A post fractionation process for removing heavy hydrocarbons from the C4+ olefins conversion process reactor effluent, which act as foulants when recycled to the C4+ olefins conversion reactor. This simple and effective process improves the run length of the reactor by reducing catalyst fouling, which also improves yields in a C4+ olefins conversion process to light olefins. Essential to present invention is the efficient recycling of a hydrocarbon stream to the reactor, utilizing well proven equipment in a novel way to separate more valuable product from less desirable components in the recycle product stream..
The present invention provides an improved process for the catalytic conversion of a feedstock comprising an alkylatable aromatic compound and an alkylating agent to form a conversion product comprising the desired alkylaromatic compound by contacting said feedstock in at least partial liquid phase under catalytic conversion conditions with a catalyst composition comprising a porous crystalline material having a structure type of FAU, BEA* or MWW, or a mixture thereof, wherein the porous crystalline material has a Relative Activity measured at 220°C as an RA220 of at least 7.5 or measured at 180°C as RA180 of at least 2.5, allowing operation at lower reaction pressures, e.g., a reaction pressure of about 450 psig (3102 kPa) or less, and lower alkylating agent feed supply pressure of 450 psig (3102 kPa) or less.
The present invention is directed to a method for producing, inter alia, olefins from refinery saturated and unsaturated off-gas. Furthermore, said refinery streams are not required to undergo deoxygenation reaction in a separate reactor system provided they are fed to the pyrolysis furnace. The refinery off-gases are treated to produce olefins such as ethylene and propylene. Gases from petrochemical facilities, gas separation plants and similar facilities that produce light gases containing ethane and propane are useful in the present method.
C07C 5/32 - Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with formation of free hydrogen
4.
Bathtub-type spent catalyst distributor for effective counter-current regeneration in fluid catalytic cracking units
An improved spent catalyst regenerator which contains sub-troughs branching off from the main trough, distribution troughs which extend outward from the sides of the main trough and the sub-troughs, and downflow tubes extending downward from the bottom of the main trough and sub-troughs.
A system and method are disclosed that allow a user to combine raw light hydrocarbons (e.g., C4 hydrocarbons) and raw heavy hydrocarbons (e.g., gasolines and/or C5+ hydrocarbons) streams together prior to hydrogenation. The system and method allow light and heavy hydrocarbons to be hydrogenated simultaneously within a single reactor. An system and method are also disclosed which provides specific conditions for minimizing light hydrocarbon losses during hydrocarbon processing. In particular, the disclosed method provides pressure conditions in post reactor stabilizers that facilitate venting of un-reacted hydrogen and the condensation of light hydrocarbons. Under the disclosed conditions, light hydrocarbon losses are minimized during the method and the condensed light hydrocarbons can be either recycled back into the system or utilized as a fungible energy source.
An apparatus designed to completely vaporize an intake of heavy hydrocarbon feedstock is described. The apparatus, a so-called heavy feed mixer, is comprised of pipes being disposed coaxially about a common longitudinal axis. The inner tubular section delivers a two-phase liquid-vapor mixture of hydrocarbon feedstock and dilution steam to the apparatus. The converging/diverging tubular section has a unique structure which converges to a throat section and then diverges to an outlet section. The converging section directs a uniform shroud of superheated steam onto the hydrocarbon stream delivered by the inner tubular section. Impingement of the superheated steam with the intake stream initiates mixing and further vaporization within the throat section. The mixture traverses the converging/diverging tubular section and passes into the outlet section where vaporization is complete. The completely vaporized stream is directed out of the apparatus for further processing downstream.
C10G 9/14 - Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils in pipes or coils with or without auxiliary means, e.g. digesters, soaking drums, expansion means
C10G 9/36 - Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts with heated gases or vapours
7.
Method for contaminants removal in the olefin production process
The present invention provides a method and reactor system for hydrogenating acetylenes present in the olefin stream derived from the following streams, alone or in combination: petroleum catalytic cracking process and/or oxygenate-to-olefin reactor, such as methanol-to-olefin (MTO) reactor, in an olefin production plant before the distillation steps, wherein the acetylene hydrogenation occurs before or just after the acid gas removal step.
