EP3113867A1 - Procédé et dispositif de dispersion de gaz dans un liquide - Google Patents
Procédé et dispositif de dispersion de gaz dans un liquideInfo
- Publication number
- EP3113867A1 EP3113867A1 EP15714025.2A EP15714025A EP3113867A1 EP 3113867 A1 EP3113867 A1 EP 3113867A1 EP 15714025 A EP15714025 A EP 15714025A EP 3113867 A1 EP3113867 A1 EP 3113867A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- liquid
- gas
- jets
- tube
- vertical tube
- 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
- 239000007788 liquid Substances 0.000 title claims abstract description 145
- 238000000034 method Methods 0.000 title claims abstract description 30
- 230000008569 process Effects 0.000 title claims abstract description 6
- 239000000203 mixture Substances 0.000 claims abstract description 25
- 239000007789 gas Substances 0.000 claims description 151
- 238000002347 injection Methods 0.000 claims description 25
- 239000007924 injection Substances 0.000 claims description 25
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 21
- 238000009826 distribution Methods 0.000 claims description 11
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 10
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims description 9
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 5
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 5
- 239000001569 carbon dioxide Substances 0.000 claims description 5
- 238000004519 manufacturing process Methods 0.000 claims description 5
- 229910052760 oxygen Inorganic materials 0.000 claims description 5
- 239000001301 oxygen Substances 0.000 claims description 5
- 239000002351 wastewater Substances 0.000 claims description 5
- 230000003247 decreasing effect Effects 0.000 claims description 3
- 239000002245 particle Substances 0.000 claims description 3
- 230000005514 two-phase flow Effects 0.000 claims description 2
- 150000003839 salts Chemical class 0.000 claims 1
- 239000006185 dispersion Substances 0.000 description 20
- 230000014759 maintenance of location Effects 0.000 description 15
- 239000012071 phase Substances 0.000 description 15
- 239000000463 material Substances 0.000 description 10
- 238000013022 venting Methods 0.000 description 9
- 230000000694 effects Effects 0.000 description 8
- 230000003068 static effect Effects 0.000 description 8
- 238000012546 transfer Methods 0.000 description 8
- 239000012530 fluid Substances 0.000 description 4
- 239000007792 gaseous phase Substances 0.000 description 4
- 238000012423 maintenance Methods 0.000 description 4
- 239000007970 homogeneous dispersion Substances 0.000 description 3
- 238000007654 immersion Methods 0.000 description 3
- 239000007791 liquid phase Substances 0.000 description 3
- 230000002829 reductive effect Effects 0.000 description 3
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- 230000005540 biological transmission Effects 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 230000000875 corresponding effect Effects 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 238000009792 diffusion process Methods 0.000 description 2
- 239000003651 drinking water Substances 0.000 description 2
- 235000020188 drinking water Nutrition 0.000 description 2
- 239000011261 inert gas Substances 0.000 description 2
- 229940090046 jet injector Drugs 0.000 description 2
- 230000000670 limiting effect Effects 0.000 description 2
- 238000010008 shearing Methods 0.000 description 2
- 239000011780 sodium chloride Substances 0.000 description 2
- 238000011144 upstream manufacturing Methods 0.000 description 2
- 108010074506 Transfer Factor Proteins 0.000 description 1
- 241000722921 Tulipa gesneriana Species 0.000 description 1
- 238000005299 abrasion Methods 0.000 description 1
- 238000013019 agitation Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- UHZZMRAGKVHANO-UHFFFAOYSA-M chlormequat chloride Chemical compound [Cl-].C[N+](C)(C)CCCl UHZZMRAGKVHANO-UHFFFAOYSA-M 0.000 description 1
- 238000004581 coalescence Methods 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000002596 correlated effect Effects 0.000 description 1
- 238000007872 degassing Methods 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000013213 extrapolation Methods 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 238000006385 ozonation reaction Methods 0.000 description 1
- 230000036961 partial effect Effects 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000007704 transition Effects 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
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
- B01F23/236—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids specially adapted for aerating or carbonating beverages
-
- 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
- B01F23/232—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids using flow-mixing means for introducing the gases, e.g. baffles
- B01F23/2323—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids using flow-mixing means for introducing the gases, e.g. baffles by circulating the flow in guiding constructions or conduits
-
- 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
- B01F23/231—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids by bubbling
-
