Abstract: A method is disclosed in which a gas of hydrogen and nitrogen, or hydrogen and ammonia, or hydrogen, nitrogen, and ammonia, is introduced to a fluidized bed. The gas flows through the fluidized bed, and titanium dioxide particles are introduced to the fluidized bed to form a fluid mixture of the particles and gas in the fluidized bed. The particles are reacted with the gas in the fluid mixture to form particles including titanium dioxide and nitrogen. The particles can be disposed along an air flow path in operative communication with a light source for air treatment.

Abstract: The present invention relates to a gas distribution unit for a fluidized bed reactor system, a fluidized bed reactor system having the gas distribution unit, and a method for preparing granular polysilicon using the fluidized bed reactor system. The gas distribution unit for a fluidized bed reactor system according to the present invention enables gas flow rate control and gas composition control for each zone within the plenum chamber. In addition, a fluidized bed reactor system having the gas distribution unit enables shape control of a fluidized bed (in particular, transition between a bubbling fluidized bed and a spout fluidized bed). The method for preparing granular polysilicon using the fluidized bed reactor system not only simultaneously improves process stability and productivity, but also enables more flexible handling in the event of an abnormal situation.

Abstract: The invention relates to a plant and to a method for chemical looping oxidation-reduction combustion of a gaseous hydrocarbon feed, for example natural gas essentially containing methane. According to the invention, catalytic pre-reforming of the feed is performed in a pre-reforming zone comprising a fixed reforming catalyst, while benefiting from a heat transfer between the reduction or oxidation zone of the chemical loop and the pre-reforming zone adjoining the reduction or oxidation zone. Pre-reforming zone (130) and oxidation zone (110) or pre-reforming zone (130) and reduction zone (120) are thus thermally integrated within the same reactor (100) while being separated by at least one thermally conductive separation wall (140).

Abstract: A process for reducing the size of sulfur removal units is presented. The process includes passing a regeneration gas from a regenerated contaminant adsorption unit through a fixed bed adsorber. The fixed bed adsorber adsorbs sulfur compounds above an equilibrium condition and releases adsorbed sulfur compounds below the equilibrium condition. The peak levels of sulfur in the regeneration gas are reduced and the processing of the regeneration gas reduces the size of sulfur removal units.

Abstract: A two-stage reactor is disclosed for the conversion of solid particulate biomass material. The reactor is designed to maximize conversion of the solid biomass material, while limiting excess cracking of primary reaction products. The two-stage reactor comprises a first stage reactor, in which solid biomass material is thermally pyrolyzed to primary reaction products. The primary reaction products are catalytically converted in a second stage reactor.

Abstract: A fluidized bed reactor includes a bottom portion, a roof portion, and side walls vertically extending between the bottom portion and the roof portion, forming a reaction chamber of the reactor. At least one side wall of the reaction chamber forms at least one vertical indentation in the reaction chamber, which indentation extends from the plane of the at least one side wall towards the reaction chamber. The indentation extending from the plane of the at least one side wall towards the reaction chamber is formed of a portion of the at least one side wall, protruding from the plane of the at least one side wall towards the reaction chamber, and the portion of the at least one side wall includes at least two substantially vertical indenting wall portions deviating from the plane of the at least one side wall at vertical lines within a distance from each other.

Abstract: A method and assembly for producing substantially tar free product gas from gasification of carbonaceous material. The assembly preferably includes a first stage gasifier to produce char-ash and tar laden product gas and a second stage gasifier which has a char-ash heating zone, at least one cyclone, and at least one standpipe for the purpose of allowing selective delivery of char-ash to the char-ash heating zone. A char-ash heating zone that utilizes oxidation of char-ash is preferred and this results in the heat required to convert tar, additional yield of product gas, and an oxidized, activated carbon surface to facilitate tar conversion in the riser, thereby reducing the temperature required to achieve the desired tar conversion. Alternatively, external heat is supplied to the heating zone.

Abstract: 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.

