Abstract: A co-extrusion die is configured to produce a multilayer extrusion comprising component layers of an electrochemical cell. The die comprises a plurality of inlet ports configured to receive a plurality of pressurized fluids comprising at least a first metallic ink, a second metallic ink, and a polymeric ink. A plurality of channels are configured to separately transport and shape the plurality of fluids from the plurality of inlet ports to a merge section, such that the plurality of fluids flow together in the merge section to form the multilayer extrusion comprising a polymeric membrane layer disposed between and in contact with a first metallic layer and a second metallic layer. A thickness of each layer within the merge section is controllable by adjustment of a pressure of the plurality of pressurized fluids. An outlet port is configured to output the multilayer extrusion onto a substrate.

Abstract: A mixture of gas and solid particles are conveyed through a piping circuit connected between initial and terminal points. The gas is introduced at the initial point and the particles are introduced between the initial and terminal points. A diameter of the piping circuit increases downstream of where the particles are introduced, and a velocity of the gas is at least as great as a pick-up velocity of the particles at the point where the particles are introduced into the piping circuit. In addition to the above constraints, the piping circuit is sized so that total pressure losses due to flow in the piping circuit between the initial and terminal points are within a designated amount.

Abstract: A method for starting a slurry bubble column reactor that includes a reactor vessel holding a settled or slumped bed of particles and a liquid phase from which the particles have settled includes introducing a flow of a re-suspension liquid into the settled or slumped bed to loosen the settled or slumped bed. The introduction of the re-suspension liquid takes place before the introduction of any gas into the settled or slumped bed, or together with feeding of gas into the settled or slumped bed, provided that, if gas is fed together with the re-suspension liquid into the settled or slumped bed before the settled or slumped bed has been loosened, the gas has a superficial gas velocity in the reactor below 10 cm/s. Once the settled or slumped bed has been loosened by at least the re-suspension liquid, gas is passed at a superficial gas velocity above 10 cm/s through the liquid phase.

Abstract: A process for mixing regenerated and carbonized catalyst involves obstructing upward flow of catalyst by one or more baffles between a catalyst inlet and a feed distributor. Each catalyst stream may be passed to opposite sides of a riser. Baffles obstruct upward flow to effect mixing of regenerated and carbonized catalyst to obtain a more uniform temperature and catalyst mixture before contacting the feed.

Abstract: Process for the preparation of C3 and C4 olefins and gasoline by: (a) contacting in a fluidised bed reactor a light hydrocarbon feedstock with a first catalyst inventory comprising a medium pore size zeolite catalyst, wherein the first catalyst inventory is a fresh catalyst inventory; (b) combining at least part of the catalyst inventory as used in step (a) with one or more catalyst streams to form a second catalyst inventory comprising a medium pore size zeolite catalyst and a large pore size zeolite catalyst; (c) contacting a hydrocarbon feedstock with the second catalyst inventory in a reactor riser to form cracked products.

Abstract: An apparatus for mixing regenerated and carbonized catalyst involves obstructing upward flow of catalyst by one or more baffles between a catalyst inlet and a feed distributor. Each catalyst stream may be passed to opposite sides of a riser. Baffles obstruct upward flow to effect mixing of regenerated and carbonized catalyst to obtain a more uniform temperature and catalyst mixture before contacting the feed.

Abstract: The present invention provides a thermodynamic cracking process wherein the cracking takes place in a cyclone reactor and in a riser of varying areas under the influence of a rotating and turbulent fluidised energy carrier which is put in motion in a fluidised regenerator by injection of combustion gases or air. A cracking unit is also described.

Abstract: A process for selectively producing C2 to C4 olefins from feedstock such as a gas oil or resid. The feedstock is reacted in a first stage comprising a fluid catalytic cracking unit wherein it is converted in the presence of a mixture of conventional large pore zeolitic catalyst and a medium pore zeolitic catalyst to reaction products, including a naphtha boiling range stream. The naphtha boiling range stream is introduced into a second stage where it is contacted with a catalyst containing from about 10 to about 50 wt. % of a crystalline zeolite having an average pore diameter less than about 0.7 nanometers at reaction conditions which include temperatures ranging from about 500 to about 650° C. and a hydrocarbon partial pressure from about 10 to about 40 psia (about 70 to about 280 kPa).

