Fluid Bed Reactor with Staged Baffles

The invention relates to a process of alkylating aromatic hydrocarbons, and more particularly a process of making paraxylene by alkylation of benzene and/or toluene with methanol and/or dimethyl ether, and to an apparatus for carrying out said process, the improvement comprising staged injection of one of the reactants, with the stages separated by structured packing so as to minimize at least one of gas phase back-mixing, by-pass phenomena, and gas bubble size.

HEAT TREATING APPARATUS FOR POWDER PARTICLES AND METHOD OF PRODUCING TONER

A heat treating apparatus for powder particles including a cylindrical treating chamber; a powder particle-supplying unit; a hot air-supplying unit that supplies hot air for heat-treating powder particles; a cold air-supplying unit that supplies cold air for cooling the heat-treated powder particles; a regulating unit for regulating a flow of the supplied powder particles; and a recovering unit that recovers the heat-treated powder particles. The regulating unit is a substantially circular columnar member, the hot air-supplying unit has an outlet opposite to the upper end portion of the columnar member, and the regulating unit is equipped with a substantially conic distributing member for distributing the supplied hot air in a circumferential direction and a rotating member for rotating the distributed hot air in a spiral manner, on the center of the upper end portion. 1. A heat treating apparatus for powder particles each of which contains a binder resin and a colorant , the heat treating apparatus comprising:(1) a cylindrical treating chamber in which a heat treatment of the powder particles is performed,(2) a powder particle-supplying unit provided on an outer peripheral portion of the treating chamber, for supplying the powder particles to the treating chamber,(3) a hot air-supplying unit that supplies hot air for heat-treating the supplied powder particles to the treating chamber,(4) a cold air-supplying unit that supplies cold air for cooling the heat-treated powder particles to the treating chamber,(5) a regulating unit provided on the treating chamber, for regulating a flow of the supplied powder particles, and(6) a recovering unit provided at a lower end portion side of the treating chamber, that recovers the heat-treated powder particles, whereinthe regulating unit is a columnar member with a substantially circular cross-section and is arranged on a central axis of the treating chamber so as to be protruded from the lower end portion of the treating ...

REACTION DEVICE FOR PREPARING LIGHT OLEFINS FROM METHANOL AND/OR DIMETHYL ETHER

A reaction device for preparing light olefins from methanol and/or dimethyl ether, and more specifically relates to a reaction device for preparing light olefins from methanol and/or dimethyl ether, which mainly comprises a dense phase fluidized bed reactor (), a cyclone separator (), a stripper (), a lift pipe (), a dense phase fluidized bed regenerator (), a cyclone separator (), a stripper (), and a lift pipe (), wherein the dense phase fluidized bed reactor () is separated into n (n≧2) secondary reaction zones by a material flow controller (), and the dense phase fluidized bed regenerator () is separated into m (m≧2) secondary regeneration zones by the material flow controller (). 1. A reaction device for preparing light olefins from methanol and/or dimethyl ether comprising a dense phase fluidized bed reactor , a cyclone separator , a stripper , a lift pipe , a dense phase fluidized bed regenerator , a cyclone separator , a stripper , and a lift pipe; wherein a feeding line for reactor is connected to the bottom of the dense phase fluidized bed reactor; a part of the stripper is in the dense phase fluidized bed reactor , and the remaining part thereof is below the dense phase fluidized bed reactor; the bottom of the lift pipe is connected to the bottom of the stripper , and the top of the lift pipe is connected to the dense phase fluidized bed regenerator; a feeding line for regenerator is connected to the bottom of the dense phase fluidized bed regenerator; a part of the stripper is in the dense phase fluidized bed regenerator , and the remaining part thereof is below the dense phase fluidized bed regenerator; the bottom of the lift pipe is connected to the bottom of the stripper , and the top of the lift pipe is connected to the dense phase fluidized bed reactor , wherein a material flow controller is provided in the dense phase fluidized bed reactor and/or the dense phase fluidized bed regenerator , and the dense phase fluidized bed reactor is separated into ...

METHOD AND SYSTEM FOR THE TREATMENT OF MATERIALS

A system for the treatment of materials, to be selected from between materials in a fluid state () and particles suspended in a fluid material (), comprising at least one upper kinematic pair equipped with two mechanical elements (), said kinematic pair being in contact with a material in a fluid state () or with particles suspended in a fluid material (); motor means () to generate a pre-set relative velocity (v) between the elements () of said kinematic pair, and tensioning means () to subject said kinematic pair to a pre-set pressure (P). 1. A system for the treatment of materials , selected from between materials in a fluid state and particles suspended in a fluid material , comprising:at least one upper kinematic pair equipped with two mechanical elements, said kinematic pair being in contact with a material in a fluid state or in contact with particles suspended in a fluid material;motor means to generate a pre-set relative velocity (v) between the mechanical elements of said kinematic pair; andtensioning means to subject said kinematic pair to a pre-set contact pressure (p); characterised in that the upper kinematic pair is formed by at least one bearing equipped with rolling elements arranged between a moving ring and a fixed ring.2. The treatment system according to claim 1 , characterised in that the bearing comprises a cage for separating the rolling elements.3. The treatment system according to claim 1 , characterised in that it comprises at least one upper kinematic pair formed by a gear claim 1 , a cam-follower mechanism claim 1 , a chain-sprocket mechanism claim 1 , a chain transmission claim 1 , a belt transmission claim 1 , a cable transmission claim 1 , a pin-on-disk tribometer claim 1 , or a ball-on-disk tribometer.4. The treatment system according to claim 1 , characterised in that the upper kinematic pairs are housed in a chamber hermetically closed by a cover.5. The treatment system according to claim 4 , characterised in that the closed ...

SYSTEMS AND METHODS FOR CONVERTING CARBONACEOUS FUELS

A system for converting carbonaceous fuels is provided. The system includes a gaseous fuel conversion reactor, a solid fuel conversion reactor, and a fuel pretreatment fluidized bed reactor disposed between the gaseous fuel conversion reactor and the solid fuel conversion reactor. The fuel pretreatment fluidized bed reactor devolatilizes a solid fuel using heat to produce an off-gas and a devolatilized solid fuel. The gaseous fuel conversion reactor converts the off-gas from the fuel pretreatment fluidized bed reactor to a product gas stream comprising carbon dioxide and water. The solid fuel conversion reactor receives a mixture of oxygen carrier solids and devolatilized solid fuel from the pretreatment reactor discharge and reduces the devolatilized solid fuel with the oxygen carrier solids to convert the devolatilized solid fuel to an intermediate gas.

METHOD FOR FLUIDIZING COPPER SILICIDE AND PROCESS FOR PREPARING A HALOSILANE USING THE METHOD

A method is useful for maintaining a uniformly fluidized bed in a fluidized bed apparatus. The method includes the steps of charging a mixture of particles including copper silicide particles and fluidization additive particles into the fluidized bed apparatus, and uniformly fluidizing the particles at a temperature of at least 400° C. in the fluidized bed apparatus. 1. A method maintaining a uniformly fluidized bed in a fluidized bed apparatus comprises:(A) heating, at a temperature of at least 400° C., a mixture of particles comprising greater than 80 weight % to less than 100% copper silicide particles and greater than 0 to 20 weight % fluidization additive particles in the fluidized bed apparatus, and(B) feeding a fluid into the fluidized bed apparatus at a velocity sufficient to maintain uniform fluidization.2. The method of claim 1 , where the copper silicide particles have a particle size of 10 μm to 150 μm.3. The method of claim 1 , where the additive particles are present in an amount of greater than 0 weight % to 10 weight % claim 1 , based on total weight of the mixture.4. The method of claim 1 , where the copper silicide particles are present in an amount of 95 weight % to 98 weight % of the mixture claim 1 , and the fluidization additive particles are present in an amount of 2 weight % to 5 weight % of the mixture.5. The method of claim 1 , where the copper silicide is selected from the group consisting of (i) CuSi claim 1 , (ii) CuSi claim 1 , (iii) CuSi claim 1 , and (iv) CuSi claim 1 , and a mixture of two or more of (i) claim 1 , (ii) claim 1 , (iii) claim 1 , (iv).6. The method of claim 1 , where the copper silicide comprises CuSi.7. The method of claim 1 , where the copper silicide has empirical formula CuSiCrCoFeIrNiPdPtReRu claim 1 , where subscripts b claim 1 , c claim 1 , d claim 1 , e claim 1 , f claim 1 , g claim 1 , h claim 1 , i claim 1 , j claim 1 , k claim 1 , and m represent the molar amounts of each element present claim 1 , and b>0 ...

GAS DISTRIBUTION PLATE FOR THERMAL DEPOSITION

Apparatus and methods for providing high velocity gas flow showerheads for deposition chambers are described. The showerhead has a faceplate in contact with a backing plate that has a concave portion to provide a plenum between the backing plate and the faceplate. A plurality of thermal elements is within the concave portion of the backing plate and extends to contact the faceplate. 1. A gas distribution plate comprising:a faceplate having a front surface and a back surface defining a thickness and a plurality of apertures extending through the thickness; anda backing plate having a front surface and a back surface defining a thickness, the front surface in contact with the back surface of the faceplate, the front surface of the backing plate including a concave portion to form a plenum bounded by the concave portion and the back surface of the faceplate, and a plurality of thermal elements extending from a concave surface the concave portion and contacting the back surface of the faceplate.2. The gas distribution plate of claim 1 , wherein each of the thermal elements independently extends a length from the concave surface of the concave portion to a front surface of the thermal element.3. The gas distribution plate of claim 2 , wherein the front surfaces of the thermal elements are substantially coplanar.4. The gas distribution plate of claim 2 , wherein each of the thermal elements has a tapered profile with a flared base at the concave surface of the concave portion and a narrower end at the front surface.5. The gas distribution plate of claim 2 , wherein the backing plate has an outer peripheral edge and the concave portion has an outer peripheral edge.6. The gas distribution plate of claim 5 , wherein an outer front face ring defined as the front surface of the backing plate between the outer peripheral edge of the concave portion and the outer peripheral edge of the backing plate is substantially flat.7. The gas distribution plate of claim 6 , wherein the ...

Multiple Reactor and Multiple Zone Polyolefin Polymerization

Apparatuses and processes that produce multimodal polyolefins, and in particular, polyethylene resins, are disclosed herein. This is accomplished by using two reactors in series, where one of the reactors is a multi-zone circulating reactor that can circulate polyolefin particles through two polymerization zones optionally having two different flow regimes so that the final multimodal polyolefin has improved product properties and improved product homogeneity. 1. A trimodal polyethylene resin having a low molecular weight (LMW) component , an intermediate molecular weight (IMW) component , and a high molecular weight (HMW) component; wherein the LMW component is present in an amount of from about 20 wt. % to about 75 wt. %; wherein the IMW component is present in an amount of from about 5 wt. % to about 40 wt. %; wherein the LMW component has a weight average molecular weight of from about 20 kg/mol to about 150 kg/mol; wherein the IMW component has a weight average molecular weight of from about 85 kg/mol to about 350 kg/mol; wherein the weight average molecular weight of the IMW component is greater than the weight average molecular weight of the LMW component; wherein the weight average molecular weight of the HMW component is greater than the weight average molecular weight of the IMW component; wherein the trimodal polyethylene resin has a Young's modulus (E) of equal to or greater than about 900 MPa , when tested in accordance with ASTM D638; and wherein the trimodal polyethylene resin has a density of equal to or greater than about 0.952 g/cc , when tested in accordance with ASTM D1505.2. The trimodal polyethylene resin of claim 1 , wherein the trimodal polyethylene resin has a melt index of less than about 1 g/10 min claim 1 , when tested in accordance with ASTM D1238 under a force of 2.16 kg.3. The trimodal polyethylene resin of claim 1 , wherein the trimodal polyethylene resin has a density of equal to or greater than about 0.955 g/cc claim 1 , when tested ...

FLUIDIZED BED COOLER WITH REGIONAL COORDINATION ENHANCEMENT

The present disclosure discloses a fluidized bed cooler with regional coordination enhancement, comprising a shell, a catalyst inlet, an interior of the shell is divided into a catalyst inlet influence region, a dilute phase region, a dense phase region and a gas distributor influence region; a catalyst inlet inclined tube is provided obliquely upward at the catalyst inlet, and a regional particle distributor is provided at the catalyst inlet; the dense phase region is provided with a plurality of dense phase baffle plates, and the dilute phase region is provided with a plurality of dilute phase baffle plates; and the gas distributor influence region is provided with double gas distributors. The fluidized bed cooler simultaneously well solves the low internal stability and the low heat exchange efficiency of the fluidized bed cooler, thereby realizing the stable and efficient operation of the fluidized bed cooler. 1. A fluidized bed cooler with regional coordination enhancement , comprising a shell which is cylindrical and vertically provided , wherein a plurality of heat exchange tubes are vertically distributed in the shell , a catalyst inlet is provided at an upper portion of the shell , a catalyst outlet is provided at a bottom portion of the shell , and an interior of the shell is divided into a catalyst inlet influence region , a dilute phase region at the upper portion , a dense phase region at the lower portion and a gas distributor influence region at the bottom portion , and wherein the dilute phase region and the dense phase region are located above and below the catalyst inlet influence region , respectively , wherein a catalyst inlet inclined tube is provided obliquely upward at the catalyst inlet , and a regional particle distributor is provided at the catalyst inlet positioned in the catalyst inlet inclined tube;wherein the regional particle distributor comprises a local gas distribution plate, a local gas pre-distributor, a left splitter partition ...

