CA2073908A1 - Rotary gas injector - Google Patents
Rotary gas injectorInfo
- Publication number
- CA2073908A1 CA2073908A1 CA002073908A CA2073908A CA2073908A1 CA 2073908 A1 CA2073908 A1 CA 2073908A1 CA 002073908 A CA002073908 A CA 002073908A CA 2073908 A CA2073908 A CA 2073908A CA 2073908 A1 CA2073908 A1 CA 2073908A1
- Authority
- CA
- Canada
- Prior art keywords
- impeller
- diameter
- gas injector
- rotary gas
- liquid
- 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.)
- Abandoned
Links
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
- B01F23/20—Mixing gases with liquids
- B01F23/23—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids
- B01F23/233—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids using driven stirrers with completely immersed stirring elements
- B01F23/2331—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids using driven stirrers with completely immersed stirring elements characterised by the introduction of the gas along the axis of the stirrer or along the stirrer elements
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
- B01F23/20—Mixing gases with liquids
- B01F23/23—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids
- B01F23/233—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids using driven stirrers with completely immersed stirring elements
- B01F23/2331—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids using driven stirrers with completely immersed stirring elements characterised by the introduction of the gas along the axis of the stirrer or along the stirrer elements
- B01F23/23311—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids using driven stirrers with completely immersed stirring elements characterised by the introduction of the gas along the axis of the stirrer or along the stirrer elements through a hollow stirrer axis
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
- B01F23/20—Mixing gases with liquids
- B01F23/23—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids
- B01F23/233—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids using driven stirrers with completely immersed stirring elements
- B01F23/2331—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids using driven stirrers with completely immersed stirring elements characterised by the introduction of the gas along the axis of the stirrer or along the stirrer elements
- B01F23/23314—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids using driven stirrers with completely immersed stirring elements characterised by the introduction of the gas along the axis of the stirrer or along the stirrer elements through a hollow stirrer element
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
- B01F23/20—Mixing gases with liquids
- B01F23/23—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids
- B01F23/233—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids using driven stirrers with completely immersed stirring elements
- B01F23/2334—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids using driven stirrers with completely immersed stirring elements provided with stationary guiding means surrounding at least partially the stirrer
- B01F23/23341—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids using driven stirrers with completely immersed stirring elements provided with stationary guiding means surrounding at least partially the stirrer with tubes surrounding the stirrer
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
- B01F23/20—Mixing gases with liquids
- B01F23/23—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids
- B01F23/233—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids using driven stirrers with completely immersed stirring elements
- B01F23/2336—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids using driven stirrers with completely immersed stirring elements characterised by the location of the place of introduction of the gas relative to the stirrer
- B01F23/23364—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids using driven stirrers with completely immersed stirring elements characterised by the location of the place of introduction of the gas relative to the stirrer the gas being introduced between the stirrer elements
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F27/00—Mixers with rotary stirring devices in fixed receptacles; Kneaders
- B01F27/05—Stirrers
- B01F27/11—Stirrers characterised by the configuration of the stirrers
- B01F27/111—Centrifugal stirrers, i.e. stirrers with radial outlets; Stirrers of the turbine type, e.g. with means to guide the flow
Abstract
Abstract of the Disclosure:
A rotary gas injector comprises a graphite impeller attached to the end of a hollow cylindrical graphite shaft having a central bore. The impeller is cylindrical in shape and has a plurality of cuts equally spaced around the circumference thereof to define blades for the impeller, and radial holes are drilled in the centre of the cuts and communicate with the central bore of the shaft, whereby gas injected through the bore in the shaft and the radial holes of the impeller are sheared by the blades to form fine bubbles to enhance mass transfer and chemical reaction in gas-liquid and gas-liquid-solid systems.
A rotary gas injector comprises a graphite impeller attached to the end of a hollow cylindrical graphite shaft having a central bore. The impeller is cylindrical in shape and has a plurality of cuts equally spaced around the circumference thereof to define blades for the impeller, and radial holes are drilled in the centre of the cuts and communicate with the central bore of the shaft, whereby gas injected through the bore in the shaft and the radial holes of the impeller are sheared by the blades to form fine bubbles to enhance mass transfer and chemical reaction in gas-liquid and gas-liquid-solid systems.
Description
2073~J~
ROTARY GAS INJECTOR
This invention relates to a rotary gas injector ~or use in gas-liquid and gas-liquid-solid systems.
Background of the Invention:
For chemical reactions to occur it is necessary to bring the reagents into contact with one another. When the reagents are present in different phasessuch as oxygen in air and sodium sulphite in water this can be a non-trivial problem. Practical reaction rates are achieved by maximizing the contact area between the different phases. In the case of most gas-liquid and gas-liquid-solid reactions this involves dispersing the gas phase, as small bubbles into the liquid phase. These fine bubbles can be generated by a number of mechanisms such as porous spargers, lances, or rotating impellers. If a rotating impeller is used, fine bubbles are formed by sheating the gas in vortexes created at the trailing edge of the impeller blades. When the impeller is rotated faster, the shear increases, creating larger numbers of smaller bubbles, with higher total gas-liquid surface area per unit gas volume.
