. The coal feed is pyrolyzed into a coal tar stream and a coke stream in a pyrolysis zone. The coal tar stream is fractionated into at least a pitch stream. The pitch stream is hydrogenated, and the hydrogenated pitch stream is recycled into the pyrolysis zone. The hydrocarbon stream may be processed further by at least one of hydrotreating, hydrocracking, fluid catalytic cracking, alkylation, and transalkylation. 1. A process comprising:pyrolyzing a coal feed into a coal tar stream and a coke stream in a pyrolysis zone;separating the coal tar stream into at least a pitch stream;hydrogenating the pitch stream; andrecycling the hydrogenated pitch stream into the pyrolysis zone.2. The process of wherein hydrogenating the pitch stream comprises contacting the pitch stream with a hydrogenation catalyst consisting of metal selected from the group consisting of Group VI metals (Cr claim 1 , Mo claim 1 , W) claim 1 , Group VII metals (Mn claim 1 , Tc claim 1 , Re) claim 1 , or Group VIII metals (Fe claim 1 , Co claim 1 , Ni claim 1 , Ru claim 1 , Rh claim 1 , Pd claim 1 , Os claim 1 , Ir claim 1 , Pt) and combinations thereof supported on an inorganic oxide claim 1 , carbide or sulfide support claim 1 , including AlO claim 1 , SiO claim 1 , SiO—AlO claim 1 , zeolites claim 1 , non-zeolitic molecular sieves claim 1 , ZrO claim 1 , TiO claim 1 , ZnO claim 1 , and SiC.3. The process of wherein hydrogenating the pitch stream takes place at a temperature between about 250° C. and about 500° C.4. The process of wherein the hydrogenation takes place at a pressure between about 1.72 MPa (about 250 psig) and about 20.7 MPa (about 3 claim 1 ,000 psig).5. The process of wherein separating the coal tar stream further provides a hydrocarbon stream.6. The process of further comprising:recovering at least one product from the hydrocarbon stream.7. The process of further comprising:feeding additional coal feed into the pyrolysis zone; ...

HYDROTREATING PROCESS AND MULTIFUNCTION HYDROTREATER

A multifunction hydrotreater includes a particulate removal zone having a particulate trap to remove particulate contaminants from a coal tar stream and a demetallizing zone including a demetallizing catalyst to remove organically bound metals from the departiculated stream. The demetallizing zone is positioned after the particulate removal zone. The hydrotreater also includes a hydrodesulfurization, hydrodenitrogenation, and hydrodeoxygenation zone positioned after the demetallization zone, which includes at least one hydrodesulfurization, hydrodenitrogenation, and hydrodeoxygenation catalyst to provide a hydrotreated coal tar stream. 1. A multifunction hydrotreater comprising:a particulate removal zone comprising a particulate trap to remove particulate contaminants from a coal tar stream;a demetallizing zone comprising a demetallizing catalyst to remove organically bound metals from the de-particulated stream, the demetallizing zone positioned after the particulate removal zone; anda hydrodesulfurization, hydrodenitrogenation, and hydrodeoxygenation zone comprising at least one hydrodesulfurization, hydrodenitrogenation, and hydrodeoxygenation catalyst to provide a hydrotreated coal tar stream, the hydrodesulfurization, hydrodenitrogenation, and hydrodeoxygenation zone positioned after the demetallizing zone.2. The multifunction hydrotreater of claim 1 , wherein said hydrodesulfurization claim 1 , hydrodenitrogenation claim 1 , and hydrodeoxygenation zone comprises:a first zone comprising a first hydrodesulfurization, hydrodenitrogenation, and hydrodeoxygenation catalyst; anda second zone comprising a second hydrodesulfurization, hydrodenitrogenation, and hydrodeoxygenation catalyst.3. The multifunction hydrotreater of claim 2 , wherein each of said first and second catalysts includes one or more of a nickel-molybdenum catalyst claim 2 , a cobalt-molybdenum catalyst claim 2 , a nickel-tungsten catalyst claim 2 , and a nickel-cobalt-molybdenum catalyst.4. The ...

PROCESS FOR REMOVING ASH AND HEAVY HYDROCARBONS FROM COAL TAR

A process for removing ash and heavy hydrocarbon compounds from coal is described. The coal feed, the coal tar stream, or a coal tar fraction is contacted with a solvent to dissolve a soluble portion of the coal tar stream, the ash and heavy hydrocarbons being insoluble in the solvent, the solvent selected from the group consisting of dimethyl sulfoxide, sulfolane, dimethyl formamide, glyme, diglyme, ionic liquids, and combinations thereof, with the proviso that an anion of the ionic liquid is not a dialkylphosphate. 1. A process for removing ash and heavy hydrocarbon compounds from coal comprising:pyrolyzing a coal feed into a coal tar stream and a coke stream;separating the coal tar stream into at least two fractions;contacting one or more of the coal tar stream, or one of the fractions with a solvent to dissolve a soluble portion of the coal tar stream, or one of the fractions, the ash and heavy hydrocarbons being insoluble in the solvent, the solvent selected from the group consisting of dimethyl sulfoxide, sulfolane, dimethyl formamide, glyme, diglyme, ionic liquids, and combinations thereof, with the proviso that an anion of the ionic liquid is not a dialkylphosphate.2. The process of further comprising separating the ash and heavy hydrocarbons from the solvent.3. The process of wherein the ash and heavy hydrocarbons are separated from the solvent by one or more of settling claim 2 , decantation claim 2 , filtration claim 2 , centrifugation claim 2 , and using a filter column.4. The process of wherein the solvent is the ionic liquid and wherein the ionic liquid comprises imidizolium-based ionic liquids claim 1 , pyridinium-based ionic liquids claim 1 , pyrrolidinium-based ionic liquids claim 1 , ammonium-based ionic liquids claim 1 , sulphonium-based ionic liquids claim 1 , phosphonium-based ionic liquids claim 1 , caprolactam-based ionic liquids claim 1 , or combinations thereof.5. The process of wherein the solvent is the ionic liquid and wherein the anion ...

Hydroprocess for a hydrocarbon stream from coal tar

A coal tar process is described. A coal tar stream is provided, and the coal tar stream is separated to provide a plurality of hydrocarbon streams. At least one of the hydrocarbon streams is hydroprocessed in a fluidized bed hydroprocessing zone with a catalyst to provide a gaseous volatile product and a solid heavy hydrocarbon product absorbed onto the catalyst. The gaseous volatile product is separated from the catalyst. The catalyst is regenerating by separating the absorbed heavy hydrocarbon product from the catalyst. The regenerated catalyst is recycled into the hydroprocessing zone.