Abstract: A bitumen/steam pre-mixer and atomizing nozzle combine to produce a jet of minute liquid droplets (bitumen) in carrier gas (steam). The jet is injected into a draft tube mixer positioned in a fluid bed of hot coke particles suspended in steam and contained within a fluid coking reactor. The movement of the jet through the draft tube passageway induces a stream of coke particles in steam to be drawn into the passageway, where the jet and stream mix vigorously and bitumen droplets have an enhanced probability of contacting coke particles.

Abstract: A cavitation enhanced atomizing process comprises forming a flowing solution of the liquid to be atomized and a lower boiling cavitating liquid. This flowing solution is then contacted with a pressure reducing means, at a temperature below the bubble point of the cavitating liquid in the solution, to produce cavitation bubbles. These bubbles comprise cavitation liquid vapor and the bubble nucleation produces a two-phase fluid of the bubbles and liquid solution. The two-phase fluid is passed downstream into and through an atomizing means, such as an orifice, and into a lower pressure atomizing zone, in which the bubbles vaporize to form a spray of liquid droplets. The nucleated bubbles also grow in size as the so-formed two-phase fluid passes downstream to and through the atomizing means.

Abstract: A shelf is incorporated into a typical FCC riser that permits the tips of the nozzles to extend past the wall of the riser while preventing the tips from promoting coke build-up and protecting the tips from erosion. The shelf can be part of an angled section that often appears in a transition zone for increasing the internal diameter of the riser to accommodate the volumetric expansion of the feed. The shelf section reduces the non-uniformity in the mixing of the catalyst and feed and minimizes backmixing of the feed injection. The shelf of this invention accomplishes these objectives without recessing the feed injectors into the riser wall which can interfere with the spray pattern.

Abstract: The invention relates to chemistry and in particular to technology for processing hydrocarbon fuel, including engine fuel. The invention makes it possible to obtain a fuel with high cetane and octane numbers by means of the following: the initial fuel supply occurs simultaneously with ejection; an ozone containing gas is fed into the ejection area; turbulent flows are created by displacement of such a mixture; the transformed mixture is directed into a volume with a stable pressure level; and thermodynamic equalization of the mixture parameters is achieved. During thermodynamic equalization, sprayed water is injected into said mixture.

Abstract: A catalytic cracking process is described wherein the cracking takes place in a reactor under the influence of a rotating fluidized bed catalyst and compressed gases and/or steam is injected in order to effect movement of the catalyst bed.

Abstract: A cavitation enhanced atomizing process comprises forming a flowing solution of the liquid to be atomized and a lower boiling cavitating liquid. This flowing solution is then contacted with a pressure reducing means, at a temperature below the bubble point of the cavitating liquid in the solution, to produce cavitation bubbles. These bubbles comprise cavitation liquid vapor and the bubble nucleation produces a two-phase fluid of the bubbles and liquid solution. The two-phase fluid is passed downstream into and through an atomizing means, such as an orifice, and into a lower pressure atomizing zone, in which the bubbles vaporize to form a spray of liquid droplets. The nucleated bubbles also grow in size as the so-formed two-phase fluid passes downstream to and through the atomizing means.

Abstract: A slurry feed of a heavy hydrocarbon feedstock and coke-inhibiting additive particles together with a hydrogen-containing gas, are fed upward through a confined hydrocracking zone in a vertical, elongated, cylindrical vessel with a generally dome-shaped bottom head. A mixed effluent is removed from the top containing hydrogen and vaporous hydrocarbons and liquid heavy hydrocarbons. The slurry feed mixture and a portion of the hydrogen-containing gas are fed into the hydrocracking zone through an injector at the bottom of the dome-shaped bottom head and the balance of the hydrogen-containing gas is fed into the hydrocracking zone through injection nozzles arranged within of the hydrocracking zone at a location above the slurry-feed injector. The combined slurry feed and hydrogen-containing gas are injected at a velocity whereby the additive particles are maintained in suspension throughout the vessel and coking reactions are prevented.