ROTARY GAS INJECTOR
This invention relates to a rotary gas injector ~or use in gas-liquid and gas-liquid-solid systems.
Background of the Invention:
For chemical reactions to occur it is necessary to bring the reagents into contact with one another. When the reagents are present in different phasessuch as oxygen in air and sodium sulphite in water this can be a non-trivial problem. Practical reaction rates are achieved by maximizing the contact area between the different phases. In the case of most gas-liquid and gas-liquid-solid reactions this involves dispersing the gas phase, as small bubbles into the liquid phase. These fine bubbles can be generated by a number of mechanisms such as porous spargers, lances, or rotating impellers. If a rotating impeller is used, fine bubbles are formed by sheating the gas in vortexes created at the trailing edge of the impeller blades. When the impeller is rotated faster, the shear increases, creating larger numbers of smaller bubbles, with higher total gas-liquid surface area per unit gas volume.
2 ~i3~'33 In most systems it is possible to fabricate shafts and impellers from a variety of materials. Graphite has been used in some specialized applications,where the gases, liquids or solids present in the system are highly reactive to metals, or the temperature is extremely high. Graphite is a relatively inert andinexpensive material, but it is difficult to manufacture most standard impeller designs from graphite. Many unique impeller designs using graphite have been developed for such uses as aluminum degassing.
In some processes used for hydrogen removal from aluminum, an inert gas is injected using a rotary gas injector consisting of a graphite shaft and impeller. The gas is injected through an internal cavity in the graphite shaft and impeller, exiting either above or below the impeller. For the gas to be sheared into small bubbles the injected gas must be drawn into the low pressure zones createdbehind the impeller blades (relative to the direction of rotation). Depending on the impeller rotational speed and the gas injection rate, some gas may bypass the impeller and not be sheared and dispersed. This is not an efficient mode of operation.
Summary of ~e Invention:
The present invention provides an improved design for a rotary gas injector fabricated from graphite. This injector consists of an impeller attached to a hollow cylindrical shaft having a central bore. The impeller is cylindrical inshape and has a plurality of cuts equally spaced around the circumference thereof to define blades for the impeller. Radial holes are drilled in the centre of the cuts 2 ~ ~ 3 ,~ f.~ l3 and communicate with the central bore of the shaft.
When the shaft is rotated at sufficient speed and gas is injected through the shaft, exiting between the blades of the impeller through the radialholes, fine bubbles are formed by the shearing action of the blades. These fine bubbles serve to enhance gas-liquid mass transfer and chemical reaction in gas-liquid and gas-liquid-solid systems. The performance (total gas-liquid interfacial area per unit liquid volume) of the impeller can be measured as via the total rate of mass transfer or chemical reaction (for mass transfer limited reactions).
Short Description of the Drawings:
The present invention will now be described by way of example, with reference to the accompanying drawings in which:
Figures la and lb are drawings of one embodiment of the impeller of the rotary gas injector of the present invention;
Figure 2 is a drawing of the shaft of the rotary gas injector;
Figure 3 is a schematic drawing of the lay-out of the rotary gas injector;
Figure 4 is a plot of sodium sulphite concentration against time; and Figure S is a plot of solid magnesium oxide content against time.
Detailed Descripffon of the Invention:
Referring to Figures 1 through 3, the rotary gas injector 1 consists of an impeller 2 with diameter D, attached to a hollow cylindrical shaft 3 of diameter S. The impeller of the gas injector is cylindrical in shape, with the 4 2Q7390~
thickness W to diaMeter D ratio typically being between 0.2 and 1Ø In chemicalengineering applications for gas dispersion most impellers have a W/D ratio of 0.2 or less. It was found that increasing the impeller thickness to a W/D over 0.2 greatly improved gas dispersion at the expense of higher power consumption for agiven impeller speed. A practical limit exists on the thickness of the impeller because of the impeller weight and the strength of the graphite construction material. The impeller is fabricated with a series of U-shaped cuts 4 equally spaced around the circumference thereof, such that the width of the cut opening is equal to twice the radius of the curved end of the U. The width db of the U-shaped cuts 4 is between 0.12 and 0.20 of the diameter D of the impeller 2. The number of cuts can vary from 6 to 12 and is typically 9. The curved edges of the impeller remaining between these cuts, act as blades 5 of the impeller 2. Holes 6 with diameter do are drilled in the centre of each cut, located at height dc between 1/4 and 1/2 times the width W of the impeller, and preferably 1/3 the width of the impeller from the bottom of the impeller. The hole diameter do should be from 0.05 to 0.03 times the diameter D of the impeller. When the shaft 3 is rotated at sufficient speed and gas is injected through a bore 7 of diameter Sb centrally located in the shaft 3, entering a windbox 8 of diameter Sw, inside the impeller 2, and exiting between the blades of the impeller, through holes 6, fine bubbles 9 are formed by the shearing action of the blades.
