EP0367799A1 - Device for dispersing gas within a liquid phase - Google Patents
Device for dispersing gas within a liquid phaseInfo
- Publication number
- EP0367799A1 EP0367799A1 EP88910055A EP88910055A EP0367799A1 EP 0367799 A1 EP0367799 A1 EP 0367799A1 EP 88910055 A EP88910055 A EP 88910055A EP 88910055 A EP88910055 A EP 88910055A EP 0367799 A1 EP0367799 A1 EP 0367799A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- liquid phase
- chimney
- gas
- lining
- phase
- 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.)
- Granted
Links
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
- B01F25/20—Jet mixers, i.e. mixers using high-speed fluid streams
- B01F25/21—Jet mixers, i.e. mixers using high-speed fluid streams with submerged injectors, e.g. nozzles, for injecting high-pressure jets into a large volume or into mixing chambers
-
- 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
- B01F23/40—Mixing liquids with liquids; Emulsifying
- B01F23/45—Mixing liquids with liquids; Emulsifying using flow mixing
- B01F23/454—Mixing liquids with liquids; Emulsifying using flow mixing by injecting a mixture of liquid and gas
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
- B01F25/30—Injector mixers
- B01F25/31—Injector mixers in conduits or tubes through which the main component flows
- B01F25/312—Injector mixers in conduits or tubes through which the main component flows with Venturi elements; Details thereof
-
- 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F33/00—Other mixers; Mixing plants; Combinations of mixers
- B01F33/80—Mixing plants; Combinations of mixers
- B01F33/81—Combinations of similar mixers, e.g. with rotary stirring devices in two or more receptacles
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
- Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10S261/00—Gas and liquid contact apparatus
- Y10S261/75—Flowing liquid aspirates gas
Definitions
- the present invention relates to a device allowing the transfer of a gaseous phase into a liquid phase, the addition of the gaseous phase being intended to ensure the course of reactions which have to develop subsequently in the liquid phase.
- This device is mainly intended for carrying out treatments such as. chemical, biological and metabolic reactions comprising the transfer of a gaseous phase into a liquid phase, this liquid phase possibly being industrial or domestic water.
- the transfer coefficient in seconds minus one This coefficient is defined as that which links the rate of variation of concentration to the difference between this concentration and the concentration corresponding to that of saturation of the gas phase in the liquid phase.
- the devices usually used have specific gross inputs generally between 0.8 and 1.8 kilograms of oxygen per kilowatt hour.
- a study carried out by WANG and AL in 1978 and published in Chem. Eng. Sci. , 33, 945 in 1978 showed that transfer coefficients of up to 0.22 seconds minus one could be obtained using bubble columns equipped with static mixers for liquid and gas velocities of 0.17 respectively meter per second and 0.25 meter per second.
- the more usual devices that are the classic venturi or the porous diffuser make it possible to obtain transfer coefficients generally between 0.06 and 0.13 seconds minus one.
- the device comprises a device for dispersing a gaseous phase in a liquid phase comprising at least one venturi ejector composed of a convergent for the inlet of the liquid, a neck for the inlet of the gas and a divergent characterized in that the divergent is extended by a chimney of diameter equal to or greater than that of the divergent and contiguous or not with it, the device being used in a substantially vertical position, and in that the flow of the liquid phase is descending.
- the device or devices are immersed in a basin or any other type of tank containing the liquid phase. This is introduced by a pump at the inlet of the convergent with an initial speed adapted to the venturi.
- the gaseous phase is introduced at the neck of the venturi and can, as the case may be, be sucked in by the liquid phase which then plays the role of motive fluid or introduced by the combined effect of the pressure due to a gas compressor and the suction due in the liquid phase.
- the divergent ensures a mixture between the two phases.
- the chimney placed at the outlet of the divergent considerably reinforces the effect of the venturi by ensuring a large contact area in a relatively confined space which makes it possible to obtain a much better gas / liquid transfer than by the methods currently known.
