WO2010049617A1 - Dispositif de lit fluidise a fluidisation rapide et a flux sature de solides circulants - Google Patents
Dispositif de lit fluidise a fluidisation rapide et a flux sature de solides circulants Download PDFInfo
- Publication number
- WO2010049617A1 WO2010049617A1 PCT/FR2009/051964 FR2009051964W WO2010049617A1 WO 2010049617 A1 WO2010049617 A1 WO 2010049617A1 FR 2009051964 W FR2009051964 W FR 2009051964W WO 2010049617 A1 WO2010049617 A1 WO 2010049617A1
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- WO
- WIPO (PCT)
- Prior art keywords
- reactor
- cyclone
- solids
- pipe
- fluidized bed
- Prior art date
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Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/005—Separating solid material from the gas/liquid stream
- B01J8/0055—Separating solid material from the gas/liquid stream using cyclones
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/08—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles
- B01J8/082—Controlling processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/1809—Controlling processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/1872—Details of the fluidised bed reactor
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C10/00—Fluidised bed combustion apparatus
- F23C10/005—Fluidised bed combustion apparatus comprising two or more beds
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C10/00—Fluidised bed combustion apparatus
- F23C10/02—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed
- F23C10/04—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone
- F23C10/08—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone characterised by the arrangement of separation apparatus, e.g. cyclones, for separating particles from the flue gases
- F23C10/10—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone characterised by the arrangement of separation apparatus, e.g. cyclones, for separating particles from the flue gases the separation apparatus being located outside the combustion chamber
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
Definitions
- the invention relates to a circulating fluidized circulating fluidized bed device with fast fluidization and saturated flow of circulating solids.
- a circulating fluidized bed device has a circulating loop configuration of solids associating a reactor, a cyclone, a solids return, exchangers and a set of operating parameters in terms of gas velocity in empty casks, circulating granulometry and flow rate. solid.
- EP 0 147 445 discloses a circulating fluidized bed device with fast fluidization. If with a multi-solid device as described in this document, the fluidization velocity reaches relatively high values, the pressure drop in the flow zone of solids out dense bed is relatively low. The concentration of the flow of circulating solids is therefore relatively low.
- the neighboring enriched air combustion technology reduces the flue gas flow rate and possibly boosts the power of an existing installation or the combustion temperature for ores to be calcined, but there remains a nitrogen content in the flue gas fumes. carbon dioxide and water that is to be treated downstream if only carbon dioxide is to be produced for final storage after condensation of the water vapor.
- the technical problem is to obtain the complete conversion of the carbonaceous substances and to circulate enough oxygen-carrying solids. at much higher fluxes than those obtained by conventional circulating fluidized bed technology.
- thermochemical cycle conversions it is better external recirculation to the reactor which is sought, ie better reactor / cyclone circulation. return / reactor and thus a passage of a maximum of particles from the top of the reactor to the cyclone.
- the object of the invention is to propose a fast fluidized bed device which makes it possible to reach solid external circulation rates three to five times higher than those of conventional circulating fluidized bed technology, while lowering the cost of equipment by improved compactness.
- the invention proposes a fast fluidized bed device comprising a reactor, at least one solid separation cyclone at the outlet of this reactor, comprising a so-called upper ceiling wall, a solid return line to the outlet reactor. solids of said cyclone and exchangers associated with the flue gas circuit at the outlet of said cyclone, a pipe connecting in the upper part said reactor to said cyclone, characterized in that said conduit opens into said cyclone ceiling.
- the invention also relates to a process for implementing such a fast fluidized bed device, characterized in that a fuel and / or a reaction support having a particle size of less than 100 microns for 90% of its quantity is injected. in said reactor.
- the invention relates to a method for implementing such a fast fluidized bed device, characterized by the same axial gas velocity of between 7 and 9 m / s in said reactor and in said cyclone.
- the invention finally relates to a method of implementing such a fast fluidized bed device, characterized by a concentration of solids at the place where said pipe opens into said cyclone ceiling, between 20 and 60 kg / Nm 3 at full charge.
- Figure 1 is a vertical sectional view of a fast fluidized bed device according to the invention.
- Figure 2 is a partial perspective view of a circulating fluidized bed device according to the invention.
- Figure 3 is a partial vertical sectional view of a circulating fluidized bed device according to the invention.
- Figure 4 is a vertical sectional view of a circulating fluidized bed device according to the invention, according to another embodiment, particularly under pressure.
- Figures 5 and 6 are partial sectional views of a reactor according to the invention.
- Figure 7 is a half sectional view of another embodiment of a reactor according to the invention.