- 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
- B01F23/2319—Methods of introducing gases into liquid media
-
- 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
- B01F23/232—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids using flow-mixing means for introducing the gases, e.g. baffles
-
- 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
- B01F23/234—Surface aerating
- B01F23/2341—Surface aerating by cascading, spraying or projecting a liquid into a gaseous atmosphere
- B01F23/23412—Surface aerating by cascading, spraying or projecting a liquid into a gaseous atmosphere using liquid falling from orifices in a gaseous atmosphere, the orifices being exits from perforations, tubes or chimneys
-
- 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
- B01F23/237—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids characterised by the physical or chemical properties of gases or vapours introduced in the liquid media
- B01F23/2376—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids characterised by the physical or chemical properties of gases or vapours introduced in the liquid media characterised by the gas being introduced
- B01F23/23761—Aerating, i.e. introducing oxygen containing gas in liquids
- B01F23/237613—Ozone
-
- 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
- B01F23/237—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids characterised by the physical or chemical properties of gases or vapours introduced in the liquid media
- B01F23/2376—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids characterised by the physical or chemical properties of gases or vapours introduced in the liquid media characterised by the gas being introduced
- B01F23/23762—Carbon dioxide
-
- 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
- B01F25/314—Injector mixers in conduits or tubes through which the main component flows wherein additional components are introduced at the circumference of the conduit
- B01F25/3142—Injector mixers in conduits or tubes through which the main component flows wherein additional components are introduced at the circumference of the conduit the conduit having a plurality of openings in the axial direction or in the circumferential direction
- B01F25/31423—Injector mixers in conduits or tubes through which the main component flows wherein additional components are introduced at the circumference of the conduit the conduit having a plurality of openings in the axial direction or in the circumferential direction with a plurality of perforations in the circumferential direction only and covering the whole circumference
-
- 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
- B01F25/40—Static mixers
- B01F25/42—Static mixers in which the mixing is affected by moving the components jointly in changing directions, e.g. in tubes provided with baffles or obstructions
- B01F25/43—Mixing tubes, e.g. wherein the material is moved in a radial or partly reversed direction
- B01F25/433—Mixing tubes wherein the shape of the tube influences the mixing, e.g. mixing tubes with varying cross-section or provided with inwardly extending profiles
- B01F25/4334—Mixers with a converging cross-section
-
- 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
- B01F23/237—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids characterised by the physical or chemical properties of gases or vapours introduced in the liquid media
- B01F23/2376—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids characterised by the physical or chemical properties of gases or vapours introduced in the liquid media characterised by the gas being introduced
- B01F23/23761—Aerating, i.e. introducing oxygen containing gas in liquids
- B01F23/237611—Air
-
- 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
- B01F23/237—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids characterised by the physical or chemical properties of gases or vapours introduced in the liquid media
- B01F23/2376—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids characterised by the physical or chemical properties of gases or vapours introduced in the liquid media characterised by the gas being introduced
- B01F23/23761—Aerating, i.e. introducing oxygen containing gas in liquids
- B01F23/237612—Oxygen
Definitions
- the invention relates to a method and a device for dispersing gas in a downward flow of liquid.
- the invention more particularly relates to a method and a dispersing device with hybrid liquid gas jet mixer and jet injector.
- the method is intended to homogeneously disperse the gas in the form of fine bubbles in a liquid engine for contacting liquid gas or for subsequent contact with the mass of liquid in a surrounding contactor in which the device is implanted.
- the device is composed of an injection head comprising a liquid-jet mixing chamber at the top and a vertical coaxial tube with diphasic jet at the bottom, forming a nozzle.
- Said homogeneous liquid gas dispersion is produced for a gas retention of between 5 and 70%, preferably between 30 and 50%.
- the invention relates more particularly to a method and a device for injecting ozone or a mixture of ozone and oxygen and / or air into a stream of water, to purify it.
