Abstract:
Studies of the variation in latent heat of fluids with temperature and the rate of heat increase with compression were applied to thermodynamic cycles represented in columns ( 190, 193, 199 ). This showed that heat may be circulated and that power output ( 194 ) can be boosted by catalysts. Practical layouts show that the present  45 % efficiency of thermal power stations may be doubled. The invented layouts produce power from reject heat ( 185, 188 ) and saves the water required of cooling thermal power stations.

Description:
FIELD OF THE INVENTION 
     This invention relates to the fundamental principles of combining different types of energy and systems for converting energy into power, and more particularly for converting heat energy into electric power energy, mostly with gravitational acceleration, according to improvements of the methods and systems disclosed in South African patent number 97/1984 and patent application 98/8561 which has not been published. 
     BACKGROUND TO THE INVENTION AND THE STATE OF ART 
     Denotation: Represent depth below surface by z, measured positive downwards; g to denote gravitational acceleration and m to be mass. For purposes of this application the term: 
     “N” is the ratio of two energy values like two latent heat values; 
     “T-s diagram” means the presentation on a graph with scales of temperature and entropy, of the state of condition of a fluid subject to variable temperature and energy levels; 
     “Work” is one of the forms of energy; 
     “Cycle” means a thermodynamic T-s cycle as presented in a T-s diagram and/or a mass circulation system operating in a closed loop; 
     “Preheating” means to increase the energy and/or entropy of a fluid; 
     “Drenching” means the addition of low entropy fluid(s) to a high entropy fluid(s) to reduce the high entropy of the formed fluid. The lower level of the high entropy limit of the entropy state of condition can also be reached by heat extraction and/or incomplete heat supply to fluid, 
     “Power Cycle” includes thermodynamic cycle(s) employed to produce more output power than power consumed to complete the cycle. In the “conventional” power cycle fluid is pressurised, vaporised or gassified by the addition of heat, depressurised to do work, liquefied by the removal of heat in a continual process to form a cycle. In this document the power cycle includes a cycle in which low entropy fluid, preheated and drenched to any convenient level, is pressurised mostly by gravity, the pressurised fluid is partly depressurised to produce power, heated to higher entropy level by addition of heat, depressurised further by elevation against gravity, fluidised or liquified by the removal of heat in a continual process to form a cycle. The entropy extent of the power cycle is conveniently reduced to a more profitable value by preheating and/or drenching to produce less netto work per cycle and to produce globally more work per co-operating countercycle of a refrigeration fluid. 
     “Refrigeration Cycle” means a “conventional” cycle that discards heat at high, or high and intermediate temperature(s), consumes heat at low, or low and intermediate temperature(s) and consumes and produces heat and work in circulation. fluid(s),mostly gas or vapour at high entropy level is pressurised to a significant extent by gravity in being lowered in a column, is vaporised or liquefied to be a low entropy fluid by the release or rejection of heat, to become a liquid and/or vapour or pre-heated vapour, in order to be of decreased entropy, the low entropy fluid becomes pressurised mechanically and depressurised to a significant extent by gravity, in moving up a column, the depressurised fluid heated by receiving heat to become a gas or vapour or drenched to be a high entropy fluid, recirculated to become a continual cycle. 
     “Countercycle” mens a cycle running in the opposite sense compared to another cycle. In this document a countercycle includes two thermodynamic cycles operating as a combination as a power cycle and a refrigeration cycle, mostly in the sense that the refrigeration cycle prescribes the operation of the power cycle and the combined countercycle consumes heat and produces power. Commonly the temperature range of the refrigeration cycle must be cooler at the cold end and hotter at the hot end of the two thermodynamic cycles. In this document the dominance of the refrigeration cycle over the power cycle is maintained in the sense that power input to the refrigeration cycle maintains the running of countercycles, even if the two or more cycle fluids are mixed to operate at the same temperatures. 
     For purposes of this application Countercycle Power Production is obtained by running a power T-s cycle inside or up to the boundary of a refrigeration T-s cycle. 
     Heat engines and refrigeration systems are well known in the art and have been subjected to extensive theoretical analysis. Typically the systems operate on closed circuits of fluid. 