Process for pyrolysis of a coal feed

A process for pyrolyzing a coal feed is described. A coal feed is pyrolyzed into a coal tar stream and a coke stream in a pyrolysis zone. The coal tar stream is separated into at least a pitch stream comprising aromatic hydrocarbons. The pitch stream is reacted in a reaction zone to add at least one functional group to an aromatic ring of the aromatic hydrocarbons in the pitch stream. The functionalized pitch stream is recycled to the pyrolysis zone.

Process for producing alkylated aromatic compounds

A process for producing alkylated aromatic compounds includes pyrolyzing a coal feed to produce a coke stream and a coal tar stream. The coal tar stream is hydrotreated and the resulting hydrotreated coal tar stream is cracked. A portion of the cracked coal tar stream is separated to obtain a fraction having an initial boiling point in the range of about 60° C. to about 180° C., and an aromatics-rich hydrocarbon stream is extracted by contacting the fraction with one or more solvents. The aromatics-rich hydrocarbon stream is contacted with an alkylating agent to produce an alkylated aromatic stream, or the aromatics-rich hydrocarbon stream is reacted with an aliphatic compound or methanol in the presence of a catalyst to produce a methylated aromatic stream. The alkylated aromatic stream, the methylated aromatic stream, or both are separated into at least a benzene stream, a toluene stream, and a xylenes stream.

HYDROCRACKING PROCESS FOR A HYDROCARBON STREAM

A process for transalkylating a coal tar stream is described. A coal tar stream is provided, and is fractionated to provide at least one hydrocarbon stream having polycyclic aromatics. The hydrocarbon stream is hydrotreated in a hydrotreating zone, and then hydrocracked in a hydrocracking zone. A light aromatics stream is added to the hydrocracking zone. The light aromatics stream comprises one or more light aromatics having a ratio of methyl/aromatic available position that is lower than a ratio of methyl/aromatic available position for the hydrotreated stream. The hydrocracked stream is transalkylated in the hydrocracking zone. 1. A process comprising:providing a coal tar stream;fractionating the coal tar stream to provide at least one hydrocarbon stream having polycyclic aromatics;hydrotreating the hydrocarbon stream in a hydrotreating zone;hydrocracking the hydrotreated stream in a hydrocracking zone;adding a light aromatics stream to the hydrocracking zone; andtransalkylating the hydrocracked stream in the hydrocracking zone;wherein the light aromatics stream comprises one or more light aromatics having a ratio of methyl/aromatic available position that is lower than a ratio of methyl/aromatic available position for the hydrotreated stream.2. The process of wherein hydrocracking the hydrotreated stream takes place at a pressure between about 1.4 MPa (200 psig) to about 17.24 MPa (2500 psig).3. The process of further comprising:feeding an effluent stream from the hydrocracking zone to a dehydrogenation zone; anddehydrogenating the effluent stream in the dehydrogenation zone to convert cycloparaffins in the effluent stream to aromatics.4. The process of wherein dehydrogenating the effluent stream takes place at dehydrogenating conditions comprising 0.21-3.4 MPa (30-500 psig) and 427-538° C. (800-1000° F.).5. The process of further comprising:feeding an effluent stream from the dehydrogenation zone to a transalkyation zone; andtransalkylating the effluent stream ...

PROCESS FOR HYDROTREATING A COAL TAR STREAM

A process for hydrotreating a coal tar stream is described. A coal tar stream is provided, and the coal tar stream is fractionated into at least a light naphtha range hydrocarbon stream having a boiling point in the range of about 85° C. (185° F.) to about 137.8° C. (280° F.). The light naphtha range hydrocarbon stream is hydrotreated by contacting the light naphtha range hydrocarbon stream with a naphtha hydrotreating catalyst. 1. A process comprising:providing a coal tar stream;fractionating the coal tar stream into at least a light naphtha range hydrocarbon stream having a boiling point in a range of about 85° C. (185° F.) to about 137.8° C. (280° F.); andhydrotreating the light naphtha range hydrocarbon stream by contacting the light naphtha range hydrocarbon stream with a naphtha hydrotreating catalyst.2. The process of wherein hydrotreating the light naphtha range hydrocarbon stream removes sulfur claim 1 , nitrogen claim 1 , or both.3. The process of wherein hydrotreating the light naphtha range hydrocarbon stream removes sulfur to provide a hydrotreated stream having a sulfur concentration of less than about 0.2 ppm.4. The process of wherein the naphtha hydrotreating catalyst comprises molybdenum and one or more of cobalt and nickel.5. The process of wherein the naphtha hydrotreating catalyst comprises nickel and molybdenum.6. The process of wherein the light naphtha range hydrocarbon stream comprises a hexane insoluble stream claim 1 , a benzene insoluble stream claim 1 , or both.7. The process of further comprising:blending the hydrotreated stream with a gasoline stream.8. The process of further comprising:reforming the hydrotreated stream to provide an aromatics stream.9. The process of wherein providing a coal tar stream comprises pyrolyzing a coal feed in a pyrolysis zone to provide the coal tar stream and a coke stream.10. A process comprising:pyrolyzing a coal feed into at least a coke stream and a coal tar stream in a pyrolysis zone, the coal tar ...

Process for selectively dealkylating aromatic compounds

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

Process for providing aromatics from coal tar

A process for providing aromatics from a coal tar stream. A coal tar stream is provided, and the coal tar stream is fractionated into at least a naphtha range stream. The naphtha range stream is hydrotreated, and the hydrotreated naphtha range stream is separated to provide at least a naphthene rich stream. The naphthene rich stream is reformed or dehydrogenated to convert the naphthene. The dehydrogenated naphthene rich stream may be combined with a portion of a reformed crude oil hydrocarbon stream.