Abstract: The upstream portion of a reactor (1), contains, between the feeding area of the catalyst flow and the injection area of the charge to be cracked, at least one solid and attached packing element (6, 6′), that extends over all or part of the cross section of the reactor and consists of a network of cells through which pass the catalyst particles. This network makes it possible to create at least one step of division and recombination of the flow of catalyst particles, so as to redistribute the latter in a homogenous manner over the cross section of the reactor.

Abstract: A cavitation enhanced atomizing process comprises forming a flowing solution of the liquid to be atomized and a lower boiling cavitating liquid. This flowing solution is then contacted with a pressure reducing means, at a temperature below the bubble point of the cavitating liquid in the solution, to produce cavitation bubbles. These bubbles comprise cavitation liquid vapor and the bubble nucleation produces a two-phase fluid of the bubbles and liquid solution. The two-phase fluid is passed downstream into and through an atomizing means, such as an orifice, and into a lower pressure atomizing zone, in which the bubbles vaporize to form a spray of liquid droplets. The nucleated bubbles also grow in size as the so-formed two-phase fluid passes downstream to and through the atomizing means.

Abstract: An FCC feed injection arrangement injects feed transversely from the sides of a restricted opening into a stream of FCC catalyst to provide good feed and catalyst contacting in an arrangement that simplifies external pipe configurations and maintenance of the feed injection system. The invention forms a venturi or restricted opening by forming a generally square opening between two parallel extended chords on opposite sides of the riser. A venturi area may be built out of refractory lining or other abrasion resistant structures. The invention may use horizontally extended pipes that are tangentially positioned apart from each other across from the restricted opening to provide a simple construction for the feed injection arrangement. The pipes are easily inserted and withdrawn from the riser to permit easy maintenance of the nozzles in the highly erosive environment.

Abstract: An improved apparatus and method for the fluidized catalytic cracking (FCC) of hydrocarbons. Turbulence generation means disposed on the internal surface of an FCC riser-reactor are utilized to provide for a more uniform catalyst flow pattern within the riser-reactor and to thereby provide for a better conversion and product slate.

Abstract: This invention makes possible substantially continuous flow of uniformly distributed hydrogen and hydrocarbon liquid across a densely packed catalyst bed to fill substantially the entire volume of a reactor vessel by introducing the fluids as alternate annular rings of gas and liquid (i.e. a mixture of liquid hydrocarbon and a hydrogen-containing gas) at a rate insufficient to levitate or ebullate the catalyst bed. Catalyst are selected by density, shape and size at a design feed rate of liquids and gas to prevent ebullation of the packed bed at the design feed rates. Catalysts are selected by measuring bed expansion, such as in a large pilot plant run, with hydrocarbon, hydrogen, and catalyst at the design pressures and flow velocities. The liquid and gas components of the feed flow into the bed in alternate annular rings across the full area of the bed.

Abstract: An apparatus is described for promoting annularly uniform flow in a reaction space of a mixed phase reactor. The apparatus defines ports which face a shared direction relative to the axis. The apparatus is useful in a process, also described, in which fluid emerging from the ports creates a turning moment which rotates fluid in a plenum adjacent the reaction space.

Abstract: This invention makes possible substantially continuous flow of uniformly distributed hydrogen and hydrocarbon liquid across a densely packed catalyst bed which substantially fills the entire volume of a reactor vessel. Catalyst are selected to be essentially the same density, shape and size at a design feed rate of liquids and gas to prevent ebullation of the packed catalyst bed at the design feed rates. The liquid and gas components of the hydrocarbon feed stream flow into the bed of catalyst and a quenching medium, which is preferably a liquid, is injected into the bed of catalyst. Injection of a liquid quench reduces the gas component of the hydrocarbon feed stream while simultaneously increasing the residence time and reducing the liquid velocity of the liquid component of the hydrocarbon feed stream within the substantially packed bed of catalyst.