- this chimney it is possible to make this chimney so that its diameter is greater than the exit diameter of the divergent.
- the divergent and the chimney are no longer contiguous and the speed of the mixing in the said chimney causes the suction of part of the liquid phase in which the device bathes.
- an intermediate cylindrical connecting piece is interposed between the outlet of the divergent pipe and the inlet of the chimney. This intermediate part is pierced with lights connecting the interior of the chimney and the liquid phase in which the device is bathed.
- the speed of the liquid phase and gas phase mixture in the chimney causes the suction of part of the external liquid phase.
- the nature of the material or materials used to make the device has no influence on the effectiveness of the latter. It is the nature of the phases involved which will determine the materials to be used.
- the connections of the device to the various pipes can be of any type and in particular to be welded, to be glued, to flanges, and to be screwed.
- the venturi is calculated in such a way that the speed of the flow in the chimney ensures the gas bubbles which are subject to two influences: the upward flow of the mixture and the arched force, a low downward speed allowing the said bubbles to be dissolved as much as possible by the liquid phase.
- Tests carried out with the device which is the subject of the invention have led to results showing transfer coefficients of up to 0.35 seconds minus one, much higher than those obtained by the known devices and cited above.
- the device which is the subject of the invention can be used for all the processes requiring the transfer of a gaseous phase into a liquid phase, in particular for the treatment of industrial or domestic water, used or drinkable, in particular for aeration operations with air or enriched air, oxygenation, chlorination and ozonation.
- the devices can be associated in parallel, their number depending on the volume of liquid phase to be treated. Two or more devices can be connected in series, in particular when the absorption conditions of the gas phase in the liquid phase are difficult, that is to say when the solubility of the gas phase is low under the conditions provided for the treatment, or if a reaction occurs with consumption of the dissolved gas.
- Figure lb is a view, similar to that of Figure la, of a second embodiment
- FIG. 2 shows an example of implementation of the invention
- FIG. 4 gives several curves showing the variation of the oxygenation capacity of the devices of Figure 1 as a function of the specific power, established starting from results obtained partly by tests made by the inventors, partly by results coming from '' a study by the Technical Center of Rural Water and Forest Engineering (CEMAGREF) and published by the French Ministry of Agriculture in 1980.
- CEMAGREF Technical Center of Rural Water and Forest Engineering
- FIG. 5 to 7 each show a sectional view of a device according to a third embodiment of the invention.
- FIG. 8 is a view, similar to those of Figures 5 to 7, of a variant.
- FIG. 9 is a view of a packing element.
- the devices which are the subject of the invention and described by way of example have been determined to be used in a basin of 400 square meters in surface area and 2.5 meters in depth, the oxygen requirements of the liquid phase of which are 51 kilograms per hour.
- the device comprises a convergent 1 with an angle of about 40 degrees and a length of 127 millimeters.
- a cylindrical part 6 intended for connection of the piping bringing the liquid phase.
- the inlet diameter of the convergent 1 is equal to 114 millimeters.
- the neck 2 of the venturi After the convergent is the neck 2 of the venturi. It has a diameter of 25.4 millimeters and a length of 25.4 millimeters.
- the neck 2 has equidistant from its two ends a tap 7 projecting externally by 50.8 millimeters and intended for supplying the device by the gas phase.
- the diameter of this nozzle is 6 millimeters.
- the diameter is 8 millimeters.
- the neck 2 is followed by the divergent 3 forming an angle of 10 degrees. Its length is such that the outlet diameter either equal to the inlet diameter of the convergent, or 506 millimeters.
- a spacer 4 is inserted between the venturi and the chimney 5.
- its diameter is equal to 114 millimeters, its length to 114 millimeters.
- the intermediate piece is perforated by three lights presenting a maximum clearance compatible with its realization.