The shaft 3 should be constructed of graphite of a grade identical to that used in the fabrication of the impeller. The diameter of the shaft, should be 5 2~73~08 from 0.17 to 0.425 times the iMpeller diameter, and preferably from 0.300 to 0.375.
The shaft length can be determined by the skilled practitioner based on the known properties of graphite and the special requirements of the intended application. The diameter Sb of the centrally located bore 7 can be made of uniform dimension along the length of the shaft or can vary. The maximum bore diameter Sb should not exceed 1/3 of the shaft diameter to insure the mechanical integrity of the shaft. The skilled practitioner can couple the top portion 10 of the shaft 3 to any suitable drive mechanism, insuring that the shaft turns true and that provision for gas injection is given in the drive mechanism. The bottom portion of the shaft should be threaded11 such that the shaft and impeller can be coupled together. The diameter of thethread 11 should be as standard size and preferably equal to the shaft diameter.The length t of the thread 11 should be between 0.25 and 0.3 of the diameter of the impeller. I~or a clockwise rotation, the thread 11 should be right hand, while a left hand thread 11 should be used for counterclockwise rotation of the gas injector.The impeller should be equipped with a threaded hole 12 such that the shaft 3 can be coupled to the impeller. The diameter dc of the hole 12 should be such that afemale thread matching the thread 11 on the shaft can be machined into the hole 12. The depth of the hole 12 should be incrementally less than the length t of the threaded portion 11 of the shaft. A hole should be drilled at the bottom of the threaded hole 12 to meet the radial holes 6 at the centre of the impeller, forming the windbox 8. The diameter Sw of the windbox 8 should be from 0.5 to 1.5 times the diarneter Sb of the bore 7 in the shaft 3, and preferably of identical diameter.
2 ~ 3 ~
The performance of the rotary gas injector is maximi~ed when it is used in a vessel 13 of proper dimensions. Best results are obtained when the ratio of the impeller diameter to the characteristic transverse length T of the vessel 13 is between 0.25 and 0.5, and particularly between 0.3 and 0.4. For cylindrical vessels the characteristic length T is the diameter, while for square vessels the characteristic length, is the length of one side. If a rectangular vessel is used both the length 1 to diameter D and width w to diameter D ratios, should be between 0.25 and O.S.
The impeller should be centrally located in the vessel, with the height C of the impeller 2 off the bottom of the vessel 13 between 0.125 and l.û times the diameter of the impeller for flat bottomed vessels. Best results are obtained when the impeller is between 0.25D and 0.5D from the bottom of the vessel. The liquidheight h above the impeller should be between 1.0 and 2.0 times the diameter of the impeller. The total liquid height (H=[h+C+W]), should be from 1.5 to 3.0 times the diameter of the impeller.
Baffles 14 with width B equal to 0.1 to 0.12 times the characteristic length T of the vessel 13 should be used to prevent vortexing of the liquid in the vessel. From 1 to 4 baffles should be used, with maximum performance (and maxirnum power consumption) being obtained when using 4 baffles. For cylindrical vessels, the baffles should be attached to the wall of the vessel at 90 degree intervals. For square or rectangular vessels the baffles should be positioned in the centre of each wali. For the purposes of determining the baMe width B in 2~3~0~
rectangular vessels the baffles width should be 0.1 to 0.12 times the smallest of the length I or width w.
The rotary gas injector can be used in vessels, which are neither round, square, or rectangular, without departing from the spirit of this invention.
S Baffles should be used regardless of the shape of the vessel.
The use of the present invention is described in the following examples. These examples are purely illustrative and should not restrict the applicability of the present invention.
Example 1:
A rotary gas injector was operated in a square plexiglass vessel, containing 141 L of water. Initially, 0.33 KgmoVm3 of sodium sulphite (Na2SO3) was dissolved in the water. The impeller was located at the centre of the tank, perpendicular to the bottom, and was rotated at 320 revolutions per minute. Air at 25 Deg C was injected at a rate equivalent to 250 L/min at standard temperature and pressure (S.T.P. or 1 atm and 0 Deg C) down the bore in the shaft, passing through the centre of the impeller, and exiting a 15.9 mm diameter hole located in the bottom of the impeller. A small amount (103 M) of copper sulphate was added to the solution to catalyse the sulphite oxidation reaction which is given below:
S3(aq) + 0 5 2(aq) = So4(aq) (l) It is well known as disclosed in the following references:
1) Cooper, C.M., Fernstrom, G.A., Miller, S.A., "Gas-Liquid Contactors,"
2 0 ~ ~ r, ~ ~ .
Industrial and Engineering Chemistry, Vol. 36, No. 6, p504-509, 1944.
