CA1167086A - Process of and apparatus for the pneumatic transport of pulverized solids - Google Patents
Process of and apparatus for the pneumatic transport of pulverized solidsInfo
- Publication number
- CA1167086A CA1167086A CA000387185A CA387185A CA1167086A CA 1167086 A CA1167086 A CA 1167086A CA 000387185 A CA000387185 A CA 000387185A CA 387185 A CA387185 A CA 387185A CA 1167086 A CA1167086 A CA 1167086A
- Authority
- CA
- Canada
- Prior art keywords
- cells
- carrier gas
- feeder
- vessel
- mixing 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
Links
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B65—CONVEYING; PACKING; STORING; HANDLING THIN OR FILAMENTARY MATERIAL
- B65G—TRANSPORT OR STORAGE DEVICES, e.g. CONVEYORS FOR LOADING OR TIPPING, SHOP CONVEYOR SYSTEMS OR PNEUMATIC TUBE CONVEYORS
- B65G53/00—Conveying materials in bulk through troughs, pipes or tubes by floating the materials or by flow of gas, liquid or foam
- B65G53/34—Details
- B65G53/40—Feeding or discharging devices
- B65G53/46—Gates or sluices, e.g. rotary wheels
- B65G53/4608—Turnable elements, e.g. rotary wheels with pockets or passages for material
- B65G53/4625—Turnable elements, e.g. rotary wheels with pockets or passages for material with axis of turning perpendicular to flow
- B65G53/4633—Turnable elements, e.g. rotary wheels with pockets or passages for material with axis of turning perpendicular to flow the element having pockets, rotated from charging position to discharging position, i.e. discrete flow
Abstract
Process of and apparatus for the pneumatic transport of pulverized solids A B S T R A C T
A pulverulent material-carrier gas stream of sub-stantially constant solids-to-gas weight ratio is formed by establishing direct communication between cells of a rotary feeder and a mixing chamber. The emptying of the contents of the cells of the feeder into the mixing chamber is insured by directing the inflowing carrier gas stream into the cells while they are in communication with the mixing chamber.
A pulverulent material-carrier gas stream of sub-stantially constant solids-to-gas weight ratio is formed by establishing direct communication between cells of a rotary feeder and a mixing chamber. The emptying of the contents of the cells of the feeder into the mixing chamber is insured by directing the inflowing carrier gas stream into the cells while they are in communication with the mixing chamber.
Description
1 ~ 670~6 Process of and apparatus for the pneumatic transport of pulverized solids The present invention relates to a process of and apparatus for causing the entrainment of a pulverized solid material in a carrier gas and especially to apparatus wherein the pulverized material is periodically supplied and the resulting pulverized material/carrier gas stream has a substant-ially constant solid to gas ratio. More specifically, this in-vention is directed to the pneumatic transport of pulverulentmaterials and particularly to the establishment of a fuel stream of substantially constant density and comprising a pulverized combustible material entrained in an appropriate carrier gas.
While not limited thereto in its utility, the present invention is particularly well suited for use in the establishment of a fuel stream for injection into a pressurlæed furnace such as, for example, a blast furnace.
Apparatus and techniques for the establishment of a fuel stream comprising a pulverized solid fuel and a carrier gas are known in the art. An example of such apparatus may be found in our Canadian patent application No: 354,110.
As discussed in said application, a blast furnace may be provided with injection nozzles to which are delivered coal dust or powdered lignite from a reservoir. The move-ment of the pulverized fuel from the reservolr to the furnace is effected pneumatically with the aid of devices known in the art as rotary air-lock feeders. Such feeders comprise a honeycombed or compartmented rotor which will be of cylin-drical shape and will have a plurality of blades or vaneswhich define a series of cells which communicate with the periphery of the rotor. The rotor blades establish a sub-stantially air-tight seal with the wall of the chamber in which the rotor turns and pulverized material delivered to the indlvidual cells by gravity from a reservoir at the top of the rotor will be released into the carrier gas stream at a spacially separated location, typically the bottom of the chamber. The carrier gas is directed through the chamber in a direction parallel to the rotation axis of the 1 ~ ~70~
~ 2 feeder. The pulverized material will thus be entrained in the carrier gas and conveyed into a conduit which communi-cates with the furnace injector nozzles.