JOINT DESIGN FOR SEGMENTED SILICON CARBIDE LINER IN A FLUIDIZED BED REACTOR

Segmented silicon carbide liners for use in a fluidized bed reactor for production of polysilicon-coated granulate material are disclosed, as well as methods of making and using the segmented silicon carbide liners. Non-contaminating bonding materials for joining silicon carbide segments also are disclosed. One or more of the silicon carbide segments may be constructed of reaction-bonded silicon carbide. 1. A segmented silicon carbide liner for a fluidized bed reactor for production of polysilicon-coated granulate material , comprising:a first silicon carbide segment having a first segment upper edge surface defining one of an upwardly opening first segment depression or an upwardly extending first segment protrusion;a second silicon carbide segment located above and abutted to the first silicon carbide segment, the second silicon carbide segment having a second segment lower edge surface defining a downwardly opening second segment depression if the first segment upper edge surface defines an upwardly extending first segment protrusion or a downwardly extending second segment protrusion if the first segment upper edge surface defines an upwardly opening first segment depression, the protrusion being received within the depression and having smaller dimensions than the depression such that the surface of the depression is spaced apart from the surface of the protrusion and a space is located between the protrusion and the depression; anda volume of bonding material comprising a lithium salt, the bonding material disposed within the space between the protrusion and the depression.2. The segmented silicon carbide liner of claim 1 , wherein:the first silicon carbide segment comprises a first tubular wall having an annular upper surface, the first segment upper edge surface being at least a portion of the annular upper surface, and the first segment depression is a groove that is defined by and extends along at least a portion of the first segment upper edge surface or ...

SYSTEM AND METHOD FOR PREVENTING CATALYST FROM OVERHEATING

A system for preventing a catalyst from overheating is provided. The system includes: a first reactor filled with a catalyst at least in part and configured to receive reaction gas and produce product gas; and a second reactor configured to cool a catalyst discharged from the first reactor. The catalyst is circulated between the first reactor and the second reactor by injecting the catalyst cooled in the second reactor into the first rector. 1. A system for preventing a catalyst from overheating , the system comprising:a first reactor filled with a catalyst at least in part and configured to receive reaction gas and produce product gas; anda second reactor configured to cool a catalyst discharged from the first reactor,wherein the catalyst is circulated between the first reactor and the second reactor by injecting the catalyst cooled in the second reactor into the first rector.2. The system of claim 1 , wherein the catalyst is a catalyst of a particle shape having a diameter ranging from 1 to 9 claim 1 ,000 micrometers.3. The system of claim 1 , further comprising a path of a first cooling fluid passing through the first reactor claim 1 , andwherein the catalyst in the first reactor is cooled by the first cooling fluid.4. The system of claim 1 , wherein the first reactor is a fluidized bed reactor and the product gas is produced in a state in which the catalyst in the first reactor is fluidized.5. The system of claim 1 , wherein the second reactor is filled with the catalyst discharged from the first reactor at least in part claim 1 , andwherein the system further comprises a path of a second cooling fluid passing through the second reactor.6. The system of claim 1 , further comprising a path to allow the reaction gas to pass through the second reactor claim 1 , andwherein the reaction gas passing through the path of the reaction gas is pre-heated and supplied to the first reactor.7. A method for preventing a catalyst from overheating claim 1 , the method comprising ...

CONTINUOUS GAS FLUIDIZED BED POLYMERIZATION PROCESS

The invention relates to a process for the preparation of a polyolefin in a reaction system from one or more α-olefin monomers of which at least one is ethylene or propylene, 5 wherein the reaction system comprises a reactor, a product purge bin, a granular feed bin, wherein the granular feed bin is located downstream of the product purge bin, a recovery unit and an extrusion unit directly coupled to the granular fed bin, 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 10 inlet for a recycle stream located under the distribution plate, wherein the process comprises a) feeding a polymerization catalyst to the fluidized bed in the area above the distribution plate, b) feeding the one or more α-olefin monomers to the reactor, 15 c) 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, d) withdrawing a stream comprising the polyolefin and fluids from the reactor and 20 passing said stream into the product purge bin, e) purging the product purge bin with a purge stream comprising a first inert gas, preferably nitrogen and steam such that a stream comprising a purged polyolefin and a stream comprising fluids, wherein the stream comprising the fluids is substantially free of steam, is obtained, 25 f) introducing at least part of the stream comprising the fluids back into the reactor via the recovery unit, g) introducing the stream comprising the purged polyolefin into the granular feed bin and h) contacting a deactivating stream comprising steam with the purged polyolefin in the 30 granular feed bin to obtain a polyolefin that is substantially free of active polymerization catalyst. 1. A process ...

FEEDSTOCKS FOR FORMING CARBON ALLOTROPES

Methods and systems are provided for forming carbon allotropes. An exemplary method includes forming a feedstock that includes at least about 10 mol % oxygen, at least about 10 mol % carbon, and at least about 20 mol % hydrogen. Carbon allotropes are formed from the feedstock in a reactor in a Bosch reaction at a temperature of at least about 500° C., and the carbon allotropes are separated from a reactor effluent stream. 1. A method for forming carbon allotropes , comprising:forming a feedstock comprising at least about 10 mol % oxygen, at least about 10 mol % carbon, and at least about 20 mol % hydrogen;forming carbon allotropes from the feedstock in a reactor in a Bosch reaction at a temperature of at least about 500° C.; andseparating the carbon allotropes from a reactor effluent stream.2. The method of claim 1 , comprising holding the temperature of the reactor to less than about 1000° C. during the Bosch reaction.3. The method of claim 1 , comprising holding the temperature between about 575° C. and 700° C.4. The method of claim 1 , comprising forming a forming a feedstock comprising at least about 20 mol % oxygen claim 1 , at least about 20 mol % carbon claim 1 , and at least about 40 mol % hydrogen.5. The method of claim 1 , comprising forming a forming a feedstock comprising at least about 15 mol % oxygen claim 1 , at least about 15 mol % carbon claim 1 , and at least about 60 mol % hydrogen.6. The method of claim 1 , comprising adding steam to the feedstock.7. The method of claim 1 , comprising forming the feedstock from a mixture comprising carbon dioxide and methane.8. The method of claim 1 , comprising forming the feedstock from a mixture comprising carbon dioxide claim 1 , carbon monoxide claim 1 , hydrogen claim 1 , and methane.9. The method of claim 1 , comprising:analyzing the feedstock to determine the composition; andmodifying the materials to control the ratio between the carbon, the hydrogen, and the oxygen.10. The method of claim 1 , comprising ...

PREPARATION DEVICE AND PREPARATION METHOD OF AMMONIA GAS

Disclosed are a preparation device and a preparation method of ammonia gas. The preparation device, prepares ammonia gas by reacting ammonium chloride with a particulate inorganic salt, includes one fluidized bed reactor with at least two fluidization chambers, in which one is a preheating chamber configured to preheat the particulate inorganic salt, and the other is a reaction chamber inside provided with at least one atomizing nozzle, the particulate inorganic salt forming a fluidized bed layer and reacting with an aqueous solution of ammonium chloride in the reaction chamber to generate the ammonia gas. The particulate inorganic salt can be sequentially flowed through a plurality of preheating chambers and reaction chambers under an impetus of a density difference of the particulate bed layers, finally achieving the required conversion rate. 1. A preparation device of ammonia gas , configured to prepare ammonia gas by reacting ammonium chloride with a particulate inorganic salt , comprising a fluidized bed reactor , the fluidized bed reactor comprising:at least one preheating chamber, configured to preheat the particulate inorganic salt;at least one reaction chamber, configured for the particulate inorganic salt to contact and react with an aqueous solution of ammonium chloride to generate the ammonia gas; andan atomizing nozzle, located in the reaction chamber, configured to atomize the ammonium chloride aqueous solution,wherein carrier gas is introduced into the preheating chamber and the reaction chamber to cause the particulate inorganic salt to form a fluidized particulate bed layer, and an empty bed gas velocity of the carrier gas in the preheating chamber is higher than an empty bed gas velocity of the carrier gas in the reaction chamber, so that a particulate bed layer density in the preheating chamber is smaller than a particulate bed layer density in the reaction chamber.2. The preparation device according to claim 1 , wherein the fluidized bed reactor ...

PROCESS AND PLANT FOR REFINING RAW MATERIALS CONTAINING ORGANIC CONSTITUENTS

A plant for refining raw materials containing organic constituents includes a reactor configured to receive raw materials; a furnace configured to receive solids and fuel from the reactor; a return conduit configured to recirculate hot solids generated in the furnace to the reactor; and a sealing device configured to separate an oxidizing atmosphere of the furnace from an atmosphere of the reactor. The sealing device includes: a downpipe disposed between the furnace and the reactor, the downpipe being configured to withdraw a stream of solids from the furnace; a rising pipe disposed near a bottom of the downpipe and branching off there from to a top, the rising pipe being configured to transport a fluidized stream of solids to the reactor; and a conveying gas supply disposed below the rising pipe, the conveying gas supply being configured to fluidize a stream of solids withdrawn from the furnace. 1. A plant for refining raw materials containing organic constituents , the plant comprising:a reactor configured to receive raw materials;a furnace configured to receive solids and fuel from the reactor;a return conduit configured to recirculate hot solids generated in the furnace to the reactor; a downpipe disposed between the furnace and the reactor, the downpipe being configured to withdraw a stream of solids from the furnace,', 'a rising pipe disposed near a bottom of the downpipe and branching off therefrom to a top, the rising pipe being configured to transport a fluidized stream of solids to the reactor, and', 'a conveying gas supply disposed below the rising pipe, the conveying gas supply being configured to fluidize a stream of solids withdrawn from the furnace., 'a sealing device configured to separate an oxidizing atmosphere of the furnace from an atmosphere of the reactor, the sealing device including2. The plant as recited in claim 1 , wherein the reactor is a fluidized-bed reactor.3. The plant as recited in claim 1 , further comprising at least one of a drier ...

SYSTEMS AND METHODS FOR REDUCING HEAT EXCHANGER FOULING RATE

Systems and methods of reducing heat exchanger fouling rate and of producing polyolefins are provide herein. In some aspects, the methods include providing a first gas stream comprising a gas and entrained fine polyolefin particles to a gas outlet line; preferentially removing a portion of the entrained fine polyolefin particles from the gas outlet line to form a bypass stream comprising a higher concentration of the entrained fine polyolefin particles than is present in the first gas stream; providing the bypass stream to a bypass line comprising a bypass line inlet and a bypass line outlet, wherein the bypass line inlet is located upstream of a first heat exchanger, and wherein the bypass line outlet is located downstream of the first heat exchanger; providing at least a portion of the first gas stream to the first heat exchanger, which produces a first cooled gas stream; and combining the bypass stream and a second gas stream at the bypass line outlet to form a combined gas stream comprising one or more olefins or paraffins, wherein a temperature of the combined gas stream is below the dew point of the combined gas stream. 1. A system for reducing heat exchanger fouling rate comprising:a gas outlet line configured to pass a first gas stream comprising a gas and entrained fine polyolefin particles;a first heat exchanger configured to receive at least a portion of the first gas stream and produce a first cooled gas stream; anda bypass line configured to remove a portion of the entrained fine polyolefin particles from the gas outlet line to form a bypass stream comprising a higher concentration of the entrained fine polyolefin particles than is present in the first gas stream, the bypass line comprising a bypass line inlet and a bypass line outlet,wherein the bypass line inlet is located upstream of the first heat exchanger,wherein the bypass line outlet is located downstream of the first heat exchanger, andwherein the bypass line is configured so that the bypass ...

Processes for producing light olefins

A process for producing light olefins is provided. A feedstock enters a pre-reaction zone and contacts a catalyst comprising at least one silicon-aluminophosphate molecular sieve and produces a gas-phase stream; the gas-phase stream and the catalyst enter at least one riser, and the gas-phase stream and the catalyst pass from an outlet of the at least one riser and enter a gas-solid rapid separation zone; the separated gas-phase stream enters a separation section; a first portion of the separated catalyst returns to the pre-reaction zone, and a second portion is regenerated in a regenerator; wherein an inlet of the at least one riser extends into the pre-reaction zone, about 60% to about 90% of the height of the at least one riser passes through a heat exchange zone, and the outlet extends into the gas-solid rapid separation zone.