- Figure 8 is a top view of a set of reactors according to the invention.
- Figures 9 and 10 are views in vertical and horizontal section of an alternative embodiment.
- Figure 11 is a vertical sectional view of an alternative embodiment.
- Figures 12 and 13 each show an installation according to the invention.
- FIG. 14A to 14C show a vertical sectional detail, in front view and in horizontal sectional view, according to a first embodiment.
- FIG. 15 represents a detail in vertical section, according to a second variant embodiment.
- Figures 16A to 16C show a vertical sectional detail, in front view and in horizontal sectional view, according to a third embodiment.
- FIG. 1 represents a fast fluidized bed device, comprising a reactor 1, a pipe 6 connecting a cyclone 2 for separating the solids at the outlet of this reactor, comprising a top wall 2A called a ceiling, a solid return pipe 4 to the reactor at the outlet of solids of cyclone 2 and exchangers 5 associated with the flue gas circuit at the exit of cyclone 2.
- the walls of the reactor, ducts and cyclone are preferably cased walls, covered with refractory but may be made of sheet metal with refractory lining thick.
- a pipe 6 connects the reactor 1 to the cyclone 2 at the top and opens into the ceiling 2A of the cyclone.
- this pipe 6 is substantially axial to the reactor 1 in a first section 6A in the upper part of the reactor, with upwardly directed flow, aligned with or parallel to the vertical axis of symmetry of the reactor.
- This first section 6A where a solids and gas velocity of 25 to 35 m / s can be obtained at the outlet of this section 6A, is connected to the reactor 1 by a frustoconical part of acceleration IA forming the ceiling of the reactor, inclined from 15 to 60 ° with respect to a horizontal plane.
- This ceiling IA may be circular or square section.
- An inlet transverse deflector 6C is disposed near the inlet of the first section 6A of the pipe 6 connecting the reactor and the cyclone. This deflector 6C accelerates and concentrates the diluted solids in a concentrated layer.
- This first deflector 6C is followed by a second directional deflector 6D which allows to concentrate the solids again.
- This first section 6A comprises at its inlet a restriction skirt section 7, providing a section of 3 to 7 times less than the cross section of the reactor 1, where air or reactive fluid can be injected at a speed of 80 at 150 m / s to allow the control of the external circulation of solids at the desired level by the operating load of the installation and therefore by the residence time of the solids in the conversion zones of two interconnected reactors, for example.
- This skirt 7 is therefore flared in shape, of lower horizontal section at its lower end and advantageously comprises fluidization injections at this lower end and expansion joints near its upper end.
- This pipe 6 is inclined in a last section 6B in the upper part of the cyclone, flow directed downwards, the inclination being at least 35 ° relative to a horizontal plane. This inclination of 35 ° can be reduced to 20 ° if this section has auxiliary fluidizations. Thus, a dense phase flow is obtained at the bottom of this last section 6B and a mass gravity flow of the solids is favored.
- this first section 6A and this last section 6B are connected by an intermediate section 6E with an inclined lower bottom providing a flow angle of at least 20 °.
- the pipe 6 opens into the ceiling 2A of the cyclone near the periphery of the latter by a slot 3 in an arc of a constant width.
- the outer peripheral edge of this slot 3 is arranged in continuity with the cylindrical wall of the cyclone 2, in order not to reduce the speed of the solids and contributes to an optimal gas / solids separation efficiency in the cyclone.
- Cyclone 2 has a side smoke outlet 2B, its lower cone, or central 2B ', its ceiling, bringing these fumes to the heat exchangers 5.
- a horizontal heat recovery boiler, posed, can be installed, as shown in FIG. 1.
- the cyclone is provided with an internal cylindrical skirt 2B "which faces the end of the outlet 2B with a distance between them. skirt 2B "is to prevent a direct passage of the circulating solids to the outlet 2B.
- the solids return line 4 at the exit of the cyclone is frustoconical at least on its lower part, flared by an overall angle ⁇ of 5 to 10 °, its section increasing downstream of the outlet of the cyclone towards its lower end. Its lower end is connected to a U-shaped device 8 with rounded internal angles. As a variant shown in FIG. 3, this device 8 may be U-shaped at angles formed by faces 8A inclined by 45 °. This return sheath solids 4 can be vertical or inclined at most
- This line 4 may comprise a bypass 8B to an adjacent reactor and means for introducing by gravity 8A fuels and / or fresh reaction solids. It may also include fluid injections walls and perforated 4A ventilation rods located in the heart of the flow to lubricate the walls and reduce friction coefficients.