PROCESS FOR PRODUCING OLEFINS FROM A COAL FEED

A process for producing olefins from a coal feed includes providing a coal tar stream and fractionating the coal tar stream to provide a hydrocarbon stream that includes hydrocarbons having an initial boiling point of about 250° C. or greater. The hydrocarbon stream is hydrotreated to reduce a concentration of one or more of nitrogen, sulfur, and oxygen in the hydrocarbon stream, and the hydrotreated hydrocarbon stream is cracked in a fluidized catalytic cracking zone to produce an olefin stream. 1. A process for producing olefins from a coal feed , comprising:providing a coal tar stream;fractionating the coal tar stream to provide a hydrocarbon stream comprising hydrocarbons having an initial boiling point of about 250° C. or greater;hydrotreating the hydrocarbon stream to reduce a concentration of one or more of nitrogen, sulfur, and oxygen in the hydrocarbon stream; andcracking the hydrotreated hydrocarbon stream in a fluidized catalytic cracking zone to produce an olefin stream.2. The process of claim 1 , wherein hydrotreating the hydrocarbon stream comprises contacting the hydrocarbon stream with a hydrotreating catalyst including a metal function comprising one or more of nickel claim 1 , molybdenum claim 1 , cobalt claim 1 , and tungsten.3. The process of claim 1 , wherein the hydrocarbon stream comprises hydrocarbons having the initial boiling point between about 300° C. and about 400° C.4. The process of claim 1 , wherein the olefin stream comprises a plurality of olefins claim 1 , the process further comprising:separating the olefin stream into a plurality of olefin product streams based on a carbon number of the olefins.5. The process of claim 4 , wherein separating the olefin stream comprises distilling the olefin stream.6. The process of claim 4 , wherein separating the olefin stream comprises performing a solvent extraction on the olefin stream.7. The process of claim 4 , wherein separating the olefin stream produces at least a first olefin product ...

Process for selectively dealkylating aromatic compounds

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

Process for providing aromatics from coal tar

A process for providing aromatics from a coal tar stream. A coal tar stream is provided, and the coal tar stream is fractionated into at least a naphtha range stream. The naphtha range stream is hydrotreated, and the hydrotreated naphtha range stream is separated to provide at least a naphthene rich stream. The naphthene rich stream is reformed or dehydrogenated to convert the naphthene. The dehydrogenated naphthene rich stream may be combined with a portion of a reformed crude oil hydrocarbon stream.

HYDROCRACKING PROCESS FOR A HYDROCARBON STREAM

A process for transalkylating a coal tar stream is described. A coal tar stream is provided, and is fractionated to provide at least one hydrocarbon stream having polycyclic aromatics. The hydrocarbon stream is hydrotreated in a hydrotreating zone, and then hydrocracked in a hydrocracking zone. A light aromatics stream is added to the hydrocracking zone. The light aromatics stream comprises one or more light aromatics having a ratio of methyl/aromatic available position that is lower than a ratio of methyl/aromatic available position for the hydrotreated stream. The hydrocracked stream is transalkylated in the hydrocracking zone. 1. A process comprising:providing a coal tar stream;fractionating said coal tar stream to provide at least one hydrocarbon stream comprising polycyclic aromatics;introducing the hydrocarbon stream to a hydrocracking zone;hydrocracking the hydrocarbon stream in the hydrocracking zone to convert a first portion of the polycyclic aromatics to monocyclic aromatics; andhydrogenating a second portion of the polycyclic aromatics in the hydrocracking zone to form a hydrogen donor molecule.2. The process of further comprising introducing the hydrogen donor molecule to an upstream pyrolysis zone.3. The process of further comprising introducing the hydrogen donor molecule to an upstream hydrotreating zone.4. The process of wherein the portion of the polycyclic aromatics comprises tetralin.5. The process of further comprising:{'sub': '5', 'introducing a light fraction (C−) output from the hydrocracking zone to an olefin production zone;'}producing olefins in the light fraction output by steam cracking, wherein excess hydrogen is produced; andintroducing the excess hydrogen to a hydroprocessing zone.6. The process of further comprising pyrolyzing a coal feed in a pyrolysis zone to provide at least a coke stream and the coal tar feed.7. The process of claim 6 , further comprising introducing the hydrogen donor molecule to the pyrolysis zone.8. A process ...

Detergent alkylation process using a fluorided silica-alumina

A fluorided silca-alumina catalyst, particularly one with a silica:alumina ratio in the range of 1:1-9:1 containing from 1 to 6 weight percent fluoride, is particularly effective in the liquid phase alkylation of benzene to produce linear alkyl benzenes at temperatures no greater than 140° C. Conversions in excess of 98% with selectivity exceeding 85% and linearity exceeding 90% may be achieved readily.

Regeneration of an alkylation catalyst with hydrogen

Catalytic composites of the reaction product of a metal halide having Friedel-Crafts activity with the bound surface hydroxyl group of inorganic oxides and containing a zerovalent metal with hydrogenation activity, often are effective catalysts in motor fuel alkylation which, however, undergo rapid deactivation. Deactivated catalysts are readily regenerable by treating the composite from which alkylate feedstock has been removed with hydrogen at temperatures in the range of 10 to 300° C. Multiple regenerations are possible without appreciable activity loss.

Production of aviation fuel from biorenewable feedstocks

A process has been developed for producing aviation fuel from renewable feedstocks such as plant oils and animal fats and oils. The process involves treating a renewable feedstock by hydrogenating and deoxygenating to provide n-paraffins having from about 8 to about 24 carbon atoms. At least some of the n-paraffins are isomerized to improve cold flow properties. At least a portion of the paraffins are selectively cracked to provide paraffins meeting specifications for different aviation fuels such as JP-8.

Production of aviation fuel from renewable feedstocks

A hydrocarbon product stream having hydrocarbons with boiling points in the aviation fuel range is produced from renewable feedstocks such as plant and animal oils. The process involves treating a renewable feedstock by hydrogenating, deoxygenating, isomerization, and selectively hydrocracking the feedstock to produce paraffinic hydrocarbons having from about 9 to about 16 carbon atoms and a high iso/normal ratio in a single reaction zone containing a multifunctional catalyst, or set of catalysts, having hydrogenation, deoxygenation, isomerization and selective hydrocracking functions.

Controlling production of transportation fuels from renewable feedstocks

A process for controlling the concurrent production of both diesel range hydrocarbons and aviation range hydrocarbons from renewable feedstocks such as plant oils and animal oils. The process involves determining the required specification of the desired products and the desired relative yields of the product that still meet the required specifications. The necessary isomerization and selective hydrocracking zone conditions are determined in order to create a mixture of paraffins which meet the required product specifications and yields. The necessary fractionation zone conditions are determined to separate the desired products. A renewable feedstock is treated by hydrogenating and deoxygenating to provide an effluent comprising paraffins, isomerizing and selectively hydrogenating at least a portion of the paraffins at the predetermined conditions, and separating by fractionation at the predetermined fractionation conditions to generate a diesel range hydrocarbon product and an aviation range hydrocarbon product.