- the liquid phase is sent to the input of the devices 12 by means of a pump 9 and a supply ramp 10.
- the gaseous phase is sent to the neck of the devices 12 by the by means of a compressor .11 and a ramp 13.
- the basin has a capacity of 1000 cubic meters
- pump 9 has a flow rate of 2400 cubic meters per hour for a pressure of 1 bar
- compressor 11 has a flow rate 3.3 cubic meters per minute for a pressure of 0.4 bar.
- the installation is preferably equipped with 263 devices, each arranged substantially vertically. It provides an oxygenation capacity of 51 grams of oxygen per cubic meter per hour. The gross power required is 30 kilowatts, or a specific power of 30 watts per cubic meter.
- FIG. 3 makes it possible to compare the values of the transfer coefficients as a function of the speed of the liquid phase, namely 0.2624 meters per second by using the device which is the subject of the invention: curve 14 and the coefficients obtained using the devices already known: curves 15 (porous plateau), 16 (classic venturi), 17 (bubble column and static mixer).
- Curves 16 and 17 were obtained by WANG and A in 1978, the others experimentally by the inventors.
- E abscissa shows the surface gas velocities e meter per second, the ordinates show the transfer coefficients in seconds minus one.
- FIG. 4 makes it possible to compare the values of the oxygenation capacities as a function of the specific powers implemented by the devices which are the subject of the invention: curves 18 and 19 (flow rate of the liquid phase equal to 2.5 liters per second for curve 18, flow rate of the liquid phase equal to 5 liters per second for curve 19) and the coefficients obtained by the already known devices: curve 20 (maximum envelope curve of the statistical values relating to fast, slow turbines and brushes), 21
- 5 to 8 differ from those described above in that they further comprise a lining in the chimney which acts as a bubble breaker and thus prevents the coalescence of the gas bubbles.
- the device comprises a lining 30 arranged in the chimney 5.
- the lining is formed by two elements 32 and 34, each comprising a mesh structure 36 as shown in FIG. 9.
- the mesh structure 36 comprises two series of wires 38 arranged orthogonally forming square meshes which are either welded or entangled.
- the wires 38 can be, for example, of a material plastic, stainless steel or consist of plasticized metal wires.
- the first element 32 of the lining 30 is formed of a mesh structure 36 which is rolled up so that it takes on a substantially spiral shape.
- the second element 34 of the lining 30 is also formed of a mesh structure which is folded so as to have a substantially sawtooth section. Once folded, the grid structure is rolled up to take a shape corresponding to that of the first element.
- the two elements 32 and 34 are wound together. Once wound up, the lining 30 is mounted inside the chimney 5
- the device further comprises a means for retaining the lining 30 in place in the chimney 5.
- the devices represented in FIGS. 5 to 7 each comprise a different means for retaining the lining 30.
- the lining 30 is retained by a locking spring 40 which is substantially C-shaped and which has two arms, extremes 42 directed towards the center of C.
- the locking spring 40 is mounted around the outside of the chimney 5, the arms 42 passing through openings 44 formed in the chimney 5 to engage the meshes of the element 32.
- the locking spring 40 is retained in place between two flanges 46 which are each formed by folding back part of the sheet metal of the chimney 5.
- FIG. 6 differs from that of FIG. 5 in that the locking spring 40 'is mounted inside the chimney 5.
- the arms 42' are folded outwards and pass through openings 44 'formed in the chimney 5.
- a third opening 48 is formed in the chimney and allows a part 50 in the form of a loop of the spring 40 ′ to protrude outside the chimney 5.
- the locking spring 40 ′ is arranged in the chimney between the lining 30 and the outlet of the chimney 5.
- the lining 30 comprises two bayonets 52 which are welded to the meshes of the elements 32 and 34.
- the chimney 5 is provided with two L-shaped recesses 54 which are intended to receive the bayonets 52 thus locking the lining 30 in place .
