CA1189112A - Uniform pulverant flow after metering feeder - Google Patents
Uniform pulverant flow after metering feederInfo
- Publication number
- CA1189112A CA1189112A CA000381120A CA381120A CA1189112A CA 1189112 A CA1189112 A CA 1189112A CA 000381120 A CA000381120 A CA 000381120A CA 381120 A CA381120 A CA 381120A CA 1189112 A CA1189112 A CA 1189112A
- Authority
- CA
- Canada
- Prior art keywords
- carrier gas
- rotary valve
- conduit
- valve feeder
- fluidized bed
- 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
-
- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B5/00—Making pig-iron in the blast furnace
- C21B5/001—Injecting additional fuel or reducing agents
- C21B5/003—Injection of pulverulent coal
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Manufacturing & Machinery (AREA)
- Materials Engineering (AREA)
- Metallurgy (AREA)
- Mechanical Engineering (AREA)
- Filling Or Emptying Of Bunkers, Hoppers, And Tanks (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Paper (AREA)
- Air Transport Of Granular Materials (AREA)
- Crucibles And Fluidized-Bed Furnaces (AREA)
- Furnace Charging Or Discharging (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
A B S T R A C T
In a pneumatic system for the transport of pulverulent material which is introduced into a carrier gas by means of rotary valve there is provided a "buffer" enclosure in which is formed a fluidized bed of pulverulent material.
In a pneumatic system for the transport of pulverulent material which is introduced into a carrier gas by means of rotary valve there is provided a "buffer" enclosure in which is formed a fluidized bed of pulverulent material.
Description
[~NIFO~I puLvE~Nrr IL~ AFTER METERIN(~ FEEDFJR
The present invention relates to a process for the pneumatic transport at a uniform rate, of pulverulent mate-riaLs which are introduced into a carrier gas by means oE
rotary valve and wherein said carrier gas is guided through the rotary valve in a direction parallel to the rota~ion a~ls of the latter. The invention likewise relates ~o an install-ation for the performance of this process and also, as anexample of its application, to a process and an installation for the injec-tion of solid fuels in a shaft furnace.
Canadian Paten~ application ~i~,llO ~escri~es a process and an installation for the dosing and transport, by pneumatic means, of solid materials to an enclosure under pressure, particularly for the injection c,f solid Euels into a blast furnace. According -to the said patent applicatjon each nozzle or pair of no7zles is fed separately from a reservoir supplied with the necessary quantities of coal dust or powdered lignite. The transport of this powder between the said reservoir and the blast furnace is effected pneumatically/ and it has been found that the safest and most reliable means of taking selected quantities of materials from the reservoir is a rotary valve, already well known se. A valve of this kind consists essentially of a cylin-drical rotor provided on its periphery with a certain number of blades defining ~ corresponding n~mber of cells. This rotor rotates in a tight manner inside a case, and the mate-rial fed in from the top is conveyed downwards by the cells into a currerlt of air under pressure, which serves as a ,....
,;L~ J~
carrier gas. This carrier gas take~ up and c~rries along with it each quantity of mater:Lal as the latter is fed from a cell of the rotor.
In the aforementioned applicationl however, it has been found that the cells are ins~antaneousl~ emptied as soon as they en-ter the current of air in the pneumatic E~ipe. In other words, as soon as a cell gives up its con-tents there is a certain "deadl'' period during which the pul-verulent material is not taken into the pneumatic pipe, this inoperative period lasting until the mornent when the sub-sequent cell moves into position. The pulverulent fuel is thus injected into the blast furnace in small intermittent "lots" of which the periodici.ty depends on the speed of the rotor. In the application in question this speed is such that the cells cut across the pneumatic conduit at the rate of one cell per second, thus feeding the l'lots" of fuel to i.t at the same rate.
This phenomenon is due to the fact that a high speed and pressure have to be adopted in the pneumatic pipe~
The speed cannot be below 18 m/sec~ if deposits and back-firing from the blast furnace are to be avoided, while the pressure must be above the counter-pressure prevailing inside the furnace. In other applications than that envisaged in the present invention this phenomenon is of no consequence.
