Abstract: Olefin separation processes may comprise: introducing a first aqueous salt stream and a mixed feed stream comprising at least one olefin to a salt ion membrane; obtaining an olefin-rich permeate stream and an olefin-lean retentate stream from the salt ion membrane, at least the olefin-lean retentate stream comprising a salt ion membrane aqueous salt phase; introducing the olefin-lean retentate stream to a separation device to obtain a first portion comprising a hydrocarbon stream and a second portion comprising the salt ion membrane aqueous salt phase; introducing to an absorption device the hydrocarbon stream and a second aqueous salt stream under conditions effective to promote olefin extraction, in which the salt ion membrane aqueous salt phase is provided as a portion of the second aqueous salt stream; and obtaining an olefin-rich aqueous salt stream from the absorption device that is provided as at least a portion of the first aqueous salt stream.

Abstract: A nonlimiting example method for producing a diesel boiling range composition comprises: oligomerizing an ethylene stream to a C4+ olefin stream in a first olefin oligomerization unit, wherein the C4+ olefin stream contains no greater than 10 wt% of methane, ethylene, and ethane combined in a first oligomerization; and wherein the ethylene stream contains at least 50 wt% ethylene, at least 2000 wppm ethane, no greater than 1000 wppm of methane, and no greater than 20 wppm each of carbon monoxide and hydrogen; oligomerizing the C4+ olefin stream and a propylene/C4+ olefin stream in a second oligomerization unit to produce an isoolefinic stream; wherein at least a portion of the isoolefinic stream is used to create the diesel boiling range composition.

Abstract: A method for producing an isoolefinic stream may include: oligomerizing an ethylene stream to a C4+ olefin stream in a first olefin oligomerization unit comprising a serial reactor and a lights removal column, wherein the C4+ olefin stream contains no greater than 10 wt % of methane, ethylene, and ethane combined; and wherein the ethylene stream contains at least 50 wt % ethylene, at least 2000 wppm ethane, no greater than 1000 wppm of methane, and no greater than 20 wppm each of carbon monoxide and hydrogen; and oligomerizing the C4+ olefin stream and a propylene/C4+ olefin stream in a second oligomerization unit to produce the isoolefinic stream.

Abstract: A method for producing a blended jet boiling range composition stream may include: oligomerizing an ethylene stream to a C4+ olefin stream in a first olefin oligomerization unit, wherein the C4+ olefin stream contains no greater than 10 wt % of methane, ethylene, and ethane combined; wherein the ethylene stream contains at least 50 wt % ethylene, at least 2000 wppm ethane, no greater than 1000 wppm of methane, and no greater than 20 wppm each of carbon monoxide and hydrogen; oligomerizing the C4+ olefin stream and a propylene/C4+ olefin stream in a second oligomerization unit to produce an isoolefinic stream; subjecting at least a portion of the isoolefinic stream to a hydroprocessing process with hydrogen as treat gas to produce an isoparaffinic stream having no greater than 10 wt % olefin content; and using least a portion of the isoparaffinic stream to create the blended jet boiling range.

Abstract: A method for washing an oligomerization reactor using by-product solvent recovered from the reactor can include: catalytically converting a monomer in a reactor section in a reaction mode in the presence of a catalyst to form a product stream comprising an oligomer, a by-product solvent, and a polymeric by-product; separating the product stream into a first fraction comprising the oligomer and a second fraction comprising a mixture of the by-product solvent and the polymeric by-product; and separating, in a thin film evaporator, the second fraction into a third fraction comprising the by-product solvent and a fourth fraction comprising the polymeric by-product.

Abstract: A method for washing an oligomerization reactor using by-product solvent recovered from the reactor can include: catalytically converting a monomer in a reactor section in a reaction mode in the presence of a catalyst to form a product stream comprising an oligomer, a by-product solvent, and a polymeric by-product; separating the product stream into a first fraction comprising the oligomer and a second fraction comprising a mixture of the by-product solvent and the polymeric by-product; and separating, in a thin film evaporator, the second fraction into a third fraction comprising the by-product solvent and a fourth fraction comprising the polymeric by-product.

Abstract: In a process for separating a mixture comprising cyclohexanone and phenol, a solid-phase basic material, such as basic ion-exchange resin, is used to remove acid and/or sulfur from the mixture prior to separation. The process results in reduced amount of contamination such as cyclic ethers in the cyclohexanone and/or phenol products.

Abstract: Disclosed are processes for making cyclohexanone from a mixture comprising phenol, cyclohexanone, cyclohexylbenzene, and an S-containing component, comprising a step of removing at least a portion of the S-containing component to reduce poisoning of a hydrogenation catalyst used for hydrogenating phenol to cyclohexanone.

Abstract: In a process for separating a mixture comprising cyclohexanone and phenol, a solid-phase basic material, such as basic ion-exchange resin, is used to remove acid and/or sulfur from the mixture prior to separation. The process results in reduced amount of contamination such as cyclic ethers in the cyclohexanone and/or phenol products.

Abstract: Disclosed herein is a process for producing phenol. The process includes oxidizing at least a portion of a feed comprising cyclohexylbenzene to produce an oxidation composition comprising cyclohexyl-1-phenyl-1-hydroperoxide. The oxidation composition may then be cleaved in the presence of an acid catalyst to produce a cleavage reaction mixture comprising the acid catalyst, phenol and cyclohexanone. At least a portion of the cleavage reaction mixture may be neutralized with a basic material to form a treated cleavage reaction mixture. In various embodiments, the treated cleavage reaction mixture contains no greater than 50 wppm of the acid catalyst or no greater than 50 wppm of the basic material.