- FIG. 8 A second embodiment of the lining 30 is shown in FIG. 8. This lining differs from that of FIGS. 5 to 7 in that the second element is formed of a mesh structure to which a wavy or substantially sinusoidal section has previously been given. .
- the axial length of the lining 30 is between 10 to 40% of the axial length of the chimney 5.
- the gas-liquid transfer is therefore improved, which leads to a reduction in the viscosity of the liquid due to the large amount of dissolved gas;
- the lining allows the free circulation of solid particles if the mesh is approximately 5 times larger than the diameter of the particles;
- the first element 32 of the lining 30, intended for use in a device having the dimensions given above, is preferably formed of square meshes having a side of 10 mm produced from a wire with a diameter of 0.25 to 0.5 mm.
- the length of each panel is 14.14 mm and the angle between two neighboring panels is 90 °.
- the wavelength of the corrugations is 20 mm and the amplitude is 10 mm.
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
Abstract
L'invention a pour objet un dispositif de dispersion d'une phase gazeuse dans une phase liquide comprenant au moins un éjecteur venturi d'axe vertical ou incliné, composé d'un convergent (1) pour l'entrée du liquide, d'un col (2) pour l'entrée du gaz et d'un divergent (3) caractérisé en ce que ledit divergent est prolongé par une cheminée (5) de diamètre égal ou supérieur à celui du divergent et jointive ou non avec celui-ci. Elle a également pour objet l'application de ce dis positif à la réalisation de traitements tels que les réactions chimiques, biochimiques ou métaboliques comportant le trans fert d'un gaz dans une phase liquide. The subject of the invention is a device for dispersing a gaseous phase in a liquid phase comprising at least minus a venturi ejector with a vertical or inclined axis, composed of a convergent (1) for the entry of the liquid, a neck (2) for the gas inlet and a divergent (3) characterized in that said diverging is extended by a chimney (5) of diameter equal to or greater than that of the divergent and contiguous or not with it. It also relates to the application of this say positive for carrying out treatments such as chemical, biochemical or metabolic reactions comprising the trans fert of a gas in a liquid phase.
A device for dispersing a gaseous phase in a liquid phase comprises at least one Venturi ejector with a vertical or in clined axis, composed of a mixer head (1) for admitting the liquid, a neck (2) for admitting the gas and an injector tube (3). The injector tube is prolonged by a chamber (5) whose diameter is equal to or greater than that of the injector tube with which it possibly merges. Also described is the application of this device to treatments such as chemical, biochemical or metabolic reactions involving the transfer of a gas to a liquid phase. A device for dispersing a gaseous phase in a liquid phase understood at least one Venturi ejector with a vertical or in clined axis, composed of a mixer head (1) for admitting the liquid, a neck (2) for admitting the gas and an injector tube (3). The injector tube is extended by a chamber (5) whose diameter is equal to or greater than that of the injector tube with which it possibly merges. Also described is the application of this device to treatments such as chemical, biochemical or metabolic reactions involving the transfer of a gas to a liquid phase.
