Abstract: A distributor device for effecting the uniform distribution of a mixed-phase vapor/liquid reactant stream across the upper surface of a fixed-bed of catalyst particles. Mixed-phase reactants or components are first separated into a principally vapor-phase and a principally liquid-phase. These separated phases are then re-mixed in a manner which creates a vapor/liquid froth; the latter being re-distributed to the upper surface of the bed of catalyst particles. Briefly, the distributor comprises three chordal-form, catalyst-free volumes which are defined by the interior surface of the chamber and three pairs of spaced-apart, parallel chordal baffles.

Abstract: An improved isoparaffin/olefin HF alkylation process designed to function absent the commonly-utilized acid regenerator. Polymer products, formed during the alkylation reaction, are recovered with the normally liquid alkylate product, substantially free from HF, without effecting degradation in the product quality. In addition to enhanced economic considerations stemming from a reduction in equipment costs, the operational stability of the process is significantly improved.

Abstract: A distributor device for effecting uniform distribution of a fluid stream to a fixed-bed of catalyst particles. Distribution of a vaporous phase, liquid phase, or a mixed-phase is effected in a plurality of spaced-apart parallel conduits, each of which consists of two concentric and coaxial perforated pipes. Fluid for distribution is introduced into the inner conduit, while fluid from that portion of catalyst above the device flows into the outer conduit and is distributed therefrom into the catalyst particles below.

Abstract: Ethylene and maximum benzene are co-produced via a combination process involving (1) thermal cracking, or pyrolysis, (2) aromatic hydrocarbon separation, or extraction, and, (3) dealkylation of alkyl-substituted aromatics to yield additional benzene. Unconverted feed paraffins are recycled to thermal cracking for additional ethylene and benzene production.

Abstract: A catalytic reaction chamber for contacting a reactant stream with catalyst particles which are disposed as an annular-form bed and are downwardly movable therethrough via gravity-flow. The annular catalyst bed is spaced between a catalyst-retaining screen and a scalloped, perforated centerpipe. A plurality of vertically-positioned catalyst-transfer, or withdrawal, conduits are circumferentially-disposed substantially adjacent the outer surface of the scalloped centerpipe and extend the entire length of the catalyst bed. These contain a first plurality of apertures which face into the bed of catalyst particles and which are sized to permit catalyst particles to flow therethrough. A second plurality of apertures is disposed opposite the first plurality of apertures, and sized to inhibit the flow of catalyst particles therethrough.

Abstract: A multiple-stage catalytic conversion system in which a hydrocarbonaceous charge stock and hydrogen flow serially through a plurality of catalytic reaction zones in each of which the catalyst particles are downwardly movable via gravity-flow. Dissimilar catalyst particles are utilized in the reactor systems, each of which is integrated with separate regenerating towers through which the catalyst particles are also downwardly movable via gravity-flow. Dissimilarity of the catalysts stems from a difference in activity and stability characteristics. In turn, this difference may be attributed either to physical, or chemical changes between the two composites, or a combination of both.

Abstract: A multiple-stage catalytic conversion system in which a hydrocarbonaceous charge stock and hydrogen flow serially through a plurality of catalytic reaction zones in each of which the catalyst particles are movable via gravity-flow. Dissimilar catalyst particles are utilized in the reactor systems which share a common regenerating tower through which the catalyst particles are also downwardly movable via gravity-flow. Dissimilarity of the catalyst particles stems from a difference in activity and stability characteristics. In turn, this difference may be attributed either to physical, or chemical changes between the two composites, or both.

Abstract: Field butanes, otherwise introduced into an isostripping column, also utilized to recover alkylate product from unreacted isobutane, are separately fractionated to provide an isobutane concentrate and a normal butane concentrate. The former is increased in pressure and reacted with the olefinic feed stream in admixture with HF-acid catalyst. The latter is introduced into the reaction zone wherein it is vaporized via indirect contact with the reaction mixture. Vaporous normal butane is introduced into the fractionation facility wherein the exothermic heat of reaction serves to separate the field butane stream. Alkylation reactions can thus be conducted at sub-ambient temperatures which results in an alkylate product of improved quality. This technique also obviates the necessity for a cooling water system, thus eliminating the possibility of HF-acid contamination of water bodies.

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: Hydrocarbonaceous black oils are converted into lower-boiling hydrocarbons via a process which utilizes two separate catalytic reactor systems interconnected by way of a multiple-stage separation facility. Fresh feed charge stock is reacted in the first reactor system in admixture with hydrogen recovered from the second reactor system. Conversely, unconverted material from the first reactor system is reacted in the second system with make-up hydrogen and all the recycle hydrogen recovered from both reactor systems.

Abstract: Multiple-stage separation of a mixed-phase product effluent resulting from the hydrocracking and/or hydrorefining conversion of a hydrocarbonaceous charge stock. Reaction product effluent is initially separated in a high temperature, high pressure first separation zone, the vapor phase from which is cooled and separated in a second separation zone to provide a hydrogen-rich vaporous phase. The liquid phase from the second separation zone is increased in temperature and separated in a third separation zone at a substantially lower pressure. At least a portion of the liquid phase from the third separation zone is combined with the vaporous phase from the first separation zone prior to cooling and separation in the second separation zone. A savings of about 10.0% in hydrogen loss is realized or about 12 standard cubic feet per barrel of charge stock.