C07C 7/167 - Purification, separation or stabilisation of hydrocarbonsUse of additives by treatment giving rise to a chemical modification of at least one compound by hydrogenation for removal of compounds containing a triple carbon-to-carbon bond
C07C 7/163 - Purification, separation or stabilisation of hydrocarbonsUse of additives by treatment giving rise to a chemical modification of at least one compound by hydrogenation
An apparatus designed to completely vaporize an intake of heavy hydrocarbon feedstock is described. The apparatus, a so-called heavy feed mixer, is comprised of pipes being disposed coaxially about a common longitudinal axis. The inner tubular section delivers a two-phase liquid-vapor mixture of hydrocarbon feedstock and dilution steam to the apparatus. The converging/diverging tubular section has a unique structure which converges to a throat section and then diverges to an outlet section. The converging section directs a uniform shroud of superheated steam onto the hydrocarbon stream delivered by the inner tubular section. Impingement of the superheated steam with the intake stream initiates mixing and further vaporization within the throat section. The mixture traverses the converging/diverging tubular section and passes into the outlet section where vaporization is complete. The completely vaporized stream is directed out of the apparatus for further processing downstream.
The invention is directed to effective means for joining materials having dissimilar coefficients of thermal expansion, such as advanced ceramics with metallic compounds. Moreover, the present invention relates to furnace tubes and methods of fabricating a joint between two different materials, which is compositionally graded to provide a substantially graded coefficient of thermal expansion between the joint materials.
The present invention provides a compact riser separation system for Fluid Catalytic Cracking reactors possessing an external riser system wherein the riser enters the reactor from outside the reactor vessel.
B01J 8/24 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with fluidised particles according to "fluidised-bed" technique
C10G 47/30 - Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, to obtain lower boiling fractions with moving solid particles according to the "fluidised bed" technique
11.
SEPARATING AND STRIPPING APPARATUS FOR EXTERNAL FCC RISERS
The present invention provides a compact riser separation system for Fluid Catalytic Cracking reactors possessing an external riser system wherein the riser enters the reactor from outside the reactor vessel.
An improved spent catalyst regenerator which contains sub-troughs branching off from the main trough, distribution troughs which extend outward from the sides of the main trough and the sub-troughs, and downflow tubes extending downward from the bottom of the main trough and sub-troughs.
Improved methods and related apparatus are disclosed for efficiently recovering the heat of condensation from overhead vapor produced during separation of various components of dehydrogenation reaction effluent, particularly in ethylbenzene-to-styrene operations, by the use of at least a compressor to facilitate azeotropic vaporization of an ethylbenzene and water mixture within a preferred range of pressure/temperature conditions so as to minimize undesired polymerization reactions.
C07C 4/02 - Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms by cracking a single hydrocarbon or a mixture of individually defined hydrocarbons or a normally gaseous hydrocarbon fraction
C07C 5/00 - Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
C07C 2/64 - Addition to a carbon atom of a six-membered aromatic ring
A process is disclosed for producing an alkylaromatic compound in a multistage reaction system comprising at least first and second series-connected alkylation reaction zones, each containing an alkylation catalyst. A first feed comprising an alkylatable aromatic compound and a second feed comprising an alkene are introduced into the first alkylation reaction zone. The first and second alkylation reaction zones are operated under conditions of temperature and pressure effective to cause alkylation of the aromatic compound with the alkene in the presence of the alkylation catalyst, the temperature and pressure being such that the aromatic compound is at least partly in the liquid phase. The alkylation catalyst in the first alkylation reaction zone, which may be a reactor guard bed, has more acid sites per unit volume of catalyst than the alkylation catalyst in the second reaction zone.
An improved fluidized catalyst withdrawal well containing packing or other structured internals is disclosed for improving the flow of particular solids between two apparatus, such as between a catalyst regenerator and riser reactor.
2S down to low single digits parts per million concentration and the upper sections employing a stronger caustic solution on a once-through basis to produce a mercaptans depleted gas stream.
C07C 7/00 - Purification, separation or stabilisation of hydrocarbonsUse of additives
B01D 53/14 - Separation of gases or vapoursRecovering vapours of volatile solvents from gasesChemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases or aerosols by absorption
17.