The fact is that it either does not occur, as a result of a low pressure and speed, or else can be eliminated, by re-ducing the pressure, for example, and where the only purpose in view is the transport of the pulverulent products it can even be allowed to continue, for in such cases it is immate-rial whether the subs~ance is propelled continuously or dlscontlrluously.
In the application ln questlon, ho~ever, i.e. inthe injection of coal dust or powdered 1.ignite into a blast furllace, it must be borrle in m.ind that thls powder has to be ~urnt in the furnace, for which purpose a certain q~antity of oxygen, servlng to rnaintain the combllstion process, is injected continuously through the tuyere stocks. l'hls quan-tity of oxygen or enriched air is needless to say calculated in accordance with the quan-tity of fuel, i.e. the quantity injected will be -that necessary and sufficient to burn the quantity of fuel to be injected into the furnace.
Now if the ligrlite or coal is injected in small separate quantities, the oxygen injected during the "dead"
periods elapsing between two successive "lots" of fuel will remain unused, entering -the rnass of material inside the furnace. Similarly, when a separate quantity of fuel is injected its mass is too great for the quantity of oxygen supplied, so that the fuel will not undergo complete com-bustion. To su~ up, it may be said that although ~he total quantity of fuel injected wil3 be that for which the quantity of oxygen has been calculated the intermittent injection of the former will lead to an alternating excess and shortage thereof accompanying a constant quantity of oxygen.
The purpose of the present invention is to provide a new process which avoids this "pulsation" in the transport of material in the pneumatic conduit, as well. as an install-ation for the performace of the process.
a, In accordance with the present: .invention there i.s provided a process for the pneumatic transport of pulverized material, the pulverized material being deliverecl into a pressurized carrier gas stream by a rotary valve feeder and tne velocity of the carrier gas being sufficiently great to entrain the material fro[n a first compa:rtment of the rotary valve feeder before a second filled compartment is exposecl to the gas whereby the ratio of the quantity of pulverized ~aterial to carrier gas varies periodically, the improvement comprising:
causing the carrier gas-pulverized material stream to expand and undergo a reduction in velocity while 10wi2lg vertically upward to thereby create a fluidized hed dowrlstream of the rotary valve feeder;
such velocity reduction being produced by causing the carrier gas-pulverized material mixture to flow through a divergent conduit section in the shape of a trunca-ted cone having an angle of conicity of at least ~0, and extracting a carrier gas~pulverized material stream having a substantially uniform solid material to carrier gas ratio fro~ the fluidized bedO
Preferably, the carrier gas pulverized m~terial stream forming the fluidized bed is subsequently caused to flow through a convergent conduit section in the shape of a truncated cone.
Also in accordarlce with the inven-tion there is provided an installation for the uniform pneumatic transport of pulverulent material, comprising a rotary valve feeder having a - 4a plurality o:E cel.ls for the distribu~ion of measured quantities of pulverulent material, a pneumatic transport conduit connecting the rotary valve feeder to a receiving station for the perverulent material, the pneumatic transport conduit delivering carrier gas to pass through the cells of the rotor of the rotary valve feeder4 in a di.rec-tivn parallel to the latter's rotation axis and servLng to take up the pulverulent material in the rotor cells as and when it is fed into position by the rotor cells and carry it along, a vertical elongated "buEfer"
enclosure connected into the pneumatic transport conduit downstream fr~m the rotary valve feede.r and of which the cross section is greater than that of the said transport conduit, the said "buffer" enclosure comprising a cylindrical body connected to the said transport conduit by divergent and convergent conduit sections of the shape of a trunca-ted cone, wherein the angle oE conicity oE the conical section on the side corresponding to the rotary valve feeder is at least 20, -the cross section of the enclosure being such that the speed oE the fluid will be suEficient to maintain a fluidi~ed bed.
Although the process and tile inst~llcltlor~ can be adop-ted wherever required for the purpose of elimlnatin~
a pneurnatic transport pipe the pvlsating effect described farther back, the invention offers paLticular clclval~tayex for the injection of soli,d fuels in a sl~aft furnaceO
Fur~her features and characteristics will emerge from the following detail,ed clescription of one advantageous en~odiment illustratiny the invention by reference to the single drawing provi,ding a schematic diagram, partly in section, of a chamber having a rotary valve and traversed by a pneumatic pipe provided with a "buffer" enclosure in accordance with the invention.
