Abstract: Mixtures of isomers, e.g., mixtures of phenethyl bromide and 1-phenyl-1-bromoethane, are separated by (a) selectively condensing one such isomer with an aromatic compound bearing at least one aryl (nuclear) hydrogen atom, e.g., xylene, in the presence of a catalytically effective amount of a Friedel-Crafts catalyst, e.g., ferric chloride, and then (b) separating the product of condensation, e.g., phenylxylylethane, from the unreacted isomer.

Abstract: Aromatic compounds are alkylated in a combination reactor/distillation column comprising a vessel suitable for operating between 70.degree. C. and 500.degree. C. and from 0.5 to 20 atmospheres pressure; an inert distillation packing in the lower one-third of said vessel; solid acidic catalytic material such as zeolites or an acidic cation exchange resin supported in the middle one-third of said vessel; and inert distillation packing in the upper one-third of said vessel. A benzene inlet is located near the upper end of the vessel; an olefin inlet is juxtaposed with said solid acidic catalytic material; a bottoms outlet is positioned near the bottom of said vessel for removing said cumene and ethyl benzene; and an overhead outlet is placed at the top of said vessel for removing any unreacted benzene and olefin.

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: An integrated reactor system for converting methanol or the like to ether and gasoline hydrocarbons. Alcohol feedstock containing water is extracted with olefinic liquid and reacted catalytically to produce tertiary ether. Unreacted alcohol and olefin vapor separated from etherification effluent is converted along with aqueous alcoholic raffinate in a zeolite catalysis step to produce gasoline and paraffinic intermediate. By dehydrogenating the C.sub.3 -C.sub.5 paraffins, an olefinic liquid rich in isoalkenes is obtained for recycle to the extractor as solvent for alcohol feedstock.

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: 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 multi-stage reactor-separator for the fermentative production of volatile inhibitory products from non-volatile substrate includes a stirred tank reactor and a packed or tray-type gas-liquid contacting column separator. Each reactor and separator form a stage and a plurality of stages may be stacked into a tower, or otherwise placed to operate consecutively, forming a reactor-separator in which stages having gas flowing cocurrent to the liquid flow in the separator portion form an enriching section, and stages having gas flowing countercurrent to the liquid flow in the separator portion form a stripping section. In a method of using the reactor-separator, a volatile fermentation product is produced and simultaneously separated into a gas phase.

Abstract: A method and apparatus is provided for removing catalyst from a distillation column reactor and replacing the catalyst with fresh or regenerated catalyst. More specifically a small particulate catalyst is supported by wire mesh or screen or filter medium on trays in a conventional distillation column and substantially submerged by the liquid on the trays. The vapor rising through the liquid tends to keep the catalyst in suspension in the liquid. A draw-off is provided for each tray having catalyst supported thereon whereby liquid containing the suspended or slurried catalyst can be removed to a separator during operation. The catalyst is separated, as in a settling tank separator, from the liquid recycled to the tray until all the catalyst has been removed. The separated catalyst is removed for either regeneration or discarding. Fresh catalyst can then be added to the separator where it is slurried into the liquid again being recirculated from the tray.

Abstract: To achieve good liquid-vapor contact and at the same time better utilize the heat of reaction in a distillation column reactor a system is provided wherein a reaction tray and distillation tray are "coupled" by a continuous liquid level between the two. A reaction tray, containing the appropriate catalyst, is situated directly below a distillation tray. A vapor riser is provided through the reaction tray as a by-pass which carries the vapor from a lower distillation tray to a vapor distribution area underneath the "coupled" distillation tray. Liquid flows downward through a downcomer by-passing the "coupled" distillation tray, and onto and across the "coupled" reaction tray immersing the catalyst and rises upward, onto and across the "coupled" distillation tray where it is intimately contacted with the rising vapor effecting fractional distillation.

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 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: 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: There is provided a process for recovering acetic acid from methyl acetate wherein the methyl acetate is hydrolyzed catalytically to methanol and acetic acid in the same tower or column that is used to separate the methanol from the acetic acid and the hydrolysis and separation are carried out coextensively in the vessel. The process is employed suitably in a process for the partial oxidation of a polymethylbenzene to a polycarboxylic acid in the presence of an oxidation catalyst and an acetic acid solvent.

