Abstract: A process for the nonoxidative dehydrogenation of an alkylaromatic feed stream wherein the feed stream is passed through a radial reactor containing nonoxidative dehydrogenation catalysts, wherein the nonoxidative dehydrogenation catalysts are arranged in vertically layered beds within the radial reactor, and wherein the nonoxidative dehydrogenation catalysts include at least a first and a second nonoxidative dehydrogenation catalyst, wherein at least one of the nonoxidative dehydrogenation catalysts has a different performance and/or operating characteristic than at least one of the other nonoxidative dehydrogenation catalysts.

Abstract: Process for the catalytic dehydrogenation of ethylbenzene in which a feedstock containing ethylbenzene and steam is supplied into the inlet of a tubular reactor containing a dehydrogehation catalyst. Within the reactor, the feedstock flows through at least a portion of the reactor along a spiral flow path extending longitudinally of the reactor. The resulting styrene product is then recovered from a downstream or outlet section of the reactor. The spiral flow path through which the feedstock is passed is located at least adjacent the inlet side of the reactor and at least a portion of the spiral flow path contains a particulate dehydrogenation catalyst. The spiral flow path may extend throughout a major portion of the elongated tubular reactor and may contain a particulate dehydrogenation catalyst in a substantial portion there.

Abstract: A hydrocarbon gas to be decomposed, optionally mixed with water vapor, is allowed to flow through the gap between various porous tubes 4 constituting a group of porous tubes provided extending vertically in a decomposition reaction column 1 while air or oxygen is jetted homogeneously from the interior to the exterior of the porous tubes in the direction perpendicular to the stream of the hydrocarbon gas to be decomposed, optionally mixed with water vapor. The mixture is then ignited to form a diffusion flame layer B on the outer surface of the porous tubes 4. With the diffusion flame layer as a heat source, the hydrocarbon gas to be decomposed, optionally mixed with water vapor, undergoes pyrolysis.

Abstract: A process for hydrocarbon conversion to prepare lower olefins such as ethylene, propylene, etc., and light aromatics by bringing hydrocarbons into contact with a solid granular catalyst. In order to optimize the reaction conditions and product structure and save the capital and operating costs, a piston flow reactor is used in this process and multiple groups of feed inlets, which allow hydrocarbons with different properties to enter the device from different feed inlets and proceed pyrolysis under different operation conditions, are set on the reactor. This process is usable for individual pyrolysis or co-feed pyrolysis of hydrocarbons from refinery gases, liquid hydrocarbons, to heavy residues.

Abstract: The present invention is directed to a continuous process for producing a desired hydrocarbon product using a heterogeneous slurry catalyst, to the product of said process, and to the reactor utilized in such process.

Abstract: This invention pertains to a continuous catalytic process, for example, for the metathesis of olefins that uses a catalyst circulating in a moving bed in at least one reaction zone operating in the liquid phase and in a regenerator, with a lift to transfer the deactivated catalyst emerging from the reaction zone to the regenerator, whereby said process is characterized by the fact that the transfer is accomplished by a gas that does not react with the catalyst and with the stripping off of at least a portion of the organic matter that is adsorbed on the deactivated catalyst.

Abstract: Upgrading of a hydrocarbon feed containing sulfur, metals, and asphaltenes involves applying the feed to a distillation column for producing a substantially asphaltene-free, and metal-free fraction and a non-distilled fraction containing sulfur, asphaltenes, and metals. At least some of the substantially asphaltene-free, and metal-free distillate fraction is converted to a hydrogen donor diluent. The non-distilled fraction is processed in a solvent deasphalting unit for producing a deasphalted oil stream and an asphaltene stream. After a combined stream is formed from the hydrogen donor diluent and the deasphalted oil stream, the combined stream is thermally cracked forming a thermally cracked stream that is applied to the distillation column.

Abstract: A process for thermal pyrolysis of a feedstock containing at least 80% ethane to convert to ethylene at a conversion rate of at least equal 80% by feeding the feedstock into a reaction zone in which heating means are arranged approximately perpendicular to the direction of flow of the feedstock. The temperature of the outlet of the heating zone in the reaction zone is between 880 and 960° C. and the dwell time of the feedstock in the heating zone is between 1005 and 3000 milliseconds.

