EP0152201A2 - Dissolving gas in liquid - Google Patents
Dissolving gas in liquid Download PDFInfo
- Publication number
- EP0152201A2 EP0152201A2 EP85300488A EP85300488A EP0152201A2 EP 0152201 A2 EP0152201 A2 EP 0152201A2 EP 85300488 A EP85300488 A EP 85300488A EP 85300488 A EP85300488 A EP 85300488A EP 0152201 A2 EP0152201 A2 EP 0152201A2
- Authority
- EP
- European Patent Office
- Prior art keywords
- stream
- gas
- liquid
- conduit
- venturi
- 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 70
- 239000006185 dispersion Substances 0.000 claims abstract description 25
- 238000011144 upstream manufacturing Methods 0.000 claims abstract description 20
- 238000000034 method Methods 0.000 claims description 18
- 230000035939 shock Effects 0.000 claims description 12
- 239000000203 mixture Substances 0.000 claims description 6
- 230000003247 decreasing effect Effects 0.000 claims 1
- 239000007789 gas Substances 0.000 abstract description 68
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 abstract description 36
- 239000001301 oxygen Substances 0.000 abstract description 36
- 229910052760 oxygen Inorganic materials 0.000 abstract description 36
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 9
- 239000002351 wastewater Substances 0.000 description 2
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- PIYVNGWKHNMMAU-UHFFFAOYSA-N [O].O Chemical compound [O].O PIYVNGWKHNMMAU-UHFFFAOYSA-N 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 230000002706 hydrostatic effect Effects 0.000 description 1
- 230000001706 oxygenating effect Effects 0.000 description 1
- 230000000717 retained effect Effects 0.000 description 1
- 239000011555 saturated liquid Substances 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 238000013517 stratification Methods 0.000 description 1
Images
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
- B01F23/237—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
-
- 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
-
- 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
- B01F25/20—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
- 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
- B01F25/3122—Injector mixers in conduits or tubes through which the main component flows with Venturi elements; Details thereof the material flowing at a supersonic velocity thereby creating shock waves
-
- 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
- B01F25/50—Circulation mixers, e.g. wherein at least part of the mixture is discharged from and reintroduced into a receptacle
- B01F25/53—Circulation mixers, e.g. wherein at least part of the mixture is discharged from and reintroduced into a receptacle in which the mixture is discharged from and reintroduced into a receptacle through a recirculation tube, into which an additional component is introduced
-
- 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
- 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
Definitions
- This invention relates to a method and apparatus for dissolving gas in liquid.
- the invention is particularly but not exclusively concerned with dissolving oxygen or a gas mixture including oxygen as one of its constituents in an aqueous or non-aqueous liquid.
- Our U.K. patent specification No. 1 455 567 discloses a process for treating liquid, including the steps of taking a stream of the liquid, pressurising the stream, introducing a treatment gas into the pressurised stream so as to dissolve therein some of the gas, and introducing the stream containing dissolved and undissolved gas into a volume of the liquid under turbulent conditions such that the undissolved gas enters the volume of liquid in the form of fine bubbles that either dissolve or are consummed within the volume of liquid.
- a method of dissolving gas in a liquid comprising the steps of pressurising a stream of liquid, introducing the gas into the pressurised stream, creating turbulence in the stream so as to dissolve therein some of the gas and to form a dispersion of undissolved gas bubbles in the liquid, transporting said stream as a dispersion of gas bubbles in the liquid to at least one outlet in a volume of the liquid at a substantially lower pressure than that to which said stream is subjected, and introducing the stream through the said outlet into the volume of liquid such that resulting turbulence causes substantially all the remaining undissolved gas bubbles to dissolve in the volume of liquid or be consumed thereby, wherein some of the gas carried in the stream is taken therefrom at a relatively downstream position and is returned to said stream at a relatively upstream position.
- the invention also provides apparatus for dissolving gas in a liquid comprising means (e.g. a pump) for pressurising a stream of liquid, a vessel for holding a volume of liquid in which gas is to be dissolved, a conduit placing the outlet of the pressurising means in communication with at least one nozzle (or the like) for introducing the stream of pressurised liquid into the volume of liquid, means for introducing gas into the stream flowing through the conduit, means for creating turbulence in the stream so as to dissolve therein some of the gas and to form a dispersion of undissolved gas bubbles in the liquid, means for taking some of the gas from the stream at a relatively downstream position in the conduit, and means for returning said gas to the conduit at a relatively upstream position.
- means e.g. a pump for pressurising a stream of liquid
- a vessel for holding a volume of liquid in which gas is to be dissolved
- a conduit placing the outlet of the pressurising means in communication with at least one nozzle (or the like
- the method and apparatus according to the invention make it possible to provide an enhanced ratio of mass of gas to mass of liquid in the stream and thereby increase the dissolving efficiency of the method described in our U.K. patent specification 1 455 567.