Description
Claims
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR8715219A FR2622470B1 (en) | 1987-11-03 | 1987-11-03 | GAS DISPERSION DEVICE WITHIN A LIQUID PHASE AND APPLICATION OF THIS DEVICE TO CARRYING OUT TREATMENTS INCLUDING THE TRANSFER OF A GAS PHASE INTO A LIQUID PHASE |
FR8715219 | 1987-11-03 |
Publications (2)
Publication Number | Publication Date |
---|---|
EP0367799A1 true EP0367799A1 (en) | 1990-05-16 |
EP0367799B1 EP0367799B1 (en) | 1992-03-18 |
Family
ID=9356430
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP88910055A Expired - Lifetime EP0367799B1 (en) | 1987-11-03 | 1988-10-27 | Device for dispersing gas within a liquid phase |
Country Status (9)
Country | Link |
---|---|
US (1) | US5073309A (en) |
EP (1) | EP0367799B1 (en) |
JP (1) | JPH02502085A (en) |
DE (1) | DE3869417D1 (en) |
ES (1) | ES2013358A6 (en) |
FR (1) | FR2622470B1 (en) |
GR (1) | GR880100740A (en) |
PT (1) | PT88911B (en) |
WO (1) | WO1989004208A1 (en) |
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US20030201227A1 (en) * | 1996-12-17 | 2003-10-30 | Perriello Felix Anthony | Remediation of odorous media |
US6669846B2 (en) | 1996-12-17 | 2003-12-30 | Global Biosciences, Inc. | Wastewater treatment with alkanes |
US7192523B2 (en) | 1996-12-17 | 2007-03-20 | Global Biosciences, Inc. | Methods for treating agricultural waste and producing plant growth-enhancing material |
US6923914B2 (en) * | 1996-12-17 | 2005-08-02 | Global Biosciences, Inc. | Remediation of metal contaminants with hydrocarbon-utilizing bacteria |
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US7329532B2 (en) | 2001-07-27 | 2008-02-12 | Global Biosciences, Inc. | Remediation of sulfur-containing pollutants with hydrocarbon-utilizing bacteria |
US6875356B2 (en) * | 2001-07-27 | 2005-04-05 | Global Biosciences, Inc. | Method and apparatus for recovery of metals with hydrocarbon-utilizing bacteria |
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US7303156B1 (en) * | 2004-04-08 | 2007-12-04 | Louisiana Tech University Research Foundation As A Division Of The Louisiana Tech University Foundation | Generation and usage of microbubbles as a blood oxygenator |
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KR101506654B1 (en) * | 2007-12-20 | 2015-03-27 | 레이브 엔.피., 인크. | Fluid injection assembly for nozzles |
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EP3609346B1 (en) | 2017-04-12 | 2023-08-02 | Gaia USA Inc. | Apparatus and method for generating and mixing ultrafine gas bubbles into a high gas concentration aqueous solution |
US10953375B2 (en) | 2018-06-01 | 2021-03-23 | Gaia Usa, Inc. | Apparatus in the form of a unitary, single-piece structure configured to generate and mix ultra-fine gas bubbles into a high gas concentration aqueous solution |
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1987
- 1987-11-03 FR FR8715219A patent/FR2622470B1/en not_active Expired - Fee Related
-
1988
- 1988-10-27 DE DE8888910055T patent/DE3869417D1/en not_active Expired - Fee Related
- 1988-10-27 EP EP88910055A patent/EP0367799B1/en not_active Expired - Lifetime
- 1988-10-27 WO PCT/FR1988/000526 patent/WO1989004208A1/en active IP Right Grant
- 1988-10-27 US US07/392,952 patent/US5073309A/en not_active Expired - Fee Related
- 1988-10-27 JP JP63509231A patent/JPH02502085A/en active Pending
- 1988-10-31 PT PT88911A patent/PT88911B/en not_active IP Right Cessation
- 1988-11-01 GR GR880100740A patent/GR880100740A/en unknown
- 1988-11-02 ES ES8803343A patent/ES2013358A6/en not_active Expired - Fee Related
Non-Patent Citations (1)
Title |
---|
See references of WO8904208A1 * |
Also Published As
Publication number | Publication date |
---|---|
PT88911A (en) | 1989-09-14 |
EP0367799B1 (en) | 1992-03-18 |
PT88911B (en) | 1993-12-31 |
JPH02502085A (en) | 1990-07-12 |
FR2622470A1 (en) | 1989-05-05 |
ES2013358A6 (en) | 1990-05-01 |
FR2622470B1 (en) | 1991-05-10 |
GR880100740A (en) | 1994-03-31 |
WO1989004208A1 (en) | 1989-05-18 |
DE3869417D1 (en) | 1992-04-23 |
US5073309A (en) | 1991-12-17 |
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