PROCESS FOR ALKYLATION USING LOW IONIC LIQUID VOLUME FRACTION

An alkylation process utilizing less than 10 vol % of a halometallate based ionic liquid catalyst is described. By decreasing the catalyst volume fraction, the level of subsequent undesirable reactions may be minimized. The total residence time is typically in the range of about 1 min to about 30 min. The alkylate typically has a research octane number of at least about 93, and the olefin conversion is typically at least about 96%. 1. An alkylation process comprising:passing an isoparaffin having from 4 to 10 carbon atoms to an alkylation reactor; andpassing an olefin having from 3 to 10 carbon atoms to the alkyation reactor, wherein the alkylation reactor contains a halometallate based ionic liquid catalyst for reacting the olefin and isoparaffin to generate an alkylate having a research octane number of at least about 93, wherein the alkylation reactor is operated at reaction conditions comprising an operating temperature greater than about 20° C., a molar ratio of isoparaffin to olefin of less than about 20:1, an overall olefin feed rate of greater than about 30 mol olefin/mol ionic liquid catalyst/hr, a total residence time in a range of about 1 min to about 30 min, and less than about 10 vol % of the halometallate based ionic liquid catalyst.2. The process of wherein the halometallate based ionic liquid catalyst has a viscosity of less than about 120 cSt at a temperature of 25° C. claim 1 , and wherein there is less than about 5 vol % of the halometallate based ionic liquid catalyst.3. The process of wherein the halometallate based ionic liquid catalyst has a viscosity of less than about 100 cSt at a temperature of 25° C. claim 1 , and wherein there is less than about 4 vol % of the halometallate based ionic liquid catalyst.4. The process of wherein the halometallate based ionic liquid catalyst has a viscosity of less than about 60 cSt at a temperature of 25° C. claim 1 , and wherein there is less than about 3 vol % of the halometallate based ionic liquid ...

PROCESSES FOR PRODUCING A FUEL FROM A RENEWABLE FEEDSTOCK

Processes for the production of transportation fuel from a renewable feedstock. A gaseous mixture of carbon monoxide and hydrogen is used to deoxygenate and hydrogenate the glycerides to produce long chain hydrocarbons. Water is also introduced into the reaction zone to increase the amount of hydrogen and to increase the utilization of carbon monoxide within the reaction zone. Synthesis gas may also be used to supply at least a portion of the gaseous mixture of carbon monoxide and hydrogen. The amount of hydrogen equivalents in the reaction zone is at least 100% of a stoichiometric hydrogen demand within the reaction zone.

Process for increasing a mole ratio of methyl to phenyl

One exemplary embodiment can be a process for increasing a mole ratio of methyl to phenyl of one or more aromatic compounds in a feed. The process can include reacting an effective amount of one or more aromatic compounds and an effective amount of one or more aromatic methylating agents to form a product having a mole ratio of methyl to phenyl of at least about 0.1:1 greater than the feed.

Process for alkylation using low ionic liquid volume fraction

An alkylation process utilizing less than 10 vol % of a halometallate based ionic liquid catalyst is described. By decreasing the catalyst volume fraction, the level of subsequent undesirable reactions may be minimized. The total residence time is typically in the range of about 1 min to about 30 min. The alkylate typically has a research octane number of at least about 93, and the olefin conversion is typically at least about 96%.

HIGH EFFICIENCY PROCESSES FOR OLEFINS, ALKYNES, AND HYDROGEN CO-PRODUCTION FROM LIGHT HYDROCARBONS SUCH AS METHANE

High efficiency processes for producing olefins, alkynes, and hydrogen co-production from light hydrocarbons are disclosed. In one version, the method includes the steps of combusting hydrogen and oxygen in a combustion zone of a pyrolytic reactor to create a combustion gas stream, transitioning a velocity of the combustion gas stream from subsonic to supersonic in an expansion zone of the pyrolytic reactor, injecting a light hydrocarbon into the supersonic combustion gas stream to create a mixed stream including the light hydrocarbon, transitioning the velocity of the mixed stream from supersonic to subsonic in a reaction zone of the pyrolytic reactor to produce acetylene, and catalytically hydrogenating the acetylene in a hydrogenation zone to produce ethylene. In certain embodiments, the carbon efficiency is improved using methanation techniques. 1. A method of making alkenes and alkynes , the method comprising:(a) combusting a fuel and an oxidizer in a combustion zone of a pyrolytic reactor to create a combustion gas stream;(b) transitioning a velocity of the combustion gas stream from subsonic to supersonic in an expansion zone of the pyrolytic reactor;(c) injecting a light hydrocarbon into the supersonic combustion gas stream to create a mixed stream including the light hydrocarbon;(d) transitioning the velocity of the mixed stream from supersonic to subsonic in a reaction zone of the pyrolytic reactor to produce an alkyne; and(e) catalytically hydrogenating the alkyne in a hydrogenation zone to produce an alkene.2. The method of wherein:the fuel is hydrogen,the oxidizer is oxygen,the light hydrocarbon is methane,the alkyne is acetylene, andthe alkene is ethylene.3. The method of wherein:transitioning the velocity of the mixed stream from supersonic to subsonic in step (d) forms a shockwave resulting in an increase in pressure and temperature of the mixed stream.4. The method of wherein:a first temperature of the mixed stream immediately upstream of the shock ...