Th~ technique and apparatus briefly described above suffers from the disadvantage that the pulverulent material is delivered to the carrier gas stream in separate "lots", each corresponding to the capacity of one cell of the rotary feeder, and the resulting pulverized matexial/
carrier gas stream is thus characterized by "pulsations", i.e., by variations in the solid material to carrier gas ratio. This problem is discussed in detail in our Canadian patent application number 381,120.
To prevent the above-discussed "pulsations" from occurring in the pneumatic transport conduits, the said European application proposes to separate the step of deli-very of the pulverized material from the reservoir via rotary air-lock feeders from the step of production of the actual pneumatic current, i.e., the pulverized material/carrier gas stream, which is delivered to the furnace or other down-stream apparatus. This may, for example, be accomplished bycausing the pulverized material which exlts the rotary feeder to flow into an enclosure into which the carrier gas is introduced. By promoting turbulence of the carrier gas inside this enclosure, a mixture of solid material and gas ls formed and this pressurized mixture may then be extracted from the enclosure as a stream having a substantially constant density.
The technique described immediately above, wherein the solid material is delivered to an enclosure where it is mixed with a turbulent carrier gas, presents a problem which ls not encountered in apparatus such as that discussed in our Canadian application No: 354,110. This new problem is associated with the operation of the rotary feeder and par-tlcularly wlth the emptylng of the cells of the rotor. The materlal ln the cells of the rotor will undergo a slight compression during the course of rotation and the degree of compression may increase with an increase in the humidlty of the operatlng environment. This compression, although slight, may result in the pulverulent material failing to - I 1 67~86 drop out of the cells. If a rotor cell retains all or part of its contents, which continue to move with the cell back to the point of communication with the reservoir, the solid material in the cell will undergo further compression and the point will be reached where the pulverized material will not be removed from the cells simply through the force of gravity.
Accordingly, a number of cells may "fail" resulting in the breakdown of the entlre system. Such a breakdown can be remedied only by shutting down the system and dismantling the rotary air-lock feeder to manually free the compressed pul-verized material from the cells.
The purpose of the present invention is to over-come the above-brlefly discussed and other deficiencies and dlsadvantages of the prior art by providing novel and improved apparatus for the establlshment of a pulverized material-carrier gas stream which is characterized by a substantially constant solids to gas welght ratio. The present invention also encompasses a novel method for the creation of a uniform pneumatic current and especially a fuel-air stream.
In accordance with the present invention, there is provided apparatus or forming a substantially constant density stream comprlslng a pulverulent material entrained in a carrler gas comprlslng rotary feeder means for serially transportlng measured quantities of the pulverulent material from a source of such materlal along an accuate path, said rotary feeder means lncluding a plurallty of spacially dls-placed materlal receiving cells, mixing vessel means, said vessel means deflning a mlxlng chamber, said vessel means belng coupled to said feeder means and belng located with respect thereto such that durlng rotatlon at least part of a plurallty of adjacent of sald feeder cells extend into said mixing chamber, the location of sald feeder means with res-pect to sald vessel means being such that pulverized material will tend to fall from cells which are in co~munication with mlxing chamber under the lnfluence of gravity, and means or ".~
~s f r, .
1 3 B70~6 - 3a del~vering a pressurized carrier gas to the interior of said vessel means, said carrier gas delivering means beinq positi~ned to direct the carrier gas onto at least that portion of the feeder means cells which extend int~ the mixlng chamber.
Also in accordance with the invention there is provided a process for the pneumatic transport of pulverized solid material, the pulverized material being deli-vered from a source via a rotary feeder having a plurallty of adjacent material conveying cells, the improvement c~mprislngestablishing direct communlcation between a plurality of adja-cent cells of the rotary feeder and the interior of a mixing vessel during rotation of the cells whereby pulverized material ln the feeder cells may fall into the vessel under the influ ence of gravity, lntroduclng a pressurized carriex gas into the mlxing ~essel, and directing the thus lntroduced carrier ga~ as a stream into the cells of the rotary feeder.