PROCESS AND REACTOR FOR ARSENIC FIXATION

A process and reactor for arsenic fixation in which a first gas stream comprises oxygen and an iron-containing particulate material. The oxygen and particulate material may be fed to reactor through respective first and second inlets. A second gas stream containing one or more volatile arsenic compounds is fed through a third inlet and mixed with the first gas stream and the particulate material to produce a combined gas stream containing the volatile arsenic compounds and the particulate material. The arsenic compounds are reacted with iron in the particulate material as the combined gas stream flows through the reactor to produce solid iron arsenates which are then recovered. The portion of the reactor including the first, second and third inlets is vertically oriented, and the reactor may include a venturi arrangement having a throat at which the second inlet is located. 125.-. (canceled)26. A process for arsenic fixation , comprising:(a) providing a reactor having an internal space;(b) providing a first gas stream in said internal space, wherein the first gas stream comprises oxygen and an iron-containing particulate material;(c) providing a second gas stream in said internal space, wherein the second gas stream comprises one or more arsenic species;(d) mixing the first gas stream and the second gas stream in said internal space to produce a combined gas stream;(e) reacting the one or more volatile arsenic compounds, the iron-containing particulate material and the oxygen in the combined gas stream to produce solid iron arsenates in the combined gas stream; and(f) separating the solid iron arsenates from the combined gas stream.27. The process according to claim 26 , wherein the internal space of the reactor has a first end and a second end claim 26 , with a gas flow direction being defined from the first end to the second end.28. The process according to claim 27 , wherein at least a portion of the internal space is oriented vertically claim 27 , wherein the ...

METHOD FOR PROCESSING FINE PARTICLES WITH A SPOUTED BED REACTOR

One or more embodiments relate to a contactor/separator vessel for reacting with fine particles. The contractor/separator vessel includes a spouted bed containing fine Geldart class C particles; and an additional spoutable media to facilitate spouting of the fine Geldart class C particles in order to improve mixing, gas-solid contact/separation. 1. A contactor/separator vessel for reacting with fine particles , comprising:a spouted bed containing fine Geldart class C particles; andan additional spoutable media to facilitate spouting of the fine Geldart class C particles in order to improve mixing, gas-solid contact/separation.2. The vessel of comprising a chemical reactor wherein a temperature varies between about 150° C. and 1000° C.3. The vessel of wherein the chemical reactor uses a gas distributor and a spout to assist with at least one of fluidization claim 2 , flow rate and material transport.4. The vessel of wherein a gas distributed through the gas distributor is pulsed.5. The vessel of further comprising multiple spouting beds are adjoined.6. The vessel of wherein the multiple spouting beds are adjoined in a stacked pattern.7. The vessel of wherein the multiple spouting beds are adjoined in a modular pattern.8. The vessel of wherein the multiple spouting beds are thermally controlled using heating chambers.9. The vessel of wherein the multiple spouting beds are thermally controlled using cooling chambers.10. The vessel of wherein the spouted bed includes an angle of a spout bottom wherein an angle of the spotted bottom ranges from a horizontal to vertical orientation.11. The vessel of having an internal design and operation promoting mixing and gas-solid contact.12. The vessel of having one or more pairs of parallel plates or tubes aligned axially in the vessel to stabilize a gas jet to improve spouting stability claim 1 , facilitate increased solids inventory as well as promoting operation as lower gas velocities.13. A chemical reactor for reacting with ...

Method Of Making Oxygenates From A Non-Catalytic Chemical Reaction

A system and a method for forming oxygenates from a non-catalytic reaction. A hydrocarbon gas and an oxygen-containing gas are fed into a mixer and then heated to form a reactant gas stream. The reactant gas stream is fed into a fluidized bed reactor where the reaction of the gases occurs by oxidization to produce oxygenates. The oxygenate products are then removed from the reactor.

REACTOR COMPONENT PLACEMENT INSIDE LINER WALL

Reaction chamber liners for use in a fluidized bed reactor for production of polysilicon-coated granulate material are disclosed. The liners include an aperture and a cavity configured to receive a reactor component, such as a probe, a sensor, a nozzle, a feed line, a sampling line, a heating/cooling component, or the like. In some embodiments, the liner is a segmented liner comprised of vertically stacked or laterally joined segments, wherein at least one segment includes an aperture and a cavity configured to receive a reactor component. 1. A reaction chamber liner for use in a fluidized bed reactor for production of polysilicon-coated granulate material , the liner comprising:{'sub': W', 'W, 'a tubular wall having an upper surface, a lower surface, an outwardly facing surface, an inwardly facing surface configured to define a portion of a reaction chamber, a height Hbetween the upper surface and the lower surface, and a thickness Tbetween the outwardly facing surface and the inwardly facing surface,'}{'sub': 'C', 'the tubular wall defining an upper aperture in the upper surface and a cavity that extends from the upper aperture toward the lower surface and that has a depth D.'}2. The reaction chamber liner of claim 1 , wherein the depth Dof the cavity is less than the height Hof the tubular wall.3. The reaction chamber liner of claim 1 , wherein the depth Dof the cavity is equal to the height Hof the tubular wall claim 1 , and the tubular wall defines a lower aperture such that the cavity extends through the tubular wall from the upper aperture to the lower aperture.4. The reaction chamber liner of claim 1 , wherein the cavity has an inner dimension ID between the outwardly facing surface and the inwardly facing surface of the tubular wall that is smaller than the thickness Tof the tubular wall claim 1 , and the cavity is positioned between the outwardly facing surface and the inwardly facing surface of the tubular wall.5. The reaction chamber liner of claim 1 , ...

Continuous Preparation of Calcined Chemically-Treated Solid Oxides

The present invention discloses a continuous calcination vessel which can be used to prepare calcined chemically-treated solid oxides from solid oxides and chemically-treated solid oxides. A process for the continuous preparation of calcined chemically-treated solid oxides is also provided. Calcined chemically-treated solid oxides disclosed herein can be used in catalyst compositions for the polymerization of olefins. 1. A continuous calcination vessel comprising:(a) a fluidized bed vessel having a slope from horizontal in a range from about 5 degrees to less than about 15 degrees;(b) a particulate material inlet capable of introducing inlet particulate material into the fluidized bed vessel;(c) a fluidizing gas inlet capable of introducing a fluidizing gas into the fluidized bed vessel;(d) a fluidizing gas path capable of directing the fluidizing gas from the fluidizing gas inlet into the fluidized bed vessel to fluidize the inlet particulate material;(e) a heating zone within the fluidized bed vessel; and(f) an outlet capable of removing outlet particulate material from the fluidized bed vessel.2. The continuous calcination vessel of claim 1 , wherein the inlet particulate material comprises a solid oxide claim 1 , a chemically-treated solid oxide claim 1 , or a combination thereof.3. The continuous calcination vessel of claim 1 , wherein the outlet particulate material comprises a calcined chemically-treated solid oxide.4. The continuous calcination vessel of claim 1 , wherein the heating zone comprises at least one baffle claim 1 , and wherein the fluidized bed vessel contains sufficient baffles to cause a substantially plug flow profile through the fluidized bed vessel.5. The continuous calcination vessel of claim 1 , further comprising a filter apparatus adapted to remove a portion of the inlet particulate material and/or the outlet particulate material entrained in the fluidizing gas.6. The continuous calcination vessel of claim 1 , further comprising a ...

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 FOR HEATING CATALYST 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 regenerator for regenerating a first catalyst stream to produce a regenerated first catalyst stream and a first flue gas stream;a reactor vessel comprising a feed inlet, a catalyst outlet in the reactor vessel and a catalyst inlet to the reactor vessel above the catalyst outlet;a hopper in said regenerator in downstream communication with said catalyst outlet, said hopper having a bottom closed to an interior of said regenerator and a top open to said interior of said regenerator;said catalyst inlet to the reactor vessel being in communication with said hopper;an air heater located outside of said regenerator, and said hopper being in downstream communication with said air heater; anda riser in downstream communication with said catalyst outlet and said air heater at a first end, and said hopper being in downstream communication with a second end of said riser.2. The reactor apparatus of further comprising a first outlet for said regenerated first catalyst stream in said regenerator and a second claim 1 , separate outlet for said second catalyst stream in said regenerator.3. The reactor apparatus of further comprising a single flue gas outlet from said regenerator.4. The reactor apparatus of further comprising a side wall of said hopper being closed to an interior of said regenerator.56-. (canceled)7. The reactor apparatus of wherein said regenerator comprises a lower chamber and an upper chamber and said hopper is in said upper chamber.8. The reactor apparatus of wherein said riser is in ...

HYDROPROCESSING SYSTEM WITH IMPROVED COOLING LIQUID ATOMIZATION

A hydroprocessing system having a processing vessel that discharges a high temperature effluent that must be cooled prior to collection in a reflux drum. One or more gas assisted spray nozzle are provided that utilize light atomizing gas having a density of 8-15 times less than air, such as hydrogen, which preferably is the processing or recycle gas of the system. The spray nozzles are designed for the efficient atomization and direction of cooling water into a micron sized droplet distribution utilizing the light atomizing gas for affecting higher mass and heat transfer from the effluent. The spray nozzles each include a unique atomizing gas and cooling liquid passageway systems, a downstream impingement post, and a plurality of discharge orifices which sequentially breakdown the liquid into micron sized droplets as low as 500 microns and less. 1. A hydroprocessing system comprising:a processing vessel having a hydrocarbon inlet coupled to a hydrocarbon supply for directing hydrocarbon into the processing vessel,said processing vessel having a process gas inlet coupled to a light process gas supply for directing light process gas into said processing vessel;said processing vessel having a vapor outlet for directing high temperature vapor from the processing vessel to a vapor discharge line for direction to an effluent cooler;a spraying system for directing atomized cooling water into the high temperature vapor directed through said vapor discharge line;said spraying system including a spray nozzle having an atomizing gas inlet coupled to a light gas supply and a water inlet coupled to a cooling water supply;said nozzle body having an internal protrusion extending downstream within an enlarged diameter expansion chamber of said nozzle body, said protrusion having a central gas passage communicating with said atomizing gas inlet and spray nozzle light gas supply;said protrusion having a plurality of circumferentially spaced cross gas passages communicating with said ...

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 ...

Pilot Plant Scale Semi-Condensing Operation

A process for testing a commercial polyolefin condensed mode operation on a pilot plant scale is provided. A feed stream including one or more olefin monomers and one or more inert fluids can be introduced to a fluidized bed contained within a reactor housing having a length to diameter ratio of 1.0 to 20. The one or more olefin monomers can be contacted with one or catalysts within the fluidized bed at conditions sufficient to produce a polyolefin. A cycle gas stream can be withdrawn from the housing, the cycle gas stream having a gas velocity of 1.0 ft/sec to 3.0 ft/sec and including the unreacted monomers and the inert fluids. The cycle gas stream can be compressed to a pressure above the reaction pressure within the housing. The cycle gas stream can be cooled to a temperature that is above the dew point of the cycle gas, and a portion of the compressed cycle gas stream can be removed to create a side stream of the compressed cycle gas stream. The side stream can be cooled to a temperature that is below its dew point to create a gas-liquid mixture, and the cycle gas stream and the cooled side stream including the gas-liquid mixture can be returned to the reactor housing. 1. A process for testing a commercial polyolefin condensed mode operation on a pilot plant scale , comprising:flowing a feed stream comprising one or more olefin monomers and one or more inert fluids through a fluidized bed contained within a reactor housing having a length to diameter ratio of 1.0 to 20;contacting the one or more olefin monomers with one or catalysts within the fluidized bed at conditions sufficient to produce a polyolefin;withdrawing a cycle gas stream from the housing, the cycle gas stream having a gas velocity of 1.0 ft/sec to 3.0 ft/sec and comprising the unreacted monomers and the inert fluids;compressing the cycle gas stream to a pressure above the reaction pressure within the housing;cooling the cycle gas stream to a temperature that is above the dew point of the cycle ...

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.