Process for increasing a mole ratio of methyl to phenyl

One exemplary embodiment can be a process for increasing a mole ratio of methyl to phenyl of one or more aromatic compounds in a feed. The process can include reacting an effective amount of one or more aromatic compounds and an effective amount of one or more aromatic methylating agents to form a product having a mole ratio of methyl to phenyl of at least about 0.1:1 greater than the feed.

Process for the synthesis of aromatic dicarboxylic acids

A method is provided for synthesizing an aromatic carboxylic acid compound comprising providing an aromatic compound or an aromatic compound with at least one carboxylic group; providing a metal hydroxide and at least one carboxylate to produce a mixture; and adding carbon dioxide to the mixture under pressures from about atmospheric to 1000 psig and sufficient heat for a time sufficient to produce aromatic carboxylic acid compounds. The aromatic carboxylic acid compounds may include terephthalic acid, naphthalic acid, thiophene dicarboxylic acid, pyridine dicarboxylic acid, carbazole dicarboxylic acid, and dibenzothiophene dicarboxylic acid.

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 ...

DISPROPORTIONATION OF HYDROCARBONS USING SOLID ACID CATALYSTS

A hydrocarbon disproportionation process is described. The process includes contacting a hydrocarbon feed in a disproportionation reaction zone with a disproportionation catalyst in the presence of hydrogen and an added chloride promoter under disproportionation conditions including to obtain disproportionation products, wherein the disproportionation catalyst comprises a solid catalyst comprising a refractory inorganic oxide having a metal halide dispersed thereon. 1. A hydrocarbon disproportionation process comprising:contacting a hydrocarbon feed in a disproportionation reaction zone with a disproportionation catalyst in the presence of hydrogen and an added chloride promoter under disproportionation conditions to obtain disproportionation products, wherein the disproportionation catalyst comprises a solid catalyst comprising a refractory inorganic oxide having a metal halide dispersed thereon.2. The process of wherein the disproportionation catalyst further comprises a Group VIII metal component dispersed thereon.3. The process of wherein the hydrogen is present in a mole ratio of hydrogen to hydrocarbon feed of greater than 0:1 to about 0.5:1.4. The process of wherein the chloride concentration from the added chloride promoter is in a range of greater than 0 to about 5000 ppm and a mole ratio of hydrogen to chloride from the added chloride promoter is in a range of greater than 0:1 to about 5000:1.5. The process of wherein a selectivity for disproportionation is at least about 25%.6. The process of wherein the hydrocarbon feed comprises alkanes having 4 to 7 carbon atoms.7. The process of wherein the disproportionation conditions include at least one of: a temperature in a range of about 100° C. to about 250° C. claim 1 , a pressure in a range of about 0 MPa (g) to about 13.8 MPa (g) claim 1 , and a liquid hourly space velocity of about 0.25 hrto about 10 hr.8. The process of wherein the added chloride promoter comprises carbon tetrachloride claim 1 , ...

IONIC LIQUID ALKYLATION OF 1-BUTENE TO PRODUCE 2,5-DIMETHYLHEXANE

A process for producing dimethylhexanes (DMH) is provided. The DMH can be used to produce p-xylene. The process involves the alkylation of isobutane and 1-butene using an ionic liquid to produce naphtha that is rich in DMH. The DMH is then converted in high selectivity to xylene, including p-xylene, by dehydrocyclization. 1. A process for producing dimethylhexane comprising:introducing a stream comprising isobutane and a stream comprising 1-butene or a stream comprising isobutane and 1-butene to an alkylation reaction zone to form a reaction mixture, the stream comprising 1-butene or the stream comprising isobutane and 1-butene containing less than about 50 wt % total of 2-butene and isobutene; andalkylating the isobutane and the 1-butene in the alkylation reaction zone in the presence of a haloaluminate ionic liquid catalyst under alkylation conditions to form a stream rich in dimethylhexane, the stream rich in dimethylhexane having a ratio of dimethylhexane to trimethylpentane of at least about 2:1.2. The process of wherein the haloaluminate ionic liquid catalyst comprises a chloroaluminate ionic liquid catalyst claim 1 , a bromoaluminate ionic liquid catalyst claim 1 , or combinations thereof.4. The process of wherein the stream rich in dimethylhexane comprises at least about 25 wt % 2 claim 1 ,5-dimethylhexane based on a total weight of dimethylhexane claim 1 , or at least about 25 wt % 2 claim 1 ,4-dimethylhexane based on a total weight of dimethylhexane claim 1 , or both.5. The process of wherein a ratio of isobutane to 1-butene is in a range of about 1:1 to about 50:1.6. The process of wherein the alkylation conditions include a temperature in a range of about −20° C. to about 100° C. claim 1 , and a pressure in a range of about 0.101 MPa to about 8.0 MPa.7. The process of wherein a ratio of catalyst to olefins is in a range of about 0.1:1 to about 10:1.8. The process of claim further comprising stirring the reaction mixture and the acidic ionic liquid ...