The method and apparatus of the present invention enables "pulsations" in the stream being produced to be avoided since, as discussed in oUr aforementioned Canadian ~patent application 3~1,120, the mixing of the carrier gas and the pulverlzed materlal is uniformly eff~cted in the mixing ~hamber.
The present lnventlon also prevents the obstructlon of the cells of the rotary feeder through the dlrection of the jet of carrier gas into the cells during a polnt in time ~ 1 670~6 !
when the cells are in communication with the mixing chamber.
Accordlngly, should a cell fail to discharge its contents under the influence of gravity, the jet of pressurized carrier gas will dislodge the pulverized material and cause it to be ejected from the cell.
An added advantage incident to the present inven-tion resides in the fact that a denser stream, i.e., a higher solid material to carrier gas ratio, can be obtained than, for example, in apparatus such as that generally disclosed in our aforementioned Canadian application ~o: 354,110. Thus, in that application the pulverized material is extracted horizontally from the rotary feeder and thus must be accele-rated from zero horizontal velocity up to the pneumatic transport speed. This acceleration requires an additional quantity of carrier gas and thus places an upper limit on the solids/gas ratio. In accordance with the present inven-tion, the initial vertical motion of the pulverized material is in the direction of flow of the stream to be formed, i.e., toward the exlst port of the mixlng chamber, and thus the quantity of the carrier gas required to move a given quantity of pulverulent material may be reduced.
Apparatus in accordance with the present invention may have the rotary feeder mounted above the mixing chamber so that, at the moment when the pulverized material is released 25 into the chamber under the influence of gravity during rotation, the rotor cells will be in communication with the interior of the mixing chamber. Additionally, as noted above, the carrier gas supply conduit is located such that the carrier gas will be directed into rotor cells which are in communication with the 30 mixing vessel.
It is also possible with the present invention to achieve an eddying effect in the mixing chamber by positioning the vertical axis of the rotary feeder a slight distance from that of the mixing chamber so that the jet of carrier gas, 35 although conveyed through the cells of rotary feeder in a direction parallel to the axis of rotation thereof will not be perpendicular to a wall of the mixing chamber. Under these circumstances, the carrier yas jet will prefer-!:
i 1 67086 -- 5ably have an axis which approaches being tangential to the wall of the mixing chamber and the mixing vessel will be of cyllndrlcal shape and have a portion which converges in the direction of the discharge port.
It is also possible to configure the rotor of the feeder so that the blades which define the cells are angularly displaced from their normal position, wherein they define planes which extend radially with respect to the axis of rota~ion, to thus establish a generally helicoidal configuration which extends around the rotor. This arrangement automatically imparts a gyratory motion to the jet of carrier gas which sweeps the cells and thus aids in the creation of turbulence and mixing within the mixing chamber.
The present invention may be better understood and its numerous objects and advantages will become apparent to those skilled in the art by reference to the accompanying drawlng wherein like reference numerals refer to like elements in the two figures and in which :
Figure 1 is a schematic side elevation view, partly in section, of apparatus in accordance with a preferred embodiment of the lnvention, and Figure 2 is a view, partly in section, of the apparatus of E'lgure 1 seen from a direction perpendicular to the view of Figure 1.
Referring now to the drawing, a feeder of the rotary air-lock type is indicated generally at 2. The feeder
While not limited thereto in its utility, the present invention is particularly well suited for use in the establishment of a fuel stream for injection into a pressurlæed furnace such as, for example, a blast furnace.
Apparatus and techniques for the establishment of a fuel stream comprising a pulverized solid fuel and a carrier gas are known in the art. An example of such apparatus may be found in our Canadian patent application No: 354,110.
As discussed in said application, a blast furnace may be provided with injection nozzles to which are delivered coal dust or powdered lignite from a reservoir. The move-ment of the pulverized fuel from the reservolr to the furnace is effected pneumatically with the aid of devices known in the art as rotary air-lock feeders. Such feeders comprise a honeycombed or compartmented rotor which will be of cylin-drical shape and will have a plurality of blades or vaneswhich define a series of cells which communicate with the periphery of the rotor. The rotor blades establish a sub-stantially air-tight seal with the wall of the chamber in which the rotor turns and pulverized material delivered to the indlvidual cells by gravity from a reservoir at the top of the rotor will be released into the carrier gas stream at a spacially separated location, typically the bottom of the chamber. The carrier gas is directed through the chamber in a direction parallel to the rotation axis of the 1 ~ ~70~
~ 2 feeder. The pulverized material will thus be entrained in the carrier gas and conveyed into a conduit which communi-cates with the furnace injector nozzles.