Abstract: An improved riser reactor containing a plurality of substantially vertically oriented venturis connected in series whereby the venturis have a maximum diameter, D.sub.1, and a minimum diameter, D.sub.2 ; and, apparatus for connecting the venturis end to end in which the cross-sectional area of the venturis at D.sub.1 is A.sub.1 and the cross sectional area at D.sub.2 is A.sub.2 and the ratio of A.sub.1 /A.sub.2 is between about 1.1 and about 113, preferably between about 2 and about 100, most preferably between about 5 and about 50. The present invention also includes a process for catalytic cracking of a liquid hydrocarbon feed by use of the riser reactor of this invention.

Abstract: This invention makes possible substantially continuous flow of uniformly distributed hydrogen and hydrocarbon liquid across a densely packed catalyst bed to fill substantially the entire volume of a reactor vessel by introducing the fluids as alternate annular rings of gas and liquid (i.e. a mixture of liquid hydrocarbon and a hydrogen-containing gas) at a rate insufficient to levitate or ebullate the catalyst bed. Catalyst are selected by density, shape and size at a design feed rate of liquids and gas to prevent ebullation of the packed bed at the design feed rates. Catalysts are selected by measuring bed expansion, such as in a large pilot plant run, with hydrocarbon, hydrogen, and catalyst at the design pressures and flow velocities. The liquid and gas components of the feed flow into the bed in alternate annular rings across the full area of the bed.

Abstract: This invention makes possible substantially continuous flow of uniformly distributed hydrogen and hydrocarbon liquid across a densely packed catalyst bed to fill substantially the entire volume of a reactor vessel by introducing the fluids as alternate annular rings of gas and liquid (i.e. a mixture of liquid hydrocarbon and a hydrogen-containing gas) at a rate insufficient to levitate or ebullate the catalyst bed. Catalyst are selected by density, shape and size at a design feed rate of liquids and gas to prevent ebullation of the packed bed at the design feed rates. The liquid and gas components of the hydrocarbon feed flow into the catalyst bed from concentric annular rings that are coaxial with the catalyst bed. At the desired hydrocarbon flow rate, such catalyst bed continually flows in a plug-like manner downwardly through the reactor vessel. Catalyst is removed on a periodic or semicontinuous basis by laminarly flowing catalyst particles in a liquid stream out of the bottom of the catalyst bed.

Abstract: This invention makes possible substantially continuous flow of uniformly distributed hydrogen and hydrocarbon liquid across a densely packed catalyst bed which substantially fills the entire volume of a reactor vessel. Catalyst are selected to be essentially the same density, shape and size at a design feed rate of liquids and gas to prevent ebullation of the packed catalyst bed at the design feed rates. The liquid and gas components of the hydrocarbon feed stream flow into the bed of catalyst and a quenching medium, which is preferably a liquid, is injected into the bed of catalyst. Injection of a liquid quench reduces the gas component of the hydrocarbon feed stream while simultaneously increasing the residence time and reducing the liquid velocity of the liquid component of the hydrocarbon feed stream within the substantially packed bed of catalyst.

Abstract: In an ebullated bed process for hydrotreating a distillate hydrocarbon feedstock it has been found that a catalyst addition slurry is made up with catalyst and feedstock. A control system provides for a constant distillate feedstock rate during intermittent catalyst addition.

Abstract: A reactor for refining resid includes an elongated vertical vessel containing a bed of catalyst which is expanded or ebullated by a liquid/gas mixture. The mixture rises in an updraft through the bed and then is recirculated with an increased velocity by an ebullating pump. To reduce gas holdup of the ebullated bed and to promote a more uniform flow, the gas is entrapped by two cascaded stages of baffles which have an internal conical shape to guide, direct, and entrap the gas. One of these two stages has a shape which creates a countercurrent in the flowing liquid to deflect any catalyst particles which might otherwise be elutriated by the increased velocity.

