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: 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: Ethane is catalytically dehydrogenated in a reaction zone comprising at least two separate beds of dehydrogenation catalyst. The reactants are reheated and hydrogen is consumed through use of an intermediate bed of hydrogen selective oxidation catalyst. The amount of hydrogen consumed in the combustion step is increased by cooling the effluent of the first dehydrogenation catalyst bed by direct or indirect heat exchange.

Abstract: A process flow for a catalytic oligomerization process is presented. The feed contacts a solid catalyst in a tubular reactor cooled by indirect heat exchange. The mixed-phase coolant used in the reactor is the reactor effluent itself, which has been cooled by indirect heat exchange and depressurized. The reactor effluent is then passed into a rectified separation zone. The heat picked up by the effluent stream in the reactor is thereby used in separating light hydrocarbons from the effluent to produce a recycle stream.

Abstract: Hydrocarbons are catalytically dehydrogenated in a reaction zone comprising at least two separate beds of dehydrogenation catalyst. The reactants are reheated and hydrogen is consumed through use of an intermediate bed of hydrogen selective oxidation catalyst. The amount of hydrogen consumed in the combustion step is increased by cooling the effluent of the first dehydrogenation catalyst bed by direct or indirect heat exchange.

Abstract: Plural vertical tube reactor provides downward flow only, in a serial manner, through a plurality of sets of tubes containing a particulate contact material such as a catalyst which are located in adjacent sectors or reigons of a shell and tube reactor. An empty tube(s) is provided to carry the reactant fluid upwardly from the bottom of one sector of tubes to the top of another. In a two sector configuration, the upper and lower end chambers are each partitioned in half, but the lower partition has a screened port to allow reacted fluid from the first sector to reach, and move upwardly through, an empty tube(s) in the second sector which is isolated from the other tubes in the second sector at its bottom end but not at its top end.

Abstract: A method is disclosed for fractionating a hydrocarbon conversion zone effluent stream comprising at least three components which are to be isolated into separate streams. A two-column system for fractionating the effluent of a benzene alkylation zone is employed. The overhead vapor of a downstream second column is condensed in a side reboiler of a preceding recycle column. This side reboiler is located between the feed point to the recycle column and a separate reboiler located at the bottom of the recycle column. The utilities cost of performing the fractionation is reduced.

Abstract: A hydrocarbon conversion process for light olefin isomerization is disclosed. The feed stream is admixed with the overhead vapor stream of a fractionation column, which also acts as a feed stream drying column. The resultant admixture flows through an isomerization zone, and the isomerization zone effluent is partially condensed and passed into the overhead receiver of the column. Uncondensed vapor from the overhead receiver is recycled to the isomerization zone as a hydrogen recycle stream and liquid hydrocarbons withdrawn from the receiver are charged to the top of the fractionation column as the feed stream to the column.

Abstract: A multi-step hydrocarbon conversion process for producing gasoline from propane or butane is disclosed. The feed hydrocarbon is passed into a dehydrogenation zone and the entire dehydrogenation zone effluent including hydrogen and light by-products is then passed into a catalytic condensation zone wherein the resulting olefins are converted into dimers and trimers. The condensation zone effluent stream is passed into a separation zone in which the dimers and trimers are concentrated into a product stream, with unconverted feed hydrocarbon and hydrogen being recycled to the dehydrogenation zone.

Abstract: A process for producing gasoline from a charge stream comprising a mixture of butanes and butylenes is disclosed. The quality of a product alkylate is improved by increasing the butene-2 content of an alkylation zone feed stream. A first portion of the charge stream is passed into a dimerization zone in which isobutylene is reacted with normal butylenes, with butene-1 being reacted to a greater extent than butene-2. A C.sub.8 hydrocarbon-containing product stream and a C.sub.4 stream having a higher butene-2 concentration than the charge stream are recovered from the dimerization zone. This high butene-2 content C.sub.4 stream is admixed with a second portion of the charge stream and passed into an alkylation zone wherein butylenes are reacted with isobutane to yield a second product stream containing C.sub.8 hydrocarbons.

Abstract: A multi-step hydrocarbon conversion process for producing gasoline from butane is disclosed. Butane is passed into a dehydrogenation zone and the entire dehydrogenation zone effluent is then passed into a catalytic condensation zone wherein butylene is converted into C.sub.8 and C.sub.12 hydrocarbons. The condensation zone effluent, a stripper overhead stream and an absorber bottoms stream are commingled and then separated into vapor and liquid portions. The liquid is passed into the stripper, and the vapor portion is contacted with stripper bottoms liquid in an absorber. The absorber overhead stream is contacted with liquid butane in a second absorber to remove C.sub.8 hydrocarbons and is then recycled to the dehydrogenation zone. Debutanizing a portion of the stripper bottoms yields the liquid butane and a gasoline product.