Abstract: Selected aromatic hydrocarbon concentrates -- benzene, mixed xylenes, etc. -- are produced by way of a combination process which involves catalytic reforming followed by hot flash separation of a portion of the reformed product and dealkylation of the resulting hot flash liquid phase in admixture with a second portion of the reformed product. Although the process affords flexibility respecting the precise aromatic concentrate produced, it is particularly directed toward the maximization of benzene from normally liquid naphtha hydrocarbons boiling up to about 425.degree. F. (218.degree. C.).

Abstract: Selected aromatic hydrocarbon concentrates -- benzene, mixed xylenes -- are produced by way of a combination process which involves catalytic reforming followed by dealkylation. Although the process affords flexibility respecting the precise aromatic concentrate produced, it is particularly directed toward the maximization of benzene.

Abstract: Selected aromatic hydrocarbon concentrates--benzene, mixed xylenes, etc.--are produced by way of a combination process which involves catalytic reforming followed by hot flash separation and dealkylation of the separated hot flash liquid phase. Although the process affords flexibility respecting the precise aromatic concentrate produced, it is particularly directed toward the maximization of benzene.

Abstract: A catalytic reaction chamber for contacting a reactant stream with catalyst particles which are disposed as an annular-form bed and are downwardly movable therethrough via gravity-flow. The annular bed is spaced between a catalyst-retaining screen and a perforated centerpipe. A plurality of vertically-positioned catalyst-transfer, or withdrawal, conduits are circumferentially-disposed substantially adjacent the outer surface of the centerpipe and extend the entire length of the catalyst bed. These contain a first plurality of apertures which face into the bed of catalyst particles and which are sized to permit catalyst particles to flow therethrough. A second plurality of apertures is disposed substantially 180.degree. opposite the first plurality of apertures, and sized to inhibit the flow of catalyst particles therethrough.

Abstract: Distribution of a mixed-phase, vapor/liquid reactant stream to a fixed-bed of catalyst particles is accomplished through the use of a distributor tray in the form of a horizontal plate (or deck) having a plurality of vertically-disposed venturi-shaped eductors. The distributing device is installed within a substantially catalyst-free area of the reaction chamber and serves (i) to initially distribute the reactant stream as a froth to the reaction chamber and/or, (2) to distribute the effluent from one bed of catalyst particles to the next succeeding bed of catalyst particles.

Abstract: Uniform reactor temperature and temperature control of an HF acid-catalyzed reactant mixture of isobutane and an olefinic feed stream is achieved through indirect vaporization of a liquefied hydrocarbon by the reaction mixture. The exothermic heat of reaction is utilized to effect a fractional distillation. This concept and technique obviates the need for a water-cooled exchanger, thereby eliminating the possibility of HF-acid contamination of water bodies.

Abstract: A method and distributor device for effecting the uniform distribution of a mixed-phase vapor/liquid reactant stream across the upper surface of a fixed-bed of catalyst particles. Mixed-phase reactants or components are first separated into a principally vapor-phase and a principally liquid-phase. These separated phases are then re-mixed in a manner which creates a vapor/liquid froth; the latter being re-distributed to the upper surface of the bed of catalyst particles. Briefly, the distributor comprises three annular-form, catalyst-free volumes which are defined by the interior surface of said chamber and three cylindrical walls in concentric relationship therewith.

Abstract: A catalytic reaction chamber for contacting a reactant stream with catalyst particles which are disposed as an annular-form bed and are downwardly movable therethrough via gravity-flow. The annular bed is formed between a catalyst-retaining screen and a perforated center-pipe. A plurality of vertically-positioned catalyst-transfer, or withdrawal, conduits are circumferentially-disposed substantially adjacent the outer surface of the centerpipe and extend the entire length of the catalyst bed. These contain a plurality of apertures which face into the bed of catalyst particles and which are sized to permit catalyst particles to flow therethrough. The use of these perforated catalyst-transfer conduits serves to alleviate the problems associated with the occurrence of stagnant catalyst areas which result from catalyst particles being "pinned" against the perforated centerpipe within the reaction zone, and unable to assume a downward flow pattern.

Abstract: Normal paraffinic hydrocarbons, having from three to about twenty carbon atoms per molecule, are dehydrogenated to produce corresponding linear mono-olefins.These are separated from unreacted paraffins, preferably via an adsorption-separation technique. Raffinate, containing the unreacted normal paraffins, is subjected to mild hydrotreating, as is the hydrogen-rich vaporous phase recovered from the dehydrogenation zone product effluent,to saturate the olefins therein. Hydrotreated effluent is introduced, generally in admixture with fresh feed paraffins, into the dehydrogenation reaction zone.This technique avoids by-product dehydrogenation reactions otherwise resulting in non-linear mono-olefins, di-olefinic hydrocarbons and aromatics.