Abstract: On-stream catalyst replacement hydroprocessing method wherein an upstream mixture of hydrogen and hydrocarbon liquid counter flows through a downwardly moving bed of hydroprocessing catalyst in a reactor vessel. The mixed feed stream of hydrogen and liquid hydrocarbon components enters a surge zone between the lower end of the reactor and a plenum zone to form a common pool under a conical support for the lower end of the downflowing catalyst bed. The mixed feed enters the plenum chamber through a plurality of passageways extending downwardly from the plenum zone to the same depth adjacent the lower end of the surge zone so that the liquid component normally prevents hydrogen from establishing independent paths before entering the plenum zone. Separation of the hydrogen and hydrocarbon liquid components from the mixed feed is thus assured to occur in the plenum zone directly below the pervious conical support to form a plurality of stepped concentric local reservoir rings under the conical support.

Abstract: In an ebullated bed process the feedstock conduit is provided with at least 50 psi (4.4 atm) head in excess of a liquid-vapor separation pressure. The excess head is used in combination with an eductor to recycle a reactor effluent liquid. The expanded catalyst bed is thereby maintained at 110 vol % to vol % of a settled catalyst volume. A separate pump to expand (ebullate) the catalyst bed is not required.

Abstract: In an ebullated bed process reactor effluent is subjected to high pressure followed by intermediate flash separation. An ebullation liquid is formed by educting high pressure flash separation liquid into an intermediate flash separation liquid. The ebullation liquid is recycled to the reactor to expand the catalyst bed to 110 vol % to 200 vol % of a settled catalyst bed volume. As a result of recycle pressure balance is advantageously maintained. Carry over catalyst and catalyst fines are recycled to the reactor and kept out of downstream equipment.

Abstract: In a fluidized catalytic cracking (FLC) type unit for contacting of a hydrocarbon feedstock with hot solid particles in a fluidized bed in an upright tubular-type upflow hydrocarbon conversion reactor, there is provided, between the means for fluidization and the means for injection of the feedstock, a means for causing the fluidized phase at the periphery of the reactor to rotate about the axis of the reactor.

Abstract: A process and apparatus for achieving hot catalyst stripping of spent FCC catalyst in a stripper mounted over a bubbling bed regenerator. Hot catalyst stripping is achieved by indirect transfer of heat from the regenerator to the stripper. Heat pipes, surface modifications such as fins on the stripper vessel, or use of a stripper in, or connective with, a heat exchange tube bundle may be used to heat spent catalyst with heat from the regenerator dilute phase, without transferring catalyst from the regenerator. The benefits of hotter catalyst stripping are achieved, without increasing catalyst traffic in the regenerator.

Abstract: A fluid catalytic cracking unit equipped with multiple feed injection points along the length of the riser is operated such that all of the fresh feed is charged to one of different feed injection points, depending on the ratio of light distillate (gasoline) to middle distillate (light catalytic gas oil) that is desired in the product slate. When all of the fresh feed is charged to one of the upper injection points in the riser in order to increase middle distillate yield, the unconverted slurry oil (650.degree. F.+material) can be recycled to a location below the injection point of the fresh feed so as to increase conversion to middle distillate while lowering the activity of the catalyst (via coke deposition) for single pass conversion of the fresh feed. Steam in excess of levels typically employed for dispersion is used at the bottom of the riser to lift the regenerated catalyst up to the feed injection points.

Abstract: This invention makes possible substantially continuous flow of uniformly distributed hydrogen and hydrocarbon liquid across a densely packed catalyst bed to fill substantially the entire volume of a reactor vessel by introducing the fluids as alternate annular rings of gas and liquid at a rate insufficient to levitate the bed and with catalyst selected by a density, shape and size at a design feed rate of liquids and gas to prevent ebulation of the packed bed at the design feed rates. Catalysts are selected by measuring bed expansion in a large pilot plant run with hydrocarbon, hydrogen, and catalyst at the design pressures and flow velocities. The liquid and gas components of the feed flow into the bed in alternate annular rings across the full area of the bed.

