CA1069681A - Process for preventing deposits on a gas inlet nozzle - Google Patents
Process for preventing deposits on a gas inlet nozzleInfo
- Publication number
- CA1069681A CA1069681A CA237,228A CA237228A CA1069681A CA 1069681 A CA1069681 A CA 1069681A CA 237228 A CA237228 A CA 237228A CA 1069681 A CA1069681 A CA 1069681A
- Authority
- CA
- Canada
- Prior art keywords
- nozzle
- bed
- angle
- gas
- particles
- 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
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- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
ABSTRACT
A gasification process wherein an oxygen-containing fluidizing gas is introduced through a nozzle into a bed of carbonaceous particles containing metallic contaminants, characterized in that the formation of metallic ash deposits on said nozzle is prevented by introducing said oxygen-containing fluidizing has into said bed as a downwardly directed stream at an angle of declination from a horizontal axis at least as great as the angle of repose of said bed particles and at an inlet velocity into said bed in the range of about 50 to 500 feet per second. The presence of stagnant or slow moving particles near the oxidizing gas inlet nozzle and the consequent formation of a solid deposition on the nozzle can be minimized or prevented when the oxidizing gas which also serves as fluidizing has is injected into a bed of particles in a downward direction at a specified angle and at a given gas exit velocity from the nozzle.
A gasification process wherein an oxygen-containing fluidizing gas is introduced through a nozzle into a bed of carbonaceous particles containing metallic contaminants, characterized in that the formation of metallic ash deposits on said nozzle is prevented by introducing said oxygen-containing fluidizing has into said bed as a downwardly directed stream at an angle of declination from a horizontal axis at least as great as the angle of repose of said bed particles and at an inlet velocity into said bed in the range of about 50 to 500 feet per second. The presence of stagnant or slow moving particles near the oxidizing gas inlet nozzle and the consequent formation of a solid deposition on the nozzle can be minimized or prevented when the oxidizing gas which also serves as fluidizing has is injected into a bed of particles in a downward direction at a specified angle and at a given gas exit velocity from the nozzle.
Description
~06968~
BACKGROUND OF THE IN~IENTION
1, Field of the InYention This invention relates to a process for pre~
venting the deposition of solids on a gas inlet nozzle positioned in a fluidized ~ed of particles It particularly relates to a method of preventing the presence of a stagnant Of slow moving particles in t~e zone of the gas inlet in a bed of particles. More particularly, it relates to pre-Yenting the formation of metallic ash deposits on the lQ nozzle inlet which supplies an o~idizing gas to fluidize a bed of car~onaceous solids containing metallic contaminants.
BACKGROUND OF THE IN~IENTION
1, Field of the InYention This invention relates to a process for pre~
venting the deposition of solids on a gas inlet nozzle positioned in a fluidized ~ed of particles It particularly relates to a method of preventing the presence of a stagnant Of slow moving particles in t~e zone of the gas inlet in a bed of particles. More particularly, it relates to pre-Yenting the formation of metallic ash deposits on the lQ nozzle inlet which supplies an o~idizing gas to fluidize a bed of car~onaceous solids containing metallic contaminants.
2. Description of the Prior Art Fluid ~ed gas:ification Pxocesses in ~hich a solid carbonaceous material is ~eacted with an oxygen-containing gas, such as, air or oxygen, and/or steam are well known in the art. Such a gasification process is shown, for example, in U.S. Patent 3,661,543, and in which an oxidizing gas ~air or oxygen2 and steam are injected into the ~ottom of a coke gasification zone. In such processes, the gas inlet nozzle is located in the fluid coke bed and conventionally aischarges a gas stream upwardly into the ~ed. Usually, areas of defluid-ized coke are present between nozzle injection points. When petroleum coke, which contains metallic contaminants, such as, vanadium and nickel components, is gasifiea by reaction with steam and an oxidizing gas to produce a fuel gas, a metallic ash-rich coke residue ~uilds up near and around the oxidiz-~ . ' .
