Abstract: Processes using mid-column reboilers in at least one benzene separation columns to reduce the heat duty in alkylation processes are provided. The feed to the aromatics removal zone may exchange heat in a mid-column reboiler in the benzene separation column in the alkylbenzene separation zone followed by exchanging heat in a mid-column reboiler in the benzene separation column in the aromatics removal zone. This arrangement minimizes the hot oil duty on the reboilers in both benzene separation columns.

Abstract: To economically regenerate a catalyst and to produce aromatic hydrocarbon stably for a long time maintaining a high aromatic hydrocarbon yield when the aromatic hydrocarbon is produced upon making a contact reaction between lower hydrocarbon and the catalyst. A method of producing aromatic hydrocarbon and an apparatus for producing aromatic hydrocarbon by repeating a reaction step for obtaining aromatic hydrocarbon upon making a contact reaction between lower hydrocarbon and a catalyst and a regeneration step for regenerating the catalyst used in the reaction step. Off-gas which is gas obtained by removing aromatic hydrocarbon produced in the reaction step from discharge gas passing through the reaction step is used as a regeneration gas in the regeneration step.

Abstract: The present invention is a process for purifying a liquid stream having an aqueous phase with polyaromatics, and optionally an organic phase. The process can include sending the liquid stream to a mixing tank and introducing an aromatic component to produce a mixture of an organic phase and of an aqueous phase. The mixture can be sent to a decanter to recover a clean aqueous phase and an organic phase. The clean aqueous phase can go through a stripper to remove a substantial part of any remaining organic component. The liquid stream can be the whole or a fraction of an aqueous phase recovered by condensation of an effluent gas leaving an ethylbenzene dehydrogenation reactor.

Abstract: A process for increasing the yield of ethylene and propylene, comprising: (1) feeding a feedstock into a reaction zone with a catalyst to produce (i) a product stream and a catalyst to be regenerated; (2) stripping and then dividing the catalyst to be regenerated into at least two parts, wherein a first part is recycled into the reaction zone at a first position, and a second part is regenerated in the regenerator to form a regenerated catalyst and then recycled into the reaction zone at a second position; and (3) controlling the temperature increase in the reaction zone.

Abstract: An aromatics complex producing one or more xylene isomers offers a large number of opportunities to conserve energy by heat exchange within the complex. One previously unrecognized opportunity is through providing two parallel distillation columns operating at different pressures to separate C8 aromatics from C9+ aromatics. The parallel columns offer additional opportunities to conserve energy within the complex.

Abstract: To improve stability of catalytic performance, an aromatizing catalyst for converting lower hydrocarbons into aromatic compounds is regenerated. A regeneration process of the aromatizing catalyst according to the present invention includes the steps of: (a) reacting the aromatizing catalyst with a hydrogen gas in an atmosphere containing the hydrogen gas after using the aromatizing catalyst in an aromatizing reaction for converting lower hydrocarbons into aromatic compounds; (b) decreasing a temperature of the atmosphere containing the hydrogen gas reacted with the aromatizing catalyst, by supplying one of an inert gas and a reducing gas to the atmosphere; (c) reacting the aromatizing catalyst reacted with this inert gas, with an oxidizing gas; and (d) reacting the aromatizing catalyst reacted with the oxidizing gas, with a reducing gas.

Abstract: The invention relates to a process for cracking a hydrocarbon-containing feed in a cracking furnace. A plurality of heat exchangers are arranged in the convection zone of the cracking furnace to utilize the heat of flue gas formed in the radiation zone by combustion. Depending on the type and state of matter of the hydrocarbon-containing feed, flow occurs through the heat exchangers to achieve, independently of the type and state of matter of the hydrocarbon-containing feed, an exit temperature of the flue gas in the range from 80° C. to 150° C.

Abstract: In one aspect, the inventive process comprises a process for pyrolyzing a hydrocarbon feedstock containing nonvolatiles in a regenerative pyrolysis reactor system. The inventive process comprises: (a) heating the nonvolatile-containing hydrocarbon feedstock upstream of a regenerative pyrolysis reactor system to a temperature sufficient to form a vapor phase that is essentially free of nonvolatiles and a liquid phase containing the nonvolatiles; (b) separating said vapor phase from said liquid phase; (c) feeding the separated vapor phase to the pyrolysis reactor system; and (d) converting the separated vapor phase in said pyrolysis reactor system to form a pyrolysis product.