METHODS FOR CONVERTING PLASTIC TO WAX

Methods for converting plastic to wax are provided. In one embodiment, a method for converting a waste plastic to wax includes introducing the waste plastic into a chamber and adding hydrogen to the chamber. The method includes heating the waste plastic and hydrogen sufficiently to thermally depolymerize the waste plastic to form a wax product comprising paraffin and olefin compounds. 1. A method for converting a waste plastic to wax , the method comprising the steps of:introducing the waste plastic into a chamber;adding hydrogen to the chamber;heating the waste plastic and hydrogen sufficiently to thermally depolymerize the waste plastic to form a wax product comprising paraffin and olefin compounds.2. The method of further comprising providing the chamber with a depolymerization catalyst selected from solid acid catalysts claim 1 , liquid acid catalysts claim 1 , radical initiators claim 1 , hydrogenation catalysts claim 1 , zeolites claim 1 , and catalysts on supports.3. The method of wherein:melting the waste plastic comprises heating the waste plastic to a temperature of about 100° C. to about 150° C.; andheating the waste plastic and hydrogen comprises heating the waste plastic and hydrogen to a temperature of from about 300° C. to about 500° C.4. The method of wherein heating the waste plastic and hydrogen comprises forming a polyethylene wax product comprising paraffin and olefin compounds in a paraffin:olefin ratio of at least about 1.1:1 and having a weight average molecular weight of from about 5000 gram per mole (g/mol) to about 15000 g/mol.5. The method of wherein introducing the waste plastic into a chamber comprises introducing the waste plastic to a chamber in a batch process.6. The method of wherein hydrogen is added to the chamber after the waste plastic is introduced into the chamber.7. A method for converting a plastic to wax claim 1 , the method comprising the steps of:contacting the plastic with hydrogen; andheating the plastic and the hydrogen ...

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 ...

PROCESS FOR THE SELECTIVE HYDROGENATION OF ACETYLENE TO ETHYLENE

A process for a liquid phase selective hydrogenation of acetylene to ethylene in a reaction zone. In order to decrease the selectivity to C+ hydrocarbons, the concentration of acetylene in solvent is lowered by recycling solvent, using a split feed injection, or both. The streams can be split in to equal or unequal portions. A hot separator may be used to separate solvent from the reactor effluent, and the solvent may be recovered and used to decrease the concentration of acetylene in the solvent. 1. A process for a liquid phase selective hydrogenation of acetylene to ethylene comprising:contacting acetylene from an acetylene rich stream with hydrogen in the presence of a catalyst under hydrogenation reaction conditions in a reaction zone to produce a reaction effluent;separating the reaction effluent in a separation zone into an overhead stream and a bottoms stream, the overhead stream being an ethylene rich stream; and,{'sub': '4', 'decreasing an amount of C+ hydrocarbons in the bottoms stream by decreasing a concentration of acetylene in at least a portion of the acetylene rich stream.'}2. The process of further comprising:combining a fraction of the bottoms stream from the separation zone with at least a portion of the acetylene rich stream.3. The process of wherein the acetylene rich stream includes solvent and wherein the bottoms stream from the separation zone includes solvent.4. The process of further comprising:splitting the acetylene rich stream into at least two acetylene rich split streams; and,injecting each acetylene rich split stream into the reaction zone.5. The process of wherein the reaction zone comprises a reactor with at least two beds claim 4 , each bed containing catalyst and further comprising:injecting a portion of acetylene rich stream into each bed of the reaction zone.6. The process of claim 4 , wherein the acetylene rich stream are split into unequal amounts.7. The process of claim 4 , further comprising:combining a fraction of the ...

Process for the selective hydrogenation of acetylene to ethylene

A process for a liquid phase selective hydrogenation of acetylene to ethylene in a reaction zone in which acetylene is contacted with hydrogen under hydrogenation conditions and a molar ratio of hydrogen to acetylene in the reaction zone is at least 5, preferably at least 9. A molar ratio of hydrogen to carbon monoxide is preferably approximately 10. The acetylene is preferably absorbed in a solvent.

Metallo aluminophosphate molecular sieve with novel crystal morphology and methanol to olefin process using the sieve

A catalyst for converting methanol to light olefins along with the process itself are disclosed and claimed. The catalyst is a metalloaluminophosphate molecular sieve having the empirical formula (ELxAlyPz)O2 where EL is a metal such as silicon or magnesium and x, y and z are the mole fractions of EL, Al and P respectively. The molecular sieve has a crystal morphology in which the average smallest crystal dimension is at least 0.1 microns. Use of this catalyst gives a product with a larger amount of ethylene versus propylene.

