GB2141179A - Vapour turbine power plant - Google Patents

Abstract

The plant is of the closed-cycle type and comprises special vaporisation and condensation units in combination, designed to achieve recycling of the Latent Heat of the working fluid. The vaporisation unit, via special sub-systems which cause vaporisation of the working fluid to occur under reduced pressure resulting from entrainment with separated vapour flows, achieves the dual purpose of maximising the efficiency of the vapour energy production, whilst a heat transfer fluid becomes sufficiently cooled down under supercooling to then act as a condensing fluid in the condenser unit wherein absorption of the latent heat occurs to then become recycled, with further supplementary heating as required. The special sub-systems in the vaporisation unit involve a fractionalised vaporisation technique and a two-stage vaporisation system, coupled with working fluid atomisation and parameter optimisation, whilst the condensation unit contains an interrelated fractionalised cooling system in which the working fluid becomes fed back to the vaporisation unit at optimised temperatures. <IMAGE>

Description

SPECIFICATION Latent heat energy This innovation is concerned with a new pro cess, of a Closed-Cycle Vapour Turbine type, which is specifically designed to facilitate for the recycling of the Latent Heat of Condensation of the Liquid-vapour fluid used in the Turbine process. This is achieved through special new designs for the Vapourisation side of the process and for the Condensation Unit, and the Patent Application is concerned pri marily with these two aspects of the innovation. However on a more general basis it is also concerned with the system design of the process itself, the inventive step in this latter case being that the process enables the recycl ing of the Latent Heat of Condensation of the Turbine fluid, unlike other processes of this type.This latter aspect has in fact been previously dealt with embodied in a more general Patent Application dealing with closely associated work. This being No. 8211175 and Claim 1 therein.

Then Vapourisation side of the process is a totally new design system, whereas the Condensation Unit is along more conventional lines, but with particular new design features which distinguish it from other types of Condensation Units. The Vapourisation side of the process is referred to as a Vapourisation Unit in the ensueing discussions, but the Unit is more complex and performs more functions than just a normal conventional Vapourisation Unit.

The fields of use for this innovation would be for electrical generation over a wide power output range, and also for powering a drive shaft, which among other uses could be used for most propulsion systmes. Examples of these would be road vehicle; locomotive; ship propellor; aeroplane propellor.

The basic concept of the process is that the fluid circuit which carries the heat to the Vapourisation Unit, referred to as the Vapouriser fluid, having passed on its heat to the Turbine fluid, then goes on to the Condensation Unit for use in the Condensation process, where the Vapouriser fluid acting as a Coolant absorbs the Latent Heat of Condensation of the condensing Turbine fluid. This is able to be achieved through the special designs for the Condensation Unit, and the new design for the Vapourisation Unit in particular. the latter making it possible for the Vapouriser fluid to become so cooled down in the Vaporourisation Unit that this fluid can then be used as an effective Coolant for the Turbine fluid vapour in the Condensation Unit.The Vapouriser fluid, having absorbed the Latent Heat of Condensation, is then recycled back to the Vapourisation Unit and en route has its heat content supplemented to the required input level either from other heat recovery systems from other processes, or by a fresh heat supply source, or by a combination of such heat sources.

VAPOURISATION UNIT, FIGURE 1:This special design for a Vapourisation Unit employs new and different techniques for vapourising the Turbine fluid and is intended to effect maximised extraction of heat from the Vapouriser fluid in order that this fluid can then be used for, and be very effective at, absorbing the Latent Heat of Condensation in the subsequent condensation process, whilst at the same time maximising the effectiveness of the heat extracted with respect to the thermodynamic efficiency of the vapour energy production, and then the Turbine Efficiency on the vapourisation side of the process.

The basic Vapourisation Unit has several distinct sections, each having a special function, and these are shown on Fig. 1. These sections are also shown on,Fig. 3, which illustrates the whole of the vapourisation side of the process and encompasses several more distinct sections which are given further references. These sections are referred to in the ensueing discussions on the process.

The main concept on which the Vapourisation Unit is based, and which distinguishes this vapourisation process from any other process, is comprised of a number of features.

The first of these being the creation of a very high velocity dynamic vapour flow system immediately on formation of the vapour, commencing along the central region of Section A of the Vapourisation Unit, hereinafter sometimes referred to as the mainstream vapour flow. This high velocity mainstream flow in turn creates a low static pressure in the system, which becomes manifested on the edges of the mainstream flow, (sometimes in the ensueing discussion referred to as the side pressure).

In effect these two pressures then form the two halves of the Bernoullis equation governing streamlined fluid flows, which basically states that the sum of the dynamic and static pressures of a vapour stream flow remains a constant, even under extreme polarisation of the vapour pressure into a high dynamic pressure and a low static pressure, as in this system. Present normal systems produce randomised vapour initially, which usually only becomes to be fully expanded on passage through the small turbine nozzles, immediately at entry to the turbine system of the process.

The early formation of a high dynamic pressure, enhances the vapour energy for driving the turbine by compounding the dynamic pressure build up in the vapour flow path leading to the turbine entry. However, more importantly than this the low static pressure created in the system is used firstly to very advantageous effect in improving the thermo dynamic efficiency of the Turbine fluid va pourisation. But moreso than this, the artificially created low pressure conditions, as compared with true normal randomised thermodynamic pressure, enables vapourisation of the proportions of the Turbine fluid to take place at a range of temperatures, down to relatively very low temperatures in comparison to the pre-determined temperature conditions under which a normal randomised system would necessarily have to vapourise.This provides a means of cooling the vapouriser fluid far more than would be possible in other processes, through the action of the turbine fluid under reduced pressure being able to extract heat from the vapouriser fluid at comparatively low temperatures for absorption of its latent heat of vapourisation quotient, and then the turbine fluid vapour so produced being able to escape into the main stream flow, carrying low temperature heat away from the vapouriser fluid.Thus operating under this system both the vapourisation efficiency is improved upon over a normal process and the vapouriser fluid is able to be cooled down at the same time very effectively and sufficiently for it to be used as a very efficient coolant, or more aptly heat absorber, in the condensation side of the process, enabling maximum reclamation of the latent heat of condensation for further use as vapourisation heat in the vapouriser fluid.

The potential quantity for heat reclamation in this way is of the order of 60-70% of the total heat input placed into the process per cycle. The heat of condensation is heat energy which is locked up in the vapour molecules, and on a one pass through the process cannot be used to perform external mechanical work.

In present processes all or most of this heat energy is wasted by dissipation into an external heat absorber, which does not become recycled back into the process. Although, in these processes a small proportion of this heat energy does in fact usually become recycled by virtue of some being left remaining in the turbine fluid on passing through the Condensation Process, but this is a very small quantity in comparison to the amount wasted.

The full vapourisation system is subdivided into several fairly distinctly separate systems, the first of these being Sections A, B and D, which between them effect the first stages of the vapourisation, and these system together with the special techniques employed are discussed following.

Firstly atomization of a large proportion of the turbine liquid fluid is carried out prior to its entry into the Vapourisation System. This in effect vastly increases the surface area of turbine fluid to heated surface contact, which in turn will vastly improve upon the thermodynamic efficiency of the heat transferrence process from turbine fluid to vapouriser fluid.

However, moreso than this it is also a neces sary feature in order for the system to function properly with respect to the creation of the high velocity vapour stream along the central flow path. This is achieved by the action of a fairly complex cavity system in conjunction with the atomization system in Section A of the Vapourisation Unit. These systems are illustrated on Figs. 1, 2 and 3.

The primary function of Section A is to transfer middle grade heat from vapouriser fluid to turbine fluid, and equally important functions of the cavity system are to further increase surface area of heat exchanging surface, and also to facilitate for better optimisation of the thermodynamic conditions under which the vapourisation is being carried out-discussed in more detail below.

It is also possibly intended to have the turbine fluid which enters into Section B in atomized form, entering through the base and spraying upwards through the liquid bath of turbine fluid and amongst the submerged pipes carrying the vapouriser fluid. This feature has not been illustrated on the diagrams of the process.

A very special technique is used to maximise the cooling of the vapouriser fluid, which at the same time helps towards maximisation of the thermodynamic efficiency of the vapour energy production, and this technique is hereafter referred to as Fractionalised Vapourisation. It is a system in which several subsystems are created within the overall vapourisation system, with each of the sub-systems having the facility for optimising the conditions under which the vapourisation is carried out in order to then enable vapourisation for reducing temperature of the vapouriser fluid under more optimum thermodynamic conditions.