Abstract: Processes and apparatus for providing improved catalytic cracking, specifically improved recovery of olefins, LPG or hydrogen from catalytic crackers. The improvement is achieved by passing part of the wet gas stream across membranes selective in favor of light hydrocarbons over hydrogen.

Abstract: The specification describes a method and a fixed bed apparatus for producing olefinic hydrocarbons from a charge of saturated aliphatic hydrocarbons with 2 to 20 carbon atoms and hydrogen in a chamber 1 comprising a plurality of parallel tubes 3 filled with a catalyst and arranged in rows. A so-called reaction phase and a catalyst-regenerating phase are carried out in the tubes of the chamber. The tubes are heated by appropriate radiant heating means 6, arranged in layers substantially perpendicular to the tubes. These layers heat a first part of the tubes (at the feed side) with a heat flux greater than the mean heat flux of the chamber and a second, subsequent part with a mean flux no more than equal to the mean heat flux, so that the isothermicity of the catalyst is substantially maintained, using appropriate control means.

Abstract: A process and apparatus for indirectly heating an endothermic reaction by combustion of reactants or products from the endothermic reaction using a plate heat exchange arrangement in a highly efficient manner. This invention is particularly suited for processes such as the production of styrene or synthesis gas. When producing synthesis gas, oxidizing reactants in a secondary reforming step generates heat for a primary reforming step and the process improves selectivity and yield with a highly efficient heat exchange step that uses narrow channel for indirect heat exchange. The narrow channels are preferably defined by corrugated plates. The primary reaction channels will contain a catalyst for the promotion of the primary reaction such as steam reforming or ethylbenzene dehydrogenation.

Abstract: A process and apparatus produces reaction products by indirectly preheating and heating reactants by indirect heat exchange. The use of the preheating step simplifies the reaction zone design by eliminating the need for external exchangers and is particularly suited for an arrangement of plates that defines narrow channels for indirect heat exchange. The narrow channels are preferably defined by corrugated plates. The primary reaction channels will contain a catalyst for the promotion of the desired reaction product from the principal reactants. The heating fluid passes through adjacent heating channels defined by shared partition plates to provide indirect heating. At least a portion of the heating channels exchange heat with a non-catalytic portion of the reaction channels to preheat the reactants ahead of a catalytic section of the reaction channels. Catalytic combustion within the heating channels may provide in-situ heat input for the heating medium.

Abstract: A channel reactor arrangement and a process uses a heat exchange fluid with a high thermal density to indirectly heat or cool the reactants by indirect heat exchange. The system brings the efficiency of plate reactor arrangements to the effectiveness of high heat capacity heat exchange fluids such as molten salts and liquid metals. The channel reactor arrangement maintains a limited temperature gradient through the channels at all points to improve process selectivity. This type of arrangement is of a particular advantage where the reaction zone uses a heterogeneous catalyst system within a heat exchanging reaction section. The plate and channel heat transfer arrangement is particularly beneficial because of its high surface area provided per unit volume of channels.

Abstract: The metal surface protected against metal-dusting corrosion has an insulating layer of a gas-permeable, thermally insulating material. The side of the thermal insulating layer that is colder during operation is in direct vicinity of the metal surface, and the side of the insulating layer that is hotter during operation is heated by a gas stream containing carbon monoxide, which in addition contains hydrogen and/or steam and has a temperature in the range from 300 to 1700.degree. C. In the region between the metal surface to be protected and the hot side of the insulating layer a catalyst is provided for reacting carbon monoxide with hydrogen and/or steam.

Abstract: A method to condense or coalesce matter is carried out by providing a suitable, narrow passageway for throughput of matter in a vapor state, and passing the matter in a vapor state through said passageway, under conditions such that the matter is coalesced into a more ordered state. Also, a matter coalescing apparatus has a hollow housing in communication with at least one of--(A) a plurality of suitably narrow hollow passageways and (B) a suitably narrow, elongately hollow, matter-coalescing passageway--for throughput of matter to include as a vapor therein. Consequently, highly efficient yields of coalesced matter, to include liquid coalesced from vapor, even under only mild vacuum or at about ambient atmospheric pressure can be obtained. This is especially so with respect to oils, where yields as high as 95 percent or greater can be provided hereby. The invention can be practiced under such outstanding yield efficiencies without a general need for significant external cooling.

