Process for preparing aromatics from methane

The present invention relates to a process for carrying out endothermic, heterogeneously catalyzed reactions in which the reaction of the starting materials is carried out in the presence of a mixture of inert heat transfer particles and catalyst particles, where the catalyst particles are regenerated in a nonoxidative atmosphere at regular intervals and the heat of reaction required is introduced by separating off the inert heat transfer particles, heating the heat transfer particles in a heating zone and recirculating the heated heat transfer particles to the reaction zone. The process of the invention is particularly suitable for the nonoxidative dehydroaromatization of C 1 -C 4 -aliphatics in the presence of zeolite-comprising catalysts.

Enclosure of an FCC Unit Comprising an Inner Support Device Rigidly Connected to Cyclones

The invention relates to an enclosure () of a fluid catalytic cracking unit in which an inner space is defined by a side wall () having a longitudinal axis extending substantially in the direction of gravity, said enclosure being provided with a plurality of mechanical separation cyclones () located inside the inner space. The enclosure () comprises a supporting device () attached only to the cyclones () by: an annular peripheral support element () extending along the side wall () in a plane perpendicular to the longitudinal axis (X), separated from the side wall by a predetermined clearance; and a plurality of beams () extending in the same plane as the peripheral support element (), the beams being rigidly connected to the peripheral support element and to at least one mechanical separation cyclone by one end or by an attachment part distant from the ends thereof. 116.-. (canceled)17. A chamber of a fluid catalytic cracking unit comprising a lateral wall which delimits an internal volume having a longitudinal axis extending substantially in the direction of gravity , said chamber being provided with a plurality of mechanical separation cyclones situated inside said internal volume , characterized in that said chamber comprises , inside said internal volume , a support device secured only to the mechanical separation cyclones and comprising:a peripheral support element extending along the lateral wall in a plane perpendicular to the longitudinal axis (X), distant from the lateral wall by a predetermined clearance in the plane of the support element,a plurality of beams extending in the same plane as the peripheral support element, the beams being secured to the peripheral support element and to at least one mechanical separation cyclone by an end or by a fixing part distant from its ends.18. The chamber as claimed in claim 17 , characterized in that the support device comprises other beams extending in the same plane as the peripheral support element and chosen ...

FLUIDIZED BED MEMBRANE REACTOR

Herein disclosed is a dry reforming reactor comprising a gas inlet near the bottom of the reactor; a gas outlet near the top of the reactor; a fluidized bed comprising a catalyst; and one or more hydrogen membranes comprising palladium (Pd). In some cases, the one or more hydrogen membranes comprises Pd alloy membranes, or Pd supported on ceramics or metals. In some cases, the one or more hydrogen membranes are placed vertically in the reactor as hydrogen membrane tubes hanging from the top of the reactor. In some cases, the hydrogen membranes are configured to selectively collect hydrogen from the tubes via one or more internal manifolds and sent to an external hydrogen collection system. 1. A dry reforming reactor comprisinga gas inlet near the bottom of the reactor;a gas outlet near the top of the reactor;a fluidized bed comprising a catalyst; andone or more hydrogen membranes comprising palladium (Pd).2. The reactor of wherein said one or more hydrogen membranes comprises Pd alloy membranes claim 1 , or Pd alloys supported on ceramic or metal substrates.3. The reactor of wherein said one or more hydrogen membranes are placed vertically in the reactor as hydrogen membrane tubes hanging from the top of the reactor.4. The reactor of wherein the hydrogen membranes are configured to selectively collect hydrogen from the tubes via one or more internal manifolds and sent to an external hydrogen collection system.5. The reactor of wherein the gas inlet is configured to allow one or more feed streams to enter the reactor via a manifold or distributor.6. The reactor of wherein the catalyst comprises nickel and alumina.7. The reactor of wherein the reactor is configured to allow reformed gas to exit the top of the reactor and separate from spent catalyst.8. The reactor of wherein no steam or oxygen injection is needed.9. The reactor of is operated at a temperature range of 600-700° C. and a pressure range of 700-800 kPa.10. A method of producing dimethyl ether (DME) ...

FLUIDIZED BED MEMBRANE REACTOR

Herein disclosed is a dry reforming reactor comprising a gas inlet near the bottom of the reactor; a gas outlet near the top of the reactor; a fluidized bed comprising a catalyst; and one or more hydrogen membranes comprising palladium (Pd). In some cases, the one or more hydrogen membranes comprises Pd alloy membranes, or Pd supported on ceramics or metals. In some cases, the one or more hydrogen membranes are placed vertically in the reactor as hydrogen membrane tubes hanging from the top of the reactor. In some cases, the hydrogen membranes are configured to selectively collect hydrogen from the tubes via one or more internal manifolds and sent to an external hydrogen collection system. 1. A dry reforming reactor comprisinga gas inlet near the bottom of the reactor;a gas outlet near the top of the reactor;a fluidized bed comprising a catalyst; andone or more hydrogen membranes comprising palladium (Pd).2. The reactor of wherein said one or more hydrogen membranes comprises Pd alloy membranes claim 1 , or Pd alloys supported on ceramic or metal substrates.3. The reactor of wherein said one or more hydrogen membranes are placed vertically in the reactor as hydrogen membrane tubes hanging from the top of the reactor.4. The reactor of wherein the hydrogen membranes are configured to selectively collect hydrogen from the tubes via one or more internal manifolds and sent to an external hydrogen collection system.5. The reactor of wherein the gas inlet is configured to allow one or more feed streams to enter the reactor via a manifold or distributor.6. The reactor of wherein the catalyst comprises nickel and alumina.7. The reactor of wherein the reactor is configured to allow reformed gas to exit the top of the reactor and separate from spent catalyst.8. The reactor of configured to use no process water and no oxygen.9. The reactor of is operated at a temperature range of 600-700° C. and a pressure range of 700-800 kPa.10. The reactor of comprising one or more internal ...

PROCESSES AND SYSTEMS FOR USING SILICA PARTICLES IN FLUID BED REACTOR

The present disclosure relates to fluid bed processes that utilize silica particles as a fluidization aid. The process comprises reacting one or more reactants in a reactor comprising a fluid bed to form a product. The fluid bed comprises a catalyst composition comprising a catalyst and an inert additive composition comprising silica particles from 0.5 wt % to 30 wt %, based on the total weight of the catalyst composition. The silica particles are discrete, inert particles that are mixed with the catalyst in the fluid bed. 1. A process comprising:reacting one or more reactants in a reactor comprising a fluid bed to form a product;wherein the fluid bed comprises a catalyst composition comprising a catalyst and an inert additive composition comprising from 0.5 wt % to 30 wt % of silica particles, based on the total weight of the catalyst composition,wherein the silica particles have an equivalent median particle diameter ranging from 10 microns to 500 microns.2. The process of claim 1 , wherein the catalyst comprises one or more of antimony claim 1 , uranium claim 1 , iron claim 1 , bismuth claim 1 , vanadium claim 1 , molybdenum claim 1 , nickel claim 1 , potassium claim 1 , cobalt claim 1 , oxides thereof claim 1 , or salts thereof.3. The process of claim 1 , wherein the catalyst has an equivalent median diameter ranging from 1 microns to 125 microns.4. The process of claim 1 , wherein the silica particles have a real density ranging from 1.8 g/cmto 2.8 g/cm claim 1 , and wherein the difference between the density of the silica particles and the catalyst is less than 75%.5. The process of claim 1 , wherein the silica particles have a surface area less than 50 m/g claim 1 , and wherein the silica particles have a hardness ranging from 500 to 720 as measured by ASTM E384 (2018).6. The process of claim 1 , wherein the silica particles have a sphericity ranging from 60% to 99.9%7. The process of claim 1 , wherein the catalyst composition further comprises alumina ...

FLUID CATALYTIC CRACKING PROCESSES AND APPARATUS

Apparatus and processes herein provide for converting hydrocarbon feeds to light olefins and other hydrocarbons. The processes and apparatus include a conventional riser reactor in combination with a mixed flow (e.g., including both counter-current and co-current catalyst flows) fluidized bed reactor designed for maximizing light olefins production. The effluents from the riser reactor and mixed flow reactor are processed in a catalyst disengagement vessel, and the catalysts used in each reactor may be regenerated in a common catalyst regeneration vessel. Further, integration of the two-reactor scheme with a catalyst cooler provides a refinery the flexibility of switching the operation between the two-reactor flow scheme, a catalyst cooler only flow scheme, or using both simultaneously. 1. A system for processing hydrocarbons , comprising:a riser reactor configured to contact a mixture of first particles and second particles with a hydrocarbon feedstock to convert at least a portion of the hydrocarbon feedstock and to recover a riser reactor effluent comprising mixed hydrocarbons and the mixture of the first and second particles, wherein the first particle has a smaller average particle size and/or is less dense than the second particle, and wherein the first particle and second particle may independently be catalytic or non-catalytic particles; an overhead product line for recovering from the reactor a reactor effluent comprising first particles, a first portion of the second particles, and hydrocarbons;', 'a bottoms product line for recovering from the reactor a second stream comprising a second portion of the second particles;, 'a reactor configured to contact a mixture comprising the first particles and the second particles with a second hydrocarbon feedstock to convert at least a portion of the second hydrocarbon feedstock, wherein the reactor is fluidly connected toa particle separator configured to separate second particles from the reactor effluent, and to ...

FLUID CATALYTIC CRACKING PROCESS AND APPARATUS FOR MAXIMIZING LIGHT OLEFIN YIELD AND OTHER APPLICATIONS

Apparatus and processes herein provide for converting hydrocarbon feeds to light olefins and other hydrocarbons. The processes and apparatus include, in some embodiments, feeding a hydrocarbon, a first catalyst and a second catalyst to a reactor, wherein the first catalyst has a smaller average particle size and is less dense than the second catalyst. A first portion of the second catalyst may be recovered as a bottoms product from the reactor, and a cracked hydrocarbon effluent, a second portion of the second catalyst, and the first catalyst may be recovered as an overhead product from the reactor. The second portion of the second catalyst may be separated from the overhead product, providing a first stream comprising the first catalyst and the hydrocarbon effluent and a second stream comprising the separated second catalyst, allowing return of the separated second catalyst in the second stream to the reactor. 1. A process for the conversion of hydrocarbons , comprising:feeding a mixture of first particles and second particles from a regenerator to a transport vessel or riser reactor, wherein the first particles have a smaller average particle size and/or are less dense than the second particles, and wherein the first particles and second particles may independently be catalytic or non-catalytic particles;feeding a reactive and/or non-reactive carrier fluid to the transport vessel or riser reactor;recovering an overhead product from the transport vessel/riser reactor comprising the carrier fluid and/or a reaction product of the carrier fluid, the second particles, and the first particles; a housing;', 'a solids separation device disposed within the housing for separating the second particles from the overhead product to provide a first stream, comprising the first particles and the carrier fluid and/or a reaction product of the carrier fluid, and a second stream, comprising the separated second particles;', 'one or more cyclones disposed within the housing for ...

PROCESS AND APPARATUS FOR PRODUCING OLEFINS FROM LIGHT ALKANES

A process and an apparatus for producing olefins from light alkanes. A light alkane feed is contacted with catalyst particles in each of reactors, wherein each of the reactors is a fluidized bed reactor. At least a portion of the alkane feed is converted to olefins using the catalyst particles, wherein the olefins form a part of a reactor effluent stream. The reactor effluent streams from each of the reactors are merged to form a merged effluent stream. The merged effluent stream is separated into an olefin stream and the other streams. The other streams may comprise a recycle stream and light gases. 1. A method for producing olefins comprising:contacting a light alkane feed with dehydrogenation catalyst particles in each of reactors, wherein each of the reactors is a fluidized bed reactor partially embedded in a furnace;converting at least a portion of the alkane feed to olefins using the catalyst particles, wherein the olefins form a part of a reactor effluent stream;merging the reactor effluent streams from each of the reactors to form a first merged effluent stream; andseparating an olefin stream comprising the olefins from the first merged effluent stream.2. The method of claim 1 , wherein the light alkane feed comprises propane claim 1 , butane claim 1 , or a combination thereof.3. The method of claim 1 , wherein the olefin stream comprises propylene claim 1 , 1-butene claim 1 , 2-butene claim 1 , isobutene claim 1 , 1 claim 1 ,3-butadiene claim 1 , or a combination thereof.4. The method of claim 1 , wherein the separating step separates the first merged effluent stream into the olefin steam claim 1 , a recycle stream claim 1 , and light gases claim 1 , wherein the recycle stream comprises propane claim 1 , butane claim 1 , or a combination thereof claim 1 , and the light gases comprises methane and hydrogen.5. The method of claim 1 , wherein the catalyst particles are fluidized inside each of the reactors.6. The method of claim 1 , wherein the catalyst ...

PROCESS AND APPARATUS FOR REACTING FEED WITH A FLUIDIZED CATALYST OVER A TEMPERATURE PROFILE

A fluidized catalytic reactor utilizes an ascending temperature profile. The apparatus and process deliver cooler spent catalyst to a first catalyst distributor and a hotter regenerated catalyst to a second catalyst distributor that are spaced apart from each other. The reactant stream first encounters the first stream of catalyst and then encounters the second stream of catalyst. The process and apparatus stage the addition of hot catalyst to the reactant stream. The process and apparatus may be particularly advantageous in an endothermic reaction because the hotter catalyst will encounter reactants that have cooled due to the progression of endothermic reactions. 1. A reactor for contacting a reactant stream with a catalyst comprising:a reactant distributor for distributing the reactant stream to the reactor;a first catalyst inlet for feeding a first stream of catalyst to the reactor;a second catalyst inlet for feeding a second stream of catalyst to the reactor, the first catalyst inlet being closer to the reactant distributor than the second catalyst inlet;a product outlet for discharging product from the reactor, the second catalyst distributor being closer to the reactant distributor than the product outlet.2. The reactor of further comprising a regenerated catalyst pipe connected to said second catalyst inlet claim 1 , the regenerated catalyst pipe having an inlet connected to a catalyst regenerator.3. The reactor of further comprising a reaction chamber containing said first catalyst inlet and said second catalyst inlet and a separation chamber comprising a primary catalyst separator for separating catalyst from product gases claim 1 , said primary catalyst separator being located closer to the second catalyst inlet than the product outlet.4. The reactor of further comprising a recycle catalyst pipe connected to said first catalyst inlet claim 3 , the recycle catalyst pipe having an inlet in the separation chamber.5. The reactor of further comprising a ...

PARTICLE DISENGAGEMENT DEVICE

A particle disengagements device comprising a baffle plate, wherein the baffle plate comprises one or more guide baffles and one or more separation baffles, wherein the one or more guide baffles and the one or more separation baffles define one or more air flow paths and one or more solid flow paths and associated systems and methods. 1. A particle disengagement device comprising a circular baffle plate , wherein the baffle plate comprises one or more guide baffles and one or more separation baffles , wherein the one or more guide baffles and the one or more separation baffles define one or more air flow paths and one or more solid flow paths.2. The particle disengagement device of claim 1 , wherein the baffle plate has a diameter in the range of from 1 meter to 15 meters.3. The particle disengagement device of claim 1 , wherein the baffle plate has a height in the range of from 1 to 20 inches.4. The particle disengagement device of claim 1 , wherein the one or more guide baffles comprise 10 to 50 guide baffles and the one or more separation vessel comprise 10 to 50 separation baffles.5. The particle disengagement device of claim 1 , wherein the baffle plate has a baffle arrangement comprising one or more parallel rows of guide baffles and separation baffles.6. The particle disengagement device of claim 1 , wherein the guide baffles comprise a protrusion.7. The particle disengagement device of claim 1 , wherein the separation baffle comprises a protrusion.8. The particle disengagement device of claim 6 , wherein the protrusion has a length in the range of from 0.1 inches to 8 inches.9. The particle disengagement device of claim 6 , wherein the protrusion has a rectangular cross sectional shape.10. The particle disengagement device of claim 1 , wherein the one or more guide baffles are spaced apart a distance in the range of from 4 inches to 25 inches.11. The particle disengagement device of claim 1 , wherein the one or more separation baffles are spaced apart a ...