Abstract: The invention features methods and systems for recovering carbon dioxide, for producing commercial quality carbon dioxide (CO2) of 90% to +99% purity using, wet calcium carbonate lime mud produced in a recausticizing process that also produces caustic soda, for instance, Kraft paper pulp mill lime mud (a.k.a., “lime mud”) as a feedstock to a multi-stage lime mud calcination process. This process may be fueled with low, or negative cost “carbon-neutral” fuels such as waste water treatment plant (WWTP) sludge, biomass, precipitated lignins, coal, or other low cost solid fuels. High reactivity, high-quality calcined lime mud (a.k.a. re-burned lime, or calcine), required in the Kraft paper pulp mill's recausticizing process is also produced, and superheated high pressure steam and hot boiler feed-water is generated and exported to the mill's steam distribution and generation system as well as hot process water for use in the mill's manufacturing operation.

Abstract: At least one heat pipe for removing heat is led into a reactor housing of a fluidized bed reactor, so that the temperature in the reactor housing can be controlled.

Abstract: The present invention relates to a process for preparing low-chloride LiPF6, in particular low-chloride LiPF6 solutions, from PCl3 as starting material and via PCl5 as intermediate product, and also to apparatus to be used for this.

Abstract: Apparatuses and processes are provided for stripping gaseous hydrocarbons from particulate material. One process comprises the step of contacting particles containing hydrocarbons with a stripping vapor in countercurrent flow to remove at least a portion of the hydrocarbons with the stripping vapor to form stripped particles. Contacting the particles includes advancing the particles down a sloping element of a structured packing toward a reinforcing rod that is disposed along a lower channel portion of the sloping element. The particles are advanced over the reinforcing rod. The particles are contacted with the stripping vapor that is rising up adjacent to the lower channel portion.

Abstract: The present invention provides isothermal multitube reactors suitable for the production of chlorinated and/or fluorinated propene and higher alkenes from the reaction of chlorinated and/or fluorinated alkanes and chlorinated and/or fluorinated alkenes. The reactors utilize a feed mixture inlet temperature at least 20° C. different from a desired reaction temperature.

Abstract: A system includes a reactor-adsorber configured to receive a gas, a regenerator configured to receive a saturated CO2 adsorption material from the reactor-adsorber, a first solids pressurizing feeder configured to convey the saturated CO2 adsorption material from the reactor-adsorber to the regenerator, and a second solids pressurizing feeder configured to convey a regenerated CO2 adsorption material from the regenerator to the reactor-adsorber. The reactor-adsorber includes a catalyst material configured to catalyze a water gas shift reaction of the gas to generate a hydrogen-rich gas, and a CO2 adsorption material configured to adsorb CO2 from the hydrogen-rich gas to generate the saturated CO2 adsorption material. The regenerator is configured to regenerate the saturated CO2 adsorption material to provide the regenerated CO2 adsorption material and CO2.

Abstract: Embodiments of apparatuses and methods for controlling heat for rapid thermal processing of carbonaceous material are provided herein. The apparatus comprises a reheater for containing a fluidized bubbling bed comprising an oxygen-containing gas, inorganic heat carrier particles, and char and for burning the char into ash to form heated inorganic particles. An inorganic particle cooler is in fluid communication with the reheater to receive a first portion of the heated inorganic particles. The inorganic particle cooler is configured to receive a cooling medium for indirect heat exchange with the first portion of the heated inorganic particles to form first partially-cooled heated inorganic particles that are fluidly communicated to the reheater and combined with a second portion of the heated inorganic particles to form second partially-cooled heated inorganic particles. A reactor is in fluid communication with the reheater to receive the second partially-cooled heated inorganic particles.

Abstract: A method can include combusting an expanded turbine exhaust and a first fuel within a first reformer to produce a first exhaust. A hydrocarbon can be reformed in the first reformer to produce a reformed hydrocarbon and heat can be transferred from the first exhaust to a first medium. A refrigeration unit can be powered with thermal energy from the heated first medium and can cool a second medium. Heat can be transferred from one or more oxidants to the cooled second medium to produce cooled first and second oxidants. The cooled first oxidant and a second fuel can be introduced to a gas turbine unit to produce the expanded turbine exhaust and mechanical power. The cooled second oxidant can be compressed in a compressor powered with the mechanical power and the compressed second oxidant and the reformed hydrocarbon can be introduced to a second reformer to produce a syngas.

Abstract: Systems and methods for gasifying a feedstock are provided. A gasifier can include a transfer line having a first leg and a second leg. A first end of the first leg can be adapted to be coupled to a cyclone and a second end of the first leg can be coupled to a first end of the second leg. The second end of the second leg can be adapted to be coupled to a standpipe. A centerline through the first leg can be oriented at an angle with a centerline through the second leg of from about 40° to about 140°.