Th~ technique and apparatus briefly described above suffers from the disadvantage that the pulverulent material is delivered to the carrier gas stream in separate "lots", each corresponding to the capacity of one cell of the rotary feeder, and the resulting pulverized matexial/
carrier gas stream is thus characterized by "pulsations", i.e., by variations in the solid material to carrier gas ratio. This problem is discussed in detail in our Canadian patent application number 381,120.
To prevent the above-discussed "pulsations" from occurring in the pneumatic transport conduits, the said European application proposes to separate the step of deli-very of the pulverized material from the reservoir via rotary air-lock feeders from the step of production of the actual pneumatic current, i.e., the pulverized material/carrier gas stream, which is delivered to the furnace or other down-stream apparatus. This may, for example, be accomplished bycausing the pulverized material which exlts the rotary feeder to flow into an enclosure into which the carrier gas is introduced. By promoting turbulence of the carrier gas inside this enclosure, a mixture of solid material and gas ls formed and this pressurized mixture may then be extracted from the enclosure as a stream having a substantially constant density.
The technique described immediately above, wherein the solid material is delivered to an enclosure where it is mixed with a turbulent carrier gas, presents a problem which ls not encountered in apparatus such as that discussed in our Canadian application No: 354,110. This new problem is associated with the operation of the rotary feeder and par-tlcularly wlth the emptylng of the cells of the rotor. The materlal ln the cells of the rotor will undergo a slight compression during the course of rotation and the degree of compression may increase with an increase in the humidlty of the operatlng environment. This compression, although slight, may result in the pulverulent material failing to - I 1 67~86 drop out of the cells. If a rotor cell retains all or part of its contents, which continue to move with the cell back to the point of communication with the reservoir, the solid material in the cell will undergo further compression and the point will be reached where the pulverized material will not be removed from the cells simply through the force of gravity.
Accordingly, a number of cells may "fail" resulting in the breakdown of the entlre system. Such a breakdown can be remedied only by shutting down the system and dismantling the rotary air-lock feeder to manually free the compressed pul-verized material from the cells.
The purpose of the present invention is to over-come the above-brlefly discussed and other deficiencies and dlsadvantages of the prior art by providing novel and improved apparatus for the establlshment of a pulverized material-carrier gas stream which is characterized by a substantially constant solids to gas welght ratio. The present invention also encompasses a novel method for the creation of a uniform pneumatic current and especially a fuel-air stream.
In accordance with the present invention, there is provided apparatus or forming a substantially constant density stream comprlslng a pulverulent material entrained in a carrler gas comprlslng rotary feeder means for serially transportlng measured quantities of the pulverulent material from a source of such materlal along an accuate path, said rotary feeder means lncluding a plurallty of spacially dls-placed materlal receiving cells, mixing vessel means, said vessel means deflning a mlxlng chamber, said vessel means belng coupled to said feeder means and belng located with respect thereto such that durlng rotatlon at least part of a plurallty of adjacent of sald feeder cells extend into said mixing chamber, the location of sald feeder means with res-pect to sald vessel means being such that pulverized material will tend to fall from cells which are in co~munication with mlxing chamber under the lnfluence of gravity, and means or ".~
~s f r, .
1 3 B70~6 - 3a del~vering a pressurized carrier gas to the interior of said vessel means, said carrier gas delivering means beinq positi~ned to direct the carrier gas onto at least that portion of the feeder means cells which extend int~ the mixlng chamber.
Also in accordance with the invention there is provided a process for the pneumatic transport of pulverized solid material, the pulverized material being deli-vered from a source via a rotary feeder having a plurallty of adjacent material conveying cells, the improvement c~mprislngestablishing direct communlcation between a plurality of adja-cent cells of the rotary feeder and the interior of a mixing vessel during rotation of the cells whereby pulverized material ln the feeder cells may fall into the vessel under the influ ence of gravity, lntroduclng a pressurized carriex gas into the mlxing ~essel, and directing the thus lntroduced carrier ga~ as a stream into the cells of the rotary feeder.