Abstract: A process and apparatus are disclosed for achieving turbulent or fast fluidized bed regeneration of spent FCC catalyst in a bubbling bed regenerator having a stripper mounted over the regenerator and a stripped catalyst standpipe within the regenerator. A closed coke combustor vessel is added alongside an existing regenerator vessel, and spent catalyst is discharged into a transfer pot beneath the existing dense bed, then into the coke combustor. Catalyst is regenerated in a turbulent or fast fluidized bed, and discharged into the dilute phase region above the existing bubbling dense bed. The discharge line preferably encompasses, and is in a heat exchange relationship with, the spent catalyst standpipe. Discharge catalyst is collected in the bubbling dense bed surrounding the coke combustor, and may be given an additional stage of regeneration. Catalyst may be recycled from the dense bed to the transfer pot.

Abstract: A process and apparatus for achieving multistage, hot catalyst stripping of spent FCC catalyst in a bubbling bed regenerator having a stripper mounted over the regenerator and a stripped catalyst standpipe within the regenerator. Hot catalyst stripping is achieved by lifting regenerated catalyst into the conventional stripper or to a secondary catalyst stripper under the primary stripper. Spent catalyst is heated by direct contact heat exchange with hot regenerated catalyst. Three different types of lift gas may be used to transport catalyst from the regenerator to the hot stripper, a light reactive hydrocarbon, an inert, or steam.

Abstract: A process and apparatus are disclosed for achieving turbulent or fast fluidized bed regeneration of spent FCC catalyst in a bubbling bed regenerator having a stripper mounted over the regenerator and a stripped catalyst standpipe within the regenerator. A coke combustor vessel is immersed in, and in open fluid communication with, the bubbling dense bed of the existing regenerator vessel. Spent catalyst is discharged into the coke combustor, mixes with hot regenerated catalyst which flows into the coke combustor, and regenerated with combustion air in a turbulent or fast fluidized bed. Catalyst and flue gas are discharged up into a dilute phase transport riser, preferably into cyclone which separate hot regenerated catalyst from flue gas. Regenerated catalyst is collected in the bubbling dense bed surrounding the coke combustor, and some is recycled by flowing into the coke combustor for direct contact heat exchange.

Abstract: A process and apparatus for achieving turbulent or fast fluidized bed regeneration of spent FCC catalyst in a bubbling bed regenerator having a stripper mounted over the regenerator and a stripped catalyst standpipe within the regenerator. A closed coke combustor vessel is added to the existing regenerator vessel, and spent catalyst is discharged into the coke combustor and regenerated in a turbulent or fast fluidized bed, and discharged up into a dilute phase transport which preferably encompasses, and is in a countercurrent heat exchange relationship with, the spent catalyst standpipe. Regenerated catalyst is discharged from the dilute phase transport riser, and collected in the bubbling dense bed surrounding the coke combustor. Catalyst may be recycled from the dense bed to the coke combustor for direct contact heat exchange. Catalyst coolers may be used on catalyst recycle lines to the coke combustor, or on the line returning regenerated catalyst to the cracking reactor.

Abstract: A process and apparatus for achieving multistage, hot catalyst stripping of spent FCC catalyst in a bubbling bed regenerator having a stripper mounted over the regenerator and a stripped catalyst standpipe within the regenerator. A secondary or hot catalyst stripper is placed under the primary stripper and within the existing regenerator vessel. Spent catalyst from the primary stripper is heated in the secondary stripper by at least one of immersion in the bubbling dense bed of hot regenerated catalyst, addition of hot regenerated catalyst recovered from the discharged into the coke combustor and regenerated in a turbulent or fast fluidized bed, and discharged up into a dilute phase transport riser which preferably encompasses, and is in a countercurrent heat exchange relationship with, the spent catalyst standpipe. Regenerated catalyst is discharged from the dilute phase transport riser, and collected in the bubbling dense bed surrounding the coke combustor.

Abstract: A hydrotreating process is provided with at least one deflector to minimize catalyst agglomeration and buildup. Preferably, the deflectors comprise an inner annular baffle and an outer annular baffle.

Abstract: A process for separating finely divided petroleum cracking catlyst from a mixture of the finely divided catalyst particles with a high boiling refractory hydrocarbon oil by intimately contracting said mixture with a concentrated aqueous solution of a basic alkali metal compound at a temperature above 170.degree. F., the quantity of aqueous solution employed being substantially greater than the quantity of said mixture with which it is contracted.

