Patent Application
20120160333
The present invention relates to the field of multi-phase fluid flows and in particular to introducing gas into a flowing liquid.
Injecting gases into a liquid is desirable in many fields. The ability to inject large quantities of gas into substantial bodies of liquid varies depending on a number of factors, such as turbulence, orifice size etc. The mixing of the gas within the liquid and mass transfer between them are also issues that vary depending on conditions.
Examples of fields where the introduction of a gas into a liquid is desirable are fermentation, industrial and wastewater treatment, clean water treatment and energy generation.
With regard to the treatment of water, a certain concentration of dissolved oxygen (DO) is necessary in any body of water to ensure the occurrence of self purification processes. If the oxygen requirement cannot be supplied naturally, then the purification processes cease and the water turns septic. Engineering techniques exist to avoid this extreme condition occurring. Assisted aeration maintains DO levels and accelerates the purification processes. An added advantage of assisted aeration may be the removal of volatile organic compounds which are ultimately responsible for tastes and odours.
There are several different designs of aerators. They are classified into two broad types: surface mechanical agitator devices (which are better suited for shallow tanks as they entrain air at the water surface by violent agitation) and dispersed air units. In the latter, the air is introduced in the aeration tank under the form of bubbles. The main design issues associated with all dispersed air systems are that they have to generate fine bubbles in order to ensure large interfacial area and therefore enhanced oxygen transfer from the gas to the liquid. At the same time, the practical problems and large power requirements they entail have to be minimised or at least reduced. Comparisons between the various types and relative advantages are reported in a standardised form as the Standard Oxygen Transfer Efficiency (SOTE) which represents the fraction of oxygen brought in contact with the water that actually dissolves into the water at standard temperature and pressure conditions, the Standard Oxygen Transfer Rate (SOTR) which represents the rate of oxygen transfer observed at standard temperature and pressure when the DO level in the water is initially zero, and the Standard Aeration Efficiency (SAE) which represents the energy consumed in dissolving a specified amount of oxygen.
The diffusers which belong to the family of dispersed air systems, are the most commonly used aerators. Fine air bubbles are injected at the bottom of an aeration tank via porous ceramic plates or perforated membranes. These diffusers rely on an energy intensive process (the compression of gas) but provide a high performance in terms of oxygen transfer (SAE around 3.6-3.7 kg/kWh).
Another category of dispersed air systems is venturi-based devices. Their operating theory is based on the Bernoulli's principle. The water phase flows through a converging section before being accelerated in the throat (or constriction), thus creating reduced pressures and allowing a continuous air stream to be entrained into the water system by a pressure difference. The mixture air+water penetrates the diverging section and the oxygen transfer from the gaseous to the liquid phases begins. These devices are less expensive in terms of energy consumption than the diffusers but they suffer an inferior performance in terms of oxygen transfer from air to liquid (SAE around 0.9-2.3 kg/kWh).
The aeration performance of a given device depends not only on the supply of oxygen (i.e. in the form of fine bubbles) in the treatment liquid, but also on the thorough and uniform distribution of the gas within the diffusion region. There are clear advantages to the use of a simple cylindrical geometry, as in venturi-based aerators, in terms of reducing energy losses. However, this argument becomes less clear when large volumes of air are introduced along the tube wall. In this case, a major difficulty with such devices is the tendency of the air bubbles to accumulate in the boundary layer at the walls of the pipe. This phenomenon may be responsible for creating instabilities in the diverging section resulting in separation, stall and high energy losses.
The introduction of a gas into a liquid is also known in the field of power generation. WO03/081029 for example discloses a gaseous transmission fluid that is used to drive a turbine and gets its kinetic energy from being sucked into a venturi in which liquid flows. A problem with such a device is that it requires high suction pressures to effect delivery of the gas directly into the venturi and to generate a pressure differential that is large enough for satisfactory turbine operation. Such high pressures are difficult to achieve with a venturi and this document addresses the problem by providing a fluid directing arrangement prior to the venturi for imparting angular momentum to the primary liquid flow as it enters the venturi. This provides a reduced pressure which helps entrain the driving gas. However it has the drawback of additional infrastructure in the path of the liquid flow.
In general, when a gas is injected into a liquid there is a propensity for bubbles to congregate on upper surfaces and to coalesce with each other. These events inhibit good mixing and mass transfer between the two phases. They may also result in dramatic accumulation of air in the device leading to saturation and stall phenomenon thus inhibiting further gas injection into the liquid flow. Recirculation zones may form in the liquid flow generating substantial energy losses. These are typical challenges that need to be addressed in this field.