Enhanced light olefin production

A process is disclosed for enhancing the production of light olefins with a catalytic reaction zone containing small pore zeolitic and non-zeolitic catalysts which can significantly improve the yield of ethylene and propylene in a process for the conversion of light olefins having four carbon atoms per molecule and heavier. Specifically, a C 4 olefin stream from an ethylene production complex is converted in a reaction zone over a non-zeolitic catalyst at effective conditions to produce a product mixture containing ethylene and propylene. Ethylene and propylene are separated from the product mixture and recovered. A portion of the remaining heavy hydrocarbons and paraffins may be recycled to the reaction zone for further conversion, or oligomerized to produce valuable downstream products. The additional step of removing iso-olefins from the recycle stream provided significant advantages. The process of the present invention may be applied in commercial ethylene plants, in petroleum refining catalytic cracking operations, and in processes for the conversion of oxygenates such as methanol-to-olefins to enhance the production of ethylene and propylene.

Methanol conversion process with catalyst containing a hydrothermally treated sapo molecular sieve

A silicoaluminophosphate molecular sieve is hydrothermally treated at temperatures in excess of about 700°C for periods sufficient to destroy a large proportion of their acid sites while retaining at least 80 percent of their crystallinity to form a catalyst for converting methanol to lower olefins. This catalyst shows increased catalyst life, increased selectivity for C2 - C3 olefins and decreased selectivity for paraffin production relative to the untreated molecular sieve.

Improved process for the alkylation of alkanes with C3-C5-haloalkylene in the presence of a solid acid catalyst

Converting methanol to light olefins using small particles of elapo molecular sieve

Methanol is converted to light olefins in a conversion process using a catalyst catalyst comprising a metal aluminophosphate molecular sieve having the empirical formula (EL x Al y P z)O2 where EL is a metal and x, y and z are mole fractions of El, Al and P respectively where preferred metals are silicon, magnesium and cobalt, with silicon especially preferred and where the metal aluminophosphate is composed of particles at least 50% of which have a particle size less than 1.0 µm and no more than 10% of the particles have a particle size greater than 2.0 µm. It is also preferred that the metal content (x) of the metal aluminophosphate be from about 0.005 and 0.05 mole fraction. The catalyst containing the small particles of the metal aluminophosphate is also part of the invention.

Oil Recovery by In-Situ Cracking and Hydrogenation

Enhanced recovery of crude oil from an oil well is provided by in-situ cracking of an oxygenated organic compound to form hydrogen. The crude oil is then hydrogenated and hydrogenation reaction products and crude oil are recovered from the oil well.

Converting methanol to light olefins using small particles of elapo molecular sieve

Methanol is converted to light olefins in a conversion process using a catalyst catalyst comprising a metal aluminophosphate molecular sieve having the empirical formula (EL x Al y P z)O2 where EL is a metal and x, y and z are mole fractions of El, Al and P respectively where preferred metals are silicon, magnesium and cobalt, with silicon especially preferred and where the metal aluminophosphate is composed of particles at least 50% of which have a particle size less than 1.0 µm and no more than 10% of the particles have a particle size greater than 2.0 µm. It is also preferred that the metal content (x) of the metal aluminophosphate be from about 0.005 and 0.05 mole fraction. The catalyst containing the small particles of the metal aluminophosphate is also part of the invention.

Metallo aluminophosphate molecular sieve with cubic crystal morphology and methanol to olefin process using the sieve

A catalyst for converting methanol to light olefins along with the process itself are disclosed and claimed. The catalyst is a metalloaluminophosphate molecular sieve having the empirical formula (ELxAlyPz)O2 where EL is a metal such as silicon or magnesium and x, y and z are the mole fractions of EL, Al and P respectively. The molecular sieve has predominantly a plate crystal morphology in which the average smallest crystal dimension is at least 0.1 microns and has an aspect ratio of no greater than 5. Use of this catalyst gives a product with a larger amount of ethylene versus propylene.

Process for increasing methyl to phenyl mole ratios and reducing benzene content in a motor fuel product

One exemplary embodiment can be a process for increasing a mole ratio of methyl to phenyl of one or more aromatic compounds in a feed. The process can include reacting an effective amount of one or more aromatic compounds and an effective amount of one or more non-aromatic compounds to convert 90%, by weight, of one or more C6+ non-aromatic compounds.

Metallo aluminophosphate molecular sieve with cubic crystal morphology and methanol to olefin process using the sieve

Methanol conversion process with catalyst containing a hydrothermally treated sapo molecular sieve

Enhancement of molecular sieve performance

A catalyst for converting methanol to light olefins and the process for making and using the catalyst are disclosed and claimed. SAPO-34 is a specific catalyst that benefits from its preparation in accordance with this invention. A seed material is used in making the catalyst that has a higher content of the EL metal than is found in the principal part of the catalyst. The molecular sieve has predominantly a roughly rectangular parallelepiped morphology crystal structure with a lower fault density and a better selectivity for light olefins.