The rotary valve shown in this diagram is marked "2" as a whole. This char~ber consists essentially of a rotor 4 rotating about an axis perpendicular to the drawing and provided on its periphery with a set o blades 6 forming the boundari,es of a corresponding number of cells 8~ Pulve rulent material such as powdered lignite or coal dust acc~nulates by gravity ln an upper hopper 10 and fills each of the cells 8 as and when the rotor 4 rotatesO This rota-tion, in the case of the example shown, takes place in a clockwise direction. A pneumatic pipe 12 traverses the lower part of thle rotary valve 2, in a direction parallel to the rotation axis of the ro-tor 4, and carries along the pulve-rulent rnaterial as and when the bl.ades 6 pass the pOsitlo in question. Now owing to the high speed and pressure of the carrier gas ci.rculating in tire pipe 12, the contents of the cells 4 are evacua-ted -therefrom as soon as the saicl cells enter the current in -the pipe :l2. In the diagram ~he blade marked 6a has just entered the pneumatic current and the cell pxeceding it is being emptied, while the ce].1 4a precedin~ the blade 6a has already been comple-tely emptied As soon as the cell situated behind this bl.ade 6a has been emptied a "dead" period will occur during wh:ich no pulve-rulen-t ma-terial is bei.ng caused -to enter the pne~a-tic current and which will con-tinue until the subseqwent cell enters the passage of -the said current.
In order to ensure that the pneumatic transport of the pulverulent ma-terial will take place at a uniform rate and the intermittent ac-tion will be eliminated, the pipe 12 contains a "buffer" enclosure 14 "downstream" from -the valve 2. This enclosure consists of a cylinder 16 connected into the pipe by means of two sections 18 and 70 o the shape of a truncated cone. The aperture angle ~ of -the lower frusto-conical section must be above a certain value in oxder to prevent the pneumatic current from passing direct through -the enclosure 14 without undergoing any modification~ This angle ~ rnust be above 20 and preferably equal to 45, in order to cause eddies -to form a-t the entry into the enclosure 14. The divergence and -the e~pansion taking place in the said encl.osure 14 re.sult in a reduction in spe~d. The section of this enclosure 14, however, mus-t not exceed a certaln limit, corresponding to the speed required for the purpose of maintaining a kind o-f fluidized sJ
bed lnside the sai.cl enclosure l~o From this fl.l:lidi.zed bed onwards -the pulverule~t material is carri.ed along at a uni.form ratè by the air under pressu.re :leaviny the enclosu-re 14 It should be noted that instead of causing it to pass through the enclosure from the bottom upwards it is equally possiblé to cause it to pass through lt in t}le V~
opposite direc-tion, i.e. from the bottom ~w~r~l~. It 1s essential, however, tha-t the movement shoulcl be vertical, 1..e. that the enclosure should be connected into a vertical section of the pneuma-tic pipe.
Finally, it should be emphasized that the experi.-mental installation has provided proof of the effici.ency of a "buffer" enclosure such as that propo~ed in the foregoing.
In this experimen-tal installation the diameter of the pipe lS 40 mm, whereas -the diameter of the "buffer" encl.osure 14 i5 100 mm, its height being 4000 mm.
The present invention relates to a process for the pneumatic transport at a uniform rate, of pulverulent mate-riaLs which are introduced into a carrier gas by means oE
rotary valve and wherein said carrier gas is guided through the rotary valve in a direction parallel to the rota~ion a~ls of the latter. The invention likewise relates ~o an install-ation for the performance of this process and also, as anexample of its application, to a process and an installation for the injec-tion of solid fuels in a shaft furnace.