It would be desirable to be able to introduce gas efficiently into a liquid in relatively large amounts while avoiding the problems of stalling of the device due to coalescence of bubbles and increased resistance to flow caused by large zones of flow separation. It would also be desirable to achieve a well-distributed mixture of liquid-gas bubbles within the device, while keeping energy consumption low.
Viewed from a first aspect, the present invention provides an apparatus for introducing gas into a liquid comprising: a conduit; a fluid directing formation arranged within said conduit and defining a plurality of discrete channels within said conduit, said channels being isolated from each other in a direction perpendicular to a direction of fluid flow through said channels, each channel providing a flow accelerating constriction to said fluid flow such that fluid flowing in each of said channels is caused to accelerate as it flows through said flow accelerating constrictions; wherein at least some of said channels comprise orifices within said flow accelerating constrictions, said orifices being in fluid communication with a gas source, such that said gas is drawn through said orifices to be entrained in said fluid flow by virtue of a reduced pressure in said channels caused by said fluid flow.
The present invention recognises the problems associated with introducing gas into a liquid, such as the coalescence of the bubbles resulting in increased resistance to flow and possibly stalling of the device. It recognises that this problem can be particularly acute where a large volume of gas is introduced and where it is introduced in a flow accelerating constriction. It addresses this problem by segmenting the flow such that a plurality of discrete channels are provided that are isolated from one another in a direction perpendicular to the overall direction of flow of fluid through the conduit. Thus, the gas is introduced into the liquid in discrete channels, which is a simple yet effective way of helping to avoid the bubbles from coalescing, as portions of the flow are physically isolated from each other. When the portions of the flow later join, the bubbles are distributed across the flow which reduces the risk of them coalescing.
It should be noted that in the above where the term fluid flow is used this may be the liquid flow just prior to and during introduction of the gas and it may also be the two phase flow following introduction of the gas, where the gas is entrained in the liquid.
In some embodiments, said plurality of channels are arranged to segment flow about a central point of said conduit.
Although the channels can be arranged in a number of different ways provided that they segment the flow and thereby ensure that bubbles are introduced into different physically separated portions, it may be advantageous to segment the flow about a central point as such an arrangement segments flow while generally not providing too great an increase in resistance to flow.
In some embodiments, said plurality of channels each have a form of a sector of said conduit.
A particularly advantageous way of splitting the flow is to segment it such that the conduit is separated into sectors. This is a way of segmenting the flow into portions with fairly equal flow patterns, thus each channel can absorb similar amounts of gas assuring a good distribution of the gas within the flow.
In some embodiments, said conduit comprises a flow accelerating constriction, said fluid directing formation being arranged within said flow accelerating constriction.
In some embodiments, the fluid directing formation can itself form the flow accelerating constriction while in others it can be arranged in a flow accelerating constriction. The latter arrangement provides an increased acceleration of the flow and therefore a greater reduction in pressure. Although introducing gas into a flow accelerating constriction provides an increased sucking power it does have the disadvantage that the flow is already constricted and as such, there is more likelihood of the bubbles coalescing. However, the individual channels help ensure the bubbles are introduced into different parts of the flow and thereby help alleviate this problem.
In some embodiments, at least some of said orifices are conduit orifices formed in an outer surface of said conduit at positions corresponding to at least some of said channels.
Although, the orifices can be formed in a number of places, it may be advantageous to form them in the outer surface of the conduit as this is simple to design with the gas being easy to supply to such a formation.
In some embodiments, said conduit orifices are arranged such that adjacent orifices along a length of said conduit are at different circumferential positions on said conduit.
For the orifices that are arranged on the outer surface of the conduit it may be advantageous to arrange them so that they are located at different circumferential positions. This helps the mixing of the gas within the liquid and reduces bubble coalescence as the orifices are located at a distance from each other and it also avoids gas entrained into the conduit via these orifices being introduced directly upstream of a neighbouring orifice at a same circumferential position.
In some embodiments, said conduit orifices are arranged along at least one substantially helical path.
A helical path is a particularly advantageous arrangement as this shape may introduce a rotational component to the flow and also keeps the orifices spread across the circumference of the conduit.
In some embodiments, at least some of said conduit orifices comprise shielding elements for shielding said orifices from said flow, said shielding elements being arranged at an upstream side of said orifices and being at an angle of less than 45° with respect to a direction of flow.