Process for the isomerization of dimethylnaphthalenes

Superior isomerization performance is obtained in an isomerization process employing a catalytic composition comprising a Group VIII noble metal and a hydrogen form mordenite incorporated with alumina. The superior isomerization performance is achieved using a catalyst composition having a surface area of at least 580 m 2 /g. A novel method of preparing an isomerization catalyst having a surface area of at least 580 m 2 /g is characterized by contacting a formed catalytic composite with an acidic aqueous solution prior to addition of the Group VIII noble metal. The isomerization process is particularly useful in the isomerization of a dimethylnaphthalene containing feedstock into a product that contains a higher concentration of the 2,6-dimethylnaphthalene isomer than did the feedstock.

Combination process for enhanced light olefin production

The production of light olefins is enhanced with a catalytic reaction zone containing small pore zeolitic and non-zeolitic catalysts which can significantly improve the yield of ethylene and propylene in a process for the conversion of light olefins having four carbon atoms per molecule and heavier. Specifically, a C4 olefin stream from an ethylene production complex is converted in a reaction zone over a non-zeolitic catalyst at effective conditions to produce a product mixture containing ethylene and propylene. Ethylene and propylene are separated from the product mixture and recovered. A portion of the remaining heavy hydrocarbons and paraffins may be recycled to the reaction zone for further conversion, or oligomerized to produce valuable downstream products. The additional step of removing iso-olefins from the recycle stream provided significant advantages. The combination process of the present invention may be applied in commercial ethylene plants, in petroleum refining catalytic cracking operations, and in processes for the conversion of oxygenates such as methanol-to-olefins to enhance the production of ethylene and propylene.

Protection of solid acid catalysts from damage by volatile species

The invention provides a method to avoid catalyst damage and achieve longer catalyst life by selecting appropriate materials for reactor spacers, liners, catalyst binders, and supports, in particular, by not using crystalline silica-containing and high phosphorus-containing materials, if the presence of even small amount of steam is anticipated. In addition, alkali metals and alkaline earth metals are avoided due to potential damage to the catalyst.

Improved process for alkylation of alkanes with C3 to C5 alkyl halides using a solid acid catalyst

Improved process for alkylation of alkanes with c3 to c5 alkenes using a solid acid catalyst

Although olefins commonly are used to alkylate alkanes using various solid acid catalysts, the process is severely hampered by short catalyst lifetimes attending substantial olefin oligomerization. This problem is avoided by using an alkyl halide as the alkylating agent. Thus, alkylation of isobutane by olefin in the presence of a modified, AlCl3-type Friedel-Crafts catalyst at 30°C falls to about 77% in four hours, whereas alkylation with sec-butyl chloride at the same conditions fell to 88% over 30 hours.

Alkylation/transalkylation process for selective production of monoalkylated aromatics

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.

Process to Maximize Methane Content in Natural Gas Stream

The present invention relates to a hydrogenolysis process and catalyst for conversion of ethane to methane in a natural gas stream when such streams contain large quantities of ethane. Such natural gas streams include the product of the in situ treatment of oil shale to produce oil and gas. Hydrogenolysis catalysts have been identified that produce high yields of ethane at low light-off temperatures.

process for increasing a methyl to phenyl molar ratio of one or more aromatic compounds in a feed

processo para aumentar uma razão molar de metila para fenila de um ou mais compostos aromáticos em uma alimentação. uma forma de realização exemplar pode ser um processo para aumentar uma razão molar de metila para fenila de um ou mais compostos aromáticos em uma alimentação. o processo pode incluir reagir uma quantidade efetiva de um ou mais compostos aromáticos e uma quantidade efetiva de um ou mais agentes de metilação aromáticos para formar um produto tendo uma razão molar de metila para fenila de pelo menos cerca de 0,1:1 maior do que a alimentação. process for increasing a methyl to phenyl molar ratio of one or more aromatic compounds in a feed. An exemplary embodiment may be a process for increasing a methyl to phenyl molar ratio of one or more aromatic compounds in a feed. the process may include reacting an effective amount of one or more aromatic compounds and an effective amount of one or more aromatic methylating agents to form a product having a methyl to phenyl molar ratio of at least about 0.1: 1 greater than that the food.

High efficiency processes for olefins, alkynes, and hydrogen co-production from light hydrocarbons such as methane

High efficiency processes for producing olefins, alkynes, and hydrogen co-production from light hydrocarbons are disclosed. In one version, the method includes the steps of combusting hydrogen and oxygen in a combustion zone of a pyrolytic reactor to create a combustion gas stream, transitioning a velocity of the combustion gas stream from subsonic to supersonic in an expansion zone of the pyrolytic reactor, injecting a light hydrocarbon into the supersonic combustion gas stream to create a mixed stream including the light hydrocarbon, transitioning the velocity of the mixed stream from supersonic to subsonic in a reaction zone of the pyrolytic reactor to produce acetylene, and catalytically hydrogenating the acetylene in a hydrogenation zone to produce ethylene. In certain embodiments, the carbon efficiency is improved using methanation techniques.

An aromatic alkylating agent and an aromatic production apparatus

One exemplary embodiment can be a process using an aromatic methylating agent. Generally, the process includes reacting an effective amount of the aromatic methylating agent having at least one of an alkane, a cycloalkane, an alkane radical, and a cycloalkane radical with one or more aromatic compounds. As such, at least one of the one or more aromatic compounds may be converted to one or more higher methyl substituted aromatic compounds to provide a product having a greater mole ratio of methyl to phenyl than a feed.