- the benefit of an increased efficiency of dissolving gas may be reaped, if desired, in meeting a particular demand for dissolved gas at a lower power consumption (i.e. by subjecting the stream to a lower pressure) than would be needed if the method described in the aforesaid patent specification were used.
- Preferably, up to about 60% by volume of the gas originally introduced into the stream is taken therefrom and is returned to the relatively upstream position.
- the gas is preferably separated from said stream.
- an outlet aperture for gas from the conduit at said relatively downstream position is an outlet aperture for gas from the conduit at said relatively downstream position.
- the pipe terminates in the throat of a venturi through which the said stream flows, thereby obviating the need to supply any external pump to draw the gas from the relatively downstream location of the conduit and return it to a relatively upstream location.
- the gas being returned to the liquid stream may be combined with the gas being introduced therein for the first time.
- the said pipe leading from the relatively downstream location of the conduit to the location relatively upstream thereof preferably has a restriction therein so as to limit the amount of gas that is recycled.
- the restriction is provided by a flow control valve which is typically manually operable.
- the main inlet for the gas is at a region where the resulting mixture of gas and liquid travels at a velocity less than that of sound in said mixture.
- the stream is then preferably accelerated to a supersonic velocity to create a shock wave effective to reduce the size of the gas bubbles in the stream and thereby to form a dispersion of particularly small gas bubbles in the liquid.
- shock wave can be created by passing the stream through a restriction in the conduit. The restriction may be provided by the venturi that is used to draw recycled gas into the stream.
- the velocity of sound in a dispersion of gas in liquid is substantially less than that of the sound in the gas itself and for oxygen-water systems will be in the order of 50 feet per second.
- the resulting shockwave as the dispersion of gas and liquid goes supersonic is found to be particularly effective in causing the gas to be formed into bubbles of a relatively small size.
- the velocity of the stream Downstream of where the shock wave is created the velocity of the stream is preferably reduced once again to below supersonic velocity. Preferably, however, the velocity of the stream is increased to a value above that of the velocity of sound through the dispersion at a region immediately upstream of the said outlet so as to create a second shock wave effective to reduce further the size of the gas bubbles.
- the second shock wave is preferably created by passing the stream through another restriction, typically immediately upstream of the or each outlet.
- the second shock wave is effective to reduce the size of the bubbles even further immediately before the dispersion of gas in the liquid enters the main volume of liquid. Typically the main volume of the liquid is kept in a tank open to the atmosphere.
- the outlet typically takes the form of a pipe having one or more orifices therein through which the gas-in-liquid dispersion enters the main volume of liquid.
- an open topped tank 2 contains a volume 4 of waste water having a biochemical oxygen demand. Near its bottom, the tank 2 has an outlet 6 communicating with a pipe 8 which terminates at the inlet end of a pump 10 adapted to pressurise liquid flowing there through.
- the outlet of the pump 10 communicates with an elongate conduit 12 which terminates in a sparge pipe 14 located in the volume 4 of the liquid at a region near to the bottom and to one side thereof.
- the pipe 14 has a plurality of outlet orifices 16 which face towards the other side of the tank. Instead of the pipe 14, a single outlet nozzle may be employed.
- An oxygen supply pipe 18 terminates in the conduit 16 at a region thereof near to and downstream of the outlet of the pump 10.
- the oxygen is introduced into the stream flowing through the conduit 12 from the pipe 18.
- the oxygen is typically supplied from a source (not shown) at an elevated pressure sufficient to enable the oxygen to enter the pressurised stream.
- the source may be one or more cylinders of compressed, gaseous oxygen or a vacuum insulated evaporator of liquid oxygen.
- a venturi 20 Downstream of the union of the pipe 18 and the conduit 12 is a venturi 20 having a throat 22.
- a conduit 26 terminates at one end in the throat 22 of the venturi 20 and at its other end in an outlet aperture 24 formed in the wall of the conduit 12 at a downstream region of the conduit 12 near to the pipe 14.
- flow of liquid through the venturi 20 causes a reduction in the static pressure at the throat 22 such that gas that disengages from the liquid and enters the conduit 26 is drawn along the conduit 26 in the direction of the venturi 20 and is introduced into the liquid flowing through the venturi 20.
- the dissolving efficiency is increased.
- a flow control valve 28 is located in the pipe 26 and is manually adjustable to control the rate at which gas is recycled from the aperture 24 to the venturi 20. Typically the rate of recycle is selected to be from 20 to 60% of the rate at which gas is introduced into the conduit 12 from the pipe 18.
- the pump 10 is energised and it withdraws a stream of water from the tank 2.
- the pump 10 is of the kind able to raise the pressure of the liquid passing therethrough to a pressure in the range 2 to 4 atmospheres absolute.