The use of shielding elements arranged at an angle helps divert the flow away from the orifice and allows the gas stream to emerge with greater momentum and align itself to the flow direction. It also enables smaller bubbles to be generated. These effects reduce energy losses and thereby increases the amount of gas that can enter the flow.
In some embodiments, said flow directing formation is hollow and is in fluid communication with said gas source, at least some of said orifices being arranged on said fluid directing formation at a position corresponding to said channels.
Alternatively, or even additionally the flow directing formation may be hollow and be in fluid communication with the gas source with the orifices being arranged on the fluid directing formation. The provision of the fluid directing formation within the flow provides additional possible sites for orifices for introducing gas into the flow. Furthermore, introducing gas from the fluid directing formation means that the gas is introduced towards the middle of the flow and prevents or at least reduces the possibility of bubbles collecting at the edge of the conduit where flow is often slower.
In some embodiments, said fluid directing formation comprises a central structure supporting a plurality of vanes, said plurality of vanes defining said channels.
Although the fluid directing formation can have a number of forms an effective form is a central structure supporting a plurality of vanes, the vanes defining the channels. Such a shape can be aerodynamic and thus, produce little resistance to flow increasing the devices' overall efficiency.
In some embodiments, said fluid directing formation comprises a central structure with a plurality of vanes, said plurality of vanes defining said channels, wherein said plurality of orifices are arranged on said vanes at a region of reduced pressure.
An advantageous place to position the orifices is on the vanes at a region of reduced pressure as this encourages the gas to be sucked into the fluid flow and thus, helps increase the amount of gas that can be introduced.
In some embodiments at least some of said fluid directing formation orifices are located in a region of an apex of a wedge-shaped depression on said vanes.
Providing the orifices towards an apex of a wedge-shaped depression on the vanes allows the gas to spread out into a broad sheet which is swept along the face of the vane, giving a large surface area from which bubbles can be generated.
In some embodiments, said plurality of vanes are arranged at an angle with respect to the direction of flow such that a rotational component is introduced by said vanes to said fluid flowing between them.
It may be advantageous to arrange the vanes at an angle with respect to the direction of flow so that a rotational component is introduced by the vanes. This helps produce a swirling motion which helps mix the gas and liquid and also tends to send the gas towards the centre of the flow stopping it adhering to the edge and restricting the flow. If the flow is oriented horizontally, the rotational acceleration also acts to counteract the effects of gravity by suppressing bubble rise due to buoyancy. This can enhance mass transfer due to the prolonged existence of a bubbly flow. Turbulence in the region downstream of the device may also be reduced leading to reduced energy demands.
In some embodiments, said plurality of vanes are mounted rotationally on said central structure.
Although there are advantages in having vanes that do not move, as moving structures under water may require maintenance, it may be advantageous to mount the vanes rotationally on the central structure so that they themselves can provide a swirling motion to the liquid helping mix the flow and further reduce the likelihood of bubbles coalescing.
In some embodiments, said fluid directing formation has an aerofoil shape with rounded surfaces at an upstream position leading to tapered surfaces.
It may be advantageous if the fluid directing formation has an aerofoil shape as this reduces the resistance to the flow that this formation provides.
In some embodiments, said plurality of vanes have flat inner surfaces.
Vanes with flat inner surfaces are effective for providing channels with low resistance to flow.
In some embodiments, said central structure is between 3 and 6 times as long as a diameter of said conduit and said blades are between one and 3 times as long as said diameter.
The length of the vanes and the central structure affect the flow and bubble coalescence. A long structure separates the flow for a longer time and decreases turbulence, it also increases the extent of the flow experiencing strong strain which is beneficial to bubble break up. However, there is an increased resistance to flow in the constricted region. An advantageous length for the central structure and blades that provide a good balance of these effects is one where the central structure is between 3 and 6 times as long as a diameter of the conduit it is located in, while the blades are between 1 and 3 times as long.
In some embodiments, said orifices are formed on a strip mounted on a surface of said channels.
Although the orifices can be formed in a number of ways they may be formed on a strip mounted on a surface of the channels as this is a convenient way of forming the orifices.
