CA1264524A - Apparatus for separating solid material in a circulating fluidized bed reactor - Google Patents
Apparatus for separating solid material in a circulating fluidized bed reactorInfo
- Publication number
- CA1264524A CA1264524A CA000494411A CA494411A CA1264524A CA 1264524 A CA1264524 A CA 1264524A CA 000494411 A CA000494411 A CA 000494411A CA 494411 A CA494411 A CA 494411A CA 1264524 A CA1264524 A CA 1264524A
- Authority
- CA
- Canada
- Prior art keywords
- reactor
- duct
- flue
- return duct
- separator chamber
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
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Abstract
An apparatus for use in a circulating fluidized bed reactor for separating solid material from the flue gases and for recirculating the solid material to the reactor. The apparatus comprises a duct for directing the flue gases from the reactor slantingly downwards to a return duct adapted to return a part of the flues laden with solid particles back to the reactor. At a point of entry of particle laden gases into the return duct, a deflecting wall diverts a major portion of the gases to the inlet of a vortex separator. The separator chamber has a discharge opening concentrical with its generally horizontal axis, for discharge of flues from which solid particles have been removed.
Description
i2~
APPARATUS FOR SEPARATING SOLID MATERIAL
IN A CIRCULATING Fl.UIDIZED BED REACTOR
The present invention relates to an apparatus for separating solid particles from the flue gases of a reactor and for recycling the separated solids to the reactor.
Circulating fluidized bea technique has long been used in various reactors such as calcinators and recently to a larger extent in combustion furnaces and gasifiers. In the known applications, the separation of solid6 is carried out in a conventional cyclone separator having a vertical axis and a hopper-shaped bottom. The cylindrical vortex chamher of the cyclone is provided with a gas discharge pipe which guides the gases upwards and the solids are recycled to the reactor through a stand pipe via a gas trap. The gas trap is employed to prevent reactor gase6 from flowing into the cyclone through the stand pipe. A mechanical trap is most commonly used as a gas trap. In more advanced applications a fluidized bed of sand in a U-pipe is known to have been applied for the purpose. The solids recycling system becomes complex and expensive especially in high temperature reactors. Part of the air required for fluidizing the gas trap flows upwards in the stand pipe which has a detrimental effect on the separation of solids, in particular on the 6eparation of light and fine particles.
Furthermore, the rising gas flow decreases the transport capacity of the stand pipe.
As is known, a substantial vacuum and a high axial flow velocity are created in the centre of a conventional cyclone due to which the cyclone tends to draw the particles from the stand pipe. The suction flow generated in this way has usually no tangential velocity. Thus, almost all the solid material the flow carries with it is transported out through the centre pipe of the cyclone.
A recycling system provided with a conventional cyclone is therefore very sensitive to the suction flow from the stand pipe and requires a reliable gas trap.
In steam boiler applications the use of a conventional cyclone results in disadvantageous constructions a~ a conventional cyclone divides the boiler into a separate combustion chamber and ~2~
~ convection part downstream of the cyclone between which the equipment for recycling the solids must be installed.
Mechanical gas traps are rapidly worn particularly in hot condition and breakdowns in their operation are frequent.
5 Also, applications having a conventional cyclone in~talled inside the reactor are known in which the whole solids recycling system is built inside the reactor. This application has, however, severe disadvantages such as cor~osion and erosion of the cyclone, as cooling of the supporting structure cannot be arranged in a simple way. Furthermore, as is the case in conventional cyclonss, the arrangment inside the reactor is subject to sensitivity to the suction flow from the stand pipe.
It is an object of the invention to provide an apparatus by whiQh solid particles can be efficiently separated from flue gases discharged from a circulating fluidized bed reactor, and recycled to a desired point in the reactor.