Conversion of acyclic symmetrical olefins to higher and lower carbon number olefin products

Processes for the conversion, under conditions and with a catalyst system effective for olefin metathesis, of hydrocarbon feedstocks comprising an acyclic symmetrical olefin (e.g., butene-2) are described. Olefin products of lower and higher carbon numbers (e.g., propylene and pentene) are formed in the presence of a catalyst comprising a solid support and a tungsten hydride bonded to alumina present in the support. This occurs despite the olefin metathesis reaction mechanism leading to a degenerative result, without any expected production of different carbon number products from acyclic symmetrical olefins.

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.

Improved process for alkylation of alkanes with C3 to C5 alkenes using a solid acid catalyst

Although olefins commonly are used to alkylate alkanes using various solid acid catalysts, the process is severely hampered by short catalyst lifetimes attending substantial olefin oligomerization. This problem is avoided by using an alkyl halide as the alkylating agent. Thus, alkylation of isobutane by olefin in the presence of a modified, AlCl 3 -type Friedel-Crafts catalyst at 30°C falls to about 77% in four hours, whereas alkylation with sec-butyl chloride at the same conditions fell to 88% over 30 hours.

Enhancement of Molecular Sieve Performance

A catalyst for converting methanol to light olefins and the process for making and using the catalyst are disclosed and claimed. SAPO-34 is a specific catalyst that benefits from its preparation in accordance with this invention. A seed material is used in making the catalyst that has a higher content of the EL metal than is found in the principal part of the catalyst. The molecular sieve has predominantly a roughly rectangular parallelepiped morphology crystal structure with a lower fault density and a better selectivity for light olefins.

Method of cumene's selective production

A method of selective production of cumene where the flow of charge containing propylene and benzene is fed into the alkylation reaction zone containing a solid catalyst on a base of phosphoric acid maintained under conditions in which alkylation of the aromatic substrate in the liquid phase occurs, whereas a) in the first separation zone the product from the alkylation reaction zone and from the below mentioned transalkylation reaction zone is divided into fractions that include the fraction of aromatic substrate, fraction of essentially pure monoalkylation aromatic product and fraction containing compounds with boiling temperature higher than the boiling temperature of the required monoalkyl aromatic compound, b) the fraction occurring from the first separation zone and containing compounds with boiling temperature higher than the boiling temperature of the required monoalkyl aromatic compound are divided in the second separation zone into a fraction rich in dialkyl aromatic compounds and two fractions with boiling temperature both higher and lower than the boiling temperature of the fraction rich in dialkyl aromatic compounds, c) the flow of charge formed by the aromatic substrate and in the second separation zone the separated hydrocarbon fraction rich in dialkyl aromatic hydrocarbon is fed into the transalkylation reaction zone, where it is maintained under conditions in which the transalkylation of the hydrocarbon fraction rich in dialkyl aromatic compounds occurs causing the product of the transalkylation reaction zone, and d) the product of the transalkylation zone of level c) is fed into the first separation zone in level a).<IMAGE>

Metallo aluminophosphate molecular sieve with cubic crystal morphology and methanol to olefin process using the sieve

A catalyst for converting methanol to light olefins along with the process itself are disclosed and claimed. The catalyst is a metalloaluminophosphate molecular sieve having the empirical formula (EL x Al y P z )O 2 where EL is a metal such as silicon or magnesium and x, y and z are the mole fractions of EL, Al and P respectively. The molecular sieve has predominantly a plate crystal morphology in which the average smallest crystal dimension is at least 0.1 microns and has an aspect ratio of no greater than 5. Use of this catalyst gives a product with a larger amount of ethylene versus propylene.

method for making alkenes and alkynes

Aromatics Co-Production in a Methanol-to-Propylene Unit

The present invention provides a reactor system having: (1) a first reactor receiving an oxygenate component and a hydrocarbon component and capable of converting the oxygenate component into a light olefin and the hydrocarbon component into alkyl aromatic compounds; (2) a separator system for providing a first product stream containing a C 3 olefin, a second stream containing a C 7 aromatic, and a third stream containing C 8 aromatic compounds; (3) a first line connecting the separator to the inlet of the first reactor for conveying the second stream to the first reactor; (4) a second line in fluid communication with the separator system for conveying the C 3 olefin to a propylene recovery unit, and (4) a third line in fluid communication with the separator system for conveying the C 8 aromatic compounds to a xylene recovery unit.

Methods for converting plastic to wax

Methods for converting plastic to wax are provided. In one embodiment, a method for converting a waste plastic to wax includes introducing the waste plastic into a chamber and adding hydrogen to the chamber. The method includes heating the waste plastic and hydrogen sufficiently to thermally depolymerize the waste plastic to form a wax product comprising paraffin and olefin compounds.