Abstract: A process for the catalytic distillation production of alkylated aromatic compounds is provided wherein the vapor pressure of the olefin may be increased while maintaining the same olefin feed rate and aromatic to olefin ratio. In one embodiment a side stream from the vapor from the second column below the catalyst and olefin feed is condensed and rerouted to the aromatic make up stream from the reflux drum. The vapor pressure of the olefin in the lower end of the first column in the catalyst bed is thus increased which increases the equilibrium concentration of the olefin in the liquid phase. In another embodiment of the invention the effective driving force for the reaction is increased by injecting the olefin at different heights within the catalyst bed. If additional olefin is injected more catalyst bed height would be required, but the additional catalyst is more that offset by the increased throughput at the same overall olefin conversion.

Abstract: A method of preparing a column for a reaction with distillation process utilizing a solid particulate catalyst includes the steps of providing a plurality of vertically spaced apart distillation devices, coupling these devices with a plurality of vertically extending horizontally spaced catalyst enclosing containers, extending at least some of the containers through at least two successive distillation devices, then loading a particulate catalyst into the containers to form a catalyst bed whereby distillation and catalytic reaction may occur simultaneously in the column. The method also encompasses a process for concurrent catalytic reaction with distillation which includes the foregoing steps as well as the steps of feeding a liquid stream to the column reactor and onto the distillation devices while a vapor stream moves vertically up through the distillation devices while products of reaction and distillation are withdrawn from the reactor.

Abstract: A process for the treatment of waste water containing boron compounds and radionuclides. The waste water is essentially vaporized until dry to yield a concentrate. Boric acid ester and an azeotropic mixture of water and alcohol are produced in a reaction by the addition of an excess of a long chain primary alcohol, e.g. butyl alcohol, to the concentrate. The azeotropic mixture, excess alcohol and boric acid ester are then separated from the concentrate by distilling. The non-radioactive components are then separated from the concentrate leaving behind a radioactive residue, which can be safely disposed of. The azeotropic mixture is then separated back into water and alcohol, and the boric acid ester is saponified back into boric acid and alcohol. The alcohol and boric acid are recycled back into the treatment process and to the nuclear reactor.

Abstract: Method of preparing para-cumylphenol including reacting an excess of phenol with alpha-methylstyrene by the slow addition of alpha-methylstyrene to a 50% to 200% molar excess of phenol at a temperature from about 80.degree. C. to about 90.degree. C. in the presence of an acid catalyst and thereafter maintaining the temperature at about 95.degree. to about 100.degree. C. to obtain a crude cumylphenol reaction product containing acid derived from the catalyst, and distilling the reaction product in the presence of an amount of base sufficient to neutralize the acid therein.

Abstract: An aromatic alkylation process comprising continuously feeding catalyst particles through at least one substantially vertically-positioned permeable tube disposed in a vessel surrounding said permeable tube, contacting said catalyst particles with at least one aromatic hydrocarbon and at least one alkylating agent under liquid phase alkylation conditions, continuously removing said catalyst particles from a lower end of said tube, and recovering said alkyl-substituted aromatic.

Abstract: A process for the catalytic distillation production of alkylated aromatic compounds is provided wherein the vapor pressure of the olefin may be increased while maintaining the same olefin feed rate and aromatic to olefin ratio. In one embodiment a side stream from the vapor from the second column below the catalyst and olefin feed is condensed and rerouted to the aromatic make up stream from the reflux drum. The vapor pressure of the olefin in the lower end of the first column in the catalyst bed is thus increased which increases the equilibrium concentration of the olefin in the liquid phase. In another embodiment of the invention the effective driving force for the reaction is increased by injecting the olefin at different heights within the catalyst bed. If additional olefin is injected more catalyst bed height would be required, but the additional catalyst is more that offset by the increased throughput at the same overall olefin conversion.