In general terms, the present invention provides apparatus for use with a circulating fluidized bed reactor, for separating solid particles from the flue gases of the reactor and for recycling the solid particles to the reactor, the apparatus comprising: a flue duct for guiding the flue gases of the reactor obliquely downwardly and away from the reactor; a vortex separator chamber having a generally horizontal axis; deflecting means for changiny the direction of the flow of a ma~or portion of the gases exiting from said flue duct to direct the ga~es into said vortex separator chamber; a return duat communicating with said flue duct and with one end of said vortex separator chamber; and a ga~ discharge concentric with ~aid generally horizontal axis and disposed in an end wall of the vortex separator chamber.
The invention will now be described by way of exemplary embodiments with reference to the accompanying diagrammatic, simplifi ed dra~i ~gs, wherein:
Fig. 1 illustrates an embodiment of the invention in a vertical sectional view taken along line A-A of Fig. 2;
Fig. 2 is a top view of the apparatus of Fig. l;
Fig. 3 is a view of a part of Fig. 1 in the direction of the arrow B;
Fig. 4 is another embodiment of the invention in a vertical ., . ~
~LZ6~L5;~D~
sec-tion taken along line C~C of Fig. 5;
Fig. 5 is a top view of the apparatu~ of ~ig. 4;
Fig. 6 is an alternative embodiment of the construction illustrated in Fig. 3;
Fig. 7 is yet another embodiment of the construction illustrated in Fig. 3; and Fig. 8 is a sectional view taken along line D-D of Fig. 2.
In Figs. 1, 2 and 3, reference numeral 1 refers to a vertical fluidized bed reactor from the upper part of which the flue gases flow obliquely downwardly and away from the reactor 1, through a flue duct 2. A separator 3 is disposed beside the reactor 1 such that the inlet section of its horizontal vortex chamber 4 and the discharge end of the flue duct 2 are di posed in a downwardly tapering transition chamber 5 which is formed between a lower wall 6 of the flue duct 2 and an intarmediata wall 7 connected tangentially to the cylindrical jacket of ~he vortex chamber 4.
The transition chamber 5 constitutes the inlet of a return duct for solid material. The return duct 8 has a diameter which is ~maller than the diamater of the vortex chamber 4.
A gas discharge outlet 10, which is concentric with the horizontal axis of the vortex chamber 4, i8 arranged in that end wall 9 of the vortex chamber which i6 opposite to the end at which the vortex chamber 4 communicates with the flue duct 2. The discharge outlet 10 is connectsd through a pipe 11 to a convection part 1~
of the reactor. There is no axial pa6sage in the end wall of the separator opposite to the end wall 9. The width b of the gas channel 2 is ~maller than the axial length B of the vortex chamber 4. The flue duct 2 is offset relative to the axial length of the vortex chamber 4.
The flue duct 2 guides the flue gases of the reactor ohliquely downwards to the tran~ition chamber 5 acting as a pre-separator, wherein the main portion of the flue gases i~ deflected upwards (counter-clock-wise in FIG. 1) to the vortex chamber 4, tang~ntially thereto. Due to the change of direction a major part of the flue gases, the solid material contained in the gases is separated and recirculated to the reactor. A part of the remaining 601ias is separated to the cylindric wall of the vortex chamber and is projected against the intermediate wall 7 between the L52~
vortex chamber 4 and the return duct 8 from which it ~alls down to the return duct 8. As ment.i.~ned above, the purified gases are discharged through the axial outlet 10 to the convection part 13.
In the embodiment illustrated in FIGURES 4 and 5, the reactor 21 communicates through a pair of flue ducts 22~, 22b, with coaxial separators 23a, 23b. The gases leaving the upper part of the reactor 21 are at first directed, by the flue ducts 23a, 23b, obliquely downwardly and away from the reactor 21. Each flue duct 22a, 22b is associated with one of the separators 23a, 23b. As in the first embodiment described, the main portion of the gases coming through each duct 22a, 22b changes its direction and flows obliquely upwards to an associated vortex chamber 24a, 24b of the respective separator 23a, 23b. In the embodiment shown, the vortex chambers 24a, 24b are co-axial with each other. The upper part of a return duct 28 and a respective lower wall 26a 26b connecting the respective flue ducts 22a, 22b with the return duct 28, are arranged to be ~ubstantially parallel with the direction of flow in flue ducts ~2a, 22b. Thus, they guide the solid particles æeparated by the change of the direction of flow of the gases, directly to the return duct 28, much in thes fashion of the first embodiment described.
