Abstract: An etherification process for reacting tertiary olefin compounds with primary alcohols to produce an ether product is described. The etherification process includes two reactor stages for producing ether compounds and providing high conversion across the etherification process of the tertiary olefin compounds at reduced energy consumption.

Abstract: A process is disclosed for the production of tertiary alkyl ethers wherein linear olefins, particularly n-butene, are isomerized in the vapor phase at high temperature in contact with shape selective metallosilicate catalyst to produce iso-olefin vapor, particularly isobutene. The vaporous iso-butene is then etherified with alkanol to provide alkyl tert-alkyl ether such as MTBE. Unreacted iso-olefin and/or linear olefin and product ether are separated by fractionation and unreacted olefin components recycled. Fractionation of the vapor phase etherification product is carried out by using the fresh liquid linear olefin feedstream as a reflux stream to the fractionator.

Abstract: Ethers suitable for use as high octane oxygenate additives for motor fuels are produced by a multistage catalytic distillation process wherein a multi-carbon number range olefin feed stream, e.g. C.sub.5 -C.sub.7 isoolefins, is charged to two catalytic distillation zones operated in series. The heavier paraffins and olefins in the olefin feed stream and a first product ether are concentrated into the bottoms stream of the first catalytic distillation zone. This bottoms stream and additional alcohol is passed into the second catalytic distillation zone in which the heavier isoolefin is consumed in the production of a second ether. Preferably a portion of the catalytic distillation zone overhead liquid is passed into an external close coupled adiabatic reactor.

Abstract: A method for the preparation of methyl tertiary butyl ether is provided wherein a mixture of methanol and substantially peroxides-free tertiary butyl alcohol are catalytically reacted to form a reaction product that is separated into a first lighter distillation fraction comprising isobutylene, methanol and methyl tertiary butyl ether and a second heavier distillation fraction comprising methanol, tertiary butyl alcohol and water, wherein the first distillation fraction and a first recycle isobutylene fraction are reacted to form an isobutylene conversion product that is charged, together with recycle isobutylene to a methanol extraction zone and countercurrently contacted with water to provide an overhead extract comprising aqueous isobutylene, and wherein the isobutylene is recovered and recycled.

Abstract: A process for the production of an ether-rich additive for gasoline, and more particularly, the production of TAME from light hydrocarbon streams by admixing the light hydrocarbon stream, preferably from an FCC feedstock, prior to distillation of the feedstock with an alcohol in a C.sub.5 feedstock and contacting the feedstock with a catalyst under etherification process conditions.

Abstract: An etherification process for reacting tertiary olefin compounds with primary alcohols to produce an ether product. The etherification process has the advantage of permitting dual operating modes for producing methyl tertiary butyl ether and tert amyl methyl ether and it provides high conversion across the etherification process of the tertiary olefin compounds.

Abstract: A novel integrated olefin processing scheme is provided where olefins and paraffins are processed to produce high octane gasoline blending components. The integrated process involves the dehydrogenation of paraffin compounds to olefin compounds and the processing of olefins by hydroisomerization to produce hydroisomerate streams which are subsequently etherified. Those olefin compounds which are not etherified pass to an alkylation process where they are alkylated with branched chain paraffin compounds to produce an alkylate product.

Abstract: A process for the etherification and separation of C.sub.3 -C.sub.5 hydrocarbons is improved by the advantageous integration of an oxygenate recovery unit having a 3-bed arrangement into the etherification separation section. A feedstream including C.sub.3 hydrocarbons and isobutene are reacted with methanol in an etherification to produce an etherification effluent that is separated in a first separator into a bottoms stream of MTBE product and an overhead stream of unreacted isobutane, methanol, other oxygenate compounds and C.sub.3 -hydrocarbons. After recovery of methanol, in an adsorptive separation process, the methanol deficient overhead stream enters a second separation zone in the form of depropanizer for the separation of isobutane and higher boiling hydrocarbons from the C.sub.3 hydrocarbons. Any oxygenate compounds that are carried from the bottom of the column with the C.sub.

Abstract: An integrated two stage process for the production of isoolefin by the dehydration of isoalcohol and the synthesis of a corresponding ether, for example the production of methyl tertiary butyl ether by (a) feeding tertiary butyl alcohol to a first distillation column reactor into a feed zone; (b) concurrently in said first distillation column reactor (i) contacting said TBA with an acid ion exchange resin catalyst as a component of a distillation structure, at a temperature in the range of 165.degree. to 200.degree. F.