2) Linek, V., Vacek, V., "Chemical Engineering Use of Catalyzed Sulphite Oxidation Kinetics For The Determination of Mass Transfer Characteristics of Gas-Liquid Contactors," Chemical Engineering Science, Vol. 36, No. 11, pl747-1768, Gt. Br., 1981. Example 2:
that the addition of copper sulphate increases the oxidation rate of sulphite, such that the reaction rate becomes limited by the rate of oxygen mass transport into the water. The rate of reaction can then be described by the following equation:
~ ( CNa2SO3) k ( ~ ) (i) where: kL is the liquid phase mass transfer coefficient (m/h), a is the gas liquid interfacial area (m2Jm3), C' is the solubility of oxygen in water (KgmoVm3), Cb is the actual buLk concentration of oxygen in the water (negligibly small).
The rate of reaction (1) is therefore independent of the sulphite concentration and linearly dependant on time {for constant gas flow and impeller speed). For a fixed mass transport coefficient, the reaction rate is directly proportional to the gas-liquid interfacial area. The increase in the rate of sulphite oxidation due to agitation, is then directly indicative of the increase in the gas surface area per liquid volume.
The dimensions of this system are given in Table 1.
9 2 ~ ~ ~ 9 Q ~
Table 1 Impeller Parameter Value diameter, D 229 mm thickness, W 114 mm cut size, db 42.9 mm height off bottom, C 114 mm rotation rate 320 r.p.m.
Shaft diameter, S 38.1 mm bore diameter, Sb 6.4 mm Vessel characteristic dimension, T 521 mm liquid depth, H 521 mm The concentration of dissolved sodium sulphite has been plotted as a function oftime in Figure 4. The rate of change of the concentration is linear with time, indicating that the reaction rate (slope) is constant at 0.483 Kgmol of Na2SO3 reacting per m3 of water per hour.
Example 2:
In this exarnple, the gas outlet hole in the impeller of example 1 was - :
.
:
::
2Q7s~3~3~3~
plugged. New gas outlets with a diameter of 6.4 mm were created between the impeller blades in accordance with the present invention. The procedure used in example 1 was again followed. Air was injected at a rate equivalent to 250 L/min@ S.T.P., and the impeller was rotated at 320 r.p.m.. The initial sulphite S concentration was 0.32 Kgmol/m3. Over 31 minutes, 5.280 Kg of sodium sulphite were reacted. The new sulphite oxidation rate was 0.575 KgmoVm3/h, and was 19 percent higher than the oxidation rate in example 1. The only change from example 1 to example 2 was the change in the location of the gas outlet. It can therefore be concluded that gas injection between the impeller blades increases the gas-liquid interfacial area available for mass-transfer.
Example 3:
The effect of impeller thickness to diameter ratio (W/D ratio) is illustrated the following examples. In this example the reaction rate in a gas-liquid-solid system is accelerated using the rotary gas injector of this invention with an impeller W/D ratio of 0.26. A 51:49 mixture of chlorine (Cl2) and carbon monoxide (CO) was injected using the rotary gas injector at a total gas ilow rate equivalent to 57.9 L/min @ S.T.P.. This gas mixture reacted with solid magnesium oxide (MgO) particles of approximately 20 micron size, in a molten bath of magnesium chloride (MgC12). The products of the reaction where carbon dioxide (CO2) and MgC12, as shown below:
Cl2(g) + CO~g~ + MgO(s~ = MgCl2(,) + CO2(g) (2) Since chlorine is extremely reac~ive with metals at the temperature of the reaction (820 C) both the square vessel, and rotary gas injector were fabricated from graphite. The physical parameters describing the present example are given in Table 2.
Table: 2 Impeller Parameter Value diameter, (D) 146 mm thickness, (W) 38.1 mm hole size, (do) 6.4 mm cut size, (db) 22.2 mm height from bottom of vessel, (C) 19 mm rotation rate 551 r.p.m.
Shaft diameter, (S) 57 mm bore diameter, (Sb) 6.4 mm Vessel characteristic dimension, (T) 292 mm liquid depth, (H) 297 mm 4 baffles, (B) 29.2 mm ~ ,.
Reaction (2) had been found previously to proceed at a ne2gl~g71b~e rate (<O.lKgmol/m3/h) using a lance type injector in the absence of a catalyst. Usingthe rotary gas injector, the MgO content of the MgCI2 bath was reduced linearly with time from 6.1 weight percent to 0.57 weight percent over 150 minutes. The rate of reaction (2) was then calculated to be 1.0~ Kgmol of MgO per m3 of liquid MgCI2 per hour. The change in the rate of reaction with agitation is due to the increase in gas-liquid area available for mass transfer of the gaseous reagents into the liquid MgC12.