FLUIDIZED BED REACTOR HEATER

This invention is a heater used to heat the feed process gas from 450° C. to greater than about 600° C. for the fluidized bed reactor (FBR) used for conversion of silicon tetrachloride (STC) to trichlorosilane (TCS). The invention involves stacked heater element carbon plates. The design of the plates allow the plates to act as baffles which improve heat transfer to the feed gas. Also, the heat gradients across each plate is calculated to be approximately 100° C. which is much lower than the gradient seen by conventional vertical heater elements. The design of the present invention prevents electrical grounding. In the design, the elements are surrounded by graphite wrapped in carbon felt to prevent heat loss by radiation and conduction. 1. An apparatus for producing trichlorosilane comprising:a reactor;a raw material supply device that supplies metallurgical grade silicon powder as raw material to the reactor;a gas introduction device that introduces a feed gas, comprising at least a hydrogen gas and STC, to the reactor so that the hydrogen gas and STC reacts with the metallurgical grade silicon powder while the metallurgical grade silicon powder is fluidized by the hydrogen gas and STC;a heater of stacked heater element carbon plates for heating the feed gas before contact with the metallurgical grade silicon power; anda gas discharge device that discharges generated gas containing trichlorosilane from the reactor.2. The apparatus of claim 1 , wherein the heater element stacked carbon plates act as baffles for the feed gas.3. The apparatus of claim 1 , wherein the heater element stacked carbon plates are surrounded by graphite wrapped in carbon felt to prevent heat loss by radiation and conduction.4. The apparatus of claim 1 , where the gradient across each heater element stacked carbon plate is approximately 100° C.5. The apparatus of claim 1 , wherein each heater element stacked carbon plate has an alignment hole on each opposing side of the carbon plate for ...

PROCESS FOR THE LARGE-SCALE MANUFACTURE OF ZEOLITE-TEMPLATED CARBON

A method for the large-scale synthesis of a zeolite-templated carbon (ZTC). The method includes the steps of: introducing a bed material comprising a zeolite to a fluidized bed reactor and heating the bed material to a temperature between 550° C. and 800° C.; fluidizing the bed material with a fluidizing gas and maintaining the temperature of the bed material between 550° C. and 800° C.; introducing an organic carbon precursor while fluidizing the zeolite for a period of time such that carbon is deposited on the zeolite by chemical vapor deposition to produce a zeolite-carbon composite; and treating the zeolite-carbon composite with an acid solution such that the zeolite template is dissolved and the ZTC is obtained. 1. A method for large-scale synthesis of a zeolite-templated carbon (ZTC) , the method comprising the steps of:introducing a bed material comprising a zeolite to a fluidized bed reactor and heating the bed material to a first temperature between 550 degrees Celsius (° C.) and 800° C.;fluidizing the bed material with a fluidizing gas and maintaining the temperature of the bed material between 550° C. and 800° C.;introducing an organic carbon precursor while fluidizing the zeolite for a first period of time such that carbon is deposited on the zeolite by chemical vapor deposition to produce a zeolite-carbon composite;treating the zeolite-carbon composite with an acid solution such that the zeolite is dissolved and the ZTC is obtained.2. The method of claim 1 , wherein at least 100 grams of the ZTC is obtained.3. The method of claim 1 , wherein the fluidizing gas has an average gas velocity in the fluidized bed reactor that is between 5 centimeters per second (cm/s) and 25 cm/s.4. The method of claim 1 , wherein the step of fluidizing the bed material further comprises introducing the fluidizing gas such that the bed material is fluidized in a bubbling fluidization regime.5. The method of claim 1 , wherein the zeolite is a bead-type zeolite having a ...

DELTA TEMPERATURE CONTROL OF CATALYTIC DEHYDROGENATION PROCESS REACTORS

A chemical plant or a petrochemical plant or a refinery may include one or more pieces of equipment that process one or more input chemicals to create one or more products. For example, catalytic dehydrogenation can be used to convert paraffins to the corresponding olefin. A delta temperature controller may determine and control differential temperature across the reactor, and use a delta temperature to control a set point for a heater temperature controller. By doing so, the plant may ramp up a catalytic dehydrogenation unit faster and ensure it does not coke up the catalyst and/or foul a screens too quickly. Catalyst activity may be taken into account and allow the plant to have better control over production and run length of the unit. 1. A system comprising:at least two sensors configured to measure operating information in a catalytic reactor unit, wherein the at least two sensors comprise at least one reactor inlet temperature sensor and at least one reactor outlet temperature sensor; one or more processors of the data collection platform; and', receive sensor data collected by the at least two sensors, the sensor data comprising reactor inlet temperature data and reactor outlet temperature data;', 'correlate the sensor data with metadata comprising time data; and', 'transmit the sensor data;, 'memory of the data collection platform, storing computer-readable instructions that, when executed, cause the data collection platform to], 'a data collection platform comprising one or more processors of the data analysis platform; and', receive the sensor data from the data collection platform;', 'use the sensor data to determine a delta temperature based on the reactor inlet temperature data and reactor outlet temperature data; and', 'based on the delta temperature, transmit a command for an adjustment to an operating temperature of a heater of the catalytic reactor unit;, 'memory of the data analysis platform, storing computer-readable instructions that, when ...

PRODUCTION OF AROMATIC HYDROCARBONS

A process for producing aromatic hydrocarbons from a light alkane feedstock such as an ethane-containing hydrocarbon stream is disclosed. The process comprises: contacting a light alkane feedstock comprising at least 50% ethane with a bi-functional aromatization catalyst in a fluidized bed reactor of bubbling or turbulent fluidization regime. The fluidized bed reactor comprise a catalyst bed, catalytic combustor and internal heat exchanger tubes embedded in the catalyst bed to provide the heat supply necessary for production of aromatic hydrocarbons. Continuous and uninterrupted production of aromatic hydrocarbons is realized by fluidly connecting multiple reactors in parallel and cycling operation of individual reactors between aromatics production mode and catalyst regeneration mode. 1. A process for producing aromatic hydrocarbons comprising:feeding a light alkane feedstock comprising at least 50% ethane by weight into a fluidized bed reactor, and wherein the fluidized bed reactor comprises a catalyst bed, a heat exchanger embedded in the catalyst bed, and a catalytic combustor inside the heat exchanger,', 'wherein the catalyst bed comprises a bi-functional catalyst, and', 'wherein the bi-functional catalyst comprises a dehydrogenation catalyst and a solid acid catalyst., 'contacting the feedstock with a catalyst bed at a temperature of less than 620° C. and a pressure between 0-200 psig to produce a reactor effluent stream comprising aromatic hydrocarbons,'}2. The process of further comprising:separating the reactor effluent stream into an aromatic hydrocarbons stream and a gaseous products stream;separating the gaseous products stream into a fuel gas stream containing hydrogen and methane and a hydrocarbon recycle stream containing C2, C3, C4, and C5 hydrocarbons;recycling the fuel gas stream for heat generation; andrecycling the hydrocarbon recycle stream into the light alkane feedstock.3. The process of claim 1 , wherein the fluidized bed reactor is operated ...

PROCESS AND APPARATUS FOR FLUIDIZING A CATALYST BED

A process and apparatus for fluidizing a catalyst cooler with fluidization gas fed to the cooler below the catalyst bed is disclosed. Fluidization headers extend through an outlet manifold and deliver fluidization gas through distributors protruding through an outlet tube sheet defining said outlet manifold. The outlet manifold collects heated water vapor from the catalyst cooler and discharges it from the catalyst cooler. 1. A process for fluidizing a bed of catalyst in a catalyst cooler comprising internals and said bed of catalyst:passing water from a water manifold to an inner tube;heating water in said inner tube by indirect heat exchange with said bed of catalyst to vaporize at least some of the water;passing vaporized water to an outer tube nested around said inner tube;collecting said vaporized water in an outlet manifold;feeding fluidizing gas to said catalyst cooler through an inlet located below said bed of catalyst and distributing said fluidizing gas to said bed of catalyst to fluidize said bed of catalyst.2. The process of further comprising a plurality of inner tubes and a plurality of outer tubes are respectively nested around a respective inner tube and water is passed from the water manifold to said plurality of inner tubes and vaporized water is passed from said outer tubes to said outlet manifold.3. The process of further comprising feeding said fluidizing gas to said catalyst cooler through a header that supplies fluidization distributors.4. The process of further comprising passing fluidizing gas from said header to said bed of catalyst between said outer tubes.5. The process of further comprising feeding said fluidizing gas through said header in said outlet manifold.6. The process of further comprising heating said fluidizing gas by indirect heat exchange with said vaporized water in said outlet manifold.7. The process of further feeding water to said water manifold and vaporized water exits from said outlet manifold.8. The process of further ...

FLUIDIZED BED REACTOR FOR PRODUCTION OF GRANULAR POLYCRYSTALLINE SILICON

A subject of the invention is a fluidized-bed reactor for producing granular polycrystalline silicon. The fluidized-bed reactor comprises a segmented reactor tube, which is disposed between a reactor top and a reactor bottom, a heating facility, at least one nozzle for supplying fluidizing gas, at least one nozzle for supplying reaction gas, a facility for supplying silicon seed particles, a product removal line, and an offgas removal line. The segmented reactor tube comprises a base segment and at least one spacer segment, there being disposed, between base segment and spacer segment, a flat seal made from a carbon-containing material, the spacer segment consisting of a material which, within a temperature range from to ° C., has a thermal conductivity of <2 W/mK. 115-. (canceled)16. A granular polycrystalline silicon fluidized-bed reactor , comprising:a segmented reactor tube disposed between a reactor top and a reactor bottom, one or more heaters, at least one nozzle for supplying fluidizing gas, at least one nozzle for supplying silicon-containing reaction gas, a silicon seed particle feed, a product removal line, and an off gas removal line, wherein the reactor tube comprises a base segment and at least one spacer segment, there being disposed, between base segment and spacer segment, a flat seal of a carbon-containing material, the spacer segment constructed of a material which, within a temperature range from 100 to 950° C., has a thermal conductivity of <2 W/mK.17. The fluidized-bed reactor of claim 16 , wherein the material of the spacer segment comprises fused silica.18. The fluidized-bed reactor of claim 16 , wherein the base segment consists of a material which claim 16 , within a temperature range from 500 to 1400° C. claim 16 , has a thermal conductivity of between 20 and 100 W/mK.1915. The fluidized-bed reactor of claim claim 16 , wherein at least one material of the base segment is selected from the group consisting of silicon claim 16 , silicon ...

METHOD AND DEVICE FOR PROCESSING A MIXTURE OF RECYCLED POLYESTER MATERIAL AND A POLYESTER PREPOLYMER FROM A POLYESTER MANUFACTURING PROCESS

A method for processing a mixture of recycled polyester material and a polyester prepolymer from a polyester manufacturing process, wherein a recycled polyester material is mixed with a polyester prepolymer, from a polyester manufacturing process, and treated in a bulk thermal treatment reactor () with a process gas which flows in a counter-current or a cross-current flow direction to the flow direction of the mixture. In this process, the process gas, before entering a catalyst vessel (), is passed through a protective bed () containing a solid adsorbent material that removes high-boiling organic substances or organic substances, with a high combustion temperature, from the process gas stream. 115.-. (canceled)16. A method for processing a mixture of recycled polyester material and a polyester prepolymer from a polyester manufacturing process , comprising the following steps:blending said recycled polyester material with said polyester prepolymer from the polyester manufacturing process to produce a mixture of solids;treating this mixture of solids in a reactor for thermal treatment of bulk materials with a process gas in counter-current or cross-current to a flow direction of the mixture;introducing the process gas, containing organic impurities, into at least one heat exchanger to heat the process gas, and heating the process gas in said heat exchanger,controlling supply of an oxygen-containing gas to the process gas,introducting the process gas mixed with the oxygen-containing gas into a catalyst vessel with at least one catalyst bed arranged therein, through which the process gas flows from an inlet side to an outlet side of said catalyst vessel,combusting the organic impurities in the process gas in the at least one catalyst bed,at least partial recirculation of the process gas,wherein before entering the catalyst vessel, passing the process gas through a protective bed containing a solid adsorbent material, arranged upstream of the heat exchanger for heating ...

Multiple Reactor and Multiple Zone Polyolefin Polymerization

Apparatuses and processes that produce multimodal polyolefins, and in particular, polyethylene resins, are disclosed herein. This is accomplished by using two reactors in series, where one of the reactors is a multi-zone circulating reactor that can circulate polyolefin particles through two polymerization zones optionally having two different flow regimes so that the final multimodal polyolefin has improved product properties and improved product homogeneity. 120.-. (canceled)21. An apparatus for producing a multimodal polyolefin , comprising:a first reactor configured to produce a first polyolefin; a riser configured to produce the second polyolefin;', 'an upper conduit having an end fluidly connected to a top portion of the riser;', 'a separator fluidly connected to an opposite end of the upper conduit;', 'a downcomer configured to produce the third polyolefin, wherein a top portion of the downcomer is fluidly connected to the separator, optionally via a liquid barrier in the top portion of the downcomer; and', 'a lower conduit having an end fluidly connected to a bottom portion of the downcomer and an opposite end fluidly connected to a bottom portion of the riser,, 'a second reactor configured to produce a second polyolefin and a third polyolefin, where the second reactor comprises the second reactor is configured to receive the first polyolefin from the first reactor, or,', 'the first reactor is configured to receive the second polyolefin and the third polyolefin from the second reactor., 'wherein22. The apparatus of claim 21 , further comprising:a heat apparatus configured to add or remove heat from the downcomer.23. The apparatus of claim 21 , wherein the second reactor further comprises:a first elbow connector connected to the bottom portion of the riser and to the opposite end of the lower conduit;a second elbow connector connected to the top portion of the riser and to the end of the upper conduit; anda third elbow connector connected to the bottom ...