- the performance of the gas dispersion can be expressed on the one hand as a function of the size of the gas bubbles produced and on the other hand as a function of a gas / liquid volume ratio of the two-phase gas-liquid mixture resulting from the dispersion.
- ratio related to the gas retention defined as the ratio of the volume of the gas phase relative to the total volume of the contactor equal to the sum of the volumes of gas and liquid that it contains or as the ratio of the volumetric flow rate of the gaseous phase reported the sum of the volume flow rates of gas and liquid.
- the two-phase liquid gas contactors correspond to many industrial applications, such as liquid phase oxidation and hydrogenation or gas absorption by a liquid with or without a chemical reaction.
- the gaseous and liquid phase contacting devices are designed to respond as efficiently as possible to the requirement to ensure the transfer of the quantities of material required, at the best cost, including furthermore notions related to the operation such as flexibility with regard to the quantities of material to be used, safety and stability of operation, speed of execution of the start-up and start-up steps, potential duration of operation (corrosion, maintenance, .... ).
- N the quantity of material exchanged within a two-phase apparatus
- N Material Transfer Factor x Interchange Interface Area x Exchange Potential
- liquid gas contactors are designed to offer the largest exchange surface compatible with hydrodynamic conditions relating to the circulating flow rates of the fluids and the physicochemical properties of the latter. It is also essential that the pressure drop on the gas side is as moderate as possible in order to avoid unacceptable energy expenditure or pressure conditions that are incompatible with the application conditions.
- the contactors in which the gas is dispersed in the form of bubbles in a liquid cover the bubble column, mechanically stirred tank, perforated plate column, co-current tubular contactor such as static mixer, submerged jet ejector and venturi ejector. engine liquid (M.
- WO 2012025214 discloses a device and method for absorbing ozone in a tubular contactor for treating liquids in which the ozonated gas injection takes place in the circulating liquid stream by means of at least two static mixers spaced from zones of contact.
- WO 2013082132 discloses a method and apparatus for injecting a gas into a liquid, wherein a rotating helical helix located inside a suction tube immersed in the liquid creates a downward flow of liquid inside the suction tube fed with gas through nozzles arranged either above or below or along the helical helix.
- the liquid is sucked into the suction tube at a superficial velocity greater than a terminal rate of rise of the gas bubbles, so as to allow undissolved gas bubbles to be entrained in the bulk of the liquid within the liquid that is sucked into the suction tube.
- a transfer efficiency of 90% is obtained in the contactor for a gas retention of 5% in the tube of less than one meter in length.
- EP 0 086 019 relates to a two-stage hybrid contactor combining a rain column and a bubble column for dissolving a gas in a liquid, preferably for the ozonation of water, according to which the gas injection is carried out by means of a submerged tube.
- a fraction of the liquid flow is used to inject the gas in the form of bubbles by means of a submerged tube which introduces the two-phase mixture into a downward flow of the main flow of liquid fed by runoff into the annular portion upper outer of the contactor.
- This device thus involves a free space of significant volume runoff that promotes degassing so that the yield of dissolution of the gas is reduced. Gaseous retention in the injection tube is indicated as 13% maximum.
- FR 2,762,232 also discloses a method and a device for contacting ozone in liquids, in particular water, according to which a two-phase mixture of the partial flow of the liquid to be treated and a gas charged with pressurized ozone is formed in a downwardly co-current gas and liquid-containing vertical tube optionally containing bubble-shearing devices, all of which form part of an ozone-absorbing contactor in the liquid in the form of U-shaped tube as described in FR 2 545 732.
- the dispersion of the gas in the form of bubbles is obtained in the descending tube under the effect of the liquid velocity of about 1.5 m / s.
- the height of the contactor is between 20 and 35 m. This type of contactor involves operating with a gas retention of less than 20% to control the two-phase water and gas mixture (Degrémont, Mémento Technique de l'eau, Editions Lavoisier, 2005).
- US6001247 also discloses a contactor composed of a diffusion compartment equipped with a submerged vertical tube cocurrent descending ozonated gas and water to introduce the gas uniformly.