Example 4:
As in the previous example, a rotary injector fabricated from graphite was used to inject chlorine and carbon monoxide into a molten bath of MgCI2. Initially the bath contained 3.3 weight percent MgO. The injector was rotated at 554 r.p.m.
and a 48:52 mixture of chlorine and carbon monoxide was injected at a rate equivalent to 60.8 L/min @ S.T.P.. The impeller had a W/D ratio of 0.52 (twice that of the impeller used in the previous example). All other physical parameters were identical to those given in Table 2. The MgO content of the vessel has beenplotted as a function of time in Figure 5. The observed rate of MgO chlorinationwas 1.44 Kgmol of MgO per m3 of liquid MgCl2 per hour. Therefore the rate of reaction (2) was increased by 32 percent by increasing the W/D ratio of the impeller from 0.26 to 0.52. As shown in Figure 5 the reaction rate is independent of the MgO content at MgO concentrations above about 0.1 weight percent MgO
in the MgC1~.
In some processes used for hydrogen removal from aluminum, an inert gas is injected using a rotary gas injector consisting of a graphite shaft and impeller. The gas is injected through an internal cavity in the graphite shaft and impeller, exiting either above or below the impeller. For the gas to be sheared into small bubbles the injected gas must be drawn into the low pressure zones createdbehind the impeller blades (relative to the direction of rotation). Depending on the impeller rotational speed and the gas injection rate, some gas may bypass the impeller and not be sheared and dispersed. This is not an efficient mode of operation.
Summary of ~e Invention:
The present invention provides an improved design for a rotary gas injector fabricated from graphite. This injector consists of an impeller attached to a hollow cylindrical shaft having a central bore. The impeller is cylindrical inshape and has a plurality of cuts equally spaced around the circumference thereof to define blades for the impeller. Radial holes are drilled in the centre of the cuts 2 ~ ~ 3 ,~ f.~ l3 and communicate with the central bore of the shaft.
When the shaft is rotated at sufficient speed and gas is injected through the shaft, exiting between the blades of the impeller through the radialholes, fine bubbles are formed by the shearing action of the blades. These fine bubbles serve to enhance gas-liquid mass transfer and chemical reaction in gas-liquid and gas-liquid-solid systems. The performance (total gas-liquid interfacial area per unit liquid volume) of the impeller can be measured as via the total rate of mass transfer or chemical reaction (for mass transfer limited reactions).
Short Description of the Drawings:
The present invention will now be described by way of example, with reference to the accompanying drawings in which:
Figures la and lb are drawings of one embodiment of the impeller of the rotary gas injector of the present invention;
Figure 2 is a drawing of the shaft of the rotary gas injector;
Figure 3 is a schematic drawing of the lay-out of the rotary gas injector;
Figure 4 is a plot of sodium sulphite concentration against time; and Figure S is a plot of solid magnesium oxide content against time.
Detailed Descripffon of the Invention:
Referring to Figures 1 through 3, the rotary gas injector 1 consists of an impeller 2 with diameter D, attached to a hollow cylindrical shaft 3 of diameter S. The impeller of the gas injector is cylindrical in shape, with the 4 2Q7390~
thickness W to diaMeter D ratio typically being between 0.2 and 1Ø In chemicalengineering applications for gas dispersion most impellers have a W/D ratio of 0.2 or less. It was found that increasing the impeller thickness to a W/D over 0.2 greatly improved gas dispersion at the expense of higher power consumption for agiven impeller speed. A practical limit exists on the thickness of the impeller because of the impeller weight and the strength of the graphite construction material. The impeller is fabricated with a series of U-shaped cuts 4 equally spaced around the circumference thereof, such that the width of the cut opening is equal to twice the radius of the curved end of the U. The width db of the U-shaped cuts 4 is between 0.12 and 0.20 of the diameter D of the impeller 2. The number of cuts can vary from 6 to 12 and is typically 9. The curved edges of the impeller remaining between these cuts, act as blades 5 of the impeller 2. Holes 6 with diameter do are drilled in the centre of each cut, located at height dc between 1/4 and 1/2 times the width W of the impeller, and preferably 1/3 the width of the impeller from the bottom of the impeller. The hole diameter do should be from 0.05 to 0.03 times the diameter D of the impeller. When the shaft 3 is rotated at sufficient speed and gas is injected through a bore 7 of diameter Sb centrally located in the shaft 3, entering a windbox 8 of diameter Sw, inside the impeller 2, and exiting between the blades of the impeller, through holes 6, fine bubbles 9 are formed by the shearing action of the blades.
The shaft 3 should be constructed of graphite of a grade identical to that used in the fabrication of the impeller. The diameter of the shaft, should be 5 2~73~08 from 0.17 to 0.425 times the iMpeller diameter, and preferably from 0.300 to 0.375.