- the U-shaped device 8 ensures a blockage of the direct passage of gas from the bottom of the reactor 1 at higher pressure to the return line of the solids 4. It comprises a supply 8A by gravity fuel and / or solid reaction media. Its rising part is of a height h, of value between the value of its diameter and three times this diameter value, in order to minimize the pressure losses.
- Figures 9 to 11 show alternative embodiments of this U-shaped device and the return of the solids to the (s) reactor (s).
- Figures 9 and 10 show an embodiment of multiple returns of solids to several reactors.
- the return sheath of solids 4 at the outlet of cyclone 2 opens into an enclosure 18 provided on its bottom bottom of fluidization injection and carrying on its upper part four downwardly inclined pipes and two of which 19, 20 can be connected to the reactor 1, one of which can be connected to another reactor and one of which can be connected to an exchanger.
- the arrangement of U previously described here is shaped three-dimensionally around the return sheath 4.
- FIG. 11 shows an arrangement of U 28 connected to the lower part 12 of the reactor 1. It is then a part of the reactor wall that forms the U. This arrangement comprises fluidization injections 29 on its lower bottom.
- the lower part of the reactor 1 has an inclined wall provided with primary fluidization injections 30.
- such a fast fluidized bed device can be pressurized, by a moderate pressurization of the order of 6 to 10 bar, the cased walls then being completed by a second metal enclosure external resistant to internal pressure.
- the connecting pipe 6 'of the reactor 1' and cyclone 5 'then only has a first axial portion 6'A, at the top of the reactor, with upwardly directed flow and a last section 6'b inclined at the top. cyclone, downwardly directed flow, the inclination being at least 20 ° with respect to a horizontal plane.
- Such a pipe arrangement 6 'therefore does not comprise an intermediate section of horizontal direction, as seen in FIG. 2. It should be noted that even in the case of a non-pressurized device, an arrangement according to FIG. 4 can be used. and is even advantageous because suppressing a horizontal directional transfer of solids between the reactor and the cyclone.
- a reactor 1 for a fast fluidized bed in accordance with the invention comprises a substantially cylindrical enclosure 10 for pressurized applications, of polyhedral section, preferably square or rectangular, a top 11 of connection to the inlet of the solids separation cyclone 2 and a lower connection portion 12 to the cyclone solids outlet line 4 of corresponding shape.
- the enclosure 10 may be of substantially constant section, as illustrated, or be flared at an angle of about 5 °, its lower section being at the top.
- the enclosure 10 comprises re-mixing profiles 13 in the form of ribs, internal annular of constant section, for example trapezoidal, distributed over at least a part of its height and preferably, as shown, over the entire height of the pregnant.
- ribs 13 have dimensions dependent on the dimensions of the reactor and have a thickness of between 50 and 400 mm and are spaced from each other by a distance of 1 to 4 m.
- these ribs 13 have the function of separating the downward axial annular flow layer of solids which is formed in the upper part of the reactor and deflecting it towards the upstream central gas flow core. at high speed loaded in finer solids.
- FIGS. 14 to 16 Three embodiments of the re-mixing ribs are shown in FIGS. 14 to 16.
- FIGS. 14A to 14C show cased ribs 102 which are created by tubes deported at a certain periodicity, for example every other tube, from a wall formed of common tubes 101 and welded fins 100. These ribs are coated with a refractory lining 103.
- Figure 15 shows ribs on anchors 106 welded to a wall consisting of common tubes 101 and welded fins 100, on which is cast or tamped a refractory lining 103 which gives the desired geometry.
- FIGS. 16A to 16C show ribs on perforated horizontal metal shelves 104 supported by vertical stiffenesses 105 periodically welded to a wall consisting of common tubes 101 and welded fins 100.
- a refractory lining 103 provides the desired geometry.
- the lower part 12 of the reactor, shown in FIG. 6, has an inlet 14 that is substantially axial, that is to say aligned with the vertical symmetry axis of the reactor, with frustoconical, multi-frustoconical or conical shaped solids.
- the kinetic energy loss of the flow rates of circulating solids is minimized and thus an accumulation of solids in the lower part of the reactor is avoided which is a typical characteristic of the circulating fluidized bed. It is therefore no longer necessary to use as much fluidization energy and the internal erosions of the refractories and fluidization nozzles are also minimized.
- the fluidization speeds are between 10 and 40 m / s in this lower part.
- the reactor 1 may therefore be devoid of multiple nozzle fluidization grid, which is a complex and expensive investment component, subject to plugging and erosion.
- the reactor 1 comprises injections 15 of fluidization means on three to five levels in walls of the enclosure 10 and the lower part 12.