Abstract: Olefin is etherified with alcohol to provide an ether or mixture of ethers employing a catalyst comprising MCM-36.

Abstract: A process for upgrading olefin feedstock containing a mixture of diene, iso-olefin and linear olefin to produce tertiary-alkyl ether and high octane gasoline components comprising iso-olefin. Product recovery is integrated between primary and secondary reaction stages.In a preferred embodiment, a two stage etherification process employs a secondary solid acid regenerable catalyst bed to etherify and/or oligomerize unconverted diene, and optionally, iso-butene in the debutanizer overhead stream of a conventional MTBE primary reactor stage. Both stages can utilize a regenerable acid catalyst such as ZSM-5 or Zeolite Beta for etherification and to upgrade unconverted alkenes and methanol from the primary stage.

Abstract: A process for the preparation of tertiary olefins by decomposition of a tertiary alkyl ether in the vapor phase in the presence of a catalyst, wherein the catalyst used is a composition of: (i) 5 to 95 percent by weight of a crystalline aluminosilicate zeolite having a silica-to-alumina mole ratio of at least about 5 and a Constraint Index of about 1 to about 12, and (ii) 95 to 5 percent by weight of a binder selected from amorphous silica, alumina, silica-alumina and mixtures thereof.

Abstract: A process is disclosed for the production of alkyl tertiary alkyl ether from alkanol and iso-olefin employing zeolite catalyst, particularly zeolite Beta, that results is a high ether selectivity and a significant reduction in the formation of olefin oligomer by-product. The improvement is realized by incorporating a catalyst pretreatment step in the overall etherification process. The zeolite catalyst pretreatment comprises either steaming or a hydrothermal treatment using liquid water at elevated temperature. The process is particularly effective in reducing the formation of dimer by-product in the zeolite Beta catalyzed process for the formation of MTBE with high selectivity.

Abstract: A method and apparatus for conducting a catalytic distillation process is provided which allows for maintaining a liquid level in selected portions of the catalyst bed. Three particular processes disclosed are the production of methyl tertiary butyl ether, tertiary butyl alcohol and cumene.

Abstract: A combination of an etherification process and a process for the isomerization of linear alkenes to isoalkenes uses a separation zone that receives an effluent stream from the etherification reaction zone and separates it into a high boiling stream, a low boiling stream and an intermediate boiling stream in order to reduce the mass flow of reactants through the isomerization and etherification reaction zones. The separation zone normally has an arrangement of a distillation column. The distillation column can provide a distillation function only, or can also provide a reactive distillation zone. The intermediate boiling stream typically leaves the column as a sidecut which in the case of reactive distillation is taken from the point above a bed of catalyst within the column. Taking the sidecut stream substantially eliminates the circulation of isoalkane hydrocarbons through the etherification and isomerization zone and maintains normal alkanes at an acceptable equilibrium level.

Abstract: A process for the production of an ether-rich additive for gasoline, and more particularly, the production of MTBE, TAME and mixtures thereof from light hydrocarbon streams comprising passing the light hydrocarbon stream, preferably from an FCC feedstock, through a superactivated alumina medium so as to remove nitrogen compounds, mercaptan and water prior to contacting the feedstock with a catalyst under etherification process conditions. The present invention further includes a process for regenerating the spent superactivated alumina mediums used for purifying the feedstock employed in the process for the production of ether-rich additives for gasoline.

Abstract: Low value feed hydrocarbons are converted to high octane value tertiary ethers using a multiple riser fluidized solids catalytic reactor wherein in a first riser the hydrocarbon feed is converted to iso and linear C.sub.4 and C.sub.5 olefins, the iso-olefins are etherified, the linear C.sub.4 and C.sub.5 olefins are isomerized to iso C.sub.4 and C.sub.5 olefins in a second riser of the fluidized solids reactor, iso C.sub.4 and C.sub.5 olefins from the second riser are also etherified to high octane value tertiary ethers, and catalyst from both risers is regenerated in a common regeneration zone.

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: Dimethyl carbonate and methyl tert-butyl ether are prepared by a continuous integrated process comprising:a) feeding methanol, carbon monoxide and oxygen into a reaction environment maintained under methanol oxidative carbonylation conditions, to form a liquid reaction mixture containing dimethyl carbonate and unaltered methanol;b) at least partly eliminating the water from the reaction mixture of stage a);c) feeding the dehydrated mixture of stage b) and isobutene, or a hydrocarbon fraction containing isobutene, into a reaction environment maintained under etherification conditions, to form a liquid reaction mixture containing dimethyl carbonate and methyl tert-butyl ether; andd) recovering the dimethyl carbonate and methyl tert-butyl ether from the reaction mixture of stage c).