Canadian Paten~ application ~i~,llO ~escri~es a process and an installation for the dosing and transport, by pneumatic means, of solid materials to an enclosure under pressure, particularly for the injection c,f solid Euels into a blast furnace. According -to the said patent applicatjon each nozzle or pair of no7zles is fed separately from a reservoir supplied with the necessary quantities of coal dust or powdered lignite. The transport of this powder between the said reservoir and the blast furnace is effected pneumatically/ and it has been found that the safest and most reliable means of taking selected quantities of materials from the reservoir is a rotary valve, already well known se. A valve of this kind consists essentially of a cylin-drical rotor provided on its periphery with a certain number of blades defining ~ corresponding n~mber of cells. This rotor rotates in a tight manner inside a case, and the mate-rial fed in from the top is conveyed downwards by the cells into a currerlt of air under pressure, which serves as a ,....
,;L~ J~
carrier gas. This carrier gas take~ up and c~rries along with it each quantity of mater:Lal as the latter is fed from a cell of the rotor.
In the aforementioned applicationl however, it has been found that the cells are ins~antaneousl~ emptied as soon as they en-ter the current of air in the pneumatic E~ipe. In other words, as soon as a cell gives up its con-tents there is a certain "deadl'' period during which the pul-verulent material is not taken into the pneumatic pipe, this inoperative period lasting until the mornent when the sub-sequent cell moves into position. The pulverulent fuel is thus injected into the blast furnace in small intermittent "lots" of which the periodici.ty depends on the speed of the rotor. In the application in question this speed is such that the cells cut across the pneumatic conduit at the rate of one cell per second, thus feeding the l'lots" of fuel to i.t at the same rate.
This phenomenon is due to the fact that a high speed and pressure have to be adopted in the pneumatic pipe~
The speed cannot be below 18 m/sec~ if deposits and back-firing from the blast furnace are to be avoided, while the pressure must be above the counter-pressure prevailing inside the furnace. In other applications than that envisaged in the present invention this phenomenon is of no consequence.
The fact is that it either does not occur, as a result of a low pressure and speed, or else can be eliminated, by re-ducing the pressure, for example, and where the only purpose in view is the transport of the pulverulent products it can even be allowed to continue, for in such cases it is immate-rial whether the subs~ance is propelled continuously or dlscontlrluously.
In the application ln questlon, ho~ever, i.e. inthe injection of coal dust or powdered 1.ignite into a blast furllace, it must be borrle in m.ind that thls powder has to be ~urnt in the furnace, for which purpose a certain q~antity of oxygen, servlng to rnaintain the combllstion process, is injected continuously through the tuyere stocks. l'hls quan-tity of oxygen or enriched air is needless to say calculated in accordance with the quan-tity of fuel, i.e. the quantity injected will be -that necessary and sufficient to burn the quantity of fuel to be injected into the furnace.
Now if the ligrlite or coal is injected in small separate quantities, the oxygen injected during the "dead"
periods elapsing between two successive "lots" of fuel will remain unused, entering -the rnass of material inside the furnace. Similarly, when a separate quantity of fuel is injected its mass is too great for the quantity of oxygen supplied, so that the fuel will not undergo complete com-bustion. To su~ up, it may be said that although ~he total quantity of fuel injected wil3 be that for which the quantity of oxygen has been calculated the intermittent injection of the former will lead to an alternating excess and shortage thereof accompanying a constant quantity of oxygen.
The purpose of the present invention is to provide a new process which avoids this "pulsation" in the transport of material in the pneumatic conduit, as well. as an install-ation for the performace of the process.
a, In accordance with the present: .invention there i.s provided a process for the pneumatic transport of pulverized material, the pulverized material being deliverecl into a pressurized carrier gas stream by a rotary valve feeder and tne velocity of the carrier gas being sufficiently great to entrain the material fro[n a first compa:rtment of the rotary valve feeder before a second filled compartment is exposecl to the gas whereby the ratio of the quantity of pulverized ~aterial to carrier gas varies periodically, the improvement comprising:
causing the carrier gas-pulverized material stream to expand and undergo a reduction in velocity while 10wi2lg vertically upward to thereby create a fluidized hed dowrlstream of the rotary valve feeder;
such velocity reduction being produced by causing the carrier gas-pulverized material mixture to flow through a divergent conduit section in the shape of a trunca-ted cone having an angle of conicity of at least ~0, and extracting a carrier gas~pulverized material stream having a substantially uniform solid material to carrier gas ratio fro~ the fluidized bedO
Preferably, the carrier gas pulverized m~terial stream forming the fluidized bed is subsequently caused to flow through a convergent conduit section in the shape of a truncated cone.