- : :
.. . ., . -~, ing gas inlet of th.e conyentional straigh.t tu~e, upwardly directed, nozzle. Some of this ash:su~sequently farms a deposit on the surface and tip of the gas inlet nozzle and there~y interferes with the operation of the nozzle. It is believed that the passage of the metallic ash-rich coke ' . ~ 2A
.. . .
:
. .
-particles through the small oxidizing zone near the gas inlet causes some of the metallic components to be converted to metallic oxides, some of which melt at a temperature lower than the ~emperature at which the gasification zone is maintained. This molten material readily adheres to the surface and tip of the gas inlet nozzle, solidifies and clogs the orifice of the nozzle.
It has now been found that the presence of stagnant or slow moving particles near the oxidizing gas inlet nozzle and the consequent formation of a solid deposition on the nozzle can be minimized or prevented when the oxidizing gas which also serves as fluidizing gas is in]ected into a bed of particles in a downward direction at a specified angle and at a given gas exit velocity from the nozzle.
SUMMARY OF THE INVENTION
In accordance with the invention there is provided a gasification process wherein an oxygen-containing fluidizing gas is introduced through a nozzle into a bed of carbonaceous particles containing metallic contaminants, characterized i~ that the formation of metallic ash deposits on said nozzle is prevented by introducing said oxygen-containing fluidizing gas into said bed as a downwardly directed stream at an angle of declination from a horizontal axis at least as great as the angle of repose of said bed particles and at an inlet velocity into said bed in the range of about 50 to 500 feet per second.
An improved apparatus for carrying out the process of the invention is also provided.
BRIEF DESCRIPTION OF THE DRAWING
Figure 1 illustrates, in diagrammatic form, a suitable
- : :
.. . ., . -~, ing gas inlet of th.e conyentional straigh.t tu~e, upwardly directed, nozzle. Some of this ash:su~sequently farms a deposit on the surface and tip of the gas inlet nozzle and there~y interferes with the operation of the nozzle. It is believed that the passage of the metallic ash-rich coke ' . ~ 2A
.. . .
:
. .
-particles through the small oxidizing zone near the gas inlet causes some of the metallic components to be converted to metallic oxides, some of which melt at a temperature lower than the ~emperature at which the gasification zone is maintained. This molten material readily adheres to the surface and tip of the gas inlet nozzle, solidifies and clogs the orifice of the nozzle.
It has now been found that the presence of stagnant or slow moving particles near the oxidizing gas inlet nozzle and the consequent formation of a solid deposition on the nozzle can be minimized or prevented when the oxidizing gas which also serves as fluidizing gas is in]ected into a bed of particles in a downward direction at a specified angle and at a given gas exit velocity from the nozzle.
SUMMARY OF THE INVENTION
In accordance with the invention there is provided a gasification process wherein an oxygen-containing fluidizing gas is introduced through a nozzle into a bed of carbonaceous particles containing metallic contaminants, characterized i~ that the formation of metallic ash deposits on said nozzle is prevented by introducing said oxygen-containing fluidizing gas into said bed as a downwardly directed stream at an angle of declination from a horizontal axis at least as great as the angle of repose of said bed particles and at an inlet velocity into said bed in the range of about 50 to 500 feet per second.
An improved apparatus for carrying out the process of the invention is also provided.
BRIEF DESCRIPTION OF THE DRAWING
Figure 1 illustrates, in diagrammatic form, a suitable
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106968~
apparatus for carrying out a preferred embodiment of the invention.
Figure 2 is a detailed schematic representation of the gas inlet nozzle shown in the apparatus of Figure 1.
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PRE ERRED EMBODIMENT OF THE INVENTION
The preferred embodiment of the invention will be described with reference to the accompanying drawing.