FCC UNITS, SEPARATION APPARATUSES, AND METHODS FOR SEPARATING REGENERATED CATALYST

Apparatuses and methods for separating regenerated catalyst are provided. In one embodiment, an apparatus for separating regenerated catalyst includes a regeneration vessel including a catalyst bed section. The apparatus includes a catalyst settler physically separated from the catalyst bed section by a wall extending within the regeneration vessel. The catalyst overflowing the catalyst bed section flows over the wall and enters the catalyst settler. The apparatus further includes a pipe in fluid communication with the catalyst settler and configured to deliver regenerated catalyst from the regeneration vessel to another vessel. 1. An apparatus for separating regenerated catalyst , the apparatus comprising:a regeneration vessel comprising a catalyst bed section;a catalyst settler physically separated from the catalyst bed section by a wall extending within the regeneration vessel, wherein the catalyst overflowing the catalyst bed section flows over the wall and enters the catalyst settler; anda pipe in fluid communication with the catalyst settler and configured to deliver regenerated catalyst from the regeneration vessel to another vessel.2. The apparatus of wherein the catalyst settler is located in the regeneration vessel.3. The apparatus of wherein the catalyst settler is bounded by the regeneration vessel.4. The apparatus of further comprising a catalyst settler baffle within the catalyst settler.5. The apparatus of further comprising packing within the catalyst settler.6. The apparatus of further comprising an injection port in the catalyst settler configured to inject a gas into the catalyst settler and into contact with the regenerated catalyst to separate entrained gas therefrom.7. The apparatus of further comprising a nitrogen or steam source in fluid communication with the injection port claim 6 , wherein the injection port is configured to inject nitrogen or steam into the catalyst settler and into contact with the regenerated catalyst to separate ...

Method and apparatus for discharging a polymer from a gas-phase reactor

Process for discharging polyolefin particles from a gas-phase polymerization reactor of a pressure from 1.0 MPa to 10 MPa to a discharge vessel of a pressure from 0.1 MPa to 1.0 MPa wherein the discharging is carried out discontinuously through at least two discharge lines in which the polyolefin particles are transported horizontally or upwards, process for polymerizing olefins at temperatures of from 30° C. to 160° C. and pressures of from 1.0 MPa to 10 MPa in the presence of a polymerization catalyst in a gas-phase polymerization reactor comprising discharging the obtained polyolefin particles from the gas-phase polymerization reactor by the process for discharging polyolefin particles and apparatus for polymerizing olefins in the gas-phase comprising a polymerization reactor, a discharge vessel and at least two pipes connecting the polymerization reactor and the discharge vessel for discharging polyolefin particles, wherein the discharge lines are constructed in a way that the polyolefin particles conveyed from the polymerization reactor to the discharge vessel are transported horizontally or upwards.

TAPERED FLUIDIZED BED REACTOR AND PROCESS FOR ITS USE

A fluidized bed reactor includes a gas distributor, a tapered section above the gas distributor, and an expanded head above the tapered section. The gas distributor defines a plurality of inlets surrounding a product withdrawal tube, which extends away from the fluidized bed reactor. The fluidized bed reactor is useful in a process for fluidizing relatively large particles, such as Geldart Group B particles and/or Geldart Group D particles, where said particles are in a bubbling fluidized bed residing, in whole or in part, in the tapered section. The fluidized bed reactor and process may be used for manufacturing polycrystalline silicon. 1. A process for preparing polycrystalline silicon in a fluidized bed reactor , where the process comprises:feeding gases comprising hydrogen and a silicon bearing source gas comprising a silicon monomer into a bubbling fluidized bed containing silicon particles, where at least a portion of the bubbling fluidized bed resides in a tapered section of the fluidized bed reactor, where the tapered section expands upward and outward at a cone angle from vertical;feeding silicon particles into the fluidized bed reactor above the tapered section;heating the fluidized bed reactor, thereby causing thermal decomposition of the silicon monomer to produce polycrystalline silicon on surfaces of the silicon particles, thereby producing larger diameter particles; andremoving the larger diameter particles from the fluidized bed reactor.2. The process of claim 1 , where the cone angle ranges from 2.5° to 10.0°.3. The process of claim 1 , where the silicon bearing source gas comprises HSiCland optionally SiCl.4. The process of claim 1 , where the silicon bearing source gas comprises HSiBrand optionally SiBr.5. The process of claim 1 , where the silicon bearing source gas comprises SiH.6. The process of claim 1 , wherein i. a product withdrawal tube is mounted to the gas distributor,', 'ii. the gas distributor defines a plurality of feed inlets, and', ...

CATALYST ACTIVATOR

The invention relates generally to a catalyst activator, and in particular to a catalyst activator for heat conditioning a catalyst, comprising: a) a vessel for containing a catalyst charge having an internal diameter of at least 1.2 metres and/or an internal volume of at least 5 m; b) a fluidisation grid plate disposed in said vessel, said fluidisation grid plate and having an upper major surface and a lower major surface; c) an array of generally conical depressions in said upper major surface that overlap by less than 17%; and d) an array of holes perforating said fluidisation grid plate, said holes extending from at least some of said generally conical depressions through said lower surface. 123-. (canceled)24. A process for activating a batch of polymerisation catalyst which comprises fluidising the batch of polymerisation catalyst in a fluidisation zone of an activator vessel , wherein the activator vessel comprises a fluidisation zone and a disengagement zone above the fluidisation zone , the diameter of the fluidisation zone of the activator vessel being at least 1 m , the height of the fluidised bed of catalyst being at least twice the diameter of the fluidisation zone and the height of the disengagement zone being between 1 to 3 m.25. A process according to wherein the height of the fluidised bed of catalyst is at least three times the diameter claim 24 , for example at least four times the diameter.26. A process according to wherein the height of the fluidised bed of catalyst is between 2 and 8 m claim 24 , and preferably between 4 and 8 m.27. A process according to wherein the expansion on fluidisation is above 100% claim 24 , such as at least 120%.28. A process according to wherein the diameter of the fluidisation zone of the activator vessel is at least 1.2 m claim 24 , and preferably at least 1.5 m.29. A process according to wherein the settled bed has a depth between 1.8 and 3 m.30. A process according to wherein the settled bed has a bulk volume of ...

FLUID CATALYTIC CRACKING PROCESS AND APPARATUS FOR MAXIMIZING LIGHT OLEFIN YIELD AND OTHER APPLICATIONS

Apparatus and processes herein provide for converting hydrocarbon feeds to light olefins and other hydrocarbons. The processes and apparatus include, in some embodiments, feeding a hydrocarbon, a first catalyst and a second catalyst to a reactor, wherein the first catalyst has a smaller average particle size and is less dense than the second catalyst. A first portion of the second catalyst may be recovered as a bottoms product from the reactor, and a cracked hydrocarbon effluent, a second portion of the second catalyst, and the first catalyst may be recovered as an overhead product from the reactor. The second portion of the second catalyst may be separated from the overhead product, providing a first stream comprising the first catalyst and the hydrocarbon effluent and a second stream comprising the separated second catalyst, allowing return of the separated second catalyst in the second stream to the reactor. 1. (canceled)2. (canceled)3. (canceled)4. (canceled)5. (canceled)6. An integrated disengagement vessel comprising:a housing;a solids separation device disposed within the housing for separating a hydrocarbon stream comprising a hydrocarbon fraction, a second particles, and a first particles into a first stream, comprising the first particles and the hydrocarbon fraction, and a second stream, comprising the separated second particles;one or more cyclones disposed within the housing for separating the first stream to recover a solids fraction, comprising the first particles, and a vapor fraction, comprising the hydrocarbon fraction;an internal vessel disposed within the housing for receiving the second stream comprising the separated second particles;an annular region between the housing and the internal vessel for receiving the solids fraction comprising the first particles;a vapor outlet for recovering the vapor fraction.7. The system of claim 6 , further comprising a flow line for feeding the solids fraction from the annular region to a regenerator.8. The ...

DEVICE AND METHOD FOR PREPARING PARA-XYLENE AND CO-PRODUCING LIGHT OLEFINS FROM METHANOL AND/OR DIMETHYL ETHER AND BENZENE

A fast fluidized bed reactor, device and method for preparing para-xylene and co-producing light olefins from methanol and/or dimethyl ether and benzene, resolving or improving the competition problem between an MTO reaction and an alkylation reaction during the process of producing para-xylene and co-producing light olefins from methanol and/or dimethyl ether and benzene, and achieving a synergistic effect between the MTO reaction and the alkylation reaction. By controlling the mass transfer and reaction, competition between the MTO reaction and the alkylation reaction is coordinated and optimized to facilitate a synergistic effect of the two reactions, so that the conversion rate of benzene, the yield of para-xylene, and the selectivity of light olefins are increased. 124-. (canceled)25. A fast fluidized bed reactor for preparing para-xylene and co-producing light olefins from methanol and/or dimethyl ether and benzene , wherein the fast fluidized bed reactor comprises a first reactor feed distributor and a plurality of second reactor feed distributors , the first reactor feed distributor and the plurality of second reactor feed distributors are sequentially arranged along the gas flow direction in the fast fluidized bed reactor.26. The fast fluidized bed reactor of claim 25 , wherein the number of the second reactor feed distributors is in a range from 2 to 10.27. The fast fluidized bed reactor of claim 25 , wherein the fast fluidized bed reactor comprises a first reactor gas-solid separator and a second reactor gas-solid separator claim 25 , the first reactor gas-solid separator is placed in a dilute phase zone or outside a reactor shell claim 25 , and the second reactor gas-solid separator is placed in the dilute phase zone or outside the reactor shell;the first reactor gas-solid separator is provided with a regenerated catalyst inlet, a catalyst outlet of the first reactor gas-solid separator is placed at the bottom of a reaction zone, and a gas outlet of the ...

CATALYST REGENERATORS AND METHODS FOR REGENERATING CATALYSTS

Catalyst regenerators and methods of their use are provided. A catalyst regenerator includes a combustion chamber with a combustion chamber diameter and a combustion chamber bottom. A mixing chamber is fluidly coupled to the combustion chamber at the combustion chamber bottom, where the mixing chamber has an exterior wall and a mixing chamber diameter less than the combustion chamber diameter. A first and second catalyst inlet are fluidly coupled to the mixing chamber, and a mixing cylinder is within the mixing chamber. The mixing cylinder and the exterior wall define an annular space there-between, and the mixing cylinder includes a cylinder opening. 1. A catalyst regenerator comprising:a combustion chamber having a combustion chamber diameter and a combustion chamber bottom;a mixing chamber fluidly coupled to the combustion chamber at the combustion chamber bottom, wherein the mixing chamber has an exterior wall and a mixing chamber diameter less than the combustion chamber diameter;a first catalyst inlet fluidly coupled to the mixing chamber;a second catalyst inlet fluidly coupled to the mixing chamber; anda mixing cylinder within the mixing chamber, wherein the mixing cylinder and the exterior wall define an annular space there-between, and wherein the mixing cylinder comprises a cylinder opening.2. The catalyst regenerator of wherein the cylinder opening extends from below a lower most portion of the first catalyst inlet to above an upper most portion of the first catalyst inlet.3. The catalyst regenerator of wherein the mixing cylinder comprises a cylinder top that is closed claim 1 , and wherein the cylinder opening terminates below the cylinder top.4. The catalyst regenerator of wherein the mixing cylinder comprises a cylinder wall section claim 1 , and wherein the cylinder wall section is positioned facing the first catalyst inlet and the second catalyst inlet.5. The catalyst regenerator of wherein the cylinder opening faces one of the first catalyst inlet ...

Apparatuses and methods for cooling catalyst

Apparatuses and methods for cooling catalyst are provided. In one embodiment, an apparatus for cooling catalyst includes a catalyst cooler vessel having a catalyst inlet for receiving catalyst. The apparatus includes a gas distributor lance positioned in the catalyst cooler vessel and having a gas outlet configured for injecting gas into the catalyst. The apparatus also includes a heat exchange tube positioned in the catalyst cooler vessel and having an outer surface. The heat exchange tube is configured to transfer heat from the catalyst to a heat exchange fluid. The apparatus further includes a hard surfacing material located on the outer surface of the heat exchange tube.

USE OF A FUEL OIL WASH TO REMOVE CATALYST FROM A FLUIDIZED-BED PROPANE DEHYDROGENATION REACTOR EFFLUENT

A process where external fuel oil is used to wash entrained catalyst from a fluidized-bed propane dehydrogenation reactor effluent, where the fuel oil and catalyst mixture is returned to the reactor to provide the net fuel required for catalyst regeneration. Optionally the fluidized-bed propane dehydrogenation reactor effluent and the fuel oil are contacted in a direct contact inline device before entering a flash zone in the reactor vessel. 1. A method for recovering catalyst from a fluidized-bed propane dehydrogenation reactor effluent gas , the method comprising:(a) cooling fluidized-bed propane dehydrogenation reactor effluent gas;(b) contacting the cooled effluent gas with fuel oil in a wash section to wash out catalyst to obtain a cooled effluent gas essentially free of catalyst;(c) withdrawing an oil-catalyst slurry from the wash section and circulating the oil-catalyst slurry through a filter thereby removing catalyst from the fuel oil giving filtered wash oil;(d) returning filtered wash oil to the wash section as recirculated wash oil; and(e) backwashing the filter thereby recovering catalyst.2. The method of where the contacting and returning steps are effected in a quench tower comprising vapor-liquid contact elements and a bottoms zone holding a fuel oil inventory.3. The method of further comprising cooling the recirculated wash oil before the contacting step.4. The method of where circulating the oil-catalyst slurry through a filter comprises continuously passing the oil-catalyst slurry through at least one first filter in a filtration mode to separate the catalyst therefrom giving filtrate while at least one second filter in parallel with the first filter is in a backwashing mode thereby removing the separated catalyst therefrom.5. The method of further comprising returning filtrate from the first filter to the fuel oil inventory.6. The method of where the backwashing of the at least one filter further comprises periodically alternating the at least ...

PROCESS AND APPARATUS FOR ENHANCED REMOVAL OF CONTAMINANTS IN A FLUID CATALYTIC CRACKING PROCESSES

Systems for separating a contaminant trapping additive from a cracking catalyst may include a contaminant removal vessel having one or more fluid connections for receiving contaminated cracking catalyst, contaminated contaminant trapping additive, fresh contaminant trapping additive, and a fluidizing gas. In the contaminant removal vessel, the spent catalyst may be contacted with contaminant trapping additive, which may have an average particle size and/or density greater than the cracking catalyst. A separator may be provided for separating an overhead stream from the contaminant removal vessel into a first stream comprising cracking catalyst and lifting gas and a second stream comprising contaminant trapping additive. A recycle line may be used for transferring contaminant trapping additive recovered in the second separator to the contaminant removal vessel, allowing contaminant trapping additive to accumulate in the contaminant removal vessel. A bottoms product line may provide for recovering contaminant trapping additive from the contaminant removal vessel. 1. A system for cracking hydrocarbons , comprising:a first reactor for contacting a cracking catalyst with a hydrocarbon feedstock to convert at least a portion of the hydrocarbon feedstock to lighter hydrocarbons;a separator for separating the lighter hydrocarbons from spent cracking catalyst;a feed line for feeding separated spent cracking catalyst from the separator to a catalyst regenerator;a catalyst transfer line for transferring a portion of the spent cracking catalyst from the catalyst regenerator to a contaminant removal vessel;the contaminant removal vessel, for contacting the spent catalyst with a contaminant trapping additive having an average particle size and/or density greater than those of the cracking catalyst;a second separator for separating an overhead stream from the contaminant removal vessel into a first stream comprising cracking catalyst and lifting gas and a second stream comprising ...