Six pairs of sub-systems have been incorporated into Section A, which are also referred to as cavities, as above. The first stages of the vapourisation are carried out in three primary sections, Sections A, B and D and therefore the cavities should perhaps be more aptly regarded as secondary sub systems.

The vapouriser fluid passes around the outer of the vapourisation system, as shown on Fig. 1 and 3. On arriving at Section A the vapouriser fluid passes around the cavity subsystems and its heat is transferred to the atomized turbine fluid, this being sprayed in atomized form onto suitably positioned highly heat conducting back plates. Fig. 2 shows an alternative design for the cavity system of Section A to that illustrated.on Fig. 1. Both designs are intended to enable good entrainment of the vapour produced in the cavities by the action of the high velocity central stream and the low side pressure that this creates.The positioning of the atomised sprays in relation to the back plates and vapour being produced is to minimise the lowering of the thermodynamic efficiency that would result from initial vapour subsequently becoming entrapped in fresh incoming liquid phase.

The suctional effect of the central vapour flow will have the action of lowering the vapour pressures inside the cavities below that of the normal thermodynamic pressure that would otherwise exist under the normal temperatures of the sub-systems, and this in turn will lower the temperature at which the turbine liquid fluid is able to vapourise and carry away the heat of the vapouriser fluid. Thus, this will result in the temperature of the subsystem, and the vapouriser fluid therein going below the temperature that would otherwise exist under normal conditions of vapourisation.

The main otimisable parameters within these sub-systems are: (i) Vapour Pressu re--variability being effected by facilitating for variable application of the low central stream side pressure, rather than say flow velocity, which in turn would be achieved by altering the width of the cavity outlets by an appropriate sliding cover mechanism.

(ii) Temperature of turbine liquid fluid on entry into the sub-systems.-Achieved by a fractionalised system of fluid extraction at different temperatures from the Condensation Unit (discussed later).

(iii) Temperature of vapouriser fluid acting on the backplates-Achievable by an appropriate system of vapouriser fluid mixing in which this fluid would be drawn off from various suitable points along the vapourisation unit at different temperatures, mixed accordingly, and then fed back into the helical fluid flow system at the required points.

(iv) Varying throughput quantities into the sub-systems of both the turbine fluid and the vapouriser fluid containing the heat energy.

(v) Appropriate design and correct dimensions of the sub-systems, coupled with correct positioning of atomised sprays.

Section D's principle function is to commence the high velocity flow of the central vapour stream, although the vapouriser fluid will continue to cool in this section as heat is transferred to the turbine fluid from the surrounding helical flow system carrying the vapouriser fluid. The vapourisation of the turbine fluid in this section will be more under the thermodynamic conditions associated with normal systems.

Section B's principle function is to effect vapourisation of the turbine fluid with low grade heat, which would not be possible in other processes, and in so doing effect cooling down of the vapouriser to relatively very low temperatures compared with other normal processes of vapourisation. This is achieved by creating a further and increased entrainment suctional force with the main stream vapour flow as it exists from Section A by passing the vapour through a narrow throat of a venturi shaped tunnel. This venturi section being referred to as Section C on the diagrams. Although not shown on the diagrams Section B could also be further subdivided into secondary sub-systems, with separate entrainment to each sub-system.

Fig. 4 illustrates a design for Section C, the Venturi shaped tunnel, which should create an improved entrainment suctional action acting upon the vapour being produced in Section B by the creation of the void zone in the region just beyond the outlets, referenced A on Fig.

4. This design also better facilitates for subdividing Section B into sub-systems, and control over separate entrainment actions could be readily achieved by suitable infinitely variable covers, or shutters, over the outlets.

Thus, in passing through Section A, then Section B via Section D the vapouriser fluid will in effect be supercooled and calculations show that the temperature could drop from an inlet temperature at the turbine end of the vapourisation side of say 95"C to a temperature on exiting from Section B of the order of 1 5 C. For the vapouriser fluid in a normal system to cool by this amount, if indeed it were possible, the thermodynamic efficiency of the vapour energy production would be drastically impaired.However, the fractionalised vapourisation technique, in addition to the cooling function has the equal or more important role of maximising the thermodynamic efficiency of the vapour production, which is achieved by optimising the various parameters affecting the efficiency of vapourisation in each of the sub-systems, as prev ously discussed. Optimisation of these parameters will enable each sub-system of Section A to vapourise its proportion of the turbine fluid as close as possible to the maximum carnot efficiency for the particular temperatures existing in the sub-systems, which will range from about 70"C-40"C. The overall Carnot Efficiency of Section A then being the average of the sum of the individual Carnot Efficiencies.Since Section A will vapourise of the order of 75% of the vapour then the overall carnot efficiency of the process should be high, in addition to the fact that for similar reasons the vapourisation efficiency of Section B should be high.

Therefore, this system will probably result in a much better Carnot Efficiency, with respect to the heat input and expansion stages, than other existing processes even though in this process the average temperature of the initial heating and vapourisation will be relatively low compared to normal systems. The important aspect of the thermodynamic efficiency at this stage being how fast and easily the heat energy can be transferred from the vapouriser fluid into the separated vapour stream, via escaping vapour molecules, and not on the temperature at which this process takes place. The efficiency at this stage being purely a function of the combination of all the parameter conditions concerned.

In this process the low average temperature of the initial vapourisation will in fact be a factor that will improve upon the thermodynamic efficiency of the vapourisation since a much larger proportion than normal of the total heat input will substantially have to be placed into the separated vapour phase under conditions more approaching those of superheating, i.e. under the most efficient means of converting heat energy into vapour translational energy. This process could operate in two ways. One in which this subsequent superheating is carried out prior to the vapour flows meeting by appropriate superheating equipment in the regions of the cavity exits and also in the upper of Section B. This method would avoid subsequent condensation taking place as vapour flows of different temperatures meet.However it is considered that it would be very beneficial to the process to allow subsequent condensation to take place providing it could be controlled to a mist formation which was supportable by the main stream flow. The principle advantageous of this mechanism would be (i) better entrainment and combination of the seperate sub vapour flows, (ii) Super densification of the mainstream flow over and above the normal density associated with the average thermodynamic conditions, (iii) the required level of subsequent superheating perhaps being better facilitated for by the mist droplets acting as heat sink sites, (iv) most important of all, the boost to the dynamic vapour stream pressure that would be created as condensed mist in the superdensified vapour revapourises in the subsequent heating equipment.

Most of the subsequent heating will be carried out in two further main sections, Section E and Section F.

Section E is a diffuser section which is primarily intended to slow down the vapour stream to better facilitate for the subsequent heating requirement, and this section will contain some initial heating heating equipment of a fairly simple design which will allow fairly streamlined passage of laminar vapour flow.

This equipment will probably be comprised of suitably spaced thin vertical plates, or fins, in the direction of vapour flow, with hot vapouriser fluid pipes passing through the unit in the horizontal direction at suitable distances apart.

These pipes, or tubes, being tear drop shaped in cross-sectional profile for smoother passage of the vapour. This section will be more for commencing the revapourisation of the condensed mist, with some superheating.

Section F will also perform both functions but be designed for superheating. It will probably be comprised of similar designed equipment to that used in Section E, but probably of a more complicated design in addition to the unit having hotter vapouriser fluid passing through. The design may be something along the lines of a car radiator.

On passing through Sections E and F the vapour will receive a large boost to its forward dynamic pressure by the action of the heating and super heating. The vapour flow then goes on to be streamlined along Section G and H prior to entering the turbine. Sections G and H will in effect act as a very large expansion nozzle of a converingdivergíng type and will replace the normal small turbine nozzles of a normal turbine, although it is proposed that the turbine will incorporate some additional final nozzle type of expansion system.

The turbine will be of a modified velocity compounding design, something along the lines of a Curtis design.

An important design aspect of the dynamic flow system in order to ensure that its dynamic nature is sustained, and particularly to ensure that the vapour velocity is maintained at a maximum through the initial vapourisation sections will be to have a correct crosssectional area for the volume of the expanding vapour at all stages in the flow system, such that the forward dynamic pressure will overcome any tendency for backward pressure.

This will be of particular importance at the exit from Section C and the throat of this venturi shaped section in order to ensure maintenance of high velocity vapour stream through Sections A and C. Then also between Section F and the turbine entry for maximum build up of dynamic pressure in the forward vector prior to impact with the turbine impellors.