Multiple Reactor and Multiple Zone Polyolefin Polymerization

Apparatuses and processes that produce multimodal polyolefins, and in particular, polyethylene resins, are disclosed herein. This is accomplished by using two reactors in series, where one of the reactors is a multi-zone circulating reactor that can circulate polyolefin particles through two polymerization zones optionally having two different flow regimes so that the final multimodal polyolefin has improved product properties and improved product homogeneity.

MULTIPLE REACTOR AND MULTIPLE ZONE POLYOLEFIN POLYMERIZATION

Apparatuses and processes that produce multimodal polyolefins, and in particular, polyethylene resins, are disclosed herein. This is accomplished by using two reactors in series, where one of the reactors is a multi-zone circulating reactor that can circulate polyolefin particles through two polymerization zones optionally having two different flow regimes so that the final multimodal polyolefin has improved product properties and improved product homogeneity. 15-. (canceled)6. A trimodal polyethlene resin having a low molecular weight (LMW) component , an intermediate molecular weight (IMW) component , and a high molecular weight (HMW) component; wherein the LMW component is present in an amount of from about 20 wt. % to about 75 wt. %; wherein the IMW component is present in an amount of from about 5 wt. % to about 40 wt. %; wherein the LMW component has a weight average molecular weight of from about 20 kg/mol to about 150 kg/mol; wherein the IMW component has a weight average molecular weight of from about 85 kg/mol to about 350 kg/mol; wherein the weight average molecular weight of the IMW component is greater than the weight average molecular weight of the LMW component; wherein the weight average molecular weight of the HMW component is greater than the weight average e molecular weight of the IMW component; and wherein the trimodal polyethylene resin has a strain hardening modulus of from about 50 MPa to about 90 MPa , when tested in accordance with ISO 18488-2015(E) ,wherein (A1) the HMW component is present in an amount of from about 10 wt. % to about 60 wt. %; (A2) the HMW component has weight average molecular weight of great than about 350 kg/mol; or (A3) both the HMW component is present in an amount of from about 10 wt. % to about 60 wt. %, and the HMW component has weight average molecular weight of greater than about 350 kg/mol;wherein the trimodal polyethylene resin is characterized by (B1) a short chain branching content in the LMW component of ...

MULTIPLE REACTOR AND MULTIPLE ZONE POLYOLEFIN POLYMERIZATION

Apparatuses and processes that produce multimodal polyolefins, and in particular, polyethylene resins, are disclosed herein. This is accomplished by using two reactors in series, where one of the reactors is a multi-zone circulating reactor that can circulate polyolefin particles through two polymerization zones optionally having two different flow regimes so that the final multimodal polyolefin has improved product properties and improved product homogeneity. 18-. (canceled)9. A trimodal polyethylene resin having a low molecular weight (LMW) component , an intermediate molecular weight (IMW) component , and a high molecular weight (HMW) component; wherein the LMW component is present in an amount of from about 20 wt. % to about 75 wt. %; wherein the LMW component is present in an amount of from about 5 wt. % to about 40 wt. %; wherein the LMW component has a weight average molecular weight of from about 20 kg/mol to about 150 kg/mol; wherein the IMW component has a weight average molecular weight of from about 85 kg/mmol to about 350 kg/mol; wherein the weight average molecular weight of the IMW component is greater than the weight average molecular weight of the LMW component; wherein the weight average molecular weight of the HMW component is greater than the weight average molecular weight of the IMW component; and wherein the trimodal polyethylene resin has a tensile strength in the machine direction (MD) of greater than about 13 ,000 psi (89.6 MPa) , when tested in accordance with ASTM D638 at 90 MPa;wherein (A1) the HMW component is present in an amount of from about 10 wt. % to about 60 wt. %; (A2) the HMW component has weight average molecular weight of greater than about 350 kg/mol; or (A3) both the HMW component is present in an amount of from about 10 wt. % to about 60 wt. %, and the HMW component has weight average molecular weight of greater than about 350 kg/mol;wherein the trimodal polyethylene resin is characterized by (B1) a short chain branching ...

GASIFIER GRID COOLING SAFETY SYSTEM AND METHODS

An apparatus for cooling a gas distribution grid of fluidized bed gasifier and a method is provided in the present invention. The apparatus comprises a gas flow failure event detector for detecting a gasifying gas flow failure event, a flow control device for controlling the introduction of a flow stream of a liquid material into a spaying device placed in the plenum space of the gasifier, wherein the gas flow failure event detector is in signal connection with the flow control device, and a spaying device for spaying into the plenum space the liquid material as mist which evaporates and generates a positive pressure to cause through the gas distribution grid a flow which prevents the hot bed material from settling on the gas distribution grid. 1. An apparatus for cooling a gas distribution grid of fluidized bed gasifier , wherein the fluidized bed gasifier comprises a vessel housing a headspace above a fluidized bed of a solid materials being gasified , a gas distribution grid below the bed through which the gasifying gas flow is introduced to fluidize the solid materials in the gasifier , and a plenum space underneath the gas distribution grid , the apparatus comprising:a gas flow failure event detector for detecting a gasifying gas flow failure event,a flow control device for controlling the introduction of a flow stream of a liquid material into a spaying device placed in the plenum space when a gasifying gas flow failure event is detected, wherein the gas flow failure event detector is in signal connection with the flow control device,a spaying device for spaying into the plenum space the liquid material as mist which evaporates and generates a positive pressure to cause, through the gas distribution grid, a flow which prevents the hot bed material from settling on the gas distribution grid.2. The apparatus according to claim 1 , wherein the flow control device stops the introduction of the flow stream into the plenum space when the gasifying gas flow failure ...

Synthesis of Methyl Carbamate and Dimethyl Carbonate (DMC) in Presence of Stripping with Inert Gas or Superheated Vapours and a Reactor for the Same

The invention relates to synthesis of methyl carbamate (MC) and dimethyl carbonate (DMC) in presence of stripping inert gas or superheated methanol vapors using packed column reactor and bubble column reactor. 1. A horizontal sectionalized bubble column reactor for synthesis of methyl carbamate and dimethyl carbonate (DMC) comprising:a. a cylindrical bubble column reactor with single or multiple compartments to receive liquid reactant feed comprising of urea and methanol or methyl carbamate and methanol through inlet ports for a reaction to occur;b. a gas distributor chamber located within the cylindrical bubble column reactor comprising a plate intersecting a cylinder of the cylindrical bubble column reactor with or without an angle to an axis of the cylinder;c. single or multiple inlet ports fitted to the gas distributor chamber for distributing gas;d. single or multiple inlet ports fitted with a constant pressure regulator, single or multiple gas/vapor outlet ports fitted with a back pressure regulator for gaseous phase, wherein, a pressure difference of 10 psi is maintained to ensure positive flow of inert gas into the cylindrical bubble column reactor;e. single or multiple liquid outlet ports with an in-line filter fitted to the cylindrical bubble column reactor for liquid phase withdrawal;f. a heat transfer device fitted to the cylindrical bubble column reactor for maintaining temperature of the reaction;g. a condenser and a gas-liquid separator fitted to the outlet port(s) wherein a product in vapor form is condensed and separated from liquid components;h. an outlet for condensate and an outlet for non-condensate connected to the gas-liquid separator.2. The horizontal sectionalized bubble column reactor as claimed in claim 1 , wherein the cylindrical bubble column reactor further comprises an expanded slurry bed of solid catalyst particles suspended in a suspension liquid or in a packed bed of solid catalyst.3. The horizontal sectionalized bubble column ...

FLUIDIZED-BED REACTOR HAVING MULTIPLE RECYCLE GAS INLET NOZZLES

Fluidized-bed reactor for the gas-phase polymerization of olefins including a gas distribution grid installed in a lower part of the fluidized-bed reactor and a gas recycle line, which is equipped with a compressor and a heat exchanger and which is connected at the upper end with the top of the fluidized-bed reactor, wherein the gas recycle line splits at the lower end in at least two horizontal branches which are connected tangentially with the fluidized-bed reactor below the gas distribution grid and a process for preparing an olefin polymer carried out in the fluidized-bed reactor. 1. A fluidized-bed reactor for the gas-phase polymerization of olefins comprising:a gas distribution grid installed in a lower part of the fluidized-bed reactor anda gas recycle line, which is equipped with a compressor and a heat exchanger and which is connected at the upper end with the top of the fluidized-bed reactor, wherein the gas recycle line splits at the lower end in at least two horizontal branches which are connected tangentially with the fluidized-bed reactor below the gas distribution grid.2. The fluidized-bed reactor of claim 1 , wherein the gas recycle line splits in two branches which are attached to the fluidized-bed reactor on opposite sides.3. The fluidized-bed reactor of claim 1 , wherein the gas distribution grid has the form of an inverted cone.4. The fluidized-bed reactor of claim 3 , wherein the cone angle is from 100° to 160°.5. The fluidized-bed reactor of claim 1 , wherein the gas distribution grid comprises a plurality of trays being attached to each other to form slots in the overlapping area of adjacent trays and being successively overlapped claim 1 , thereby forming annular modules of trays.6. The fluidized-bed reactor of claim 1 , wherein the gas distribution grid comprises slots through which recycled gas enters the fluidized-bed reactor and the slots are formed such that the flow of gas after having passed the slots is parallel to the plane of the ...

SYSTEMS AND METHODS FOR REDUCING HEAT EXCHANGER FOULING RATE

Methods of reducing heat exchanger fouling rate or of producing polyolefins may include providing a first gas stream comprising a gas and entrained fine polyolefin particles to a gas outlet line; removing a portion of the entrained fine polyolefin particles from the gas outlet line to form a bypass stream; and providing the bypass stream to a bypass line comprising a bypass line inlet and a bypass line outlet. The bypass line inlet and outlet are located upstream and downstream of a first heat exchanger. The methods may further include providing at least a portion of the first gas stream to the first heat exchanger; and combining the bypass stream and a second gas stream at the bypass line outlet to form a combined gas stream comprising one or more olefins or paraffins. A temperature of the combined gas stream is below the dew point of the combined gas stream. 1. A method of reducing heat exchanger fouling rate , the method comprising:providing a first gas stream comprising a gas and entrained fine polyolefin particles to a gas outlet line;removing a portion of the entrained fine polyolefin particles from the gas outlet line to form a bypass stream comprising a higher concentration of the entrained fine polyolefin particles than is present in the first gas stream;providing the bypass stream to a bypass line comprising a bypass line inlet and a bypass line outlet, wherein the bypass line inlet is located upstream of a first heat exchanger, and wherein the bypass line outlet is located downstream of the first heat exchanger;providing at least a portion of the first gas stream to the first heat exchanger, which produces a first cooled gas stream; andcombining the bypass stream and a second gas stream at the bypass line outlet to form a combined gas stream comprising one or more olefins or paraffins, wherein a temperature of the combined gas stream is below the dew point of the combined gas stream.2. The method of claim 1 , wherein the first gas stream comprises one or ...

REACTOR SYSTEM FOR THE PRODUCTION OF CARBON ALLOTROPES

Systems and a method for forming carbon allotropes are described. An exemplary reactor system for the production of carbon allotropes includes a hybrid reactor configured to form carbon allotropes from a reactant gas mixture in a Bosch reaction. The hybrid reactor includes at least two distinct zones that perform different functions including reaction, attrition, catalyst separation, or gas separation. 1. A reactor system for the production of carbon allotropes , comprising a hybrid reactor configured to form carbon allotropes from a reactant gas mixture in a Bosch reaction , wherein the hybrid reactor comprises at least two distinct zones that perform different functions comprising reaction , attrition , catalyst separation , or gas separation.2. The system of claim 1 , wherein the hybrid reactor comprises:a first zone comprising a fluidized bed disposed in a narrow portion of a reactor vessel; anda second zone comprising an expanded area bed disposed in a wider portion of the reactor vessel, wherein a reactant gas stream in the reactor flows from the narrow fluidized bed to the wider fluidized bed.3. The system of claim 2 , wherein the expanded area bed is configured to slow the reactant gas stream to allow catalyst particles to fall back into the fluidized bed.4. The system of claim 1 , wherein the hybrid reactor comprises:a first zone comprising a fluidized bed reactor; anda second zone comprising a transport reactor, wherein the transport reactor is configured to circulated a portion of material from the fluidized bed reactor to an opposite end of the fluidized bed reactor.5. The system of claim 4 , comprising dividing a reactant gas stream into portions claim 4 , wherein a first portion of the reactant gas stream is injected into the fluidized bed to maintain fluidization claim 4 , and a second portion of the reactant gas stream is injected into the transport reactor to push material through the transport reactor.6. The system of claim 1 , wherein the hybrid ...