Production of aviation fuel from renewable feedstocks

A hydrocarbon product stream having hydrocarbons with boiling points in the aviation fuel range is produced from renewable feedstocks such as plant and animal oils. The process involves treating a renewable feedstock by hydrogenating, deoxygenating, isomerization, and selectively hydrocracking the feedstock to produce paraffinic hydrocarbons having from 9 to 16 carbon atoms and a high iso/normal ratio in a single reaction zone containing a multifunctional catalyst, or set of catalysts, having hydrogenation, deoxygenation, isomerization and selective hydrocracking functions.

Methods of denitrogenating diesel fuel

A process for denitrogenating diesel fuel includes contacting diesel fuel containing one or more nitrogen compounds with an acid ionic liquid in an extraction zone to selectively remove the nitrogen compound(s) and produce a denitrogenated diesel fuel effluent containing denitrogenated diesel fuel and acid ionic liquid containing nitrogen species; and separating denitrogenated diesel fuel from the denitrogenated diesel fuel effluent.

Process for removing sulfur from vacuum gas oil

A process for removing a sulfur compound from a vacuum gas oil feed includes contacting the vacuum gas oil feed comprising the sulfur compound with a VGO-immiscible ionic liquid to produce a vacuum gas oil and VGO-immiscible ionic liquid mixture, and separating the mixture to produce a vacuum gas oil effluent having a reduced sulfur content relative to the vacuum gas oil feed.

Process for removing metals from vacuum gas oil

A process for removing a metal from a vacuum gas oil feed includes contacting the vacuum gas oil feed comprising the metal with a VGO-immiscible ionic liquid to produce a vacuum gas oil and VGO-immiscible ionic liquid mixture, and separating the mixture to produce a vacuum gas oil effluent having a reduced metal content relative to the vacuum gas oil feed.

Process for removing nitrogen from vacuum gas oil

A process for removing a nitrogen compound from a vacuum gas oil feed includes contacting the vacuum gas oil feed comprising the nitrogen compound with a VGO-immiscible phosphonium ionic liquid to produce a vacuum gas oil and VGO-immiscible phosphonium ionic liquid mixture, and separating the mixture to produce a vacuum gas oil effluent having a reduced nitrogen content relative to the vacuum gas oil feed.

Controlling production of transportation fuels from renewable feedstocks

A process for controlling the concurrent production of both diesel range hydrocarbons and aviation range hydrocarbons from renewable feedstocks such as plant oils and animal oils. The process involves determining the required specification of the desired products and the desired relative yields of the product that still meet the required specifications. The necessary isomerization and selective hydrocracking zone conditions are determined in order to create a mixture of paraffins which meet the required product specifications and yields. The necessary fractionation zone conditions are determined to separate the desired products. A renewable feedstock (2) is treated by hydrogenating and deoxygenating (4) to provide an effluent (6) comprising paraffins, isomerizing and selectively hydrogenating (22) at least a portion of the paraffins at the predetermined conditions, and separating by fractionation (42) at the predetermined fractionation conditions to generate a diesel range hydrocarbon product (46) and an aviation range hydrocarbon product (45).

Controlling production of transportation fuels from renewable feedstocks

A process for controlling the concurrent production of both diesel range hydrocarbons and aviation range hydrocarbons from renewable feedstocks such as plant oils and animal oils. The process involves determining the required specification of the desired products and the desired relative yields of the product that still meet the required specifications. The necessary isomerization and selective hydrocracking zone conditions are determined in order to create a mixture of paraffins which meet the required product specifications and yields. The necessary fractionation zone conditions are determined to separate the desired products. A renewable feedstock (2) is treated by hydrogenating and deoxygenating (4) to provide an effluent (6) comprising paraffins, isomerizing and selectively hydrogenating (22) at least a portion of the paraffins at the predetermined conditions, and separating by fractionation (42) at the predetermined fractionation conditions to generate a diesel range hydrocarbon product (46) and an aviation range hydrocarbon product (45).

Controlling production of transportation fuels from renewable feedstocks

A process for controlling the concurrent production of both diesel range hydrocarbons and aviation range hydrocarbons from renewable feedstocks such as plant oils and animal oils. The process involves determining the required specification of the desired products and the desired relative yields of the product that still meet the required specifications. The necessary isomerization and selective hydrocracking zone conditions are determined in order to create a mixture of paraffins which meet the required product specifications and yields. The necessary fractionation zone conditions are determined to separate the desired products. A renewable feedstock (2) is treated by hydrogenating and deoxygenating (4) to provide an effluent (6) comprising paraffins, isomerizing and selectively hydrogenating (22) at least a portion of the paraffins at the predetermined conditions, and separating by fractionation (42) at the predetermined fractionation conditions to generate a diesel range hydrocarbon product (46) and an aviation range hydrocarbon product (45).

Catalytic process for continuously generating polyols

A catalytic process for generating at least one polyol from a feedstock comprising cellulose is performed in a continuous manner. The process involves, contacting, continuously, hydrogen, water, and a feedstock comprising cellulose, with a catalyst to generate an effluent stream comprising at least one polyol, water, hydrogen, and at least one co-product. The water, hydrogen, and at least one co-product are separated from the effluent stream and recycled to the reaction zone. The polyol is recovered from the effluent stream.

Bound pillared clay for use in the production of alkyl aromatic compounds

Alkyl aromatic compounds are prepared by reacting at alkylation conditions an aromatic compound such as benzene with an alkylating agent such as an olefin, alkyl halide or alkyl alcohol in the presence of an alkylation catalyst comprising a pillared clay and a binder which has been prepared by dispersing a clay in a metallic pillaring agent sol, separating the resultant pillared clay, washing and drying said pillared clay, forming a dough of said pillared clay and a binder compound, extruding said dough extudate and calcining the resultant extrudate. This catalyst enables improved selectivity for the desired linear alkyl aromatic compound which may then be used in the preparation of biodegradable detergents.

NEW ENGINE FUEL COOLING CATALYST AND PROCEDURES USING THIS.

Recovery and recycle of hf-amine complex in hf alkylation

An HF-amine complex such as HF-pyridine is recovered and recycled from a by-product containing stream [10] in an alkylation process using the complex as the catalyst system by (a) selectively removing a portion of the HF from the by-product stream [10] to produce an HF-depleted stream [22] containing an HF to complexing agent mole ratio of 3:1 to 5:1, (b) separating the resulting HF-depleted stream [22] into a hydrocarbon phase [26] enriched in ASO and an acid phase [28] depleted in ASO and containing a substantial portion of the complex, and (c) recycling the acid phase [28] to the hydrocarbon alkylation step.