The method and apparatus of the present invention enables "pulsations" in the stream being produced to be avoided since, as discussed in oUr aforementioned Canadian ~patent application 3~1,120, the mixing of the carrier gas and the pulverlzed materlal is uniformly eff~cted in the mixing ~hamber.
The present lnventlon also prevents the obstructlon of the cells of the rotary feeder through the dlrection of the jet of carrier gas into the cells during a polnt in time ~ 1 670~6 !
when the cells are in communication with the mixing chamber.
Accordlngly, should a cell fail to discharge its contents under the influence of gravity, the jet of pressurized carrier gas will dislodge the pulverized material and cause it to be ejected from the cell.
An added advantage incident to the present inven-tion resides in the fact that a denser stream, i.e., a higher solid material to carrier gas ratio, can be obtained than, for example, in apparatus such as that generally disclosed in our aforementioned Canadian application ~o: 354,110. Thus, in that application the pulverized material is extracted horizontally from the rotary feeder and thus must be accele-rated from zero horizontal velocity up to the pneumatic transport speed. This acceleration requires an additional quantity of carrier gas and thus places an upper limit on the solids/gas ratio. In accordance with the present inven-tion, the initial vertical motion of the pulverized material is in the direction of flow of the stream to be formed, i.e., toward the exlst port of the mixlng chamber, and thus the quantity of the carrier gas required to move a given quantity of pulverulent material may be reduced.
Apparatus in accordance with the present invention may have the rotary feeder mounted above the mixing chamber so that, at the moment when the pulverized material is released 25 into the chamber under the influence of gravity during rotation, the rotor cells will be in communication with the interior of the mixing chamber. Additionally, as noted above, the carrier gas supply conduit is located such that the carrier gas will be directed into rotor cells which are in communication with the 30 mixing vessel.
It is also possible with the present invention to achieve an eddying effect in the mixing chamber by positioning the vertical axis of the rotary feeder a slight distance from that of the mixing chamber so that the jet of carrier gas, 35 although conveyed through the cells of rotary feeder in a direction parallel to the axis of rotation thereof will not be perpendicular to a wall of the mixing chamber. Under these circumstances, the carrier yas jet will prefer-!:
i 1 67086 -- 5ably have an axis which approaches being tangential to the wall of the mixing chamber and the mixing vessel will be of cyllndrlcal shape and have a portion which converges in the direction of the discharge port.
It is also possible to configure the rotor of the feeder so that the blades which define the cells are angularly displaced from their normal position, wherein they define planes which extend radially with respect to the axis of rota~ion, to thus establish a generally helicoidal configuration which extends around the rotor. This arrangement automatically imparts a gyratory motion to the jet of carrier gas which sweeps the cells and thus aids in the creation of turbulence and mixing within the mixing chamber.
The present invention may be better understood and its numerous objects and advantages will become apparent to those skilled in the art by reference to the accompanying drawlng wherein like reference numerals refer to like elements in the two figures and in which :
Figure 1 is a schematic side elevation view, partly in section, of apparatus in accordance with a preferred embodiment of the lnvention, and Figure 2 is a view, partly in section, of the apparatus of E'lgure 1 seen from a direction perpendicular to the view of Figure 1.
Referring now to the drawing, a feeder of the rotary air-lock type is indicated generally at 2. The feeder
2 lncludes a cylindrical housing which cooperates with a plurality of blades which extend from a rotary hub to define a series of cells 4. The roto~ of feeder 2 rotates about the axis O of the hub whereby the cells 4 move between a loading position, where they are in communication with a reservoir of pulverized solid material, not shown, and the posltion where the pulverized material will fall from the cells under the influence of gravity.
In accordance with the inventlon, the feeder 2 is mounted immed1ately above a mixing vessel, indicated generally at 6, such that portions of a plurality of the cells 4 ac-tually extend into the mixing chamber defined by vessel 6 ,~
1 1 ~70~6 during the unloading portion of each circular cycle of the cells. The pulverized material which falls from the feeder cells which are in communication with the mixing chamber is mixed with a carrier gas delivered to the interior of the mixing chamber via conduit 12 which penetrates the wall 8 of vessel 6. The pulverulent material-carrier gas mixture formed within the vessel 6 is discharged therefrom via a conduit 14 and transmitted via this conduit to a furnace or o~her con-suming load.
