Abstract: Methanol-to-gasoline (MTG) conversion may be performed with forward methanol processing. Methanol may be fed to a first reactor where it may be catalytically converted under dimethyl ether formation conditions in the presence of a first catalyst to form a product mixture comprising dimethyl ether (DME), methanol, and water. The DME may be separated from the methanol and the water and delivered to a second reactor. In the second reactor, the DME may be catalytically converted under MTG conversion conditions in the presence of a second catalyst to form a second product mixture comprising gasoline hydrocarbons and light hydrocarbon gas. The methanol and the water from the first reactor may be separated further to obtain substantially water-free methanol, which may be delivered to the second reactor. The separation of methanol from the water may be performed using the light hydrocarbon gas to effect stripping of the methanol.

Abstract: Methanol-to-gasoline (MTG) conversion may be performed with a methanol recycling. Methanol may be fed to a first reactor where it may be catalytically converted under dimethyl ether formation conditions in the presence of a first catalyst to form a product mixture comprising dimethyl ether (DME), methanol, and water. The DME may be separated from the methanol and the water and delivered to a second reactor. In the second reactor, the DME may be catalytically converted under MTG conversion conditions in the presence of a second catalyst to form a second product mixture comprising gasoline hydrocarbons and light hydrocarbon gas. The methanol and the water from the first reactor may be separated further to obtain substantially water-free methanol, which may be returned to the first reactor. The separation of methanol from the water may be performed using the light hydrocarbon gas to effect stripping of the methanol.

Abstract: Methanol-to-gasoline (MTG) conversion may be performed with a methanol recycling. Methanol may be fed to a first reactor where it may be catalytically converted under dimethyl ether formation conditions in the presence of a first catalyst to form a product mixture comprising dimethyl ether (DME), methanol, and water. The DME may be separated from the methanol and the water and delivered to a second reactor. In the second reactor, the DME may be catalytically converted under MTG conversion conditions in the presence of a second catalyst to form a second product mixture comprising gasoline hydrocarbons and light hydrocarbon gas. The methanol and the water from the first reactor may be separated further to obtain substantially water-free methanol, which may be returned to the first reactor. The separation of methanol from the water may be performed using the light hydrocarbon gas to effect stripping of the methanol.

Abstract: Methanol-to-gasoline (MTG) conversion may be performed with forward methanol processing. Methanol may be fed to a first reactor where it may be catalytically converted under dimethyl ether formation conditions in the presence of a first catalyst to form a product mixture comprising dimethyl ether (DME), methanol, and water. The DME may be separated from the methanol and the water and delivered to a second reactor. In the second reactor, the DME may be catalytically converted under MTG conversion conditions in the presence of a second catalyst to form a second product mixture comprising gasoline hydrocarbons and light hydrocarbon gas. The methanol and the water from the first reactor may be separated further to obtain substantially water-free methanol, which may be delivered to the second reactor. The separation of methanol from the water may be performed using the light hydrocarbon gas to effect stripping of the methanol.

Abstract: The present disclosure relates to a material preferably used in a guard bed, and having an increased capacity to adsorb catalyst poisons, as measured by collidine update at 200° C. The material is made by a method in which it is treated by being dried with a drying gas, preferably, at a temperature greater than about 200° C. The treated material may be used to remove impurities from untreated feed streams to, for example, aromatic alkylation and transalkylation processes, where such impurities act as catalyst poisons that cause deactivation of the acidic molecular sieve-based catalysts used, thereby increasing the cycle length of such catalysts.

Abstract: A process is described for converting at least one isomer of a dialkyl-substituted biphenyl compound, such as at least one 2,X? dialkylbiphenyl isomer (where X? is 2?, 3? and/or 4?), into at least one different isomer, 3,3?, 3,4? and/or 4,4? dialkylbiphenyl isomer. The process comprises contacting a feed comprising the dialkyl-substituted biphenyl compound isomer with an acid catalyst under isomerization conditions.

Abstract: The present disclosure relates to a material preferably used in a guard bed, and having an increased capacity to adsorb catalyst poisons, as measured by collidine update at 200° C. The material is made by a method in which it is treated by being dried with a drying gas, preferably, at a temperature greater than about 200° C. The treated material may be used to remove impurities from untreated feed streams to, for example, aromatic alkylation and transalkylation processes, where such impurities act as catalyst poisons that cause deactivation of the acidic molecular sieve-based catalysts used, thereby increasing the cycle length of such catalysts.

Abstract: The present disclosure relates to a method for treating a catalyst that is useful for producing mono-alkylaromatic compounds, the method comprises the steps of (a) contacting the untreated catalyst with water to produce water-contacted catalyst, and (b) drying the water-contacted catalyst with a drying gas without steam being formed at a temperature of less than 300° C. to produce a treated catalyst. The treatment is effective to improve the activity and catalyst selectivity. A process for producing a mono-alkylaromatic compound comprising such a catalyst treatment is also disclosed.

Abstract: This invention relates to process for producing biphenyl esters, the process comprising: (a) contacting a feed comprising toluene, xylene or mixtures thereof with hydrogen in the presence of a hydroalkylation catalyst to produce a hydroalkylation reaction product comprising (methylcyclohexyl)toluene, wherein the hydroalkylation catalyst comprises: 1) binder present at 40 wt % or less (based upon weight of final catalyst composition), 2) a hydrogenation component present at 0.2 wt % or less (based upon weight of final catalyst composition), and 3) an acidic component comprising a molecular sieve having a twelve membered (or larger) ring pore opening, channel or pocket and a largest pore dimension of 6.