Abstract: Fluid catalytic cracking units having risers with improved hydrodynamics through the use of baffles are described. The baffles break up the high concentration of catalyst in the slower moving outer annulus and redistribute it into the faster moving, more dilute center of the riser flow.

Abstract: A fluidized bed reactor system is disclosed. The system may be used in connection with a locally cooled gas distribution plate, which may control the reaction and increase system efficiency. A thermal bridge breaking system for disrupting heat transfer across the reactor is also disclosed. The thermal bridge breaking system may be provided in connection with, or separate from, the gas distribution plate cooling system.

Abstract: A hydrocarbon synthesis reaction apparatus includes a reactor, and a synthesis gas supply line through which a synthesis gas is supplied to the reactor, and syntheses hydrocarbons by contacting the synthesis gas and the catalyst slurry in the reactor. The hydrocarbon synthesis reaction apparatus includes a spare supply line which is connected to the synthesis gas supply line, and supplies inert gas or hydrogen gas to the reactor through the synthesis gas supply line when supply of the synthesis gas to the synthesis gas supply line from the synthesis gas supply device is stopped, and a fluid heating device which heats at least one of a fluid which flows through a flowing line of the synthesis gas supply line located closer to the reactor than a portion connected with the spare supply line, and a fluid which flows through the spare supply line.

Abstract: An apparatus for catalytic cracking of feedstock includes a first channel in which a feedstock is treated with an adsorbent to obtain a treated intermediate. The apparatus further comprises a separator-reactor vessel. The separator-reactor vessel includes an adsorbent separating region to remove the adsorbent from the treated intermediate. The separator-reactor vessel further includes a second channel connected to the adsorbent separating region. The treated intermediate is contacted with a catalyst in the second channel to produce a cracking yield. The second channel terminates in a catalyst separating region of the separator-reactor vessel. The catalyst is removed from the cracking yield in the catalyst separating region. The separator-reactor vessel further includes a physical partition disposed between the adsorbent separating region and the catalyst separating region to separate the two regions.

Abstract: The thermochemical conversion of biomass material to one or more reaction products includes generating thermal energy with at least one heat source, providing a volume of feedstock, providing a volume of supercritical fluid, transferring a portion of the generated thermal energy to the volume of supercritical fluid, transferring at least a portion of the generated thermal energy from the volume of supercritical fluid to the volume of feedstock, and performing a thermal decomposition process on the volume of feedstock with the thermal energy transferred from the volume of supercritical fluid to the volume of the feedstock in order to form at least one reaction product.

Abstract: Methods and systems utilizing gas jets to carry biomass into a biomass conversion reactor are described. Reactor configurations and conditions for carrying out processes utilizing the gas jets are also described. The use of gas jets has been found to be especially desirable for operation with pyrolysis of biomass in catalytic fluidized bed reactors.

Abstract: A process or a system for converting a solid biomass material is provided, comprising contacting the solid biomass material with a catalytic cracking catalyst at a temperature of more than 400° C. in a riser reactor to produce one or more cracked products. The riser reactor contains: a riser reactor pipe, which riser reactor pipe has a diameter that increases in a downstream direction; and a bottom section connected to the riser reactor pipe, which bottom section has a larger diameter than the riser reactor pipe.

Abstract: An integrated drying gasification system comprises a gasifier for gasifying carbonaceous fuel to produce hot product gas and an entrained flow dryer which receives the hot product gas to dry the carbonaceous fuel prior to gasification. At least one inlet to the gasifier communicates one or more additional gases from the system, such as recycled syngas, steam and/or recycled carbon dioxide, to the gasifier to generate an increased hot product gas mass flow rate from the gasifier. The system may comprise a plurality of lock hopper systems coupled to the entrained flow dryer. At least one intermediate storage vessel may be provided in one or more feed legs to the gasifier maintain a constant supply of carbonaceous fuel to the gasifier for a temporary period independently of carbonaceous fuel supplied to the entrained flow dryer.

Abstract: The disclosed invention relates to a process, comprising: conducting unit operations in at least two process zones in a process microchannel to treat and/or form a non-Newtonian fluid, a different unit operation being conducted in each process zone; and applying an effective amount of shear stress to the non-Newtonian fluid to reduce the viscosity of the non-Newtonian fluid in each process zone, the average shear rate in one process zone differing from the average shear rate in another process zone by a factor of at least about 1.2.