APPARATUSES AND METHODS FOR FLUID CATALYTIC CRACKING WITH FEEDSTOCK TEMPERATURE CONTROL

Apparatuses and methods are provided for fluid catalytic cracking. A fluid catalytic cracking apparatus includes a riser with a first inlet. A first distributor pipe is coupled to the riser at the riser inlet. A heat transfer device is coupled to the first distributor pipe, where the heat transfer device includes a coolant outlet exterior to the riser, and wherein the heat transfer device is a counter current heat transfer device. 1. A fluid catalytic cracking apparatus comprising:a riser, wherein the riser defines a first inlet;a first distributor pipe coupled to the riser at the first inlet; anda heat transfer device coupled to the first distributor pipe, wherein the heat transfer device comprises a coolant outlet exterior to the riser, and wherein the heat transfer device is a counter current heat transfer device.2. The fluid catalytic cracking apparatus of further comprising a nozzle coupled to the first distributor pipe claim 1 , wherein the nozzle is configured to inject a fluid from the first distributor pipe into the riser.3. The fluid catalytic cracking apparatus of wherein the nozzle is configured to atomize the fluid from within the first distributor pipe and inject the fluid into the riser.4. The fluid catalytic cracking apparatus of further comprising a coolant inlet fluidly coupled to the heat transfer device claim 1 , wherein the coolant inlet is exterior to the riser.5. The fluid catalytic cracking apparatus of wherein the riser defines a second inlet.6. The fluid catalytic cracking apparatus of wherein the first inlet is positioned higher on the riser than the second inlet.7. The fluid catalytic cracking apparatus of wherein the heat transfer device comprises an exterior sleeve and an interior sleeve claim 1 , wherein the first distributor pipe is positioned within the interior sleeve and the interior sleeve is positioned within the exterior sleeve.8. The fluid catalytic cracking apparatus of wherein the heat transfer device comprises a face plate ...

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 ...

APPARATUS AND METHOD FOR PRODUCING CARBON NANOTUBES

A CNT production apparatus provided by the present invention includes a cylindrical chamber and a control valve provided to a gas discharge pipe The chamber includes a reaction zone provided in a partial range of the chamber in the direction of the cylinder axis, a deposition zone which is provided downstream of the reaction zone and a deposition state detector that detects a physical property value indicating a deposition state of carbon nanotubes in the deposition zone The apparatus is configured to close the control valve and deposit carbon nanotubes in the deposition zone when the physical property value detected by the deposition state detector is equal to or less than a predetermined threshold value, and configured to open the control valve and recover the carbon nanotubes deposited in the deposition zone when the physical property value exceeds the predetermined threshold value. 1. Apparatus for producing carbon nanotubes;comprising:a cylindrical chamber;a carbon source supply unit having a carbon source supply port opening to the chamber, the carbon source supply unit supplying a carbon source from the carbon source supply port to the chamber;a gas supply unit having a gas supply port opening to the chamber, the gas supply unit supplying a non-oxidizing gas from the gas supply port to the chamber;a gas discharge pipe having a gas release port, the gas discharge pipe being configured to be capable of discharging gas in the chamber from the gas release port; anda control valve provided to the gas discharge pipe, whereinthe chamber hasa reaction zone is provided in a part of a range along a cylinder axis direction inside the chamber, and be heated to a temperature at which carbon nanotubes are generated; anda deposition zone provided downstream of the reaction zone inside the chamber and upstream of the gas release port and in which the generated carbon nanotubes are deposited; andthe chamber comprises a deposition state detector that detects a physical ...

FLUIDIZED BED SYSTEM HAVING SPARGER CAPABLE OF MINIMIZING BLOCKAGE BY SOLIDS AND CONTROLLING METHOD THEREOF

The present invention relates to a fluidized bed system having a sparger capable of minimizing a blockage by solids and controlling method thereof. And, more specifically, the present invention relates to a fluidized bed system having a sparger capable of minimizing a blockage by solids comprising a fluidized bed reactor to store a solid layer with a certain height and to fluidize the solid layer by using fluidization gases; a sparger having a pipe shape submerged in the solid layer and having a plurality of gas-discharging holes to spray fluidization gases onto the solid layer; and a gas-supplying line having its one end contacting a gas-supplying source and the other end connected to the sparger, wherein fluidization gases are introduced through the gas-supplying line into the sparger by driving the gas-supplying source, the fluidization gases are sprayed through the gas-discharging holes onto the solid layer, the gas-supplying source is placed higher than the sparger and the height difference (H) between the gas-supplying source and the sparger is greater than the height of the solid layer. 1. A fluidized bed system having a sparger ,the fluidized bed system having a sparger capable of minimizing a blockage by solids comprising:{'sub': 's', 'a fluidized bed reactor to store a solid layer with a certain height (H) inside of it and to fluidize the solid layer via injected fluidization gases;'}a sparger having a pipe shape submerged in the solid layer in the fluidized bed reactor and having a plurality of gas-discharging holes to spray fluidization gases onto the solid layer;a gas-supplying line having its one end contacting a gas-supplying source and the other end connected to the sparger;wherein fluidization gases flow through the gas-supplying line into the sparger and are sprayed through the gas-discharging holes onto the solid layer,{'sub': g', 's, 'wherein the gas-supplying source is placed higher than the sparger and the height difference (H) between the gas- ...

Multiple Reactor and Multiple Zone Polyolefin Polymerization

Apparatuses and processes that produce multimodal polyolefins, and in particular, polyethylene resins, are disclosed herein. This is accomplished by using two reactors in series, where one of the reactors is a multi-zone circulating reactor that can circulate polyolefin particles through two polymerization zones optionally having two different flow regimes so that the final multimodal polyolefin has improved product properties and improved product homogeneity. 1. A trimodal polyethylene resin having a low molecular weight (LMW) component , an intermediate molecular weight (IMW) component , and a high molecular weight (HMW) component; wherein the LMW component is present in an amount of from about 20 wt. % to about 75 wt. %; wherein the IMW component is present in an amount of from about 5 wt. % to about 40 wt. %; wherein the LMW component has a weight average molecular weight of from about 20 kg/mol to about 150 kg/mol; wherein the IMW component has a weight average molecular weight of from about 85 kg/mol to about 350 kg/mol; wherein the weight average molecular weight of the IMW component is greater than the weight average molecular weight of the LMW component; wherein the weight average molecular weight of the HMW component is greater than the weight average molecular weight of the IMW component; wherein the trimodal polyethylene resin has an η(eta_0) of equal to or greater than about 0.7×10Pa-s; and wherein the trimodal polyethylene resin has a strain hardening modulus of from about 50 MPa to about 90 MPa , when tested in accordance with ISO 18488-2015(E).2. The trimodal polyethylene resin of claim 1 , wherein (A1) the HMW component is present in an amount of from about 10 wt. % to about 60 wt. %; (A2) the HMW component has weight average molecular weight of greater than about 350 kg/mol; or (A3) both the HMW component is present in an amount of from about 10 wt. % to about 60 wt. % claim 1 , and the HMW component has weight average molecular weight of greater ...

Multiple Reactor and Multiple Zone Polyolefin Polymerization

Apparatuses and processes that produce multimodal polyolefins, and in particular, polyethylene resins, are disclosed herein. This is accomplished by using two reactors in series, where one of the reactors is a multi-zone circulating reactor that can circulate polyolefin particles through two polymerization zones optionally having two different flow regimes so that the final multimodal polyolefin has improved product properties and improved product homogeneity. 1. A trimodal polyethylene resin having a low molecular weight (LMW) component , an intermediate molecular weight (IMW) component , and a high molecular weight (HMW) component; wherein the LMW component is present in an amount of from about 20 wt. % to about 75 wt. %; wherein the IMW component is present in an amount of from about 5 wt. % to about 40 wt. %; wherein the LMW component has a weight average molecular weight of from about 20 kg/mol to about 150 kg/mol; wherein the IMW component has a weight average molecular weight of from about 85 kg/mol to about 350 kg/mol; wherein the weight average molecular weight of the IMW component is greater than the weight average molecular weight of the LMW component; wherein the weight average molecular weight of the HMW component is greater than the weight average molecular weight of the IMW component; wherein the trimodal polyethylene resin has an η(eta_0) of equal to or greater than about 0.7×10Pa-s; and wherein the trimodal polyethylene resin has a tensile strength in the machine direction (MD) of greater than about 13 ,000 psi (89.6 MPa) , when tested in accordance with ASTM D638 at 90 MPa.2. The trimodal polyethylene resin of claim 1 , wherein (A1) the HMW component is present in an amount of from about 10 wt. % to about 60 wt. %; (A2) the HMW component has weight average molecular weight of greater than about 350 kg/mol; or (A3) both the HMW component is present in an amount of from about 10 wt. % to about 60 wt. % claim 1 , and the HMW component has weight ...

Synthesis of methyl carbamate and dimethyl carbonate (dmc) in presence of stripping with inert gas or superheated vapours and a reactor for the same

The invention relates to synthesis of methyl carbamate (MC) and dimethyl carabonate (DMC) in presence of stripping inert gas or superheated methanol vapors using packed column reactor and bubble column reactor.

MACHINE AND METHODS FOR TRANSFORMING BIOMASS AND/OR WASTE PLASTICS VIA SUPERCRITICAL WATER REACTION

The machinery and methods disclosed herein are based on the use of a specialized extruder configured to continuously convey and plasticize/moltenize selected lignocellulosic biomass and/or waste plastic materials into a novel variable volume tubular reactor, wherein the plasticized/moltenized material undergoes reaction with circumferentially injected supercritical water—thereby yielding valuable simple sugar solutions and/or liquid hydrocarbon mixtures (e.g., “neodiesel”), both of which are key chemical commodity products. The reaction time may be adjusted by changing the reactor volume. The machinery includes four zones: (1) a feedstock conveyance and plasticization/moltenization zone; (2) a steam generation and manifold distribution zone; (3) a central supercritical water reaction zone; and (4) a pressure let-down and reaction product separation zone. The machinery and methods minimize water usage—thereby enabling the economic utilization of abundant biomass and waste plastics as viable renewable feedstocks for subsequent conversion into alternative liquid transportation fuels and valuable green-chemical products. 1. A machine for transforming a selected polymeric material into a plurality of reaction products via supercritical water reaction , comprising:an extruder having an inlet and a downstream outlet, wherein the downstream outlet is coincident with the longitudinal axis of the extruder;a steam generator fluidically connected to a downstream inlet manifold, wherein the inlet manifold forms a ring having a plurality of inwardly facing exit portals, wherein the plurality of exit portals is circumferentially positioned about the inner surface of the ring;a tubular reactor having an interior space fluidically connected to an inlet end and an outlet end, wherein the inlet end of the tubular reactor is adjacent and fluidically connected to both (i) the outlet of the extruder, and (ii) the plurality of circumferentially positioned exit portals of the inlet ...

METHOD FOR THERMAL PRECONDITIONING OF NATURAL GRAPHITE FLAKES USING ELECTROMAGNETIC WAVES

An apparatus for processing graphite particles is disclosed. The apparatus may comprise an electromagnetic radiation emitting device including a microwave device coupled to the reaction chamber for the creation of electromagnetic waves, the electromagnetic waves comprising microwaves. The apparatus may also comprise an inlet attached to the reaction chamber for introducing graphite particles, and an outlet attached to the reaction chamber for allowing processed graphite particles to exit the reaction chamber. The graphite particles in the reaction chamber thermally altered by exposure to the electromagnetic radiation such that the graphite particles are heated 1. An apparatus for processing graphite particles , the apparatus comprising:a reaction chamber;an electromagnetic radiation emitting device comprising a microwave device coupled to the reaction chamber for creating electromagnetic waves, the electromagnetic waves comprising microwaves;an inlet attached to the reaction chamber for introducing graphite particles; andan outlet attached to the reaction chamber for allowing processed graphite particles to exit the reaction chamber,wherein the graphite particles in the reaction chamber thermally altered by exposure to the electromagnetic radiation such that the graphite particles are heated.2. The apparatus of claim 1 , wherein the apparatus further comprises:a dispersion device coupled to the reaction chamber to disperse the graphite particles; anda process gas dispersion device coupled to the reaction chamber to disperse process gas.3. The apparatus of claim 2 , wherein the microwave device provides microwaves of one or more fixed frequencies.4. The apparatus of claim 1 , wherein the microwave device provides tunable microwaves or microwaves with sweeping frequencies.5. The apparatus of claim 1 , wherein the reaction chamber varies in cross section along a length of the reaction chamber.6. The apparatus of claim 1 , wherein the reaction chamber varies in cross ...

