WO1994002234A1 - Injecteur de gaz rotatif - Google Patents

Injecteur de gaz rotatif Download PDF

Info

Publication number
WO1994002234A1
WO1994002234A1 PCT/CA1993/000273 CA9300273W WO9402234A1 WO 1994002234 A1 WO1994002234 A1 WO 1994002234A1 CA 9300273 W CA9300273 W CA 9300273W WO 9402234 A1 WO9402234 A1 WO 9402234A1
Authority
WO
WIPO (PCT)
Prior art keywords
impeller
diameter
gas injector
liquid
gas
Prior art date
Application number
PCT/CA1993/000273
Other languages
English (en)
Inventor
Mark W. Kennedy
John G. Lenz
Earle E. Chin
Original Assignee
Noranda Inc.
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Noranda Inc. filed Critical Noranda Inc.
Priority to AU45538/93A priority Critical patent/AU4553893A/en
Publication of WO1994002234A1 publication Critical patent/WO1994002234A1/fr

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

Definitions

  • This invention relates to a rotary gas injector for 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 phases such 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.
  • 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.
  • the injected gas must be drawn into the low pressure zones created behind the impeller blades (relative to the direction of rotation).
  • some gas may bypass the impeller and not be sheared and dispersed. This is not an efficient mode of operation.
  • 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 in shape 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 and communicate with the central bore of the shaft.
  • 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
  • FIG. 5 is a plot of solid magnesium oxide content against time.
  • 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 thickness W to diameter D ratio typically being between 0.2 and 1.0. In chemical engineering applications for gas dispersion most impellers have a W/D ratio of 0.2
  • the width d b 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.
  • Holes 6 with diameter d 0 are drilled in the centre of each cut, located at height d c 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 d 0 should be from
  • the shaft 3 should be constructed of graphite of a grade identical to
  • 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 S b 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 S nominal 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 threaded 11 such that the shaft and impeller can be coupled together.
  • the diameter of the thread 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.
  • the thread 11 For 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 d c of the hole 12 should be such that a female 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 S w of the windbox 8 should be from 0.5 to 1.5 times the diameter S b of the bore 7 in the shaft 3, and preferably of identical diameter.
  • the performance of the rotary gas injector is maximized when it is used in a vessel 13 of proper dimensions. Best results are obtained when the ratio
  • 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
  • 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 1.0 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 liquid height h above the impeller should be between 1.0 and 2.0 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 maximum power consumption) being obtained when using 4 baffles.
  • the 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 wall. For the purposes of determining the baffle width B in , consider acute pressure_, date, 02234
  • the baffles width should be 0.1 to 0.12 times the smallest of the length 1 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. Baffles should be used regardless of the shape of the vessel.
  • Example 1 A rotary gas injector was operated in a square plexiglass vessel, containing
  • k L is the liquid phase mass transfer coefficient (m/h)
  • a is the gas liquid interfacial area (m 2 /m 3 )
  • C * is the solubility of oxygen in water (Kgmol m 3 )
  • C b is the actual bulk concentration of oxygen in the water (negligibly small).
  • P. rate of reaction (1) is therefore independent of the sulphite concentration and early dependant on time (for constant gas flow and impeller speed).
  • 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.
  • Impeller Parameter Value diameter D 229 mm thickness, W 114 mm cut size, d b 42.9 mm height off bottom, C 114 mm rotation rate 320 r.p.m.
  • the gas outlet hole in the impeller of example 1 was 234
  • impeller thickness to diameter ratio (W/D ratio) is illustrated the following examples.
  • 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 (Cl 2 ) and carbon monoxide (CO) was injected using the rotary gas injector at a total gas flow 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 (MgCl 2 ).
  • MgO solid magnesium oxide
  • MgCl 2 molten bath of magnesium chloride
  • Impeller Parameter Value diameter (D) 146 mm thickness, (W) 38.1 mm hole size, (d 0 ) 6.4 mm
  • the MgO content of the MgCl 2 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 1.09 Kgmol of MgO per m 3 of liquid
  • 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 MgCl 2 . 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 IJmin @ 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 been plotted as a function of time in Figure 5.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)

