EP0152201B1

EP0152201B1 - Dissolving gas in liquid

Info

Publication number: EP0152201B1
Application number: EP85300488A
Authority: EP
Inventors: Michael Ernest Garrett
Original assignee: BOC Group Ltd
Current assignee: BOC Group Ltd
Priority date: 1984-01-24
Filing date: 1985-01-24
Publication date: 1991-09-04
Anticipated expiration: 2005-01-24
Also published as: IN163926B; AU578063B2; JPH0547252B2; KR850005286A; ZA85364B; GB2153245B; JPS60222136A; GB8401781D0; EP0152201A2; DE3583950D1; GB2153245A; CA1257195A; AU3800185A; EP0152201A3; GB8501799D0; KR920000537B1

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. Such methods are disclosed in WO 81/01700, UK-A-1 455 567 and US-A-4 163 712.
UK-A-1 455 567 and US-A- 4 163 712 disclose 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 consumed within the volume of liquid.
The method described in the aforesaid publications 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 the aforesaid publications 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 taking a stream of liquid from a volume of the liquid, pressurising the stream, 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 said volume of the liquid 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 position remote from and downstream of where the turbulence is created and is returned to said stream at a relatively upstream position such that it re-enters the turbulent region of the stream.
The invention also provides apparatus for dissolving gas in a liquid comprising means (e.g. a pump) for pressurising a stream of liquid having an inlet communicating with 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, wherein the conduit has, downstream of the means for creating turbulence, an outlet communicating with an inlet at a position such that the gas is returned to the region of turbulence in the stream.
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 UK-A-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 as 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 15m s⁻¹ (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 was 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 an 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, 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 12 at a region thereof near to an 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.
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. In operation, 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. Typically, it is the larger bubbles of gas that disengage from the stream of liquid and enter the conduit 26. Thus, 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.
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 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 13 to 26 x 10⁵ Pa (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. Thus, 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. Accordingly, a shockwave is created within the said region of the venturi 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 dissolve a small additional amount of oxygen in the water. After passing through the throat 22 of the venturi 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 the conduit 12 so there is a further gradual dissolution of bubbles of oxygen in the water. 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. 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. 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 the orifices 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 the tank 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 to 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 the throat 22 of the venturi 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 the throat 22 of the venturi 20 no shock wave is produced upstream.
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. Typically, 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. By so increasing the proportion of undissolved oxygen bubbles in the stream in that length of the conduit 12 between the outlet of the venturi 20 and the portion of the conduit 12 where the outlet 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 the venturi 20 and the outlet 24 than if no such oxygen were recycled. Alternatively, the same amount of oxygen can be dissolved at a lower operating pressure in the pump 10. Typically, 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.
If desired, 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.

Claims

A method of dissolving gas in a liquid, comprising the steps of taking a stream of liquid from a volume of the liquid, pressurising the stream 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 said volume of the liquid 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, characterised in that some of the gas carried in the stream is taken therefrom at a position remote from and downstream of where the turbulence is created and is returned to said stream at a relatively upstream position such that it re-enters the turbulent region of the stream.
A method as claimed in claim 1, in which up to about 60% by volume of the gas originally introduced into the stream is taken therefrom and is returned to the said turbulent region.
A method as claimed in claim 1 or claim 2, in which said turbulent region is defined by the throat of a venturi through which said stream flows, and there is a restricted gas passage affording communication between said relatively downstream position and the throat of the venturi; whereby gas disengaging from said stream is drawn from said relatively downstream position into the throat of the venturi.
A method as claimed in claim 3, in which a mixture of gas-in-liquid is formed and the resulting mixture travels at first at a velocity less than that of sound in said mixture, the mixture subsequently being accelerated to a supersonic velocity, whereby a shock wave is created and gas bubbles in the stream are reduced in size.
A method as claimed in claim 4, wherein said shock wave is created by passing the stream through said venturi, the gas being introduced into the pressurised stream upstream of the venturi.
A method as claimed in claim 5, wherein the velocity of the stream is decreased to a subsonic velocity downstream of where said shock wave is created, and then increased again at said outlet to a supersonic velocity whereby a second shock wave is created.
Apparatus for dissolving gas in liquid, comprising means (10) for pressurising a stream of liquid, having an inlet communicating with a vessel (2) for holding a volume (4) of liquid in which gas is to be dissolved, a conduit (12) placing the outlet of the pressurising means (10) in communication with at least one nozzle (14) in the volume (4) of liquid, means (18) for introducing gas into the stream flowing through the conduit (12), means (22) 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, characterised in that the conduit (12) has, downstream of the means (22) for creating turbulence, an outlet (24) communicating with an inlet (20) at a position such that the gas is returned to the region of turbulence in the stream.
Apparatus as claimed in claim 7, in which a restricted pipe (26) affords communication between said outlet (24) and said inlet (20).
Apparatus as claimed in claim 8, in which said pipe (26) terminates in the throat (20) of a venturi (22) through which the said stream flows in operation of the apparatus.
Apparatus as claimed in claim 8 or claim 9, in which said pipe (26) terminates in a chamber circumscribing the throat of a venturi and communicating therewith, the said stream passing through the venturi in operation of the apparatus.
Apparatus as claimed in claim 9 or claim 10, in which said means (18) for introducing gas into the stream communicates with the conduit (12) upstream of the venturi.