Abstract: Method and apparatus for liquid feed dispersion in fluid catalytic cracking systems wherein an improved fluidized catalytic cracking nozzle assembly having a nozzle unit so constructed that substantially all liquid fed through the unit is converted to mist-sized particles over a wide-angle dispersion pattern, the unit being recessed within a protective pipe having a shield on the inside thereof in the area of the recess, is disclosed.

Abstract: A catalytic cracking process is disclosed which comprises catalytically cracking a hydrocarbon charge stock in a catalytic cracking unit possessing at least one reaction zone, stripping zone and catalyst regeneration zone to provide a gasiform product employing as catalyst a mixed catalyst system which comprises, as a first catalyst component, particles of a cracking catalyst which requires relatively frequent regeneration and is relatively hydrothermally stable, and as a second catalyst component, particles of a catalyst which requires less frequent regeneration than the first catalyst component, physical characteristic(s) of particles of first catalyst component differing sufficiently from physical characteristic(s) of particles of second catalyst component as to permit their separation in the stripping zone.

Abstract: A feedstock pipe for a FCC unit is provided with a plurality of turbulence generating members mounted on its interior surface. Each of the turbulence generating members has a pointed tip pointing toward the discharge end of the pipe and a ramp inclined toward the center of the pipe leading to the pointed tip.

Abstract: Catalyst/oil mixing in a catalytic cracking unit can be effected at approximately right angles by introducing the liquid oil axially into the mouth of the riser and bringing the catalyst radially inwardly into the mouth of the riser from substantially the entire circumference thereof.

Abstract: A gas-liquid or a gas-liquid-solid feed is contacted in a vessel containing a packed bed of contact particles. At least a portion of the feed is passed upwardly through the packed bed and the mass flow rate of the feed is periodically increased sufficiently to cause a portion of the particles within the vessel to form an expanded region within the packed bed.

Abstract: Improvements in converting C.sub.1 -C.sub.3 monohydric alcohols, particularly methanol, related oxygenates of said alcohols and/or oxygenates produced by Fischer-Tropsch synthesis to light olefins, gasoline boiling range hydrocarbons and/or distillate boiling range hydrocarbons are obtained in a fluidized bed of ZSM-5 type zeolite catalyst operating under conditions effective to provide fluidization in the turbulent regime.

Abstract: A two-stage catalytic hydroconversion process for heavy hydrocarbon feedstocks usually containing fine particulate solids to produce lower boiling hydrocarbon liquid and gas products. The feedstock is fed into a first stage ebullated bed reactor containing fine sized catalyst and operated at moderate reaction conditions for hydroconversion to produce hydrocarbon gas and liquid fractions, from which a low boiling liquid fraction is separated and withdrawn as a product. The remaining gas and heavier liquid fractions are recombined and fed to a second stage ebullated bed reactor containing larger size catalyst for further hydroconversion reactions at less severe conditions to produce lower boiling hydrocarbon liquid fractions. Following product distillation steps, liquid product fractions are withdrawn and a portion of vacuum bottoms material is recycled to the second stage reactor to provide increased hydroconversion and improved yields of the light hydrocarbon liquid product.

Abstract: An improved process for economically converting carbo-metallic oils to lighter products. Enhanced catalyst activity is enjoyed through use of a select process to vaporize and atomize the high boiling portion of a carbo-metallic oil feed. The carbo-metallic oil feed is dispersed into droplets having a diameter of at least smaller than 350 microns and preferably 100 microns or less. These small droplets ensure more even coverage of the catalyst surface and decrease diffusion problems. The water utilized for dispersion of the carbo-metallic oil feed is present as a homogenized mixture in fine oil droplets with an average diameter below 1,000 microns. The water is dispersed in the carbo-metallic oil feed through use of a select mixing apparatus and can be dispersed as finer droplet sizes through use of an emulsifying or dispersing agent. The ratio of water to carbo-metallic oil feed ranges from about 0.04 to 0.25 by weight and the concentration of emulsifying agent ranges from 0.01 to 10 wt.