     With heat engines the fluid is pressurised and then heated, to cause an increase in temperature and pressure. The pressurised fluid is then made to do work, usually by driving a turbine whereafter heat and energy is removed from the system to be pressurised again. Generally, the fluid will be in a liquid state before heating and in a gaseous or superheated gas state after heating. 
     With refrigeration systems a fluid in gas and/or fluid state is compressed mechanically and/or mostly by gravity, which heats the fluid. Heat is removed in a heat exchanger and/or fluid mixer and discarded from the refrigeration fluid. Thereafter the compressed fluid is depressurised mostly against gravity and/or to do work and cool by evaporation. At the lower pressure the fluid is allowed to vaporise partially or in whole to consume heat at low temperature. The low pressure vapour and/or liquid is then pressurised mechanically and/or by gravity to repeat the cycle. 
     Typical examples of the use of heat engines are power stations, and of refrigeration systems are household refrigerators. Some mine cooling systems performs work to reduce the internal, potential, velocity and/or gravitational energy. 
     Although the power and refrigeration systems tend to function well, they also tend to be inefficient due to a number of factors, such as mechanical and thermodynamic inefficiencies inherent in equipment used to do work, and the need to reject heat and/or energy. 
     South African patent number 97/1984 discloses a method of performing work in a cyclic manner. The method being characterised in that the gas and liquid are pressurised to a significant extent by the action of gravity in columns. 
     State of the art features applied are hysteresis loops, velocity energy, and common T-s diagram applications. 
     A yet further feature of the above patent provides for heat flow into the cycle(s) to be used in energy conversion, applying countercycles of fluid at different temperature values, consuming low grade heat and even in freezing water in the process of producing electric power. 
     The above patent further provides for a system for performing work substantially as described above comprising a closed circuit defining a flow path, the circuit being oriented to have an upper and a lower end and such that the action of gravity will cause a predetermined pressure difference in a fluid contained therein between the ends of the flow path. 
     The patent therefore includes gravitational refrigeration of water and power generation in countercycles by applying fluids having dissimilar latent heat exposures. The new application claims new versions of the above which change the application of the academic principles to become practical production units as described in the examples, and displayed in the figures. 
     The applicant&#39;s co-pending South African complete patent application number 98/8561 has not been accepted and has not been published. It describes methods for performing work by the countercycle method including drenching of the power cycle up to 50%. The present application describes variable drenching and/or preheating up to or more than 50%, the gas and liquid being pressurised and depressurised to a significant extent by the action of gravity, the method being characterised in that the density of the fluid in the column is increased by drenching the vapour with a liquid component of the fluid or drenching it by a catalyst fluid or drenching it by any fluid. The new application includes drenching by internal countercycles of similar fluid(s) or mixtures of fluids exceeding 50% drenching. 
     The unpublished patent application 98/8561 further discloses a method for performing work in thermodynamic countercycle in which temperature differences for heat transfer are obtained by applying two fluids with different rates of heat increase for shaft depth increase, applied in a manner which causes heat flow at shallow depth from one fluid to the other and at greater depth to cause reverse heat flow between the fluids. This has now been extended to fluids of similar rates of heat increase and for a continuous variation in fluid mix entropies. 
     The proceeding definitions of terms and figures are applied onwards without limiting the invention by the abbreviated descriptions. The description of the examples and figures are local descriptions only. The basic theories will apply universally and beyond the examples. 
     The state of art including patent ZA971984 is illustrated in FIG.  1  and in the following example which is theoretically correct but unpractical. 
     State of the art example: From patent ZA971984, example 2 it is calculated that power can be produced as shown diagrammatically in FIG. 1 of this document. Columns or shafts of 3574 meters length numbered  2 ,  3 ,  4  and  5  are filled with C318 gas and/or vapour, C318 liquid, HFC134a liquid and HFC134 vapour and/or gas. Input heat exchanger  8  balances the power energy withdrawn at 9. Heat transfer occurs in heat exchangers  6  and  7 . The power yield is 14.8 kJ/kg. The unappropriated shaft lengths and heat exchangers  6  and . 7  are addressed in this text and in FIGS. 14 and 17 of this application. 