The wallæ 27a 21b (only 27b being visible in FIGURE 4) between the vortex chambers 24a, 24b and the return duct 2a form with the wall of the return duct 28 a slope terminatlng at a respective edge 31a. 31b. As in the first example of FIGURES 1 3, the sloping wall 27a, 27b of each vortex chamber guides the separated solid material slantin~ly downwards to the return duct 28 which is common to both vortex chambers 24a, 24b. ~he respective end walls ~ 2~b of the vortex chambers 24a, 24b are each provided with a gas outlet passage 30a. 30b. The gas outlet passages 30a, 30b are concentric with the vortex chambers 24a, 24b and with each other.
~hey connect their associated vortex chambers 24a, 24b with a discharge channel 25 common to both separators and leading to a common convection part ~3.
The separator illu~trated in Fig. 6 is imilar to the separators illustrated in Figs. 1, 2 and 3 except that in FIGURE 6 there are two adjacent return ducts 18 and 38 for the separated ~olids are connected to the associated vortex chamber 4. The diameter b of ' ':
~2~5Z4 ..he return duct 18 is equal to the width of the flue duct 2 of the reactor. The inlet of the seasnd return duct 38 i~ located at the same end of the vortex chamber 34 as the gas outlet 20.
The vortex chamber 34 i6 provided with a partition wall 36 S disposed between the port of the flue duct 2. The partition wall has an orifice, 80 as to form, in eff~ct, two adjacent vortex chamber sections 3S. 37.
The return duct 18 receives both the solids separated by the change of the directi~n of flow and the solids ~eparated on the walls of the vortex chamber 34. On the other hand, the return duct 38 receives only the solids separated on the wall of the vortex chamber section 37. Thus, the solid material returned by duct 38 is finer than the material returned by duct 18.
The separat~r i~lustrated by Figs. 7 and 8 is provided with two adjacent vortex chambers ~4 and ~4 having different diameters. The vortex chamber 44, having a larger diameter, i8 ~imilar to that illustrated in Figs. 1, 2 and 3 e~cept that the outlet 40 in its end i~ connected to the concentric vortex chamber 54 having a smaller diameter. The gas outlet ~0 in the end wall ~1 of the smaller vortex cham~er 54 i6 connected through a pipe 52 to a convection part 53. The solid material return duct 48 connected to the larger vortex chamber section 44 is similar to the duct 8 in Figs. 1, 2 and 3. The solid material return duct 58 is connected tagentially t~ ~he smaller vortex chamber section 54.
The separatox is two-staged. In the first stage aoarse material is separated at 810w peripheral speeds and in the second stage finer particles at hiyh peripheral speeds.
As to its flow technology, the sy6tem of the present invention differs from the conventional system, in that the solid material is recirculated to the reactor carried by the gas flow (1 - 10 %
of the gases). As the flue duct 2, 22 i8 directed towards the inlet of the solid matsrial return duct, the dynamic pressure of the gas and the solid material facilitates circulation of the solid material whereby the separation rate is incrsased.
Furthermore, the apparatus according to the invention provides the following advantages compared to a conventional cyclone separator:
- as the flue duct is directed obliquely downwards, no solid material is accumulated at its bottom; in conventional
APPARATUS FOR SEPARATING SOLID MATERIAL
IN A CIRCULATING Fl.UIDIZED BED REACTOR
The present invention relates to an apparatus for separating solid particles from the flue gases of a reactor and for recycling the separated solids to the reactor.