Protection of solid acid catalysts from damage by volatile species

The invention provides a method to avoid catalyst damage and achieve longer catalyst life by selecting appropriate materials for reactor spacers, liners, catalyst binders, and supports, in particular, by not using crystalline silica-containing and high phosphorus-containing materials, if the presence of even small amount of steam is anticipated. In addition, alkali metals and alkaline earth metals are avoided due to potential damage to the catalyst.

Enhancement of molecular sieve performance

A catalyst for converting methanol to light olefins and the process for making and using the catalyst are disclosed and claimed. SAPO-34 is a specific catalyst that benefits from its preparation in accordance with this invention. A seed material is used in making the catalyst that has a higher content of the EL metal than is found in the principal part of the catalyst. The molecular sieve has predominantly a roughly rectangular parallelepiped morphology crystal structure with a lower fault density and a better selectivity for light olefins.

Process for increasing methyl to phenyl mole ratios and reducing benzene content in a motor fuel product

One exemplary embodiment can be a process for increasing a mole ratio of methyl to phenyl of one or more aromatic compounds in a feed. The process can include reacting an effective amount of one or more aromatic compounds and an effective amount of one or more non-aromatic compounds to convert 90%, by weight, of one or more C6+ non-aromatic compounds.

Two-stage process for producing diisopropyl ether using catalytic distillation

A process for the efficient production of diisopropyl ether where catalytic distillation is used to increase the yield of product beyond thermodynamic equilibrium limitations has been developed. In a hydration zone the propylene in a feedstock is reacted with water in the presence of a catalyst to effect hydration to produce an effluent stream containing at least water, unreacted propylene, and isopropyl alcohol, and then, in an etherification zone, at least a portion of the effluent stream is further reacted by catalytic distillation in the presence of a catalyst to effect reaction of propylene and isopropyl alcohol to form diisopropyl ether while concurrently separating an organic portion containing the diisopropyl ether and an aqueous portion, and collecting the organic portion containing the diisopropyl ether.

An aromatic alkylating agent and an aromatic production apparatus

One exemplary embodiment can be a process using an aromatic methylating agent. Generally, the process includes reacting an effective amount of the aromatic methylating agent having at least one of an alkane, a cycloalkane, an alkane radical, and a cycloalkane radical with one or more aromatic compounds. As such, at least one of the one or more aromatic compounds may be converted to one or more higher methyl substituted aromatic compounds to provide a product having a greater mole ratio of methyl to phenyl than a feed.

Conversion of butylene to propylene under olefin metathesis conditions

Processes for the conversion, under conditions and with a catalyst system effective for olefin metathesis, of hydrocarbon feedstocks comprising butylene, for example all or a large proportion of a single C4 olefin isomer such as butene-1, are described. Olefin products, and particularly propylene, are formed in the presence of a catalyst comprising a solid support and a tungsten hydride bonded to alumina present in the support. This occurs despite the expectation that the olefin metathesis reaction mechanism leads to the formation of olefin products having other carbon numbers.

Erhöhung der leistung eines molekularsiebs

Verfahren zur umsetzung von methanol in niedrigen olefinen mit verwendung kleiner teilchen von elapo molekularsieben

High-temperature pyrolysis of plastics to monomers

A high-temperature plastic pyrolysis process that can produce high yields of ethylene, propylene and other light olefins from waste plastics is disclosed. The plastic feed is pyrolyzed at a high temperature of 600 to 900C directly to monomers, such as ethylene and propylene. During pyrolysis, the plastic feed is contacted with a diluent gas stream at a mole ratio of carbon feed to diluent gas of 0.6 to 20.

Process for the selective hydrogenation of acetylene to ethylene

A process for the synthesis of aromatic dicarboxylic acids

A method is provided for synthesizing an aromatic carboxylic acid compound comprising providing an aromatic compound or an aromatic compound with at least one carboxylic group; providing a metal hydroxide and at least one carboxylate to produce a mixture; and adding carbon dioxide to the mixture under pressures from about atmospheric to 1000 psig and sufficient heat for a time sufficient to produce aromatic carboxylic acid compounds. The aromatic carboxylic acid compounds may include terephthalic acid, naphthalic acid, thiophene dicarboxylic acid, pyridine dicarboxylic acid, carbazole dicarboxylic acid, and dibenzothiophene dicarboxylic acid.

A process for the synthesis of aromatic dicarboxylic acids

A method is provided for synthesizing an aromatic carboxylic acid compound comprising providing an aromatic compound or an aromatic compound with at least one carboxylic group; providing a metal hydroxide and at least one carboxylate to produce a mixture; and adding carbon dioxide to the mixture under pressures from about atmospheric to 1000 psig and sufficient heat for a time sufficient to produce aromatic carboxylic acid compounds. The aromatic carboxylic acid compounds may include terephthalic acid, naphthalic acid, thiophene dicarboxylic acid, pyridine dicarboxylic acid, carbazole dicarboxylic acid, and dibenzothiophene dicarboxylic acid.

A process for the synthesis of aromatic dicarboxylic acids

Alkane dehydrogenation catalyst and methods of converting alkanes to alkenes

Provided herein is an alkane dehydrogenation catalyst, a method of manufacturing an alkane dehydrogenation catalyst, and a method of converting alkanes to alkenes.