Referring to Figure 1, a gasefier 1 contains a bed of carbonaceous material (coke) 2 supported on a bed support sheet 3. When the bed is fluidized by the intro-duction of a fluidizing gas into the bedJ as will be de-scribed later~ the fluidized bed has an upper level indicated at 4. Generally, a portion of defluidized carbonaceous particles having a level indicated at 11 is also present under operating conditions. Although in the following de-scription the carbonaceous material present in the gasifier will be designated as coke, suitable solid carbonaceous ma-terials for the gasification process include petroleum coke, coal coke, coal, peat, graphite, charcoal or mixtures there-of. When it iB desired to obtain a fuel gas comprising hy-drogen and carbon monOxite by gasification of coke wlth stea~ and an oxygen-containing gas, the gasifier is main-tainet at a temperature of about 1000F. to 2800F., prefer-ably in the range of about 1700 to 1900F. ant at a pressure up to about 2000 pounds per square inch gauge (psig), pref-erably at a pressure not greater than about 60 psig. An oxygen-containing gas, such as air or oxygen, which in the preferret embodiment also contains steam, is passed vla line 5 through internal inlet contuit 6 into nozzles 7 located in the gasifier to serve also as the fluidizing gas needed to form a fluitized bed of the coke particles. Each nozzle 7 is connected to a vertical inlet conduit 6. Nore than one nozzle 7 may be connected to the same vertical inlet conduit.
Although vertical inlet conduit 6 is shown as having two sym-metrical nozzles 7~ one or more than two nozzles connected to a single inlet conduit would also be suitable. In Figure _ 4 -.. . ~ , . . . . .
.' :' :- .: -: : , - -. ~ . . . . : -, . .: : - -.. ~ .
` 106~68~
l, three inlet conduits, each having two nozzles, are shown. It is to be understood that one or more such inlet conduits having one or more nozzles could be used depending on the specific gasification process and si~e of the gasi-fication vessel utilized. In commercial size gasifiers, more than one such nozzle would be utilized to fluidize the bed. Returning to Figure 1, each nozzle 7 is directed in a downward direction at an angle of declination from horizontal axis 8 at least as great (that is, at least equal to) or greater than the angle of repose 9 of the coke parti-cles present in gasifier 1. The angle of declination of nozzle 7 can range up to an angle of about 90 degrees. By the expression "angle of repose" is intended herein the specific angle that a powdered, granular or particulate matter will assume when it is unloaded in an unconfined man-ner. For example, for fluid petroleum coke, a typical angle of repose is 30 degrees. Preferably, the nozzle is downward-ly directed at an angle 15 to 60 degrees greater than the angle of repose of the particles present in the gasifier. -The gaseous mixture of steam and an oxidizing gas introduced into the gasifier via line 5, then through internal vertical conduit 6, leaves the orifice of nozzle 7 at an exit velocity in the ran8e of about 50 to 500 feet per second, preferably at a g8S exit velocity from the nozzle in the ran8e of about 100 to 350 feet per second. For example~ an angle of declina-tion 15 to 30 degrees greater than the angle of repose of the particles may be utilized with a gas exit velocity great-er than 175 feet per second. Desirably, the higher gas exit velocitiès are utilized as the angle of declination of the nozzle approaches the angle of repose of the particles.
Reaction of the coke particles with the steam and oxygen-containing gas produces a fuel gas which is removed .. .... .. . .... . ... .. . . . . .
~.069681 1 overhead from the gasifier via line 10. kn ash-rich coke 2 residue containing me~allic components, including vanadium 3 compounds, is present in ~he gasifier. The surface and tip
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..
- . . - : . . . ~ .. , - :
.. ~ . . .. . . - .
~;. : . . .' : ' , ~ . ~, . .. . -- : ~ ' . ~: , .
106968~
apparatus for carrying out a preferred embodiment of the invention.
Figure 2 is a detailed schematic representation of the gas inlet nozzle shown in the apparatus of Figure 1.
-3a-r~1 . .