Abstract: The present invention provides a process for the manufacture of acetylene and other higher hydrocarbons from methane feed using a reverse-flow reactor system, wherein the reactor system includes (i) a first reactor and (ii) a second reactor, the first and second reactors oriented in a series relationship with respect to each other, the process comprising supplying each of first and second reactant through separate channels in the first reactor bed of a reverse-flow reactor such that both of the first and second reactants serve to quench the first reactor bed, without the first and second reactants substantially reacting with each other until reaching the core of the reactor system.

Abstract: A process for alkylation of benzene, including: feeding benzene, a polyalkylate, and a catalyst to a reactor comprising a first and a second reaction zone; reacting the benzene and the polyalkylate in the first reaction zone under transalkylation conditions to form a monoalkylate product; feeding a C2-C4 olefin to the reactor intermediate the first and second reaction zones; reacting benzene and the C2-C4 olefin in the second reaction zone under alkylation conditions to form additional monoalkylate product; recovering an effluent from the reactor, wherein the effluent comprises benzene, the monoalkylate product, any unreacted C2-C4 olefins, heavy hydrocarbons, and the catalyst; separating the catalyst from the effluent; separating the benzene from the monoalkylate product and the heavy hydrocarbons within the liquid effluent; separating the monoalkylate product from the heavy hydrocarbons within the liquid effluent; and recovering the monoalkylate product.

Abstract: Nanoparticulates of oxygen transfer materials that are oxides of rare earth metals, combinations of rare earth metals, and combinations of transition metals and rare earth metals are used as catalysts in a variety of processes. Unexpectedly large thermal efficiencies are achieved relative to micron sized particulates. Processes that use these catalysts are exemplified in a multistage reactor. The exemplified reactor cracks C6 to C20 hydrocarbons, desulfurizes the hydrocarbon stream and reforms the hydrocarbons in the stream to produce hydrogen. In a first reactor stage the steam and hydrocarbon are passed through particulate mixed rare earth metal oxide to crack larger hydrocarbon molecules. In a second stage, the steam and hydrocarbon are passed through particulate material that desulfurizes the hydrocarbon. In a third stage, the hydrocarbon and steam are passed through a heated, mixed transition metal/rare earth metal oxide to reform the lower hydrocarbons and thereby produce hydrogen.

Abstract: In a process for converting methane to aromatic hydrocarbons, a feed containing methane and a particulate catalytic material are supplied to a reaction zone operating under reaction conditions effective to convert at least a portion of the methane to aromatic hydrocarbons and to deposit carbonaceous material on the particulate catalytic material causing catalyst deactivation. At least a portion of the deactivated particulate catalytic material is removed from the reaction zone and is heated to a temperature of about 700° C. to about 1200° C. by direct and/or indirect contact with combustion gases produced by combustion of a supplemental fuel. The heated particulate catalytic material is then regenerated with a hydrogen-containing gas under conditions effective to convert at least a portion of the carbonaceous material thereon to methane and the regenerated catalytic particulate material is recycled back to the reaction zone.

Abstract: A process for the alkylation of aromatic hydrocarbons such as cumene and ethylbenzene is disclosed. A portion of the effluent stream from an alkylation reactor passes through an indirect heat exchanger to transfer heat to a flashed stream containing the product aromatic hydrocarbons. The heat exchanger recovers the exothermic heat of reaction from the effluent stream for use elsewhere in the process. This method of heat exchange is especially useful in alkylation processes where the temperature of the effluent stream is relatively low, such as where the alkylation reactor contains a zeolite catalyst.

Abstract: The present invention provides a method and apparatus for reforming a hydrocarbon feedstock in the presence of steam using a steam-active reforming catalyst The present invention can generally be used in conjunction with any steam-active reforming processes wherein the hydrocarbon reforming and catalyst regeneration operations are conducted simultaneously and the catalyst is regenerated using a steam-diluted oxygen (or air) regeneration medium. In the present invention, catalyst regeneration effluent gas is advantageously reused in the reforming operation to provide at least a portion of the steam environment required for reforming the hydrocarbon feedstock. Free oxygen is preferably removed from the regeneration effluent gas before the regeneration effluent gas is brought into contact with the hydrocarbon feedstock.