In some embodiments this strip is a flexible permeable membrane which provides an effective way of introducing many gas bubbles into the flow. Flexible permeable membranes are well suited for introducing bubbles of gas into a liquid as they have many small orifices. However, there is a technical prejudice against using these flexible permeable membranes in fluid flow systems as they are quite fragile and where a reduced pressure is used to suck in the gas they can be distorted and possibly break. Furthermore, it is thought that a membrane that is pulled into the constriction of a constricted flow will obstruct the constriction and cause resistance to the fluid flow. However, it has surprisingly been found that these flexible permeable membranes do provide a good mechanism for introducing gas into a liquid flow. Furthermore, they have the advantages of breaking up the liquid/gas interface at the injection point. Furthermore, due to the large number of orifices, lower gas flows through each orifice can be used with the resulting large number of bubbles causing disruption to the flow. This design offers the potential of highly stable flows (low head loss) with high mass transfer characteristics.
In some embodiments, said apparatus further comprises a fluid driveable engine, said fluid driveable engine being arranged in fluid communication between said gas source and said orifices such that gas being drawn from said gas source through said orifices acts to drive said fluid driveable engine.
Where a sufficient amount of gas is able to be drawn into the liquid flow it may be advantageous to use the flow of gas not only to provide a gas liquid mixture but also to drive a fluid drivable engine such as a turbine. If for example this device was located somewhere remotely then this turbine could be used for powering systems that might be needed in association with the device.
Although the apparatus can be used for a number of gas/liquid mixtures it is particularly useful for adding air into water. Aeration of water is a common problem and embodiments of the invention are particularly well suited to providing water aeration devices.
In some embodiments, said gas comprises air and said apparatus further comprising an ozone generator, said ozone generator being arranged in fluid communication between said gas source and said orifices such that at least a portion of said gas being drawn from said gas source through said orifices passes through said ozone generator.
Where the air being drawn into the fluid flow is being used to improve water or other fluid quality by aerating it, this can be made more effective if an ozone generator is used to generate ozone from the oxygen within the air. This will provide better oxygenation and oxidization of polluting materials of the water or other fluid from the same air flow and can be used to increase the fluid quality where this is important.
In some embodiments said fluid drivable engine comprises a turbine for generating electricity and said ozone generator is powered by electricity generated by said turbine or supplied from elsewhere.
Although the ozone generator can be powered in a number of ways, where the air flow is suitable for driving a turbine a particularly advantageous system can be produced whereby the air flow passing through the turbine generates the electricity required by the ozone generator. In this way no external power supply is required for the system and good oxygenation of the flow and oxidization of polluting materials therein can be produced.
In some embodiments, the apparatus comprises a portion of a water treatment plant while in other embodiments it comprises a part of a fermentation apparatus and in others it can form part of an air cooling plant. In the latter case it can be advantageous if a heat exchanger is arranged to cool the inlet air flow prior to it being entrained in the water. Cooler air is denser and thus, greater quantities can be entrained whilst the heat taken out through the heat exchanger can be utilised for other purposes.
A further aspect of the invention provides a method of introducing gas into a liquid comprising the steps of: sending a flow of liquid through a plurality of discrete channels defined by a flow directing formation within a conduit, said fluid directing formation being arranged such that said channels are isolated from each other in a direction perpendicular to a direction of fluid flow through said channels, and each channel providing a flow accelerating constriction to said fluid flow such that fluid flowing in said channels is caused to accelerate as it flows through said constriction; sending a flow of gas to a plurality of orifices arranged within said flow accelerating constrictions of at least some of said channels; wherein said flow of gas is caused to be drawn from said gas source through said orifices by a reduced pressure in said flow accelerating constriction caused by said increased fluid flow rate, to become entrained in said fluid flow.
The present invention will be described further, by way of example only, with reference to embodiments thereof as illustrated in the accompanying drawings, in which:
a shows an aerofoil for a zero angle of attack;
b shows a cross section of the channels generated by the aerofoil of
a shows an aerofoil for a non-zero angle of attack;
b shows a cross section of the channels generated by the aerofoil of
a shows gas entry ports on a blade of an aerofoil;
b shows a cross section through a blade of an aerofoil;
The shape of the fluid directing arrangement 10 is such that it combines high aerodynamic performance with manufacturability. It presents the following key feature: a streamlined structure inserted into a straight pipe with the objective to create a flow constriction.
The fluid directing arrangement 10 has in this embodiment the form of an aerofoil surrounded by blades and has the following characteristics.
It presents a rounded front and a tapering back edge, to reduce resistance to flow.
The blades have rounded outer faces to fit flush within a straight circular pipe, and thereby provide channels that are isolated from each other.
The blades have flat inner faces, providing a low resistance to fluid flow.