Also in accordance with the present invention the carrier gas, which will typically be air, is injected into the mixing chamber as a jet of pressurized fluid which passes through rotating cells of the rotary feeder 2. Referring to Figure 1, wherein the arrow A indicates clockwise rotation of the rotor of feeder 2, the carrier gas jet is preferably directed into the cells 4 when they are in the sector ~ .
Thus, the carrier gas jet preferably sweeps the cells ~ust prior to their exit from the mixing vessel 6, i.e., prior to reentry of the cell defining rotor blades into a sealing relationship with the inner wall of the housing which in part defines the feeder 2. If a cell 4 has not been comple-tely evacuated as a result of gravity forces acting on the pulverlzed materlal when the cell enters into communication with the interior of mixing vessel 6, the pulverized materlal will ~e ejected from this cell under the effect of the gas jet ln the ~ector ~ immediately prior to the disruptlon of communlcatlon between the cell and the mixing chamber.
It 1~ to be noted that the vertical axls of the rotary feeder 2 can be offset, either to the left or to the rlght as the apparatus ls deplcted, any deslred amount from the vertical axls of mlxlng vessel 6 in the lnterest of pro-duclng a preselected eddylng action ln the mixing chamber as a result of the deflection of the carrier gas stream by the inner wall of ve~sel 6.
It is also possible, in accordance wlth the present invention, to impart a desired orientation and/or conflgura-tion to the cells 4 of the rotary feeder 2 bearing ir. mlnd that the cize and shape of the cells must be selected in accordance wlth the other pneumatic characteristlcs of the I J 670~6 system. In particular, the blades which define therebetween the cells 4 may be angularly offset from the radial plane defining orientation shown in Figure 2 in order to present a hellcoidal configuration around the rotor to thereby assist the complete discharge of the cells both under the effect of gravity and by a blowing action. It is also to be noted that, when the rotor feeder fulfills the dual functions of proportloning the pulverized material and causing it to be entrained in the carrier gas as in the prior art, design flexibility with respect to the size and shape of the indivi-dual cells is llmited. However, in the apparatus described above, greater flexibility in design is possible. Thus the number of cells can be increased, with the volumne of each lndividual cell thus being decreased, and the most efficient cell shape to achieve optimum operating conditions may be selected. Accordingly, as previously discussed, the cells of the rotary air-lock feeder need not be formed by blades which deflne pla~es extending radially from the axls of rotation O of the rotor of the feeder.
In accordance with the inventlon, the feeder 2 is mounted immed1ately above a mixing vessel, indicated generally at 6, such that portions of a plurality of the cells 4 ac-tually extend into the mixing chamber defined by vessel 6 ,~
1 1 ~70~6 during the unloading portion of each circular cycle of the cells. The pulverized material which falls from the feeder cells which are in communication with the mixing chamber is mixed with a carrier gas delivered to the interior of the mixing chamber via conduit 12 which penetrates the wall 8 of vessel 6. The pulverulent material-carrier gas mixture formed within the vessel 6 is discharged therefrom via a conduit 14 and transmitted via this conduit to a furnace or o~her con-suming load.
Also in accordance with the present invention the carrier gas, which will typically be air, is injected into the mixing chamber as a jet of pressurized fluid which passes through rotating cells of the rotary feeder 2. Referring to Figure 1, wherein the arrow A indicates clockwise rotation of the rotor of feeder 2, the carrier gas jet is preferably directed into the cells 4 when they are in the sector ~ .
Thus, the carrier gas jet preferably sweeps the cells ~ust prior to their exit from the mixing vessel 6, i.e., prior to reentry of the cell defining rotor blades into a sealing relationship with the inner wall of the housing which in part defines the feeder 2. If a cell 4 has not been comple-tely evacuated as a result of gravity forces acting on the pulverlzed materlal when the cell enters into communication with the interior of mixing vessel 6, the pulverized materlal will ~e ejected from this cell under the effect of the gas jet ln the ~ector ~ immediately prior to the disruptlon of communlcatlon between the cell and the mixing chamber.