Also in accordarlce with the inven-tion there is provided an installation for the uniform pneumatic transport of pulverulent material, comprising a rotary valve feeder having a - 4a plurality o:E cel.ls for the distribu~ion of measured quantities of pulverulent material, a pneumatic transport conduit connecting the rotary valve feeder to a receiving station for the perverulent material, the pneumatic transport conduit delivering carrier gas to pass through the cells of the rotor of the rotary valve feeder4 in a di.rec-tivn parallel to the latter's rotation axis and servLng to take up the pulverulent material in the rotor cells as and when it is fed into position by the rotor cells and carry it along, a vertical elongated "buEfer"
enclosure connected into the pneumatic transport conduit downstream fr~m the rotary valve feede.r and of which the cross section is greater than that of the said transport conduit, the said "buffer" enclosure comprising a cylindrical body connected to the said transport conduit by divergent and convergent conduit sections of the shape of a trunca-ted cone, wherein the angle oE conicity oE the conical section on the side corresponding to the rotary valve feeder is at least 20, -the cross section of the enclosure being such that the speed oE the fluid will be suEficient to maintain a fluidi~ed bed.
Although the process and tile inst~llcltlor~ can be adop-ted wherever required for the purpose of elimlnatin~
a pneurnatic transport pipe the pvlsating effect described farther back, the invention offers paLticular clclval~tayex for the injection of soli,d fuels in a sl~aft furnaceO
Fur~her features and characteristics will emerge from the following detail,ed clescription of one advantageous en~odiment illustratiny the invention by reference to the single drawing provi,ding a schematic diagram, partly in section, of a chamber having a rotary valve and traversed by a pneumatic pipe provided with a "buffer" enclosure in accordance with the invention.
The rotary valve shown in this diagram is marked "2" as a whole. This char~ber consists essentially of a rotor 4 rotating about an axis perpendicular to the drawing and provided on its periphery with a set o blades 6 forming the boundari,es of a corresponding number of cells 8~ Pulve rulent material such as powdered lignite or coal dust acc~nulates by gravity ln an upper hopper 10 and fills each of the cells 8 as and when the rotor 4 rotatesO This rota-tion, in the case of the example shown, takes place in a clockwise direction. A pneumatic pipe 12 traverses the lower part of thle rotary valve 2, in a direction parallel to the rotation axis of the ro-tor 4, and carries along the pulve-rulent rnaterial as and when the bl.ades 6 pass the pOsitlo in question. Now owing to the high speed and pressure of the carrier gas ci.rculating in tire pipe 12, the contents of the cells 4 are evacua-ted -therefrom as soon as the saicl cells enter the current in -the pipe :l2. In the diagram ~he blade marked 6a has just entered the pneumatic current and the cell pxeceding it is being emptied, while the ce].1 4a precedin~ the blade 6a has already been comple-tely emptied As soon as the cell situated behind this bl.ade 6a has been emptied a "dead" period will occur during wh:ich no pulve-rulen-t ma-terial is bei.ng caused -to enter the pne~a-tic current and which will con-tinue until the subseqwent cell enters the passage of -the said current.
In order to ensure that the pneumatic transport of the pulverulent ma-terial will take place at a uniform rate and the intermittent ac-tion will be eliminated, the pipe 12 contains a "buffer" enclosure 14 "downstream" from -the valve 2. This enclosure consists of a cylinder 16 connected into the pipe by means of two sections 18 and 70 o the shape of a truncated cone. The aperture angle ~ of -the lower frusto-conical section must be above a certain value in oxder to prevent the pneumatic current from passing direct through -the enclosure 14 without undergoing any modification~ This angle ~ rnust be above 20 and preferably equal to 45, in order to cause eddies -to form a-t the entry into the enclosure 14. The divergence and -the e~pansion taking place in the said encl.osure 14 re.sult in a reduction in spe~d. The section of this enclosure 14, however, mus-t not exceed a certaln limit, corresponding to the speed required for the purpose of maintaining a kind o-f fluidized sJ
bed lnside the sai.cl enclosure l~o From this fl.l:lidi.zed bed onwards -the pulverule~t material is carri.ed along at a uni.form ratè by the air under pressu.re :leaviny the enclosu-re 14 It should be noted that instead of causing it to pass through the enclosure from the bottom upwards it is equally possiblé to cause it to pass through lt in t}le V~
opposite direc-tion, i.e. from the bottom ~w~r~l~. It 1s essential, however, tha-t the movement shoulcl be vertical, 1..e. that the enclosure should be connected into a vertical section of the pneuma-tic pipe.