- the inside of the tube contains coaxial porous elements to distribute the ozonated gas in the form of bubbles in the water flowing through it.
- FR 2 776 942 also details a device for dispersing a gas in a liquid by submerged jet.
- the dispersing device consists of a single emitting nozzle of a downward directed liquid jet, a coaxial jet tube, and an impact plate located near the lower end of the tube. .
- the level of the dispersion is maintained as close as possible to the outlet of the nozzle by maintaining the level in the surrounding contactor.
- the jet produced by the nozzle draws the gas admitted laterally to the nozzle and the vehicle in the tube simultaneously with the dispersion which penetrates from the outside to the inside of the tube through submerged holes.
- the assembly is dispersed in the mass of the surrounding contactor by impact on the plate.
- the method according to the invention is intended, above all, to avoid the many disadvantages of tubular contactors operating co-current of gas and liquid capable of producing a significant interfacial area and described in the state of the prior art.
- the main disadvantages are recalled below:
- the invention also aims to provide a two-phase mixture with a gaseous / liquid volume ratio greater than 0.3, without however consuming too much energy and without bringing into play high liquid pressures, of the order 4 bars. It is further desirable that the method and the dispersing device are simple to implement, and that their maintenance is not made difficult by the presence of particles in the liquid.
- the method of dispersing gas in a downward flow of liquid is characterized in that:
- the liquid is distributed in at least one jet directed downwards, preferably in a plurality of jets,
- the gas is distributed radially towards the jetting or jets of liquid in order to be driven by the liquid
- the gas is distributed under a pressure of less than 2 bar, preferably less than 1.5 bar.
- the speed of the liquid jets can be between 4 and 10 m / s, preferably between 6 and 8 m / s.
- the cross section of the vertical tube is at least equal to the total emission surface of the liquid jets, and at most equal to twice the same surface, said cross section preferably being between 1, 2 and 1.5 times the total emission area of the jets.
- the liquid is directed above a horizontal plate having a plurality of orifices within an area, to flow downwards in a plurality of jets,
- the gas is distributed radially inward of said orifice zone for the liquid
- the liquid gas mixture is channeled in a decreasing section until it reaches the downward vertical tube.
- the liquid gas mixture is channeled in the descending vertical tube for at least 0.2 seconds.
- the injected gas may be selected from air, oxygen, ozone, carbon dioxide, these gases being injected alone or in mixtures.
- the liquid is aqueous including natural fresh or saline water, wastewater and more generally aqueous effluents, process water in industry including the drinking water production sector.
- the invention also relates to a device for dispersing gas in a liquid, in particular for the implementation of a method as defined above, comprising an inlet conduit for the liquid to be treated, characterized in that has:
- an injection head connected to the inlet duct and comprising a liquid jet mixing chamber
- the injection head comprises a compartment with, in the lower part, a horizontal dispensing plate for the liquid pierced with at least one orifice, and an annular chamber provided under the plate at its periphery and comprising at least one dispensing opening of the gas in a centripetal radial direction,
- the mixing chamber located below the plate, being in the form of a converging connection to the downward vertical tube.
- the diameter of the orifices of the plate is sufficient, in particular at least equal to 10 mm, to prevent clogging due to particles contained in the liquid, in particular wastewater.
- the device may comprise a radial inlet of the gas in the annular distributing chamber, from a gas pipe extending beyond the radial inlet for possible venting to the atmosphere.
- venting is particularly advantageous, in particular because it improves the safety during the operation of such a device, in particular during a stop sequence of the device.
- a sequence stopping it typically begins by evacuating the gas contained in the device by replacing it with outside air, through the extension, or vent pipe, of said gas pipe.
- a vent valve is gradually opened so as to introduce outside air into the mixing chamber through this vent pipe, and then a gas inlet valve is closed so as to interrupt the arrival. of gas in the mixing chamber through said gas conduit.
- the venting thus makes it possible to avoid any phenomenon of implosion of the device. This is particularly advantageous in cases where the gas introduced into the mixing chamber through the gas pipe is dangerous, typically ozone.
- venting makes it possible to comply with such safety constraints, particularly when the device performs an injection of gas into a water level situated at a relatively low altitude relative to the altitude of the injection head. , that is to say when said downward vertical tube has a relatively long length before submersion, for example 10 meters.