Generation of polyols from saccharides

A process for generating at least one polyol from a feedstock comprising saccharide is performed in a continuous or batch manner. The process involves, contacting, hydrogen, water, and a feedstock comprising saccharide, with a catalyst system to generate an effluent stream comprising at least one polyol and recovering the polyol from the effluent stream. The catalyst system comprises at least one unsupported component and at least one supported component.

process for controlling the production of a diesel component, and, diesel fuel or diesel fuel mixture component and an aviation fuel or aviation fuel mixture component

Process for oxidizing alkyl aromatic compounds

A process and a mixture for oxidizing an alkyl-aromatic compound comprises forming a mixture comprising the alkyl-aromatic compound, a solvent, a bromine source, and a catalyst; and contacting the mixture with an oxidizing agent at oxidizing conditions to produce an oxidation product comprising at least one of an aromatic aldehyde, an aromatic alcohol, an aromatic ketone, and an aromatic carboxylic acid. The solvent comprises a carboxylic acid having from 1 to 7 carbon atoms and an ionic liquid selected from the group consisting of an imidazolium ionic liquid, a pyridinium ionic liquid, a phosphonium ionic liquid, a tetra alkyl ammonium ionic liquid, and combinations thereof. The catalyst comprises at least one of cobalt, titanium, manganese, chromium, copper, nickel, vanadium, iron, molybdenum, tin, cerium, and zirconium.

Production of Aviation Fuel from Renewable Feedstocks

A hydrocarbon product stream having hydrocarbons with boiling points in the aviation fuel range is produced from renewable feedstocks such as plant and animal oils. The process involves treating a renewable feedstock by hydrogenating, deoxygenating, isomerization, and selectively hydrocracking the feedstock to produce paraffinic hydrocarbons having from about 9 to about 16 carbon atoms and a high iso/normal ratio in a single reaction zone containing a multifunctional catalyst, or set of catalysts, having hydrogenation, deoxygenation, isomerization and selective hydrocracking functions.

Alkylating catalyzer for fuel production and the method servicing for carrying out the alkylating catalyzer

Catalytic process for continuously generating polyols

A catalytic process for generating at least one polyol from a feedstock comprising cellulose is performed in a continuous manner. The process involves, contacting, continuously, hydrogen, water, and a feedstock comprising cellulose, with a catalyst to generate an effluent stream comprising at least one polyol, water, hydrogen, and at least one co-product. The water, hydrogen, and at least one co-product are separated from the effluent stream and recycled to the reaction zone. The polyol is recovered from the effluent stream.

Methods of denitrogenating diesel fuel.

Un proceso para desnitrogenar combustible diesel incluye contactar combustible diesel que contiene uno o más compuestos de nitrógeno con un líquido iónico ácido en una zona de extracción, para eliminar selectivamente los compuestos de nitrógeno y producir un efluente de combustible diesel desnitrogenado que contiene combustible diesel desnitrogenado y líquidos iónicos ácidos que contienen especies nitrogenadas; y separar combustible diesel desnitrogenado del efluente de combustible diesel desnitrogenado.

Low oxygen biomass-derived pyrolysis oils and methods for producing the same

Low oxygen biomass-derived pyrolysis oils and methods for producing them from carbonaceous biomass feedstock are provided. The carbonaceous biomass feedstock is pyrolyzed in the presence of a catalyst comprising base metal-based catalysts, noble metal-based catalysts, treated zeolitic catalysts, or combinations thereof to produce pyrolysis gases. During pyrolysis, the catalyst catalyzes a deoxygenation reaction whereby at least a portion of the oxygenated hydrocarbons in the pyrolysis gases are converted into hydrocarbons. The oxygen is removed as carbon oxides and water. A condensable portion (the vapors) of the pyrolysis gases is condensed to low oxygen biomass-derived pyrolysis oil.

Bound bridged clay for use in the manufacture of alkyl aromatic compounds.

Low oxygen biomass-derived pyrolysis oils and methods for producing the same

Low oxygen biomass-derived pyrolysis oils and methods for producing them from carbonaceous biomass feedstock are provided. The carbonaceous biomass feedstock is pyrolyzed in the presence of a catalyst comprising base metal-based catalysts, noble metal- based catalysts, treated zeolitic catalysts, or combinations thereof to produce pyrolysis gases. During pyrolysis, the catalyst catalyzes a deoxygenation reaction whereby at least a portion of the oxygenated hydrocarbons in the pyrolysis gases are converted into hydrocarbons. The oxygen is removed as carbon oxides and water. A condensable portion (the vapors) of the pyrolysis gases is condensed to low oxygen biomass-derived pyrolysis oil.

Process for pyrolysis of coal

A process for pyrolyzing a coal feed is described. The coal feed is pyrolyzed into a coal tar stream and a coke stream in a pyrolysis zone. The coal tar stream is fractionated into at least a pitch stream. The pitch stream is hydrogenated, and the hydrogenated pitch stream is recycled into the pyrolysis zone. The hydrocarbon stream may be processed further by at least one of hydrotreating, hydrocracking, fluid catalytic cracking, alkylation, and transalkylation.

Benzene alkylation process using a fluorided silica-alumina and a linear C6 to C20 monoolefin

Novel motor fuel alkylation catalyst and process for the use thereof

A novel hydrocarbon alkylation catalyst is disclosed comprising a mineral acid and an ether component. A process for utilizing the novel catalyst is also disclosed.

Ring opening for increased olefin production

A process for cracking a naphtha feedstream to light olefins is presented. The process comprises converting aromatics and naphthenes to paraffins, and separating iso- and normal paraffins using a ring opening reactor (50) and an adsorption separation unit (20).

Processes for converting lignocellulosics to reduced acid pyrolysis oil

Processes for producing reduced acid lignocellulosic-derived pyrolysis oil are provided. In a process, lignocellulosic material is fed to a heating zone. A basic solid catalyst is delivered to the heating zone. The lignocellulosic material is pyrolyzed in the presence of the basic solid catalyst in the heating zone to create pyrolysis gases. The oxygen in the pyrolysis gases is catalytically converted to separable species in the heating zone. The pyrolysis gases are removed from the heating zone and are liquefied to form the reduced acid lignocellulosic-derived pyrolysis oil.

Process for oxidizing alkyl aromatic compounds

A process and a mixture for oxidizing an alkyl-aromatic compound comprises forming a mixture comprising the alkyl-aromatic compound, a solvent, a bromine source, and a catalyst; and contacting the mixture with an oxidizing agent at oxidizing conditions to produce an oxidation product comprising at least one of an aromatic aldehyde, an aromatic alcohol, an aromatic ketone, and an aromatic carboxylic acid. The solvent comprises a carboxylic acid having from 1 to 7 carbon atoms and an ionic liquid selected from the group consisting of an imidazolium ionic liquid, a pyridinium ionic liquid, a phosphonium ionic liquid, a tetra alkyl ammonium ionic liquid, and combinations thereof. The catalyst comprises at least one of cobalt, titanium, manganese, chromium, copper, nickel, vanadium, iron, molybdenum, tin, cerium, and zirconium.