It 1~ to be noted that the vertical axls of the rotary feeder 2 can be offset, either to the left or to the rlght as the apparatus ls deplcted, any deslred amount from the vertical axls of mlxlng vessel 6 in the lnterest of pro-duclng a preselected eddylng action ln the mixing chamber as a result of the deflection of the carrier gas stream by the inner wall of ve~sel 6.
It is also possible, in accordance wlth the present invention, to impart a desired orientation and/or conflgura-tion to the cells 4 of the rotary feeder 2 bearing ir. mlnd that the cize and shape of the cells must be selected in accordance wlth the other pneumatic characteristlcs of the I J 670~6 system. In particular, the blades which define therebetween the cells 4 may be angularly offset from the radial plane defining orientation shown in Figure 2 in order to present a hellcoidal configuration around the rotor to thereby assist the complete discharge of the cells both under the effect of gravity and by a blowing action. It is also to be noted that, when the rotor feeder fulfills the dual functions of proportloning the pulverized material and causing it to be entrained in the carrier gas as in the prior art, design flexibility with respect to the size and shape of the indivi-dual cells is llmited. However, in the apparatus described above, greater flexibility in design is possible. Thus the number of cells can be increased, with the volumne of each lndividual cell thus being decreased, and the most efficient cell shape to achieve optimum operating conditions may be selected. Accordingly, as previously discussed, the cells of the rotary air-lock feeder need not be formed by blades which deflne pla~es extending radially from the axls of rotation O of the rotor of the feeder.
Claims (8)
1. - In a process for the pneumatic transport of pulverized solid material, the pulverized material being deli-vered from a source via a rotary feeder having a plurality of adjacent material conveying cells, the improvement comprising establishing direct communication between a plurality of adja-cent cells of the rotary feeder and the interior of a mixing vessel during rotation of the cells whereby pulverized material in the feeder cells may fall into the vessel under the influ-ence of gravity, introducing a pressurized carrier gas into the mixing vessel, and directing the thus introduced carrier gas as a stream into the cells of the rotary feeder.
2. - The method of claim 1 wherein the step of directing the carrier gas includes causing the gas to flow along the cells.
3. - The method of claims 1 or 2, wherein the carrier gas is directed into the rotary feeder cells imme-diately prior to the interruption of communication between the cells and the interior of the mixing vessel.
4. - Apparatus for forming a substantially constant density stream comprising a pulverulent material entrained in a carrier gas comprising rotary feeder means for serially transporting measured quantities of the pulverulent material from a source of such material along an accuate path, said rotary feeder means including a plurality of spacially dis-placed material receiving cells, mixing vessel means, said vessel means defining a mixing chamber, said vessel means being coupled to said feeder means and being located with respect thereto such that during rotation at least part of a plurality of adjacent of said feeder cells extend into said mixing chamber, the location of said feeder means with res-pect to said vessel means being such that pulverized material will tend to fall from cells which are in communication with mixing chamber under the influence of gravity, and means for delivering a pressurized carrier gas to the interior of said vessel means, said carrier gas delivering means being positioned to direct the carrier gas onto at least that portion of the feeder means cells which extend into the mixing chamber.
5. The apparatus of claim 4, wherein said mixing vessel means comprising a cylindrical upper portion, said feeder means being supported above one end of said cylindrical portion, and a frustoconical lower portion extending from the other end of said cylindrical portions said frustoconical lower portion defining a mixing chamber discharge port at its smaller diameter end.
6. The apparatus of claim 4 or 5, wherein said feeder means and said vessel means have vertical axes and wherein the vertical axis of said feeder means is offset with respect to the vertical axis of said vessel means.
7. The apparatus of claim 4 or 5, wherein said carrier gas delivery means is positioned to discharge a stream of carrier gas into the rotor cells in a region adjacent the point where communication between the rotating cells and mixing chamber is disrupted.