- venting also makes it possible to improve the flexibility of the device during a start-up sequence during which a liquid is injected into the mixing chamber via said inlet duct for the liquid to be treated.
- the vent valve is opened, allowing at least a portion of the gas present in the mixing chamber to be evacuated. Venting also allows the gas supply to be closed until the desired hydraulic speed is achieved. The gas inlet is then opened and the vent valve is closed.
- the cross section of the vertical tube is at least equal to the total surface of the holes of the plate, and at most equal to twice the same surface, and is preferably between 1, 2 and 1.5 times the total surface of the orifices. of the plate.
- the length of the descending tube may be between 1 and 30 meters, and is preferably between 1 and 15 meters.
- the convergent of the mixing chamber may be frustoconical, the angle of inclination of the generatrices of the truncated cone relative to the axis being between 15 ° and 45 °.
- the injection system which is the subject of the invention is a dispersion system with a hybrid liquid gas jet mixer and a jet injector. Said system is composed of an injection head comprising a liquid-jet mixing chamber at the top and a vertical coaxial tube with diphasic jet at the bottom, forming a nozzle. Its function is to homogeneously disperse the gas in the form of fine bubbles in the engine liquid as a liquid gas contactor or for subsequent contact with the mass of liquid in a surrounding contactor. Said liquid gas dispersion is produced for a gas retention of between 5 and 70%, preferably between 30 and 50%.
- the injection head is designed to pre-mix the liquid and the gas upstream of the nozzle, the mixture being made homogeneous along the descent into the nozzle.
- the gas and the liquid may be those involved in any operation requiring the formation of a liquid gas dispersion.
- the injected gas will be selected from air, oxygen, ozone, carbon dioxide, these gases being injected alone or in mixtures.
- the liquid will be aqueous including natural fresh or saline water, wastewater and more generally aqueous effluents, industrial process water in the industry including the drinking water production sector.
- the injection head is fed by the liquid discharged by a pumping system and the gas from the distribution system is at a pressure equal to or greater than atmospheric pressure.
- the injection head performs a premixing of the liquid and the gas under the effect of one to several turbulent streams of liquid emitted into the radially admitted gas stream.
- the jets of liquid are produced by means of a liquid distribution member in the form of jets at high speed, typically between 4 and 10 m / s, preferably between 6 and 8 m / s.
- the dispensing member is preferably an orifice distribution plate.
- a mixing chamber located below the dispenser member has the shape of the section of the dispensing plate as an upper section.
- the mixing chamber is tulip-shaped or frustoconical convergent or cylindrical or parallelepipedal.
- the turbulence of the jets is demonstrated by Reynolds numbers greater than 10 5 .
- the emission of the liquid jets produces an interfacial friction rate in the gas, which can thus reach more than 0.3 m / s, ie a speed greater than the terminal gas bubble speed of the order of 3 mm.
- a liquid flow diagram shows the liquid flow lines and highlights the areas of liquid recirculation within the mixing chamber also filled with gas.
- the high speed liquid jets thus shear the gas and suck up the produced gas pockets towards the down tube.
- the liquid jets initiate the transfer of liquid gas material. Considering an average contact time of the liquid jets of 0.15 s, the transfer coefficient is of the order of 1.10 m / s according to the nature of the gas.
- the exchange potential is equal to the equilibrium concentration between the gas and the liquid.
- the quantity The amount of carbon dioxide transferred is 0.3 kg / s.
- the mixing chamber is followed downstream of a preferably cylindrical coaxial tube.
- the section of the tube is at least equal to the total emission surface of the liquid jets in the mixing chamber and at most equal to twice the same surface.
- the ratio of these surfaces is preferably between 1, 2 and 1.5.
- the bubble flow appears at low values of the ratio of gas and liquid flow rates. It is characterized by a highly turbulent continuous liquid phase with homogeneous dispersion of gas-sized bubbles relatively uniform,
- the flow chart in vertical pipe depends, in order of importance: superficial velocities of gas and liquid, the diameter of the pipe and the properties of the fluids.