Abstract: An improvement in iso-olefin etherification is obtained in an integrated process combining a fluidized catalytic cracking reaction and a fluidized catalyst etherification reaction wherein zeolite catalyst particles are withdrawn in partially deactivated form from the ether reaction stage and added as part of the catalyst in the FCC reaction.

Abstract: A method is disclosed wherein t-butanol is reacted with methanol in a reaction zone in one step to provide methyl tert-butyl ether and the improvement of accomplishing the reaction which comprises:a. Using a catalyst comprising a montmorillonite clay treated with a fluorophosphoric acid,b. Continuously contacting said t-butanol and methanol in a molar amount of about 0.1 to 10 moles of methanol per mole of t-butanol with said catalyst at a temperature of about 20.degree. C. to about 250.degree. C. and a pressure of about atmospheric to about 1000 psig to obtain the methyl tert-butyl ether product.

Abstract: A catalyst comprising a novel zeolite NU-87, is useful in a wide variety of hydrocarbon conversion reactions including isomerisation, transalkylation and alkylation.

Abstract: A liquid phase process for oligomerization of C.sub.4 and C.sub.5 isoolefins or the etherification thereof with C.sub.1 to C.sub.6 alcohols wherein the reactants are contacted in a reactor with a fixed bed acid cation exchange resin catalyst at an LHSV of 5 to 20, pressure of 0 to 400 psig and temperature of 120.degree. to 300.degree. F. wherein the improvement is the operation of the reactor at a pressure to maintain the reaction mixture at its boiling point whereby at least a portion but less than all of the reaction mixture is vaporized. By operating at the boiling point and allowing a portion of the reaction mixture to vaporize, the exothermic heat of reaction is dissipated by the formation of more boil up and the temperature in the reactor is controlled.

Abstract: A technique for converting olefinic light hydrocarbons rich in butenes and butanes to ether-rich liquid fuels including etherification and transhydrogenation operations. The preferred process includes: reacting a mixed C4 hydrocarbon stream containing isobutene and n-butenes with lower aliphatic alcohol in an etherification zone in contact with an acidic etherification catalyst under etherification conditions whereby an effluent stream containing C5+ tertiary-alkyl ether is produced; separating the etherification effluent stream to provide a liquid stream comprising C5+ ether and an olefinic stream comprising unreacted C4 hydrocarbons; contacting at least the n-butenes from the C.sub.

Abstract: Disclosed is a two-step method for separating isobutylene from a C-4 hydrocarbon fraction comprising:a) Reacting the C-4 fraction with a glycol in the presence of a catalyst comprising heteropoly acid on an inert support at a temperature of about 60.degree. to 160.degree. C. to yield the corresponding glycol mono-t-butyl ether, and subsequentlyb) reacting the intermediate glycol ether product over the same class of catalyst at a temperature of about 100.degree. to 220.degree. C. to regenerate the isolatable isobutylene.

Abstract: Alkylaromatic hydrocarbons are produced in a process which comprises concentrating a feed aromatic hydrocarbon into a sidecut stream removed from a fractionation column. A feed acyclic olefin is then admixed with the aromatic hydrocarbon and passed through an alkylation reaction zone operated at optimum alkylation conditions. The reaction zone effluent is returned to the fractionation column to recover the product and to recycle untreated feed aromatics. This technique can be applied to hydrocarbon conversion processes in general to obtain benefits of catalytic distillation while operating the reaction zone at conditions not suitable for catalytic distillation. Hydrogen and other light gases are preferably separated from the reaction zone effluent by cooling and vapor-liquid separation external to the column.

Abstract: A process for production of gasoline comprising oligomerizing a C.sub.2 -C.sub.6 olefin containing feedstock over an intermediate pore size siliceous crystalline molecular sieve catalyst. The catalyst may take the form of silicalite, halogen stabilized silicalite, or a zeolite. Water may be supplied to the oligomerization reaction. The product from the oligomerization reaction is then subjected to an etherification reaction in the presence of methanol over an acid cation exchange catalyst to provide a gasoline product of enhanced octane number.