Abstract: Catalyst particles are separated from the wax in a Fischer-Tropsch reactor by feeding a portion of the reactor slurry to a dynamic settler which does not require any pump. As the slurry flows down a pipe in the center of the settler, the slurry flows into the surrounding annular region at the bottom of the settler. The heavier catalyst particles settle down and are removed as the slurry at the bottom of the settler is recycled back to the reactor. The wax rises up in the annular section and this clarified wax is removed by a wax outlet pipe. In an embodiment with an expanded diameter section above the Fischer-Tropsch reactor an additional dynamic settler can be placed inside this section. The Fischer-Tropsch catalyst can be regenerated by purging the catalyst with an inert gas for a period of time and by treating the catalyst with naphtha.

Abstract: A thermowell assembly and method which allows for arresting leakage in the case a thermowell begins to leak in a hydroprocessing process without having to shut down a flow of a hydrocarbon feed stream through a hydroconversion reaction zone in the hydroprocessing process. The thermowell assembly comprises a first hollow sleeve section which supports a thermowell member, a ferrule sealing member which engages the first hollow sleeve section, a second generally cup-shaped second sleeve section wherethrough a thermocouple member slidably passes, and an outer sleeve member for maintaining the union of the first sleeve section, the ferrule sealing member, and the second sleeve section. The method comprises severing and/or removing the thermocouple member from the commenced-leaking thermowell member and placing a high pressure cap over an aperture left vacant by the thermocouple member to seal-off the leaking thermowell member from the atmosphere.

Abstract: The proposed method comprises passing the hydrodynamic flow of liquid hydrocarbons through a flow-through passage accomodating a baffle body providing for a local constriction of the flow; establishing the local flow constriction on at least one portion of the flow-through passage whose cross-sectional profile area is so selected as to maintain such a velocity of the flow on the portion of the passage that promotes the development of a hydrodynamic cavitation field past the baffle body having the degree of cavitation of at least one; processing the flow of a mixture of liquid hydrocarbons in the hydrodynamic cavitation field to initiate chemical transformations of liquid hydrocarbons resulting in a change in the qualitative and quantitative composition of the mixture of liquid hydrocarbons.

Abstract: A distributor assembly for hydroprocessing a hydrocarbon mixture of hydrogen-containing gas and liquid hydrocarbon is presented. The distributor assembly has a circular plate with a plurality of hollow risers bound thereto for distributing hydrogen-containing gas and liquid hydrocarbon through openings in the circular plate member. Each of the hollow risers has a tubular opening In its associated side. The distributor assembly is connected to an internal wall of a reactor. A method is also presented for hydroprocessing a hydrocarbon feed stream comprising flowing a mixture of hydrogen-containing gas and liquid hydrocarbon into a reactor zone to produce evolved hydrogen-containing gas; and flowing the mixture of hydrogen-containing gas and liquid hydrocarbon through a plurality of tubular zones while admixing simultaneously therewith the evolved hydrogen-containing gas.

Abstract: An apparatus for mixing vapor and liquid reactants within a column. The apparatus forms a first mixing zone into which a first reactant (e.g., vapor) is homogenized by swirl flow and flows vertically downward. The apparatus further forms a second mixing zone into which a second reactant (e.g., liquid) is homogenized by swirl flow and flows vertically downward. Additional amounts of either the first reactant, the second reactant or both may be added into or ahead of the first mixing zone or the second mixing zone as appropriate. The first reactant is directed radially to collide in crossflow with a thin sheet of the second reactant to provide intense mixing of the first and second reactants. Due to separate mixing zones for the two reactants, the mixing conditions for each can be tailored to best mix each reactant while minimizing pressure drop and minimizing the space and volume requirements for this mixing.