- Oxygen is then introduced from the pipe 18 into the pressurised stream leaving the pump 10 and flowing through the conduit 12.
- the oxygen is preferably added at a rate 2 to 10 times in excess of the equilibrium value required to saturate the liquid in dissolved oxygen at the prevailing pressure in the conduit 12.
- the majority of the oxygen introduced through the conduit 18 into the stream 12 remains undissolved and a dispersion of relatively coarse bubbles of oxygen in water is formed immediately downstream of the union of the pipe 18 with the conduit 12.
- the velocity of the stream in this region of the conduit 12 is arranged to be less than that of the velocity of sound in the dispersion but sufficient for the gas bubbles to remain dispersed by turbulence. We have found that should the velocity be too low slug flow or even stratification will be created and such conditions must be avoided.
- the limiting value below which slug flow occurs can be determined empirically for any particular apparatus and is related to the size range of bubbles present. In general, the limiting value will not be less than about 2 metres per second. In the region between the upstream end and the throat 22 of the venturi 20, the velocity of the stream of gas-in-liquid dispersion increases and reaches a value in excess of the velocity of sound in the dispersion.
- a shockwave is created within the said region of the venturi 20.
- the relatively coarse bubbles of oxygen are sheared into smaller or finer bubbles by the turbulence resulting from the shockwave. This helps to dissove a small additional amount of oxygen in the water.
- the pressurised stream is decelerated as the venturi widens until it is returned to a subsonic velocity which is still sufficient to maintain the bubbles in dispersion in the stream..
- the length of the conduit 12 is chosen to dissolve the optimum amount of gas in the stream having regard to the pressure drop that occurs along the conduit.
- each orifice 16 of the sparge pipe 14 As the stream passes through the orifices 16 of the sparge pipe 14 so it is once again accelerated to a velocity in excess of that of the velocity of sound in the dispersion. Accordingly, a second shockwave is created and this shockwave is effective to create large numbers of very small oxygen bubbles as the stream enters and mixes withthe main volume 4 of water.
- the orifices 16 each typically have a diameter in the range 6mm to 50mm or more. A dispersion of oxygen bubbles in the water leaves each orifice 16 in the form of a divergent jet.
- the pressurising of the stream increases the amount of dissolved oxygen that can be held in equilibrium with undissolved oxygen in the stream and also creates kinetic energy in the stream which is utilised help dissolve the bubbles of gas that are carried in the dispersion.
- the size of gas bubbles entering the main body of liquid is in the range 0.01 to 0.15 mm.
- the outlet aperture 24 As the stream flows along the conduit 12 where the outlet aperture 24 is located so there is a tendency for the liquid to flow in a straight line while the gas having relatively little momentum tends to disengage from the liquid (particularly the larger bubbles) and flow into the inlet of the conduit 26 at the side of the conduit 12. There is thus some disengagement of gas from the dispersion.
- the gas may carry with it a small or insubstantial amount of liquid entrained in the gas.
- the suction created by the venturi 20 is effective to draw this gas into the conduit 26 and hence into the throat 20 of the venturi 22.
- the Valve 28 is set so as to limit the amount of oxygen that is recycled in this way to 20 - 60% of that introduced into the conduit 12 through the pipe 18.
- the driving force for dissolving oxygen in the stream is increased and hence the overall power efficiency of dissolving oxygen can be increased.
- the same amount of oxygen can be dissolved at a lower operating pressure in the pump 10.
- in the order of up to 5% to 10% or more of the electrical power required to operate the pump 10 may be so saved.
- the union between the pipe 18 and the conduit 12 may comprise an annular chamber (not shown) circumscribing said conduit 12 and communicating therewith e.g. through orifices in the wall of the conduit.
- An analogous arrangement can be used to introduce gas from the pipe 26 into the throat of the venturi.
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Accessories For Mixers (AREA)
Abstract
Description
- This invention relates to a method and apparatus for dissolving gas in liquid. The invention is particularly but not exclusively concerned with dissolving oxygen or a gas mixture including oxygen as one of its constituents in an aqueous or non-aqueous liquid.
- Our U.K. patent specification No. 1 455 567 discloses a process for treating liquid, including the steps of taking a stream of the liquid, pressurising the stream, introducing a treatment gas into the pressurised stream so as to dissolve therein some of the gas, and introducing the stream containing dissolved and undissolved gas into a volume of the liquid under turbulent conditions such that the undissolved gas enters the volume of liquid in the form of fine bubbles that either dissolve or are consummed within the volume of liquid.
- The method described in the aforesaid U.K. patent specification has been successful technically and commercially, particularly as a means of dissolving oxygen in waste water so as to improve the treatment of sewage. We attribute this success at least in part to the fact that the process permits much more gas to be retained in the body of the liquid than prior methods operating with the same power consumption. By using the stream as a carrier of gas bubbles a significantly higher quantity of gas can be successfully carried in the stream into the main volume of liquid and dissolved therein without pressurising that volume of liquid than if the amount of gas carried in the stream is merely limited to the theoretical amount needed to produce a fully saturated liquid at equilibrium. This result can be obtained without the need to introduce the stream into the main volume of liquid at the location under the large hydrostatic head.