Abstract: A process has been discovered for the conversion of C.sub.5 -C.sub.7 olefinic hydrocarbons, such as those contained in FCC light naphtha, to iso-butene-rich and isoamylene-rich streams in an integrated process for the production of MTBE and TAME. The process involves the initial separation of the isoamylene-rich C.sub.5 -fraction of the feedstream which is converted to TAME. The C.sub.6 -C.sub.7 fraction plus unreacted C.sub.5 's are converted by olefin interconversion with medium pore zeolite catalyst into an isobutylene and isoamylene-rich stream which is then used as feedstream for etherification to MTBE and TAME.

Abstract: A multistage process for etherifying C.sub.4.sup.+ aliphatic hydrocarbon feedstock containing isoalkane including the step of contacting the hydrocarbon feedstock with dehydrogenation catalyst at elevated temperature under dehydrogenation reaction conditions to obtain C.sub.4.sup.+ isoalkene and hydrogen, and separating dehydrogenation effluent to obtain an olefinic stream rich in isoalkene and a hydrogen stream.The olefinic stream and aliphatic alcohol are contacted in an esterification stage under partial etherification conditions with a regenerable inorganic metal oxide acid solid catalyst to convert a major amount of the isoalkene to C.sub.5.sup.+ tertiary-alkyl ether.

Abstract: A process for production of dialkyl ether by hydration and etherification of olefinic feedstock containing at least one lower alkene by contacting the olefinic feedstock and water in a catalytic reaction zone with porous solid metallosilicate acidic catalyst under olefin hydration and etherification conditions. Improvement is achieved by recovering a first fluid effluent stream from the reaction zone; splitting the first fluid effluent stream into a liquid product recovery stream and a fluid recycle stream; and passing the fluid recycle stream consisting essentially of olefin, alcohol and ether in effluent stream proportions for feeding to the reaction zone along with fresh olefinic feedstock and fresh water, wherein the amount of fluid recycle stream is sufficient to maintain a homogeneous single fluid reaction phase in the reaction zone.

Abstract: A method for upgrading paraffinic naphtha to high octane fuel by contacting a feedstock, such as C7-C22 fresh virgin naphtha, with porous acid cracking catalyst under low pressure selective cracking conditions effective to produce C4 -C5 isoalkenes and C4-C5 isoalkanes. The preferred feedstock is straight run naphtha containing C7+ alkanes, at least 15 wt % C7+ cycloaliphatic hydrocarbons and less than 20% aromatics, which can be converted with a fluidized zeolite catalyst in a vertical riser reactor during a short contact period.The isoalkane products of cracking are dehydrogenated and etherified to provide high octane fuel components.

Abstract: For the separation of tert. butyl ethyl ether from mixtures with ethanol, there are provided two distillation stages, the first being carried out at a pressure p.sub.1 equal to or higher than 1 bar, the second at a pressure p.sub.2 below p.sub.1 by a value .DELTA.p or 0.5 to 12 bars, p.sub.2 then being 0.5 to 10 bars. The second column distillate is partly supplied as reflux to the head of the second column and is in part recycled to the head of the first column. The purified TBEE is collected at the bottom of the first column and the purified ethanol at the bottom of the second column.This separation process can be integrated into a TBEE production unit comprising etherification by ethanol of the isobutylene contained in a C.sub.4 fraction from a catalytic cracking or steam cracking stage. The ethanol separated from the TBEE is then recycled to the etherification zone.

Abstract: A catalyzed, continuous vapor phase process to convert a C.sub.2 or higher olefin in combination with methanol to a mixture containing at least one higher molecular weight alcohol, for example, isobutanol, over a magnesium oxide composition. The process also may contain a lower aldehyde and/or ketone in the feed.

Abstract: An improved process combination is disclosed for the production of an oxygenated gasoline component from an FCC gasoline feed. Olefins in the cracked gasoline are isomerized using a medium-pore molecular-sieve catalyst to achieve high yields of C.sub.5 + isomerized gasoline and avoid conversion of highly branched paraffins to equilibrium values. The isomerized gasoline is etherified to obtain oxygenated gasoline.

Abstract: In the diisopropyl ether production process, the distallation step for the separation of aqueous IPA recovered from the DIPE extraction operations is modified to avoid carrying out the distillation under conditions that yield IPA-water azeotrope providing lower overall process cost. The determination has been made that the overhead and bottom streams form an aqueous IPA fractionation process operated under off-azeotrope conditions in DIPE production can be recycled, respectively, to the DIPE reactor and extractor operations. Recycling the water and IPA overhead mixture eliminates the requirement for adding fresh water to the DIPE reactor. Returning the water and IPA bottom stream to the extractor reduces the requirement for distilled water addition to the extraction step. As a consequence, a less complex and costly aqueous IPA separation process is implemented.