Abstract: In its simplest sense, the present invention is directed toward a process for the thermal conversion of methane into unsaturated gaseous hydrocarbons, especially olefins, comprising first compressing methane in the presence of an inert gas having a higher ratio of heat capacities, Cp/Cv, than methane. The inert gas used is present in an amount sufficient to provide a compressed gas mixture having a peak temperature of adiabatic compression in the range of about 900.degree. C. to about 2200.degree. C. Under these conditions, at least some of the methane is converted to unsaturated gaseous hydrocarbons. Immediately thereafter, the compressed gas mixture is expanded, thereby substantially preventing thermal conversion of the gaseous hydrocarbons. Importantly, the compression and expansion are achieved in a single cycle of less than about one second.

Abstract: A process and apparatus are disclosed for the catalytic conversion of hydrocarbons in a transport or sub-transport fluidized bed reaction zone. Inert particles are used to transfer heat to the reaction zone. The particles may be heated separately from the catalyst in a combustion zone or together with the catalyst in a regenerator. Fuel is fired to heat the inert particles or a mixture of catalyst and inert particles. Hydrogen deficient fuels such as charcoal or coke are preferred.

Abstract: An improved fluid-bed reaction process and apparatus are disclosed in which feedstock is preheated and may be at least partially converted by contacting the feedstock with spent catalyst in a preheat zone. Additional benefits include a reduction in catalyst poisons and coke production in the reaction zone. By contacting the fresh feed with hot spent catalyst, at least a portion of the coke which would otherwise form in the reactor is deposited on the spent catalyst. Temporary catalyst poisons are also sorbed onto the spent catalyst. The spent catalyst is then withdrawn from the preheat zone, stripped of entrained hydrocarbon and regenerated.

Abstract: A multitubular catalytic reactor for exothermal catalytic reactions comprises a bundle of parallel tubes all of the same length and a catalyst within the tubes. The tube bundle has an inlet side and an outlet side. Devices are provided for introducing separately reactants to within the tubes of the reactor and coolant to the channels defined between adjacent tubes of the bundle. The coolant is introduced into the channels co-currently with the direction of flow of the reactants. The products are withdrawn from the tubes independently of the coolant. The reactor is particularly adapted to a single stage conversion of methanol into gasoline boiling point range constituents using crystalline aluminosilicate catalysts.

Abstract: Lower alkanes are converted to olefins in a `third bed` external catalyst cooler (ECC) in which hot catalyst, from a first regenerator (`second bed`) operating in conjunction with a fluid catalytic cracker (`first bed`), thermally cracks and dehydrogenates the alkanes. Because this is an endothermic reaction, the catalyst is autogeneously cooled before it is recirculated to the FCC regenerator. The cracking catalyst is the catalyst of choice in the FCC reactor. Maximum conversion of alkanes to olefins is sought, and can be maintained because the FCC regenerator burns the coke made during alkane dehydrogenation. The olefins produced are then oligomerized in an oligomerization reactor ("fourth" bed) operating in conjunction with a second regenerator ("fifth" bed) to produce a gasoline range stream.

Abstract: A heat balanced system for converting an olefinic feedstock comprising ethylene and C.sub.3.sup.+ olefins to heavier liquid hydrocarbon product in a catalytic exothermic process. Means are provided for prefractionating the olefinic feedstock to obtain a gaseous stream rich in ethylene and a liquid stream containing C.sub.3.sup.+ olefin, and a reactor for contacting an olefinic feedstock stream from the prefractionating step with ZSM-5 type oligomerization catalyst in a series of exothermic catalytic reactors to provide a heavier hydrocarbon effluent stream comprising distillate, gasoline and lighter hydrocarbons. In a preferred embodiment a catalytic system is provided for making gasoline or diesel fuel from an olefinic feedstock containing ethylene and C.sub.3.sup.+ lower olefins comprising a prefractionation system for separating and recovering ethylene and a liquid stream rich in C.sub.3.sup.

Abstract: A methanol-to-gasoline (MTG) catalytic conversion system in which the conversion is conducted in a fixed bed catalytic reactor. A C.sub.3 -C.sub.4 hydrocarbon diluent is generated from pressurized liquid effluent and recycled to the fixed bed reactor in order to dissipate the heat of reaction.

Abstract: A methanol-to-gasoline (MTG type) conversion process in which the conversion is conducted in a fixed bed catalytic reactor. A C.sub.3 -C.sub.4 hydrocarbon diluent is generated from the effluent in a series of steps and recycled to the fixed bed reactor in order to dissipate the heat of reaction.