Abstract

Un injecteur de gaz rotatif comprend une roue en graphite fixée à l'extrémité d'un arbre en graphite cylindrique creux à alésage central. La roue est de forme cylindryque et possède une pluralité de découpures espacées régulièrement autour de sa circonférence pour former les pales de la roue, et des trous radiaux sont percés dans le centre des découpures et communiquent avec l'alésage central de l'arbre. Les gaz sont injectés dans l'alésage de l'arbre et les trous radiaux de la roue et sont cisaillés par les pales pour former de fines bulles afin d'améliorer le transfert de matière et la réaction chimique dans les systèmes gaz-liquides et gaz-liquides-solides.
PCT/CA1993/000273 1992-07-16 1993-07-14 Injecteur de gaz rotatif WO1994002234A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AU45538/93A AU4553893A (en) 1992-07-16 1993-07-14 Rotary gas injector

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
CA2,073,908 1992-07-16
CA002073908A CA2073908A1 (fr) 1992-07-16 1992-07-16 Injecteur de gaz rotatif

Publications (1)

Publication Number Publication Date
WO1994002234A1 true WO1994002234A1 (fr) 1994-02-03

Family

ID=4150159

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/CA1993/000273 WO1994002234A1 (fr) 1992-07-16 1993-07-14 Injecteur de gaz rotatif

Country Status (5)

Country Link
CN (1) CN1084429A (fr)
AU (1) AU4553893A (fr)
CA (1) CA2073908A1 (fr)
IL (1) IL106341A0 (fr)
WO (1) WO1994002234A1 (fr)

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1995014526A1 (fr) * 1993-11-26 1995-06-01 Hyperno Proprietary Limited Traitement chimique des dechets
DE19620040A1 (de) * 1996-05-17 1997-11-20 Suedmo Schleicher Ag Verfahren und Vorrichtung zum Eintragen von Gas in eine Flüssigkeit
US9656187B2 (en) 2014-11-12 2017-05-23 Honeywell International Inc. Fuel deoxygenation system contactor-separator
US9687773B2 (en) 2014-04-30 2017-06-27 Honeywell International Inc. Fuel deoxygenation and fuel tank inerting system and method
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

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103611462B (zh) * 2013-12-18 2016-01-13 上海弗鲁克科技发展有限公司 蜂窝形搅拌器

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0017451A1 (fr) * 1979-03-30 1980-10-15 Chemineer Inc. Dispositif et procédé pour la production d'une dispersion de gaz dans un liquide
US4283357A (en) * 1978-02-28 1981-08-11 Trodhjems Mek. Versted A/S Device for distribution of a gas in a liquid medium
US4611790A (en) * 1984-03-23 1986-09-16 Showa Aluminum Corporation Device for releasing and diffusing bubbles into liquid

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4283357A (en) * 1978-02-28 1981-08-11 Trodhjems Mek. Versted A/S Device for distribution of a gas in a liquid medium
EP0017451A1 (fr) * 1979-03-30 1980-10-15 Chemineer Inc. Dispositif et procédé pour la production d'une dispersion de gaz dans un liquide
US4611790A (en) * 1984-03-23 1986-09-16 Showa Aluminum Corporation Device for releasing and diffusing bubbles into liquid

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1995014526A1 (fr) * 1993-11-26 1995-06-01 Hyperno Proprietary Limited Traitement chimique des dechets
US6033576A (en) * 1993-11-26 2000-03-07 Hyperno Proprietary Limited Chemical waste treatment
DE19620040A1 (de) * 1996-05-17 1997-11-20 Suedmo Schleicher Ag Verfahren und Vorrichtung zum Eintragen von Gas in eine Flüssigkeit
DE19620040C2 (de) * 1996-05-17 1998-06-10 Suedmo Schleicher Ag Verfahren und Vorrichtung zum Eintragen eines Gases in eine Flüssigkeit
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

Also Published As

Publication number Publication date
IL106341A0 (en) 1993-11-15
CN1084429A (zh) 1994-03-30
CA2073908A1 (fr) 1994-01-17
AU4553893A (en) 1994-02-14

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