Abstract: Organic aromatic compounds are alkylated in a Reactive Distillation.TM. reactor, wherein the solid particulate catalyst is slurried in the aromatic feed stream and fed to a reaction zone containing inert distillation packing. Olefin is vaporized and fed to the bottom of the reaction zone and agitates the catalyst while reacting the olefin with the aromatic to form an alkylation product. The alkylation product is removed from the lower end of the reaction zone and recovered. Any unreacted aromatic is distilled overhead and recycled or recovered. Recycling the aromatic controls the molar ratio of aromatic to olefin to the extent that substantially all of the olefin is reacted.

Abstract: 2,3-Difluoro-5-(trifluoromethyl)pyridine is prepared by contacting a 2,3-dihalo-5-(trifluoromethyl) pyridine with an effective amount of KF or CsF in a polar aprotic solvent (diluent) at an elevated temperature under substantially anhydrous conditions with removal of the difluoropyridine products essentially as they are formed. The starting material may optionally be added as the reaction proceeds to minimize decomposition. The reaction is also optionally conducted in the presence of an acid scavenger and/or a crown ether or other phase-transfer catalyst.

Abstract: A concurrent catalytic reaction with distillation structure involves a plurality of vapor permeable plates which are arranged in spaced apart relationship with a catalyst placed in the open space between two adjacent plates. The catalyst filled area presents a reaction zone where catalytic reaction can take place and the vapor permeable plates present a large surface area for vapor and liquid phase exchange. The invention also encompasses a process for concurrent catalytic reaction with distillation employing structure as aforedescribed and including the steps of feeding a liquid stream to a column employing such structure and directing the stream through the catalytic reaction zone while concurrently distilling a portion of the liquid to present a vapor stream which is directed in countercurrent relationship to the liquid stream flow.

Abstract: An oligomerization system is provided for upgrading lower olefins to distillate hydrocarbons, especially useful as high quality jet or diesel fuels. The olefinic feedstock is reacted over a shape selective acid zeolite, such as ZSM-5, to oligomerize feedstock olefins and further convert recycled hydrocarbons. Reactor effluent is fractionated to recover a light-middle distillate range product stream and to obtain gasoline and heavy hydrocarbon streams for recycle.

Abstract: An improved reactor system reacts crude aqueous methanol feedstock with iso-olefinic hydrocarbons to produce C.sub.5.sup.+ methyl t-alkyl ethers. The system includes an extractor for contacting the aqueous methanol feedstock with a liquid hydrocarbon extraction solvent rich in C.sub.4.sup.+ isoalkene. Both an organic extract phase and an aqueous methanol raffinate phase recovered from the extractor and fed to a primary reactor. This primary reactors reacts the methanol and C.sub.4.sup.+ isoalkene from the organic extract phase under catalytic conditions to produce an ether product. The ether product is fed to an etherification effluent fractionator to separate the ether product from unreacted methanol and C.sub.4.sup.+ isoalkene. A secondary reactor then converts methanol from the aqueous methanol raffinate phase with the unreacted methanol and C.sub.4.sup.+ isolakene to produce hydrocarbons.

Abstract: A process for the separation of 2-methylalkanals from a mixture thereof with at least one alpha unbranched aldehyde thereof comprising distillation of said mixture in the presence of formaldehyde and an aldolization catalyst whereby the alpha unbranched aldehydes are converted to alpha alkylacrolein and the 2-methylalkanals are recovered in a high purity.

Abstract: The present invention provides catalytic distillation structures which are useful in the concurrent reaction and distillation of a reaction mixture. The distillation structures are provided as rigid containers having a volume substantially smaller than the volume of conventional distillation column reactors. The catalyst component is loaded into the containers and the containers are closed. Openings are provided to allow vapor and liquid passage into and out of the containers. The surfaces of the containers provide the necessary/vapor liquid contact surfaces for the distillation. The rigidity of the containers provides for spacing the structures and the necessary free space for the distillation.