REACTOR AND MULTIFUNCTIONAL RISER AND DOWNER SIMULATOR INCORPORATING THE SAME

A reactor comprises a reactor vessel defining a confined reactor volume, a support assembly extending about a periphery of the confined reactor volume, a basket positioned within the reactor vessel and supported by the support assembly, the basket having an interior surface and an exterior surface, a downflow zone being defined between the exterior surface of the basket and an interior surface of the confined reactor volume, an inlet screen positioned adjacent to one end of the interior surface and an outlet screen positioned adjacent to an opposite end of the interior surface, an upflow zone defined between the inlet screen and outlet screen, the inlet screen and the outlet screen containing a quantity of particulate catalyst, and a circulating device positioned above said upflow zone and configured to continuously circulate fluid upwardly though said upflow zone and downwardly through said downflow zone, the support assembly and the basket configured to promote the formation of a fluid vortex within a portion of the downflow zone. 1. A reactor comprising:a reactor vessel defining a confined reactor volume;a support assembly extending about a periphery of the confined reactor volume;a basket positioned within the reactor vessel and supported by the support assembly, the basket having an interior surface and an exterior surface, a downflow zone being defined between the exterior surface of the basket and an interior surface of the confined reactor volume;an inlet screen positioned adjacent to one end of the interior surface and an outlet screen positioned adjacent to an opposite end of the interior surface, an upflow zone defined between the inlet screen and outlet screen, the inlet screen and the outlet screen containing a quantity of particulate catalyst; anda circulating device positioned above said upflow zone and configured to continuously circulate fluid upwardly though said upflow zone and downwardly through said downflow zone;the support assembly and the ...

INDUCTION HEATER SYSTEM FOR A FLUIDIZED BED REACTOR

A system for the production of a polycrystalline silicon product is disclosed. The system includes a reaction chamber, a susceptor, an induction unit, and a plurality of energy sources. The reaction chamber has a reactor wall, and the susceptor encircles the reactor wall. The induction heater surrounds the susceptor, and has multiple induction coils for producing heat in the susceptor. The coils are grouped into a plurality of zones. The plurality of energy sources supply electric current to the coils. Each energy source is connected with the coils of at least one zone. 1. A system for producing a polycrystalline silicon product , the system comprising:a reaction chamber having a reactor wall;a susceptor encircling the reactor wall;an induction unit surrounding the susceptor, the induction unit having multiple induction coils for producing heat in the susceptor, the coils grouped into a plurality of zones; anda plurality of energy sources for supplying an electric current to the coils, each energy source connected with the coils of at least one zone.2. The system of claim 1 , further comprising insulation between the induction unit and the susceptor for preventing heat loss from the susceptor to ambient.3. The system of claim 1 , further comprising a high-pressure fluidized bed reactor.4. The system of claim 1 , wherein the reactor wall has a diameter of at least 20 inches.5. The system of claim 1 , wherein the coils of each zone being divided into multiple sub-zones claim 1 , at least one sub-zone from each zone connected with the same energy source.6. The system of claim 1 , further comprising an enclosure surrounding the induction unit for masking a stray magnetic field generated by the coils.7. The system of claim 1 , wherein the coils have passages therethrough for circulating deionized water to cool the coils.8. A method for producing a polycrystalline silicon product in a reactor having multiple induction coils grouped into multiple zones and a plurality of ...

APPARATUS AND METHODS FOR TREATMENT OF RADIOACTIVE ORGANIC WASTE

Treatment of radioactive waste comprising organic compounds, and sulfur-containing compounds and/or halogen-containing compounds. An apparatus comprises a reaction vessel comprising a filter for carrying out thermal treatment of the waste and a thermal oxidizer. Utilizing co-reactants to reduce gas phase sulfur and halogen from treatment of wastes. 1. An apparatus for the treatment of radioactive waste comprising organic compounds , and sulfur-containing compounds and/or halogen-containing compounds , the apparatus comprising:(a) a reaction vessel comprising a filter for carrying out thermal treatment of the waste; and(b) a thermal oxidizer.2. The apparatus of claim 1 , wherein the apparatus further comprises:(c) an adsorption vessel comprising one or more types of adsorbent media for adsorbing sulfur-containing compounds and/or halogen-containing compounds after treatment of the waste by the reaction vessel.3. The apparatus of claim 1 , wherein the reaction vessel comprising a filter further comprises a bed in the lower portion of the reaction vessel comprising a filter.4. The apparatus of claim 3 , wherein the bed in the reaction vessel comprising a filter comprises the waste claim 3 , one or more co-reactants and optionally claim 3 , inert bed media.5. The apparatus of claim 4 , wherein the bed is partially fluidized or jetted.6. The apparatus of claim 1 , wherein the apparatus further comprises a process reaction vessel upstream of the reaction vessel comprising a filter.7. The apparatus of claim 6 , wherein the process reaction vessel further comprises a bed in the lower portion of the process reaction vessel.8. The apparatus of claim 7 , wherein the bed in the process reaction vessel comprises the waste claim 7 , one or more co-reactants and optionally claim 7 , inert bed media.9. The apparatus of claim 1 , wherein the temperature of the reaction vessel comprising a filter is below the temperature at which the sulfur-containing compounds and/or halogen- ...

LOADING A CATALYST INTO A BUBBLE COLUMN FOR FISCHER-TOPSCH SYNTHESIS

A method for charging a catalyst into a reactor () comprising a separation loop (), comprising the following steps: 14021. A method for charging a catalyst into a synthesis reactor () , of the bubble column type , comprising a separation loop () , said method comprising the following steps:{'b': 40', '1, 'a) filling at least a portion of the synthesis reactor () with a solvent S;'}{'b': 21', '40', '1, 'b) filling at least a portion of the separation loop () of said synthesis reactor () with said solvent S;'}{'b': 1', '40', '21', '40, 'c) causing said solvent S to move from the synthesis reactor () to the separation loop () and from the separation loop to the synthesis reactor ();'}{'b': '40', 'd) heating the synthesis reactor () to a temperature of 100° C. or less;'}{'b': 40', '40, 'e) injecting an inert gas into the bottom of the synthesis reactor () and increasing the pressure of the synthesis reactor () in a manner such as to obtain an absolute pressure in the range 0.1 to 0.6 MPa;'}{'b': 2', '30, 'f) mixing said catalyst with a solvent S in a vessel () in order to obtain a liquid/solid mixture;'}{'b': 30', '40', '40, 'g) increasing the pressure in the vessel () to a pressure which is at least 0.2 MPa higher than the pressure of the synthesis reactor (), then sending the liquid/solid mixture obtained in step f) to the synthesis reactor ();'}{'b': 1', '2', '40', '21, 'h) withdrawing at least a portion of said solvent S and/or S contained in the synthesis reactor () and/or in the separation loop ().'}212. The method as claimed in claim 1 , characterized in that the solvent S is identical to the solvent S.312. The method as claimed in claim 1 , characterized in that the solvent S and/or the solvent S are selected from hydrogenated polyalphaolefin solvents or hydrogenated isoparaffinic solvents.4. The method as claimed in claim 1 , further comprising the following steps after step h):{'b': '40', 'i) heating the synthesis reactor () to a temperature in the range 150° ...

Multiple Reactor and Multiple Zone Polyolefin Polymerization

Apparatuses and processes that produce multimodal polyolefins, and in particular, polyethylene resins, are disclosed herein. This is accomplished by using two reactors in series, where one of the reactors is a multi-zone circulating reactor that can circulate polyolefin particles through two polymerization zones optionally having two different flow regimes so that the final multimodal polyolefin has improved product properties and improved product homogeneity. 1. A process for producing a multimodal polyolefin , comprising:(a) polymerizing ethylene in a first reactor to produce a first polyolefin;(b) polymerizing ethylene in a first reaction mixture in a riser of a second reactor to produce a second polyolefin;(c) passing the first reaction mixture through an upper conduit from the riser to a separator;(d) recovering, in the separator, the second polyolefin from the first reaction mixture;(e) passing the second polyolefin from the separator into a downcomer of the second reactor, optionally via a liquid barrier;(f) polymerizing ethylene in a second reaction mixture in the downcomer to produce a third polyolefin in a downcomer product mixture;(g) passing the downcomer product mixture through a lower conduit from the downcomer to the riser; and (1) after step (a) and before steps (b)-(g), receiving the first polyolefin into the second reactor; or', '(2) before step (a) and after steps (b)-(g), receiving the second polyolefin and the third polyolefin into the first reactor., '(h) one of2. The process of claim 1 , wherein an elbow connector is connected i) to a bottom portion of the riser and to an end of the lower conduit claim 1 , ii) to a top portion of the riser and to an end of the upper conduit claim 1 , or iii) to a bottom portion of the downcomer and to an opposite end of the lower conduit claim 1 , wherein the elbow connector comprises:a first tap on an outside radius of the elbow connector;a second tap on an inside radius of the elbow connector;a first sensing ...

THERMOLYTIC FRAGMENTATION OF SUGARS

A process for large scale and energy efficient production of oxygenates from sugar is disclosed in which a sugar feedstock is introduced into a thermolytic fragmentation reactor including a fluidized stream of heat carrying particles. The heat carrying particles may be separated from the fluidized stream prior to cooling the fragmentation product and may be directed to a reheater to reheat the particles and recirculate the heated particles to the fragmentation reactor. 1. A process for thermolytic fragmentation of a sugar into C-Coxygenates , said process comprising the steps of:a. providing particles carrying heat and suitable for fluidization;b. providing a fluidized bed fragmentation reactor comprising a riser and suitable for conducting thermolytic fragmentation and suitable for fluidizing a stream of particles;c. providing a feedstock solution comprising a sugar;d. introducing the particles into the reactor at a rate sufficient to maintain a temperature of at least 250° C., such as at least 300 350, 400 or 450° C., after the thermolytic fragmentation has taken place, and sufficient to obtain a fluidized stream of particles;e. introducing the feedstock into the fluidized stream of particles to obtain thermolytic fragmentation of the sugar to produce a particle dense fragmentation product; thenf. separating a fraction of the particles from the particle dense fragmentation product to produce a particle lean fragmentation product;g. quenching the particle lean fragmentation product at least 50° C. such that from introducing the feedstock into the particle containing fluidization stream to the quench is performed, the mean residence time of the gas is maximum 5, such as maximum 3 seconds, such as maximum 2, 1, 0.8 or 0.6 seconds;h. recovering the crude fragmentation product,i. transferring the particles separated in step f) to a reheater for heating; andj. recirculating the heated particles to the fragmentation reactor. The present application is a continuation of U ...

オレフィンの気相重合法

Apparatus and its use for oxychlorination

The preparation of 1,2-dichloroethane from ethylene, hydrogen chloride and oxygen or an oxygen-containing gas (oxychlorination) advantageously proceeds in a reactor having a lower delimitation for a catalyst fluid bed, a first gas inlet (distributor tubes) being arranged above the delimitation and within the catalyst fluid bed, which gas inlet contains nozzles distributed over the entire cross section of the reactor, these nozzles opening into tubes which conduct the exiting gas stream essentially in the opposite direction to the gas stream which fluidizes the catalyst, this gas stream being fed through a second gas inlet beneath the delimitation.

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 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.

Calcination method and system

The invention relates to a method for the calcination of powdery or fine-particled plaster, comprising two steps: the plaster is subjected to a flash-calcination in a calcinator (3) and the hot plaster is post-calcinated in a reaction vessel (6). According to the invention, post-calcination is carried out in the reaction vessel (6) by adding humid gas, said reaction vessel (6) not being heated. Said post-calcination takes place over a long period of time, that is at least 10 times, preferably 50 - 100 times longer than the amount of time taken for flash calcination. Said invention enables complete calcination to take place without expending additional energy, and the remaining dihydrate produced during the flash calcination is also transformed into semi-hydrate and undesired anhydrite fractions are reduced. Said method ensures consistency in the product quality and also increases product quality. The temperature in the upstream calcinator (3) can be lowered thus saving more energy. Said invention can also be used to accelerate the ageing of calcinated plaster.

Multiple reactor and multiple zone polyolefin polymerization

Apparatuses and processes that produce multimodal polyolefins, and in particular, polyethylene resins, are disclosed herein. This is accomplished by using two reactors in series, where one of the reactors is a multi-zone circulating reactor that can circulate polyolefin particles through two polymerization zones optionally having two different flow regimes so that the final multimodal polyolefin has improved product properties and improved product homogeneity.

Methods of controlling polyolefin melt index while increasing catalyst productivity

The catalyst productivity of a polyolefin catalyst in the methods disclosed herein may be increased by increasing the concentration of an induced condensing agent (ICA) in the reactor system. The effect the increased ICA concentration may have on a melt index may be counteracted, if necessary, in various ways.