To further enhance this aspect of the process specially designed equipment will be used based on tear drop profile shapes in order to shift the equilibrium between the forward and backward pressures towards the turbine entry. These special design features will be in the superheating sections and probably also'along the streamlining section of Section G, although these are not shown on the diagrams.

Therefore, from the aforegoing, the vapourisation side of the process will effect supercooling of the vapouriser fluid and the turbine output one-pass thermodynamic efficiency will be sustained at a high level, firstly from improved thermodynamic efficiency of the heat energy transference from the vapouriser fluid, and its conversion to dynamic vapour energy, and secondly by compounding the dynamic pressure of the vapour flow prior to its impacting with the impellors of the turbine.

The supercooled vapouriser fluid will exit from the vapourisation side of the process at a sufficiently low temperature to be used as an effective heat absorber in the condensation side of the process, where it will recover the latent heat of condensation of the turbine fluid vapour for subsequent recycling back into the process.

CONDENSATION PROCESS, FIGURES 5 8 6/EMBODIEMENT EXAMPLE, FIGURE 7: The Condendation Unit is comprised of a bank of sets of concentric tubes, one set being as illustrated on Fig. 5. For larger scale electrical generation, on Industrial sites, the Condensation Unit will probably be stacked vertically, although it could function just as well in the horizontal position, as schematically illustrated on Fig. 7, and this would probably be the positioning for some propulsion systems. However, for the purposes of the following discussion I will assume a vertical stack.

The cooled vapouriser fluid will enter at the base of the unit and pass upwards through the inner and outer tubes, as illustrated on Fig. 5. The turbine fluid vapour, after the turbine stage, will enter at the top of the unit, firstly as vapour and then will liquify as the fluid flow passes downwards through the middle concentric tube of the unit. For maximising the heat energy flow paths from turbine fluid to vapouriser fluid, vanes, or fins, have been incorporated into the Condensing Unit and these will contain suitable sized holes to allow lateral fluid flow. A cross-section of this system is shown in Fig. 6.

The liquifaction is achieved through the effect of both the cold coolant and also some elevation of vapour pressure above the condensing liquid. For this latter purpose a vapour pressurising pump has been included in the circuit for improved controlled over this pressure, rather than just relying on vapour pressure control at exhause from the turbine.

This pump is shown on the embodiment example Fig. 7.

The elvated pressure would only by of the order of 4-5 atmospheres, sufficient to elevate the boiling point and allow liquifaction to take place at around 60"C, (in the embodiement example). The coolant, or heat dissipator, in its action of absorbing the Heat of Condensation of the condensing vapour will be the main action in overcoming the Van der Waal forces of the fluid, although the elevated vapour pressure will obviously contribute something towards this aspect. The main point being that the energy expenditure on the pressurising pump will be a very small percentage of the energy that the vapour is capable of producing in the transformed state on impacting with the turbine. This being of the order of 5%.

The relationship between the specific heats of the Turbine and Vapouriser fluid are particularly important at this stage of the process, since the system can only operate fully successfully if the vapouriser fluid can hold all the heat of condensation of the turbine fluid, whilst at the same time still remaining at a temperature well below the boiling point of the vapouriser fluid as existing at reasonable elevated pressures, e.g. 4-5 atmospheres.

This would minimise the expenditure on en ergy for the pressurising pump, since lower pressures could be used, and would be a necessary condition to minimise internal va pourisation within the liquid phase, which could otherwise lower the thermodynamic effi ciency of vapourisation. However, a further principle reason is to ensure that a tempera ture gradient is maintained in the cooling process to facilitate for improved flow of heat from turbine fluid to vapouriser fluid. In the embodiement example given Freon-li (R.T.M.) is used for the turbine fluid, Trichlo rofluoromethane, and water for the vapouriser fluid, and the relative specific heats of these fluids are of the order of a ratio of 1 5 respectively.Thus the water turbine fluid is able to hold five times more heat energy that the Freon-i 1 vapouriser fluid per 1 C ex change of temperature. However, because of the relative quantities of the flows of the two fluids this ratio may become reduced to about 1:4.

In the embodiement example the maximum temperature that the water could attain, bas ing on a maximum quantity of heat of con densation, and the relative specific heats/fluid flows, would be of the order of 60"C. There fore, if the boiling point of Freon-i 1 is ele vated to around 70"C, by holding under a vapour pressure of 5 atmospheres, then it will be possible to liquify and maintain reasonable temperature gradients up to temperatures of approaching 60"C in the Condensation Unit.

At this order of temperature under a pressure of 5 atmospheres it should be possible for the Freon-i 1 fluid to be existing virtually all in the 100% liquid phase. However, it is pro posed to draw off the liquified fluid in stepwise temperature fractions of 5"C incre ments for feeding to the sub-systems of the Vapourisation process, ranging from 60"C to the hottest, largest cavity of Section A, to 30"C and below to Section B. Therefore at these lower temperatures under the pressure of 5 atmospheres 100% liquid phase liquifac tion should be easily attainable.

Since a large proportion of the liquified fluid is required at 60"C for feeding to Section A of the Vapourisation Unit it would be the intention to allow the temperatures of the two fluids to fully even out towards the upper of the Condensation Unit, rather than striving to maintain a temperature gradient as far as possible towards the upper of the Condensa tion Unit. This aspect of the process, coupled with the fact that the Turbine fluid quantity will be substantially reducing as the fractions are drawn off will vastly improve upon the 100% achievability of the condensing pro cess.

Obviously, in order for this fractionalised liquid take-off system to function at the higher temperatures it will be necessary to continue to hold the liquified Freon-i 1 under the condensing pressure of 5 atmospheres up to entry into the Vapourisation System. However, in any event this order of pressure is required for all the fractions for atomization purposes, and furthermore it will obviate the need for Turbine fluid feed pumps in this stage of the process, which in other processes would be necessary. Possibly with similar expenditure of energy.In the embodiment example it is proposed to have seven liquid take-offs from the condensation unit of the Freon- 1 at temperatures of 60"C, 55"C, 50"C, 45"C, 40"C, 35"C, 30"C and below.

The 60"C-40"C flows for feeding to the subsystems of Section A, and possibly some of the 35"C fraction. Then the 35"C fraction to Section D and the 30"C and below fraction to Section B.

The heated water vapouriser fluid will enter the system at around 95"C, pass on 20"C of Superheating in Sections E and F and then enter the hottest, largest cavity pair of Section A at around 75"C. In this section it should transfer about 30"C and exit from the section at about 45"C. The prime objective with the liquid Freon feeds to Section will be to achieve temperatures which are just below the latent heat energy levels for the thermodynamic conditions that exist in the cavities, and also temperatures which give reasonable temperature gradients from the water vapouriser fluid to the Freon-11 turbine fluid.Examples of typical conditions would possible be: Hottest, largest cavity pair: Temperature gradient 75"C-60'C, vapourising under a cavity vapour pressure of 3-3.5 atmospheres. Coldest, smallest cavity pair: temperature gradient 45"C-40"C vapourising under a vapour pressure of say 1.5 atmospheres.

In both systems the Freon-i 1 liquid on entry to the cavities will just contain a little of its latent heat for the thermodynamic conditions existing within the cavities, remembering that the liquid itself will be under a pressure of 5 atmospheres and therefore vapourisation will not be taking place prior to entry. In the case of the hottest cavity a fairly large temperature gradient will already exist for good flow of heat from water to turbine fluid. However, in the coldest cavity the temperature gradient will be fairly low and therefore in these lower temperature cavities a higher entraining action would probably be applied in order to quickly lower the temperature of the entering turbine fluid and thereby improve the temperature gradient for better flow of the low grade heat, which would also be capable of vapourising at a reduced temperature.An alternative parameter in these lower temperature cavities would be to feed the Freon liquid to them at lower temperatures, but in this case the condensing unit would have to be that much more effective. In practice it would be a question of optimising between the parameters on both the Vapourisation side and condensation side of the process. Probably the more important functions of the cavity system, are (i) increased surface area, which is particularly necessary for the atomization technique to be applied properly. (ii) Creation of the very high dynamic central vapour flow, (iii) in order to improve the thermodynamic efficiency by minimising the entrapment of vapour in fresh incoming liquid phase.