FLUID CATALYTIC CRACKING PROCESS AND APPARATUS FOR MAXIMIZING LIGHT OLEFIN YIELD AND OTHER APPLICATIONS

Apparatus and processes herein provide for converting hydrocarbon feeds to light olefins and other hydrocarbons. The processes and apparatus include, in some embodiments, feeding a hydrocarbon, a first catalyst and a second catalyst to a reactor, wherein the first catalyst has a smaller average particle size and is less dense than the second catalyst. A first portion of the second catalyst may be recovered as a bottoms product from the reactor, and a cracked hydrocarbon effluent, a second portion of the second catalyst, and the first catalyst may be recovered as an overhead product from the reactor. The second portion of the second catalyst may be separated from the overhead product, providing a first stream comprising the first catalyst and the hydrocarbon effluent and a second stream comprising the separated second catalyst, allowing return of the separated second catalyst in the second stream to the reactor. 1. A process for the conversion of hydrocarbons , comprising:feeding a first particle and a second particle to a reactor, wherein the first particle has a smaller average particle size and/or is less dense than the second particle, and wherein the first particle and second particle may independently be catalytic or non-catalytic particles;feeding a hydrocarbon feedstock to the reactor;recovering an overhead product from the reactor comprising a converted hydrocarbon effluent, the second particle, and the first particle;separating the second particle from the overhead product to provide a first stream comprising the first particle and the converted hydrocarbon effluent and a second stream comprising the separated second particle;returning the separated second particle in the second stream to the reactor.2. The process of claim 1 , further comprising recovering a bottoms product from the reactor comprising the second particle.3. The process of claim 1 , further comprising:feeding a second hydrocarbon feedstock and a mixture of first particle and second particle ...

Catalyst Regenerator and a Riser Terminator Used Therein

A catalyst regenerator for combusting carbonaceous deposits from a catalyst comprising a first chamber which comprises a catalyst inlet for feeding spent catalyst with carbonaceous deposits to said first chamber, a supplemental fuel gas distributor, and a distributor for an oxygen containing gas for distributing oxygen containing gas into said first chamber to contact said spent catalyst and combust carbonaceous deposits and supplemental fuel which further deactivates the spent catalyst and generates flue gas; a riser section extending from said first chamber for transporting the spent catalyst and the flue gas, the riser section comprising an outer wall, at least one slot in the outer wall, and a riser termination device which comprises a substantially internally flat cover plate, at least one arm extending from the cover plate, wherein the arm extends about the slot from the outer wall, the arm comprising an outer shell that encloses the arm and wherein no internal portion of the cover plate extends above an upper surface of the outer shell of the at least one arm is provided. Further provided is a riser termination device. 1. A catalyst regenerator for combusting carbonaceous deposits from a catalyst comprising: a catalyst inlet for feeding spent catalyst with carbonaceous deposits to said first chamber,', 'a supplemental fuel gas distributor, and', 'a distributor for an oxygen containing gas for distributing oxygen containing gas into said first chamber to contact said spent catalyst and combust carbonaceous deposits and supplemental fuel which further deactivates the spent catalyst and generates flue gas;, 'a first chamber which comprises'}a riser section extending from said first chamber for transporting the spent catalyst and the flue gas, the riser section comprising an outer wall, at least one slot in the outer wall, and a riser termination device which comprises a substantially internally flat cover plate, at least one arm extending from the cover plate, ...

PROCESS FOR THE POLYMERIZATION OF OLEFINS

The present invention relates to a process for the continuous preparation of a polyolefm in a reactor from one or more α-olefm monomers of which at least one is ethylene or propylene, wherein the reactor comprises a fluidized bed, an expanded section located at or near the top of the reactor, a distribution plate located at the lower part of the reactor and an inlet for a recycle stream located under the distribution plate, wherein the process comprises—feeding a polymerization catalyst to the fluidized bed in the area above the distribution plate—feeding the one or more α-olefm monomers to the reactor—with-drawing the polyolefm from the reactor—circulating fluids from the top of the reactor to the bottom of the reactor, wherein the circulating fluids are cooled using a heat exchanger, resulting in a cooled recycle stream comprising liquid, and wherein the cooled recycle stream is introduced into the reactor using the inlet for the recycle stream wherein a stream comprising a thermal run away reducing agent (TRRA-containing stream) is introduced into the expanded section during at least part of the polymerization process, wherein said TRRA-containing stream is brought into contact with at least part of the interior surface of the expanded section. 1. A process for the continuous preparation of a polyolefin in a reactor from one or more α-olefin monomers of which at least one is ethylene or propylene ,wherein the reactor comprises a fluidized bed, an expanded section located at or near the top of the reactor, a distribution plate located at the lower part of the reactor and an inlet for a recycle stream located under the distribution plate feeding a polymerization catalyst to the fluidized bed in the area above the distribution plate', 'feeding the one or more α-olefin monomers to the reactor', 'withdrawing the polyolefin from the reactor', 'circulating fluids from the top of the reactor to the bottom of the reactor, wherein the circulating fluids are cooled using a ...

SEPARATION DEVICE FOR USE IN FLUIDIZED BED REACTOR, REACTION REGENERATION APPARATUS AND PROCESS FOR PREPARING OLEFINS, AND PROCESS FOR PREPARING AROMATIC HYDROCARBONS

Device for use in a fluidized bed reactor includes a gas-solid separator communicated with an outlet of the fluidized bed reactor; a vertically arranged damper, a solid outlet of the gas-solid separator communicated with a lower region of the damper, a gas outlet of the gas-solid separator communicated with an upper region of the damper; a fine gas-solid separator, an inlet of the fine gas-solid separator communicated with the upper region of the damper, and a solid outlet of the fine gas-solid separator communicated with the lower region of the damper. Product from the fluidized bed reactor is fed into the preliminary gas-solid separator, most solid catalysts separated and fed into the lower region; the product entraining the rest catalysts is fed into the upper region, and into the fine gas-solid separator, the rest catalysts fed into the lower region; and final product is obtained from the fine gas-solid separator. 1. A separation device for use in a fluidized bed reactor , comprisinga preliminary gas-solid separator communicated with an outlet of the fluidized bed reactor,a vertically arranged damper, a solid outlet of the preliminary gas-solid separator being communicated with a lower region of the damper, and a gas outlet of the preliminary gas-solid separator being communicated with an upper region of the damper, anda fine gas-solid separator, an inlet of the fine gas-solid separator being communicated with the upper region of the damper, and a solid outlet of the fine gas-solid separator being communicated with the lower region of the damper, whereinthe separation device is configured so that product having catalysts entrained therein from the fluidized bed reactor is fed into the preliminary gas-solid separator, most solid catalysts being separated and fed into the lower region of the damper; the product entraining the rest catalysts is fed into the upper region of the damper, and into the fine gas-solid separator, the rest catalysts being separated and fed ...

CATALYTIC CRACKING PROCESS FOR THE TREATMENT OF A FRACTION HAVING A LOW CONRADSON CARBON RESIDUE

Process for the fluidized-bed catalytic cracking of a weakly coking feedstock having a Conradson carbon residue equal to or less than 0.1% by weight and a hydrogen content equal to or greater than 12.7% by weight, comprising at least a step of cracking the feedstock, a step of separating/stripping the effluents from the coked catalyst particles and a step of regenerating said particles, the process being characterized in that at least one coking, carbonaceous and/or hydrocarbonaceous effluent having a content of aromatic compounds of greater than 50% by weight, comprising more than 20% by weight of polyaromatic compounds, is recycled to homogeneously distributed and weakly coked catalyst, before regeneration, in order to adjust the delta coke of the process. 112.-. (canceled)13. Plant for implementing a process for fluidized bed catalytic cracking , comprising at least a main reactor and optionally at least a secondary reactor , at least a disengager and a stripper , and a single-stage or multistage regenerator , characterized in that the stripper contains , level with a dense catalyst bed , at least one zone equipped with at least one structured packing element positioned upstream of a device for dispersing a coking fraction with respect to circulation of a stream of catalyst particles , wherein said structured packing element(s) are formed by interlacing plates , strips or fins constituting a screen , said screen occupying less than 10% of the area of flow cross section in a vessel in which it is placed , but covering , in projection on said section , the entire area thereof.14. Plant according to claim 13 , characterized in that the stripper contains at least two zones equipped with at least one structured packing element that are associated with two fluid-dispersing devices claim 13 , one for dispersing coking fractions claim 13 , the other for dispersing stripping fluid claim 13 , these devices being located downstream of said structured packing elements ...

FLUIDIZED BED REACTOR, REACTION REGENERATION APPARATUS, PROCESS FOR PREPARING OLEFINS, AND PROCESS FOR PREPARING AROMATIC HYDROCARBONS

A fluidized bed reactor is provided, comprising an inlet zone at a lower position, an outlet zone at an upper position, and a reaction zone between the inlet zone and the outlet zone. A guide plate with through holes is disposed in the reaction zone, comprising a dense channel region in an intermediate region thereof and a sparse channel region disposed on a periphery thereof and encompassing the dense channel region. Catalysts in said fluidized bed reactor can be homogeneously distributed in the reaction zone thereof, whereby the reaction efficiency can be improved. A reaction regeneration apparatus comprising said fluidized bed reactor, and a process for preparing olefins from oxygenates and a process for preparing aromatic hydrocarbons from oxygenates using the reaction regeneration apparatus. 1. A fluidized bed reactor , comprising an inlet zone at a lower position , an outlet zone at an upper position , and a reaction zone between the inlet zone and the outlet zone , whereina guide plate is disposed in the reaction zone, comprising a dense channel region in an intermediate region thereof and a sparse channel region disposed on a periphery thereof encompassing the dense channel region.2. The fluidized bed reactor according to claim 1 , wherein a dimension of a channel in the dense channel region is smaller than that of a channel in the sparse channel region.3. The fluidized bed reactor according to claim 2 , wherein a ratio of the dimension of the channel in the dense channel region to that of the channel in the sparse channel region is in a range of 1:4 to 2:3.4. The fluidized bed reactor according to claim 3 , wherein the dimension of the channel in the dense channel region is in a range of 0.01 m to 0.08 m.5. The fluidized bed reactor according to claim 1 , wherein the dense channel region and the sparse channel region each comprise a circular plate having evenly distributed pores claim 1 , or a plurality of concentric ring shaped sloping panels spaced apart ...

SLURRY PHASE APPARATUS

A method of operating a slurry phase apparatus includes feeding one or more gaseous reactants into a slurry body of solid particulate material suspended in a suspension liquid contained inside a vessel. The one or more gaseous reactants are fed into the slurry body through a gas distributor having downward facing gas outlets and are fed towards a fluid impermeable partition spanning across the vessel below the gas distributor. The partition divides the vessel into a slurry volume above the partition and a bottom volume below the partition. A differential pressure is maintained over the partition between predefined limits by manipulating or allowing changes in the pressure in the bottom volume by employing a pressure transfer passage establishing flow or pressure communication between the bottom volume and a head space above the slurry body. 19-. (canceled)10. A slurry phase apparatus which includesa slurry vessel to hold a slurry body comprising a liquid and solid particulate material with a head space volume above the slurry body;a gas distributor in a lower portion of the vessel which defines downwards facing gas outlets;a fluid impermeable partition spanning across the slurry vessel below the gas distributor partitioning the vessel into a slurry volume above the partition and a bottom volume below the partition; anda pressure transfer passage or conduit passing through or around the partition allowing transfer of pressure into and from the bottom volume, the pressure transfer passage in use establishing flow or pressure communication between the bottom volume and the head space volume in the slurry vessel above the slurry volume thereby to maintain a differential pressure over the partition between predefined limits by manipulating or allowing changes in the pressure in the bottom volume.11. The apparatus according to claim 10 , in which the fluid impermeable partition is planar or flat and arranged perpendicular to a longitudinal vertical central axis of the ...

APPARATUSES FOR DEHYDROGENATION OF ALKANES

The present disclosure relates to circulating fluidized bed apparatuses for dehydrogenation of alkanes to alkenes with higher yield and selectivity. The apparatus includes a riser-type reactor, a separator section, a regenerator and a withdrawal well disposed downstream to the regenerator. The apparatus includes a transfer line to receive hot regenerated catalyst free of oxygen from the withdrawal well, and to pre-treat the catalyst with a reducing gas to regulate-oxidation state of metals on the catalyst before reintroducing the catalyst to the riser-type reactor. The transfer line is formed in an elongated U-shaped pipe such that the oxidation state of the metals on the catalyst is regulated by the time the pre-treated catalyst reaches the bottom of the riser-type reactor. 1. A circulating fluidized bed apparatus for dehydrogenation of alkanes comprising a riser-type reactor , a separator coupled to the riser-type reactor , a regenerator coupled to the separator and a withdrawal well disposed downstream to the regenerator , and a transfer line connecting the withdrawal well with the riser-type reactor , the transfer line adapted to:receive hot regenerated catalyst free of oxygen from the withdrawal well; andpre-treat the catalyst with a reducing gas to regulate the oxidation state of metals on the catalyst before reintroducing the catalyst to the bottom of the riser-type reactor, wherein the transfer line is formed in an elongated U-shaped pipe such that the oxidation state of the metals on the catalyst is regulated by the time the catalyst reaches the bottom of the riser-type reactor.2. The circulating fluidized bed apparatus as claimed in claim 1 , wherein the riser-type reactor is adapted to accommodate a pre-heated alkane feed stream and a catalyst for dehydrogenation reaction.3. The circulating fluidized bed apparatus as claimed in claim 1 , wherein the separator comprising:a riser termination device for disengaging the catalyst and hydrocarbons;a set of ...

REACTION-REGENERATION DEVICE AND PROCESS FOR ALKANE DEHYDROGENATION TO ALKENE

A reaction-regeneration device for catalytic dehydrogenation or/and catalytic cracking of alkanes comprises a reaction device and a regeneration device. The reaction device comprises a reactor and a disengager, and the disengager is located at an upper part of the reactor. The reactor comprises a tapering section, and diameters of cross sections of the tapering section gradually decrease from bottom to top. Secondary conversion of alkenes caused by back-mixing is reduced, and thus the yield and selectivity to alkenes are increased. 1. A catalyst regeneration device , comprisinga regenerator for accommodating a catalyst and a regeneration disengager,wherein diameters of cross sections of the regenerator are decreased from top to bottom, anda circular pipe sleeve is arranged at a lower position inside the regenerator.2. The catalyst regeneration device according to claim 1 , wherein the circular pipe sleeve is parallel to an axis of the regenerator.3. The catalyst regeneration device according to claim 1 , wherein the circular pipe sleeve is coaxial with the regenerator.4. The catalyst regeneration device according to claim 1 , wherein a height of the circular pipe sleeve in the regenerator is less than two thirds of a height of a catalyst dense-phase bed layer.5. The catalyst regeneration device according to claim 1 , wherein a height of the circular pipe sleeve in the regenerator is less than one third of a height of a catalyst dense-phase bed layer.6. The catalyst regeneration device according to claim 1 , wherein claim 1 , fuel and air are directly fed into the circular pipe sleeve.7. A regeneration method for alkane dehydrogenation catalyst claim 1 , comprising the following step:spent catalyst entering a regeneration disengager, and fuel and air entering a regenerator from a lower part or bottom of the regenerator;gas moving upwards in the regenerator, a linear speed of the gas gradually decreasing from bottom to top, and, the spent catalyst moving upwards at a ...

FLUIDIZED BED DEVICE AND METHOD FOR PREPARING PARA-XYLENE AND CO-PRODUCING LIGHT OLEFINS FROM METHANOL AND/OR DIMETHYL ETHER AND TOLUENE

A turbulent fluidized bed reactor, device and method for preparing para-xylene and co-producing light olefins from methanol and/or dimethyl ether and toluene, resolving or improving the competition problem between an MTO reaction and an alkylation reaction during the process of producing para-xylene and co-producing light olefins from methanol and/or dimethyl ether and toluene, and achieving a synergistic effect between the MTO reaction and the alkylation reaction. By controlling the mass transfer and reaction, competition between the MTO reaction and the alkylation reaction is coordinated and optimized to facilitate a synergistic effect of the two reactions, so that the conversion rate of toluene, the yield of para-xylene, and the selectivity of light olefins are increased. The turbulent fluidized bed reactor includes a first reactor feed distributor and a number of second reactor feed distributors and are arranged sequentially along the gas flow direction. 126-. (canceled)27. A turbulent fluidized bed reactor for preparing para-xylene and co-producing light olefins from methanol and/or dimethyl ether and toluene , the turbulent fluidized bed reactor comprising: a first reactor feed distributor and a plurality of second reactor feed distributors , the first reactor feed distributor and the plurality of second reactor feed distributors are sequentially arranged along the gas flow direction in the turbulent fluidized bed reactor;the feed to the first reactor feed distributor comprises toluene and a portion of methanol and/or dimethyl ether;the feed to the second reactor feed distributor comprises methanol and/or dimethyl ether; andthe number of the second reactor feed distributors is in a range from 2 to 10.28. The turbulent fluidized bed reactor of claim 27 , the turbulent fluidized bed reactor further comprising a first reactor gas-solid separator and a second reactor gas-solid separator claim 27 , the first reactor gas-solid separator is placed in a dilute phase ...