Abstract: A catalyst composition comprises (i) a support; (ii) a dehydrogenation component comprising at least one metal or compound thereof selected from Groups 6 to 10 of the Periodic Table of Elements; and (iii) tin or a tin compound, wherein the tin is present in an amount of 0.01 wt % to about 0.25 wt %, the wt % based upon the total weight of the catalyst composition.

Abstract: Disclosed are (i) a process for making cyclohexylbenzene by benzene hydroalkylation with a low methylcyclopentylbenzene selectivity; and (ii) a process of making phenol and/or cyclohexanone from cyclohexylbenzene including a step of removing methylcyclopentylbenzene from the cyclohexylbenzene feed supplied to the oxidation step.

Abstract: The present invention provides a process for converting a feedstock comprising hydrocarbon compounds using a catalyst made by an improved method for manufacturing high quality porous crystalline MCM-56 material. One such conversion process involves production of monoalkylated aromatic compounds, particularly ethylbenzene and cumene, by the liquid or partial liquid phase alkylation of alkylatable aromatic compound, particularly benzene.

Abstract: A process for producing an alkylated aromatic compound comprises contacting an aromatic starting material and hydrogen with a plurality of catalyst particles under hydroalkylation conditions to produce an effluent comprising the alkylated aromatic compound, the catalyst comprising a composite of a solid acid, an inorganic oxide different from the solid acid and a hydrogenation metal, wherein the distribution of the hydrogenation metal in at least 60 wt % of the catalyst particles is such that the average concentration of the hydrogenation metal in the rim portion of a given catalyst particle is Crim, the average concentration of the hydrogenation metal in the outer portion of a given catalyst particle is Couter, the average concentration of the hydrogenation metal in the center portion of the given catalyst particle is Ccenter, where Crim/Ccenter?2.0 and/or Couter/Ccenter2.0. Also disclosed are rimmed catalyst and process for making phenol and/or cyclohexanone using the catalyst.

Abstract: A process for producing phenol and/or cyclohexanone is described in which cyclohexylbenzene is contacted with an oxygen-containing gas under conditions effective to produce an oxidation effluent comprising cyclohexylbenzene hydroperoxide and at least part of cyclohexylbenzene hydroperoxide is contacted with a cleavage catalyst under conditions effective to produce a cleavage effluent containing phenol and cyclohexanone. At least one of the oxidation effluent and the cleavage effluent contains at least one phenylcyclohexanol as a by-product and the process further comprises contacting the phenylcyclohexanol with a dehydration catalyst comprising a molecular sieve of the MCM-22 family under conditions effective to convert at least part of the phenylcyclohexanol to phenylcyclohexene.

Abstract: The present invention provides an improved method for manufacturing high quality porous crystalline MCM-56 material. It also relates to the MCM-56 material manufactured by the improved method, catalyst compositions comprising same and use thereof in a process for catalytic conversion of hydrocarbon compounds. One such conversion process involves production of monoalkylated aromatic compounds, particularly ethylbenzene and cumene, by the liquid or partial liquid phase alkylation of alkylatable aromatic compound, particularly benzene.

Abstract: In a process for producing para-xylene, benzene and/or toluene is alkylated with methanol in the presence of a catalyst under conditions including a temperature of at least 500° C. and an H2O partial pressure of at least 12 psia (83 kPaa). The catalyst comprises from 5 to 15 wt % ZSM-5, phosphorus or a compound thereof and a binder and has been steamed at a temperature of at least 900° C. The steamed catalyst has no more than two peaks in the 31P MAS NMR spectrum in the range of 0 to ?50 ppm.

Abstract: Methods are provided for liquid phase activation of dewaxing and/or hydrofinishing catalysts that include a molecular sieve or other acidic crystalline support. The methods are compatible with activating the catalysts as part of a catalyst system that also includes a hydrotreating catalyst.

Abstract: The present invention provides an improved process for producing an alkylated aromatic compound from an at least partially untreated alkylatable aromatic compound having catalyst poisons and an alkylating agent, wherein said alkylatable aromatic compound stream is treated to reduce catalyst poisons with a treatment composition having a surface area/surface volume ratio of greater than or equal to 30 in?1 (12 cm?1) in a treatment zone separate from an alkylation reaction zone under treatment conditions including a temperature of from about 30° C. to about 300° C. to form an effluent comprising said treated alkylatable aromatic compound.

Abstract: The present invention provides an improved process for producing an alkylated aromatic compound from an at least partially untreated alkylatable aromatic compound having catalyst poisons and an alkylating agent, wherein said alkylatable aromatic compound stream is treated to reduce catalyst poisons with a treatment composition having a surface area/surface volume ratio of greater than or equal to 30 in?1 (12 cm?1) in a treatment zone separate from an alkylation reaction zone under treatment conditions including a temperature of from about 30° C. to about 300° C. to form an effluent comprising said treated alkylatable aromatic compound.

Abstract: A process is described for converting at least one isomer of a dialkyl-substituted biphenyl compound, such as at least one 2,X? dialkylbiphenyl isomer (where X? is 2?, 3? and/or 4?), into at least one different isomer, 3,3?, 3,4? and/or 4,4? dialkylbiphenyl isomer. The process comprises contacting a feed comprising the dialkyl-substituted biphenyl compound isomer with an acid catalyst under isomerization conditions.