However, the entrainment action of the central stream in the cavity complex on the cavity vapours could also have an important function in commencing the supercooling of the vapouriser fluid, particularly towards the smaller, cooler end of the Section. At the hottest end of Section A, however, where there will exist quite a large temperature gradient between Vapouriser fluid and Turbine fluid it may be that the process would operate more efficiently if the vapour pressure was allowed to build up a little in the cavities in order to raise the boiling point, rather than lower as in the earlier example given. This would produce hotter initial vapour in the earlier, largest cavities, and could be achieved by means of the sliding cover mechanism across the cavity outlets.This therefore would be a further variable that could be optimised, possibly commencing with an elevated boiling point in the largest cavities, and then start to apply supercooling, by the entrainment action, towards the smaller cooler end. Any entrainment which removes the cavity vapour at a faster rate then would otherwise be being produced would be commencing the process supercooling of the Vapouriser fluid.

The water vapouriser fluid should enter Section B at around 40 C/35 C and it is in this section where a high velocity main vapour stream will be required in order to create the high entrainment acting upon the vapour being produced in Section B. Calculations show that it shbuld easily be possible to lower the vapour pressure to of the order of 0.5-0.6 atmospheres, with 20% of the total vapour production being carried out in Section B and 80% in the main stream flow.This will reduce the boiling point to around 1 O'C and evaporation of the Freon-i 1 liquid fluid under these conditions should remove a quantity of heat within the latent heat content of the vapourising fluid such that the lowest temperatures attainable within the Freon-i 1 liquid both should be of the order of 1 5 -20 C. It would probably be possible to imporve the overall level of supercooling by sub-dividing Section B into several sub-systems, since in this way a more concentrated entrainment action can be applied to a smaller system just in the region where the water is exiting from the Freon-i 1 liquid bath. It would also be the intention to overfill the bath with excess Freon-i 1 liquid so that in the steady state of the process there is always a large reservoir of the cold liquid to always maintain the water vapouriser fluid pipes fully submerged during the operation of the process. The calculations show that the water temperature on exiting from the Freon-i 1 liquid bath should quite easily be lowered to around 1 5 C by the action of the removal of the heat at the water and incoming Freon-i 1 liquid in the Latent Heat content of the evapourating Freon-l 1. If the parameters which effect the cooling are stretched then the water could theoreticaily reach temperatures as low as i0-15'C.

At these orders of temperatures the water should be very effective as a Coolant in the Condensing Unit and be very successful in absorbing all the excess Latent Heat of Condensation of the liquifying Freon-i 1 vapour.

As a result it should be possible to operate the system at reasonably low compression pressures of the vapour above the condensing liquid, with corresponding savings in energy expenditure. However, this would be a variable that could be used if required as an aid towards overcoming the Van de Waal forces, rather than mainly for simply raising the boiling point. The energy expenditure on the compression at 4-5 atmospheres should be of the order of 5-10% of the total energy output at the turbine state, but in this process this should be compensated for by the gains in energy output resulting from the compounded build up of vapour stream dynamic pressure prior to inpacting with the impellors of the turbine.

As a further variable parameter on the Condensing Unit some secondary sub inlets for the entering cold water have been included along the outer jacket of the Unit, as shown on Fig. 5, and these could be useful in helping to produce 100% liquid phase earlier in the Condensing process, i.e., closer towards the vapour entry in the Unit.

Thus in this process the highest proportion of the Heat of Condensation will enter the water flow and be recyled back to the Vapourisation Unit via this route, and a much smaller proportion will remain in the Freon-i 1 Condensed Turbine fluid liquid and become recycled in this way.

Most other systems manage to achieve some recycling of the heat of condensation in this latter way, but at present are able to recycle the whole of the heat of condensation.

Theoretically this may be possible using processes described in my earlier Patent Application No. 8211175 given under Claims 1 B and 1 C, but these processes would require an external abundant source of cold coolant fluid and, depending upon the temperature of the coolant, they would probably require far more expenditure of energy on compression.

Moreover there would probably be losses of heat energy at the stage of transferring the heat into the vapouriser fluid. In the process described in this Patent Application the heat is transferred directly into the vapouriser fluid.

Claims (25)

1. A low temperature Vapour Turbine Process, comprising special Vapourisation and Condensation Units, which between them enable the recycling of a very high proportion of the Latent Heat of Vapourisation/Condensation of the Turbine Fluid, by the action of transferring the Heat of Condensation of the said Process, after passage of the said fluid through the Turbine of the said Process, back to the Process fluid effecting vapourisation, referred to as the Vapouriser Fluid, which, after passing on it's heat content in the special Vapourisation Unit of the said Process, becomes sufficiently cooled to a level whereby the fluid can act as a heat absorbing Coolant for the said Heat of Condensation.

The uses for this innovation being various, but essentially, either for electrical generation power provision, or for the powering of a drive shaft for other uses.

2. A special design for the Vapourisation Unit in Claim 1, which employs new and different techniques for vapourising the said Turbine Fluid, with the dual purpose of (i) effecting maximised extraction of heat from the said Vapourisation Fluid, in order that the latter fluid can function with maximum effect to absorb the said Process Heat of Condensation, and (ii) maximising the thermodynamic efficiency of of the vapour energy production.

The said special design being comprised of several sub-systems with differing, but interrelated, functions and for ease of description being referenced Sections DABCEFG H, this being the section order from vapourisation to turbine end of said Vapourisation Unit. Similarly, therefore, the ensuing more detailed Claims for said Vapourisation Unit are dealt with following under the same sub-systems catagorisation. More generally, however, said Vapourisation Unit being a Unit in which the said Vapouriser Fluid first enters at it's hottest into a helical flow system of an outer surrounding heating jacket at the Turbine end of said Unit, and at the end of Section G. Then flows in this manner, in conjunction with inner heating/Superheating flows through special heating units, along said Sections G F E C A D to the main vapourising sections.

Said Section A being the principal vapour producing section, wherin an atomization technique is employed to inject the said Turbine Fluid, and wherein vapourisation, either wholly or partially, takes place under reduced pressure relative to saturation pressure to effect supercooling of said Vapouriser Fluid under an entrainment technique, being referred to as Fractionalised Vapourisation. The latter Fluid then flowing, into Section B, which, in contrast, is a pipework system immersed in a reservoir of said Turbine Fluid, to then effect further vapourisation with the low grade heat contained in the said Vapouriser Fluid, being again under conditions of reduced pressure effected by an entrainment action. However, in the process, the said Vapouriser Fluid becoming further supercooled to a relatively low temperature prior to feeding to the said Condensation Unit in Claim 1.The said Fractionalised Vapourisation and said entrainmet techniques producing initially several vapour flows, which all become combined into a central main stream flow en route to the said Turbine end, with superheating also being facilitated for, generally and where appropriate in sub-flows. Following Claims deal principally with all of these techniques, although not wholly. However, between them they in effect carry out a general, overall, process of two stage vapourisation. The entire said Vapourisation Unit being thermally insulated as required in order to prevent loss of heat to the ambience.

3. Section A of Claim 2, being a sub-unit in which several sub-systems are created, of a range of dimensions, to form the basis of the said Fractionalised Vapourisation System. The said sub-systems progressing from large to small off a central vapour streamlining section and being on either side in pairs, with the largest pair being at the end farthest from the Process Turbine Unit. Middle grade heat contained within the said Vapouriser Fluid becomes transferred in this section by means of the said Fractionalised Vapourisation Technique, after having passed on superheating in preceeding sections, and is intended and designed to maximise the thermodynamic effeciency of vapourisation, whilst at the same time enabling vapour to vapourise at an increasingly lower heat transferrence temperature.

This being achieved by causing vapour produced within the sub-systems to stream with a high velocity along the said central flow section, and thereby past the exits of following sub-systems, creating a high forward dynamic pressure and a low side static pressure. The latter then causing entrainment of vapour from following sub-systems in order to in turn create a lowered vapour pressure inside the said sub-systems, relative to saturation pressure. Thereby facilitating for vapourisation to to take place under lowering Vapouriser Fluid temperatures to effect supercooling of the said fluid, which first enters the said outer heating jacket of the largest sub-system pair.Then flows forward through the range of said subsystems to the smallest pair, and becoming cooler enr route as transferrence of heat is made possible at increasingly lower temperatures due to an increasing said entrainment action, and lowering of vapour pressure thereby. The cross-sectioned area and design shaping of the central streamlining section, including the exits from said sub-systems, being such as to create a maximum forward dynamic pressure from the expanding vapour allowable by the existing temperatures, which will vary according to temperature of vapourisation, in order then to overcome opposite back pressure force and maximise upon said entrainment action.In stream additional superheating equipment being a possible option in order to increase upon said forward dynamic pressure, but in possible optimisation with mist formation levels, which could occur as vapour streams of differing temperatures unite to the probable advantage of the process-see Claim 15.