Fluidized Catalyst Stripping Unit for Displacing Entrained Gas From Catalyst Particles

A fluidized catalyst stripping unit for displacing entrained gas from catalyst particles comprising: a vessel housing a two stage cyclonic separation section which comprises one or more primary cyclonic separation devices and one or more secondary cyclones; a stripping section which comprises internals; and an inlet in fluid communication with a catalytic reactor to feed a particulate-fluid suspension to the two stage cyclonic separation section; wherein each primary cyclonic separation device comprises an internal cylindrical surface to separate a major fraction of the particulates from the suspension and form a vortex of reduced particulate content; a particulate discharge outlet from each secondary cyclone to the stripping section; wherein the particulate discharge outlet of the secondary cyclone is submerged in a catalyst bed located above the stripper internals, and wherein the stripping section comprises one or more bubble breaking grids within the catalyst bed and above the stripping internals is provided. 1. A fluidized catalyst stripping unit for displacing entrained gas from catalyst particles comprising: a two stage cyclonic separation section which comprises one or more primary cyclonic separation devices and one or more secondary cyclones;', 'a stripping section which comprises internals and one or more bubble breaking grids supported by a hinged support system;', 'an inlet in fluid communication with a catalytic reactor to feed a particulate-fluid suspension to the two stage cyclonic separation section; and', 'a particulate discharge outlet from each secondary cyclone to the stripping section;, 'a vessel which houses'} each primary cyclonic separation device comprises an internal cylindrical surface to separate a major fraction of the particulates from the suspension and form a vortex of reduced particulate content;', 'the particulate discharge outlet of the secondary cyclone is submerged in a catalyst bed which is located above the stripper internals ...

METHOD AND APPARATUS FOR POLYMERISING OLEFINS IN GAS PHASE

The present invention deals with an olefin polymerisation process. At least one olefin is polymerised in gas phase in a fluidised bed in the presence of an olefin polymerisation catalyst in a polymerisation reactor having a vertical body; a generally conical downwards tapering bottom zone; a generally cylindrical middle zone above and connected to said bottom zone; and a generally conical upwards tapering top zone above and connected to said middle zone. Fluidisation gas is introduced to the bottom zone of the reactor from where it passes upwards through the reactor, and withdrawn from the top zone of the reactor. The gas is then compressed, cooled and returned into the bottom zone of the reactor. A fluidised bed is thus formed within the reactor where the growing polymer particles are suspended in the upwards rising gas stream wherein the superficial velocity of the fluidisation gas is less than the transport velocity of the particles. There is no fluidisation grid in the reactor. The fluidisation gas is passed from an inlet chamber into the bottom zone and the gas flows from the upper part of the inlet chamber to the lower part thereof and the gas flows from the lower part of the inlet chamber to the bottom zone. 1. An olefin polymerisation process comprising polymerising at least one olefin in gas phase in a fluidised bed in the presence of an olefin polymerisation catalyst in a polymerisation reactor having a vertical body; a generally conical downwards tapering bottom zone; a generally cylindrical middle zone above and connected to said bottom zone; and a generally conical upwards tapering top zone above and connected to said middle zone wherein (i) fluidisation gas is introduced to the bottom zone of the reactor from where it passes upwards through the reactor; (ii) the fluidisation gas is withdrawn from the top zone of the reactor , compressed , cooled and returned into the bottom zone of the reactor; (iii) a fluidised bed is formed within the reactor where ...

PROCESS AND APPARATUS FOR INDIRECT CATALYST HEATING IN A REGENERATOR

A process and apparatus for heating catalyst is presented. Cooler catalyst is removed from a reactor and heated with a hot gas in a riser, heated in a heating tube or heated in a heating chamber. Heated catalyst is disengaged from the hot gas if necessary and returned to the reactor. The process and apparatus can be used for producing light olefins. The hot gas may be a flue gas from an FCC regenerator or a combustion gas from a heater. 1. A reactor apparatus comprising:a reactor vessel comprising a feed inlet, a catalyst inlet to the reactor vessel and a catalyst outlet in the reactor vessel;a catalyst outlet conduit in direct communication with the catalyst outlet;a heating tube in downstream communication with said catalyst outlet conduit, said heating tube positioned in a catalyst regenerator; and the catalyst inlet in downstream communication with said heating tube.2. The reactor apparatus of wherein said catalyst inlet to the reactor vessel is above the catalyst outlet.3. The reactor apparatus of further comprising a riser in communication with said heating tube.4. The reactor apparatus of wherein said riser is in direct claim 3 , downstream communication with said catalyst outlet conduit and said heating tube is downstream communication with said riser.5. The reactor apparatus of wherein said heating tube is in direct downstream communication with said catalyst outlet conduit and said riser is in downstream communication with said heating tube.6. The reactor apparatus of further comprising a disengager at a top end of said riser for disengaging hot gas from said catalyst stream.7. The reactor apparatus of wherein said regenerator has two chambers and said heating tube is in said upper chamber or said lower chamber.8. The reactor apparatus of wherein said heating tube is positioned within the wall of the regenerator.9. The reactor apparatus of wherein said heating tube comprises a coil that winds around the interior of the regenerator.10. A reactor apparatus ...

PROCESS AND APPARATUS WITH CATALYST HEATING IN A RISER

A process and apparatus for heating catalyst is presented. Cooler catalyst is removed from a reactor and heated with a hot gas in a riser, heated in a heating tube or heated in a heating chamber. Heated catalyst is disengaged from the hot gas if necessary and returned to the reactor. The process and apparatus can be used for producing light olefins. The hot gas may be a flue gas from an FCC regenerator or a combustion gas from a heater. 1. A process for heating a catalyst bed to promote a reaction comprising:passing a hydrocarbon feed stream to a reactor vessel to react over a catalyst bed in the reactor vessel and produce a product gas;withdrawing said product gas stream from the reactor vessel;withdrawing a catalyst stream from the reactor vessel;passing the catalyst stream from the reactor up a riser;heating the catalyst stream with a hot gas stream in the riser; andpassing the heated catalyst stream to the reactor vessel.2. The process of wherein said product gas stream and said catalyst stream are withdrawn from the reactor vessel separately.3. The process of wherein the catalyst stream is withdrawn from a lower section of the reactor vessel.4. The process of further comprising disengaging a heated catalyst stream from the hot gas stream.5. The process of wherein the hot gas stream is a flue gas stream from an FCC regenerator.6. The process of wherein the flue gas stream is filtered before it heats the catalyst stream.7. The process of further comprising adding one or more of nitrogen claim 5 , steam claim 5 , air claim 5 , fuel oil or paraffins to the flue gas stream.8. The process of wherein the hydrocarbon feed stream is derived from a product of an FCC reactor in communication with the FCC regenerator.9. The process of wherein the hot gas stream comprises one or more of nitrogen claim 1 , steam claim 1 , air claim 1 , fuel oil claim 1 , paraffins or combustion gas.10. The process of wherein the hot gas stream propels the catalyst stream up the riser.11. The ...

METHODS FOR CATALYTIC REFORMING OF HYDROCARBONS INCLUDING REGENERATION OF CATALYST AND APPARATUSES FOR THE SAME

Embodiments of methods and apparatuses for catalytic reforming of hydrocarbons including regeneration of catalyst are provided. In one example, a method comprises heating an inert gas to form a heated inert gas stream. A first portion of the heated inert gas stream is indirect heat exchanged with hydrogen gas to form a first partially heated inert gas stream and a heated hydrogen gas stream that is for lifting the catalyst; and/or a second portion of the heated inert gas stream is indirect heat exchanged with an organic chloride-containing stream to form a second partially heated inert gas stream and a heated organic chloride-containing stream that is for chlorinating the catalyst; and/or the catalyst is preheated using at least a third portion of the heated inert gas stream for indirect heat exchange with a nitrogen gas stream or using the first and/or second partially heated inert gas streams. 1. A method for catalytic reforming of hydrocarbons including regeneration of a catalyst , the method comprising the steps of:heating an inert gas to form a heated inert gas stream;indirect heat exchanging at least a first portion of the heated inert gas stream with hydrogen gas to form a first partially heated inert gas stream and a heated hydrogen gas stream that is for lifting the catalyst; and/orindirect heat exchanging at least a second portion of the heated inert gas stream with an organic chloride-containing stream to form a second partially heated inert gas stream and a heated organic chloride-containing stream that is for chlorinating the catalyst; and/orpreheating the catalyst using at least a third portion of the heated inert gas stream for indirect heat exchange with a nitrogen gas stream that is in fluid communication with the catalyst or using the first and/or second partially heated inert gas streams for direct heat exchange with the catalyst.2. The method of claim 1 , further comprising the step of:combusting coke disposed on the catalyst in the presence of ...

Continuous production of titanium tetrachloride from titanium-bearing slags

This disclosure relates to an improved method to produce titanium tetrachloride continuously from titanium-bearing materials containing high concentrations of alkaline earth metal impurities through fluidized-bed carbochlorination. Agglomerated heavy particles in a reaction are taken out continuously from a chlorination reactor without clogging and stopping. The reactors and related methods disclosed apply to the chlorination of titanium slag containing high content of alkaline earth metal oxides of up to 15% by weight.

FLUID CATALYTIC CRACKING PROCESS AND APPARATUS FOR MAXIMIZING LIGHT OLEFIN YIELD AND OTHER APPLICATIONS

Apparatus and processes herein provide for converting hydrocarbon feeds to light olefins and other hydrocarbons. The processes and apparatus include, in some embodiments, feeding a hydrocarbon, a first catalyst and a second catalyst to a reactor, wherein the first catalyst has a smaller average particle size and is less dense than the second catalyst. A first portion of the second catalyst may be recovered as a bottoms product from the reactor, and a cracked hydrocarbon effluent, a second portion of the second catalyst, and the first catalyst may be recovered as an overhead product from the reactor. The second portion of the second catalyst may be separated from the overhead product, providing a first stream comprising the first catalyst and the hydrocarbon effluent and a second stream comprising the separated second catalyst, allowing return of the separated second catalyst in the second stream to the reactor. 143.-. (canceled)44. (canceled)45. (canceled)46. (canceled)47. (canceled)48. (canceled)49. (canceled)50. (canceled)51. (canceled)52. (canceled)53. A process for the conversion of hydrocarbons , comprising:regenerating a catalyst mixture comprising a first catalyst and a second particle in a regenerator, wherein the first catalyst has a smaller average particle size and/or is less dense than the second particle, and wherein the second particle may be catalytic or non-catalytic;feeding the catalyst mixture and hydrocarbons to a riser reactor to convert at least a portion of the hydrocarbons and recover a first effluent comprising the catalyst mixture and converted hydrocarbons;feeding the catalyst mixture to a second reactor;feeding a hydrocarbon feedstock to the second reactor and fluidizing the catalyst mixture;recovering an overhead product from the second reactor comprising the second particle, the first catalyst, and a reacted hydrocarbon product;separating the second particle from the overhead product to provide a first stream comprising the first ...

PROCESS FOR GAS-PHASE POLYMERIZATION OF OLEFINS

A process for the polymerization of olefins in gas phase carried out in a reactor having two interconnected polymerization zones, a first zone (riser) and a second zone (downcomer), wherein growing polymer particles: 2. The process according to claim 1 , wherein an amount of liquid is present in the whole riser.3. The process according to claim 1 , wherein no liquid is present above 75% of the height of the riser.4. The process according to claim 1 , wherein no liquid is present above 50% of the height of the riser.5. The process according to claim 1 , wherein the pressure of operation of the reactor is between 5 and 40 bar g.6. The process according to claim 1 , wherein the temperature of operation of the reactor is between 40 and 120° C.7. The process according to claim 1 , wherein the two interconnected polymerization zones are operated such that the fluid mixture coming from the riser is totally or partially prevented from entering the downcomer by introducing into the upper part of the downcomer a liquid and/or stream claim 1 , denominated “barrier stream” claim 1 , having a composition different from the fluid mixture present in the riser.8. The process according to claim 7 , wherein one or more feeding lines for the barrier stream are placed in the downcomer close to the upper limit of the volume occupied by the polymer particles flowing downward in a densified form.9. The process according to claim 6 , wherein the barrier stream comprises propane.10. The process according to claim 9 , wherein the barrier steam comprises:i. from 10 to 100% by mol of propylene, based upon the total moles in the barrier stream;ii. from 0 to 80% by mol of ethylene, based upon the total moles in the barrier stream;iii. from 0 to 30% by mol of propane, based upon the total moles in the barrier stream; andiv. from 0 to 5% by mol of hydrogen, based upon the total moles in the barrier stream.11. The process according to claim 10 , wherein the composition of the barrier stream derives ...

PARTICLE DISENGAGEMENT DEVICE

A particle disengagements device comprising a baffle plate, wherein the baffle plate comprises one or more guide baffles and one or more separation baffles, wherein the one or more guide baffles and the one or more separation baffles define one or more air flow paths and one or more solid flow paths and associated systems and methods. 1. A vessel comprising:a fluidized bed;one or more cyclones; and a circular baffle plate,', 'wherein the baffle plate comprises one or more guide baffles and one or more separation baffles,', 'wherein the one or more guide baffles and the one or more separation baffles define one or more air flow paths and one or more solid flow paths;', 'wherein the one or more guide baffles and the one or more separation baffles each comprise a protrusion having a length in the range of from 0.1 to 8 inches;', 'wherein the one or more guide baffles are spaced apart a distance in the range of from 4 inches to 25 inches; and', 'wherein the one or more separation baffles are spaced apart a distance in the range of from 4 inches to 25 inches., 'a particle disengagement device comprising'}2. The vessel of claim 1 , wherein the one or more cyclones comprise one or more primary cyclones and one or more secondary cyclones.3. The vessel of claim 2 , wherein the one or more cyclones comprise one or more diplegs.4. The vessel of claim 3 , wherein the one or more diplegs extend through the particle disengagement device.5. A method comprising:providing a vessel, wherein the vessel comprises fluidized bed, one or more cyclones, and a particle disengagement device, wherein the particle disengagement device is disposed within the vessel at an elevation above the fluidized bed and below a portion of the one or more cyclones; andintroducing a gas/solid feed into the vessel.6. The method of claim 5 , further comprising removing solids from the gas/solid feed. This application is a divisional of U.S. PCT application Ser. No. 15/776657, filed Nov. 22, 2016, which claims ...

Process and apparatus for quenching a reactor effluent stream

A process and apparatus cool and remove catalyst from a hot vaporous reactor effluent stream by feeding the hot vaporous reactor effluent stream comprising catalyst and a first quench liquid stream to a first quench chamber. The hot vaporous reactor effluent stream is directly contacted with the first quench liquid stream to cool the hot reactor effluent stream and wash catalyst therefrom into the first quench liquid stream. The first quench liquid stream and the vaporous reactor effluent stream are passed together through a bed while disengaging catalyst from the vaporous reactor effluent stream and transferring catalyst into the first quench liquid stream.

Process for continuous polymerization of olefin monomers in a reactor

The invention relates to a process and system for the continuous polymerization of one or more α-olefin monomers comprising the steps of: (a) withdrawing fluids from a reactor (b) cooling fluids comprising the withdrawn fluids with a cooling unit (c) introducing the cooled fluids to a separator to separate at least part of the liquid from these fluids to form a liquid phase and a gas/liquid phase (d) introducing the gas/liquid phase below to the reactor below a distribution plate (e) introducing the liquid phase to a settling tank to separate liquid from fines that settle down in the settling tank (f) introducing liquid from the settling tank up stream of the cooling unit.