- the dispersion device according to the invention makes the two-phase mixture homogeneous during the downward co-flow flow in the coaxial tube to the liquid distributor, as has been observed for a 40% gas retention. %.
- the length of the down tube can reach 30 meters to promote the transfer of material inside the tube and possibly in the surrounding contactor whose height corresponds to the useful height of the dispersion system.
- the height is preferably between 1 and 25 m.
- a gas retention in the two-phase volume equal to 50% corresponds to the compact stack of the gas inclusions in the liquid.
- the attainment of a homogeneous bubble size in the descending tube requires shearing again the volume of gas sucked under the effect of the turbulence of the mixture while the frequency of coalescence of the bubbles is all the more important than the gas retention is high.
- the turbulence of the mixture is demonstrated by Reynolds number levels of the diphasic mixture greater than 10 4 .
- This turbulence is maintained by applying a relative liquid velocity equal to the liquid velocity of the distribution jets in the mixing chamber for the best continuity of flow, ie typically between 4 and 10 m / s. This velocity tends to decrease slightly during the descent under the effect of the compression of the gas under the effect of the column of liquid and under the effect of the transfer of material which takes place.
- the regime is established in the area of bubble flow from the top of the tube.
- the quality of the mixture at the beginning of the descending tube determines the pressure required for the injected gas.
- the pressure of the liquid gas mixture is a function of the outlet pressure of the nozzle (mainly a function of the immersion height), the pressure drops and the weight of the liquid column in the injection system (which can be considered as the static component).
- an annular liquid film type flow regime such as that observed in the first meters of a tube equipped with a nozzle and without premixing of the gas and liquid operating with gaseous retention of 40% prevents the transmission of static pressure downwards.
- the loss of liquid height is reflected directly by the need to increase the pressure of the gas injection.
- the device of the invention allows on the contrary a regular transmission of the pressure because it provides a good quality of dispersion from the beginning of the descent into the tube.
- the size of the bubbles produced is correlated with the dissipated energy itself, which is dependent on the local retention rates and on the physicochemical properties of the fluids composing the dispersion.
- a dispersion of oxygen in water at 40% gas is characterized by bubbles of average diameter equal to 2.5 mm at the end of the tube 10 m in length.
- the highly concentrated two-phase jet of dissolved gas produced at the outlet of the tube can then be dispersed in a surrounding contactor or relaxed towards the outlet of the reactor according to the contact time necessary for the absorption and possibly the reaction involved in the application.
- the surrounding contactor may be any contactor known from the state of the art with a gas updraft.
- the invention consists, apart from the arrangements described above, in a certain number of other arrangements which will be more explicitly discussed hereinafter with reference to an exemplary embodiment described with reference to the appended drawing, but which is in no way limiting. On this drawing :
- Fig.1 is a schematic top perspective view of the dispersion device according to the invention.
- Fig.2 is a schematic perspective view from another angle of view and with cut parts of the device of Fig.1, and
- Fig.3 is a perspective view from below of the device of Fig.1.
- the dispersing device D comprises two sets: an injection head H and a jet dispersion tube P, forming a nozzle.
- the injection head H is the structure that connects the liquid and gas inlets, mixes these fluids and directs the resulting mixture into the down tube P.
- the injection head H is connected to the inlet pipe 1 of liquid and comprises a compartment B with, in the lower part, a liquid distribution member, preferably a horizontal distribution plate 2 for the liquid, pierced with orifices. 2a.
- the liquid flows vertically below the plate, following jets schematized by arrows A in Fig.2.
- An inlet pipe 4 of the gas to be injected is connected, by a radial box 4a, to an annular chamber 5 located under the plate 2, the lower periphery of which it surrounds.
- a wall E limiting radially inwards the chamber 5 comprises nozzles or openings O of gas distribution in centripetal radial directions represented by arrows F in Fig.2.
- a mixing chamber 3 is located under the plate 2.
- the mixing chamber 3 is preferably convergent tulip or frustoconical shape, but could be of cylindrical or parallelepipedal shape.
- the inclination of the generatrices of the convergent with respect to the geometric axis is preferably between 15 ° and 45 °.