4. The said sub-systems of Claim 3, having the flexibility of varying design to achieve the said dual purpose, but in common comprising a highly heat conducting side, or sides, onto which is sprayed the said Turbine Fluid, probably in atomized form, although not necessarily, and being at an optimum angle such as to minimise entrappment of produced vapour in fresh incoming liquid phase. Parameter optimisation also being a common aspect of the design, as given in the following Claims-5 to 9, although not necessarily wholly being required. All these features of the design given herein being aimed at maximising the effeciency of the vapour energy production, which in turn will also maximise upon the efficiency of said supercooling of said Vapouriser Fluid.

5. The use of adjustable shutters across the exits of said sub-systems of Claim 4 to facilitate for variable entrainment action.

6. Temperature adjustment of said Turbine Fluid in Claim 4, achieved by a fractionalised system of said fluid extraction from the Condenser Unit in Claim 1, being referred to, herein as Fractionalised Cooling and dealt with under Claim 21.

7. Temperature adjustment of said Vapouriser Fluid in Claim 4, achieved by an appropriate system of Vapour Fluid mixing in which this fluid is drawn off from various suitable points along the said Vapourisation Unit in Claim 2 of appropriate differing temperatures, mixed as required to yield desired optimum temperatures, and then fed back into-the outer heating jacket at desired points.

8. Facilitating for variable thoughput into the said sub-systems in Claim 4 of both the said Turbine and Vapouriser Fluids.

9. Appropriate optimum design, shaping, and dimensions of the said sub-sytems in Claim 4, coupled with optimum positioning of the said Vapouriser Fluid atomization sprays.

10. Section D, being the rear section of the said Vapourisation Unit in Claim 2, and specifically to the rear of said Section A therein, with the principal function of producing vapour for commencement of the high velocity central vapour stream in said Section A. The said Turbine Fluid entering the section at an optimum low-middle grade temperature from the said Condenser Unit take-off system, in normal liquid phase form, and being such as to maximise further cooling whilst producing maximised vapour energy, with the latter taking precedent, and of practical necessity, although beneficially so, being carried out under normal saturated vapour pressure conditions.The vapour outlet from this section into said Section A then able and being designed to create maximum forward dynamic pressure, although of course, as allowable by existing vapour temperature, which could be improved upon by one of said superheating inclusions of Claim 2. There also being a Turbine Fluid optimum level maintainer, operated as and if required, and being comprised of a fluid bleed-off pipe to the said Turbine Fluid reservoir of Section B of Claim 2, and following.

11. Section B in Claim 2, in more detail being comprised of an overfilled reservoir of the said Turbine Fluid, which will enter at an optimum temperature from the said Condenser Unit, and containing a system of submerged pipework through which is flowing the said Vapouriser Fluid to effect further vapourisation of said Turbine Fluid, and supercooling of itself, and being in contrast to the outer heating jacket system of vapourisation.

This section also functioning under reduced pressure, brought about by continueing the high velocity central vapour stream from said Section into Section C, wherein exists an entrainment system having a suction action on the vapour pressure existing above the said Turbine Fluid reservoir. Said entrainment action at this point being at it's maximum, and required to be so, in order to then cause mamximum supercooling of the said Vapouriser Fluid down to comparatively low temperatures. Extraction of low grade heat from said fluid, as Latent Heat, being the principal function of this section, in contrast to that vapourisation in the said Section A, but in doing so a quantity of vapour will also obviously be produced, with vapour combination then taking place in said Section C.The section also having a facility for having it's containing surface maintained heated by channelling hotter Vapouriser Fluid fed from the main helical flow system behind the said surfaces, into, through, and out of suitable spaces, back into the said main flow system. The said surfaces being highly heat conductive and could effect some vapour superheating in this manner, although it may prove in practicd that such heating is required to be minimal. However, notwithstanding the latter, the section probably being equipped with a facility for inflow superheating, via suitable equipment in the upper of the said section, in order to then facilitate for control and thereby optimisation of entrained vapour temperature for mist control purposes etc. on entry into said Section C.

The section also having the option of two additional facets as given following in Claims

12 and 13.

1 2. The possible sub-division of said Section B in Claim 11 into sub-systems, each having their own entrainer, in order then to apply the suction action of the main vapour stream to more effect in lowering the finally obtained temperature of the said Vapouriser Fluid by improving upon the supercooling profile therein.

13. The possible introduction of the said Turbine Fluid into said Section B in Claim 11 via upward atomized sprays through the said pipework system in the said Fluid resevoir for increased heat extraction efficiency by virtue of spreading, but concentrating, the incoming fluid whilst at it's lowest temperature. Thereby maximising temperature gradient and surface area of heat transfer.

14. Section C in Claim 11, comprised of an appropriately shaped tunnel, of optimum cross-section, designed to yield a maximised quantity of forwad Kinetic Energy, allowable by fluid temperature, in order to then, (i) yield a maximised entraining action at suitable points along the edge of the fluid stream, and (ii) overcome as much as possible of opposite back pressure exertion from the following Section, ie, said Section E, which in turn could/will become exerted and transmitted from Turbine impedence to forward flow, to then lower maximum fluid flow velocity through said Section C. There being here also an optional in-flow inclusion for the purpose of both aiding streamlining, and for heating fluid flow to an optimum temperature, both in order to then maximise upon said entrainment action. The said entrainment points being of varied design, but generally of standard design.However, having the possible option of adjustable sliding shutters to then be able to vary the entrainment profile, and thereby the said supercooling profile.

1 5. Said superheating in upper of said Section B in Claim 11, and inflow in other sub vapour flows being as required and equipped, where applicable with the facility for optimisation for the purpose of controlling/optimising mist formation on combination of vapour streams of differing temperatures, in addition to optimising kinetic energy content therein, as in Claim 3. In order then to, (i) achieve said improved entrainment action and combination of vapour flows, (ii) superdensify the said Turbine Fluid with condensed mist, which on revapourisation in the subsequent heating/superheating equipment will give a boost to the forward dynamic pressure, (iii), perhaps improve upon the superheatability of the fluid flow in the subsequent equipment.

The raising of fluid from said Section B via entrainment to then enter said Section C, as in Claim 11, to then in turn, yield a fluid vapour flow containing a condensed mist, which subsequently becomes revapourised in following heating sections being the basis of the two stage vapourisation process mentioned in Claim 2, being apart from, and after, said Fractionalised Vapourisation process in said Section A.

1 6. Section E of Claim 2, following said Section C and being a diffuser section to cause slowing down of the vapour flow in order to facilitate for improved heating/superheating by special inflow equipment, as in Claims 1 7 and 1 8 following. However, being also to create a fluid flow buffer zone through which the combined vapour from said Section C will flow, with the maintenance of forward laminar flow, but able to absorb opposite, back pressure force into forward side vector components. Thereby protecting the fluid flow through said Section C from retardation, which is necessary to be maintained at a maximised velocity for maximised entrainment action.

17. Heating to superheating equipment in said Section E of Claim 1 6 of a simple, primary, nature and probably, although not necessarily, comprising suitably spaced fins in the direction of fluid flow, having buiit-in lateral pipes carrying hot Vapouriser Fluid.

The said lateral pipes being of a special tear drop design in cross section in order to then cause forward streamlining of revapourising fluid mist, and build-up of forward dynamic pressure thereof, in addition to commencing the said boost to said forward pressure, as in Claim 1 4. Thereby shifting fluid pressure equilibrium forward, and in turn further protecting said fluid velocity through said Section C from opposite back pressure forces.

1 8. Section F of Claim 2, following said Section E and being at the broadest/highest part of the fluid flow path, and therefore at the stage of minimised forward velocity, containing similar, but probably more complicated, heating/superheating equipment as used in the preceding section, ie, said Section E, which again will facilitate for maximisation of said boost mentioned in Claim 14 into the forward vector. Thereby, commencing rebuilding of the forward dynamic pressure up to a maximum level, and further protecting the fluid velocity through said Section C from opposite back pressure force, originating from Turbine impedence to forward flow, by virtue of in effect, creating a forward pressure barrier, and thereby shifting the said fluid pressure equilibrium forward.

