Abstract: A process for post synthesis treatment of ZSM-5 catalyst for converting ethylene to liquid fuel products providing substantially improved catalyst life. The treatment comprises either a base treatment, an acid treatment or a two-step treatment where one is with an acid and the other is with a base. The base treatment is provided by a weak sodium hydroxide such as less than 1 Molar concentration. The acid treatment is stronger acid where, for example, a hydrogen chloride solution at greater than 2 Molar concentration is used.

Abstract: A process for post synthesis treatment of ZSM-5 catalyst for converting ethylene to liquid fuel products providing substantially improved catalyst life. The treatment comprises either a base treatment, an acid treatment or a two-step treatment where one is with an acid and the other is with a base. The base treatment is provided by a weak sodium hydroxide such as less than 1 Molar concentration. The acid treatment is stronger acid where, for example, a hydrogen chloride solution at greater than 2 Molar concentration is used.

Abstract: A process for post synthesis treatment of ZSM-5 catalyst for converting ethylene to liquid fuel products providing substantially improved catalyst life. The treatment comprises either a base treatment, an acid treatment or a two-step treatment where one is with an acid and the other is with a base. The base treatment is provided by a weak sodium hydroxide such as less than 1 Molar concentration. The acid treatment is stronger acid where, for example, a hydrogen chloride solution at greater than 2 Molar concentration is used.

Abstract: The invention relates to the production of aromatic hydrocarbon by the conversion of a feed comprising C2+ non-aromatic hydrocarbon, e.g., natural gas. The invention is particularly useful in converting natural gas to liquid-phase aromatic hydrocarbon, which can be more easily transported away from remote natural gas production facilities. The conversion is carried out in the presence of a dehydrocyclization catalyst comprising dehydrogenation and molecular sieve components. The dehydrocyclization catalyst has an average residence time of 90 seconds or less.

Abstract: Methods and apparatuses are provided for isomerizing a hydrocarbon stream. The method includes isomerizing a hydrocarbon stream in a reactor to produce an intermediate isomerized stream. The intermediate isomerized stream is fractionated to produce an off gas stream and a heavy isomerized stream, where the off gas stream includes an off gas recycle stream. The off gas recycle stream is dried in an off gas dryer to produce a hydrogen recycle stream, where the off gas drier includes an off gas dryer membrane separating the off gas recycle stream from an off gas purge stream. The off dryer membrane includes a perfluorosulfonated ionomer. The hydrogen recycle stream is then fed into the reactor.

Abstract: A process for reforming a hydrocarbon stream is presented. The process involves splitting a naphtha feedstream to at least two feedstreams and partially processing each feedstream in separate reactors. The processing includes passing the light stream to a combination hydrogenation/dehydrogenation reactor. The process reduces the energy by reducing the endothermic properties of intermediate reformed process streams.

Abstract: A process for reforming a hydrocarbon stream is presented. The process involves splitting a naphtha feedstream to at least two feedstreams and partially processing each feedstream in separate reactors. The processing includes passing the light stream to a combination hydrogenation/dehydrogenation reactor. The process reduces the energy by reducing the endothermic properties of intermediate reformed process streams.

Abstract: A process for the production of aromatics through the reforming of a hydrocarbon stream is presented. The process utilizes the differences in properties of components within the hydrocarbon stream to increase the energy efficiency. The differences in the reactions of different hydrocarbon components in the conversion to aromatics allows for different treatments of the different components to reduce the energy used in reforming process.

Abstract: A process for reforming hydrocarbons is presented. The process involves applying process controls over the reaction temperatures to preferentially convert a portion of the hydrocarbon stream to generate an intermediate stream, which will further react with reduced endothermicity. The intermediate stream is then processed at a higher temperature, where a second reforming reactor is operated under substantially isothermal conditions.

Abstract: A process is presented for the increasing the yields of aromatics from reforming a hydrocarbon feedstream. The process includes splitting a naphtha feedstream into a light hydrocarbon stream, and a heavier stream having a relatively rich concentration of naphthenes. The heavy stream is reformed to convert the naphthenes to aromatics and the resulting product stream is further reformed with the light hydrocarbon stream to increase the aromatics yields. The catalyst is passed through the reactors in a sequential manner.