PROCESS AND APPARATUS FOR CRACKING HYDROCARBONS WITH RECYCLED CATALYST TO PRODUCE ADDITIONAL DISTILLATE

A process and apparatus is for recycling LCO and/or HCO to an FCC unit to recover additional distillate. Spent catalyst recycle in the FCC unit may be used to improve distillate yield. A hydroprocessing zone may saturate cycle oil aromatics for cracking in an FCC unit. The recycle cracked stream may be recycled to a downstream hydroprocessing zone to avoid a first hydroprocessing zone for hydrotreating feed to the FCC unit. Additional recovery of cycle oil for recycle is obtained by heating slurry oil prior to vacuum separation. 1. An apparatus for catalytically cracking hydrocarbons comprising:a hydroprocessing unit to hydroprocess a hydrocarbon feed stream to provide a hydroprocessed effluent stream;a hydroprocessing separation section in downstream communication with said hydroprocessing unit for separating hydroprocessed products to provide an FCC feed stream;FCC reactor in downstream communication with said hydroprocessing separation section for contacting said FCC feed stream with catalyst in a riser to catalytically crack said FCC feed stream to provide a cracked stream and spent catalyst;a regenerator in downstream communication with said riser outlet for regenerating said spent catalyst; anda recycle conduit in downstream communication with said riser outlet for recycling said spent catalyst to said FCC riser.2. The apparatus of further comprising a riser inlet in downstream communication with said recycle conduit.3. The apparatus of wherein said recycle conduit is connected to said FCC riser.4. The apparatus of further comprising a regenerator conduit in downstream communication with said regenerator and said riser having an inlet in downstream communication with said regenerator conduit.5. The apparatus of wherein said regenerator conduit is connected to said FCC riser.6. The apparatus of further comprising a disengaging chamber containing said riser outlet claim 4 , said recycle conduit and said regenerator conduit in downstream communication with said ...

FLUIDIZED BED REACTION SYSTEM AND METHOD OF PRODUCING TITANIUM TETRACHLORIDE

This disclosure relates to a fluidized bed reaction system and method for continuous production of titanium tetrachloride from titanium-bearing materials containing high concentrations of alkaline earth metal impurities. Agglomerated heavy particles in a reaction are taken out continuously from a chlorination reactor without clogging and stopping. The reactors and related methods disclosed apply to the chlorination of titanium slag containing high content of alkaline earth metal oxides of up to 15% by weight. 1. A fluidized bed reaction system comprising:a reaction vessel lined with a refractory material configured for running an exothermic reaction therein;a baseplate providing a base for the reaction vessel and comprising a first surface, a second surface lower than the first surface, and a side surface interconnecting between the first and second surfaces, the side surface comprising a portion that is not parallel to either of the first and second surfaces;a collection zone comprising a space under a level of the first surface and defined by the second surface and the side surface for collecting agglomerated particles from the reaction while running the reaction in the reaction vessel;a reaction zone comprising a space above the collection zone and further above the first surface, in which the reaction is occurring primarily within the reaction vessel;a plurality of first nozzles formed through the first surface of the baseplate and configured for supplying fluidizing gas directly into the reaction zone;a plurality of second nozzles formed through the second surface and configured for supplying fluidizing gas into the reaction zone via the collection zone; anda gas flow control configured for controlling flow of the fluidizing gas to the plurality of first nozzles and to the plurality of second nozzles such that a linear fluidizing velocity of the fluidizing gas supplied through the plurality of second nozzles is substantially lower than a linear fluidizing ...

FLUIDIZED CATALYST STRIPPING UNIT FOR DISPLACING ENTRAINED GAS FROM CATALYST PARTICLES

A fluidized catalyst stripping unit for displacing entrained gas from catalyst particles comprising: a vessel housing a two stage cyclonic separation section which comprises one or more primary cyclonic separation devices and one or more secondary cyclones; a stripping section which comprises internals; and an inlet in fluid communication with a catalytic reactor to feed a particulate-fluid suspension to the two stage cyclonic separation section; wherein each primary cyclonic separation device comprises an internal cylindrical surface to separate a major fraction of the particulates from the suspension and form a vortex of reduced particulate content; a particulate discharge outlet from each secondary cyclone to the stripping section; wherein the particulate discharge outlet of the secondary cyclone is submerged in a catalyst bed located above the stripper internals, and wherein the stripping section comprises one or more bubble breaking grids within the catalyst bed and above the stripping internals is provided. 1. A fluidized catalyst stripping unit for displacing entrained gas from catalyst particles comprising: a two stage cyclonic separation section comprising one or more primary cyclonic separation devices and one or more secondary cyclones;', 'a stripping section comprising internals and one or more bubble breaking grids;', 'a particulate discharge outlet from each secondary cyclone to the stripping section; and', 'an inlet in fluid communication with a catalytic reactor to feed a particulate-fluid suspension to the two stage cyclonic separation section;', 'wherein:', 'each primary cyclonic separation device comprises an internal cylindrical surface to separate a major fraction of the particulates from the suspension and form a vortex of reduced particulate content;', 'the particulate discharge outlet of the secondary cyclone is submerged in a catalyst bed which is located above the stripper internals within the stripping section, and', 'the one or more ...

TURBULENT FLUIDIZED-BED REACTOR, DEVICE, AND METHOD USING OXYGEN-CONTAINING COMPOUND FOR MANUFACTURING PROPENE AND C4 HYDROCARBON

A turbulent fluidized-bed reactor, device and method for preparing propylene and C4 hydrocarbons from oxygen-containing compounds. The device includes the turbulent fluidized-bed reactor and a fluidized-bed regenerator for regenerating a catalyst. The method includes: a) feeding a raw material containing the oxygen-containing compounds from n reactor feed distributors to a reaction zone of the turbulent fluidized-bed reactor, and contacting the raw material with a catalyst, to generate a stream containing target product and a spent catalyst containing carbon; b) sending the stream discharged into a product separation system, obtaining propylene, C4 hydrocarbons, light fractions and the like after separation, returning 70 wt. % or more of the light fractions to the reaction zone of the turbulent fluidized-bed reactor from the reactor feed distributor, and reacting ethylene and the oxygen-containing compounds to perform an alkylation reaction in presence of the catalyst, to produce products of propylene and the like. 115-. (canceled)16. A turbulent fluidized-bed reactor for preparing propylene and C4 hydrocarbons from oxygen-containing compounds , comprising:a reactor shell, one or more reactor feed distributors, a first reactor gas-solid separator, a second reactor gas-solid separator, a reactor heat extractor, a product gas outlet and a reactor stripper, wherein the lower part of the turbulent fluidized-bed reactor is a reaction zone, the upper part of the turbulent fluidized-bed reactor is a settling zone, the one or more reactor feed distributors are disposed in the reaction zone, the reactor heat extractor is disposed in the reaction zone, the first reactor gas-solid separator and the second reactor gas-solid separator are placed in the settling zone or outside the reactor shell, the first reactor gas-solid separator is equipped with a regenerated catalyst inlet, the catalyst outlet of the first reactor gas-solid separator is located at the bottom of the reaction ...

A CATALYST REGENERATOR AND A RISER TERMINATOR USED THEREIN

A catalyst regenerator for combusting carbonaceous deposits from a catalyst comprising a first chamber which comprises a catalyst inlet for feeding spent catalyst with carbonaceous deposits to said first chamber, a supplemental fuel gas distributor, and a distributor for an oxygen containing gas for distributing oxygen containing gas into said first chamber to contact said spent catalyst and combust carbonaceous deposits and supplemental fuel which further deactivates the spent catalyst and generates flue gas; a riser section extending from said first chamber for transporting the spent catalyst and the flue gas, the riser section comprising an outer wall, at least one slot in the outer wall, and a riser termination device which comprises a substantially internally flat cover plate, at least one arm extending from the cover plate, wherein the arm extends about the slot from the outer wall, the arm comprising an outer shell that encloses the arm and wherein no internal portion of the cover plate extends above an upper surface of the outer shell of the at least one arm is provided. Further provided is a riser termination device. 1. A catalyst regenerator for combusting carbonaceous deposits from a catalyst comprising: a catalyst inlet, and', 'an oxygen-containing gas distributor for distributing oxygen containing gas into the first chamber to contact the spent catalyst and combust the carbonaceous deposits from the spent catalyst; and, 'a first chamber comprisinga riser section extending from the first chamber for transporting the catalyst and a flue gas, the riser section comprising an outer wall, at least one slot in the outer wall, and a riser termination device which comprises a substantially internally flat cover plate and at least one arm extending from the cover plate, wherein the arm extends about the slot from the outer wall, the arm comprising an outer shell, and wherein no internal portion of the cover plate extends above an upper surface of the outer shell ...

Apparatuses and risers for reacting feedstock in the presence of catalyst and methods for installing baffles in risers

Embodiments of apparatuses and risers for reacting a feedstock in the presence of a catalyst and methods for installing a baffle in such risers are provided. In one example, a riser comprises a sidewall that defines a cylindrical housing surrounding an interior. A plurality of baffle assemblies is releasably coupled to the sidewall and each comprises a baffle section. The baffle sections together define a segmented baffle ring extending inwardly in the interior.

NEW DEVICE FOR GAS-LIQUID SEPARATION, INTENDED FOR THREE-PHASE FLUIDISED BED REACTORS SUCH AS THOSE USED IN THE H-OIL PROCESS

A device for gas-liquid separation, intended to equip three-phase fluidized bed reactors such as those used in the H-oil process. The device has a succession of two bends situated in different planes, which device accomplishes excellent separation of the gas and of the liquid. 13930272830392728703039170) A gas-liquid separation device installed in the recycle zone of the three-phase fluidized reactors used in processes for the hydroconversion of heavy hydrocarbon fractions in the presence of hydrogen under high pressure , the recycle zone () being made up of the upper hemisphere of the reactor and delimited in its lower part by a conical surface () allowing the separated liquid to return to the catalytic zone , the device consisting in a plurality of separation elements () and () operating in parallel and installed vertically from the conical surface () of the recycle zone () , each separation element () and () having an inlet pipe () for admitting the gas-liquid mixture , open onto the conical surface () and rising to a height H inside the separation zone () , and ending in a succession of two bends: a first bend situated in the (zy) plane defined by the substantially vertical z-axis , and a y-axis belonging to the (xy) plane perpendicular to the z-axis , having its orientation defined by its angle α comprised between 45 and 315° , preferably between 60° and 300° , and , for preference , between 80° and 200° , and a second bend situated in the (x ,y) plane , the x-axis being itself perpendicular to the y-axis , having its orientation defined by its angle β comprised between 0° and 135° , preferably between 10° and 110° , and , for preference , between 30° and 100° , the two successive bends being separated by a distance D comprised between D/2 and 4D and preferably comprised between D/2 and 2D , D being the diameter of the pipe ().212470) The gas-liquid separation device as claimed in claim 1 , in which the distance H separating the outlet end of the second bend ...

REACTION-REGENERATION DEVICE AND PROCESS FOR ALKANE DEHYDROGENATION TO ALKENE

A reaction-regeneration device for catalytic dehydrogenation or/and catalytic cracking of alkanes comprises a reaction device and a regeneration device. The reaction device comprises a reactor and a disengager, and the disengager is located at an upper part of the reactor. The reactor comprises a tapering section, and diameters of cross sections of the tapering section gradually decrease from bottom to top. Secondary conversion of alkenes caused by back-mixing is reduced, and thus the yield and selectivity to alkenes are increased. 1. A reaction-regeneration device for catalytic dehydrogenation or catalytic cracking of alkanes , comprising a reaction device and a regeneration device ,the reaction device comprising a reactor and a disengager,the disengager being located above the reactor,wherein the reactor comprises a tapering section, and diameters of cross sections of the tapering section gradually decrease from bottom to top.2. The reaction-regeneration device according to claim 1 , wherein the reactor comprises a dense-phase section and a dilute-phase section claim 1 ,the dense-phase section is located below the tapering section, and the dilute-phase section is located above the tapering section.3. The reaction-regeneration device according to claim 1 , wherein a catalyst riser is arranged inside the reactor claim 1 ,a rising medium pipe is arranged in the catalyst riser, andan outlet end of a regenerated catalyst conduit is connected with the catalyst riser.4. The reaction-regeneration device according to claim 2 , wherein the catalyst riser extends into the reactor through the bottom of the reactor claim 2 , andan outlet of the catalyst riser is located below the tapering section in the reactor.5. The reaction-regeneration device according to claim 2 , wherein a height of the catalyst riser in the reactor is less than two thirds of a height of the dense-phase section.6. The reaction-regeneration device according to claim 1 , wherein the tapering section of the ...

Process and Apparatus for Minimizing Attrition of Catalyst Particles

An improved process and an improved apparatus for minimizing attrition of catalyst particles, especially propane dehydrogenation catalyst particles, entrained in a combined flow of such particles and an entraining gas in a catalyst recovery means during separation of such particles from the entraining gas, by use of a pre-treatment step in which the combined flow is at a rate between 7.6 and 15.2 meters per second are provided. 1. An improved process for minimizing attrition of catalyst particles entrained in a combined flow of such particles and an entraining gas in a catalyst recovery means during separation of such particles from the entraining gas , which process comprises causing the combined flow to contact a high velocity separation means at a gas flow velocity of 16.8 meters per second to 25.9 meters per second and thereby remove from said combined flow at least 99.8 percent of the catalyst particles , wherein the improvement comprises:{'sup': '2', 'subjecting the combined flow, having an axis of flow direction, to a pre-treatment step that precedes contact of the combined flow with the separation means at the high gas flow velocity of from 16.8 meters per second to 25.9 meters per second, the pre-treatment step occurring at a lower gas flow velocity within a range of from 7.6 meters per second to 15.2 meters per second in combination with a directional change away from the combined gas flow, which directional change is at least 90 degrees from the axis of flow direction and, which pre-treatment step combination of velocity and direction change causes removal from the combined flow greater than 80 percent of the catalyst particles such that less than 20 percent of the catalyst particles contact the high velocity separation means, the improved process providing a total catalyst attrition rate calculated in accord with the correlation r=Ku/√{square root over (μ)}, where r is attrition rate (mass of catalyst attrited per hour per mass of catalyst impacted per ...

CATALYSTS FOR SOFT OXIDATION COUPLING OF METHANE TO ETHYLENE AND ETHANE

Disclosed is a catalyst and methods for the oxidative coupling of methane (OCM) reaction using elemental sulfur as a soft oxidant. The process can provide ethylene from methane with high conversion and selectivity. 1. A method of producing an olefin from methane and elemental sulfur , the method comprising:(a) obtaining a reaction mixture comprising methane and elemental sulfur gas; and(b) contacting the reaction mixture with a catalyst under reaction conditions sufficient to produce a product stream comprising an olefin, wherein the catalyst is a metal, a mixed metal oxide, mixed metal sulfide, a metal oxysulfide, mixed metal oxysulfide, or any mixture thereof.2. The method of claim 1 , wherein the olefin comprises C+ hydrocarbons claim 1 , preferably ethylene.3. The method of claim 1 , wherein the product stream further comprises hydrogen sulfide.4. The method of claim 1 , wherein the reaction mixture comprises a methane to elemental sulfur molar ratio of 1:2 to 20:1.5. The method of claim 1 , wherein the conditions sufficient to produce a product stream in step (b) comprise a reaction temperature of at least 450° C.6. The method of claim 1 , wherein the conditions sufficient to produce a product stream comprise a reaction pressure of 0.05 to 10.0 MPa or 0.1 to 10.0 MPa claim 1 , a gas hourly space velocity (GHSV) of 500 to 100 claim 1 ,000 or both.7. The method of claim 1 , wherein the metal claim 1 , the mixed metal oxide claim 1 , the mixed metal sulfide claim 1 , the metal oxysulfide claim 1 , mixed metal oxysulfide claim 1 , or the metal sulfide comprises:an alkaline earth metal, preferably magnesium (Mg), calcium (Ca), strontium (Sr), barium (Ba), or any combination thereof;a transition metal, preferably yttrium (Y), zirconium (Zr), vanadium (V), tantalum (Ta), tungsten (W), manganese (Mn), rhenium (Rh), iron (Fe), cobalt (Co), iridium (Ir), nickel (Ni), copper (Cu), zinc (Zn), or any combination thereof;a post-transition metal, preferably aluminum (Al), ...