Abstract: An improvement in the operation to a catalytic distillation process for the alkylation of organic aromatic compounds with an olefin contained wherein aliphatic compounds are contained in either the olefin feed stream, the aromatic feed stream or both is disclosed. Aliphatic compounds are added to the upper portion of a secondary distillation column reactor wherein aromatic is being reacted with unreacted olefin from a primary distillation column reactor to polish the conversion of olefin. The additional aliphatic compound produces an equilibrium in the secondary column wherein unreacted aromatic and alkylation product are recovered as bottoms which may be recycled to the primary distillation column reactor.

Abstract: The invention concerns a process and apparatus for manufacturing methyl tert-butyl ether (MTBE) by reacting methanol with an isobutene-containing hydrocarbon mixture.This process is characterized by the steps of:introducing the reactants into a reaction-distillation zone containing at least two superposed and non-contiguous fixed beds (2a, 2b) of catalyst of the sulfonated resin type, wherein passageways are provided for a vapor phase, at least one distillation tray (4a), at least one liquid redistribution tray (5),maintaining distillation conditions in the zone so as to have a descending liquid phase and an ascending vapor phase,maintaining a continuous liquid phase in the lower part of the beds,discharging a vapor phase containing a high proportion of unconverted hydrocarbons from the top (8) of the zone, andwithdrawing a liquid phase of high MTBE content from the bottom (10) of the zone.

Abstract: The invention relates to a process and apparatus for manufacturing methyl tert-butyl ether (MTBE) by reacting methanol with isobutene-containing hydrocarbons in a reaction zone having alternate beds of sulfonated resin catalyst and catalyst-free distillation zones wherein the zones also contain liquid redistribution plates.

Abstract: (CF.sub.3 SO.sub.2).sub.2 O is formed by reaction of CF.sub.3 SO.sub.3 H with P.sub.2 O.sub.5 and taken out of the reaction system by distillation, but the residue of the distillation contains a considerable amount of unreacted CF.sub.3 SO.sub.3 H. From the residue unreacted by adding water or a phosphoric acid solution, preferably the latter, to the residue to obtain a fluidic mixture containing an adequate amount of water and subjecting the mixture to distillation, preferably under reduced pressure at temperatures ranging from 180.degree. to 280.degree. C. It is possible to form additional CF.sub.3 SO.sub.3 H during the recovery process by adding a metal salt of CF.sub.3 SO.sub.3 H to the aformentioned mixture since the metal salt is decomposed by phosphoric acid contained in the mixture.

Abstract: A process of preparing industrially trans-1,4-cyclohexanedimethanol of high purity by distilling a mixture of cis- and trans-1,4-cyclohexanedimethanol in the presence of alkali, or by heating a mixture of cis- and trans-1,4-cyclohexanedimethanol in the presence of alkali and then distilling the heated mixture, and a process of preparing powdered trans-1,4-cyclohexanedimethanol by pulverizing the distillate obtained above.

Abstract: A process for the dehydrohalogenation of a feed comprised of an admixture of primary, secondary and tertiary alkylhalides to selectively convert the secondary and tertiary alkylhalides of the admixture to olefins by dehydrohalogenation, with minimal conversion, if any, of the primary alkylhalides. The reaction, which is particularly applicable to the selective dehydrobromination of an admixture of primary, secondary and tertiary alkylbromides, is carried out in a distillation-reaction zone, column, or distillation-reactor, to simultaneously (i) convert the secondary and tertiary alkylbromides to olefins and hydrogen bromide, and (ii) separate the olefins and hydrogen bromide, (iii) and the primary alkyl bromides, from the reaction mixture.

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. A method for the production of methyl tertiary butyl ether by reaction of isobutene with methanol in a distillation reaction column is disclosed wherein a liquid level maintained in the distillation reaction zone.

Abstract: A process for removing iodine or soluble iodide impurities from a carboxylic acid or carboxylic acid anhydride, the carboxylic acid or carboxylic acid anhydride having been by a carbonylation process. The process includes: step (a) treating impure carboxylic acid or carboxylic acid anhydride containing iodine or soluble iodide impurities with an unsupported scavenger at a temperature of between 20.degree. and 250.degree. C. and step (b) thereafter separating the treated carboxylic acid or carboxylic acid anhydride from the scavenger. The scavenger is a silver salt in the absence of a trialkyl phosphine, a triaryl phosphine and a heterocyclic aromatic nitrogen compound. The preferred scavenger for acetic acid and acetic anhydride is silver acetate.