The shaft length can be determined by the skilled practitioner based on the known properties of graphite and the special requirements of the intended application. The diameter Sb of the centrally located bore 7 can be made of uniform dimension along the length of the shaft or can vary. The maximum bore diameter Sb should not exceed 1/3 of the shaft diameter to insure the mechanical integrity of the shaft. The skilled practitioner can couple the top portion 10 of the shaft 3 to any suitable drive mechanism, insuring that the shaft turns true and that provision for gas injection is given in the drive mechanism. The bottom portion of the shaft should be threaded11 such that the shaft and impeller can be coupled together. The diameter of thethread 11 should be as standard size and preferably equal to the shaft diameter.The length t of the thread 11 should be between 0.25 and 0.3 of the diameter of the impeller. I~or a clockwise rotation, the thread 11 should be right hand, while a left hand thread 11 should be used for counterclockwise rotation of the gas injector.The impeller should be equipped with a threaded hole 12 such that the shaft 3 can be coupled to the impeller. The diameter dc of the hole 12 should be such that afemale thread matching the thread 11 on the shaft can be machined into the hole 12. The depth of the hole 12 should be incrementally less than the length t of the threaded portion 11 of the shaft. A hole should be drilled at the bottom of the threaded hole 12 to meet the radial holes 6 at the centre of the impeller, forming the windbox 8. The diameter Sw of the windbox 8 should be from 0.5 to 1.5 times the diarneter Sb of the bore 7 in the shaft 3, and preferably of identical diameter.
2 ~ 3 ~
The performance of the rotary gas injector is maximi~ed when it is used in a vessel 13 of proper dimensions. Best results are obtained when the ratio of the impeller diameter to the characteristic transverse length T of the vessel 13 is between 0.25 and 0.5, and particularly between 0.3 and 0.4. For cylindrical vessels the characteristic length T is the diameter, while for square vessels the characteristic length, is the length of one side. If a rectangular vessel is used both the length 1 to diameter D and width w to diameter D ratios, should be between 0.25 and O.S.
The impeller should be centrally located in the vessel, with the height C of the impeller 2 off the bottom of the vessel 13 between 0.125 and l.û times the diameter of the impeller for flat bottomed vessels. Best results are obtained when the impeller is between 0.25D and 0.5D from the bottom of the vessel. The liquidheight h above the impeller should be between 1.0 and 2.0 times the diameter of the impeller. The total liquid height (H=[h+C+W]), should be from 1.5 to 3.0 times the diameter of the impeller.
Baffles 14 with width B equal to 0.1 to 0.12 times the characteristic length T of the vessel 13 should be used to prevent vortexing of the liquid in the vessel. From 1 to 4 baffles should be used, with maximum performance (and maxirnum power consumption) being obtained when using 4 baffles. For cylindrical vessels, the baffles should be attached to the wall of the vessel at 90 degree intervals. For square or rectangular vessels the baffles should be positioned in the centre of each wali. For the purposes of determining the baMe width B in 2~3~0~
rectangular vessels the baffles width should be 0.1 to 0.12 times the smallest of the length I or width w.
The rotary gas injector can be used in vessels, which are neither round, square, or rectangular, without departing from the spirit of this invention.
S Baffles should be used regardless of the shape of the vessel.
The use of the present invention is described in the following examples. These examples are purely illustrative and should not restrict the applicability of the present invention.
Example 1:
A rotary gas injector was operated in a square plexiglass vessel, containing 141 L of water. Initially, 0.33 KgmoVm3 of sodium sulphite (Na2SO3) was dissolved in the water. The impeller was located at the centre of the tank, perpendicular to the bottom, and was rotated at 320 revolutions per minute. Air at 25 Deg C was injected at a rate equivalent to 250 L/min at standard temperature and pressure (S.T.P. or 1 atm and 0 Deg C) down the bore in the shaft, passing through the centre of the impeller, and exiting a 15.9 mm diameter hole located in the bottom of the impeller. A small amount (103 M) of copper sulphate was added to the solution to catalyse the sulphite oxidation reaction which is given below:
S3(aq) + 0 5 2(aq) = So4(aq) (l) It is well known as disclosed in the following references:
1) Cooper, C.M., Fernstrom, G.A., Miller, S.A., "Gas-Liquid Contactors,"
2 0 ~ ~ r, ~ ~ .
Industrial and Engineering Chemistry, Vol. 36, No. 6, p504-509, 1944.
2) Linek, V., Vacek, V., "Chemical Engineering Use of Catalyzed Sulphite Oxidation Kinetics For The Determination of Mass Transfer Characteristics of Gas-Liquid Contactors," Chemical Engineering Science, Vol. 36, No. 11, pl747-1768, Gt. Br., 1981. Example 2:
that the addition of copper sulphate increases the oxidation rate of sulphite, such that the reaction rate becomes limited by the rate of oxygen mass transport into the water. The rate of reaction can then be described by the following equation:
~ ( CNa2SO3) k ( ~ ) (i) where: kL is the liquid phase mass transfer coefficient (m/h), a is the gas liquid interfacial area (m2Jm3), C' is the solubility of oxygen in water (KgmoVm3), Cb is the actual buLk concentration of oxygen in the water (negligibly small).
The rate of reaction (1) is therefore independent of the sulphite concentration and linearly dependant on time {for constant gas flow and impeller speed). For a fixed mass transport coefficient, the reaction rate is directly proportional to the gas-liquid interfacial area. The increase in the rate of sulphite oxidation due to agitation, is then directly indicative of the increase in the gas surface area per liquid volume.
The dimensions of this system are given in Table 1.