- the chamber 3 provides the connection to the downward vertical tube P, preferably coaxial and cylindrical.
- a venting system 6 for the start-up phase is provided at the end of the pipe 4 beyond the connection with the annular chamber 5.
- a vent valve, not shown, is provided in the system 6, and a gas inlet valve not shown.
- the jet dispersion tube P is hydraulically described as a straight vertical pipe length.
- the operation of the device is as follows. The start-up sequence of the device, integrated into a surrounding contactor not shown, provides a better understanding of the overall design of the device in its entirety.
- the water level inside the immersed tube P is equal to the water level outside. Above this level, the mixing chamber 3 and the tube P are filled with gas.
- the liquid supply is started at a rate equal to one third of the desired operating flow.
- the liquid fills the supply line 1 of the system.
- the distribution plate 2 produces jets of liquid at low speed.
- venting system 6 allows the gas initially contained in the injection head and the gas pockets entrained at the start upstream to be at the top of the tube P.
- vent pipe valve of the venting system 6 progressively switches to the gas supply via line 4 and the system can come into production.
- the shutdown sequence of the dispersing device is as follows:
- the first step is to evacuate the gas contained in the device by replacing it with outside air or an inert gas.
- the vent valve of the system 6 is progressively open on outside air or an inert gas, after which the gas inlet valve of the system 6 closes.
- the device After a short period corresponding to the renewal by 5 times of the total volume of the device, the device can be stopped under completely safe conditions, gradually decreasing the flow of water.
- the device is capable of responding correctly to abrupt changes in conditions. , resulting, for example, from a power failure or any other event that could lead to an unscheduled shutdown.
- This device makes it possible to ensure an eminently variable gaseous engagement of between 0.01 and 2 (if expressed in relation to gas and liquid flow rates), at the best cost under the effect of the necessary pressure reduction, to produce a homogeneous dispersion of gas in the liquid suitable for transferring the quantities of material required.
- it offers the following advantages:
- This device solves the disadvantages of the systems described in the state of the prior art and is also capable of replacing all or part of the gas injection and diffusion systems of the bubble column contactors, injection systems of gas and agitation of the agitated contactors.
- the resulting contactors are much more efficient both technically and economically.
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Dispersion Chemistry (AREA)
- Accessories For Mixers (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
Abstract
Description
Claims
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR1451870A FR3018206A1 (fr) | 2014-03-07 | 2014-03-07 | Procede et dispositif de dispersion de gaz dans un liquide |
PCT/IB2015/051705 WO2015132773A1 (fr) | 2014-03-07 | 2015-03-09 | Procede et dispositif de dispersion de gaz dans un liquide |
Publications (2)
Publication Number | Publication Date |
---|---|
EP3113867A1 true EP3113867A1 (fr) | 2017-01-11 |
EP3113867B1 EP3113867B1 (fr) | 2018-01-03 |
Family
ID=51168034
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP15714025.2A Active EP3113867B1 (fr) | 2014-03-07 | 2015-03-09 | Procédé et dispositif de dispersion de gaz dans un liquide |
Country Status (6)
Country | Link |
---|---|
US (1) | US10603643B2 (fr) |
EP (1) | EP3113867B1 (fr) |
CA (1) | CA2939691C (fr) |
ES (1) | ES2663342T3 (fr) |
FR (1) | FR3018206A1 (fr) |