Process for degassing and buffering polyolefin particles obtained by olefin polymerization

Process for preparing a polyolefin polymer comprising the steps of a) forming a particulate polyolefin polymer by polymerizing one or more olefins in the presence of a polymerization catalyst system in a polymerization reactor; b) discharging the formed polyolefin particles from the polymerization reactor; c) degassing the polyolefin particles by a process comprising at least a final step of contacting the polyolefin particles with a nitrogen stream in a degassing vessel; and d) transferring the polyolefin particles from the vessel, in which the contacting of the polyolefin particles with the nitrogen stream is carried out, to a melt mixing device, in which the polyolefin particles are melted, mixed and thereafter pelletized, without passing the particles through a buffering device, wherein the degassing vessel is only partly filled with polyolefin particles and the empty volume within the degassing vessel is sufficient to take up additional polyolefin particles for at least 3 hours if the transfer of polyolefin particles of step d) from the degassing vessel to the melt mixing device is discontinued and the discharge of polyolefin particles from the polymerization reactor according to step b) is continued with unchanged rate.

FLUID CATALYTIC CRACKING PROCESS AND APPARATUS FOR MAXIMIZING LIGHT OLEFIN YIELD AND OTHER APPLICATIONS

Apparatus and processes herein provide for converting hydrocarbon feeds to light olefins and other hydrocarbons. The processes and apparatus include, in some embodiments, feeding a hydrocarbon, a first catalyst and a second catalyst to a reactor, wherein the first catalyst has a smaller average particle size and is less dense than the second catalyst. A first portion of the second catalyst may be recovered as a bottoms product from the reactor, and a cracked hydrocarbon effluent, a second portion of the second catalyst, and the first catalyst may be recovered as an overhead product from the reactor. The second portion of the second catalyst may be separated from the overhead product, providing a first stream comprising the first catalyst and the hydrocarbon effluent and a second stream comprising the separated second catalyst, allowing return of the separated second catalyst in the second stream to the reactor.

FLUIDIZED BED REACTION SYSTEM AND METHOD OF PRODUCING TITANIUM TETRACHLORIDE

This disclosure relates to a fluidized bed reaction system and method for continuous production of titanium tetrachloride from titanium-bearing materials containing high concentrations of alkaline earth metal impurities. Agglomerated heavy particles in a reaction are taken out continuously from a chlorination reactor without clogging and stopping. The reactors and related methods disclosed apply to the chlorination of titanium slag containing high content of alkaline earth metal oxides of up to 15% by weight. 1. A fluidized bed reaction system comprising:a reactor base comprising a center and a rim, wherein the center is recessed relative to the rim;at least one reactor wall defining, together with the reactor base, an enclosed space comprising a collection zone and a reaction zone, wherein the collection zone comprises a space within the recessed center of the reactor base, wherein the reaction zone comprises a space above the center and the rim of the reactor base such that the reaction zone is above the collection zone;a plurality of center nozzles formed through the recessed center of the reactor base and configured to supply fluidizing gas to the reaction zone via the collection zone;a plurality of rim nozzles formed through the rim of the reactor base and configured to supply fluidizing gas directly to the reaction zone;a gas flow control configured to control flow of the fluidizing gas to the plurality of center nozzles and to the plurality of rim nozzles such that a linear fluidizing velocity of the fluidizing gas supplied through the plurality of center nozzles is substantially lower than a linear fluidizing velocity of the fluidizing gas supplied through the plurality of rim nozzles.2. A method of producing titanium tetrachloride , the method comprising:{'sub': '2', 'introducing TiO-containing slag into a reaction zone of a reactor;'} {'br': None, 'sub': 2', '2', '4', '2, 'TiO+2Cl+C→TiCl+CO/CO,'}, 'supplying fluidizing gas comprising chlorine gas to the ...

Apparatuses and methods for cracking hydrocarbons

Methods and apparatuses are provided for cracking a hydrocarbon. The method includes contacting a first hydrocarbon stream with a first cracking catalyst at a first cracking temperature in a first riser to produce a first riser effluent and a first spent catalyst. A second hydrocarbon stream is contacted with a second cracking catalyst at a second cracking temperature in a second riser to produce a second riser effluent and a second spent catalyst, where the second cracking temperature is less than the first cracking temperature. The first riser effluent and the second riser effluent are combined to produce a mixed riser effluent, and the mixed riser effluent is fractionated in a fractionation zone to produce a light cycle oil. The first spent catalyst and the second spent catalyst are combined in a reactor to produce a mixed spent catalyst.

FLUIDIZED BED SYSTEM

A fluidized bed system is a single unitary modular system that packages a circulation fan, a fluidized bed, and a dust collection system within a same structure. The structure is formed to include internal ducts to provide fluid communication between the circulation fan, the fluidized bed, and the dust collection system. The fan provides a flow of air via a pressure duct to the fluidized bed. Particulate is separated from particles included on the fluidized bed by the flow of air being uniformly distributed to the fluidized bed. Particulate separated in a disengagement area and suspended in the flow of air is conducted through a particulate clearance space surrounding the dust collection system. The particulate is captured by the dust collection system and conveyed to a location external to the system. 1. A fluidized bed system comprising:an enclosure having an inner chamber positioned below a dust hopper;a fluidized bed positioned in the inner chamber below the dust hopper and configured to process particles and remove particulate;a fan included in a plenum, the fan configured to provide a flow of air through the fluidized bed toward the dust hopper; anda wall defining the inner chamber, the dust hopper moveably positioned vertically within the inner chamber at a predetermined height above the fluidized bed to separate a predetermined size of particulate from the particles within the flow of air toward the dust hopper, the dust hopper at least partially surrounded by the wall to provide a particulate clearance space between the wall and the dust hopper, an entrance to the particulate clearance space configured to receive only the predetermined size of the particulate separated from the particles within the flow of air due to the predetermined height.2. The fluidized bed system of claim 1 , further comprising a pressure duct at an outlet of the fan and a suction duct at an inlet of the fan claim 1 , the suction duct having heated air that is in thermal communication ...

CORROSION-PROTECTED REFORMER TUBE WITH INTERNAL HEAT EXCHANGE

A reformer tube for producing synthesis gas by steam reforming of hydrocarbon-containing input gases is proposed where 110-. (canceled)11. A reformer tube for converting hydrocarbon-containing input materials , preferably natural gas , into a synthesis gas product comprising carbon oxides and hydrogen under steam reforming conditions , comprisinga. an outer, pressurized shell tube, wherein the shell tube is divided into a reaction chamber and an exit chamber by means of a separating tray, so that it is possible to set a different, preferably lower, pressure in the exit chamber than in the reaction chamber, and wherein the reaction chamber is externally heated,b. a dumped bed of a steam-reforming-active solid catalyst arranged in the reaction chamber,c. an entry for the input gas stream comprising the input material, arranged in the region of the reaction chamber, wherein the entry for the input gas stream is in fluid connection with the dumped catalyst bed,d. at least one helically coiled heat exchanger tube arranged inside the reaction chamber and inside the dumped catalyst bed, whose entry end is in fluid connection with the dumped catalyst bed and whose exit end is in fluid connection with the exit chamber, wherein the input gas stream after entry into the reaction chamber initially flows through the dumped catalyst bed and subsequently flows through the heat exchanger tube in countercurrent, and wherein the heat exchanger tube is in a heat exchange relationship with the dumped catalyst bed and the input gas stream flowing therethrough,e. a collection conduit for the synthesis gas product, which is in fluid connection with the exit chamber,wherein, in the region of the exit chamber:the exit end of the heat exchanger tube is fed through the separating tray and opens into an inner tube which is arranged in the interior of the shell tube and is in fluid connection with the collection conduit, so that the synthesis gas product is able to pass from the reaction ...

Fcc counter-current regenerator

A counter-current catalyst regenerator with at least two stages of counter-current contact is proposed. Each stage may comprise a permeable barrier that allows upward passage of oxygen-containing gas and downward passage of coked catalyst into each stage, but inhibits upward movement of catalyst to mitigate back mixing and approximate true counter-current contact and efficient combustion of coke from catalyst.

Processes and Systems for the Conversion of Acyclic Hydrocarbons

This invention relates to processes and systems for converting acyclic hydrocarbons to alkenes, cyclic hydrocarbons and/or aromatics, for example converting acyclic Chydrocarbons to cyclopentadiene in a reactor system. The process includes contacting a feedstock comprising acyclic hydrocarbons with a catalyst material and an inert material to convert at least a portion of the acyclic hydrocarbons to a first effluent comprising alkenes, cyclic hydrocarbons and/or aromatics. In particular, the catalyst material and the inert material have a different average diameter and/or density providing varying fluidization behavior in the reactor. 1. A process for converting acyclic Chydrocarbons to cyclopentadiene in a reactor system , wherein the process comprises:{'sub': 5', '5, 'contacting a feedstock comprising acyclic Chydrocarbons with a catalyst material and an inert material in at least one reaction zone under reaction conditions to convert at least a portion of the acyclic Chydrocarbons to a first effluent comprising cyclopentadiene, wherein the catalyst material and the inert material have a different average diameter and/or density, wherein the catalyst material is a crystalline aluminosilicate in combination with a Group 10 metal, Group 1 alkali metal and/or a Group 2 alkaline earth metal;'}removing an inert material-rich stream comprising at least a first portion of the catalyst material from the at least one reaction zone;optionally, separating at least a second portion of the catalyst material from the inert material-rich stream;heating the inert material-rich stream to produce a heated inert material-rich stream; andproviding the heated inert material-rich stream to the at least one reaction zone.2. The process of claim 1 , wherein the at least one reaction zone is a circulating fluidized bed reactor.3. The process of claim 1 , wherein the feedstock is provided at a temperature of less than about 650° C. and/or the first effluent exiting the at least one ...

Processes and Systems for the Conversion of Acyclic Hydrocarbons

This invention relates to processes and systems for converting acyclic hydrocarbons to alkenes, cyclic hydrocarbons and/or aromatics, for example converting acyclic Chydrocarbons to cyclopentadiene in a reactor system. The process includes contacting a feedstock comprising acyclic hydrocarbons with a catalyst material in at least one reaction zone to convert at least a portion of the acyclic hydrocarbons to a first effluent comprising alkenes, cyclic hydrocarbons and/or aromatics. A co-feed comprising H, C-Calkanes and/or C-Calkenes may also be provided to the at least one reaction zone. 1. A process for converting acyclic hydrocarbons to alkenes , cyclic hydrocarbons and/or aromatics in a reactor system , wherein the process comprises:{'sub': '2', 'contacting a feedstock comprising acyclic hydrocarbons and optionally Hwith a catalyst material comprising platinum on ZSM-5, platinum on zeolite L, and/or platinum on silica in at least one reaction zone under reaction conditions to convert at least a portion of the acyclic hydrocarbons to a first effluent comprising alkenes, cyclic hydrocarbons and/or aromatics, wherein the feedstock enters the at least one reaction zone at a temperature of about 300° C. to about 700° C.; and'}{'sub': 2', '1', '4', '1', '4, 'providing a co-feed comprising H, C-Calkanes and/or C-Calkenes at a temperature of about 600° C. to about 1100° C. to heat the at least one reaction zone, wherein the feedstock and the co-feed are provided to the at least one reaction zone at different locations via different inlets,'}wherein the feedstock and the co-feed is optionally provided to the at least one reaction zone simultaneously.2. The process of claim 1 , wherein the at least one reaction zone is a captive or circulating fluidized bed reactor.3. The process of claim 1 , wherein the first effluent exiting the at least one reaction zone has a temperature of at least about 550° C.4. The process of claim 1 , wherein the reaction conditions comprise a ...

SYSTEM COMPONENTS OF FLUID CATALYTIC REACTOR SYSTEMS

According to one or more embodiments disclosed herein, a system component of a fluid catalytic reactor system may include a catalyst separation section, a riser, and a reactor vessel. The catalyst separation section may include separation section walls defining an interior region of the catalyst separation section, a gas outlet port, a riser port, a separation device, and a catalyst outlet port. The riser may extend through the riser port of the catalyst separation section and include an external riser section and an internal riser section. The reactor vessel may include a reactor vessel inlet port, and a reactor vessel outlet port in fluid communication with the external riser section of the riser. 1. A system component of a fluid catalytic reactor system , the system component comprising:a catalyst separation section comprising separation section walls defining an interior region of the catalyst separation section, a gas outlet port, a riser port, a separation device, and a catalyst outlet port;a riser extending through the riser port of the catalyst separation section, the riser comprising a main interior riser wall segment, a main exterior riser wall segment, and a riser transition wall segment, the main interior riser wall segment positioned at least partially in the interior region of the catalyst separation section and connected with at least the main interior riser wall segment, and the exterior riser wall segment positioned at least partially outside of the catalyst separation section; anda reactor vessel comprising a reactor vessel inlet port, and a reactor vessel outlet port in fluid communication with the main exterior riser wall segment.2. The system component of claim 1 , wherein the main interior riser wall segment and the main exterior riser wall segment are substantially parallel claim 1 , and the maximum diameter of the main interior riser wall segment is less than the maximum diameter of the main exterior riser wall segment.3. The system component ...

METHOD FOR FEEDING A FLUID TO A GAS PHASE POLYMERIZATION REACTOR

A fluid is fed into a polymer bed of a fluidized bed gas phase polymerization reactor by introducing the fluid into the polymer bed through a distributor protruding into the fluidized bed zone of the reactor and terminating with a discharge end positioned so that the following equation is fulfilled: 1. A method for feeding a fluid into a polymer bed of a fluidized bed gas phase polymerization reactor comprising the step of: {'br': None, 'i': 'd/D>', '0.002'}, 'introducing a controlled and continuous flow rate of the fluid into the polymer bed through a distributor protruding into the fluidized bed zone of the reactor and terminating with a discharge end positioned so that the following equation is fulfilledwherein d is the distance of the distributor's discharge end from the wall of the reactor, and D is the diameter of the reactor in the fluidized bed zone.2. The method according to claim 1 , wherein a head loss is generated through orifices in the distributor such that a Reynolds number (Re) of from 10000 to 700000 is achieved.3. The method according to claim 1 , wherein the fluid is an antistatic composition comprising (with respect to the total weight of the antistatic composition):(a) from 0.5 to 50% by weight of a compound of formula R—OH wherein R represents hydrogen or a linear or branched, saturated alkyl group having from 1 to 15 carbon atoms; and{'sup': '2', '(b) from 50 to 99.5% by weight of an oligomeric or polymeric organic compound having one or more terminal hydroxyl groups and a viscosity at 40° C. of at least 20 mm/sec (DIN 51562).'}4. The method according to further comprising the step of feeding the antistatic composition or individual components thereof to the polymerization reactor in a flow of saturated or unsaturated hydrocarbon having from 2 to 6 carbon atoms.5. The method according to claim 3 , wherein the compound (a) of formula R—OH is water.6. The method according to claim 3 , wherein the oligomeric or polymeric organic compound (b) is ...

CORROSION-PROTECTED REFORMER TUBE WITH INTERNAL HEAT EXCHANGE

A reformer tube for producing synthesis gas by steam reforming of hydrocarbon-containing input gases is proposed where 115-. (canceled)16. A reformer tube for converting a hydrocarbon-containing feed into a synthesis gas product comprising carbon oxides and hydrogen under steam reforming conditions , the reformer tube comprising:(a) an outer, pressurized shell tube, wherein the shell tube is divided into a reaction chamber and an exit chamber by means of a separating tray and wherein the reaction chamber is externally heatable;(b) a dumped bed of a steam-reforming-active solid catalyst arranged in the reaction chamber;(c) an entry for the input gas stream comprising the input material arranged in the region of the reaction chamber, wherein the entry for the input gas stream is in fluid connection with the dumped catalyst bed;(d) at least one heat exchanger tube arranged inside the reaction chamber and inside the dumped catalyst bed whose entry end is in fluid connection with the catalyst bed and whose exit end is in fluid connection with the exit chamber, wherein the input gas stream after entry into the reaction chamber initially flows through the catalyst bed and subsequently flows through the heat exchanger tube in countercurrent and is thus continually cooled and wherein the heat exchanger tube is in a heat exchange relationship with the dumped catalyst bed and the input gas stream flowing therethrough; and(e) a collection conduit for the synthesis gas product which is in fluid connection with the exit chamber,wherein the gas-contacted metallic components of the reformer tube are made of a nickel-based alloy and those gas-contacted surfaces having a temperature during operation under defined steam reforming conditions of between 650° C. and 800° C. are equipped with an aluminum diffusion layer.17. The reformer tube according to claim 16 , wherein those regions of the inner wall of the at least one heat exchanger tube having a surface temperature between 650° C. ...