9 2 ~ ~ ~ 9 Q ~
Table 1 Impeller Parameter Value diameter, D 229 mm thickness, W 114 mm cut size, db 42.9 mm height off bottom, C 114 mm rotation rate 320 r.p.m.
Shaft diameter, S 38.1 mm bore diameter, Sb 6.4 mm Vessel characteristic dimension, T 521 mm liquid depth, H 521 mm The concentration of dissolved sodium sulphite has been plotted as a function oftime in Figure 4. The rate of change of the concentration is linear with time, indicating that the reaction rate (slope) is constant at 0.483 Kgmol of Na2SO3 reacting per m3 of water per hour.
Example 2:
In this exarnple, the gas outlet hole in the impeller of example 1 was - :
.
:
::
2Q7s~3~3~3~
plugged. New gas outlets with a diameter of 6.4 mm were created between the impeller blades in accordance with the present invention. The procedure used in example 1 was again followed. Air was injected at a rate equivalent to 250 L/min@ S.T.P., and the impeller was rotated at 320 r.p.m.. The initial sulphite S concentration was 0.32 Kgmol/m3. Over 31 minutes, 5.280 Kg of sodium sulphite were reacted. The new sulphite oxidation rate was 0.575 KgmoVm3/h, and was 19 percent higher than the oxidation rate in example 1. The only change from example 1 to example 2 was the change in the location of the gas outlet. It can therefore be concluded that gas injection between the impeller blades increases the gas-liquid interfacial area available for mass-transfer.
Example 3:
The effect of impeller thickness to diameter ratio (W/D ratio) is illustrated the following examples. In this example the reaction rate in a gas-liquid-solid system is accelerated using the rotary gas injector of this invention with an impeller W/D ratio of 0.26. A 51:49 mixture of chlorine (Cl2) and carbon monoxide (CO) was injected using the rotary gas injector at a total gas ilow rate equivalent to 57.9 L/min @ S.T.P.. This gas mixture reacted with solid magnesium oxide (MgO) particles of approximately 20 micron size, in a molten bath of magnesium chloride (MgC12). The products of the reaction where carbon dioxide (CO2) and MgC12, as shown below:
Cl2(g) + CO~g~ + MgO(s~ = MgCl2(,) + CO2(g) (2) Since chlorine is extremely reac~ive with metals at the temperature of the reaction (820 C) both the square vessel, and rotary gas injector were fabricated from graphite. The physical parameters describing the present example are given in Table 2.
Table: 2 Impeller Parameter Value diameter, (D) 146 mm thickness, (W) 38.1 mm hole size, (do) 6.4 mm cut size, (db) 22.2 mm height from bottom of vessel, (C) 19 mm rotation rate 551 r.p.m.
Shaft diameter, (S) 57 mm bore diameter, (Sb) 6.4 mm Vessel characteristic dimension, (T) 292 mm liquid depth, (H) 297 mm 4 baffles, (B) 29.2 mm ~ ,.
Reaction (2) had been found previously to proceed at a ne2gl~g71b~e rate (<O.lKgmol/m3/h) using a lance type injector in the absence of a catalyst. Usingthe rotary gas injector, the MgO content of the MgCI2 bath was reduced linearly with time from 6.1 weight percent to 0.57 weight percent over 150 minutes. The rate of reaction (2) was then calculated to be 1.0~ Kgmol of MgO per m3 of liquid MgCI2 per hour. The change in the rate of reaction with agitation is due to the increase in gas-liquid area available for mass transfer of the gaseous reagents into the liquid MgC12.
Example 4:
As in the previous example, a rotary injector fabricated from graphite was used to inject chlorine and carbon monoxide into a molten bath of MgCI2. Initially the bath contained 3.3 weight percent MgO. The injector was rotated at 554 r.p.m.
and a 48:52 mixture of chlorine and carbon monoxide was injected at a rate equivalent to 60.8 L/min @ S.T.P.. The impeller had a W/D ratio of 0.52 (twice that of the impeller used in the previous example). All other physical parameters were identical to those given in Table 2. The MgO content of the vessel has beenplotted as a function of time in Figure 5. The observed rate of MgO chlorinationwas 1.44 Kgmol of MgO per m3 of liquid MgCl2 per hour. Therefore the rate of reaction (2) was increased by 32 percent by increasing the W/D ratio of the impeller from 0.26 to 0.52. As shown in Figure 5 the reaction rate is independent of the MgO content at MgO concentrations above about 0.1 weight percent MgO
in the MgC1~.
Claims (11)
1. A rotary gas injector comprising a graphite impeller attached to the end of a hollow cylindrical graphite shaft having a central bore, said impeller being cylindrical in shape and having a plurality of U-shaped cuts equally spaced around the circumference thereof to define blades for the impeller, and radial holes drilled in the centre of the cuts and communicating with the central bore of the shaft, whereby gas may be injected through the bore in the shaft and the radial holes of the impeller and be sheared by the blades to form fine bubbles to enhance gas liquid mass transfer and chemical reaction in gas-liquid and gas-liquid-solid systems.