Process of using a high activity catalyst for the transalkylation of aromatics
A process for producing an alkylated aromatic compound from polyalkylated aromatic compound(s) having bi-alkylated aromatic compound(s) and tri-alkylated aromatic compound(s), comprising the step of contacting alkylatable aromatic compound(s) with the polyalkylated aromatic compound(s) at a transalkylation condition in the presence of a transalkylation catalyst. The transalkylation catalyst has high activity sufficient to achieve a ratio of bi-alkylated aromatic compound(s) conversion over tri-alkylated aromatic compound(s) conversion in a range of from about 0.5 to about 2.5.
C07C 6/12 - Preparation of hydrocarbons from hydrocarbons containing a different number of carbon atoms by redistribution reactions by conversion at a saturated carbon-to-carbon bond of exclusively hydrocarbons containing a six-membered aromatic ring
A process for producing an alkylated aromatic product in a reactor by reacting an alkylatable aromatic compound feedstock with another feedstock comprising alkene component and alkane component in a reaction zone containing an alkylation catalyst. The reaction zone is operated in predominantly liquid phase without inter-zone alkane removal. The polyalkylated aromatic compounds can be separated as feed stream for transalkylation reaction in a transalkylation reaction zone.
An improved spent catalyst regenerator which contains sub-troughs branching off from the main trough, distribution troughs which extend outward from the sides of the main trough and the sub-troughs, and downflow tubes extending downward from the bottom of the main trough and sub-troughs.
A process is disclosed for producing an alkylaromatic compound in a multistage reaction system comprising at least first and second series-connected alkylation reaction zones, each containing an alkylation catalyst. A first feed comprising an alkylatable aromatic compound and a second feed comprising an alkene are introduced into the first alkylation reaction zone. The first and second alkylation reaction zones are operated under conditions of temperature and pressure effective to cause alkylation of the aromatic compound with the alkene in the presence of the alkylation catalyst, the temperature and pressure being such that the aromatic compound is at least partly in the liquid phase. The alkylation catalyst in the first alkylation reaction zone, which may be a reactor guard bed, has more acid sites per unit volume of catalyst than the alkylation catalyst in the second reaction zone.
A process is disclosed for producing an alkylaromatic compound in a multistage reaction system comprising at least first and second series-connected alkylation reaction zones, each containing an alkylation catalyst. A first feed comprising an alkylatable aromatic compound and a second feed comprising an alkene are introduced into the first alkylation reaction zone. The first and second alkylation reaction zones are operated under conditions of temperature and pressure effective to cause alkylation of the aromatic compound with the alkene in the presence of the alkylation catalyst, the temperature and pressure being such that the aromatic compound is at least partly in the liquid phase. The alkylation catalyst in the first alkylation reaction zone, which may be a reactor guard bed, has more acid sites per unit volume of catalyst than the alkylation catalyst in the second reaction zone.
A mass and/or heat transfer column is provided with a multiphase vapor distributor with distributes a vapor stream about the inner periphery of the column.
B01J 10/00 - Chemical processes in general for reacting liquid with gaseous media other than in the presence of solid particlesApparatus specially adapted therefor
A nozzle for the atomized spray of liquid hydrocarbon feed in a fluidized catalytic cracking apparatus having two or more slots with at least one lateral slot wall formed at an angle of from about 30 to about 60 degrees from the axis of the discharge. Also a method of spraying atomized hydrocarbon feed/steam into a fluidized catalytic cracking reactor using the nozzle described.