Circulating fluidized bea technique has long been used in various reactors such as calcinators and recently to a larger extent in combustion furnaces and gasifiers. In the known applications, the separation of solid6 is carried out in a conventional cyclone separator having a vertical axis and a hopper-shaped bottom. The cylindrical vortex chamher of the cyclone is provided with a gas discharge pipe which guides the gases upwards and the solids are recycled to the reactor through a stand pipe via a gas trap. The gas trap is employed to prevent reactor gase6 from flowing into the cyclone through the stand pipe. A mechanical trap is most commonly used as a gas trap. In more advanced applications a fluidized bed of sand in a U-pipe is known to have been applied for the purpose. The solids recycling system becomes complex and expensive especially in high temperature reactors. Part of the air required for fluidizing the gas trap flows upwards in the stand pipe which has a detrimental effect on the separation of solids, in particular on the 6eparation of light and fine particles.
Furthermore, the rising gas flow decreases the transport capacity of the stand pipe.
As is known, a substantial vacuum and a high axial flow velocity are created in the centre of a conventional cyclone due to which the cyclone tends to draw the particles from the stand pipe. The suction flow generated in this way has usually no tangential velocity. Thus, almost all the solid material the flow carries with it is transported out through the centre pipe of the cyclone.
A recycling system provided with a conventional cyclone is therefore very sensitive to the suction flow from the stand pipe and requires a reliable gas trap.
In steam boiler applications the use of a conventional cyclone results in disadvantageous constructions a~ a conventional cyclone divides the boiler into a separate combustion chamber and ~2~
~ convection part downstream of the cyclone between which the equipment for recycling the solids must be installed.
Mechanical gas traps are rapidly worn particularly in hot condition and breakdowns in their operation are frequent.
5 Also, applications having a conventional cyclone in~talled inside the reactor are known in which the whole solids recycling system is built inside the reactor. This application has, however, severe disadvantages such as cor~osion and erosion of the cyclone, as cooling of the supporting structure cannot be arranged in a simple way. Furthermore, as is the case in conventional cyclonss, the arrangment inside the reactor is subject to sensitivity to the suction flow from the stand pipe.
It is an object of the invention to provide an apparatus by whiQh solid particles can be efficiently separated from flue gases discharged from a circulating fluidized bed reactor, and recycled to a desired point in the reactor.
In general terms, the present invention provides apparatus for use with a circulating fluidized bed reactor, for separating solid particles from the flue gases of the reactor and for recycling the solid particles to the reactor, the apparatus comprising: a flue duct for guiding the flue gases of the reactor obliquely downwardly and away from the reactor; a vortex separator chamber having a generally horizontal axis; deflecting means for changiny the direction of the flow of a ma~or portion of the gases exiting from said flue duct to direct the ga~es into said vortex separator chamber; a return duat communicating with said flue duct and with one end of said vortex separator chamber; and a ga~ discharge concentric with ~aid generally horizontal axis and disposed in an end wall of the vortex separator chamber.
The invention will now be described by way of exemplary embodiments with reference to the accompanying diagrammatic, simplifi ed dra~i ~gs, wherein:
Fig. 1 illustrates an embodiment of the invention in a vertical sectional view taken along line A-A of Fig. 2;
Fig. 2 is a top view of the apparatus of Fig. l;
Fig. 3 is a view of a part of Fig. 1 in the direction of the arrow B;
Fig. 4 is another embodiment of the invention in a vertical ., . ~
~LZ6~L5;~D~
sec-tion taken along line C~C of Fig. 5;
Fig. 5 is a top view of the apparatu~ of ~ig. 4;
Fig. 6 is an alternative embodiment of the construction illustrated in Fig. 3;
Fig. 7 is yet another embodiment of the construction illustrated in Fig. 3; and Fig. 8 is a sectional view taken along line D-D of Fig. 2.