8. The apparatus of claim 4 or 5, wherein said feeder means and said vessel means have vertical axes and wherein the vertical axis of said feeder means is offset with respect to the vertical axis of said vessel means and wherein said carrier gas delivery means is positioned to discharge a stream of carrier gas into the rotor cells in a region adjacent the point where communication between the rotating cells and mixing chamber is disrupted.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| LU82837A LU82837A1 (en) | 1980-10-10 | 1980-10-10 | METHOD AND DEVICE FOR FORMING A UNIFORM AIR CURRENT OF POWDERY MATERIALS |
| LU82.837 | 1980-10-10 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1167086A true CA1167086A (en) | 1984-05-08 |
Family
ID=19729504
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000387185A Expired CA1167086A (en) | 1980-10-10 | 1981-10-02 | Process of and apparatus for the pneumatic transport of pulverized solids |
Country Status (10)
| Country | Link |
|---|---|
| EP (1) | EP0049912A3 (en) |
| JP (1) | JPS5790326A (en) |
| AR (1) | AR224473A1 (en) |
| AU (1) | AU7562481A (en) |
| BR (1) | BR8106506A (en) |
| CA (1) | CA1167086A (en) |
| ES (1) | ES8205175A1 (en) |
| LU (1) | LU82837A1 (en) |
| PL (1) | PL233350A1 (en) |
| ZA (1) | ZA816615B (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0811625B2 (en) * | 1988-06-17 | 1996-02-07 | フクビ化学工業株式会社 | Disentanglement and transport method for short fiber agglomerates |
| JP4716788B2 (en) * | 2005-06-01 | 2011-07-06 | 三菱電機株式会社 | Gas circuit breaker |
| CN105502006A (en) * | 2015-12-22 | 2016-04-20 | 马鞍山钢铁股份有限公司 | Sintering dry and fine powder distribution device capable of avoiding ash spray |
Family Cites Families (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE1049303B (en) * | 1959-01-22 | |||
| DE456237C (en) * | 1924-03-11 | 1928-02-22 | Int Comb Eng Corp | Process for producing a fuel dust air mixture by introducing the same into a fire chamber |
| US2477414A (en) * | 1944-07-15 | 1949-07-26 | Permanente Metals Corp | Pneumatic dust conveyer |
| CH339863A (en) * | 1956-04-12 | 1959-07-15 | Buehler Ag Geb | Infeed device for pneumatic pressure conveying of lubricating material, in particular cocoa |
| FR1164083A (en) * | 1957-01-07 | 1958-10-06 | Schenck Gmbh Carl | Method and device for distributing particulate materials |
| FR1399396A (en) * | 1964-06-24 | 1965-05-14 | Equipment for handling grain materials | |
| DE2363505A1 (en) * | 1973-12-20 | 1975-07-03 | Waeschle Maschf Gmbh | Feeder for pneumatic conveying plant - has portion of clean air diverted on discharge end of cell wheel |
-
1980
- 1980-10-10 LU LU82837A patent/LU82837A1/en unknown
-
1981
- 1981-06-12 EP EP81200657A patent/EP0049912A3/en not_active Withdrawn
- 1981-09-23 AR AR286854A patent/AR224473A1/en active
- 1981-09-23 ZA ZA816615A patent/ZA816615B/en unknown
- 1981-09-23 AU AU75624/81A patent/AU7562481A/en not_active Abandoned
- 1981-09-24 ES ES505745A patent/ES8205175A1/en not_active Expired
- 1981-10-02 CA CA000387185A patent/CA1167086A/en not_active Expired
- 1981-10-07 BR BR8106506A patent/BR8106506A/en unknown
- 1981-10-08 JP JP56161912A patent/JPS5790326A/en active Pending
- 1981-10-08 PL PL23335081A patent/PL233350A1/xx unknown
Also Published As
| Publication number | Publication date |
|---|---|
| PL233350A1 (en) | 1982-05-10 |
| LU82837A1 (en) | 1982-05-10 |
| AU7562481A (en) | 1982-04-22 |
| EP0049912A2 (en) | 1982-04-21 |
| AR224473A1 (en) | 1981-11-30 |
| ES505745A0 (en) | 1982-06-16 |
| ES8205175A1 (en) | 1982-06-16 |
| JPS5790326A (en) | 1982-06-05 |
| BR8106506A (en) | 1982-06-29 |
| ZA816615B (en) | 1982-09-29 |
| EP0049912A3 (en) | 1982-08-18 |
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