- This lower part also comprises at least one gravity inlet 8A of fuel and / or solid reaction supports, situated downstream of the U-shaped device 8 which may also comprise an injection 15 'of fluidization means at its base, and an extraction arrangement 16 of the solids.
- This gravity inlet can be equipped with a concentric axial injection of gas to form a gas screen and avoid collages to the walls.
- the injections in fluidization means 15, 15 ' make it possible to precisely control the velocity profile of the gases in the primary zone of acceleration of the solids formed by the lower part 12 of the reactor. This acceleration is essential to achieve an appropriate flow rate of circulating solids in the loop and to carry out the desired reactions in the reactor 1.
- the reactor 1 may contain at least one integrated bed 14 ', as shown in FIG. 7, which can be installed on one or more faces of the reactor. Secondary air supplies 15 may be adjusted to promote solids filling of this bed 14 '.
- Such an integrated bed can operate in a fluidized bed or in a moving bed and makes it possible to control the inventory in circulation for a given global inventory and to control the flow of solids in external circulation to another reactor.
- This integrated bed 14 ' may comprise a line 14A to another reactor and can act as a carbon and sulfur barrier between two interconnected reactors.
- a method of implementing such a fast fluidized bed device consists of injecting into the reactor 1 a fuel and / or a reaction support, depending on the application, with a particle size of less than 100 microns for 90% of its quantity and injecting a fluidization gas at the bottom of the reactor 1, at a speed of the order of 10 to 40 m / s at the bottom of the reactor 1, the gas velocity being between 7 and 9 m / s in the reactor 1 and in the cyclone 2.
- the concentration of solids where said pipe 6, 6 'opens into said ceiling 2A, 2'A of the cyclone between 20 and 60 kg / Nm 3 at full load.
- the circulating fluidized bed device according to the invention has the optimum characteristics to ensure rapid fluidization and a saturated flow of circulating solids.
- the pipe 6 according to the invention has a absence of horizontal section, connecting the first section 6A and the last section 6B, and therefore results in a minimum of loss of velocity and kinetic energy and avoids any accumulation of solids that would disturb the flow, while ensuring peripheral entry into the cyclone, optimally directed for separation of solids and fumes.
- This link pipe arrangement also makes it possible to substantially lower the height of cyclone 2 relative to the ceiling of reactor 1 and thus to reduce the overall height of the installation and the supporting frameworks and thus substantially improve the compactness and reduce investment costs.
- the frustoconical shape of this pipe 4 avoids any agglomerate and any stagnant zone, bridging type, solids.
- the rounded or beveled shape of the device 8 according to the invention avoids loss of speed and therefore energy, at the level of from these angles.
- the reactor which conventionally has vertical cased walls and lateral return in solids
- the presence of the re-mixing ribs 13 ensures optimal mass and heat transfer between the gases and the different types of solids present in the reactor.
- the reactor and the substantially axial inlet 14 of the solids minimizes the kinetic energy loss of the flow rates of circulating solids.
- reactor 1 and cyclone 2 forms a simple modular structure since reactor and cyclone are characterized only by the same speed axial from 7 to 9 m / s. It is therefore possible to arrange such elementary modules in lines or polygons. We can then build a set of 2, 3, 4, 6, 8 reactors is the equivalent of 100 to 800 MWe for a combustion boiler air at atmospheric pressure.
- FIG. 8 illustrates the case of an assembly consisting of six elementary modules reactor 1 and cyclone 2.
- two cyclones 2 1 and 2 2 are associated with the reactor 1.
- the two cyclones are shaped according to the invention, with the line O 1 and 6 2 connecting the reactor and the cyclone opening into the reactor. ceiling of each cyclone.
- FIG. 13 only one cyclone 2i is thus produced, the other cyclone 2 2 being disposed at mid-height of the reactor 1 by means of a lateral outlet. There is then withdrawal of the solids at mid-height and in the upper part.