Abstract: Processes for producing aromatics from a naphtha feedstream are provided. An exemplary process includes passing the feedstream to a fractionation unit, thereby generating a first stream including hydrocarbons having less than 8 carbon atoms and a second stream including hydrocarbons having at least 8 carbon atoms. The first stream is passed to a first reformer operated at a first set of reaction conditions to generate a first product stream. The first set of reaction conditions includes a first temperature and a first pressure. The second stream is passed to a second reformer operated at a second set of reaction conditions to generate a second product stream. The second set of reaction conditions includes a second temperature and a second pressure. The first pressure is lower than the second pressure.

Abstract: A process for reforming a hydrocarbon stream is presented. The process involves splitting a naphtha feedstream to at least two feedstreams and passing each feedstream to separation reformers. The reformers are operated under different conditions to utilize the differences in the reaction properties of the different hydrocarbon components. The process utilizes a common catalyst, and common downstream processes for recovering the desired aromatic compounds generated.

Abstract: A reactor design and process for the dehydrogenation of hydrocarbons is presented. The reactor design includes a multibed catalytic reactor, where each of the reactor beds are fluidized. The catalyst in the reactor cascades through the reactor beds, with fresh catalyst input into the first reactor bed, and the spent catalyst withdrawn from the last reactor bed. The hydrocarbon feedstream is input to the reactor beds in a parallel formation, thereby decreasing the thermal residence time of the hydrocarbons when compared with a single bed fluidized reactor, or a series reactor scheme.

Abstract: A process for reforming a hydrocarbon stream is presented. The process involves splitting a naphtha feedstream to at least two feedstreams and passing each feedstream to separation reformers. The reformers are operated under different conditions to utilize the differences in the reaction properties of the different hydrocarbon components. The process utilizes a common catalyst, and common downstream processes for recovering the desired aromatic compounds generated.

Abstract: A process for the conversion of mixed lower alkanes into aromatics which comprises first reacting a mixed lower alkane feed comprising at least propane and ethane in the presence of an aromatization catalyst under reaction conditions which maximize the conversion of propane into first stage aromatic reaction products, separating ethane from the first stage aromatic reaction products, reacting ethane in the presence of an aromatization catalyst under reaction conditions which maximize the conversion of ethane into second stage aromatic reaction products, and optionally separating ethane from the second stage aromatic reaction products.

Abstract: Separated volumes can be created in a reactor using interior dividing wall or interior conduit structures. Feedstocks can be hydroprocessed in the separated volumes to allow multiple types of hydroprocessing conditions and/or feeds to be processed in a single reactor. The feedstocks can remain separate for the entire volume of the reactor, or the dividing barrier can end at some intermediate point in the reactor.

Abstract: A process for reforming a hydrocarbon stream is presented. The process involves splitting a naphtha feedstream to at least two feedstreams and passing each feedstream to separation reformers. The reformers are operated under different conditions to utilize the differences in the reaction properties of the different hydrocarbon components. The process utilizes a common catalyst, and common downstream processes for recovering the desired aromatic compounds generated.

Abstract: Olefin feeds with high olefin content and/or containing a substance that generates water when contacting the catalyst, are oligomerised over solid phosphoric acid catalyst in tubular reactors by introducing the olefin feed into the reactor and maintaining the reacting mixture under conditions whereby the peak temperature is controlled to be below 265° C. and preferably a single liquid or dense phase is maintained and the average temperature throughout the reactor is maintained in the range 190° C. to 260° C.

Abstract: Disclosed is a method for production of lower olefins from a raw material containing dimethyl ether (DME), which can produce lower olefins (e.g. propylene) with good yield and in an economically advantageous manner by prolonging the time until the reversible deactivation of a zeolite catalyst and preventing the irreversible deactivation of the catalyst, can reduce the amount of water to be recycled to increase the thermal efficiency of the process, and can simplify the facilities and operations. Also disclosed is a method for improving the yield of propylene with good efficiency under practical operating conditions. A feed gas which comprises a DME-containing feedstock gas and an additive gas and further contains steam at a specific proportion is introduced into an olefin synthesis reactor to contact the feed gas with a zeolite catalyst, thereby producing a hydrocarbon product containing C2-C5 olefins.