- We have nonetheless been looking to improve the efficiency of the method and apparatus described in our U.K. patent specification No. 1 455 567, and it is an aim of the present invention to provide such a method and apparatus for achieving this end.
- Accordingly, there is provided a method of dissolving gas in a liquid, comprising the steps of pressurising a stream of liquid, introducing the gas into the pressurised stream, creating turbulence in the stream so as to dissolve therein some of the gas and to form a dispersion of undissolved gas bubbles in the liquid, transporting said stream as a dispersion of gas bubbles in the liquid to at least one outlet in a volume of the liquid at a substantially lower pressure than that to which said stream is subjected, and introducing the stream through the said outlet into the volume of liquid such that resulting turbulence causes substantially all the remaining undissolved gas bubbles to dissolve in the volume of liquid or be consumed thereby, wherein some of the gas carried in the stream is taken therefrom at a relatively downstream position and is returned to said stream at a relatively upstream position.
- The invention also provides apparatus for dissolving gas in a liquid comprising means (e.g. a pump) for pressurising a stream of liquid, a vessel for holding a volume of liquid in which gas is to be dissolved, a conduit placing the outlet of the pressurising means in communication with at least one nozzle (or the like) for introducing the stream of pressurised liquid into the volume of liquid, means for introducing gas into the stream flowing through the conduit, means for creating turbulence in the stream so as to dissolve therein some of the gas and to form a dispersion of undissolved gas bubbles in the liquid, means for taking some of the gas from the stream at a relatively downstream position in the conduit, and means for returning said gas to the conduit at a relatively upstream position.
- The method and apparatus according to the invention make it possible to provide an enhanced ratio of mass of gas to mass of liquid in the stream and thereby increase the dissolving efficiency of the method described in our U.K. patent specification 1 455 567. The benefit of an increased efficiency of dissolving gas may be reaped, if desired, in meeting a particular demand for dissolved gas at a lower power consumption (i.e. by subjecting the stream to a lower pressure) than would be needed if the method described in the aforesaid patent specification were used. Preferably, up to about 60% by volume of the gas originally introduced into the stream is taken therefrom and is returned to the relatively upstream position. The gas is preferably separated from said stream. Preferably, to enable such gas to be separated and returned there is an outlet aperture for gas from the conduit at said relatively downstream position. As the dispersion of gas bubbles in the liquid flows past the outlet aperture so some of the gas tends naturally to flow through the outlet aperture out of said conduit and into a pipe leading from the outlet aperture back to the relatively upstream location of the conduit. In one preferred embodiment of the apparatus according to the invention the pipe terminates in the throat of a venturi through which the said stream flows, thereby obviating the need to supply any external pump to draw the gas from the relatively downstream location of the conduit and return it to a relatively upstream location. If desired, the gas being returned to the liquid stream may be combined with the gas being introduced therein for the first time.
- The said pipe leading from the relatively downstream location of the conduit to the location relatively upstream thereof preferably has a restriction therein so as to limit the amount of gas that is recycled. Preferably, the restriction is provided by a flow control valve which is typically manually operable.
- It is not necessary to recombine the recycled gas with the incoming gas. One alternative is to introduce the recycled gas downstream of where it is first introduced. Preferably, the main inlet for the gas is at a region where the resulting mixture of gas and liquid travels at a velocity less than that of sound in said mixture. The stream is then preferably accelerated to a supersonic velocity to create a shock wave effective to reduce the size of the gas bubbles in the stream and thereby to form a dispersion of particularly small gas bubbles in the liquid. Such shock wave can be created by passing the stream through a restriction in the conduit. The restriction may be provided by the venturi that is used to draw recycled gas into the stream. The velocity of sound in a dispersion of gas in liquid is substantially less than that of the sound in the gas itself and for oxygen-water systems will be in the order of 50 feet per second. The resulting shockwave as the dispersion of gas and liquid goes supersonic is found to be particularly effective in causing the gas to be formed into bubbles of a relatively small size.
- Downstream of where the shock wave is created the velocity of the stream is preferably reduced once again to below supersonic velocity. Preferably, however, the velocity of the stream is increased to a value above that of the velocity of sound through the dispersion at a region immediately upstream of the said outlet so as to create a second shock wave effective to reduce further the size of the gas bubbles. The second shock wave is preferably created by passing the stream through another restriction, typically immediately upstream of the or each outlet. The second shock wave is effective to reduce the size of the bubbles even further immediately before the dispersion of gas in the liquid enters the main volume of liquid. Typically the main volume of the liquid is kept in a tank open to the atmosphere.