Abstract: 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.

Abstract: A gasification furnace (110) of a circulation fluidized bed-type gasification furnace (100) forms a fluid medium into a fluid bed, and produces gasified gas by gasifying an input gasification raw material using heat from the fluid medium. A combustion furnace (102) heats the fluid medium output from the gasification furnace. A flow rate adjuster (106) distributes the fluid medium heated in the combustion furnace to the gasification furnace and a buffer section (112). In this manner, irrespective of the flow rate of the fluid medium in the entire circulation fluidized bed-type gasification furnace (100), the buffer section (112) enables the fluid medium to bypass to the combustion furnace. As a result, the flow rate of the fluid medium in the gasification furnace (110) can be maintained at a desired flow rate.

Abstract: The present disclosure pertains to biomass pyrolysis processes and systems that decrease entrainment of char and other contaminants in the pyrolysis vapors by filtering the vapors in a heated container comprising a moving bed granular filter (MBGF), which in turn, comprises granular heat carrier. The granular heat carrier is heated within the MBGF and fed directly to the pyrolysis reactor, optionally along with filtered solids such as char. In certain embodiments, the MBGF additionally comprises at least one upgrading catalyst that contacts the vapors to produce a hydrocarbon mixture fungible with a petroleum-derived transportation fuel, a hydrocarbon transportation fuel component, or mixtures thereof.

Abstract: Most of the abundant naturally occurring low rank coal, which has a high moisture content and a high oxygen content, is transported with poor efficiency; utilized for heating with degraded thermal efficiency because of the loss of heat due to sensible heat for heating moisture and latent heat for vaporizing moisture; and utilized in existing coal combustion facilities with difficulty due to a high volatile component content.

Abstract: A fluidized bed reactor system is disclosed. The system may be used in connection with a locally cooled gas distribution plate, which may control the reaction and increase system efficiency. A thermal bridge breaking system for disrupting heat transfer across the reactor is also disclosed. The thermal bridge breaking system may be provided in connection with, or separate from, the gas distribution plate cooling system.

Abstract: An apparatus and process are presented for drying a catalyst in a reactor-regenerator system. The process includes a continuous operating system with catalyst circulating between a reactor and regenerator, and the catalyst is dried before returning the catalyst to the reactor. The process uses air that is split between the drying stage and the combustion stage without adding equipment outside of the regenerator, minimizing energy, capital cost, and space requirements.

Abstract: A system and process for melamine production by gas-phase quenching method and its process are provided. The said system includes a urea scrubber, after which a fluidized bed reactor, a hot-air cooler, a hot-air filter, a crystallizer and a melamine collector are installed in series successively, where the said melamine collector is connected to the said urea scrubber and the said fluidized bed reactor is connected to a carrier gas pre-heater which is connected to a carrier gas compressor; the said system further includes a gas-liquid separator which is connected to the said urea scrubber which is connected to a crystallizer; wherein a cool air blower is provided between the said gas-liquid separator and the crystallizer. The production system of the invention has the advantages of high productivity, stable operation, low energy consumption, low investment and high economic value of tail gas.

Abstract: Methods and apparatus for the commercial-scale production of purified polycrystalline silicon granules with one or more tailored levels of n- and p-type impurities from an impure silicon source such as, for example, metallurgical-grade silicon.

Abstract: A fluidized bed reactor is disclosed. The fluidized bed reactor includes a head; a first body part connected with the head, located under the head, the first body part having a first reaction pipe provided therein; a second body part connected with the first body part, located under the first body part, the second body part having a second reaction pipe provided therein; and a bottom part connected with the second body part, located under the second body part, the bottom part having a flowing-gas supply nozzle, a reaction gas supply nozzle, a heater and an electrode assembled thereto.

Abstract: Process for heating a polymer-containing stream being transferred from a polymerization reactor to a separation zone or device, by passing the stream through at least two heaters operating in parallel, each heater having at least one transfer line for the stream and a heater for heating the transfer line. The average particle of the polymer is below 3 mm, the temperature of the polymer-containing stream at the outlet of all heaters is maintained above the dew point of the stream, and no heater has a volumetric flowrate of polymer-containing stream more than three times that of any other heater.