Abstract: The invention relates to a process for producing petrol of high octane number by catalytic reforming of hydrocarbons by passing these hydrocarbons through a platinum/rhenium catalyst arranged in the form of a hollow cylinder at 450.degree.-500.degree. C. and a pressure of 1.5-3 MPa in a direction perpendicular to the cylinder axis, in which the feed mixture is passed through in the direction from the cylinder axis to the circumference thereof. The invention further relates to a reactor for carrying out the process mentioned, in particular as shown in FIG. 1.

Abstract: The invention relates to a process for the production of acetylene and synthesis gas by partial oxidation of hydrocarbons with oxygen, wherein the gaseous reactants are separately preheated, intimately mixed in a mixing zone, reacted after passing a burner block and rapidly quenched with an aqueous quench medium after reaction, further characterized in that the aqueous quench medium is recirculated in a closed system. Preferably the ratio of the gaseous reactants is selected in such a way that acetylene and soot produced in the reaction are obtained in a weight ratio of 50 to 500.

Abstract: Disclosed is a process for continuous alkylation of aromatics or their derivatives in the presence of a solid acid catalyst in a liquid-solid circulating fluidized bed system, said system comprising a liquid-solid cocurrent upflow reactor, a sedimentation washing tower for the used catalyst, a liquid-solid cocurrent upflow regenerator, a sedimentation washing tower for the regenerated catalyst, and two vortical liquid-solid separators. By regeneration of the used catalyst, continuous alkylation process is achieved in this system.

Abstract: Steam-free non-catalytic cracking of hydrocarbons in reaction zomes each having surfaces heated externally and a heated surface to volume ratio above 3 cm-.sup.1, at a rate such that the flow through each reaction zone is essentially laminar.

Abstract: A reactor arrangement and process for indirectly contacting a reactant stream with a heat exchange stream uses an arrangement of corrugated heat exchange plates to control temperature conditions by varying the number and/or the arrangement of the corrugations along the plates. The reactor arrangement and process of this invention may be used to operate a reactor under isothermal or other controlled temperature conditions. The variation in corrugation arrangements within a single heat exchange section is highly useful in maintaining a desired temperature profile in an arrangement having a cross-flow of heat exchange medium relative to reactants. The corrugations arrangement eliminates or minimizes the typical step-wise approach to isothermal conditions.

Abstract: A method of separating a mixture of gases by the following stages:a) absorbing a part G2 of a gas mixture G1 by a solvent L1 in an absorption zone C1;b) expanding the solvent L1, leading to partial vaporization of the absorbed gases G2 and cooling of the solvent L1;c) desorbing the gas fraction G2 in a desorption apparatus D1 having a reboiling zone B1 and an internal heat exchange zone Z1, wherein the solvent L1 from stage (b) is circulated in countercurrent contact with the vapor phase, and simultaneously has counter-current heat exchange with the solvent phase from the reboiling zone B1;d) passing the regenerated solvent leaving the reboiling zone B1 into the heat exchange zone Z1, and transferring the regenerated solvent to the top of said internal heat exchange zone; ande) recycling the regenerated solvent to the absorption zone C1.

Abstract: A process and apparatus for the thermal conversion of methane into hydrocarbons of higher molecular weight, comprising a reactor (1) of elongate form, connected on the one hand, at a first end, to means (5) for supplying gaseous mixture containing methane (process gas) and on the other, at the opposite end, to discharge means (10), the said reactor comprising on a first part (the first end side) a plurality of elements disposed in at least two layers, substantially parallel inter se and substantially perpendicular to the axis of the reactor, at least one of these layers comprising a series of sheaths (4) inside which there are electric heating means (3) which thus form a layer of heating elements, the said elements being disposed in such a way as to define between them and/or between the layers which they form and/or between them and the walls of the spaces or passages for the circulation of gaseous mixtures and/or effluents, the said heating means and the said sheaths being adapted to heat the said passages

Abstract: A process for the thermal pyrolysis of hydrocarbons in a reactor (1) of elongate shape comprising at a first end supply means (5) for a gaseous mixture containing at least one hydrocarbon, at the opposite end discharge means (10) for the effluents produced and between these two ends supply means (9) for effluent cooling fluid, the reactor comprising in a first part (first end side) a plurality of electric heating means (3) enclosed by casings (4) disposed in substantially mutually parallel layers perpendicular to the axis of the reactor, in such a way as to define between the casings and/or the casings and the walls (22), spaces or passages for circulation of the gaseous mixtures and/or effluents. The heating means heat the passages in successive, individual, transverse sections which are substantially perpendicular to the axis of the reactor. The reactor comprises means for introducing into the casings (4) a gas G known as a casing gas which preferably contains water vapour and/or hydrogen.