- The outlet typically takes the form of a pipe having one or more orifices therein through which the gas-in-liquid dispersion enters the main volume of liquid.
- The method and apparatus according to the invention are now described by way of example with reference to the accompanying drawings, in which:
- Figure 1 is a schematic diagram illustrating an apparatus for oxygenating water having a biochemical oxygen demand, and:
- Figure 2 is a end view of a sparge pipe forming part of the apparatus shown in Figure 1.
- Referring to Figures 1 and 2 of the accompanying drawings, an open topped
tank 2 contains a volume 4 of waste water having a biochemical oxygen demand. Near its bottom, thetank 2 has anoutlet 6 communicating with apipe 8 which terminates at the inlet end of apump 10 adapted to pressurise liquid flowing there through. The outlet of thepump 10 communicates with anelongate conduit 12 which terminates in asparge pipe 14 located in the volume 4 of the liquid at a region near to the bottom and to one side thereof. Thepipe 14 has a plurality ofoutlet orifices 16 which face towards the other side of the tank. Instead of thepipe 14, a single outlet nozzle may be employed. - An
oxygen supply pipe 18 terminates in theconduit 16 at a region thereof near to and downstream of the outlet of thepump 10. The oxygen is introduced into the stream flowing through theconduit 12 from thepipe 18. The oxygen is typically supplied from a source (not shown) at an elevated pressure sufficient to enable the oxygen to enter the pressurised stream. The source may be one or more cylinders of compressed, gaseous oxygen or a vacuum insulated evaporator of liquid oxygen. - Downstream of the union of the
pipe 18 and theconduit 12 is aventuri 20 having athroat 22. Aconduit 26 terminates at one end in thethroat 22 of theventuri 20 and at its other end in anoutlet aperture 24 formed in the wall of theconduit 12 at a downstream region of theconduit 12 near to thepipe 14. In operation, flow of liquid through theventuri 20 causes a reduction in the static pressure at thethroat 22 such that gas that disengages from the liquid and enters theconduit 26 is drawn along theconduit 26 in the direction of theventuri 20 and is introduced into the liquid flowing through theventuri 20. Typically, it is the larger bubbles of gas that disengage from the stream of liquid and enter theconduit 26. Thus, the dissolving efficiency is increased. Aflow control valve 28 is located in thepipe 26 and is manually adjustable to control the rate at which gas is recycled from theaperture 24 to theventuri 20. Typically the rate of recycle is selected to be from 20 to 60% of the rate at which gas is introduced into theconduit 12 from thepipe 18. - In order to start operation of the apparatus shown in Figure 1, the
pump 10 is energised and it withdraws a stream of water from thetank 2. Thepump 10 is of the kind able to raise the pressure of the liquid passing therethrough to a pressure in therange 2 to 4 atmospheres absolute. Oxygen is then introduced from thepipe 18 into the pressurised stream leaving thepump 10 and flowing through theconduit 12. The oxygen is preferably added at arate 2 to 10 times in excess of the equilibrium value required to saturate the liquid in dissolved oxygen at the prevailing pressure in theconduit 12. Thus, the majority of the oxygen introduced through theconduit 18 into thestream 12 remains undissolved and a dispersion of relatively coarse bubbles of oxygen in water is formed immediately downstream of the union of thepipe 18 with theconduit 12. The velocity of the stream in this region of theconduit 12 is arranged to be less than that of the velocity of sound in the dispersion but sufficient for the gas bubbles to remain dispersed by turbulence. We have found that should the velocity be too low slug flow or even stratification will be created and such conditions must be avoided. The limiting value below which slug flow occurs can be determined empirically for any particular apparatus and is related to the size range of bubbles present. In general, the limiting value will not be less than about 2 metres per second. In the region between the upstream end and thethroat 22 of theventuri 20, the velocity of the stream of gas-in-liquid dispersion increases and reaches a value in excess of the velocity of sound in the dispersion. Accordingly, a shockwave is created within the said region of theventuri 20. As a result, the relatively coarse bubbles of oxygen are sheared into smaller or finer bubbles by the turbulence resulting from the shockwave. This helps to dissove a small additional amount of oxygen in the water. After passing through thethroat 22 of theventuri 20, the pressurised stream is decelerated as the venturi widens until it is