Abstract: Process for evaluating the effect of a refinery feedstock on a refinery process by (i) providing a refinery feedstock (ii) treating the refinery feedstock to produce a plurality of fractions each representative of a feedstock for the refinery process, the plurality of fractions having at least two fractions with different properties; (iii) treating each of the plurality of fractions under experimental conditions representative of those in the refinery process, the treatments being carried out in an essentially parallel manner; and (iv) determining one or more performance criteria for each fraction for the refinery process by analyzing the respective product streams produced from each fraction at least partially in parallel.

Abstract: A process for combining the catalytic conversion of organic oxygenates and the catalytic conversion of hydrocarbons: an organic oxygenate feedstock is contacted with a Y-zeolite containing catalyst to produce a reaction stream, and a coked catalyst and a product stream are obtained after separating the reaction stream; a hydrocarbon feedstock is contacted with a Y-zeolite containing catalyst to produce a reaction stream, a spent catalyst and a reaction oil vapor are obtained after separating the reaction stream, and the reaction oil vapor is further separated to give the products such as gas, gasoline and the like; a part or all of the coked catalyst and a part or all of the spent catalyst enter the regenerator for the coke-burning regeneration, and the regenerated catalyst is divided into two portions, wherein one portion returns to be contacted with the hydrocarbon feedstock, and the other portion, after cooling, returns to be contacted with the organic oxygenate feedstock.

Abstract: Catalytic methods for the production of saturated hydrocarbons with 2 to 5 carbon atoms per molecule by conversion of small hydrocarbon halides and/or hydrogenation of carbonaceous material are disclosed that result in high yield of saturated C2 to C5 hydrocarbons at reduced corrosion of the reactors and in good lifetime of the catalyst. The methods are performed in the presence of a Lewis acid comprising catalyst and in the absence of oxygen or oxygen containing compounds, whereby an upper limit of at most 50 parts per million mass of oxygen or oxygen containing compounds can be tolerated.

Abstract: A process for reforming a hydrocarbon stream is presented. The process involves splitting a naphtha feedstream to at least two feedstreams and passing each feedstream to separation reformers. The reformers are operated under different conditions to utilize the differences in the reaction properties of the different hydrocarbon components. The process further includes passing one or more catalyst streams through the reformers to optimize selectivity and conversions.

Abstract: A process for reforming a hydrocarbon stream is presented. The process involves splitting a naphtha feedstream to at least two feedstreams and passing each feedstream to separation reformers. The reformers are operated under different conditions to utilize the differences in the reaction properties of the different hydrocarbon components. The process utilizes a common catalyst, and common downstream processes for recovering the desired aromatic compounds generated.

Abstract: A process for reforming a hydrocarbon stream is presented. The process involves splitting a naphtha feedstream to at least two feedstreams and passing each feedstream to separation reformers. The reformers are operated under different conditions to utilize the differences in the reaction properties of the different hydrocarbon components. The process utilizes a common catalyst, and common downstream processes for recovering the desired aromatic compounds generated.

Abstract: A process for reforming a hydrocarbon stream is presented. The process involves splitting a naphtha feedstream to at least two feedstreams and passing each feedstream to separation reformers. The reformers are operated under different conditions to utilize the differences in the reaction properties of the different hydrocarbon components. The process utilizes a common catalyst, and common downstream processes for recovering the desired aromatic compounds generated.

Abstract: A process for producing ethylene from ethanol combining the catalytic conversion of hydrocarbons: an ethanol feedstock is contacted with a Y-zeolite containing catalyst to give a product stream, and a coked catalyst and an target product of ethylene are obtained after separating the reaction stream; a hydrocarbon feedstock is contacted with a Y-zeolite containing catalyst to give a product stream, a spent catalyst and an oil vapor are obtained after separating the reaction stream, and the oil vapor is further separated to give the products such as gas, gasoline and the like; a part or all of the coked catalyst and a part or all of the spent catalyst enter the regenerator for the coke-burning regeneration, and the regenerated catalyst is divided into two portions, wherein one portion returns to be contacted with the hydrocarbon feedstock, and the other portion, after cooling, returns to be contacted with ethanol feedstock.

Abstract: A process for increasing the yield of ethylene and propylene, comprising: (1) feeding a feedstock into a reaction zone with a catalyst to produce (i) a product stream and a catalyst to be regenerated; (2) stripping and then dividing the catalyst to be regenerated into at least two parts, wherein a first part is recycled into the reaction zone at a first position, and a second part is regenerated in the regenerator to form a regenerated catalyst and then recycled into the reaction zone at a second position; and (3) controlling the temperature increase in the reaction zone.