Finally, it should be emphasized that the experi.-mental installation has provided proof of the effici.ency of a "buffer" enclosure such as that propo~ed in the foregoing.
In this experimen-tal installation the diameter of the pipe lS 40 mm, whereas -the diameter of the "buffer" encl.osure 14 i5 100 mm, its height being 4000 mm.
Claims (7)
OR PRIVILEGE IS CLAIMED ARE DEFINED AS FOLLOWS:
1. In a process for the pneumatic transport of pulverized material, the pulverized material being delivered into a pressurized carrier gas stream by a rotary valve feeder and the velocity of the carrier gas being sufficiently great to entrain the material from a first compartment of the rotary valve feeder before a second filled compartment is exposed to the gas whereby the ratio of the quantity of pulverized material to carrier gas varies periodically, the improvement comprising:
causing the carrier gas-pulverized material stream to expand and undergo a reduction in velocity while flowing vertically upward to thereby create a fluidized bed downstream of the rotary valve feeder;
such velocity reduction being produced by causing the carrier gas-pulverized material mixture to flow through a divergent conduit section in the shape of a truncated cone having an angle of conicity of at least 20°; and extracting a carrier gas-pulverized material stream having a substantially uniform solid material to carrier gas ratio from the fluidized bed.
causing the carrier gas-pulverized material stream to expand and undergo a reduction in velocity while flowing vertically upward to thereby create a fluidized bed downstream of the rotary valve feeder;
such velocity reduction being produced by causing the carrier gas-pulverized material mixture to flow through a divergent conduit section in the shape of a truncated cone having an angle of conicity of at least 20°; and extracting a carrier gas-pulverized material stream having a substantially uniform solid material to carrier gas ratio from the fluidized bed.
2. A process as claimed in claim 1, wherein the carrier gas-pulverized material stream forming the fluidized bed is subsequently caused to flow through a convergent conduit section in the shape of a truncated cone.
3. The process of claim 2 wherein the step of creating the fluidized bed further comprises:
limiting the cross sectional area of the region of the conduit between the divergent and convergent conduit section to levels which ensure maintenance of the fluidized bed, the volume of said conduit region being greater than the volume of a single compartment of the rotary valve feeder and the volume of carrier gas which passes through a single feeder compartment.
limiting the cross sectional area of the region of the conduit between the divergent and convergent conduit section to levels which ensure maintenance of the fluidized bed, the volume of said conduit region being greater than the volume of a single compartment of the rotary valve feeder and the volume of carrier gas which passes through a single feeder compartment.
4. A process as claimed in any one of claims 1 to 3 for the injection of solid fuel in a shaft furnace.
5. An installation for the uniform pneumatic transport of pulverulent material, comprising a rotary valve feeder having a plurality of cells for the distribution of measured quantities of pulverulent material, a pneumatic transport conduit connecting the rotary valve feeder to a receiving station for the perverulent material, the pneumatic transport conduit delivering carrier gas to pass through the cells of the rotor of the rotary valve feeder in a direction parallel to the latter's rotation axis and serving to take up the pulverulent material in the rotor cells as and when it is fed into position by the rotor cells and carry it along, a vertical elongated "buffer"
enclosure connected into the pneumatic transport conduit downstream from the rotary valve feeder and of which the cross section is greater than that of the said transport conduit, the said "buffer" enclosure comprising a cylindrical body connected to the said transport conduit by divergent and convergent conduit sections of the shape of a truncated cone, wherein the angle of conicity of the conical section on the side corresponding to the rotary valve feeder is at least 20°; the cross section of the enclosure being such that the speed of the fluid will be sufficient to maintain a fluidized bed.
enclosure connected into the pneumatic transport conduit downstream from the rotary valve feeder and of which the cross section is greater than that of the said transport conduit, the said "buffer" enclosure comprising a cylindrical body connected to the said transport conduit by divergent and convergent conduit sections of the shape of a truncated cone, wherein the angle of conicity of the conical section on the side corresponding to the rotary valve feeder is at least 20°; the cross section of the enclosure being such that the speed of the fluid will be sufficient to maintain a fluidized bed.