19. Sections G and H of Claim 2, following Section F, and being in effect a very large vapour expansion nozzle of a convergingdiverging type in design and in principle, respectively, but here being used prinicpally to effect vapour streamlining to a high degree, prior to Turbine entry, of vapour which will already be fairly well expanded in the forward vector. Streamline converging through said Section G taking place down to a circular throat of cross-sectional area dimensions such as to yield a point of maximum Kinetic Energy in the forward vector.The said nozzle being heated via the main outer heating jacket, but also containing a large central component of a large tear drop design shaping for the dual purpose of aiding streamlining, and the build up of forward dynamic pressure thereof, and also to act as a further superheating element by itself having a similar outer helical flow system, in suitable combination with the said main heating system, through which the said Vapouriser Fluid at it's hottest will flow.

Thereby said superheating improving upon the kinetic energy content of the vapour, and therefore, on the forward dynamic pressure when in combination with said streamlining.

20. The possible use of smaller lateral tear drops profile at suitable points in the fluid flow path, and particularily in the final streamlining sections, which would also be for the dual purpose of heating/superheating, and for shifting the fluid pressure equilibrium between forward dynamic pressure and opposite force due to Turbine impedence, towards the former.

21. A special design for the Condensation Unit of Claim 1, comprising counterflow concentric tubes and being used in combination with the said special Vapourisation Unit, wherein the principal feature is the said Fractionalised Cooling System for the condensed Turbine Fluid, designed to draw off said Turbine Fluid from along the said Condensation Unit at desired optimum temperatures for feeding to the said Vapourisation Unit, and to the various said sub-systems therein. Said optimum temperatures being governed by desired temperature gradients balanced against desired Turbine fluid temperature levels in relation to vapourisation onset under existing vapour pressures, entrained or normal as the case may be, for input then to the said subsystems of the said Vapourisation Unit.The said counterflow concentric tube tube design having the said cooled Vapouriser Fluid on exit from said Section B enter one end of the Condensation Unit and pass through a central tube and an outer concentric tube, with the said Turbine Fluid entering the other end of the said Condensation Unit and counter flowing through a concentric tube between the said tubes containing said Vapouriser Fluid.

Thereby facilitating for heat flow outwards of the Heat of Condensation from the former fluid to the latter, on either side of the former fluid. The design also being such that the said Vapouriser Fluid entering end of the said Condensation Unit is narrower in cross-sectioned area than the said Turbine Fluid entering end, in accordance with reduction in volume of said Turbine Fluid, as portions of the latter fluid are drawn-off along said Condensation Unit in the said Fractionalised Cooling System, and as being conducive to maximisation of heat transfer.Said Heat of Condensa tion thus becoming recycled back to the said Vapourisation Unit of Claim 2, mainly via transferrence to said Vapouriser Fluid, but also a maximised quantity being recycled via the said Turbine Fluid itself, which will not only benefit the effeciency of reclamation of Latent Heat, but also the efficiency of vapourisa tion-as also in Claims 4 and 6.

22. The possible use of a vapour pressurising pump in line between Turbine Exhaust and said Turbine Fluid entry to said Condensation Unit of Claim 21 in order to raise/ maintain the vapour pressure of the said Turbine Fluid in the said Condensation Unit, and above the condensed liquid phase therein, at an optimum level in order to, in turn, raise the liquifying temperature of the said Turbine Fluid to a correspondingly optimum level.

Being conducive to maximising heat transfer, whilst controlling maximum Turbine Fluid condensed temperature to the optimum desired for the hottest sub-system of said Section A, and thereby also minimising the energy requirements of said pressurising pump.

23. The possible use of vanes, or fins, inside the Condenser Unit of Claim 21 to facilitate for improved said outward heat transfer, and containing suitably sized holes conducive to good lateral fluid flow.

24. The possible incorporation of sub-inlets for the said cold Vapouriser Fluid along the said Condenser Unit of Claim 21, to facilitate for improved condensation profile of the said Turbine Fluid therein, as may be required.

25. The incorporation of further supplementary heating systems of any type into the Vaporiser Fluid recycling circulatory after said Condensation Unit in Claim 20 in order to raise the temperature of said fluid above that attained due to absorption of the Heat of Condensation in the said Condenser Unit and to that required for re-input per cycle to the said Vapourisation Unit hot end.

25. The said Turbine Fluid pressure thus produced by the said in-line pressurising pump of Claim 22 being maintained as much as practically possible in the fluid sub-flows of the said Turbine Fluid up to various points of entry to the said Vapourisation Unit in order to facilitate for the pressure requirement for said fluid atomization and to negate the need for further pumps for said atomization purposes. Although of course, also being necessary to avoid en route premature revaporisation of said Turbine Fluid in the case of the sub-flow of the maximum temperature fluid, and then to correspondingly lesser extent in the case of the lower temperature fluid subflows.

26. The incorporation of further supplementary heating systems, of any type, into the circuitory after said Condensation Unit of Claim 21 in order to raise the temperature of the said Vapouriser Fluid above that attained due to absorption of Heat of Condensation in the said Condenser Unit, and to that required for re-input to the said Vapourisation Unit.

27. The use of other in-circuit fluid pumps as may be required, and particularly prior to entry of said heated Vapouriser Fluid to said hot end of said Vapourisation Unit, as in Claim 2.

1. A low temperature Vapour Turbine Process comprising special Vapourisation and Condensation Units which between them enable the recycling of a very high proportion of the Latent Heat of Condensation of the Turbine Fluid by the action of transferring the Heat of Condensation of the said Process back to the Process Fluid effecting vapourisation referred to as the Vapouriser Fluid, which after passing on it's heat content in the said Vapourisation Unit of the Process becomes sufficiently cooled down to a level whereby the fluid can now be used as a heat absorbing fluid in the Condensation Unit for absorption of the Heat of Condensation of the Turbine Fluid vapour as it condenses therein.The said Vapouriser Fluid so heated then becoming recycled back to the said Vapourisation Unit via it's circuitory and being supplementary heated to the desired level en route, and so on ad infinitum cycle after cycle.

The uses for this innovation being several but essentially either for electrical generation power provision or for the powering of drive shaft for other uses.

2. A special design for the Vapourisation Unit of Claim 1 which adopts mainly differing or new techniques for vapourising the said Turbine Fluid with the dual purpose of (i) effecting maximised extraction of heat from said Vapourisation Fluid in order that the latter fluid can function with maximum effect to absorb the said Process Heat of Condensation, and (ii) maximisation of the thermodynamic efficiency of the vapour energy production. The said special design being comprised of several sub-systems with differing but interrelated functions and being denoted herein for ease of reference as Sections DAB CEFGH, this being the order from the vapourisation to the turbine end of the said Vapourisation Unit. Similarly, therefore the ensuing more detailed Claims for said Vapourisation Unit are dealt with following under the same section categorisation.More generally however, said Vapourisation Unit being a Unit in which said Vapouriser Fluid first enters at it's hottest into a helical flow system of an outer heating jacket surrounding the section at the Turbine end of the said Unit, more specifically being at the farthest end of Section G. Then flows flows on through the said helical system around said sections GFECAD, there also being interlinked inner superheating/heating equipment in certain of the said sections as in the following more detailed Claims. The subsystems effecting the initial vapourisation being sections ADB, with said Section A being the main one for this purpose, itself being comprised of further sub-systems herein referred to as cavities and wherein an atomized spray technique is used to inject the said Turbine Fluid.The vapourisation therein also either in total or partially taking place under reduced vapour pressure relative to saturation pressure in order to effect supercooling of said Vapouriser Fluid during the vapour production inside the said cavities. Being effected by an entrainment technique herein referred to as Fractionalised Vapourisation as in Claim 3.