Abstract: Disclosed is a two-step method for separating isobutylene from a C-4 hydrocarbon fraction comprising:a) Reacting the C-4 fraction with a glycol in the presence of an acidic montmorillonite catalyst at a temperature of about 60.degree. to 160.degree. C. to yield the corresponding glycol mono-t-butyl ether, and subsequentlyb) reacting the intermediate glycol ether product over the same class of catalyst at a temperature of about 100.degree. to 220.degree. C. to regenerate the isolatable isobutylene.

Abstract: Improved process techniques and equipment for reacting crude aqueous ethanol feedstock with iso-olefinic hydrocarbons to produce C.sub.6.sup.+ ethyl t-alkyl ethers, which comprises: distilling the aqueous ethanol feedstock; contacting ethanol rich distillate overhead containing a minor amount of water with a liquid hydrocarbon extractant rich in C.sub.4.sup.+ isoalkene under liquid extraction conditions; recovering an aqueous phase containing water introduced from the overhead; recovering an organic extract phase comprising the hydrocarbon extractant and a major amount of ethanol introduced in the feedstock; and reacting the extracted ethanol and C.sub.4.sup.+ isoalkene in contact with an acid etherification catalyst under catalytic reaction conditions to produce ether product.

Abstract: Olefins are converted to alcohols and/or ethers employing, as catalyst, an acidic zeolite which has been bound with an essentially non-acidic refractory oxide of at least one metal of Group IVA and/or IVB of the Period Table of the Elements, e.g., silica, titania, zirconia and/or germania.

Abstract: A process for production of ether by hydration and etherification of olefinic feedstock containing at least one lower alkene by contacting the olefinic feedstock and water in a plurality of catalytic reaction zones containing porous solid metal oxide acidic olefin hydration and etherification catalyst under olefin hydration and etherification conditions. Improved operation is achieved by recovering a first effluent stream from at least one fixed bed hydration zone, splitting the first effluent stream into a product recovery stream and a plurality of recycle streams, and passing at least a portion of cooled recycle streams comprising olefin, alcohol and ether in effluent stream component proportions for quenching at least one fixed bed reaction zone to control temperature of hot effluent from a preceding reaction zone.

Abstract: A low value C.sub.5 feedstock is efficiently upgraded by a series of process steps involving reacting branched tertiary olefins in the feed and from subsequent isomerization with methanol and/or water to form TAME and/or TAA, separating isopentene by distillation from the reaction mixture, separating product TAME and/or TAA by distillation from linear C.sub.5 hydrocarbons, and converting the linear C.sub.5 hydrocarbons by skeletal isomerization to branched C.sub.5 hydrocarbons which are recycled to said reaction with methanol and/or water.

Abstract: A process is disclosed for the production of tertiary alkyl ethers wherein linear olefins, particularly n-butene, are isomerized in the vapor phase at high temperature in contact with shape selective metallosilicate catalyst to produce iso-olefin vapor, particularly isobutene. The vaporous iso-butene is then etherified with alkanol to provide alkyl tert-alkyl ether such as MTBE. Unreacted iso-olefin and/or linear olefin and product ether are separated by fractionation and unreacted olefin components recycled. Fractionation of the vapor phase etherification product is carried out by using the fresh liquid linear olefin feedstream as a reflux stream to the fractionator.

Abstract: A process for removing dimethyl ether (DME) and methanol impurities from C.sub.4 hydrocarbon stream without substantial loss of C.sub.4 hydrocarbons by fractionating a C.sub.4 hydrocarbon stream containing DME and methanol at low levels, e.g., less than 5 wt. % to produce an overhead of about 20 to 40 volume % of the C.sub.4 stream, condensing the overhead, contacting the condensed overhead with about 1 to 5 volumes of water, thereby removing a portion of the DME and methanol from the C.sub.4 stream, returning substantially all of the C.sub.4 stream, except the small amount solubilized in the water, to the fractionation and flashing the solubilized DME and hydrocarbons from the water. The fractionation and extraction are preferably carried out at elevated pressures, e.g., 200 to 300 psig to avoid refrigeration of the overhead condensation. The flashing of the DME and hydrocarbons is carried out by reducing the pressure on the water, e.g. atmospheric pressure at a temperature in the range of 20.degree. C.