Abstract: Disclosed are processes for making cyclohexanone from a mixture comprising phenol, cyclohexanone, cyclohexylbenzene, and an S-containing component, comprising a step of removing at least a portion of the S-containing component to reduce poisoning of a hydrogenation catalyst used for hydrogenating phenol to cyclohexanone.

Abstract: Disclosed is a hydroalkylation process in which the hydroalkylation catalyst is activated in the presence of a flowing fluid comprising hydrogen and a condensable agent. The presence of the condensable agent enables fast, effective activation of the hydroalkylation catalyst precursor in a cost-effective manner. It also yields superior catalyst performance.

Abstract: A process for making phenol and/or cyclohexanone, the process comprising: (A) oxidizing a cyclohexylbenzene feed to obtain an oxidation product comprising cyclohexylbenzene, cyclohexylbenzene hydroperoxide and water; (B) removing at least a portion of the water from at least a portion of the oxidation product to obtain a cleavage feed; and (C) contacting at least a portion of the cyclohexylbenzene hydroperoxide in the cleavage feed with an acid catalyst in a cleavage reactor under cleavage conditions to obtain a cleavage product comprising phenol and cyclohexanone. The removing step may also comprises a step of removing a portion of the cyclohexylbenzene contained in the oxidation product. Water removal may be advantageously conducted in a water flashing drum before a cyclohexylbenzene hydroperoxide concentrator.

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: In a process for producing a mixture of cyclohexanone and cyclohexanol, a feed comprising cyclohexanone is contacted with hydrogen in the presence of a hydrogenation catalyst under hydrogenation conditions effective to convert part of the cyclohexanone in the feed into cyclohexanol and thereby produce a hydrogenation product containing cyclohexanone and cyclohexanol. A mixture of cyclohexanone and cyclohexanol is then obtained from the hydrogenation product.

Abstract: In a process for producing phenol and cyclohexanone, a cleavage feed containing greater than 40 wt % and no greater than 95 wt % cyclohexyl-1-phenyl-1-hydroperoxide, and at least 5 wt % and less than 60 wt % cyclohexylbenzene is mixed with at least phenol, cyclohexanone, water, and sulfuric acid to produce a cleavage reaction mixture containing from 15 wt % to 50 wt % phenol, from 15 wt % to 50 wt % cyclohexanone, from 1 wt % to 10 wt % cyclohexyl-1-phenyl-1-hydroperoxide, from 5 wt % to 60 wt % cyclohexylbenzene, from 0.1 wt % to 4 wt % water, and from 10 wppm to 1000 wppm sulfuric acid. The cleavage reaction mixture is then reacted at a temperature from 30° C. and to 70° C., and a pressure of at least 1 atmosphere for a time sufficient to convert at least 50% of said cyclohexyl-1-phenyl-1-hydroperoxide in said cleavage reaction mixture and produce a cleavage effluent containing phenol and cyclohexanone.

Abstract: In a process for separating a mixture comprising cyclohexanone and phenol, at least a portion of the mixture is distilled in the presence of a solvent including at least two alcoholic hydroxyl groups attached to non-adjacent saturated carbon atoms and at least one hemiketal defined by the formula (I) or the formula (II): wherein R1, the same or different at each occurrence, is independently an alkylene group having from 2 to 10 carbon atoms, R2 is an alkylene group having from 4 to 10 carbon atoms, and R3 is hydrogen or the following group: and/or an enol-ether derived from the hemiketal defined by the formula (I) or the formula (II), wherein the total concentration of the hemiketal and the enol-ether, expressed in terms of weight percentage on the basis of the total weight of the feed to the distilling step (a), is at least 0.01%.

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

Abstract: In a process for producing phenol, benzene is reacted with a source of hydrogen containing methane in the presence of a hydroalkylation catalyst under conditions effective to produce a hydroalkylation reaction effluent comprising cyclohexylbenzene, benzene, hydrogen, and methane. A first stream comprising hydrogen, methane, and benzene is removed from the hydroalkylation reaction effluent and the first stream is washed with a second stream containing cyclohexylbenzene to produce a benzene-depleted hydrogen stream containing hydrogen and methane and a wash stream containing cyclohexylbenzene and benzene.

Abstract: In a process for producing cyclohexylbenzene, hydrogen and benzene are introduced to a first hydroalkylation reaction zone which contains a hydroalkylation catalyst and which is operated under at least partly liquid phase conditions sufficient to effect hydroalkylation of benzene to produce a mixed liquid/vapor phase effluent comprising cyclohexylbenzene and unreacted benzene, wherein at least a portion of the unreacted benzene is in the vapor phase. At least a portion of the effluent is cooled to condense a liquid phase stream containing at least some of the cyclohexylbenzene in the effluent portion and leave a residual stream containing at least some of the unreacted benzene and cyclohexylbenzene. At least a portion of the liquid stream is recycled to the first hydroalkylation reaction zone or to contact the mixed phase effluent exiting the first hydroalkylation reaction zone. Other methods of cooling the reaction effluent are disclosed.