As an example, the fluid directing arrangement 10 may have the following characteristics:
Aspect ratio of the aerofoil (length/width): between 3 and 4, preferably 3.5; Length of the aerofoil: between 500 mm and 600 mm preferably 525 mm;
A total of six blades presenting an aspect ratio of between 5 and 7, preferably 6 (20 to 30 mm preferably 25 mm wide and 150 mm to 250 mm preferably 200 mm long);
Diameter of each orifice: between 1.5 and 7.5 mm preferably 2 mm in some embodiments and 6 mm in others.
The constriction ratio is approximately 1:4, and the device is designed to fit within a 100 mm diameter pipe.
The arrangement generates a bubbly two phase flow (dispersed gas/continuous liquid) downstream of the constricted channels. The generation of a bubbly flow has two functions: it reduces the energy required to drive a given gas flow rate, and providing that the bubbles are small enough it promotes mass transfer between the two phases due to high interfacial area density.
In the embodiment of
In the throat of the venturi (or constriction) 60 a continuous gas stream is sucked in via ports located in the individual channels (not shown) that are connected to a gas source due to the pressure drop, and the flow takes the form of several mixed streams originating from each channel and made of continuous liquid phase and dispersed gas bubbles (two-phase flow).
Some of the key parameters of importance affecting the efficiency of the device relate to the total number of suction ports, their dimensions, locations and configurations.
In the diverging cylinder (or expansion) 40 the diameter increases up to a fixed value as it gets nearer to the cylindrical diffuser region 50 and the flow regime becomes more complex. The behaviour of the mixture is strongly influenced by the gas/liquid distribution as it enters this zone. Energy losses are dominated by the generation of turbulence and flow separation. The risk of formation of gas pockets is high with the detrimental consequences of reduced performance and stalling. This shows the strong influence of the expansion design on the overall performance of the device. A long smoothly curving section is preferred, due to the importance to preventing flow separation in this portion.
As an example, a device like this that is used for water aeration may have the following dimension characteristics: for the converging portion, a converging angle of between 14 and 21°, an inlet diameter of between 80 and 120 mm, preferably approximately 100 mm, an outlet diameter of between 40 and 60 mm and preferably approximately 50 mm for the throat, a constriction ratio of approximately 4:1; and for the diverging portion and diffuser region, a diverging angle of between 4° and 8° preferably approximately 6°, an inlet diameter of between 40 and 60 mm and preferably approximately 50 mm, an outlet diameter of between 80 and 120 mm, preferably approximately 100 mm, with the length of the diffuser being between 250 and 350 mm, preferably approximately 300 mm.
Introducing the gas into individual channels ensures that it is distributed evenly within the flow and helps reduce bubble coalescence.
In this embodiment the air is introduced via simple holes located on a strip 70. As the orifices are in this embodiment on the fluid directing arrangement 10 then this arrangement is hollow and is provided with a pipe 80 that is connected to a source of air, and allows air to be sucked into the hollow arrangement 10.
In this embodiment the strips 70 are positioned on the blades along the regions of lowest pressure. This helps produce a good sucking force for introducing a lot of air. However there is a risk that introducing air at these points may promote flow separation. Thus, in other embodiments such as that shown in cross section in
In still other embodiments the orifices are located in both the walls of the conduit and on the blades of the aerofoil fluid directing arrangement. This is clearly more complicated to build but has an advantage of introducing the gas into many different portions of the flow.
It should be noted that although the above embodiments are described with respect to introducing air into water, they could also be used for introducing other gases into other liquids, as would be clear to the skilled person.
In the embodiments of
An advantage of using membranes is that it breaks up the liquid/gas interface at the injection point, making use of both the momentum of the liquid stream and the geometry of the orifice itself. This strategy favours lower gas flow rates from large numbers of orifices designed to cause some form of disruption to the flow. This design offers the potential of achieving well-distributed bubbly flows with high mass transfer characteristics.
In some embodiments gas is introduced through orifices with those on the wall of the pipe have lips of shielding elements.
The orifices or ports themselves may be arranged at an angle with respect to each other as shown in
There are two possible arrangements of the aerofoils, there is the zero angle of attack where the aerofoil blades are straight and exert no rotational forces on the flow, as is shown in
Both exert a rotational force on the flow, generating a swirling flow downstream of the device as is designs aim to improve the efficiency of a traditional venturi device by reducing large scale secondary flow currents which increase energy demand while retaining high levels of linear shear which enhance mass transfer rates. The swirl generated by the non-zero angle of attack design has three additional effects:
When the flow is oriented horizontally, the rotational acceleration counteracts the effects of gravity by suppressing bubble rise due to buoyancy. This enhances mass transfer due to prolonged existence of bubbly flow.