In Figs. 1, 2 and 3, reference numeral 1 refers to a vertical fluidized bed reactor from the upper part of which the flue gases flow obliquely downwardly and away from the reactor 1, through a flue duct 2. A separator 3 is disposed beside the reactor 1 such that the inlet section of its horizontal vortex chamber 4 and the discharge end of the flue duct 2 are di posed in a downwardly tapering transition chamber 5 which is formed between a lower wall 6 of the flue duct 2 and an intarmediata wall 7 connected tangentially to the cylindrical jacket of ~he vortex chamber 4.
The transition chamber 5 constitutes the inlet of a return duct for solid material. The return duct 8 has a diameter which is ~maller than the diamater of the vortex chamber 4.
A gas discharge outlet 10, which is concentric with the horizontal axis of the vortex chamber 4, i8 arranged in that end wall 9 of the vortex chamber which i6 opposite to the end at which the vortex chamber 4 communicates with the flue duct 2. The discharge outlet 10 is connectsd through a pipe 11 to a convection part 1~
of the reactor. There is no axial pa6sage in the end wall of the separator opposite to the end wall 9. The width b of the gas channel 2 is ~maller than the axial length B of the vortex chamber 4. The flue duct 2 is offset relative to the axial length of the vortex chamber 4.
The flue duct 2 guides the flue gases of the reactor ohliquely downwards to the tran~ition chamber 5 acting as a pre-separator, wherein the main portion of the flue gases i~ deflected upwards (counter-clock-wise in FIG. 1) to the vortex chamber 4, tang~ntially thereto. Due to the change of direction a major part of the flue gases, the solid material contained in the gases is separated and recirculated to the reactor. A part of the remaining 601ias is separated to the cylindric wall of the vortex chamber and is projected against the intermediate wall 7 between the L52~
vortex chamber 4 and the return duct 8 from which it ~alls down to the return duct 8. As ment.i.~ned above, the purified gases are discharged through the axial outlet 10 to the convection part 13.
In the embodiment illustrated in FIGURES 4 and 5, the reactor 21 communicates through a pair of flue ducts 22~, 22b, with coaxial separators 23a, 23b. The gases leaving the upper part of the reactor 21 are at first directed, by the flue ducts 23a, 23b, obliquely downwardly and away from the reactor 21. Each flue duct 22a, 22b is associated with one of the separators 23a, 23b. As in the first embodiment described, the main portion of the gases coming through each duct 22a, 22b changes its direction and flows obliquely upwards to an associated vortex chamber 24a, 24b of the respective separator 23a, 23b. In the embodiment shown, the vortex chambers 24a, 24b are co-axial with each other. The upper part of a return duct 28 and a respective lower wall 26a 26b connecting the respective flue ducts 22a, 22b with the return duct 28, are arranged to be ~ubstantially parallel with the direction of flow in flue ducts ~2a, 22b. Thus, they guide the solid particles æeparated by the change of the direction of flow of the gases, directly to the return duct 28, much in thes fashion of the first embodiment described.
The wallæ 27a 21b (only 27b being visible in FIGURE 4) between the vortex chambers 24a, 24b and the return duct 2a form with the wall of the return duct 28 a slope terminatlng at a respective edge 31a. 31b. As in the first example of FIGURES 1 3, the sloping wall 27a, 27b of each vortex chamber guides the separated solid material slantin~ly downwards to the return duct 28 which is common to both vortex chambers 24a, 24b. ~he respective end walls ~ 2~b of the vortex chambers 24a, 24b are each provided with a gas outlet passage 30a. 30b. The gas outlet passages 30a, 30b are concentric with the vortex chambers 24a, 24b and with each other.
~hey connect their associated vortex chambers 24a, 24b with a discharge channel 25 common to both separators and leading to a common convection part ~3.
The separator illu~trated in Fig. 6 is imilar to the separators illustrated in Figs. 1, 2 and 3 except that in FIGURE 6 there are two adjacent return ducts 18 and 38 for the separated ~olids are connected to the associated vortex chamber 4. The diameter b of ' ':
~2~5Z4 ..he return duct 18 is equal to the width of the flue duct 2 of the reactor. The inlet of the seasnd return duct 38 i~ located at the same end of the vortex chamber 34 as the gas outlet 20.