Abstract: Process for the catalytic conversion of a charge incorporating at least one oxygen compound such as methanol, into olefinic hydrocarbons having 2 to 4 carbon atoms. Conversion takes place in a reactor (100), into which the charge is introduced by the pipe (20), the catalytic solid by the pipe (30) and the solid entrainment gas by the pipe (40), the reactor being connected by a pipe (1) to a co-current cyclone separator (S) making it possible to separate a solid phase from a gaseous phase containing the conversion products, which is recovered by the pipe (4). The solid phase is fed by the pipe (9) to a regenerator (R), in which the catalytic particles are at least partly regenerated before being returned by the pipe (80), connected to the pipe (30), to the reactor (100).

Abstract: The conversion of a charge comprising at least one oxygen compound is performed in a reactor C, into which the charge is introduced by the pipe (11), the solid catalytic particles forming the dense phase D1 by the pipe (14) and the solid entrainment gas by the pipe (12). The reactor is connected by a pipe (1) to a cocurrent cyclone separator-mixer (MS) making it possible to separate a solid phase from a gaseous phase containing the conversion products recovered by the pipe (4'), while carrying out a quenching of said gaseous phase by a product M2 introduced by the pipe (3). The phase D1 is fed by the pipe (7) to a regenerator R before being returned by the pipe (13) into the reactor C. The mixture of the gaseous phase and the product M2 is separated in a separator and the product M2, optionally after cooling, is recycled to the mixer-separator (MS).

Abstract: The invention relates to a process and an apparatus for the production of aromatic hydrocarbons from an aliphatic hydrocarbon charge with 2 to 12 carbon atoms.The process comprises a stage of contacting a charge of at least one aliphatic hydrocarbon with 2 to 12 carbon atoms and a zeolitic catalyst composition optionally containing at least one metal, in a reaction zone (40) containing reaction tubes (3), said reaction zone being heated by at least partial immersion in an enclosure (1) containing a fluidized particle bed (13), characterized in that said particle bed is at least partly heated by a heat supply (19,23) resulting from the injection of hot gases produced in a zone outside said enclosure and introduced into the fluidized bed under conditions such that the reaction temperature is 400.degree. to 600.degree. C.Application to the production of benzene, toluene and xylenes.

Abstract: An apparatus and system for the dehydrogenation of ethane to produce ethylene and hydrogen through the use of a catalytic ceramic membrane having selective permeability, thus permitting separation of hydrogen from the reaction zone which causes further dehydrogenation of ethane, the catalytic ceramic membrane being in a cylindrical form which has been treated to have a metallic catalyst of suitable metal, such as platinum, palladium or chromium, deposited on the surface adjacent to the reaction zone. The catalytic ceramic membrane tube is enclosed within an alloy tube of suitable composition to permit heating to the temperature range of 300.degree. to 650.degree. C. The annulus surrounding the ceramic membrane tube may be filled with a pelleted catalyst, thus causing the dehydrogenation reaction to take place within this annular zone, but which will be accelerated by the permeation of hydrogen out of the zone through the ceramic catalytic membrane.

Abstract: The invention provides a substantially fail-safe HF alkylation process and reactor apparatus. The elongated reactor vessel is enclosed in a subterranean well casing and an alkylate-containing hydrocarbon layer is maintained above the hydrofluoric acid to prevent release of gaseous HF in the event of sudden depressurization. In a preferred embodiment, the hydrocarbon layer contains light hydrocarbons which vaporize upon depressurization to effect Joule-Thompson cooling of the reactor vessel.