Turbulence intensity in the region downstream of the device is reduced, leading to reduced energy demand.
It further enhances mass transfer rates.
It should be noted that in both of these designs increasing the length of the aerofoil reduces the level of turbulence which leads to vortical flow motions and increased dissipation. Increased dissipation is costly in terms of energy while vortical flow has negative implications in terms of oxygen transfer efficiency. Indeed the re-circulation flow patterns tend to enhance the likelihood of bubble coalescence. Increasing the length of the aerofoil will reduce the turbulence and also increase the extent of the flow experiencing strong strain, which is beneficial to bubble break-up. Another way of reducing the level of turbulence is to alter the design of the gas entry ports as is shown in
There can be conflicting requirements for designs, in some embodiments there may be desired a very high void fraction which may lead to the production of larger gas bubbles with shorter residence time. This may be useful if the gas flow is used for power generation, for example as is shown in
Where mass transfer of the gas is desired in the diffuser region then clearly this region (50 in
It should be noted that although lower gas flow rates are generally achieved with the non zero angle of attack design, there are also lower energy losses observed so that the cost per unit of gas flow generated is approximately equal between designs.
a shows the aerofoil for the non-zero angle of attack design. In this design the blade length is between 150-250 mm, the hub length is 525 mm and gas is injected on both blade faces. The conduit that the aerofoil is inserted in is 100 mm. The geometry of the flow channels between the blades is as shown in
In
a and 9b show the orifices that are on the blades for these designs. As noted previously, in some embodiments there is only an orifice on the underside of the blade in the non-zero angle of attack design, while on the zero angle of attack design there are orifices on both sides of the blade. Gas is injected on the face of the blade to take advantage of the lower pressures and higher strain rates expected in this region. Gas is supplied through the wall of the surrounding channel directly into the aerofoil blade, from there it is directed towards the apex of a wedge shaped depression shown in
In this design, although not shown, there is a choke that has been added to the gas feed line in order to provide an independent control mechanism for the gas that is being sucked into the liquid flow. This is found to be helpful at low flow rates. Re-circulating gas pockets can occur at the top of the channel in low flow rates, however it has been found that using the choke valve so that the gas flow rate is increased slowly from an initial state helps avoid the formation of these gas pockets. Providing the ability to control the gas flow with the choke helps maintain a desirable swirling bubbly flow regime under different conditions and provides some control to the system. It can also be used to recover from unstable flow situations by reducing gas flow when such unstable flow is detected.
Although in some embodiments it was found desirable to only inject gas on the low curvature blade face, i.e. the underside of the wing, in some embodiments it is desirable to inject gas into the high curvature side of the blade the top of the wing as this reduces some of the swirl, the swirl being an unpredictable effect and therefore undesirable in some circumstances.
In this embodiment there is a controllable choke 110 on the air inlet pipe, which is controlled by control system 130 in response to signals sent by sensor 120. Sensor 120 is a flow sensor which in this embodiment is an optical sensor that senses the phase distribution of the flow in the diffuser region. If it detects that the desirable bubbly flow is not present then it signals this to choke 110 which closes slightly to slow the air intake until the desired flow is attained again.
As will be appreciated by the skilled person, embodiments of the present invention provide an improved system of introducing gas into a liquid and therefore can be used in a number of different situations where the introduction of gas into liquid is required. For example they can be used in water aeration systems or in industrial fermentation processes such as brewing or bio-fuels. They can also be used to stabilise flows such as oil flows.
One example of a further use of embodiments of the present invention is in air cooling systems. For example power stations are often located near water sources as they require substantial cooling to operate. Thus, embodiments of the present invention can be used to generate an air flow from nearby water flow using arrangements such as those shown in
It should be noted that in addition to providing cooling to the power station, entraining air into the local water source will have the additional advantage of improving the water quality.
Although, in this embodiment electricity is supplied from turbine 100, it should be noted that in other embodiments electricity could be supplied from another electrical source where this is appropriate and where it is not desirable to have a turbine driven by the water flow.
Various further aspects and features of the present invention are defined in the appended claims. Various modifications can be made to the embodiments herein before described without departing from the scope of the present invention.
| Number | Date | Country | Kind |
|---|---|---|---|
| 0910756.6 | Jun 2009 | GB | national |
| Filing Document | Filing Date | Country | Kind | 371c Date |
|---|---|---|---|---|
| PCT/GB10/01217 | 6/21/2010 | WO | 00 | 3/14/2012 |