Abstract: A multi-step hydrocarbon conversion process for producing gasoline from propane is disclosed. Propane is passed into a dehydrogenation zone and the entire dehydrogenation zone effluent is then passed into a catalytic condensation zone wherein propylene is converted into C.sub.6 and C.sub.9 hydrocarbons. The condensation zone effluent, a stripper overhead stream and an absorber bottoms stream are commingled and then separated into vapor and liquid portions. The liquid is passed into the stripper, and the vapor portion is contacted with stripper bottoms liquid in an absorber. The absorber overhead stream is contacted with liquid propane in a second absorber to remove C.sub.6 hydrocarbons and is then recycled to the dehydrogenation zone. Depropanizing a portion of the stripper bottoms yields the liquid propane and a gasoline product.

Abstract: A process for the simultaneous production of gasoline blending components and a phthalate ester useful as a plasticizer. C.sub.3 to C.sub.4 olefins are reacted in an oligomerization zone to form a mixture containing C.sub.6 to C.sub.10 olefinic hydrocarbons. A three carbon number boiling range intermediate fraction is recovered from this mixture. The less highly branched olefins in this intermediate fraction are selectively hydroformylated to yield alcohols which are then reacted with an aromatic carboxylic acid or an aromatic anhydride. The unhydroformylated olefins are combined with the other olefinic hydrocarbon fractions to form a high octane motor fuel.

Abstract: A process for the isomerization of normal olefinic hydrocarbons is disclosed. The feed stream is passed through a first reaction zone and is then cooled sufficiently to cause the condensation of from about 1 to 25 mole percent of the hydrocarbons in the isomerization zone effluent stream. The uncondensed portion of the effluent of the first reaction zone is heated and passed through a second reaction zone which is maintained at a lower temperature than the first reaction zone. The product isomer is recovered from the effluent of the second reaction zone.

Abstract: A process for the simultaneous production of gasoline blending components and a phthalate ester useful as a plasticizer. C.sub.3 to C.sub.4 olefins are reacted in an oligomerization zone to form a mixture containing C.sub.6 to C.sub.10 olefinic hydrocarbons. A three carbon number boiling range intermediate fraction is recovered from this mixture. The less highly branched olefins in this intermediate fraction are selectively hydroformylated to yield alcohols which are then reacted with an aromatic carboxylic acid or an aromatic anhydride. The unhydroformylated olefins are combined with the other olefinic hydrocarbon fractions to form a high octane motor fuel.

Abstract: A multiple-stage steam reforming process for producing a substitute natural gas from kerosene boiling range hydrocarbons. Initially, a lower-boiling feedstock is steam reformed and a portion of the effluent is subjected to hydrogen-producing conditions to provide a vaporous phase enriched in hydrogen content. This vaporous phase is utilized throughout the reaction zone circuit to decrease the extent to which carbon becomes deposited upon the various catalytic composites, and especially with respect to those reaction zones in which the kerosene boiling range hydrocarbons are processed. Gasification of the kerosene fractions is effected at a minimum catalyst temperature of about 840.degree. F. (448.9.degree. C.) and a maximum catalyst temperature of about 1,000.degree. F. (537.8.degree. C.).

Abstract: Alkylaromatic hydrocarbons including ethylbenzene are dehydrogenated in a vapor phase reactant stream, preferably at subatmospheric conditions. The resultant reaction zone effluent is partially condensed and then separated in a subatmospheric product settler. Hydrocarbons from the product settler are fractionated to yield a styrene bottoms stream, an overhead liquid recycled to the reaction zone and an overhead vapor. This vapor is admixed with vapors from the product settler, compressed to a superatmospheric pressure, and partially condensed to form a liquid which is fractionated to remove the net light aromatic hydrocarbons produced in the process.

Abstract: A butene mixture is separated to yield an n-butene rich product and an isobutylene rich product in a fractionator system. The fractionator reflux is isomerized before introduction into the fractionator. Other suitable olefins may be separated in a similar manner.

Abstract: A continuous catalytic reaction and catalyst reactivation process is performed using a simulated moving catalyst bed to effect simultaneously in different zones of a multi-zone fixed catalyst bed an alkylation reaction of olefinic and aromatic reactants and a reactivation of catalyst.