WO (1) | WO2015132773A1 (fr) |
Families Citing this family (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR3018206A1 (fr) * | 2014-03-07 | 2015-09-11 | Degremont | Procede et dispositif de dispersion de gaz dans un liquide |
US11219871B2 (en) * | 2017-03-10 | 2022-01-11 | Pronto Concepts Inc. | Liquid diffusing filter |
Family Cites Families (20)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US805653A (en) * | 1902-03-10 | 1905-11-28 | Leon P Lowe | Apparatus for cleaning manufactured gases. |
US2767127A (en) * | 1950-10-30 | 1956-10-16 | Gulf Oil Corp | Particle transporting method and apparatus for use in the catalytic conversion of hydrocarbons |
US3440018A (en) * | 1966-03-11 | 1969-04-22 | Us Stoneware Inc | Chemical treating tower |
JPS53116562A (en) * | 1977-03-22 | 1978-10-12 | Akoo Kk | Powdery material mixing method and apparatus therefor |
DE3363127D1 (en) | 1982-02-09 | 1986-05-28 | Bbc Brown Boveri & Cie | Method and apparatus for treating a liquid with a gas |
US4498819A (en) * | 1982-11-08 | 1985-02-12 | Conoco Inc. | Multipoint slurry injection junction |
FR2545732B1 (fr) | 1983-05-10 | 1989-10-27 | Lyonnaise Eaux Eclairage | Appareil pour la dissolution d'ozone dans un fluide |
CA2090619A1 (fr) * | 1990-08-27 | 1992-02-28 | John Graeme Jameson | Aeration de liquides |
US5462351A (en) * | 1994-06-20 | 1995-10-31 | Jenike & Johanson, Inc. | Conditioning vessel for bulk solids |
US6001247A (en) | 1996-05-01 | 1999-12-14 | Schulz; Christopher R. | Removable, in-line diffuser apparatus for ozone disinfection of water |
AUPO129096A0 (en) * | 1996-07-26 | 1996-08-22 | Boc Gases Australia Limited | Oxygen dissolver for pipelines or pipe outlets |
FR2762232B1 (fr) | 1997-04-17 | 1999-05-28 | Degremont | Procede et dispositif pour la mise en contact de l'ozone dans des fluides a traiter, notamment de l'eau |
US6007055A (en) * | 1997-12-29 | 1999-12-28 | Schifftner; Kenneth C. | Gas and liquid contact apparatus |
FR2776942B1 (fr) | 1998-04-07 | 2000-05-05 | Roger Botton | Dispositif pour disperser un gaz dans un liquide en vue d'effectuer des reactions chimiques, biochimiques ou de simples echanges physiques avec ou sans particules en suspension |
DE10250707B4 (de) * | 2002-10-31 | 2010-08-12 | Roland Damann | Vorrichtung zur Lösung von Gas in Flüssigkeit |
DE202006002983U1 (de) * | 2006-02-24 | 2006-04-27 | Damann, Roland | Vorrichtung zum Durchführen von Wellness-Bädern oder therapeutischen Bädern |
DE102010035519B3 (de) | 2010-08-25 | 2011-12-08 | Itt Mfg. Enterprises, Inc. | Vorrichtung und Verfahren zur Behandlung von Flüssigkeiten mittels Ozon |
US9486750B2 (en) | 2011-12-01 | 2016-11-08 | Praxair Technology, Inc. | Gas injection method and apparatus |
FR3018206A1 (fr) * | 2014-03-07 | 2015-09-11 | Degremont | Procede et dispositif de dispersion de gaz dans un liquide |
DE102017011074B3 (de) * | 2017-11-30 | 2019-01-17 | Palas Gmbh Partikel- Und Lasermesstechnik | Verfahren und Vorrichtung zum Verdünnen eines Aerosols |
-
2014
- 2014-03-07 FR FR1451870A patent/FR3018206A1/fr not_active Withdrawn
-
2015
- 2015-03-09 US US15/121,491 patent/US10603643B2/en active Active
- 2015-03-09 CA CA2939691A patent/CA2939691C/fr active Active
- 2015-03-09 ES ES15714025.2T patent/ES2663342T3/es active Active
- 2015-03-09 WO PCT/IB2015/051705 patent/WO2015132773A1/fr active Application Filing
- 2015-03-09 EP EP15714025.2A patent/EP3113867B1/fr active Active
Also Published As
Publication number | Publication date |
---|---|
EP3113867B1 (fr) | 2018-01-03 |
US20160361692A1 (en) | 2016-12-15 |
WO2015132773A1 (fr) | 2015-09-11 |
US10603643B2 (en) | 2020-03-31 |
CA2939691C (fr) | 2020-08-04 |
ES2663342T3 (es) | 2018-04-12 |
FR3018206A1 (fr) | 2015-09-11 |
CA2939691A1 (fr) | 2015-09-11 |
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