Abstract: One exemplary embodiment can be a method of modifying an alkylation unit to increase capacity. The method may include combining a first alkylation zone with a second alkylation zone. Generally, the first alkylation zone includes a first settler having a height and a width. Typically, the width is greater than the height. In addition, the second alkylation zone may have a second settler having a height and a width. Usually, the height is greater than the width.

Abstract: A process for the production of phenylalkanes comprising at least two catalytic alkylation reactors placed in parallel among which are present in reaction zones that each contain at least one acidic solid catalyst, whereby n is greater than or equal to 2, is described. One of the reactors carries out the alkylation of at least one aromatic compound by at least one olefin that has 9 to 16 atoms. An olefin fraction is introduced at the inlet of each of the reaction zones of the reactor that operates in alkylation mode. While one of the reactors carries out the alkylation, the other reactor carries out the reactivation of each catalyst, partially deactivated, that it contains. The functions of each reactor are switched regularly so as to limit the deactivation of catalysts in each of the reactors. The phenylalkanes that are obtained by the process according to the invention are particularly suitable for the production of detergents.

Abstract: A reactor design and process for the dehydrogenation of hydrocarbons is presented. The reactor design includes a multibed catalytic reactor, where each of the reactor beds are fluidized. The catalyst in the reactor cascades through the reactor beds, with fresh catalyst input into the first reactor bed, and the spent catalyst withdrawn from the last reactor bed. The hydrocarbon feedstream is input to the reactor beds in a parallel formation, thereby decreasing the thermal residence time of the hydrocarbons when compared with a single bed fluidized reactor, or a series reactor scheme.

Abstract: A process for producing at least one light olefin comprising: (a) contacting a first raw material comprising methanol with a least one catalyst comprising at least one silicon-aluminophosphate molecular sieve in a first reaction zone to produce a product stream I comprising at least one light olefin and at least one inactivated catalyst; (b) transporting the at least one inactivated catalyst to a first regeneration zone to produce at least one first regenerated catalyst, and transporting a portion of the at least one first regenerated catalyst to the first reaction zone, wherein the at least one first regenerated catalyst comprises a carbon deposit present in an amount ranging from about 0.8% to about 2.

Abstract: A method for the absorption of alkynes and diolefins from an ethylene or propylene containing stream with conversion to alkenes by catalytic hydrogenation in a solvent over a fixed bed comprising a supported catalyst.

Abstract: A method of operation for producing high yield of alkylate product using catalytic reactors. The catalytic reactors which cycle between reaction mode and catalyst regeneration mode have their contents exchanged with each other at the beginning of each cycle in order to increase the yield of the desired product. This exchange increases the yield by minimizing the contact of reactant in reaction mode with regenerant utilized in regeneration mode. Thus, reducing/preventing the undesirable alternate reaction between the two, which consumes the reactant making it unavailable for the production of the desired product.

Abstract: One exemplary embodiment can be an alkylation unit. The alkylation unit can include at least one alkylation reaction zone having an alkylation catalyst, at least one cooler communicating with the at least one alkylation reaction zone, a settler communicating with the at least one alkylation reaction zone and the at least one cooler, a fractionation zone receiving an effluent from the settler passing through a line, and a boot coupled to a substantially horizontal portion of the line. Generally, the boot receives an effluent portion rich in the alkylation catalyst.

Abstract: The invention concerns a process for the hydrodesulphurization of gasoline cuts for the production of gasolines with a low sulphur and mercaptans content. Said process comprises at least two hydrodesulphurization steps, HDS1 and HDS2, operated in parallel on two distinct cuts of the gasoline constituting the feed. The flow rate of hydrogen in the hydrodesulphurization step HDS2 is such that the ratio between the flow rate of hydrogen and the flow rate of feed to be treated is less than 80% of the ratio of the flow rates used to desulphurize in the hydrodesulphurization step HDS1.