- Such a rapid fluidized bed device has many applications and in particular can form: a combustion system, solid, liquid or gaseous fuels containing carbon of fossil or non-fossil origin and intended for the production of steam; this combustion may be carried out in air, with air enriched with not more than 90% oxygen or with recycled fumes enriched with not more than 90% oxygen; a combustion system with metal and alkali oxides in the oxidation and reduction oxygen transport cycle, comprising injections of air or enriched air for the oxidation of the oxides and of recycled water vapor / CO2 for the reduction oxides, solid, liquid or gaseous fuels containing carbon of fossil or non-fossil origin and intended for the production of steam; a system of the same type as the previous ones but of gasification of fuels of all kinds; a system of the same type as the previous ones but of pyrolysis of fuels of all kinds; a system for cracking petroleum cuts or even bitumens and crude oils; a system for capturing sulfur oxides, chlorine compounds or carbon
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Fluidized-Bed Combustion And Resonant Combustion (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
Description
Claims
Priority Applications (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP09756029A EP2342006A1 (fr) | 2008-10-30 | 2009-10-15 | Dispositif de lit fluidise a fluidisation rapide et a flux sature de solides circulants |
CA2740506A CA2740506C (fr) | 2008-10-30 | 2009-10-15 | Dispositif de lit fluidise a fluidisation rapide et a flux sature de solides circulants |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR0857388A FR2937876B1 (fr) | 2008-10-30 | 2008-10-30 | Dispositif de lit fluidise a fluidisation rapide et a flux sature de solides circulants |
FR0857388 | 2008-10-30 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2010049617A1 true WO2010049617A1 (fr) | 2010-05-06 |
Family
ID=40732260
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/FR2009/051964 WO2010049617A1 (fr) | 2008-10-30 | 2009-10-15 | Dispositif de lit fluidise a fluidisation rapide et a flux sature de solides circulants |
Country Status (4)
Country | Link |
---|---|
EP (1) | EP2342006A1 (fr) |
CA (1) | CA2740506C (fr) |
FR (1) | FR2937876B1 (fr) |
WO (1) | WO2010049617A1 (fr) |
Citations (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4419965A (en) * | 1981-11-16 | 1983-12-13 | Foster Wheeler Energy Corporation | Fluidized reinjection of carryover in a fluidized bed combustor |
US4664888A (en) * | 1985-06-27 | 1987-05-12 | Texaco Inc. | Fluid catalytic cracking catalyst-vapor separator |
US4969930A (en) * | 1989-02-22 | 1990-11-13 | A. Ahlstrom Corporation | Process for gasifying or combusting solid carbonaceous material |
US5339774A (en) * | 1993-07-06 | 1994-08-23 | Foster Wheeler Energy Corporation | Fluidized bed steam generation system and method of using recycled flue gases to assist in passing loopseal solids |
US20040076554A1 (en) * | 2002-10-18 | 2004-04-22 | Kuechler Keith Holroyd | Multiple riser reactor with centralized catalyst return |
US20070049782A1 (en) * | 2005-08-31 | 2007-03-01 | Patel Rutton D | Riser termination devices for reduced catalyst attrition and losses |
Family Cites Families (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR2662619B1 (fr) * | 1990-06-05 | 1993-02-05 | Inst Francais Du Petrole | Melangeur-separateur cyclonique a co-courant et ses applications. |
JP4852365B2 (ja) * | 2006-07-12 | 2012-01-11 | 財団法人 国際石油交流センター | 気固分離器 |
-
2008
- 2008-10-30 FR FR0857388A patent/FR2937876B1/fr not_active Expired - Fee Related
-
2009
- 2009-10-15 WO PCT/FR2009/051964 patent/WO2010049617A1/fr active Application Filing
- 2009-10-15 CA CA2740506A patent/CA2740506C/fr not_active Expired - Fee Related
- 2009-10-15 EP EP09756029A patent/EP2342006A1/fr not_active Withdrawn
Patent Citations (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4419965A (en) * | 1981-11-16 | 1983-12-13 | Foster Wheeler Energy Corporation | Fluidized reinjection of carryover in a fluidized bed combustor |
US4664888A (en) * | 1985-06-27 | 1987-05-12 | Texaco Inc. | Fluid catalytic cracking catalyst-vapor separator |
US4969930A (en) * | 1989-02-22 | 1990-11-13 | A. Ahlstrom Corporation | Process for gasifying or combusting solid carbonaceous material |
US5339774A (en) * | 1993-07-06 | 1994-08-23 | Foster Wheeler Energy Corporation | Fluidized bed steam generation system and method of using recycled flue gases to assist in passing loopseal solids |
US20040076554A1 (en) * | 2002-10-18 | 2004-04-22 | Kuechler Keith Holroyd | Multiple riser reactor with centralized catalyst return |
US20070049782A1 (en) * | 2005-08-31 | 2007-03-01 | Patel Rutton D | Riser termination devices for reduced catalyst attrition and losses |
Non-Patent Citations (1)
Title |
---|
See also references of EP2342006A1 * |
Also Published As
Publication number | Publication date |
---|---|
FR2937876A1 (fr) | 2010-05-07 |
EP2342006A1 (fr) | 2011-07-13 |
CA2740506C (fr) | 2016-02-02 |
CA2740506A1 (fr) | 2010-05-06 |
FR2937876B1 (fr) | 2011-03-25 |
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