returned to a subsonic velocity which is still sufficient to maintain the bubbles in dispersion in the stream.. As the stream flows along theconduit 12 so there is a further gradual dissolution of bubbles of oxygen in the water. The length of theconduit 12 is chosen to dissolve the optimum amount of gas in the stream having regard to the pressure drop that occurs along the conduit. As the stream passes through theorifices 16 of thesparge pipe 14 so it is once again accelerated to a velocity in excess of that of the velocity of sound in the dispersion. Accordingly, a second shockwave is created and this shockwave is effective to create large numbers of very small oxygen bubbles as the stream enters and mixes withthe main volume 4 of water. Theorifices 16 each typically have a diameter in the range 6mm to 50mm or more. A dispersion of oxygen bubbles in the water leaves eachorifice 16 in the form of a divergent jet. Such is the size of the bubbles entering the main volume 4 of water and the turbulence created therein by sparging the stream of liquid through theorifices 16 that most of the remaining oxygen dissolves in the main volume of liquid or is consumed thereby without any substantial quantities of oxygen being discharged undissolved from the surface of the liquid in thetank 2. (It can be appreciated that the pressurising of the stream increases the amount of dissolved oxygen that can be held in equilibrium with undissolved oxygen in the stream and also creates kinetic energy in the stream which is utilised help dissolve the bubbles of gas that are carried in the dispersion.) Typically, the size of gas bubbles entering the main body of liquid is in the range 0.01 to 0.15 mm. - By introducing the oxygen into the stream through the
conduit 18 rather than at thethroat 22 of theventuri 20 use is made of the shock wave created as the velocity of the dispersion of oxygen bubbles in water reaches a supersonic value. If all the oxygen were introduced into the pressurised stream through thethroat 22 of theventuri 20 no shock wave is produced upstream. - As the stream flows along the
conduit 12 where theoutlet aperture 24 is located so there is a tendency for the liquid to flow in a straight line while the gas having relatively little momentum tends to disengage from the liquid (particularly the larger bubbles) and flow into the inlet of theconduit 26 at the side of theconduit 12. There is thus some disengagement of gas from the dispersion. Typically, the gas may carry with it a small or insubstantial amount of liquid entrained in the gas. The suction created by theventuri 20 is effective to draw this gas into theconduit 26 and hence into thethroat 20 of theventuri 22. TheValve 28 is set so as to limit the amount of oxygen that is recycled in this way to 20 - 60% of that introduced into theconduit 12 through thepipe 18. By so increasing the proportion of undissolved oxygen bubbles in the stream in that length of theconduit 12 between the outlet of theventuri 20 and the portion of theconduit 12 where theoutlet 24 is located, the driving force for dissolving oxygen in the stream is increased and hence the overall power efficiency of dissolving oxygen can be increased. For optimum efficiency it may be possible to use a shorter length of conduit between theventuri 20 and theoutlet 24 than if no such oxygen were recycled. Alternatively, the same amount of oxygen can be dissolved at a lower operating pressure in thepump 10. Typically, in the order of up to 5% to 10% or more of the electrical power required to operate thepump 10 may be so saved. - If desired, the union between the
pipe 18 and theconduit 12 may comprise an annular chamber (not shown) circumscribing saidconduit 12 and communicating therewith e.g. through orifices in the wall of the conduit. An analogous arrangement can be used to introduce gas from thepipe 26 into the throat of the venturi.
Claims (11)
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
GB8401781 | 1984-01-24 | ||
GB848401781A GB8401781D0 (en) | 1984-01-24 | 1984-01-24 | Dissolving gas liquid |
Publications (3)
Publication Number | Publication Date |
---|---|
EP0152201A2 true EP0152201A2 (en) | 1985-08-21 |
EP0152201A3 EP0152201A3 (en) | 1987-08-05 |
EP0152201B1 EP0152201B1 (en) | 1991-09-04 |
Family
ID=10555427
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP85300488A Expired - Lifetime EP0152201B1 (en) | 1984-01-24 | 1985-01-24 | Dissolving gas in liquid |
Country Status (9)
Country | Link |
---|---|
EP (1) | EP0152201B1 (en) |
JP (1) | JPS60222136A (en) |
KR (1) | KR920000537B1 (en) |
AU (1) | AU578063B2 (en) |
CA (1) | CA1257195A (en) |
DE (1) | DE3583950D1 (en) |
GB (2) | GB8401781D0 (en) |
IN (1) | IN163926B (en) |
ZA (1) | ZA85364B (en) |