The vortex chamber 34 i6 provided with a partition wall 36 S disposed between the port of the flue duct 2. The partition wall has an orifice, 80 as to form, in eff~ct, two adjacent vortex chamber sections 3S. 37.
The return duct 18 receives both the solids separated by the change of the directi~n of flow and the solids ~eparated on the walls of the vortex chamber 34. On the other hand, the return duct 38 receives only the solids separated on the wall of the vortex chamber section 37. Thus, the solid material returned by duct 38 is finer than the material returned by duct 18.
The separat~r i~lustrated by Figs. 7 and 8 is provided with two adjacent vortex chambers ~4 and ~4 having different diameters. The vortex chamber 44, having a larger diameter, i8 ~imilar to that illustrated in Figs. 1, 2 and 3 e~cept that the outlet 40 in its end i~ connected to the concentric vortex chamber 54 having a smaller diameter. The gas outlet ~0 in the end wall ~1 of the smaller vortex cham~er 54 i6 connected through a pipe 52 to a convection part 53. The solid material return duct 48 connected to the larger vortex chamber section 44 is similar to the duct 8 in Figs. 1, 2 and 3. The solid material return duct 58 is connected tagentially t~ ~he smaller vortex chamber section 54.
The separatox is two-staged. In the first stage aoarse material is separated at 810w peripheral speeds and in the second stage finer particles at hiyh peripheral speeds.
As to its flow technology, the sy6tem of the present invention differs from the conventional system, in that the solid material is recirculated to the reactor carried by the gas flow (1 - 10 %
of the gases). As the flue duct 2, 22 i8 directed towards the inlet of the solid matsrial return duct, the dynamic pressure of the gas and the solid material facilitates circulation of the solid material whereby the separation rate is incrsased.
Furthermore, the apparatus according to the invention provides the following advantages compared to a conventional cyclone separator:
- as the flue duct is directed obliquely downwards, no solid material is accumulated at its bottom; in conventional
2~
separators the accumulationa reduca markedly the separation capacity;
- since a major portion of the dust flowing in is separated in the transition chambsr 5, tha dust does not overload the vortex chamber 4;
- as a major portion of the dust i6 removed before the flue enters the vortex chamber, the separator can be dimensioned for separation of greater amount of dust;
- for the same reason, a vortex chamber can be run at higher speeds as the erosion ~& not as severe as in chambers operating with more heavlly particle laden flues;
- a vortex motion occurs only in the vortex chamber, not in the solid material discharge channel.
Also, structural advantages are achieved with the system of the present invention, in particular:
- compact construction;
- e~pansion joints can be avoidedi - the connection to the convection part and the reactor is simple;
- connection of the gas discharge is simple, it can be arranged at either or both ends of the vortex chamber.
The invention is not limited to the embodtments presented herein as examples only. It can be modified to a greater or lesser degree wihtout departing from the scope of the present invention.
~5 Accordingly, we wish to protect by Letters Patent which may is~ua on this application all such embodiments as properly ~all within the scope o~ our contr~bution to the art.
separators the accumulationa reduca markedly the separation capacity;
- since a major portion of the dust flowing in is separated in the transition chambsr 5, tha dust does not overload the vortex chamber 4;
- as a major portion of the dust i6 removed before the flue enters the vortex chamber, the separator can be dimensioned for separation of greater amount of dust;
- for the same reason, a vortex chamber can be run at higher speeds as the erosion ~& not as severe as in chambers operating with more heavlly particle laden flues;
- a vortex motion occurs only in the vortex chamber, not in the solid material discharge channel.
Also, structural advantages are achieved with the system of the present invention, in particular:
- compact construction;
- e~pansion joints can be avoidedi - the connection to the convection part and the reactor is simple;
- connection of the gas discharge is simple, it can be arranged at either or both ends of the vortex chamber.