6. An installation according to claim 5, wherein the enclosure is traversed by the carrier gas and takes up pulverent material from the bottom up.
7. An installation according to any one of claims 5 and 6, and for the injection of a solid fuel in a shaft furnace.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| LU82.601 | 1980-07-09 | ||
| LU82601A LU82601A1 (en) | 1980-07-09 | 1980-07-09 | METHOD AND INSTALLATION FOR THE UNIFORM PNEUMATIC TRANSPORT OF POWDER MATERIALS AND APPLICATION TO THE INJECTION OF SOLID FUELS IN A TANK OVEN |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1189112A true CA1189112A (en) | 1985-06-18 |
Family
ID=19729436
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000381120A Expired CA1189112A (en) | 1980-07-09 | 1981-07-03 | Uniform pulverant flow after metering feeder |
Country Status (8)
| Country | Link |
|---|---|
| EP (1) | EP0043606B1 (en) |
| JP (1) | JPS5748530A (en) |
| AT (1) | ATE5899T1 (en) |
| AU (1) | AU544696B2 (en) |
| CA (1) | CA1189112A (en) |
| DE (1) | DE3161951D1 (en) |
| LU (1) | LU82601A1 (en) |
| ZA (1) | ZA814281B (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108861607A (en) * | 2018-06-29 | 2018-11-23 | 安徽省碧绿春生物科技有限公司 | A kind of multiple-effect oxygenating type Blowing stopper |
Family Cites Families (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE415120C (en) * | 1925-06-23 | Theodor Steen | Device for conveying solid, dust-like material | |
| CH102441A (en) * | 1922-07-31 | 1923-12-01 | Klug Hermann | Method and device for the pneumatic conveying of shovelable bulk goods. |
| DE555366C (en) * | 1929-11-05 | 1932-07-25 | J M Voith Maschinenfabrik | Device for introducing grainy or fibrous conveyed material into compressed air lines |
| DE892494C (en) * | 1950-12-21 | 1953-10-08 | Steinmueller Gmbh L & C | Distributor for coal dust-air mixture lines |
| US3204942A (en) * | 1963-02-18 | 1965-09-07 | Babcock & Wilcox Co | Distributor for pneumatically transported particle-form material |
| FR1458703A (en) * | 1965-10-06 | 1966-03-04 | Babcock & Wilcox Co | Distributor for particulate matter |
| IN145376B (en) * | 1975-12-02 | 1978-09-30 | Babcock & Wilcox Co |
-
1980
- 1980-07-09 LU LU82601A patent/LU82601A1/en unknown
-
1981
- 1981-06-12 EP EP81200652A patent/EP0043606B1/en not_active Expired
- 1981-06-12 DE DE8181200652T patent/DE3161951D1/en not_active Expired
- 1981-06-12 AT AT81200652T patent/ATE5899T1/en active
- 1981-06-24 ZA ZA814281A patent/ZA814281B/en unknown
- 1981-06-29 AU AU72339/81A patent/AU544696B2/en not_active Ceased
- 1981-07-03 CA CA000381120A patent/CA1189112A/en not_active Expired
- 1981-07-07 JP JP56106194A patent/JPS5748530A/en active Pending
Also Published As
| Publication number | Publication date |
|---|---|
| JPS5748530A (en) | 1982-03-19 |
| ATE5899T1 (en) | 1984-02-15 |
| DE3161951D1 (en) | 1984-02-23 |
| AU544696B2 (en) | 1985-06-13 |
| EP0043606B1 (en) | 1984-01-18 |
| AU7233981A (en) | 1982-01-14 |
| LU82601A1 (en) | 1982-02-17 |
| EP0043606A1 (en) | 1982-01-13 |
| ZA814281B (en) | 1982-09-29 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| MKEX | Expiry |