Cited By (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP0341878A1 (en) * | 1988-05-11 | 1989-11-15 | Zeneca Limited | Fermentation process and apparatus |
GB2390984A (en) * | 2002-07-20 | 2004-01-28 | Jack Elliot Taylor | Jet aeration system for dissolving gases into a liquid wherein the gases are introduced to the liquid before the liquid is pumped through a liquid nozzle |
WO2009123456A3 (en) * | 2008-04-02 | 2010-09-16 | Schuitemaker Machines B.V. | Method, filling station and storage holder for providing grit |
WO2016071691A1 (en) * | 2014-11-07 | 2016-05-12 | Oxy Solutions As | Apparatus for dissolving gas into a liquid |
Families Citing this family (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
IL88116A (en) * | 1987-10-23 | 1992-11-15 | Techno Bio Kk | Method for introducing and bonding gas into water,apparatus for carrying out the method,and water produced by the method |
KR100379298B1 (en) * | 2001-01-02 | 2003-04-07 | 동림산업 주식회사 | Pipe line system for feeding powder |
Citations (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE739665C (en) * | 1936-09-18 | 1943-10-01 | Sulzer Ag | Device for impregnating fruit juices or other non-alcoholic beverages |
DE1204636B (en) * | 1960-02-26 | 1965-11-11 | Shell Int Research | Method and device for mixing gases at supersonic speed |
US3778038A (en) * | 1970-03-06 | 1973-12-11 | Dresser Ind | Method and apparatus for mixing and modulating liquid fuel and intake air for an internal combustion engine |
US4124660A (en) * | 1975-08-25 | 1978-11-07 | Cem-Compagni Electro-Mecanique | Process and apparatus for mixing gases and liquids |
US4163712A (en) * | 1973-01-08 | 1979-08-07 | Boc Limited | Treatment of liquid |
WO1981001700A1 (en) * | 1979-12-18 | 1981-06-25 | Boc Ltd | Method and apparatus for dissolving gas in a liquid |
Family Cites Families (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB1455567A (en) * | 1973-01-08 | 1976-11-17 | Boc International Ltd | Treatment of liquid |
JPS5328257B2 (en) * | 1974-04-15 | 1978-08-14 | ||
ZA793185B (en) * | 1978-08-30 | 1981-02-25 | Dorr Oliver Inc | Apparatus and process for dissolution of gases in liquid |
GB2117657A (en) * | 1982-03-16 | 1983-10-19 | Jack Anthony Ewen | Equipment for carbonating water |
GB8401779D0 (en) * | 1984-01-24 | 1984-02-29 | Boc Group Plc | Dissolving gas liquid |
-
1984
- 1984-01-24 GB GB848401781A patent/GB8401781D0/en active Pending
-
1985
- 1985-01-16 ZA ZA85364A patent/ZA85364B/en unknown
- 1985-01-18 IN IN41/MAS/85A patent/IN163926B/en unknown
- 1985-01-23 JP JP60010702A patent/JPS60222136A/en active Granted
- 1985-01-23 CA CA000472616A patent/CA1257195A/en not_active Expired
- 1985-01-23 KR KR1019850000394A patent/KR920000537B1/en not_active IP Right Cessation
- 1985-01-23 AU AU38001/85A patent/AU578063B2/en not_active Ceased
- 1985-01-24 EP EP85300488A patent/EP0152201B1/en not_active Expired - Lifetime
- 1985-01-24 GB GB08501799A patent/GB2153245B/en not_active Expired
- 1985-01-24 DE DE8585300488T patent/DE3583950D1/en not_active Expired - Fee Related
Patent Citations (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE739665C (en) * | 1936-09-18 | 1943-10-01 | Sulzer Ag | Device for impregnating fruit juices or other non-alcoholic beverages |
DE1204636B (en) * | 1960-02-26 | 1965-11-11 | Shell Int Research | Method and device for mixing gases at supersonic speed |
US3778038A (en) * | 1970-03-06 | 1973-12-11 | Dresser Ind | Method and apparatus for mixing and modulating liquid fuel and intake air for an internal combustion engine |
US4163712A (en) * | 1973-01-08 | 1979-08-07 | Boc Limited | Treatment of liquid |
US4124660A (en) * | 1975-08-25 | 1978-11-07 | Cem-Compagni Electro-Mecanique | Process and apparatus for mixing gases and liquids |
WO1981001700A1 (en) * | 1979-12-18 | 1981-06-25 | Boc Ltd | Method and apparatus for dissolving gas in a liquid |
Cited By (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP0341878A1 (en) * | 1988-05-11 | 1989-11-15 | Zeneca Limited | Fermentation process and apparatus |
US5198362A (en) * | 1988-05-11 | 1993-03-30 | Imperial Chemical Industries, Plc | Sterile aerobic fermentation process |
GB2390984A (en) * | 2002-07-20 | 2004-01-28 | Jack Elliot Taylor | Jet aeration system for dissolving gases into a liquid wherein the gases are introduced to the liquid before the liquid is pumped through a liquid nozzle |
WO2009123456A3 (en) * | 2008-04-02 | 2010-09-16 | Schuitemaker Machines B.V. | Method, filling station and storage holder for providing grit |
WO2016071691A1 (en) * | 2014-11-07 | 2016-05-12 | Oxy Solutions As | Apparatus for dissolving gas into a liquid |
CN107427793A (en) * | 2014-11-07 | 2017-12-01 | 溶液充氧公司 | For dissolving gas into the equipment in liquid |
US11110407B2 (en) * | 2014-11-07 | 2021-09-07 | Oxy Solutions As | Apparatus for dissolving gas into a liquid |