FLUID CATALYTIC CRACKING PROCESS AND APPARATUS FOR MAXIMIZING LIGHT OLEFIN YIELD AND OTHER APPLICATIONS

Apparatus and processes herein provide for converting hydrocarbon feeds to light olefins and other hydrocarbons. The processes and apparatus include, in some embodiments, feeding a hydrocarbon, a first catalyst and a second catalyst to a reactor, wherein the first catalyst has a smaller average particle size and is less dense than the second catalyst. A first portion of the second catalyst may be recovered as a bottoms product from the reactor, and a cracked hydrocarbon effluent, a second portion of the second catalyst, and the first catalyst may be recovered as an overhead product from the reactor. The second portion of the second catalyst may be separated from the overhead product, providing a first stream comprising the first catalyst and the hydrocarbon effluent and a second stream comprising the separated second catalyst, allowing return of the separated second catalyst in the second stream to the reactor. 143.-. (canceled)44. A process for the conversion of hydrocarbons , comprising:feeding first particles and second particles to a reactor, wherein the first particles have a smaller average particle size and/or are less dense than the second particles, and wherein the first particles and second particles may independently be catalytic or non-catalytic particles;feeding a hydrocarbon feedstock to the reactor;recovering an overhead product from the reactor comprising a converted hydrocarbon effluent, the second particles, and the first particles;separating the second particles from the overhead product to provide a first stream comprising the first particles and the converted hydrocarbon effluent and a second stream comprising the separated second particles;returning the separated second particles in the second stream to the reactor.45. The process of claim 44 , further comprising recovering a bottoms product from the reactor comprising the second particle.46. The process of claim 44 , further comprising:feeding a second hydrocarbon feedstock and a mixture of ...

FLUID CATALYTIC CRACKING PROCESS AND APPARATUS FOR MAXIMIZING LIGHT OLEFIN YIELD AND OTHER APPLICATIONS

Apparatus and processes herein provide for converting hydrocarbon feeds to light olefins and other hydrocarbons. The processes and apparatus include, in some embodiments, feeding a hydrocarbon, a first catalyst and a second catalyst to a reactor, wherein the first catalyst has a smaller average particle size and is less dense than the second catalyst. A first portion of the second catalyst may be recovered as a bottoms product from the reactor, and a cracked hydrocarbon effluent, a second portion of the second catalyst, and the first catalyst may be recovered as an overhead product from the reactor. The second portion of the second catalyst may be separated from the overhead product, providing a first stream comprising the first catalyst and the hydrocarbon effluent and a second stream comprising the separated second catalyst, allowing return of the separated second catalyst in the second stream to the reactor. 1. A particle separator for separating catalysts or other particles based on size and/or density , comprising:an inlet for providing a mixture comprising a carrier gas, a first particle type, and a second particle type, each particle type having a particle size distribution, an average particle size and an average density, the second particle type having an average particle size and/or average density greater than the first particle type;a chamber for receiving the mixture, wherein the chamber is configured to separate at least a portion of the second particle type from the carrier gas and the first particle type;a first outlet to recover the second particle type;a second outlet to recover the carrier gas and the first particle type; anda distributor disposed within or proximate the first outlet for introducing a fluidizing gas, facilitating additional separation of the first particle type from the second particle type.2. The separator of claim 1 , wherein a cross-sectional area of the chamber or a portion thereof is adjustable.3. The separator of claim 1 , ...

Production of aromatic hydrocarbons from light alkanes

Provided is a method for producing aromatic hydrocarbons from light alkanes. A light alkane feed is contacted with catalyst particles in each of reactors, wherein each of the reactors is a fluidized bed reactor and arranged in parallel with each other in a furnace. At least a portion of the alkane feed is converted to aromatic hydrocarbons using the catalyst particles, wherein the aromatic hydrocarbons form a part of a reactor effluent stream. The reactor effluent streams from each of the reactors are merged to form a first merged effluent stream. The first merged effluent stream is separated into the aromatic hydrocarbons, light hydrocarbons, and a fuel gas.

A method for returning polymer to a fluidised bed reactor

The present invention deals with a process of polymerising at least one olefin in a fluidised bed in a fluidised bed polymerisation reactor comprising a top zone, a middle zone in direct contact and below, a bottom zone in direct contact with and below the middle zone and wherein the reactor does not comprise a fluidisation grid. The process comprises passing a stream comprising the fluidisation gas and polymer particles into a separation step and withdrawing a stream comprising the polymer particles from the separation step and returning it to the polymerisation reactor. The process comprises adding a support gas stream to the stream comprising the polymer particles downstream of the separation step.

APPARATUS AND PROCESS FOR SEPARATING GASES FROM CATALYST AND REVAMP

In an FCC apparatus and process structured packing should be located at the very top of the stripping section in an upper region. The lower region below the structural packing may be equipped with fluidization equipment such as stripping media distributors and one or more gratings. This arrangement enables stripping of entrained hydrocarbons off the incoming catalyst immediately upon entry into the stripping section allowing the entrained hydrocarbon to exit the stripping section with minimized residence time to minimize post-riser cracking. Revamp of stripping sections with tall stripping sections should conducted in this way to improve performance and reduce down-time for equipment installation.

FLUID CATALYTIC CRACKING PROCESS AND APPARATUS FOR MAXIMIZING LIGHT OLEFIN YIELD AND OTHER APPLICATIONS

Apparatus and processes herein provide for converting hydrocarbon feeds to light olefins and other hydrocarbons. The processes and apparatus include, in some embodiments, feeding a hydrocarbon, a first catalyst and a second catalyst to a reactor, wherein the first catalyst has a smaller average particle size and is less dense than the second catalyst. A first portion of the second catalyst may be recovered as a bottoms product from the reactor, and a cracked hydrocarbon effluent, a second portion of the second catalyst, and the first catalyst may be recovered as an overhead product from the reactor. The second portion of the second catalyst may be separated from the overhead product, providing a first stream comprising the first catalyst and the hydrocarbon effluent and a second stream comprising the separated second catalyst, allowing return of the separated second catalyst in the second stream to the reactor. 1. A system for cracking hydrocarbons , comprising:a regenerator; receive a mixture of first particles and second particles from the regenerator, wherein the first particles have a smaller average particle size and/or are less dense than the second particles, and wherein the first particles and second particles may independently be catalytic or non-catalytic particles;', 'contact a hydrocarbon fraction with the mixture of first particles and second particles to convert at least a portion of the hydrocarbon fraction; and', 'produce an overhead product from the riser reactor comprising the converted hydrocarbon fraction, the second particles, and the first particles;, 'a riser reactor configured to a housing;', 'a solids separation device disposed within the housing for separating the second particles from the overhead product to provide a first stream, comprising the first particles and the carrier fluid and/or a reaction product of the carrier fluid, and a second stream, comprising the separated second particles;', 'one or more cyclones disposed within the ...

PROCESS AND APPARATUS FOR ENHANCED REMOVAL OF CONTAMINANTS IN FLUID CATALYTIC CRACKING PROCESSES

Systems for separating a contaminant trapping additive from a cracking catalyst may include a contaminant removal vessel having one or more fluid connections for receiving contaminated cracking catalyst, contaminated contaminant trapping additive, fresh contaminant trapping additive, and a fluidizing gas. In the contaminant removal vessel, the spent catalyst may be contacted with contaminant trapping additive, which may have an average particle size and/or density greater than the cracking catalyst. A separator may be provided for separating an overhead stream from the contaminant removal vessel into a first stream comprising cracking catalyst and lifting gas and a second stream comprising contaminant trapping additive. A recycle line may be used for transferring contaminant trapping additive recovered in the second separator to the contaminant removal vessel, allowing contaminant trapping additive to accumulate in the contaminant removal vessel. A bottoms product line may provide for recovering contaminant trapping additive from the contaminant removal vessel. 1. (canceled)2. (canceled)3. (canceled)4. (canceled)5. (canceled)6. (canceled)7. A process for removing contaminants from a catalyst , comprising:feeding a catalyst comprising contaminants to a contaminant removal vessel;feeding a contaminant trapping additive to the contaminant removal vessel, wherein the contaminant trapping additive has an average particle size greater than an average particle size of the catalyst and/or a density greater than the catalyst;fluidizing the catalyst and the contaminant trapping additive with a lifting gas, contacting the catalyst with the contaminant trapping additive, and transferring contaminants from the catalyst to the contaminant trapping additive;withdrawing from the contaminant removal vessel a first stream comprising lifting gas, contaminant trapping additive, and catalyst having a reduced amount of contaminants;separating the contaminant trapping additive from the ...

Methods of changing polyolefin production rate with the composition of the induced condensing agents

Polyolefin polymerization performed by contacting in a reactor an olefin monomer and optionally a comonomer with a catalyst system in the presence of induced condensing agents (ICA) and optionally hydrogen. The ICA may include two or more ICA components where the composition of the ICA (i.e ., the concentration of each ICA component) may affect the polyolefin production rate. Changes to the relative concentration of the two or more ICA components may be according to ICA equivalency factors that allow for increasing the polyolefin production rate while maintain a sticking temperature, increasing polyolefin production rate while increasing the dew point approach temperature of the ICA, or a combination thereof.

Polyolefin reactor system having a gas phase reactor

A system and method for polymerizing olefin in a gas phase reactor into a polyolefin in presence of catalyst, measuring static charge in the reactor system; determining an indication of polyolefin fines in the reactor system, and adjusting operation of the reactor system in response to the indication.

Methods of monitoring and controlling the melt index of a polyolefin product during production

Methods for producing polyolefin polymers may use a predictive melt index regression to estimate the melt index of the polyolefin during production based on the composition of the gas phase and, optionally, the concentration of catalyst in the reactor or reactor operating conditions. Such predictive melt index regression may include multiple terms to account for concentration of ICA in the reactor, optionally concentration of hydrogen in the reactor, optionally concentration of comonomer in the reactor, optionally the catalyst composition, and optionally reactor operating conditions. One or more terms may independently be represented by a smoothing function that incorporates a time constant.

Method for degassing and buffering polyolefin particles obtained by olefin polymerization

Process for the polymerization of olefins

Process for the polymerization of olefins

Methods of changing polyolefin production rate with the composition of the induced condensing agents

Polyolefin polymerization performed by contacting in a reactor an olefin monomer and optionally a comonomer with a catalyst system in the presence of induced condensing agents (ICA) and optionally hydrogen. The ICA may include two or more ICA components where the composition of the ICA (i.e., the concentration of each ICA component) may affect the polyolefin production rate. Changes to the relative concentration of the two or more ICA components may be according to ICA equivalency factors that allow for increasing the polyolefin production rate while maintain a sticking temperature, increasing polyolefin production rate while increasing the dew point approach temperature of the ICA, or a combination thereof.

Method of degassing and imparting intermediate properties to polyolefin particles obtained during polymerisation of olefins

FIELD: chemistry. SUBSTANCE: invention relates to a method of degassing and imparting intermediate properties to polyolefin particles obtained during polymerisation of olefins. Method for production of olefin polymers involves formation of polyolefin particles by polymerisation in presence of catalyst in a polymerisation reactor. Method then includes unloading of polyolefin particles from reactor and degassing of polyolefin particles with a nitrogen stream in a degassing tank. Degassing tank is partially filled with polyolefin particles. At continuous transfer of polyolefin particles from degassing tank into melt mixing device and unloading polyolefin particles from polymerisation reactor with constant speed, free space inside degassing tank receives additional polyolefin particles during at least 3 hours. EFFECT: providing operating flexibility for continuation of polymerisation process during a certain period of time during shutdown of melt mixing device without need to install storage containers between stages of degassing and granulation of polyolefin particles and minimisation of requirements in their pneumatic transportation. 12 cl, 1 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 610 541 C2 (51) МПК C08F 6/00 (2006.01) C08F 10/00 (2006.01) C08F 10/02 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ФОРМУЛА (21)(22) Заявка: ИЗОБРЕТЕНИЯ К ПАТЕНТУ РОССИЙСКОЙ ФЕДЕРАЦИИ 2015125331, 11.12.2013 (24) Дата начала отсчета срока действия патента: 11.12.2013 Дата регистрации: (73) Патентообладатель(и): БАЗЕЛЛ ПОЛИОЛЕФИН ГМБХ (DE) Приоритет(ы): (30) Конвенционный приоритет: 11.12.2012 EP 12196450.6 (56) Список документов, цитированных в отчете о поиске: WO 2008/015228 A2, 07.02.2008. WO 2011/97119 A1, 11.08.2011. WO 2006/026493 A1, 09.03.2006. RU 2456300 С2, 20.07.2012. WO 2010/037656 A1, 08.04.2010. (45) Опубликовано: 13.02.2017 Бюл. № 5 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 26.06.2015 (86) Заявка PCT: EP 2013/076185 (11.12.2013) ...

Method and apparatus for discharging a polymer from a gas-phase reactor

Process for discharging polyolefin particles from a gas-phase polymerization reactor of a pressure from 1.0 MPa to 10 MPa to a discharge vessel of a pressure from 0.1 MPa to 1.0 MPa wherein the discharging is carried out discontinuously through at least two discharge lines in which the polyolefin particles are transported horizontally or upwards, process for polymerizing olefins at temperatures of from 30°C to 160°C and pressures of from 1.0 MPa to 10 MPa in the presence of a polymerization catalyst in a gas-phase polymerization reactor comprising discharging the obtained polyolefin particles from the gas-phase polymerization reactor by the process for discharging polyolefin particles and apparatus for polymerizing olefins in the gas-phase comprising a polymerization reactor, a discharge vessel and at least two pipes connecting the polymerization reactor and the discharge vessel for discharging polyolefin particles, wherein the discharge lines are constructed in a way that the polyolefin particles conveyed from the polymerization reactor to the discharge vessel are transported horizontally or upwards.

在生产期间监测和控制聚烯烃产物的熔融指数的方法

生产聚烯烃聚合物的方法可使用预测性熔融指数回归估计生产期间的聚烯烃的熔融指数，其基于气相的组成，并且任选地基于反应器中的催化剂的浓度或反应器操作条件。此类预测性熔融指数回归可包括多个项以考虑所述反应器中的ICA的浓度、任选地所述反应器中的氢气的浓度、任选地所述反应器中的共聚单体的浓度、任选地催化剂组成和任选地反应器操作条件。一或多个项可独立地由并入时间常量的平滑函数表示。

Gas phase reactor startup process

A gas phase reactor startup process comprising providing a reactor having a vertical cylindrical portion from a distributor plate at the base to a neck at the top and comprising a fluidized bed zone therebetween, wherein above the neck and connected thereto is a frustoconical portion closed at the top, the vertical cylindrical portion having a length from the distributor plate to the neck; providing a bed of polyolefin granules within the fluidized bed zone; wherein the polyolefin granules fill the fluidized bed zone to a resting bed level within a range from 75% to 90% of the length of the vertical cylindrical portion prior to fluidization with cycle gas; flowing cycle gas to fluidize the polyolefin granules and form a fluidized bed having a fluidized bed level greater than the resting bed level; and injecting metallocene catalyst into the fluidized bed zone.

Method and apparatus for discharging a polymer from a gas-phase reactor

Process and apparatus for discharging polyolefin particles from a gas-phase polymerization reactor of a pressure from 1.0 MPa to 10 MPa to a discharge vessel of a pressure from 0.1 MPa to 1.0 MPa wherein the discharging is carried out discontinuously through at least two discharge lines in which the polyolefin particles are transported horizontally or upwards.