Method and apparatus for polymerizing olefins in the gas phase

一种用于费托合成的系统及合成气制备低碳烯烃的方法

本发明提供了一种用于费托合成的系统及合成气制备低碳烯烃的方法。一种用于费托合成的系统，包括流化床反应器筒体、气固分离器、换热器和催化剂输送管；所述流化床反应器筒体的顶部设有产物出口，所述产物出口与所述气固分离器连接；所述气固分离器设有固体产物出口，所述固体产物出口连接所述催化剂输送管的一端，所述催化剂输送管的另一端连接所述流化床反应器筒体的底部；所述换热器用于与所述输送管交换热量，并且所述换热器与所述输送管均设置在所述流化床反应器筒体的外部。本发明的系统能够及时将反应器的反应热移出，而且避免热量移出过程中催化剂磨耗和设备易损坏的问题，还能将移出的热量回收利用。

Process for the preparation of hydrogen cyanide on a cyclically guided as a transport fluidized bed particulate heat exchanger

Die Erfindung betrifft ein Verfahren zur kontinuierlich betriebenen Herstellung von Cyanwasserstoff durch Umsetzung von Ammoniak mit Kohlenwasserstoffen, wobei das Reaktionsgasgemisch mittels indirekter Beheizung durch Kontakt mit einem partikulären Wärmeüberträger im Wirbelbett auf Reaktionstemperatur gebracht wird, und das dadurch gekennzeichnet ist, daß der Wärmeüberträger in einer Transportwirbelschicht zyklisch geführt wird, wobei in einem aufsteigenden Transportstrom der Wärmeüberträger aufgeheizt wird und dieser in einem absteigenden Transportstrom mit dem Reaktionsgasgemisch in Kontakt gebracht wird. The invention relates to a process for the continuous production of hydrogen cyanide by reaction of ammonia with hydrocarbons, wherein the reaction gas mixture is brought by indirect heating by contact with a particulate heat exchanger in the fluidized bed to reaction temperature, and which is characterized in that the heat exchanger in a transport fluidized bed cyclically is performed, wherein in an ascending transport stream of the heat exchanger is heated and this is brought in a descending transport stream with the reaction gas mixture in contact.

Method and apparatus for polymerising olefins in gas phase

Processo e aparelho para polimerização de olefinas em fase gasosa

Gas-diffusion plate for fluidized bed apparatus

The present disclosure relates to a diffusion plate to partition one space from another and pass a gas through ports in the plate in a flow pattern which is uniform over the area of the partition. Specifically, the disclosure relates to a diffusion plate, sometimes referred to as a distributor plate, having the aforesaid functions in connection with fluidized bed apparatus.

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.

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.

Methods for Controlling Polyolefin Melt Index While Increasing Catalyst Productivity

La productividad del catalizador de un catalizador de poliolefina en los métodos descritos en el presente documento puede incrementarse aumentando la concentración de un agente de condensación inducida (ICA) en el sistema del reactor. El efecto que puede tener la mayor concentración de ICA sobre el índice de fusión puede contrarrestarse, si es necesario, de varias formas. (Traducción automática con Google Translate, sin valor legal) The catalyst productivity of a polyolefin catalyst in the methods described herein can be increased by increasing the concentration of an induced condensation agent (ICA) in the reactor system. The effect that the higher concentration of ICA may have on the melt index can be counteracted, if necessary, in various ways. (Automatic translation with Google Translate, without legal value)

改变聚烯烃生产条件以减轻聚烯烃物品中的小凝胶的方法

可通过更改聚烯烃的某些生产参数来减少形成在聚烯烃薄膜中的小凝胶的数目。在一些情况下，小凝胶的数目可受到所述聚烯烃的熔融指数影响。然而，在许多情况下，熔融指数是聚烯烃产物规格的关键部分且因此不被操控。可被操控以减轻小凝胶计数同时维持所述熔融指数的两个参数是反应器中的聚烯烃滞留时间和所述反应器中的ICA浓度。

控制聚烯烃熔融指数，同时增加催化剂产率的方法

本文所公开的方法中的聚烯烃催化剂的催化剂产率可通过增加反应器系统中的诱导冷凝剂(ICA)的浓度而增加。必要时，可以不同方式抵消增加的ICA浓度可能对于熔融指数具有的影响。

オレフィンの気相重合法

Process, and Apparatus, for the Injection of Preheated Oxygen Into a High Temperature Reactor

Process, and apparatus, for the production of hydrogen and carbon monoxide in a reactor, preferably one containing a bed of a particulate solids catalyst, or catalyst and solids diluent, by contacting and reacting within the reaction zone a low molecular weight hydrocarbon feed, steam and oxygen, or a low molecular weight hydrocarbon feed and oxygen, at high temperature. An oxygen stream preheated to high temperature is fed via a nozzle inlet, or inlets, into the reactor, while the hydrocarbon and steam, or hydrocarbon, is fed via a different nozzle inlet, or inlets, into the reactor. Preferred oxygen nozzle designs are constituted of nickel-chromium-iron alloys, especially Inconel 600, and Inconel alloys of the 600 series generally. The oxygen nozzle is comprised of a tubular body with inlet, and outlets of special design, which renders the nozzle especially useful in the intensely hot oxygen environment.

控制聚烯烃熔融指数，同时增加催化剂产率的方法

本文所公开的方法中的聚烯烃催化剂的催化剂产率可通过增加反应器系统中的诱导冷凝剂(ICA)的浓度而增加。必要时，可以不同方式抵消增加的ICA浓度可能对于熔融指数具有的影响。

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.

Methods of controlling polyolefin melt index while increasing catalyst productivity

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.

Method and apparatus for polymerising olefins in gas phase

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.

用于在气相中聚合烯烃的方法和设备

本发明涉及一种烯烃聚合方法。在一种聚合反应器中，在烯烃聚合催化剂的存在下，在流化床中，在气相中聚合至少一种烯烃，所述聚合反应器具有：垂直主体；大致锥形的向下逐渐变细的底部区域；在所述底部区域上方并连接到所述底部区域的大致柱形的中部区域；以及在所述中部区域上方并连接到所述中部区域的大致锥形的向上逐渐变细的顶部区域。将流化气体引入到所述反应器的底部区域，从所述底部区域向上穿过所述反应器，并从所述反应器的顶部区域取出。然后将气体压缩、冷却并返回到所述反应器的底部区域。因此在反应器内形成流化床，其中生长的聚合物颗粒悬浮在上升气流中，其中流化气体的表观速度小于颗粒的输送速度。反应器内没有流化栅格。流化气体从入口室进入所述底部区域，气体从所述入口室的上部流向其下部，并且气体从所述入口室的下部流向所述底部区域。

REGULATION OF AMMONIA AND / OR AIR SUPPLY IN AMOXIDATION REACTOR

Описаны способ и система для регулирования количества аммиака и/или воздуха, подаваемых в реактор аммоксидирования. Способ включает поддержание рН охлаждающей воды в кубе и регулирование количества аммиака в сырье для реактора для обеспечения отношения аммиака к углеводороду от приблизительно 1 до приблизительно 2 в сырье для реактора. Кроме того, способ может включать регулирование количества воздуха в сырье для реактора для обеспечения отношения воздуха к углеводороду от приблизительно 9 до приблизительно 10 в сырье для реактора. A method and system for controlling the amount of ammonia and / or air supplied to the ammoxidation reactor is described. The method includes maintaining the pH of the cooling water in the cube and regulating the amount of ammonia in the feedstock for the reactor to ensure the ratio of ammonia to hydrocarbon from about 1 to about 2 in feedstock for the reactor. In addition, the method may include regulating the amount of air in the feedstock for the reactor to ensure the air to hydrocarbon ratio is from about 9 to about 10 in the feedstock for the reactor.

Heat exchanger type reaction tube

A heat exchanger type reaction tube includes a first tube part that forms a first flow channel into which a feed gas flows and in which the feed gas moves down; a second tube part that forms a second flow channel which is connected to the first flow channel and in which the feed gas moves up and that has a granular catalyst carrying support medium charged therein; and a heating device that heats the first tube part and the second tube part. Then, the first flow channel and the second flow channel are adjacent to each other while being separated from each other by a partition wall, and the second flow channel is provided with a distributor which holds the catalyst carrying support medium and through which the feed gas passes.

Delta temperature control of catalytic dehydrogenation process reactors

A chemical plant or a petrochemical plant or a refinery may include one or more pieces of equipment that process one or more input chemicals to create one or more products. For example, catalytic dehydrogenation can be used to convert paraffins to the corresponding olefin. A delta temperature controller may determine and control differential temperature across the reactor, and use a delta temperature to control a set point for a heater temperature controller. By doing so, the plant may ramp up a catalytic dehydrogenation unit faster and ensure it does not coke up the catalyst and/or foul a screens too quickly. Catalyst activity may be taken into account and allow the plant to have better control over production and run length of the unit.

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.

Multiple reactor and multiple zone polyolefin polymerization

Apparatuses and processes that produce multimodal polyolefins, and in particular, polyethylene resins, are disclosed herein. This is accomplished by using two reactors in series, where one of the reactors is a multi-zone circulating reactor that can circulate polyolefin particles through two polymerization zones optionally having two different flow regimes so that the final multimodal polyolefin has improved product properties and improved product homogeneity.

Multiple reactor and multiple zone polyolefin polymerization

Apparatuses and processes that produce multimodal polyolefins, and in particular, polyethylene resins, are disclosed herein. This is accomplished by using two reactors in series, where one of the reactors is a multi-zone circulating reactor that can circulate polyolefin particles through two polymerization zones optionally having two different flow regimes so that the final multimodal polyolefin has improved product properties and improved product homogeneity.

Multiple reactor and multiple zone polyolefin polymerization

Apparatuses and processes that produce multimodal polyolefins, and in particular, polyethylene resins, are disclosed herein. This is accomplished by using two reactors in series, where one of the reactors is a multi-zone circulating reactor that can circulate polyolefin particles through two polymerization zones optionally having two different flow regimes so that the final multimodal polyolefin has improved product properties and improved product homogeneity.

Multiple reactor and multiple zone polyolefin polymerization

Apparatuses and processes that produce multimodal polyolefins, and in particular, polyethylene resins, are disclosed herein. This is accomplished by using two reactors in series, where one of the reactors is a multi-zone circulating reactor that can circulate polyolefin particles through two polymerization zones optionally having two different flow regimes so that the final multimodal polyolefin has improved product properties and improved product homogeneity.

Multiple reactor and multiple zone polyolefin polymerization

Apparatuses and processes that produce multimodal polyolefins, and in particular, polyethylene resins, are disclosed herein. This is accomplished by using two reactors in series, where one of the reactors is a multi-zone circulating reactor that can circulate polyolefin particles through two polymerization zones optionally having two different flow regimes so that the final multimodal polyolefin has improved product properties and improved product homogeneity.

Multiple reactor and multiple zone polyolefin polymerization

Apparatuses and processes that produce multimodal polyolefins, and in particular, polyethylene resins, are disclosed herein. This is accomplished by using two reactors in series, where one of the reactors is a multi-zone circulating reactor that can circulate polyolefin particles through two polymerization zones optionally having two different flow regimes so that the final multimodal polyolefin has improved product properties and improved product homogeneity.

Multiple reactor and multiple zone polyolefin polymerization

Apparatuses and processes that produce multimodal polyolefins, and in particular, polyethylene resins, are disclosed herein. This is accomplished by using two reactors in series, where one of the reactors is a multi-zone circulating reactor that can circulate polyolefin particles through two polymerization zones optionally having two different flow regimes so that the final multimodal polyolefin has improved product properties and improved product homogeneity.

一种用于催化剂制备、活化的气相流化床装置及催化剂活化方法

本发明公开了一种用于催化剂制备、活化的气相流化床装置及催化剂活化方法；所述的一种用于催化剂制备、活化的气相流化床装置，包括流化床本体，所述流化床本体，包括反应器和预热管；所述预热管，用于预热流化气体，其下端口从上方插入到所述反应器的底部，并具有所述流化气体从上向下流动直至进入所述反应器底部的流经通道；所述反应器，用于提供所述流化气体活化催化剂颗粒的流化场所；解决现有流化床装置催化剂隔氧转移收集操作繁琐，反应器恒温控制难度大及能量损失大的问题，另外还解决了流化气体消耗量大、催化剂损失多等问题。

Silicon refinery

A balanced, closed cycle silicon refinery system has been developed for producing electronic grade silicon from industrial grade silicon. Impurities comprising approximately 1% of the industrial grade silicon are removed in the refinery system to produce the purified silicon, while only a relatively small percentage of make-up chemicals are added to the system. In the refinery, hydrogen chloride is reacted with the impure silicon in a halide reactor to provide trichlorosilane and silicon tetrachloride and hydrogen. The trichlorosilane and/or silicon tetrachloride are passed through purification means, and then reacted with the hydrogen from the halide reactor in a fluidized bed reactor to produce the purified silicon and an effluent comprised of unreacted trichlorosilane, silicon tetrachloride, hydrogen, and the by-product hydrogen chloride. These materials are passed through a separator and the trichlorosilane and silicon tetrachloride and hydrogen are returned to the silicon reactor while the hydrogen chloride is returned to the halide reactor to be reacted with additional industrial grade silicon.

Process, and apparatus, for the injection of preheated oxygen into a high temperature reactor