The invention is not limited to the embodtments presented herein as examples only. It can be modified to a greater or lesser degree wihtout departing from the scope of the present invention.
~5 Accordingly, we wish to protect by Letters Patent which may is~ua on this application all such embodiments as properly ~all within the scope o~ our contr~bution to the art.
Claims (8)
1. Apparatus for use in a circulating fluidized bed reactor, for separating solid particles from the flue gases of the reactor and for recycling the solid particles to the reactor, the apparatus comprising:
- a flue duct for guiding the flue gases of the reactor obliquely downwardly and away from the reactor;
a vortex separator chamber having a generally horizontal axis;
- deflecting means for changing the direction of the flow of a major portion of the gases exiting from said flue duct to direct the gases into said vortex separator chamber;
- a return duct communicating with said flue duct and with one end of said vortex separator chamber; and - a gas discharge concentric with said generally horizontal axis and disposed in an end wall of the vortex separator chamber.
- a flue duct for guiding the flue gases of the reactor obliquely downwardly and away from the reactor;
a vortex separator chamber having a generally horizontal axis;
- deflecting means for changing the direction of the flow of a major portion of the gases exiting from said flue duct to direct the gases into said vortex separator chamber;
- a return duct communicating with said flue duct and with one end of said vortex separator chamber; and - a gas discharge concentric with said generally horizontal axis and disposed in an end wall of the vortex separator chamber.
2. Apparatus as recited in claim 1 wherein said return duct extends along said reactor and has an upper part communicating and generally parallel with said flue duct, and a lower part communicating with the reactor at a lower portion thereof.
3. Apparatus as recited in claim 1 wherein the upper part of the return duct is disposed at an obtuse angle with the flue duct.
4. Apparatus as recited in claim 1, 2 or 3 wherein the vortex separator chamber communicates with the flue duct at a separator inlet which includes a wall inclined obliquely downwardly from the separator chamber to the return duct directing solid particles, which have been separated from the flue in the separator chamber, to the return duct.
5. Apparatus as recited in claim 1, 2, or 3, wherein the deflector means is a downwardly inclined wall extending obliquely downwardly from the interior of the vortex separator chamber to the return duct.
6. Apparatus as recited in one of claims 1, 2 or 3, wherein the cross-sectional area of the return duct is smaller than the diameter of the vortex separator chamber.
7. Apparatus as recited in one or more of claims 1, 2 or 3, wherein there are provided two vortex separator chambers of which only one communicates with the return duct near said deflecting means.
8. Apparatus as recited in one or more of claims 1, 2 or 3, wherein there are provided two vortex separator chambers of which only one communicates with the return duct near said deflecting means, the diameter of one of the vortex separator chambers being smaller than the corresponding diameter of the other separator chamber.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| FI844281 | 1984-11-01 | ||
| FI844281A FI844281L (en) | 1984-11-01 | 1984-11-01 | ANCILLATION OF THE FAST MATERIAL I REACTOR WITH CIRCULAR BEDD. |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CA1264524C CA1264524C (en) | 1990-01-23 |
| CA1264524A true CA1264524A (en) | 1990-01-23 |
Family
ID=8519820
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000494411A Expired - Fee Related CA1264524A (en) | 1984-11-01 | 1985-11-01 | Apparatus for separating solid material in a circulating fluidized bed reactor |
Country Status (2)
| Country | Link |
|---|---|
| CA (1) | CA1264524A (en) |
| FI (1) | FI844281L (en) |
-
1984
- 1984-11-01 FI FI844281A patent/FI844281L/en not_active Application Discontinuation
-
1985
- 1985-11-01 CA CA000494411A patent/CA1264524A/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| FI844281A0 (en) | 1984-11-01 |
| CA1264524C (en) | 1990-01-23 |
| FI844281L (en) | 1986-05-02 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| MKLA | Lapsed |