Abstract: A power generation system for converting organic material into thermal energy and electric power. A reaction of organic material with supercritical water, —OH radicals, and muon methyl radicals are released from a catalytic bed of silica particles in suspended initially transform the organic material into thermal energy. A Nano monomolecular film located on an interior surface of the reaction chamber interacts with plasma formed by conversion of the organic material into thermal energy to produce ion plasma electromagnetic energy. One or more magnetic-coil generators positioned adjacent to the reaction chamber interacts with the electromagnetic energy to produce electric power.

Abstract: To provide a treatment method having excellent purification effect, in which impurities having high ionicity in a silica powder can be removed in a short time, an apparatus thereof, and a purified silica powder. A purification method of a silica powder comprises making a silica powder into a fluid state; contacting a purified gas to the silica powder in the fluid state at high temperature; and thereby removing impurity components of the silica powder. In the method, the silica powder in the fluid state is positioned in a magnetic field region. Further, the silica powder is contacted with the purified gas, while applying voltage to the silica powder by an electric field generated by moving of the silica powder. Preferably, the silica powder in a fluid state is positioned in the magnetic region of 10 gausses or more, and contacted with the purification gas at a temperature of I000° C. or more.

Abstract: In one embodiment of the invention, the silane and hydrogen (and inert gas) mixture is produced using catalytic gasification of silicon (or si-containing compounds including silicon alloys) with a hydrogen source such as hydrogen gas, atomic hydrogen and proton. By not separating silane from hydrogen and co-purifying all the gases (silane and hydrogen, inert gas) in the gas mixture simultaneously, the mixture is co-purified and then provide feed stock for downstream application without further diluting the silane gas. One aspect of the invention addresses the need for an improved production method, apparatus and composition for silane gas mixtures for large scale low cost manufacturing of high purity silicon and distributed on-site turnkey applications including but not limited to the manufacture of semiconductor integrated circuits, photovoltaic solar cells, LCD-flat panels and other electronic devices.

Abstract: Dry dust removal method in organic chlorosilane production is provided, in which the detailed steps are as follows: delivering high-temperature flue gas (a) from fluidized bed reactor (I) into inorganic film cross-flow filter (E) to remove dust for the first time; delivering the concentrated dust gas (c) trapped by inorganic film cross-flow filter (II) into bag filter (III) to remove dust for the second time; returning the gas mixture (f) of passing through bag filter (EI) to the air intake of inorganic film cross-flow filter (II); condensing the residual clean gas (b) from the osmotic side of inorganic film in condenser (A), and then rectifying in rectifying column (B) to separate the products of chloromethane (g) and methyl chlorosilane (h) to obtain the product of methyl chlorosilane (h); returning chloromethane to fluidized bed reactor to take part in reaction; retreating the dust (e) trapped by inorganic film cross-flow filter and bag filter, and then returning it to fluidized bed reactor (I) to take par

Abstract: A reactor (6) for pyrolysing waste, in particular rubber tires, said reactor comprising a pyrolysis space (68), an inlet port (63) and an outlet port (64) enabling a flow across the pyrolysis space (68) of a heating medium for transferring heat required for the pyrolysis, and a lower discharge port (62) for discharging solid residues of the pyrolysis. The invention is, characterized in that—it comprises a baffle means (65) made of a plate material and enabling a gravitational slipping of the solid residues towards the discharge port (62), which baffle means (65) has openings (66) allowing the flow of the heating medium and is arranged to divide the inner space of the reactor (6) to form an upper pyrolysis space (68) and a lower space and—one of the inlet and outlet ports (63, 64) is in connection with the pyrolysis space (68) and the other one with the lower space. The invention is also an apparatus comprising the above reactor (6).

Abstract: According to one embodiment, there is provided a graphite nano-carbon fiber provided by using an apparatus having a reactor capable of keeping a reducing atmosphere inside thereof, a metal substrate arranged as a catalyst in the reactor, a heater heating the metal substrate, a pyrolysis gas source supplying pyrolysis gas obtained by thermally decomposing a wood material in a reducing atmosphere to the reactor, a scraper scraping carbon fibers produced on the metal substrate, a recovery container recovering the scraped carbon fibers, and an exhaust pump discharging exhaust gas from the reactor. The carbon fibers are linear carbon fibers with a diameter of 25 to 250 nm formed with layers of graphenes stacked in a longitudinal direction.