Abstract: A method of inhibiting fouling in distillation towers, overhead lines, reflux lines, and condensers operating in a process to manufacture and purify epichlorohydrin. This method resides in treating process streams entering or exiting such towers, lines and condensers, including feed streams, reflux streams, gaseous or liquid overhead streams, with an effective antifouling amount of a C.sub.3 -C.sub.9 linear or branched alkyl substituted catechol, or mixtures thereof.

Abstract: In a process for the production of methyl acetate from methanol and glacial acetic acid involving countercurrently flowing acetic acid and methanol through a single reactive distillation column having an extractive distillation section and a methyl acetate/acetic acid rectification section to obtain methyl acetate in the presence of an acidic catalyst, the improvement which comprises producing ultra high purity methyl acetate by the additional step of introducing acetic anhydride and a salt-free acid catalyst into the reactive distillation column between the extractive distillation section and the methyl acetate/acetic acid rectification section.

Abstract: A process for removing volatile acids from aqueous solutions which involves steam stripping a volatile acid from an aqueous solution and contacting the vaporized acid with a reactable cation to form a salt of the acid. A preferred embodiment of apparatus comprises an elongated distillation column having therein a plurality of zones or stages wherein the volatile acid in the aqueous feed stream is vaporized by steam and then the vaporized acid is carried by the steam into a salt formation zone or stage to react with a reactable cation to form a salt of the acid.

Abstract: An apparatus and process for separating a more volatile substance from a liquid in which it is dissolved by vacuum means. The apparatus has a perforated inner casing having a plurality of sub-stages which contain packing material to provide a tortuous path of interstices for the liquid to flow through; an outer casing surrounds the inner casing to define an evacuating space between the outer and inner casing and vacuum means to create a vacuum in the evacuating space which communicates with the sub-stages through the perforations in the inner casing. The vacuum means also acts to pull off the more volatile substance.

Abstract: An integrated process is provided for converting methanol, dimethylether or the like to heavy hydrocarbon products, especially distillate range hydrocarbons. In a first stage catalytic process oxygenate feedstock is converted to lower olefins. C.sub.3.sup.+ olefins are selectively sorbed in an interstage sorption fractionator and passed along with gasoline sorbent to a second stage oligomerization reactor. Distillate range hydrocarbons are useful as diesel fuel or the like.

Abstract: An improved catalytic process for converting an olefinic feedstock comprising ethylene and C.sub.3.sup.+ olefins to heavier liquid hydrocarbon product comprising the steps of:(a) prefractionating the olefinic feedstock to obtain a gaseous stream rich in ethylene and a liquid stream containing C.sub.3.sup.

Abstract: A process for removing volatile acids from aqueous solutions which involves steam stripping a volatile acid from an aqueous solution and contacting the vaporized acid with a reactable cation to form a salt of the acid. A preferred embodiment of apparatus comprises an elongated distillation column having therein a plurality of zones or stages wherein the volatile acid in the aqueous feed stream is vaporized by steam and then the vaporized acid is carried by the steam into a salt formation zone or stage to react with a reactable cation to form a salt of the acid.

Abstract: A process is described for the production of alcoholates from alkali metal hydroxides and aliphatic alcohol which in their molecule contain 1 to 6 carbon atoms. The alcoholates are produced in that alkali metal hydroxide is mixed with an alcohol and is reacted with said alcohol at a temperature from 80.degree. to 110.degree. C., preferably from 80.degree. to 100.degree. C., and under a pressure from 0.3 to 1.2 bars, the alcohol water mixture which evaporates during the reaction is separated into its components by at least one membrane, the alcohol vapor and the water vapor are condensed and the condensed alcohol is recycled to the reaction.