Abstract: A catalytic reaction process which involves exposing a hydrocarbon feed including nitrogenous contaminants as well as dialkyl sulfides to a material capable of adsorbing the nitrogenous contaminants as well as dialkyl sulfides from the feed before introducing the stream substantially devoid of nitrogenous contaminants and dimethyl sulfide into a feed zone of a reactor; contacting the hydrocarbon stream with a catalyst material in the reaction zone; and catalytically reacting the hydrocarbon stream under conditions which favor forming a reaction product and inhibiting reaction of nitrogenous contaminants and dimethyl sulfide with the catalyst material.

Abstract: A method and apparatus for conducting a catalytic distillation process is provided which allows for maintaining a liquid level in selected portions of the catalyst bed. Three particular processes disclosed are the production of methyl tertiary butyl ether, tertiary butyl alcohol and cumene.

Abstract: There is provided a new process for conducting heterogeneous chemical reactions in which a particulate catalyst is slurried in one of the reactant streams and fed into a distillation column reactor in a distillation reaction zone. The distillation reaction zone contains inert packing which provides the distillation structure for separation. The slurried catalyst trickles downward through the inert packing and is removed with the bottoms and separated therefrom for regeneration or replacement.

Abstract: A method for producing alkyl tertiary alkyl ether involves supplying a feed including isoolefins, alcohols, and dialkyl sulfides into a feed zone of a reactor; contacting the feed with a catalyst material in the reaction zone; and catalytically reacting the isooolefins and alcohols under conditions which favor forming resultant ether and inhibiting reaction of dialkyl sulfides with the catalyst material.

Abstract: A process is provided for etherification of essentially pure IC.sub.4.sup.= with MeOH to form MTBE in a distillation column reactor containing a fixed bed acid cation exchange resin as a catalytic distillation structure in an a distillation reaction zone. An inert C.sub.4 hydrocarbon is initially fed to the distillation column reactor to act as a diluent and a heat sink which boils at the desired temperature range for the reaction. Additionally the inert C.sub.4 diluent acts as an azeotroping agent for the MeOH in the lower end of the column carrying more of the MeOH back up into the reaction distillation zone. After start up and circulation the inert C.sub.4 hydrocarbon feed is stopped and that in the system is retained therein by total reflux of the overheads and judicious operation of the lower portion of the distillation column reactor.

Abstract: A process in which isobutane (isoparaffins), containing normal butane (normal paraffins), is dehydrogenated, and the principal product, isobutene, (isoolefin) contains some butene-1 and butene-2 (1-olefins and linear internal olefins). This mixture is subjected to a catalyzed etherification reaction with an alcohol to yield tertiaryalkyl ether. Some unreacted butene-1 and butene-2 (linear olefins) appear in the effluent from the ether reacton zone. These detrimentally affect the advantage of recycling that part of the effluent constituted by isobutane (isoparaffin) to the dehydrogenation reactor, because, as they build up in the closed system, undesirable coke lay down on the dehydrogenating catalyst occurs. The undesirable butene-1 is hydroisomerized to butene-2 which is removed from the recycle stream by fractionation.

Abstract: In the instant invention the effluent from the DIPE reactor is separated in a novel separation process that includes, in one embodiment, two extraction steps serially combined to initially separate IPA from the reaction products by extraction with water. The aqueous IPA extract is separated in a second extraction step carried out using the C.sub.3 hydrocarbon feedstream to the process as extractor. To effectuate the separation of aqueous IPA, the second extraction is carried out at a temperature higher than that of the first extraction step. The organic phase from the first extraction containing DIPE, C.sub.3 hydrocarbons and water is separated in a splitter to provide dry DIPE as product. In another embodiment dry DIPE is produced by an initial aqueous extraction of the reaction effluent followed by distillation to separate C.sub.3 hydrocarbons and water overhead and DIPE as a bottom stream.

Abstract: A process is disclosed for the production of high octane alkyl tertiary alkyl ether rich gasoline and gasoline rich in alkylated aromatics. It is disclosed that unreacted C.sub.3 -C.sub.4 hydrocarbon fraction of etherification feedstock plus unreacted alkanol can be separated and employed as alkylating agents in combination with a feedstream containing light aromatics when the alkylation reaction is carried out under conditions of high severity in contact with a high activity shape selective metallosilicate catalyst such as ZSM-5. Under high severity conditions olefin-assisted paraffin conversion also occurs as well as cracking, redistribution and alkylation. Aromatic rich gasoline is a suitable feedstream to the high severity conversion zone to produce a gasoline rich in alkylated aromatics.