The said Vapouriser Fluid then flowing on to pass around the outer of Section D and then into Section B which in contrast is comprised of a normal heat exchange pipework system carrying the said Vapouriser Fluid immersed in a reservoir of said Turbine Fluid to thereby effect vapourisation of the latter fluid by this method under the action of the lower grade heat still contained in the former fluid. This vapourisation also being carried out under reduced vapour pressure effected by a continuance of the said entrainment action, now acting upon the vapour pressure of said Section B, as in Claim 10, such that a higher level of vapourisation takes place in this section and in the process the said Vapouriser Fluid becoming further supercooled to a low temperature prior to then feeding to the said Condensation Unit of Claim 1 to absorb the Heat of Condensation therein.The dimension of said Vapourisation Unit and the sub-systems therein being as required conducive to most efficient vapour energy production as in following Claims. More generally however in the length direction the produced vapour flow system diverging following said Section C, then convering in both the breadth and depth dimension following Section F to the dimension of the circular entry to the proposed radial turbine. The entire said Vapourisation Unit being thermally insulated externally as required in order to prevent loss of heat to the environment.

3. Section A in Claim 2 being a subsystem in which a range of said cavities of varying size are present to form the basis of the said Fractionalised Vapourisation System.

The said cavities being in pairs and progressing from rear large to front small pairs off a central vapour streamlining section. One of each pair extending upwards and the other downwards to optimum distances and both extending the full width of the said Vapourisation Unit with this dimension being as required according to Turbine Fluid throughout requirement. The nozzles for the atomized spraying of said Turbine Fluid being off suitable pipes appropriately positioned inside each cavity and running the full width therein, being spaced as required conducive to maximisation of surface area of vapourisation, also as in Claim 4. Middle Grade heat contained within the said Vapouriser Fluid passing through the helical flow system around the cavities becoming transferred in this section after having passed on higher grade heating/ superheating in the preceding sections.The said Fractionalised Vapour system being intended to maximise the thermodynamic efficiency of vapourisation, whilst at the same time enabling Turbine Fluid to vapourise at an increasingly lower heat transference temperature. This achieved by causing the expanding vapour being produced within each cavity on exiting into the central vapour stream to stream along the latter with maximised forward velocity past the exits of following cavities, thereby creating a high forward dynamic pressure and a low side static pressure. The latter then causing entrainment of vapour from following cavities to thereby create a lowered vapour pressure inside said cavities.

Thus facilitating for vapourisation to be effected under a lowering Vapouriser Fluid temperature and causing supercooling of the latter fluid, which first flows at it's hottest for this section around the largest cavity pair situated at the rear, being furthest away from the Turbine end. Then progresses forward around the said range of cavity pairs to the smallest cavity pair at the front of the section, becoming cooler en route as transference of heat is made possible at an increasingly lower temperature due to an increasing entrainment action and lowering of vapour pressure.The design shaping of the central streamlining section including the exits from said cavities being such as to always maintain a maximised forward velocity/forward dynamic pressure from the exiting expanding vapour as allowable by the prevailing temperature, which will vary according to temperature of vapourisation but could be increased upon as required by superheating equipment, in order then to maximise upon said entrainment action. Said superheating being in possible optimisation with mist formation levels which could occur as vapour streams of differing temperatures unite in the central flow to the possible advantage of the process, as under Claim 1 5.

4. Said cavities of Claim 3 having the flexibility of varying design to achieve said dual purpose, but in common comprising a highly hdat conducting side or sides onto which is sprayed the said Turbine fluid at an optimised positioning and angle such as to minimise entrappment of produced vapour in fresh incoming liquid phase. The possibility of other parameter optimisation also being a common aspect of the design as given in the following claims 5 to 9. All of the various aspects of the design being to maximise upon the efficiency of the vapour energy production which in turn will also maximise upon the efficiency of the said supercooling of the said Vapouriser Fluid. As also will the particular shape and size of the said cavities, which are also intended to maximise upon the forward streamlining of the expanding vapour into the central stream section through the said cavity exits.

5. The possible use of adjustable covers across the said cavity exits in Claim 4 to facilitate for a variable entrainment action.

6. Temperature optimisation of said Turbine Fluid in Claim 4 achieved by a fractionalised system of fluid extraction from the-Condenser Unit in Claim 1 and 20 at required temperature-dealt with further in Claim 20.

7. Possible temperature optimisation of said Vapouriser Fluid in said cavities in Claim 4, achieved by an appropriate system of mixing of said fluid in which the fluid is drawn off the said helical flow system at various suitable points along the said Vapourisation Unit in Claim 2 of appropriate differing temperatures, mixed as required to yield desired optimum temperatures and then fed back into the said helical flow system surrounding said cavities at desired points.

8. Suitably facilitating for optimum throughput rate of both the said Vapouriser and Turbine fluids around and within the cavities of Claim 4 respectively.

9. Section D being the rear end sub-system of the said Vapourisation Unit in Claim 2 and essentially comprising a narrow reservoir of the said Turbine Fluid positioned immediately to the rear and lower of said Section A, extending the full width of the said Vapourisation Unit with it's exit appropriately extending into the said central streamlining part of Section A in Claim 4 across the full width of the latter. The main function of this section being to produce vapour to commence the high velocity central vapour stream passing through said Section A.The helical flow system carrying the said Vapouriser Fluid continuing on around the outer of this sub-system to form a surrounding heating jacket and the said turbine Fluid entering in a normal bulk liquid state from the said condenser Unit fractionalised extraction system at an optimum temperature, with vapourisation then being allowed to take place under normal saturated vapour pressure conditions. Middle-low grade heat becoming transferred in this section also effecting further vapouriser fluid cooling as the saturated vapour is produced. The latter collecting above the liquid phase surface and may then be subsequently superheated by suitable equipment in the vapour flow prior to exit of the vapour in order to maximise upon the forward Dynamic Pressure to an optimum level on exit.There also being a Turbine Fluid optimum level maintainer operated as and if required and being comprised of a fluid bleedoff pipe below the liquid phase surface to the said Turbine Fluid reservoir of Section B in Claim 2 and following.

10. Sub-system B in Claim 2 being comprised of an excess of the Turbine Fluid fed from said Condensation Unit at an optimum temperature in a lower reservoir unit situated beneath said Sections A and C and to the right of said Section D, such that the said central vapour stream flowing with high velocity along said Section A then continues on through said Section C wherein lower suction openings exist through which the said entrainment action on the vapour below and above the liquid surface of the said Turbine Fluid in Section B takes place. Having the effect of lowering the vapour pressure therein and therefore the temperature at which vapourisation will take place in said Section B.Thereby causing an increase in the vapourisation rate of the said Turbine Fluid therein and further supercooling of said Vapouriser Fluid passing through said submerged heat exchange pipework system, entering at one end and exiting at the other. The said reservoir probably extending the full width of the said Vapourisation Unit as at Section C stage to maximise upon entrainment and being in depth and length as required. Said entrainment action being at a maximum via design and vapour flow velocity in order to then cause maximum supercooling down to comparatively low temperatures. This aspect being the principal function of said Section B in contrast to that of vapourisation in said Section A.Section B also having a facility for having it's containing surfaces maintained heated if required being effected by channelling hotter Vapouriser Fluid fed from suitable points on the upper main helical flow system down behind the containing surfaces through suitable gaps then on to rejoin said Vapouriser Fluid in said helical flow system surrounding said Section D or in the said pipework system in said Section B as the case may be. The said containing surfaces being highly heat conductive and could effect some vapour superheating by the above means, although it could prove in practice that such heating is required to be minimal.Notwithstanding, the section probably also being equipped with a facility for inflow superheating via suitable equipment in the upper of said section in order to then facilitate for control and thereby optimisation of the temperature of the entraining vapour mainly for mist control purposes on entry into Section C. The section also having the option of two additional facets as following in Claims 12 and 13.

11. The possible sub-division of said Section B in Claim 10 into further sub-systems each with there own individual entrainment connection to the vapour flow through said section C. In order then to apply the suction action of said vapour flow to more effect in lowering the finally obtained temperature of said Vapouriser Fluid in said submerged heat exchange system by effecting improvement in the supercooling profile therein as also in Claim 13.

12. Alternatively the possible introduction of said Turbine Fluid into said Section B in Claim 11 via upward atomized sprays suitably positioned at the base of said Section B. Said spray then passing through said heat exchange pipework in said Turbine Fluid reservoir to thereby effect increased heat extraction efficiency by virtue of spreading but concentrating the incoming Turbine Fluid whilst at it's lowest temperature. Thus maximising upon heat transference temperature gradient over a maximised surface area of said heat exchange system.