Production of Aviation Fuel from Biorenewable Feedstocks

A process has been developed for producing aviation fuel from renewable feedstocks such as plant oils and animal fats and oils. The process involves treating a renewable feedstock by hydrogenating and deoxygenating to provide n-paraffins having from about 8 to about 24 carbon atoms. At least some of the n-paraffins are isomerized to improve cold flow properties. At least a portion of the paraffins are selectively cracked to provide paraffins meeting specifications for different aviation fuels such as JP-8.

Recovery and recycle of hf-amine complex in hf alkylation

An HF-amine complex such as HF-pyridine is recovered and recycled from a by-product containing stream [10] in an alkylation process using the complex as the catalyst system by (a) selectively removing a portion of the HF from the by-product stream [10] to produce an HF-depleted stream [22] containing an HF to complexing agent mole ratio of 3:1 to 5:1, (b) separating the resulting HF-depleted stream [22] into a hydrocarbon phase [26] enriched in ASO and an acid phase [28] depleted in ASO and containing a substantial portion of the complex, and (c) recycling the acid phase [28] to the hydrocarbon alkylation step.

Production of aviation fuel from renewable feedstocks

A hydrocarbon prod-uct stream having hydrocarbons with boiling points in the aviation fuel range is produced from renewable feedstocks such as plant and animal oils. The process involves treating a renewable feedstock by hydrogenat-ing, deoxygenating, isomerization, and selectively hydrocracking the feedstock to produce paraffinic hy-drocarbons having from 9 to 16 car-bon atoms and a high iso/normal ra-tio in a single reaction zone contain-ing a multifunctional catalyst, or set of catalysts, having hydrogenation, deoxygenation, isomerization and se-lective hydrocracking functions.

Hydrotreating process and multifunction hydrotreater related applications

A multifunction hydrotreater includes a particulate removal zone having a particulate trap to remove particulate contaminants from a coal tar stream and a demetallizing zone including a demetallizing catalyst to remove organically bound metals from the de-particulated stream. The demetallizing zone is positioned after the particulate removal zone. The hydrotreater also includes a hydrodesulfurization, hydrodenitrogenation, and hydrodeoxygenation zone positioned after the demetallization zone, which includes at least one hydrodesulfurization, hydrodenitrogenation, and hydrodeoxygenation catalyst to provide a hydrotreated coal tar stream.

Hydrocracking process for a hydrocarbon stream

A process for transalkylating a coal tar stream is described. A coal tar stream is provided, and is fractionated to provide at least one hydrocarbon stream having polycyclic aromatics. The hydrocarbon stream is hydrotreated in a hydrotreating zone, and then hydrocracked in a hydrocracking zone. A light aromatics stream is added to the hydrocracking zone. The light aromatics stream comprises one or more light aromatics having a ratio of methyl/aromatic available position that is lower than a ratio of methyl/aromatic available position for the hydrotreated stream. The hydrocracked stream is transalkylated in the hydrocracking zone.

Controlling production of transportation fuels from renewable feedstocks

A process for controlling the concurrent production of both diesel range hydrocarbons and aviation range hydrocarbons from renewable feedstocks such as plant oils and animal oils. The process involves determining the required specification of the desired products and the desired relative yields of the product that still meet the required specifications. The necessary iso-merization and selective hydrocracking zone conditions are determined in order to create a mixture of paraffins which meet the required product specifications and yields. The necessary fractionation zone conditions are determined to separate the desired products. A renewable feedstock (2) is treated by hydrogenating and deoxygenating (4) to provide an effluent (6) comprising paraffins, isomerizing and selectively hydrogenating (22) at least a portion of the paraffins at the predetermined conditions, and separating by fractionation (42) at the predetermined fractionation conditions to generate a diesel range hydrocarbon product (46) and an aviation range hydrocarbon product (45).

Improved process for alkylation of aromatics with linear olefins derived from a linear paraffin dehydrogenation step

Aromatic byproducts normally formed in the dehydrogenation of normal paraffins to linear monoolefins have been found to be are detrimental in the usual processes of aromatic alkylation using the dehydrogenation product mixture as an alkylation feedstock. In particular, when solids are used as the alkylation catalysts with recycle of the unreacted feedstock to the dehydrogenation reactor the aromatic byproducts increase to a level where they exert a significant decrease in the stability of the alkylation catalyst. When the aromatic byproducts are removed in whole or in part alkylation may be performed at a substantially lower temperature, which affords alkylated aromatics whose alkyl portion has greater linearity than that observed at a higher alkylation temperature.

Catalyst and process for producing aromatic compounds from C2 -C6

A catalyst for converting C 2 to C 6 aliphatic hydrocarbons to aromatics is described. The catalyst contains a zeolite, an aluminum phosphate binder and a gallium component. Examples of zeolites which can be used are the ZSM family of zeolites, with ZSM-5 being a specific example. The catalyst is characterized in that it is tolerant to exposure to hydrogen at tempertures of about 500° to about 700° C. The catalyst's tolerance to hydrogen exposure is the result of treating the catalyst with an aqueous solution of a weakly acidic ammonium salt or a dilute acid solution at a temperature of about 50° to about 100° C. for a time of about 1 to about 48 hours, followed by calcination. A process for preparing the catalyst is also described.

Benzene alkylation process using a fluorided silica-alumina and a linear c6 to c20 monoolefin

Benzene is alkylated with a C6 to C20 linear monoolefin at 98% conversion of olefin with 85% or better selectivity to monoalkylbenzene formation and with at least 90% linearity with respect to monoalkylbenzene formation by contacting the benzene and the linear monoolefin at alkylation conditions with a catalyst comprising a fluorided silica-alumina having a silica:alumina wt. ratio of 1:1 to 9:1 and a fluoride content of 1 to 6 wt.%. In a preferred embodiment, the resulting linear monoalkylbenzene is sulfonated and neutralized to form a superior biodegradable detergent.

Production of aviation fuel from renewable feedstocks

A hydrocarbon product stream having hydrocarbons with boiling points in the aviation fuel range is produced from renewable feedstocks such as plant and animal oils. The process involves treating a renewable feedstock by hydrogenating, deoxygenating, isomerization, and selectively hydrocracking the feedstock to produce paraffinic hydrocarbons having from 9 to 16 carbon atoms and a high iso/normal ratio in a single reaction zone containing a multifunctional catalyst, or set of catalysts, having hydrogenation, deoxygenation, isomerization and selective hydrocracking functions.