-, , , ~ . -- . . - . , . . - .
... . , - . : .
.. . . - , -, ,, - , : : , .
PRE ERRED EMBODIMENT OF THE INVENTION
The preferred embodiment of the invention will be described with reference to the accompanying drawing.
Referring to Figure 1, a gasefier 1 contains a bed of carbonaceous material (coke) 2 supported on a bed support sheet 3. When the bed is fluidized by the intro-duction of a fluidizing gas into the bedJ as will be de-scribed later~ the fluidized bed has an upper level indicated at 4. Generally, a portion of defluidized carbonaceous particles having a level indicated at 11 is also present under operating conditions. Although in the following de-scription the carbonaceous material present in the gasifier will be designated as coke, suitable solid carbonaceous ma-terials for the gasification process include petroleum coke, coal coke, coal, peat, graphite, charcoal or mixtures there-of. When it iB desired to obtain a fuel gas comprising hy-drogen and carbon monOxite by gasification of coke wlth stea~ and an oxygen-containing gas, the gasifier is main-tainet at a temperature of about 1000F. to 2800F., prefer-ably in the range of about 1700 to 1900F. ant at a pressure up to about 2000 pounds per square inch gauge (psig), pref-erably at a pressure not greater than about 60 psig. An oxygen-containing gas, such as air or oxygen, which in the preferret embodiment also contains steam, is passed vla line 5 through internal inlet contuit 6 into nozzles 7 located in the gasifier to serve also as the fluidizing gas needed to form a fluitized bed of the coke particles. Each nozzle 7 is connected to a vertical inlet conduit 6. Nore than one nozzle 7 may be connected to the same vertical inlet conduit.
Although vertical inlet conduit 6 is shown as having two sym-metrical nozzles 7~ one or more than two nozzles connected to a single inlet conduit would also be suitable. In Figure _ 4 -.. . ~ , . . . . .
.' :' :- .: -: : , - -. ~ . . . . : -, . .: : - -.. ~ .
` 106~68~
l, three inlet conduits, each having two nozzles, are shown. It is to be understood that one or more such inlet conduits having one or more nozzles could be used depending on the specific gasification process and si~e of the gasi-fication vessel utilized. In commercial size gasifiers, more than one such nozzle would be utilized to fluidize the bed. Returning to Figure 1, each nozzle 7 is directed in a downward direction at an angle of declination from horizontal axis 8 at least as great (that is, at least equal to) or greater than the angle of repose 9 of the coke parti-cles present in gasifier 1. The angle of declination of nozzle 7 can range up to an angle of about 90 degrees. By the expression "angle of repose" is intended herein the specific angle that a powdered, granular or particulate matter will assume when it is unloaded in an unconfined man-ner. For example, for fluid petroleum coke, a typical angle of repose is 30 degrees. Preferably, the nozzle is downward-ly directed at an angle 15 to 60 degrees greater than the angle of repose of the particles present in the gasifier. -The gaseous mixture of steam and an oxidizing gas introduced into the gasifier via line 5, then through internal vertical conduit 6, leaves the orifice of nozzle 7 at an exit velocity in the ran8e of about 50 to 500 feet per second, preferably at a g8S exit velocity from the nozzle in the ran8e of about 100 to 350 feet per second. For example~ an angle of declina-tion 15 to 30 degrees greater than the angle of repose of the particles may be utilized with a gas exit velocity great-er than 175 feet per second. Desirably, the higher gas exit velocitiès are utilized as the angle of declination of the nozzle approaches the angle of repose of the particles.
Reaction of the coke particles with the steam and oxygen-containing gas produces a fuel gas which is removed .. .... .. . .... . ... .. . . . . .
~.069681 1 overhead from the gasifier via line 10. kn ash-rich coke 2 residue containing me~allic components, including vanadium 3 compounds, is present in ~he gasifier. The surface and tip
4 of the nozzle are substantially free of ash depositions.