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.

Conversion of Butylene to Propylene Under Olefin Metathesis Conditions

Processes for the conversion, under conditions and with a catalyst system effective for olefin metathesis, of hydrocarbon feedstocks comprising butylene, for example all or a large proportion of a single C 4 olefin isomer such as butene-1, are described. Olefin products, and particularly propylene, are formed in the presence of a catalyst comprising a solid support and a tungsten hydride bonded to alumina present in the support. This occurs despite the expectation that the olefin metathesis reaction mechanism leads to the formation of olefin products having other carbon numbers.

Conversion of butylene to propylene under olefin metathesis conditions

Processes for the conversion, under conditions and with a catalyst system effective for olefin metathesis, of hydrocarbon feedstocks comprising butylene, for example all or a large proportion of a single C4 olefin isomer such as butene-1, are described. Olefin products, and particularly propylene, are formed in the presence of a catalyst comprising a solid support and a tungsten hydride bonded to alumina present in the support. This occurs despite the expectation that the olefin metathesis reaction mechanism leads to the formation of olefin products having other carbon numbers.

Conversion of butylene to propylene under olefin metathesis conditions

Conversion of butylene to propylene under olefin metathesis conditions

Processes for the conversion, under conditions and with a catalyst system effective for olefin metathesis, of hydrocarbon feedstocks comprising butylene, for example all or a large proportion of a single C4 olefin isomer such as butene-1, are described. Olefin products, and particularly propylene, are formed in the presence of a catalyst comprising a solid support and a tungsten hydride bonded to alumina present in the support. This occurs despite the expectation that the olefin metathesis reaction mechanism leads to the formation of olefin products having other carbon numbers.

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.

Process for the selective hydrogenation of acetylene to ethylene

A process for a liquid phase selective hydrogenation of acetylene to ethylene in a reaction zone in which acetylene is contacted with hydrogen under hydrogenation conditions and a molar ratio of hydrogen to acetylene in the reaction zone is at least (5), preferably at least (9). A molar ratio of hydrogen to carbon monoxide is preferably (10). The acetylene is preferably absorbed in a solvent.

Methanol conversion process with catalyst containing a hydrothermally treated sapo molecular sieve.

A SILICOALUMINOPHOSPHATE MOLECULAR SIEVE IS HYDROTHERMALLY TREATED AT TEMPERATURES IN EXCESS OF ABOUT 700?C FOR PERIODS SUFFICIENT TO DESTROY A LARGE PROPORTION OF THEIR ACID SITES WHILE RETAINING AT LEAST 80 PERCENT OF THEIR CRYSTALLINITY TO FORM A CATALYST FOR CONVERTING METHANOL TO LOWER OLEFINS. THIS CATALYST SHOWS INCREASED CATALYST LIFE, INCREASED SELECTIVITY FOR C2-C3 OLEFINS AND DECREASED SELECTIVITY FOR PARAFFIN PRODUCTION RELATIVE TO THE UNTREATED MOLECULAR SIEVE.

Conversion of plastics to monomers by pyrolysis

A plastic pyrolysis process that can produce high yields of ethylene, propylene and other light olefins from waste plastics is disclosed. The plastic feed is pyrolyzed at a low-temperature pyrolysis process and subsequently pyrolyzed in a high-temperature pyrolysis process directly to monomers, such as ethylene and propylene. Insufficiently pyrolyzed product from the low-temperature pyrolysis process can be fed to the high-temperature pyrolysis process while preserving the desired low-temperature product monomers.

A process for the synthesis of aromatic dicarboxylic acids

A method is provided for synthesizing an aromatic carboxylic acid compound comprising providing an aromatic compound or an aromatic compound with at least one carboxylic group; providing a metal hydroxide and at least one carboxylate to produce a mixture; and adding carbon dioxide to the mixture under pressures from about atmospheric to 1000 psig and sufficient heat for a time sufficient to produce aromatic carboxylic acid compounds. The aromatic carboxylic acid compounds may include terephthalic acid, naphthalic acid, thiophene dicarboxylic acid, pyridine dicarboxylic acid, carbazole dicarboxylic acid, and dibenzothiophene dicarboxylic acid.

Alkane Dehydrogenation Catalyst and Methods of Converting Alkanes to Alkenes

Provided herein is an alkane dehydrogenation catalyst, a method of manufacturing an alkane dehydrogenation catalyst, and a method of converting alkanes to alkenes.

Conversion of plastics to monomers by pyrolysis

A plastic pyrolysis process that can produce high yields of ethylene, propylene and other light olefins from waste plastics is disclosed. The plastic feed is pyrolyzed at a low-temperature pyrolysis process and subsequently pyrolyzed in a high-temperature pyrolysis process directly to monomers, such as ethylene and propylene. Insufficiently pyrolyzed product from the low-temperature pyrolysis process can be fed to the high-temperature pyrolysis process while preserving the desired low-temperature product monomers.

Conversion of plastics to monomers by pyrolysis

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.

High-temperature pyrolysis of plastics to monomers