Abstract: The invention provides a substantially fail-safe HF alkylation process and reactor apparatus. The elongated reactor vessel is enclosed in a well casing and an alkylate-containing hydrocarbon layer is maintained above the hydrofluoric acid to prevent release of gaseous HF in the event of sudden depressurization. In a preferred embodiment, the hydrocarbon layer contains light hydrocarbons which vaporize upon depressurization to effect Joule-Thompson cooling of the reactor vessel. A method for storing hazardous liquids and a penetration-resistant storage tank are also disclosed.

Abstract: Apparatus for controlling pressure in a combination hydrodesulfurization and reforming process wherein the pressure of a hydrogen-rich gas source from the reforming process is adjusted by coordinately manipulating a vent control valve for the hydrodesulfurization process and a vent control valve for the reforming process in a manner that insures maximum utilization of available hydrogen for desulfurization before any of the hydrogen from the reforming process is vented through its own vent valve.

Abstract: A process and apparatus are disclosed for acid continuous alkylation of a hydrocarbon-containing feedstream in which the inventory of acid is reduced. The apparatus used combines a reactor, settler and heat exchanger in a single vessel. The acid phase flows out of the reactor only for acid makeup, to account for acid consumption, and regeneration.

Abstract: An improved olefin upgrading technique and fixed-bed reactor system has been developed for increasing production of premium heavy hydrocarbons, such as distillate fuel, from lower olefinic feedstock. During recovery and recycle of intermediate range hydrocarbons products, a technique has been found for withdrawing a fraction rich in C.sub.5 -C.sub.9 gasoline range olefinic hydrocarbons from the oligomerization reactor effluent stream. By separating the reaction effluent in a multi-stage distillation system, fractionation feed can be separated into a heavier bottoms stream rich in C.sub.10 + hydrocarbons and a light hydrocarbon overhead, while withdrawing a liquid stream as an overflash fractionation stream rich in intermediate hydrocarbons. The overflash stream is combined to form a portion of the recycle stream to the reactor, thereby providing a more efficient and lower cost recovery process.

Abstract: A catalytic process for gas phase oxidative coupling of aliphatic and alicyclic hydrocarbon compounds to produce higher molecular weight hydrocarbon compounds, the catalyst being a mixed basic metal oxide or sulfide catalyst. One preferred mixed basic metal oxide catalyst is boron/alkali metal promoted metal oxide.

Abstract: The invention provides a catalytic method for the dimerization or codimerization or oligomerization, in particular selective, of olefins, carried out under pressure, in a reaction zone 1 containing a solid catalyst bed in which is disposed a plurality of hollow internal spaces 6.3a defined by walls, each being divided into an upper semi-space 6.3, 1a and a lower semi-space 6.3, 2a which communicate together through a connecting zone 6.6a. An autogenous thermoregulation fluid flows, in the form of a sheet, in said hollow internal spaces 6.3a after passing through a central distributing zone 6.1a and distributing zones 6.2a and before passing into collecting zone 6.4a and into a central collecting zone 6.5a.

Abstract: A catalyst and a process for oxidative coupling of aliphatic and alicyclic hydrocarbon compounds with aliphatic and alicyclic substituted aromatic hydrocarbon compounds to form a longer substituent hydrocarbon on the aromatic ring. The catalyst is mixed basic metal oxide catalyst, one preferred catalyst is boron/alkali metal promoted metal oxide. Reaction of methane with toluene and oxygen according to this invention results in conversion to styrene.

Abstract: The invention provides a catalytic method for the dimerization or codimerization or oligomerization, particularly selectively, of olefins, carried out under pressure, in a reaction zone 1 containing a solid catalyst bed into which is disposed a plurality of hollow internal spaces 6.3 defined by walls and through which an autogenous thermoregulation fluid flows, in the form of a sheet, after passing through a central distributing zone 6.1 and distributing zones 6.2 and before passing through collecting zones 6.4 and into a central collecting zone 6.5.

Abstract: A catalyst and process for oxidative coupling of methane, the catalyst being a mixed basic metal oxide catalyst. One preferred catalyst is boron/alkali metal promoted metal oxide.