By in;ecting the oxidizing gas in a downward di-6 rection into the bed, the nozzle surface is above the oxi-7 dizing zone whlch is near the inlet of the oxidiz~ng gas.
8 The presence of stagnant or 810w ving coke particles near 9 the gas inlet is con~rolled by inJecting the oxidizing gas at a specified range of velocity into the bed.
11 In Figure 2~ nozzle 7 of Figure 1 is shown in en-12 larged side elevation section.
13 Although the process of the invention is particu-14 larly well suited for gasification reactions9 it is also applicable to other fluidi~ed bed systems to inhibit the 16 presence of ~low moving particles near a gas inlet or to pro-17 vide for more uniform mixing o~ the particles in a fluid bed.
18 The following example is presented to illu~trate lq the process and nozzle of the present invention.
EXAMPLE
21 Tests were conducted with nozzles having three dif-22 ferent types of configuration as follows:
23 A. kn upwardly directed flow noz~-le having a ver-24 tical straight tube stem or inle~ conduit having an opening at its upper end. m e internal diameter of the tube was one-26 fourths of an inch and the opening in the tip was 0~23 ~Y~S.
27 Bo A side directed flow nozzle having a vertical 28 straight tube stem or inlet conduit closed at its upper end.
29 m e internal diameter of the tube was one~fourths of an inch a~d the~outer diame~er was three-eighths ~nches with four 31 holes of 2 millimeters spaced 90 degree~ apar~. The gas 32 exited from the holes at a 90 degree angle from the vertical ~.~ . .. . .................................... . ... . .
.
.
1069~;81 1 axis of the inlet tube~
2 C. A downwardly directed flow nozzle having a 3 vertical straight tube inlet stem and a nozzle directed at 4 an angle of declination 90 degrees from the horizontal axis.
The internal diameter of the stem was one-eighths of an inch 6 and the outer diameter of the stem was one-fourth of an inch.
7 The tests were carried out in a 3-inch by 96 in-8 ches reactor in which a high ash coke obtained from a com-9 mercial coker was gasified continuously by reaction with a gas mixture of steam and airc A single nozzle design was 11 evaluated during each run. The operat~ng conditions and re- ;
12 sults are su~marized in the following table.
13 ~ er 14 Nozzle Design A B C
15 A8h Content of Feed Coke, 0.68 0.68 0.68 16 wt. %
17 Vanadium Content of Feed 18 coke,ppm 2800 2800 2800 19 Temperature, F. 1800 1800 1800 20 Pressure, psig 0 0 0 21 Gasification Level,% 69 67 64 22 ~ength of Test Run, Hrs. 105 99 144 23 Gas Exit Velocity, FtlSec.
24 @1000F. 97 95 149 26 Wt of De~08it x 100 2.2 0.4 0.0 27 me above data show that no deposit was fonmed on 28 the downwardly directed nozzleO
: ......
: ~ 7 ~
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By in;ecting the oxidizing gas in a downward di-6 rection into the bed, the nozzle surface is above the oxi-7 dizing zone whlch is near the inlet of the oxidiz~ng gas.
8 The presence of stagnant or 810w ving coke particles near 9 the gas inlet is con~rolled by inJecting the oxidizing gas at a specified range of velocity into the bed.
11 In Figure 2~ nozzle 7 of Figure 1 is shown in en-12 larged side elevation section.
13 Although the process of the invention is particu-14 larly well suited for gasification reactions9 it is also applicable to other fluidi~ed bed systems to inhibit the 16 presence of ~low moving particles near a gas inlet or to pro-17 vide for more uniform mixing o~ the particles in a fluid bed.
18 The following example is presented to illu~trate lq the process and nozzle of the present invention.
EXAMPLE
21 Tests were conducted with nozzles having three dif-22 ferent types of configuration as follows:
23 A. kn upwardly directed flow noz~-le having a ver-24 tical straight tube stem or inle~ conduit having an opening at its upper end. m e internal diameter of the tube was one-26 fourths of an inch and the opening in the tip was 0~23 ~Y~S.