Also Published As
Publication number | Publication date |
---|---|
EP0152201B1 (en) | 1991-09-04 |
JPH0547252B2 (en) | 1993-07-16 |
CA1257195A (en) | 1989-07-11 |
GB8401781D0 (en) | 1984-02-29 |
DE3583950D1 (en) | 1991-10-10 |
KR850005286A (en) | 1985-08-24 |
JPS60222136A (en) | 1985-11-06 |
AU3800185A (en) | 1985-08-01 |
AU578063B2 (en) | 1988-10-13 |
EP0152201A3 (en) | 1987-08-05 |
GB2153245B (en) | 1987-03-18 |
GB2153245A (en) | 1985-08-21 |
ZA85364B (en) | 1986-05-28 |
KR920000537B1 (en) | 1992-01-16 |
GB8501799D0 (en) | 1985-02-27 |
IN163926B (en) | 1988-12-10 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
US4639340A (en) | Dissolving gas in a liquid | |
US4752383A (en) | Bubble generator | |
CA1283651C (en) | Gas dispersion process and system | |
US4163712A (en) | Treatment of liquid | |
KR0173996B1 (en) | Apparatus for dissolving a gas into and mixing the same with a liquid | |
US5057230A (en) | Dissolution of gas | |
US4863643A (en) | Apparatus for dissolution of gas in liquid | |
KR20030024631A (en) | Process and device for aerating a liquid with gas | |
US4211733A (en) | Gas-liquid mixing process and apparatus | |
JPH084731B2 (en) | Gas-liquid mixing device | |
US6241897B1 (en) | Dissolution of gas | |
EP0389230B1 (en) | Dissolution of gas | |
EP0152201B1 (en) | Dissolving gas in liquid | |
US4597877A (en) | Process and equipment for water treatment | |
US6546962B1 (en) | Introduction of air into injection water | |
JPH10225696A (en) | Pressurization type ozone treating device | |
JP2001259395A (en) | Aerator | |
GB2072027A (en) | Transfer of oxygen into waste water | |
WO2001062392A1 (en) | Sparging nozzle assembly for aerated reaction vessels and method for operating such vessels | |
SU1699616A1 (en) | Method for aeration of liquid | |
JPS62125831A (en) | Fine foam generator | |
CN216799410U (en) | Dissolved ozone adding system | |
JP2976875B2 (en) | Ozone water production equipment | |
JP2023110186A (en) | Gas-dissolved liquid generation device | |
UA119906C2 (en) | DEVICE FOR AERATION AND METHOD OF AERATION OF LARGE AMOUNT OF WATER |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
PUAI | Public reference made under article 153(3) epc to a published international application that has entered the european phase |
Free format text: ORIGINAL CODE: 0009012 |
|
AK | Designated contracting states |
Designated state(s): BE DE FR IT NL |
|
17P | Request for examination filed |
Effective date: 19860218 |
|
PUAL | Search report despatched |
Free format text: ORIGINAL CODE: 0009013 |
|
AK | Designated contracting states |
Kind code of ref document: A3 Designated state(s): BE DE FR IT NL |
|
17Q | First examination report despatched |
Effective date: 19890510 |
|
GRAA | (expected) grant |
Free format text: ORIGINAL CODE: 0009210 |
|
ITF | It: translation for a ep patent filed |
Owner name: BARZANO' E ZANARDO MILANO S.P.A. |
|
AK | Designated contracting states |
Kind code of ref document: B1 Designated state(s): BE DE FR IT NL |
|
ET | Fr: translation filed | ||
REF | Corresponds to: |
Ref document number: 3583950 Country of ref document: DE Date of ref document: 19911010 |
|
PLBE | No opposition filed within time limit |
Free format text: ORIGINAL CODE: 0009261 |
|
STAA | Information on the status of an ep patent application or granted ep patent |
Free format text: STATUS: NO OPPOSITION FILED WITHIN TIME LIMIT |
|
26N | No opposition filed | ||
PGFP | Annual fee paid to national office [announced via postgrant information from national office to epo] |
Ref country code: NL Payment date: 19981231 Year of fee payment: 15 Ref country code: FR Payment date: 19981231 Year of fee payment: 15 |
|
PGFP | Annual fee paid to national office [announced via postgrant information from national office to epo] |
Ref country code: DE Payment date: 19990104 Year of fee payment: 15 |
|
PGFP | Annual fee paid to national office [announced via postgrant information from national office to epo] |
Ref country code: BE Payment date: 19990118 Year of fee payment: 15 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: BE Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20000131 |
|
BERE | Be: lapsed |
Owner name: THE BOC GROUP P.L.C. Effective date: 20000131 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: NL Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20000801 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: FR Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20000929 |
|
NLV4 | Nl: lapsed or anulled due to non-payment of the annual fee |
Effective date: 20000801 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: DE Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20001101 |
|
REG | Reference to a national code |
Ref country code: FR Ref legal event code: ST |