Abstract: A process for the production of phenylalkanes comprising at least two catalytic alkylation reactors placed in parallel among which are present in reaction zones that each contain at least one acidic solid catalyst, whereby n is greater than or equal to 2, is described. One of the reactors carries out the alkylation of at least one aromatic compound by at least one olefin that has 9 to 16 atoms. An olefin fraction is introduced at the inlet of each of the reaction zones of the reactor that operates in alkylation mode. While one of the reactors carries out the alkylation, the other reactor carries out the reactivation of each catalyst, partially deactivated, that it contains. The functions of each reactor are switched regularly so as to limit the deactivation of catalysts in each of the reactors. The phenylalkanes that are obtained by the process according to the invention are particularly suitable for the production of detergents.

Abstract: A process for preparing a gas oil cut comprises the following steps in succession: 1) oligomerizing an olefinic C2-C12 hydrocarbon cut, preferably C3-C7 and more preferably C3-C5; 2) separating the mixture of products obtained in step 1) into three cuts: a light cut containing unreacted C4 and/or C5 olefinic hydrocarbons, an intermediate cut having a T95 in the range 200-220° C. and a heavy cut comprising the complement; T95 being the temperature at which 95% by weight of product has evaporated, as determined in accordance with standard method ASTM D2887; 3) oligomerizing the intermediate cut obtained in the separation step; characterized in that in step 3), oligomerization is carried out in the presence of an olefinic C4 and/or C5 hydrocarbon cut in a weight ratio of intermediate cut to olefinic C4 and/or C5 cut in the range of 60/40 to 80/20.

Abstract: The invention relates to a method of isomerising a charge comprising hydrocarbons containing between 5 and 8 carbon atoms per molecule. According to the invention, said charge is separated into at least two fractions: fraction A mostly comprising hydrocarbons containing 5 or 6 carbon atoms and fraction B mostly comprising hydrocarbons containing 7 or 8 carbon atoms. Subsequently, said fractions A and B are treated separately under specific conditions in different isomerisation reaction zones.

Abstract: This invention provides a process for the production of diesel boiling range hydrocarbons, the process including at least the steps of obtaining an olefinic feed stream from one or more hydrocarbon producing processes wherein the olefinic feed stream contains branched short chain olefins having a chain length of from three to eight carbon atoms, and contacting the feed stream with a shape selective medium pore acid zeolite catalyst in a pressurised reactor at elevated temperature so as to convert said short chain olefins to higher hydrocarbons. The invention also provides an apparatus for carrying out the process and recovering the catalyst for reuse.

Abstract: A continuous alkylation process performed in an apparatus comprising a series of at least two zone A reactors and a series of at least two zone B reactors, in which the zone A reactors and the zone B reactors cycle between alkylation mode and mild regeneration mode, and wherein the alkylation mode comprises introducing an alkylation agent into a first reactor of the zone through which the alkylatable compound passes, reacting a portion of the alkylatable compound with a portion of the alkylation agent to produce a product stream, and performing this operation at least once more in a downstream reactor in the same zone employing, instead of alkylatable compound, a stream comprising the product stream.

Abstract: A process for the joint preparation of styrene and propylene oxide comprising the steps of: (a) reacting ethane and benzene to form ethylbenzene; (b) reacting ethylbenzene with oxygen or air to form ethylbenzene hydroperoxide; (c) reacting at least part of the ethylbenzene hydroperoxide obtained with propene in the presence of an epoxidation catalyst to form propylene oxide and 1-phenyl ethanol, and (d) dehydrating at least part of the 1-phenyl ethanol obtained into styrene in the presence of a suitable dehydration catalyst, wherein the ethene used in step (a) and the propene used in step (c) are at least partly provided by a fluid catalytic cracking unit.

Abstract: A process is provided to react a feedstock comprising isobutane with pentenes in the presence of sulfuric acid catalyst to produce a high octane alkylate as well as a higher octane isopentane gasoline blending component. A method to reduce sulfuric acid consumption during alkylation is provided wherein a diolefinic contaminant of a pentene system feed is selectively hydrogenated before alkylation. An alkylation method is provided wherein the alkylation feed is separated into a fraction comprising substantially C.sub.4 and lower olefins and a fraction comprising substantially C.sub.5 olefins and the stream comprising C.sub.5 olefins is alkylated in a different reactor than the fraction comprising substantially C.sub.4 and lower olefins.