Abstract: An improved process for the production of styrene through dehydrogenation of ethylbenzene in the presence of steam at elevated temperatures, comprising (1) recovering heat of condensation normally lost during separation of the various components of the dehydrogenation reaction effluent, especially of ethylbenzene from styrene, without need or use of a compressor and (2) using such heat to vaporize an aqueous feed mixture of ethylbenzene and dilution water that is introduced into the dehydrogenation reactor, preferably at about atmospheric pressure, thereby obviating the need to use steam to vaporize the liquid ethylbenzene feed and also enabling much of the diluent steam needed as sensible heat for the dehydrogenation reaction to be generated from water.

Abstract: In the conversion of light olefins to heavier hydrocarbons, an improved recovery technique is provided for selectively removing unreacted light olefins from a catalytic reactor effluent. This system is useful in converting ethene-rich feedstocks to gasoline and/or distillate products, particularly in oligomerization processes employing shape selective siliceous catalysts such as ZSM-5 type zeolites. By recycling gasoline-range hydrocarbons as a sorbent liquid, unreacted C.sub.2.sup.+ components may be absorbed from reactor effluent vapor and returned for further contact with the catalyst.

Abstract: A hydrocarbon conversion process is disclosed for the dehydrogenation of alkylaromatic hydrocarbons such as ethylbenzene or ethyltoluene. A subatmospheric pressure is maintained in the reaction zone by the use of two separate compressors. The first compressor pressurizes the vapor phase reactor effluent prior to the final indirect heat exchange step(s) used to partially condense this stream. The second compressor maintains the vapor-liquid separator which receives the partially condensed reactor effluent stream at a subatmospheric pressure. This facilitates operation of the reactor at a subatmospheric pressure.

Abstract: A method and apparatus are provided in a chemical heat pipe for shifting the reaction equilibrium in order to operate at a "shifted" temperature without also "shifting" the pressure. A diluent is added to the heat pipe in a constant-pressure manner near a reaction zone. The diluent exists in the gaseous phase at the reaction zone so as to shift the reaction equilibrium. This has the effect of "shifting" the temperature required for the reaction to proceed to a predetermined extent. The diluent is chemically inert in the particular reacting system and is removed from the system so as not to increase the pressure therein. In a preferred embodiment, methylcyclohexane is dissociated by endothermic reaction at a heat source position to form toluene and hydrogen and water is added to the heat pipe at or near the heat source position to form a diluent of water vapor at the reaction zone. The diluent is removed from the system downstream of the reaction zone, as by a desiccant.

Abstract: A heat balanced technique for converting an olefinic feedstock comprising ethylene and C.sub.3.sup.+ olefins to heavier liquid hydrocarbon product in a catalytic exothermic process. Methods and means are provided for prefractionating the olefinic feedstock to obtain a gaseous stream rich in ethylene and a liquid stream containing C.sub.3.sup.+ olefin, and contacting an olefinic feedstock stream from the prefractionating step with ZSM-5 type oligomerization catalyst in a series of exothermic catalytic reactors to provide a heavier hydrocarbon effluent stream comprising distillate, gasoline and lighter hydrocarbons. In a preferred embodiment a catalytic system is provided for making gasoline or diesel fuel from an olefinic feestock containing ethylene and C.sub.3.sup.+ lower olefins comprising a prefractionation system for separating and recovering ethylene and a liquid stream rich in C.sub.3.sup.

Abstract: A process for the production of aromatic hydrocarbons from petroleum fractions containing paraffins which comprises passing said charge in the presence of hydrogen at 400.degree. C.-550.degree. C. over a catalyst containing from 0.1 to 1.5% by weight of at least one metal selected from the group consisting of platinum, rhenium, iridium, tin and germanium and containing sulfur in a sulfur/metals atomic ratio of from 0 to less than 1, supported on a crystalline, aluminum silicate zeolite containing alkaline cations, said zeolite having a pore dimension larger than 6.5 Angstroms, wherein the catalysts are in fixed beds in two reactors or sets of reactors arranged in parallel and operate at a pressure on the order of from 0.5 to 8 absolute bars wherein when a reactor set (DHC.sub.1 ) is producing aromatic hydrocarbons the other reactor set (DHC.sub.2 ) is swept by the hydrogen produced by the first reactor set (DHC.sub.

Abstract: A method of recovering heat energy from hydrocarbon pyrolysis effluent characterized by differentiated cooling systems, reduced coking, and high quality steam generation. Steam quality is improved by utilization of a minimum quenched effluent temperature of at least 370.degree. C.