Abstract: A method for producing hydrocarbons having two carbon atoms, which comprises introducing methane gas into a reactor downwardly from the top, the reactor comprising a pair of reactor walls extending vertically and facing each other, one of the walls being maintained at a high temperature and the other being maintained at a low temperature, so that the methane gas is dimerized primarily through the dehydrogenation on the surface of the high temperature wall to form C.sub.2 hydrocarbons and hydrogen, and the C.sub.2 hydrocarbons are preferentially diffused and transferred to the low temperature wall side by thermal diffusion effects.

Abstract: An integrated reactor system for conversion of methanol to ether-containing high octane gasoline and distillate. Methanol is converted to olefins in the presence of zeolite MTO catalyst. C.sub.4 and C.sub.5 olefin fraction is converted to MTBE and TAME in the presence of excess methanol and acid etherification catalyst. Unreacted methanol and hydrocarbons are passed to an olefins to gasoline and distillate oligomerization unit in conjunction with C.sub.3, C.sub.6 and C.sub.7 olefins from the methanol to olefins unit whereby distillate and LPG products are produced. Gasoline products from the oligomerization unit are passed to the etherification unit whereby an ether-rich gasoline fraction is separated.

Abstract: A process is provided for the oxidative conversion of methane to higher hydrocarbons wherein a mixture of methane and gaseous oxidant is contacted at reaction conditions with a solid oxidative contact agent which is essentially free of reducible metal oxide, the oxidative conversion taking place in the presence of a chalcogen promoter.

Abstract: Apparatus for converting crude aqueous oxygenate feedstock, such methanol or the like, to liquid hydrocarbons in contact with a medium pore shape selective crystalline acid zeolite catalyst, such as HZSM-5. In a preferred embodiment, the novel technique comprises means for: (a) contacting a crude methanol feedstock containing a minor amount of water with a liquid hydrocarbon extraction stream under extraction conditions favorable to selective extraction of the methanol, thereby providing an extract liquid stream rich in methanol and an aqueous raffinate stream lean in methanol; (b) charging the extracted methanol substantially free of water to said reaction zone under process conditions to convert substantially all methanol to hydrocarbons; (c) cooling reaction effluent to recover aqueous liquid byproduct stream, gas rich in C.sub.2.sup.- hydrocarbons, liquid rich in C.sub.3 -C.sub.4 hydrocarbons and C.sub.5.sup.

Abstract: A method for isomerizing isobutene or n-butene to produce a mixture of isobutene and normal butene, and polymerizing at least a portion thereof to produce isobutene/n-butene codimer, which comprieses feeding at least 80 weight % of either the isobutene or n-butene to a catalytic distillation reactor containing a fixed bed acidic cation exchange resin catalyst packing which provides both the catalyst sites and distillation sites for the reaction products, isomerizing a portion of the isobutene or n-butene to produce a mixture of isobutene and n-butene and reacting at least a portion of the isobutene and n-butene to form codimer of isobutene and n-butene, whereby an overhead fraction containing any unreacted isobutene and n-butene and a bottoms fraction containing codimer is produced. The result of the reaction is substantially the same regardless whether the feed is isobutene or n-butene. Other aspects of the invention, include combinations of procedures to produce high purity isobutene and n-butene.

Abstract: The isobutene in C.sub.4 hydrocarbon streams containing from 0.5 to 5% isobutene and n-butenes is reduced preferably to a level of 0.2 mole % or less by passing the feed stream at LHSV 2.5 to 12 in liquid phase through a fixed-bed cation exchange resin catalyst in a tubular reactor with a water heat exchange medium maintained at a temperature of 50.degree. to 80.degree. C., whereby the isobutene is oligomerized and easily separated from the remaining C.sub.4 's by fractionation.

Abstract: A method for the separation of isobutene from a mixture comprising n-butene and isobutene comprising feeding a C.sub.4 stream containing n-butene and isobutene to a distillation column reactor into a feed zone contacting the stream with fixed bed acidic cation exchange resin to form diisobutene which passes to the bottom of the column, said n-butene being removed overhead. The reaction and distillation occur concurrently.