     In thermodynamics most operations involving heat may be typified in the classic T-s diagram shown in FIG. 3 by state At condition points  20 ,  21 ,  22 ,  23 ,  24 ,  25  and  20 . 
     The teams of “preheat” and “drench” are shown in FIG.  3 . If heat is applied at  20  the fluid becomes preheated to (say) state of condition  26 . If power (pressure i.e. work) is applied at  26  the state of condition chance to  27  which is also a state of condition of preheat. The entropy of  20  and  21  is increased at  26  and  27 . Similarly the state of condition “gas” at  24  and  25  is changed to “vapour” by withdrawing heat, to state of conditions  23 ,  28  and  29 . The new term “drenching” implies that the high entropy of superheated gas or gas at state of conditions  24 ,  25  and  23  is decreased. The application of preheating and drenching eventually change the shape of the convention T-s diagram to a rectangular or square shape like  26 ,  27 ,  28 ,  29 ,  26 . This T-s shape modification eliminates superheating and it is hereafter commonly applied. Patent 97/1984 states that a refrigeration cycle encircles a power cycle(s) as shown in T-s diagrams in FIGS. 4 and 5. 
     A significant point of the state of art is illustrated in FIGS. 6,  7  and  8 . The conventional condition of state T-s diagram  47  and the conventional shaft length  48  are in conflict as shown by the dotted liens between  47  and  48 . The display change of  47  to  49  by rotation or inversion as defined in patent ZA971984 brings dimensions in correspondence. 
     The T-X hysteresis loop in FIG. 18 is common but its application in FIG. 20 is new. Components of energy are well known. Reference to potential energy in the form of gravitational acceleration and of velocity energy created in jetting, are applied in the inventions. 
     OBJECT OF THE INVENTION 
     It is an object of the present invention to provide methods and systems for converting heat into electric power, by extending the state of the art with improvements to and additions to the methods and systems disclosed in previous patents. It exceeds on previous patents in proposing workable power generation layouts and refrigeration layouts which invite stray heat to be converted to power in 4, 3 or 2 operating shaft layouts. This utilises detailed information of the behaviour of practical thermodynamic fluids, and applies changes in material behaviour associated with induced changes in property and entropy levels of fluids and catalysts. 
     DESCRIPTION OF THE INVENTION 
     The invention is expanding the state of the art information and new methods. The invention includes principles of invented theory, heat balance induction, practical designs, internal countercycles, new techniques to multiply output with the application of preheated and drenched countercycles, etc. The cycles are driven by internal heating on applying gravitational compression on reshaped and equal temperature T-s diagrams. This magnifies output as shown in FIG.  9 . The two column countercycles are based on new interpretations of hysteresis loops subject to gravitational acceleration applying N times countercycles and controlled by regulated temperatures at the top and bottom of shafts as shown in FIGS. 19 and 20. The preferred three column layout is utterly manageable by controlling only the pumping rate. It applies the new internal countercycle T-s diagram principle shown in FIG.  13 . The new fluids composition in the three column layout, may consist of any single or multi-mixed substance qualifying only to safety, inflammability, specified viscosity, density etc. The latter “density” becomes a design feature in so far as, increased pressure limits the physical layout size and improves performance. Ammonia, for example can be pressurised to decrease the vapour volume from 323 liter/kg at 0.382 Mega pascal to 25 liter/kg at 4.8 Mega pascals. Carbon dioxide as a monofluid in countercycle operates at temperatures below the temperature of the surround and this invites the entry of stray energy. The design pressurising fits the state of the art knowledge on pressure underground in mines and applied in rock engineering as well as with new invented feature to supply power “on the job” without contaminating the environment. The substances ammonia and carbon dioxide lend themselves to catalyst action by water. The invention extends to all fluids. 
    
    
     DESCRIPTION AND EXPLANATION OF DRAWINGS 
     FIG. 1 is a schematic display of four working shafts  2 ,  3 ,  4  and  5  filled with two thermodynamic fluids which are not shown. Heat energy is converted to electric power at  9 . The system is continual if circulation pump  10  lifts the liquid in  4 . The liquid is formed in heat exchanger  7  and evaporated in heat exchanger  6 . The second fluid is condensed in reverse, in heat exchangers  7  and  6 . The second fluids in column  3  is compressed by gravity to drive the generator  9  and may require vapour compressor  11 . Details are contained in the state of the art example. 