Abstract: A gas hydrate production apparatus capable of reacting a raw gas with a raw water to thereby form a slurry gas hydrate and capable of removing water from the slurry gas hydrate by means of a gravitational dewatering unit. The gravitational dewatering unit is one including a cylindrical first tower body; a cylindrical dewatering part disposed on top of the first tower body; a water receiving part disposed outside the dewatering part; and a cylindrical second tower body disposed on top of the dewatering part, wherein the cross-sectional area of the second tower body is continuously or intermittently increased upward from the bottom.

Abstract: Embodiments of apparatuses and methods for controlling heat for rapid thermal processing of carbonaceous material are provided herein. The apparatus comprises a reactor, a reheater for forming a fluidized bubbling bed comprising an oxygen-containing gas, inorganic heat carrier particles, and char and for burning the char into ash to form heated inorganic particles. An inorganic particle cooler is in fluid communication with the reheater. The inorganic particle cooler comprises a shell portion and a tube portion. The inorganic particle cooler is configured such that the shell portion receives a portion of the heated inorganic particles and the tube portion receives a cooling medium for indirect heat exchange with the portion of the heated inorganic particles to form partially-cooled heated inorganic particles.

Abstract: A fluidized bed reactor arrangement includes at least a bottom portion, a roof portion, and at least one side wall vertically extending between the bottom portion and the roof portion. The side wall is arranged to be inclined at the lower portion in such a manner that the cross section of a reaction chamber of the reactor diminishes towards the bottom portion. The fluidized bed reactor arrangement also includes a heat exchange chamber, in which the inclined side wall forms a partition wall between a heat exchange chamber and the reaction chamber. The rear wall of the heat exchange chamber is connected to the side wall of the reaction chamber from the upper portion of the rear wall at a connection area in such a manner that the direction thereof aligns with the direction of the side wall at least at the connection.

Abstract: Catalyst regenerators and methods for using same. The regenerator can include a regenerator housing containing a dense phase catalyst bed for receiving a catalyst to be regenerated. A heater can be disposed in the regenerator and can have a fuel nozzle configured to eject a mixture of fuel and an oxygen-lean gas for combustion to supplement the heat to satisfy the reactor heat demand when a light feedstock cracked that may not provide sufficient coke formation on the catalyst to fully satisfy the reactor heat demand.

Abstract: Systems and processes for the alkylation of a hydrocarbon are provided that utilize a plurality of moving bed radial flow reactors. An olefin injection point can be provided prior to each reactor by providing a mixer that mixes olefin with a hydrocarbon feed, or with the effluent stream from an upstream reactor, to produce a reactor feed stream. Catalyst can be provided from the reaction zone of one reactor to the reaction zone of a downstream reactor through catalyst transfer pipes, and can be regenerated after passing through the reaction zones of the reactors. The moving bed radial flow reactors can be stacked in one or more reactor stacks.

Abstract: Methods and systems for preparing catalyst, such as chromium catalysts, are provided. The valence of at least a portion of the catalyst sent to an activator is changed from Cr(III) to Cr(VI). The catalyst is prepared or activated continuously using a fluidization bed catalyst activator.

Abstract: A method of processing polymer materials, highly filled or otherwise to recover cyclic structures or monomers. The method involves providing a vessel having a heated side wall, an agitator, and at least one of an additional heated structure, other than the heated side wall, within the vessel and means for forming a thin coat of material processed in the vessel on said heated side wall. A polymer material is fed into the vessel and heated to a sufficient temperature to cause depolymerization of the polymer material into cyclic structures or monomers. The cyclic structures or monomers are removed from the vessel and collected. The method does not require the use of a solvent.

Abstract: A process for producing calcine products includes dead roasting a metal sulfide concentrate having a low sulfur content. The concentrate is roasted in a circulating fluidized bed at a temperature of about 950 to 1050° C. A waste gas of the fluidized bed is passed through at least one of a recuperator and a Venturi drier so as to respectively provide at least one of a preheating of at least a portion of air fluidizing the fluidized bed and a drying of at least a portion of the concentrate to be roasted. The calcine product obtained in the fluidized bed with a sulfur content of less than 1 wt-% is provided for further processing.