Apparatus and process for gas phase fluidised bed polymerisation reaction

The present invention relates to an apparatus and a process for polymerization, and, in particular, provides an apparatus for gas phase fluidised bed polymerization of olefins, which apparatus comprises: A) a first section which is an upright cylindrical section having a diameter, D 1 , and cross-sectional area, A 1 , and B) a second section, provided vertically above the first section and centered about a common vertical axis to the upright cylindrical first section, the base of the second section having a cylindrical cross-section of diameter D 1 and being joined to the top of the first section, and the horizontal cross-sectional area of the second section above its base being greater than the cross-sectional area of the first section, characterized in that: i) D 1 is greater than 4.5 meters, and ii) the second section has a maximum horizontal cross-sectional area, A 2 , which is between 3.2 and 6 times the cross-sectional area, A 1 , of the first section.

Process for degassing and buffering polyolefin particles obtained by olefin polymerization

Process for preparing a polyolefin polymer comprising the steps of a) forming a particulate polyolefin polymer by polymerizing one or more olefins in the presence of a polymerization catalyst system in a polymerization reactor; b) discharging the formed polyolefin particles from the polymerization reactor; c) degassing the polyolefin particles by a process comprising at least a final step of contacting the polyolefin particles with a nitrogen stream in a degassing vessel; and d) transferring the polyolefin particles from the vessel, in which the contacting of the polyolefin particles with the nitrogen stream is carried out, to a melt mixing device, in which the polyolefin particles are melted, mixed and thereafter pelletized, without passing the particles through a buffering device, wherein the degassing vessel is only partly filled with polyolefin particles and the empty volume within the degassing vessel is sufficient to take up additional polyolefin particles for at least 3 hours if the transfer of polyolefin particles of step d) from the degassing vessel to the melt mixing device is discontinued and the discharge of polyolefin particles from the polymerization reactor according to step b) is continued with unchanged rate.

Methods of changing polyolefin production conditions to mitigate small gels in a polyolefin article

The number of small gels that form in polyolefin thin films may be reduced by altering certain production parameters of the polyolefin. In some instances, the number of small gels may be influenced by the melt index of the polyolefin. However, in many instances, melt index is a critical part of the polyolefin product specification and, therefore, is not manipulated. Two parameters that may be manipulated to mitigate small gel count while maintaining the melt index are polyolefin residence time in the reactor and ICA concentration in the reactor.

Fluidized bed polymerization reactor and process for preparing polymer

The present invention provides a fluidized bed polymerization reactor, comprising: a tower body, provided therein with a liquid phase distributor and a gas phase distributor above the liquid phase distributor, so as to divide a reaction area into a first area and a second area by means of the gas phase distributor; and a recycling unit, for recycling the gaseous substances originating from the top area of the tower to the bottom area in the form of a gas liquid mixture. In this situation, the gas liquid mixture is subjected to a gas liquid separation in the bottom area, wherein the gas phase obtained is output into the gas phase distributor and thence into the second area, and the liquid phase obtained enters the first area via the liquid phase distributor, such that the temperature in the first area is lower than the temperature in the second area. A polymer with a relatively wide molecular weight distribution can thus be produced. The present invention also provides a process for preparing polymers.

Process for degassing and buffering polyolefin particles obtained by olefin polymerization

Process for preparing a polyolefin polymer comprising the steps of a) forming a particulate polyolefin polymer by polymerizing one or more olefins in the presence of a polymerization catalyst system in a polymerization reactor; b) discharging the formed polyolefin particles from the polymerization reactor; c) degassing the polyolefin particles by a process comprising at least a final step of contacting the polyolefin particles with a nitrogen stream in a degassing vessel; and d) transferring the polyolefin particles from the vessel, in which the contacting of the polyolefin particles with the nitrogen stream is carried out, to a melt mixing device, in which the polyolefin particles are melted, mixed and thereafter pelletized, without passing the particles through a buffering device, wherein the degassing vessel is only partly filled with polyolefin particles and the empty volume within the degassing vessel is sufficient to take up additional polyolefin particles for at least 3 hours if the transfer of polyolefin particles of step d) from the degassing vessel to the melt mixing device is discontinued and the discharge of polyolefin particles from the polymerization reactor according to step b) is continued with unchanged rate.

Process for the polymerization of olefins

The present invention relates to a process for the continuous preparation of a polyolefin in a reactor from one or more α-olefin monomers of which at least one is ethylene or propylene, wherein the reactor comprises a fluidized bed, an expanded section located at or near the top of the reactor, a distribution plate located at the lower part of the reactor and an inlet for a recycle stream located under the distribution plate, wherein the process comprises - feeding a polymerization catalyst to the fluidized bed in the area above the distribution plate - feeding the one or more α-olefin monomers to the reactor - withdrawing the polyolefin from the reactor - circulating fluids from the top of the reactor to the bottom of the reactor, wherein the circulating fluids are cooled using a heat exchanger, resulting in a cooled recycle stream comprising liquid, and wherein the cooled recycle stream is introduced into the reactor using the inlet for the recycle stream wherein a stream comprising a thermal run away reducing agent (TRRA-containing stream) is introduced into the expanded section during at least part of the polymerization process, wherein said TRRA-containing stream is brought into contact with at least part of the interior surface of the expanded section.

Process for the polymerization of olefins

The present invention relates to a process for the continuous preparation of a polyolefin in a reactor from one or more α-olefin monomers of which at least one is ethylene or propylene, wherein the reactor comprises a fluidized bed, an expanded section located at or near the top of the reactor, a distribution plate located at the lower part of the reactor and an inlet for a recycle stream located under the distribution plate wherein the process comprises - feeding a polymerization catalyst to the fluidized bed in the area above the distribution plate - feeding the one or more α-olefin monomers to the reactor - withdrawing the polyolefin from the reactor - circulating fluids from the top of the reactor to the bottom of the reactor, wherein the circulating fluids are compressed using a compressor and subsequently cooled using a heat exchanger to form a cooled recycle stream comprising liquid, and wherein the cooled recycle stream is introduced into the reactor using the inlet for the recycle stream wherein a part of the cooled recycle stream is drawn to form a liquid comprising stream, wherein the liquid comprising stream is introduced into the expanded section during at least part of the polymerization process, and wherein the liquid comprising stream is brought into contact with at least part of the interior surface of the expanded section.

Process for the polymerization of olefins

The present invention relates to a process for the continuous preparation of a polyolefin in a reactor from one or more α-olefin monomers of which at least one is ethylene or propylene, wherein the reactor comprises a fluidized bed, an expanded section located at or near the top of the reactor, a distribution plate located at the lower part of the reactor and an inlet for a recycle stream located under the distribution plate, wherein the process comprises—feeding a polymerization catalyst to the fluidized bed in the area above the distribution plate—feeding the one or more α-olefin monomers to the reactor—withdrawing the polyolefin from the reactor—circulating fluids from the top of the reactor to the bottom of the reactor, wherein the circulating fluids are cooled using a heat exchanger, resulting in a cooled recycle stream comprising liquid, and wherein the cooled recycle stream is introduced into the reactor using the inlet for the recycle stream wherein a stream comprising a thermal run away reducing agent (TRRA-containing stream) is introduced into the expanded section during at least part of the polymerization process, wherein said TRRA-containing stream is brought into contact with at least part of the interior surface of the expanded section.

Fluidized bed reactor system allowing particle sampling during an ongoing reaction

A fluidized gas reactor includes a system for preventing a fluidizing gas comprising a reactant from premature reaction. The fluidized gas reactor includes a reaction chamber including a particle bed; a gas distribution plate having a plurality of openings therethrough, wherein each opening opens into the reaction chamber; and a plurality of vertical fluidizing gas inlet tubes, each of the fluidizing gas inlet tubes being in fluid communication with one of the openings in the gas distribution plate. Each fluidizing gas inlet tube is configured to receive a fluidizing gas and transport the fluidizing gas to the reaction chamber. A fluidizing gas source provides a stream of the fluidizing gas to the fluidizing gas inlet tubes. A coolant system prevents the fluidizing gas from undergoing reaction before entering the reaction chamber. The coolant system has a fluid inlet; a coolant flow path in fluid communication with the fluid inlet, the coolant flow path being configured to cool each fluidizing gas inlet tube; and a fluid outlet in fluid communication with the coolant flow path. Each fluidizing gas inlet tube may include a particle outlet and a valve system, where the valve system allows the fluidizing gas flow to the fluidizing gas inlet tubes to be stopped; and allows recovery of particles from the particle bed while the fluidizing gas flow is stopped.

Apparatus and process for gas phase fluidised bed polymerisation

The present invention relates to an apparatus and a process for polymerisation, and, in particular, provides an apparatus for gas phase fluidised bed polymerisation of olefins, which apparatus comprises: A) a first section which is an upright cylindrical section having a diameter, D 1 , and cross-sectional area, A 1 , and B) a second section, provided vertically above the first section and centred about a common vertical axis to the upright cylindrical first section, the base of the second section having a cylindrical cross-section of diameter D 1 and being joined to the top of the first section, and the horizontal cross-sectional area of the second section above its base being greater than the cross-sectional area of the first section, characterised in that: i) D 1 is greater than 4.5 metres, and ii) the second section has a maximum horizontal cross-sectional area, A 2 , which is between 3.2 and 6 times the cross-sectional area, A 1 , of the first section.

Apparatus and process for gas phase fluidised bed polymerisation reaction

The present invention relates to an apparatus and a process for polymerisation, and, in particular, provides an apparatus for gas phase fluidised bed polymerisation of olefins, which apparatus comprises: A) a first section which is an upright cylindrical section having a diameter, D 1 , and cross-sectional area, A 1 , and B) a second section, provided vertically above the first section and centred about a common vertical axis to the upright cylindrical first section, the base of the second section having a cylindrical cross-section of diameter D 1 and being joined to the top of the first section, and the horizontal cross-sectional area of the second section above its base being greater than the cross-sectional area of the first section, characterised in that: i) D 1 is greater than 4.5 metres, and ii) the second section has a maximum horizontal cross-sectional area, A 2 , which is between 3.2 and 6 times the cross-sectional area, A 1 , of the first section.

用于烯烃聚合的方法

本发明涉及一种用于在反应器中由一种或多种α‑烯烃单体连续制备聚烯烃的方法，所述α‑烯烃单体中的至少一种是乙烯或丙烯，其中所述反应器包括流化床、位于所述反应器的顶部处或附近的膨胀区段、位于所述反应器的下部部分的分配板和位于所述分配板下方的再循环流的入口，其中所述方法包括‑将聚合催化剂进料到所述分配板上方的区域中的流化床中‑将所述一种或多种α‑烯烃单体进料到所述反应器中‑从所述反应器中抽取出所述聚烯烃‑将流体从所述反应器的顶部循环至所述反应器的底部，其中所述循环流体使用压缩机压缩并且随后使用热交换器冷却以形成包含液体的冷却的再循环流，并且其中将所述冷却的再循环流使用所述再循环流的入口引入到所述反应器中，其中将所述冷却的再循环流的一部分抽取出以形成含液体流，其中在所述聚合方法的至少一部分期间将所述含液体流引入到所述膨胀区段中，并且其中使所述含液体流与所述膨胀区段的内表面的至少一部分接触。

用于烯烃聚合的方法

本发明涉及一种用于在反应器中由一种或多种α‑烯烃单体连续制备聚烯烃的方法，所述α‑烯烃单体中的至少一种是乙烯或丙烯，其中所述反应器包括流化床、位于所述反应器的顶部处或附近的膨胀区段、位于所述反应器的下部部分的分配板和位于所述分配板下方的再循环流的入口，其中所述方法包括‑将聚合催化剂进料到所述分配板上方区域中的流化床中‑将所述一种或多种α‑烯烃单体进料到所述反应器中‑从所述反应器中抽取出所述聚烯烃‑将流体从所述反应器的顶部循环至所述反应器的底部，其中所述循环流体使用热交换器冷却，产生包含液体的冷却的再循环流，并且其中将所述冷却的再循环流使用所述再循环流的入口引入到所述反应器中，其中在所述聚合方法的至少一部分期间，将包含热失控减少剂的流(含TRRA的流)引入到所述膨胀区段中，其中使所述含TRRA的流与所述膨胀区段的内表面的至少一部分接触。

Process for the polymerization of olefins

The present invention relates to a process for the continuous preparation of a polyolefin in a reactor from one or more α-olefin monomers of which at least one is ethylene or propylene, wherein the reactor comprises a fluidized bed, an expanded section located at or near the top of the reactor, a distribution plate located at the lower part of the reactor and an inlet for a recycle stream located under the distribution plate wherein the process comprises—feeding a polymerization catalyst to the fluidized bed in the area above the distribution plate—feeding the one or more α-olefin monomers to the reactor—withdrawing the polyolefin from the reactor—circulating fluids from the top of the reactor to the bottom of the reactor, wherein the circulating fluids are compressed using a compressor and subsequently cooled using a heat exchanger to form a cooled recycle stream comprising liquid, and wherein the cooled recycle stream is introduced into the reactor using the inlet for the recycle stream wherein a part of the cooled recycle stream is drawn to form a liquid comprising stream, wherein the liquid comprising stream is introduced into the expanded section during at least part of the polymerization process, and wherein the liquid comprising stream is brought into contact with at least part of the interior surface of the expanded section.

用于烯烃聚合的方法

本发明涉及一种用于在反应器中由一种或多种α‑烯烃单体连续制备聚烯烃的方法，所述α‑烯烃单体中的至少一种是乙烯或丙烯，其中所述反应器包括流化床、位于所述反应器的顶部处或附近的膨胀区段、位于所述反应器的下部部分的分配板和位于所述分配板下方的再循环流的入口，其中所述方法包括‑将聚合催化剂进料到所述分配板上方区域中的流化床中‑将所述一种或多种α‑烯烃单体进料到所述反应器中‑从所述反应器中抽取出所述聚烯烃‑将流体从所述反应器的顶部循环至所述反应器的底部，其中所述循环流体使用热交换器冷却，产生包含液体的冷却的再循环流，并且其中将所述冷却的再循环流使用所述再循环流的入口引入到所述反应器中，其中在所述聚合方法的至少一部分期间，将包含热失控减少剂的流(含TRRA的流)引入到所述膨胀区段中，其中使所述含TRRA的流与所述膨胀区段的内表面的至少一部分接触。

用于烯烃聚合的方法

本发明涉及一种用于在反应器中由一种或多种α‑烯烃单体连续制备聚烯烃的方法，所述α‑烯烃单体中的至少一种是乙烯或丙烯，其中所述反应器包括流化床、位于所述反应器的顶部处或附近的膨胀区段、位于所述反应器的下部部分的分配板和位于所述分配板下方的再循环流的入口，其中所述方法包括‑将聚合催化剂进料到所述分配板上方的区域中的流化床中‑将所述一种或多种α‑烯烃单体进料到所述反应器中‑从所述反应器中抽取出所述聚烯烃‑将流体从所述反应器的顶部循环至所述反应器的底部，其中所述循环流体使用压缩机压缩并且随后使用热交换器冷却以形成包含液体的冷却的再循环流，并且其中将所述冷却的再循环流使用所述再循环流的入口引入到所述反应器中，其中将所述冷却的再循环流的一部分抽取出以形成含液体流，其中在所述聚合方法的至少一部分期间将所述含液体流引入到所述膨胀区段中，并且其中使所述含液体流与所述膨胀区段的内表面的至少一部分接触。

System for recovering entrained particles from an exhaust gas stream

Entrained particles from an exhaust gas stream may be removed from the gas stream with a device including a housing having a top, an inner surface, and a bottom with a hole passing therethrough, where the housing further includes an impact surface. An entrance pipe guides the exhaust gas stream into the housing toward the impact surface, and is arranged so that the entrance pipe has an inner diameter x; and the impact surface is separated from the opening of the entrance pipe by a distance y, wherein y is between 3x and ⅓x. An exit pipe guide the exhaust gas stream out of the housing. A receptacle is removably connected to the hole in the bottom of the housing. The impact surface diverts the exhaust gas stream from a first flow direction to a second flow direction, causing the entrained particles to fall from the exhaust gas stream into the receptacle before entering the exit pipe.

Desulfurization in turbulent fluid bed reactor

A method and apparatus for removing sulfur from a hydrocarbon-containing fluid stream wherein desulfurization is enhanced by improving the contacting of the hydrocarbon-containing fluid stream and sulfur-sorbing solid particulates in a fluidized bed reactor.