Process for the direct production of methanol from methane

A process for the production of methanol from methane has been developed. The process involves reacting methane with an oxidant such as oxygen or a peroxide in the presence of a catalyst and a solvent in a reaction zone to produce an effluent stream comprising a methanol product. The effluent stream is next separated into a gaseous stream comprising unreacted methane and carbon dioxide and a liquid stream comprising the methanol product and solvent. Next the gaseous stream is further separated to provide a methane stream which is recycled to the reaction zone. Finally, a methanol stream is isolated and a solvent stream is recycled to the reaction zone.

Process for removing nitrogen from vacuum gas oil.

Un proceso para eliminar un compuesto nitrogenado de una alimentación de gasóleo de vacío incluye contactar la alimentación de gasóleo de vacío, que comprende el compuesto nitrogenado con un líquido iónico de fosfonio inmiscible en GOV, para producir una mezcla de gasóleo de vacío y un líquido iónico de fosfonio inmiscible en GOV, y separar la mezcla para producir un efluente de gasóleo de vacío que posee un contenido reducido de nitrógeno respecto a la alimentación del gasóleo de vacío.

Catalyst for the Alkylation of an Isoparaffin with an Olefin Affecting Agent and its Use

Catalyst for selective opening of cyclic paraffins and process for using the catalyst

A catalyst and process using the catalyst for opening cyclic paraffins are described. The catalyst comprises a Group VIII metal component, a molecular sieve, a refractory inorganic oxide component and optionally a modifier component. Examples of the molecular sieve are MAPSOs, SAPOs, UZM-8 and UZM-15. Preferred Group VIII metals include platinum, palladium and rhodium while alumina is a preferred inorganic oxide. Finally, examples of the optional modifier are niobrium, titanium and rare earth elements such as ytterbium.

Low oxygen biomass-derived pyrolysis oils and methods for producing the same

Methods are provided for producing low oxygen biomass-derived pyrolysis oil from carbonaceous biomass feedstock. The carbonaceous biomass feedstock is pyrolyzed in the presence of a steam reforming catalyst to produce char and pyrolysis gases. During pyrolysis, a portion of the oxygenated hydrocarbons in the pyrolysis gases is converted into hydrocarbons by steam reforming also yielding carbon oxides and hydrogen gas. The hydrogen gas at least partially deoxygenates a residual portion of the oxygenated hydrocarbons. Additional hydrogen gas may also be produced by water-gas shift reactions to deoxygenate the residual portion of the oxygenated hydrocarbons in the pyrolysis gases. Deoxygenation may occur in the presence of a hydroprocessing catalyst. A condensable portion of the pyrolysis gases is condensed to form low oxygen biomass-derived pyrolysis oil.

Selective oxidation agent of hydrocarbons to synthesis gas based on separate particles of o-carrier and hydrocarbon activator

A solid material is presented for the partial oxidation of natural gas. The solid material includes a solid oxygen carrying agent and a hydrocarbon activation agent. The material precludes the need for gaseous oxygen for the partial oxidation and provides better control over the reaction.

Controlling production of transportation fuels from renewable feedstocks

A process for controlling the concurrent production of both diesel range hydrocarbons and aviation range hydrocarbons from renewable feedstocks such as plant oils and animal oils. The process involves determining the required specification of the desired products and the desired relative yields of the product that still meet the required specifications. The necessary iso-merization and selective hydrocracking zone conditions are determined in order to create a mixture of paraffins which meet the required product specifications and yields. The necessary fractionation zone conditions are determined to separate the desired products. A renewable feedstock (2) is treated by hydrogenating and deoxygenating (4) to provide an effluent (6) comprising paraffins, isomerizing and selectively hydrogenating (22) at least a portion of the paraffins at the predetermined conditions, and separating by fractionation (42) at the predetermined fractionation conditions to generate a diesel range hydrocarbon product (46) and an aviation range hydrocarbon product (45).

Production of aviation fuel from biorenewable feedstocks

Removal of sulfur-containing compounds from liquid hydrocarbon streams

An improved method for desulfurizing a fuel stream such as a diesel stream is disclosed which includes generation of a sulfone oil, the desulfurization of the sulfone oil and the recycling of the resulting biphenyl-rich stream and ultra-low sulfur diesel streams. The method includes combining a thiophene-rich diesel stream with an oxidant to oxidize the thiophenes to sulfones to provide a sulfone-rich diesel stream. Sulfone oil is extracted from the sulfone-rich diesel stream to provide sulfone oil and a first low-sulfur diesel stream The low-sulfur diesel stream is recycled. The sulfone-rich oil stream is combined with an aqueous oxidant-containing stream, such as caustic stream, which oxidizes the sulfones to biphenyls and forms sulfite to provide a second low-sulfur diesel stream

Process for removing sulfur from vacuum gas oil

A process for removing a sulfur compound from a vacuum gas oil feed includes contacting the vacuum gas oil feed comprising the sulfur compound with a VGO-immiscible ionic liquid to produce a vacuum gas oil and VGO-immiscible ionic liquid mixture, and separating the mixture to produce a vacuum gas oil effluent having a reduced sulfur content relative to the vacuum gas oil feed.

Catalytic process for continuously generating polyols

A catalytic process for generating at least one polyol from a feedstock comprising cellulose is performed in a continuous manner. The process involves, contacting, continuously, hydrogen, water, and a feedstock comprising cellulose, with a catalyst to generate an effluent stream comprising at least one polyol, water, hydrogen, and at least one co-product. The water, hydrogen, and at least one co-product are separated from the effluent stream and recycled to the reaction zone. The polyol is recovered from the effluent stream.

Process for removing metals from vacuum gas oil

A process for removing a metal from a vacuum gas oil feed includes contacting the vacuum gas oil feed comprising the metal with a VGO-immiscible ionic liquid to produce a vacuum gas oil and VGO-immiscible ionic liquid mixture, and separating the mixture to produce a vacuum gas oil effluent having a reduced metal content relative to the vacuum gas oil feed.