1 3. Section C in Claim 2 and 11 being a tunnel the full width of said Vapourisation Unit at this point and as long and deep as may be required for maximised entrainment function, but at the commencement being such as to connect with the said central vapour flow from said Section A, itself being the full width of said Unit, in order that said vapour continues on smoothly through said tunnel. Again being such as to maximise the forward Dynamic Pressure and minimise the static pressure and for this purpose being of a Venturi shaping top and bottom to then yield a maximised entraining action at suitable points along the lower edge of the vapour flow in the throat region of the Venturi tunnel, as induced by said static pressure acting upon the atmosphere of said Section B.Said entrainment points having the flexibility of varied design for most effect, but generally of standard design. However, having the option of all applying to the general atmosphere of said Section B or each being to separate subdivisions as in the alternative design for Section B in Claim 11. In addition in the case of the latter having the possible option of adjustable sliding covers to then be able to control the entrainment profile and thereby the said supercooling profile as in Claim 11.

14. A system in combination with said Section to effect mist control as the colder vapours from said Section B meet the warmer vapours from said Section A involving the use of the vapour superheating equipment as in Claim 11 with possibly some in flow heating inside said tunnel of said Section C. The said system being operated to either eliminate mist production or more likely to create an optimum level of mist at the said meeting of the vapours for the purposes of (i) possibly achieving an improved entrainment action via a condensation suction effect; (ii) possibly better combining of vapour flows; (iii) superdensifying of said Turbine Fluid vapour at this stage in order to thereby facilitate for a boost to forward Dynamic Pressure on re-vapourisation in subsequent inflow heating /superheating equipment; (iv) perhaps improve upon the superheatability of the fluid flow in the said subsequent heating equipment due to the creation of heat sinks. The raising of fluid from said Section B via entrainment to then enter said Section C and yield a Turbine Fluid vapour containing a mist which subsequently becomes revapourised in following heating sections being the basis of a possible two stage vapourisation technique operable in said Vapourisation Unit in Claim 2 to improve upon the efficiency of said Unit.

1 5. Section E of Claim 2 following said Section C being a diffuser section continuing smoothly on from said Venturi tunnel in Claim 1 3 diverging as required but such that as to maintain essentially forward laminar flow.

However sufficiently to cause the vapour flow at this stage to slow down for the purposes of improved heating/superheating by said inflow heating equipment as in Claim 2 and 16/17 following.

16. Heating/Superheating equipment in said Section E of Claim 1 5 of a simple primary nature probably although not necessarily comprising suitably spaced vertical fins in the direction of fluid flow containing built in lateral pipes carrying hot Vapouriser Fluid, again suitably spaced. The said lateral pipes probably being of a special tear drop design in cross-section as may also be the fins in order to then ensure maximum forward streamlining of any revapourising fluid mist and build-up of forward Dynamic Pressure thereof in the initial stages. In this manner therefore commencing said boost to said forward pressure as also in Claim 14, and also having the effect of shifting forward the equilibrium between forward and back pressure.

Furthermore having the effect of protecting vapour flow velocity through said Venturi tunnel in said Section C from retarding back pressure forces which is required to be maximised for said entrainment function.

1 7. Section F in Claim 2 following said Section E being at the broadest and deepest stage of the vapour flow path and therefore at the stage of most lowered forward velocity containing similar but probably more complex in flow heating/superheating equipment as used in the preceding section further facilitating for maximisation of said boost to forward pressure as in Claim 14 and 15. Moreover, similarly protecting the fluid velocity through said Section C from retardation as in Claim 16, whilst also commencing the rebuild of the forward Dynamic Pressure up to a maximum level and helping to overcome back pressure forces created by the subsequent convering section of the long approach nozzle in Claim 18, and by the turbine.

18. Sections G and H in Claim 2 following Section F which together in effect form a long approach nozzle of a converging-divering design respectively, the former section being far longer than the latter. Intended for the dual purpose of streamlining the expanding vapour prior to it's impact with the impellors of the turbine, thereby compounding the final forward Dynamic Pressure of the vapour, and for vapour superheating.The latter being via the main outer helical flow system carrying said Vapouriser Fluid, but for further heating also containing a large central component being of a large tear drop design shaping for maximum vapour flow streamlining and having a similar helical flow system on the out side through which the said Vapouriser Fluid also flows entering at its hottest at the Turbine end and exiting at the other to then effect further heating in earlier sections, probably via rejoining the said main helical flow system.

1 9. The possible use of smaller tear drop cross-section shaped pipes across the vapour stream flow in said Section G in Claim 1 8 for the dual purpose of superheating and to further shift the fluid pressure equilibrium between the forward and backward pressures towards the turbine entry.

20. A special design for the Condensation Unit of Claim 1 comprising counterflow concentric tubes and being used in combination with the special vapourisation Unit wherein the principal feature is the fractionalised extraction system for the condensed Turbine Fluid designed to draw off said fluid from along said Unit at desired points to yield optimum desired temperatures for feeding then to said Vapourisation Unit and to the various sub-systems therein. Said optimum temperatures being determined by desired heat transference temperature gradients optimised against desired Turbine Fluid temperature in relation to onset temperature of vapourisation under the prevailing vapour pressure in said sub-systems, reduced by entrainment or satured as the case may be.The said counterflow concentric tube design being comprised of a central tube and an outer concentric tube with an inner concentric tube between the former and the latter. Said cooled Vapouriser Fluid fed from said Section B entering at one end of said Condensation Unit and flowing through said central and outer tubes, with the said Turbine Fluid entering at the other end and counterflowing through said inner concentric tube in between said tubes carrying said Vapouriser Fluid.

Thereby facilitating for heat flow outwards of the Heat of Condensation from said Turbine Fluid to said Vapouriser Fluid, on either side of the former. The design also being such that said Vapouriser Fluid entering end of said Condensation Unit is much smaller in crosssection than said Turbine Fluid entering end being in accordance with reduction in volume of said Turbine Fluid as portions of the latter are drawn off along this fluid's inner concentric tube in said fractionalised fluid extraction system, and as being conducive to maximisation of heat transfer.Said extraction system comprising fluid take-off pipes passing through the outer concentric tube at appropriate points in accordance with required number of different temperatures of said Turbine Fluid for use in said Vapourisation Unit, but possibly having seven such take-off points ranging from 30"C to 60"C at 5"C increments. Therefore, said Heat of Condensation whilst mainly becoming recycled back to the Vapourisation Unit via transference to said Vapouriser Fluid also having a maximised quantity recycled via said Turbine Fluid itself, which will not only benefit the efficiency of reclamation of Latent Heat but also the efficiency of vapourisation as in Claims 4 and 6.There being one or several banks of said concentric tubes operating together as may be required, all being thermally insulated on the outside to prevent loss of heat to the surrounds. Said condensation Unit also operating with elevated vapour pressure above said Turbine Fluid condensed liquid phase in order to raise/maintain the liquifying temperature of said Turbine Fluid at an elevated temperature conducive to maximum heat reclamation via said two fluids, with the main controlling parameter being that vapour pressure necessary to facilitate for a miaximised optimum transfer of heat to the Vapouriser Fluid whilst minimising Compression Energy thereof.At this end of said Condensation Unit the central and outer tubes comprising the Vapouriser Fluid exits suitably passing through and out of the tube containing the pressurised vapour via turning through 90 , becoming combined flow at the same time.

21. The use of a vapour pressurising pump in-line between Turbine exhaust and said Turbine Fluid entry to said Condensation Unit in Claim 2 and 20 for production and control of said elevated vapour pressure.

22. The possible use of vanes or fins inside the tubes of said Condensation Unit of Claim 20 being in the direction of fluid flow and extending radially outward from the centre to thereby improve upon said outward heat flow from said Turbine Fluid to said Vapouriser Fluid. The number of such vanes or fins being as required and probably containing a suitable number of appropriately sized holes to facilitate for lateral fluid flow within each tube.

23. The possible incorporation of sub-inlets for said entering cold Vapouriser Fluid at suitable points along the outer concentric pipe of said Vapouriser Fluid in the Condensation Unit in Claim 20, in addition to the said main entry at the relevant end of said Unit.

24. The Turbine Fluid pressure produced by said elevated pressure in the Condensation Unit in Claim 20 being maintained as much as practically possible in the sub flows of the extracted fluid up to the point of their entry into their respective sub-systems in said Vapourisation Unit in Claim 2 in order to facilitate for the pressure requirements for said fluid atomization thereby obviating the need for further in-line pumps for this purpose, and also to avoid en route premature vapourisation, being particularly important in the case of the hotter fluid sub-flows.