Abstract: Waste oil is treated in a tubular reactor having a length of up to and in excess of 2 km in a plurality of stages each of which involves heating the product to a different temperature and maintaining the product at a different pressure. The released fractions are evacuated from the path for the flow of waste oil and are immediately condensed and distilled to yield a variety of products from oil having a low boiling point to coke. One or more withdrawn fractions can be treated (for example, hydrogenated) in one or more discrete tubular reactors. The heating can involve raising the temperature of waste oil to several times the critical cracking temperature, and the regulation of pressure can involve a reduction of pressure to less than 1 mbar. The last stage of the reactor can be cleaned by abrasive particles, by vibration at high frequencies and/or by acceleration of the conveyed stream to an elevated speed.

Abstract: Primary and secondary hydroperoxide contaminants in a tertiary hydroperoxide composition obtained by oxidation of a branched hydrocarbon are removed by contacting the tertiary hydroperoxide with a carboxylic acid derivative such as an anhydride and a basic compound such as sodium hydroxide. A tertiary hydroperoxide such as tertiary butyl hydroperoxide is purified with minimal loss of the desired tertiary hydroperoxide.

Abstract: A process for the preparation of ethyl trifluoroacetate, in which:in a first stage, trifluoroacetic acid is brought into contact with a slight excess of ethanol in the presence of concentrated sulfuric acid and a solvent, the solvent having a boiling point higher than that of trifluoroacetic acid and specific gravity relative to water less than 1 and which solvent does not form an azeotrope with ethyl trifluoroacetate, and then carrying out a phase separation and removing the sulfuric layer, followed, if required, by an additional stage in which concentrated sulfuric acid is added to complete the esterification;in a second stage, an additional quantity of sulfuric acid and trifluoroacetic acid is introduced and a phase separation is then carried out to remove the sulfuric layer; andin a third stage, the mixture obtained in the second stage is distilled to recover ethyl trifluoroacetate.

Abstract: In the hydroformylation of alkenes to aldehydes, rhodium is recovered from the stripped overhead of the hydroformylation reactor by condensing the overhead, removing the bulk of the aldehyde product from the condensed overhead, stripping the residue which remains with nitrogen gas to remove minor amounts of highly volatile aldehyde product remaining in the residue and redistilling the residue to remove components from the condensed overhead which are lower boiling than the catalyst components. The catalyst components including rhodium and phosphine ligand are returned to the hydroformylation reactor.

Abstract: A process for purifying exo-2-hydroxy-1,4-cineole contaminated with ketones is carried out by derivatizing the ketone to form a compound readily separable from the desired cineole, either by distillation, solvent extraction or like separation process. In one embodiment method of the invention, derivatization is carried out by reaction of the ketone with an amine. The amine reacts with the ketone impurities to form water and relatively stable enamine derivatives that have a much lower vapor pressure than the exo-2-hydroxy-1,4-cineole. The desired product may then be separated by distillation.

Abstract: A process which comprises treating butyrolactone in at least 95% purity with an acid to convert and remove color forming impurities for product stabilization.

Abstract: An oligomerization system is provided for upgrading lower olefins to distillate hydrocarbons, especially useful as high quality jet or diesel fuels. Thye olefinic feedstock is reacted over a shape selective acid zeolite, such as ZSM-5, to oligomerize feedstock olefins and further convert recycled hydrocarbons. Reactor effluent is fractionated to recover a light-middle distillate range product stream and to obtain gasoline and heavy hydrocarbon streams for recycle.

Abstract: The invention concerns a process for manufacturing methyl tert-butyl ether (MTBE) by reacting methanol with an isobutene-containing hydrocarbon mixture.This process is characterized by the steps of:introducing the reactants into a reaction-distillation zone containing at least two superposed and non-contiguous fixed beds (2a, 2b) of catalyst of the sulfonated resin type, wherein passage-ways are provided for a vapor phase, at least one distillation tray (4a), at least one liquid redistribution tray (5),maintaining distillation conditions in said zone so as to have a descending liquid phase and an ascending vapor phase,maintaining a continuous liquid phase in the lower part of said beds,discharging a vapor phase containing a high proportion of unconverted hydrocarbons from the top (8) of said zone, andwithdrawing a liquid phase of high MTBE content from the bottom (10) of said zone.