B05B 17/04 - Apparatus for spraying or atomising liquids or other fluent materials, not covered by any other group of this subclass operating with special methods
B05B 1/14 - Nozzles, spray heads or other outlets, with or without auxiliary devices such as valves, heating means with multiple outlet openingsNozzles, spray heads or other outlets, with or without auxiliary devices such as valves, heating means with strainers in or outside the outlet opening
B05B 1/00 - Nozzles, spray heads or other outlets, with or without auxiliary devices such as valves, heating means
B05B 1/26 - Nozzles, spray heads or other outlets, with or without auxiliary devices such as valves, heating means with means for mechanically breaking-up or deflecting the jet after discharge, e.g. with fixed deflectorsBreaking-up the discharged liquid or other fluent material by impinging jets
A62C 31/02 - Nozzles specially adapted for fire-extinguishing
A nozzle for the atomized spray of liquid hydrocarbon feed in a fluidized catalytic cracking apparatus having two or more slots with at least one lateral slot wall formed at an angle of from about 30 to about 60 degrees from the axis of the discharge. Also a method of spraying atomized hydrocarbon feed/steam into a fluidized catalytic cracking reactor using the nozzle described.
B05B 1/14 - Nozzles, spray heads or other outlets, with or without auxiliary devices such as valves, heating means with multiple outlet openingsNozzles, spray heads or other outlets, with or without auxiliary devices such as valves, heating means with strainers in or outside the outlet opening
B01J 8/24 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with fluidised particles according to "fluidised-bed" technique
C10G 11/00 - Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
The present invention is describes a novel technique for producing commercial hydrocarbon materials using a fluid catalytic cracking unit employing recycling of light cycle oil in combination with desulfurization catalysts.
C10G 69/04 - Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one step of catalytic cracking in the absence of hydrogen
C10G 11/18 - Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised bed" technique
C10G 17/095 - Refining of hydrocarbon oils, in the absence of hydrogen, with acids, acid-forming compounds, or acid-containing liquids, e.g. acid sludge with "solid acids", e.g. phosphoric acid deposited on a carrier
Methods and apparatus are disclosed for mixing fluid streams of different compositions to minimize fluid condensation inside a mixing vessel where the objective is to produce an all-vapor mixture product.
B01J 3/00 - Processes of utilising sub-atmospheric or super-atmospheric pressure to effect chemical or physical change of matterApparatus therefor
F02M 15/02 - Carburettors with heating, cooling or thermal insulating means for combustion-air, fuel or fuel-air mixture with heating means, e.g. to combat ice-formation
Improved methods and related apparatus are disclosed for efficiently recovering the heat of condensation from overhead vapor produced during separation of various components of dehydrogenation reaction effluent, particularly in ethylbenzene-to-styrene operations, by the use of at least a compressor to facilitate azeotropic vaporization of an ethylbenzene and water mixture within a preferred range of pressure/temperature conditions so as to minimize undesired polymerization reactions.
Improved integrated processes for the production of alkyl aromatic compounds are disclosed wherein aromatic compounds which may be treated for removal of deleterious substances are reacted with olefin compounds, which may also be treated for contaminant removal, in the presence of acidic zeolite catalyst(s) to produce the desired alkyl aromatic compound(s). The aromatic and preferably also the olefin feeds are treated substantially to remove contaminants, particularly the nitrogen compounds contained therein, before they are brought together for reaction in the presence of the zeolite catalyst(s). In accordance with the present invention, it has been found that feed pretreatment for removal of nitrogen compounds significantly improves the run length and life of the acidic zeolite catalyst(s). The feed pretreatment of this invention may include the steps of distillation, extraction, and/or adsorption by solid adsorbent, which may be regenerated in accordance with further embodiments of this invention.
Improved processes are provided for the production of alkyl aromatic compounds using zeolite catalyst(s) and for periodic reactivation in situ of zeolite catalyst(s) that have at least in part become deactivated. Processes according to this invention are typically carried out in a reaction section loaded with catalyst(s) wherein a desired alkyl aromatic compound is produced from feed aromatic and olefin compounds followed by a separation section in which the desired product is isolated and recovered. Alkylation, transalkylation, and/or isomerization reactions that occur in the reaction section are carried out in liquid phase or partial liquid phase over the said zeolite catalyst(s). At least a portion of the zeolite catalyst(s) employed in the reaction section is (are) reactivated in situ, periodically or when deemed necessary, by contacting the deactivated catalyst(s), at elevated temperature and in the substantial absence of olefin feedstock, with an aromatic stripping stream comprising the feed aromatic compound, the desired alkyl aromatic product, byproducts formed in the process, or mixtures thereof, to restore its (their) activity.
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