2. A rotary gas injector according to claim 1, wherein the thickness W to diameter D ratio W/D of the impeller is between 0.2 and 1Ø
3. A rotary gas injector according to claim 1, wherein the width of the cuts is between 0.12 and 0.20 of the diameter of the impeller.
4. A rotary gas injector according to claim 1 or 3, wherein the number of cuts vary from 6 to 12.
5. A rotary gas injector according to claim 4 wherein the number of cuts is 9.
6. A rotary gas injector according to claim 1 wherein the diameter of the radial holes is from 0.05 to 0.03 times the diameter of the impeller.
7. A rotary gas injector according to claim 1 wherein the injector is centrally located in a vessel which can be of any shape selected from round, square or rectangular.
8. A rotary gas injector according to claim 7, wherein the ratio of the diameter of the impeller to the characteristic transverse length of the vessel is between 0.25 and 0.5.
9. A rotary gas injector according to claim 2, wherein the height of the impeller from the bottom of the vessel is between 0.125 and 1.0 times the diameter of the impeller.
10. A rotary gas injector according to claim 2, wherein the liquid height above the impeller is between 1.0 and 2.0 times diameter of the impeller.
11. A rotary gas injector according to claim 7, wherein vertical baffles are located around the inside wall of the vessel to prevent vortexing of the liquid in the vessel.
Priority Applications (5)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA002073908A CA2073908A1 (en) | 1992-07-16 | 1992-07-16 | Rotary gas injector |
| PCT/CA1993/000273 WO1994002234A1 (en) | 1992-07-16 | 1993-07-14 | Rotary gas injector |
| IL106341A IL106341A0 (en) | 1992-07-16 | 1993-07-14 | Rotary gas injector |
| AU45538/93A AU4553893A (en) | 1992-07-16 | 1993-07-14 | Rotary gas injector |
| CN93116554A CN1084429A (en) | 1992-07-16 | 1993-07-16 | Rotary gas injector |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA002073908A CA2073908A1 (en) | 1992-07-16 | 1992-07-16 | Rotary gas injector |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA2073908A1 true CA2073908A1 (en) | 1994-01-17 |
Family
ID=4150159
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA002073908A Abandoned CA2073908A1 (en) | 1992-07-16 | 1992-07-16 | Rotary gas injector |
Country Status (5)
| Country | Link |
|---|---|
| CN (1) | CN1084429A (en) |
| AU (1) | AU4553893A (en) |
| CA (1) | CA2073908A1 (en) |
| IL (1) | IL106341A0 (en) |
| WO (1) | WO1994002234A1 (en) |
Families Citing this family (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CA2177151A1 (en) * | 1993-11-26 | 1995-06-01 | Gaetano Russo | Chemical waste treatment |
| DE19620040C2 (en) * | 1996-05-17 | 1998-06-10 | Suedmo Schleicher Ag | Method and device for introducing a gas into a liquid |
| CN103611462B (en) * | 2013-12-18 | 2016-01-13 | 上海弗鲁克科技发展有限公司 | Honeycombed agitator |
| US9687773B2 (en) | 2014-04-30 | 2017-06-27 | Honeywell International Inc. | Fuel deoxygenation and fuel tank inerting system and method |
| US9656187B2 (en) | 2014-11-12 | 2017-05-23 | Honeywell International Inc. | Fuel deoxygenation system contactor-separator |
| US9834315B2 (en) | 2014-12-15 | 2017-12-05 | Honeywell International Inc. | Aircraft fuel deoxygenation system |
| US9897054B2 (en) | 2015-01-15 | 2018-02-20 | Honeywell International Inc. | Centrifugal fuel pump with variable pressure control |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| NO142830C (en) * | 1978-02-28 | 1980-10-29 | Trondhjems Mek Verksted As | DEVICE FOR DISTRIBUTING A GAS IN A FLUID MEDIUM |
| CA1135180A (en) * | 1979-03-30 | 1982-11-09 | Charles B. Donaldson | Apparatus and method for producing a gas in liquid dispersion |
| JPS60200923A (en) * | 1984-03-23 | 1985-10-11 | Showa Alum Corp | Device for fining and dispersing foam |
-
1992
- 1992-07-16 CA CA002073908A patent/CA2073908A1/en not_active Abandoned
-
1993
- 1993-07-14 WO PCT/CA1993/000273 patent/WO1994002234A1/en active Application Filing
- 1993-07-14 AU AU45538/93A patent/AU4553893A/en not_active Abandoned
- 1993-07-14 IL IL106341A patent/IL106341A0/en unknown
- 1993-07-16 CN CN93116554A patent/CN1084429A/en active Pending
Also Published As
| Publication number | Publication date |
|---|---|
| CN1084429A (en) | 1994-03-30 |
| WO1994002234A1 (en) | 1994-02-03 |
| AU4553893A (en) | 1994-02-14 |
| IL106341A0 (en) | 1993-11-15 |
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