27 Bo A side directed flow nozzle having a vertical 28 straight tube stem or inlet conduit closed at its upper end.
29 m e internal diameter of the tube was one~fourths of an inch a~d the~outer diame~er was three-eighths ~nches with four 31 holes of 2 millimeters spaced 90 degree~ apar~. The gas 32 exited from the holes at a 90 degree angle from the vertical ~.~ . .. . .................................... . ... . .
.
.
1069~;81 1 axis of the inlet tube~
2 C. A downwardly directed flow nozzle having a 3 vertical straight tube inlet stem and a nozzle directed at 4 an angle of declination 90 degrees from the horizontal axis.
The internal diameter of the stem was one-eighths of an inch 6 and the outer diameter of the stem was one-fourth of an inch.
7 The tests were carried out in a 3-inch by 96 in-8 ches reactor in which a high ash coke obtained from a com-9 mercial coker was gasified continuously by reaction with a gas mixture of steam and airc A single nozzle design was 11 evaluated during each run. The operat~ng conditions and re- ;
12 sults are su~marized in the following table.
13 ~ er 14 Nozzle Design A B C
15 A8h Content of Feed Coke, 0.68 0.68 0.68 16 wt. %
17 Vanadium Content of Feed 18 coke,ppm 2800 2800 2800 19 Temperature, F. 1800 1800 1800 20 Pressure, psig 0 0 0 21 Gasification Level,% 69 67 64 22 ~ength of Test Run, Hrs. 105 99 144 23 Gas Exit Velocity, FtlSec.
24 @1000F. 97 95 149 26 Wt of De~08it x 100 2.2 0.4 0.0 27 me above data show that no deposit was fonmed on 28 the downwardly directed nozzleO
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: ~ 7 ~
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Claims (6)
IS CLAIMED ARE DEFINED AS FOLLOWS:
1. A gasification process wherein an oxygen-containing fluidizing gas is introduced through a nozzle into a bed of carbonaceous particles containing metallic contaminants, characterized in that the formation of metallic ash deposits on said nozzle is prevented by introducing said oxygen-containing fluidizing gas into said bed as a downwardly directed stream at an angle of declination from a horizontal axis at least as great as the angle of repose of said bed particles and at an inlet velocity into said bed in the range of about 50 to 500 feet per second.
2. The process of claim 1 wherein said inlet velocity of said oxygen-containing gas is in the range of about 100 to 350 feet per second.
3. The process of claim l wherein said downwardly directed nozzle is at an angle of declination of about 15° to 60° greater than the angle of repose of said carbonaceous bed of particles.
4. The process of claim 1 wherein said angle of declination ranges up to an angle of about 90°.
5. The process of claim 1 wherein said inlet velocity of said gas is greater than about 175 feet per second and said angle of declination is about 15° to 30° greater than said angle of repose.
6. The process of claim 1 wherein said oxygen-containing gas comprises a mixture of steam and an oxidizing gas.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA237,228A CA1069681A (en) | 1975-10-07 | 1975-10-07 | Process for preventing deposits on a gas inlet nozzle |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA237,228A CA1069681A (en) | 1975-10-07 | 1975-10-07 | Process for preventing deposits on a gas inlet nozzle |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1069681A true CA1069681A (en) | 1980-01-15 |
Family
ID=4104217
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA237,228A Expired CA1069681A (en) | 1975-10-07 | 1975-10-07 | Process for preventing deposits on a gas inlet nozzle |
Country Status (1)
| Country | Link |
|---|---|
| CA (1) | CA1069681A (en) |
-
1975
- 1975-10-07 CA CA237,228A patent/CA1069681A/en not_active Expired
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| Date | Code | Title | Description |
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| MKEX | Expiry |