Abstract: A process is provided to react a feedstock comprising isobutane with pentenes in the presence of sulfuric acid catalyst to produce a high octane alkylate as well as a higher octane isopentane gasoline blending component. A method to reduce sulfuric acid consumption during alkylation is provided wherein a diolefinic contaminant of a pentene system feed is selectively hydrogenated before alkylation. An alkylation method is provided wherein the alkylation feed is separated into a fraction comprising substantially C.sub.4 and lower olefins and a fraction comprising substantially C.sub.5 olefins and the stream comprising C.sub.5 olefins is alkylated in a different reactor than the fraction comprising substantially C.sub.4 and lower olefins.

Abstract: An integrated fluid coking/paraffin dehydrogenation process. The fluid coking unit is comprised of a fluid coker reactor, a heater, and a gasifier. Solids from the fluidized beds are recycled between the coking zone and the heater and between the heater and the gasifier. A separate stream of hot solids from the gasifier is diluted with hot solids from the heater then passed to the scrubbing zone of the coker reactor. A light paraffin stream is introduced into this stream of hot solids between the point where the heater solids are introduced and the scrubbing zone. The hot particles act to catalyze the dehydrogenation of the paraffins to olefins.

Abstract: An integrated fluid coking/paraffin dehydrogenation process. The fluid coking unit is comprised of a fluid coker reactor, a heater, and a gasifier. Solids from the fluidized beds are recycled between the coking zone and the heater and between the heater and the gasifier. A separate stream of hot solids from the gasifier is passed to the scrubbing zone or to a satellite fluidized reactor. A first stream containing an effective amount of C.sub.1 to C.sub.2 paraffins is introduced into this stream of hot solids between the point where the diluent is added and the scrubbing zone. The hot particles act to catalyze the dehydrogenation of paraffins to olefins. A second stream containing C.sub.3 to C.sub.10 paraffins is introduced downstream of the introduction of said first stream.

Abstract: A process for simultaneously producing C.sub.5 -C.sub.12 alkane(s) and C.sub.5 -C.sub.8 tertiary alkyl ether(s) employs a liquid feed mixture containing (a) at least one C.sub.4 -C.sub.7 isoalkane, (b) at least one second reactant which is at least one C.sub.4 -C.sub.8 isoalkane, and/or at least one C.sub.4 -C.sub.8 tertiary alkyl alcohol, and (c) at least one C.sub.1 -C.sub.6 linear alkyl alcohol, wherein the liquid feed mixture is contacted at effective reaction conditions with a catalyst consisting essentially of trifluoromethanesulfonic acid and a specific solid carrier material (preferably alumina).

Abstract: A process for the isomerization of C.sub.4 and higher molecular weight hydrocarbons, preferably C.sub.4 to C.sub.6 paraffins with high C.sub.6 cyclics content. A C.sub.5 to C.sub.6 hydrocarbon stream is isomerized in a first isomerization reaction zone and a C.sub.4 hydrocarbon stream is isomerized in a second isomerization reaction zone. At least one or both of the effluent streams from the first and second isomerization zones are conveyed to a gas-liquid separator which separates a hydrogen-rich recycle stream. At least a portion of the hydrogen-rich recycle stream is conveyed to the C.sub.5 to C.sub.6 hydrocarbon feed stream and at least a portion of the hydrogen-rich recycle stream is conveyed to the C.sub.4 hydrocarbon feed stream whereby the hydrogen recycle stream is shared during both the C.sub.4 isomerization reaction and the C.sub.5 to C.sub.6 isomerization reaction. The product stream is conveyed to a shared stabilizer which removes the gaseous and volatile components.

Abstract: Ethers suitable for use as high octane oxygenate additives for motor fuels are produced in increased yields by a catalytic distillation process wherein a mixture of C.sub.5 -plus isoolefin isomers and an alcohol are charged to a catalytic distillation zone containing both etherification and double bond isomerization catalysts. Otherwise unreactive isomers are isomerized to reactive species within the zone to allow them to participate in the etherification reaction, resulting in a higher ether yield.

Abstract: A process for the production of alkylaromatic hydrocarbons uses a high water content in an alkylation zone and a low water content in a transalkylation zone to improve yields improve process yields and catalyst life. An aromatic feed and an acyclic feed are first passed through the alkylation reaction zone that operates at a high water content. A separator receives the effluent from the alkylation reaction zone and removes water from a sidecut of unreacted aromatic feed. The sidecut of aromatic feed and a stream of polyalkylated aromatics are contacted in the transalkylation zone. The differing water content improves the operation of both the alkylation zone and the transalkylation zone.