Dezaktivált, szilárd alkilező katalizátor periodikus regenerálása hidrogénnel

A találmány tárgya eljárás szilárd alkilezőkatalizátor regenerálására, amely tartalmazza 1. egy első fém-halogenid és egy tűzálló szervetlen oxidon kötött felszíni hidroxilcsoportok reakciótermékét, és 2. egy nulla vegyértékű második fémet, mimellett az első fém-halogenid egy fluorid, klorid vagy bromid, és az első fém alumínium, cirkónium, ón, tantál, titán, gallium, antimon, foszfor, bór vagy ezek keveréke, és a második, nulla vegyértékű fém platina, palládium, nikkel, ruténium, ródium, ozmium, irídium vagy ezek keveréke, és a katalizátor legalább részben dezaktiválódott egy 2-6 szénatomos alkénnek egy 4-6 szénatomos alkánnal végzett folyékony fázisú katalizált alkilezési folyamata során. A találmány értelmében úgy járnak el, hogy a katalizátorról a folyékony fázisú reakciókeveréket eltávolítják, a kapott katalizátort hidrogénnel kezelik 6,9-13 790 kPa parciális nyomáson 1-20 órát, 10-300 °C hőmérsékleten, és a jelentősen megnövekedett alkilezési aktivitású regenerált katalizátort kinyerik. HU 218 872 B A leírás terjedelme 6 oldal

Process for providing aromatics from coal tar

A process for providing aromatics from a coal tar stream. A coal tar stream is provided, and the coal tar stream is fractionated into at least a naphtha range stream. The naphtha range stream is hydrotreated, and the hydrotreated naphtha range stream is separated to provide at least a naphthene rich stream. The naphthene rich stream is reformed or dehydrogenated to convert the naphthene. The dehydrogenated naphthene rich stream may be combined with a portion of a reformed crude oil hydrocarbon stream.

Periodische regenerierung von festen alkylierungskatalysator mit wasserstoff

Alkylierungsverfahren für benzol unter verwendung eines fluorierten siliciumoxid/aluminiumoxids und eines c6-c20 monoolefins

Fremgangsmåte for periodisk regenerering av en fast alkyleringskatalysator

Process for producing alkylated aromatic compounds

A process for producing alkylated aromatic compounds includes pyrolyzing a coal feed to produce a coke stream and a coal tar stream. The coal tar stream is hydrotreated and the resulting hydrotreated coal tar stream is cracked. A portion of the cracked coal tar stream is separated to obtain a fraction having an initial boiling point in the range of 60°C to 180°C, and an aromatics-rich hydrocarbon stream is extracted by contacting the fraction with one or more solvents. The aromatics-rich hydrocarbon stream is contacted with an alkylating agent to produce an alkylated aromatic stream, or the aromatics-rich hydrocarbon stream is reacted with an aliphatic compound or methanol in the presence of a catalyst to produce a methylated aromatic stream. The alkylated aromatic stream, the methylated aromatic stream, or both are separated into at least a benzene stream, a toluene stream, and a xylenes stream.

Catalyst regenerating method

Periodic regeneration of a deactivated solid alkylation catalyst with hydrogen

Periodic regeneration of a deactivated solid alkylation catalyst with hydrogen

Periodische Regenerierung von festen Alkylierungskatalysator mit Wasserstoff

Periodische Regenerierung von festen Alkylierungskatalysator mit Wasserstoff

Verfahren zur Herstellung von alkylaromatischen Verbindungen mit einem festen Katalysator.

Method of isoparafine alkylation by means of olefins containing 3 till 5 carbon atoms

Fremgangsmåte for periodisk regenerering av en fast alkyleringskatalysator

Sposób regeneracji katalizatora

1. Sposób regeneracji katalizatora, co najmniej częściowo zdezaktywowanego, zawierającego (1) produkt reakcji halogenku pierwszego metalu ze związanymi powierzchniowo grupami hydroksylowymi trudnotopliwego tlenku nieorganicznego, polegający na traktowaniu wodorem i usuwaniu zregenerowanego katalizatora, znamienny tym, że regeneruje się katalizator alkilowania zawierający wyżej określony (1) produkt reakcji oraz (2) zerowartościowy drugi metal, w którym to katalizatorzewymienionym halogenkiempierwszego metalu jest fluorek, chlorek lub bromek a pierwszy metaljest wybrany spośród glinu, cyrkonu, cyny, tantalu, tytanu, galu, antymonu, fosforu, żelaza, boru i ich mieszanin, natomiast zerowartościowy drugi metaljest wybrany spośród platyny, palladu, niklu, rutenu, rodu, osmu irydu i ich mieszanin, a wymieniony katalizator został przynajmniej częściowo zdezaktywowany w procesie katalizowania reakcji alkilowania w fazie ciekłej alkenu zawierającego od 2 do 6 atomów węgla alkanem mającym od 4 do 6 atomów węgla, w procesie polegającym na usuwaniu zasadniczo całej ilości ciekłych węglowodorów i traktowaniu uzyskanego katalizatorawodorem w obecności ciekłego izobutanu i źródła chlorku, pod ciśnieniem cząstkowym wodoru od 6,9 do 13790 kPa w czasie od 1 do 20 godzin w temperaturze od 10 do 300°C.

Periodic regeneration of a deactivated solid alkylation catalyst with hydrogen

Periodic regeneration of a deactivated solid alkylation catalyst with hydrogen

Způsob regenerace pevného alkylačního katalyzátoru

Desaktivované pevné katalyzátorové kompozice, které jsou reakčním produktem halogenidu kovu mající Friedel-Craftsovu aktivitu s povrchovou hydroxylovou skupinou anorganických oxidů, a obsahující kov s nulovým mocenstvím s hydrogenační schopností, používané jako katalyzátory v motorových palivech, se po desaktivaci regenerují zpracováním kompozice, zbavené alkylátu, za parciálního tlaku vodíku 6,9 - 3790 kPa po dobu 1 - 20 hodin při teplotě 10 - 300.sup.o.n.C.ŕ

Process for pyrolysis of a coal feed

A process for pyrolyzing a coal feed is described. A coal feed is pyrolyzed into a coal tar stream and a coke stream in a pyrolysis zone. The coal tar stream is separated into at least a pitch stream comprising aromatic hydrocarbons. The pitch stream is reacted in a reaction zone to add at least one functional group to an aromatic ring of the aromatic hydrocarbons in the pitch stream. The functionalized pitch stream is recycled to the pyrolysis zone.

Selective oxidation agent of hydrocarbons to synthesis gas based on separate particles of o-carrier and hydrocarbon activator

A solid material is presented for the partial oxidation of natural gas. The solid material includes a solid oxygen carrying agent and a hydrocarbon activation agent. The material precludes the need for gaseous oxygen for the partial oxidation and provides better control over the reaction.

Recovery process of solid alkylation catalyst