     FIG. 2 shows sections of a modified layout of columns  2 ,  3 ,  4  and  5  in display  1 . Display  12  is rewarding for design since shell  13  resists the fluid system&#39;s global pressure and shells  14 ,  15  and  16  need to resist partial pressure only. Depending on the design pressure of the fluids, the three internal column shells may profitably be inside or alongside one another at the best remunerating choice. This also holds if only three or two columns are applied. 
     FIG. 3 displays, the classic and known T-s diagram between state of condition points  20 ,  21 ,  22 ,  23 ,  24 ,  25  and  20 . The T-s diagram may be preheated according to the design, say, to line  26 - 27 . Similarly it may be drenched to line  28 - 29 . Note that the remaining T-s diagram is the rectangle  25 ,  27 ,  28 ,  29  enclosing fluid only and it is void of superheated gas. 
     FIG. 4 displays a power cycle  33  completely encircled by a refrigeration cycle  32 . Consequently the power cycle action is completely dominated by the refrigeration cycle which supplies heat q 1  and absorbs reject q 2 . Instability in  31  will be created if energy of any type or form, enters or leaves display  31 . It can be envisaged that electricity leaves at  33  and that balance is resorted to display  31  by supplying heat energy to cycle  32  or  33 . 
     FIG. 5 displays two power cycles  34  and  35  encircled by refrigeration cycle  36 . If cycles  34  and  35  are similar, twice the netto power from  34  may exceed the netto power consumed by  36 . This means that netto power is produced by display  44 . The former reference “twice” will hereafter be called N times. 
     Excessive power yield from  34  and  35  is against the first law, unless input heat is supplied at, say,  39 . If heat  40  plus  41  is less than heat  39 , N must be bigger than two and the netto power yielded by  44  can be increased from two times to N times if the heat shortfall at  39  is not over expropriated. Heat may be supplied to  40  and  41  up to a level that hot end heats  38 ,  42  and  43  are in balance. In this case N can be increased further than described above. 
     FIGS. 6 to  8  in display  46  illustrates a shaft or column  48  and two T-s diagrams. The conventional T-s diagram  47  is the same as  49  except that the signs of T and of S are reversed. In FIG. 8 the work column can be simulated directly with the shaft. For the conventional T-s diagram  47  the simulation lines cross. 
     Note: If friction is disregarded, a kilogram fluid subject to the state of condition on top of FIG. 48 may be freely contained and lowered to the bottom where it will gain condition of state of “shaft bottom”. It may be returned to the top to its original state of condition. Reasoning shows that the enthalpy change along the length of the shaft  48  is the same as the enthalpy change along the work line of FIG. 8, only over one specific shaft depth, called z. 
     FIG. 9 shows the graph of increased power yield according to the state of entropy drenching of fluid HP80, provided that the HP80 power Cycle is encircled by a refrigeration cycle. The increased power yield with the association of shafts stems from the total output yield being equal to the smaller yield of a drenched cycle multiplied by the larger N number of cycles inside the refrigeration cycle. 
     FIGS. 10 to  13  expand on FIG. 3 rotated by 180°. The conventional cycle in FIG. 10 may be slit into, a power cycle  134 ,  135 ,  131 ,  132 ,  133 ,  134  and a refrigeration cycle  134 ,  135 ,  130 ,  128 ,  127 ,  134 . The two cycles are creating an internal countercycle. The power and refrigeration cycles are shown separately in FIGS. 11 and 12. The two cycles may be run simultaneously in vertical shafts of equal length. The first shaft is filled with gas and/or vapour component  142 - 143 . The third shaft contains the components are  127 ,  128  and  129 , this being the liquid shaft for pumping liquid to the top. In the intermediate shaft the components  141 - 134  and  149 - 134  are mixed on top and allowed to pressurise one the other in going down to beyond the T-s diagram to state of condition  135 , up to  152 : At this state of condition power may be extracted up to state of condition  135 . Here the depressurised vapour may be split to complete cycle components  135 - 159  and  135 - 154 . 
     After completing the two internal countercyles in FIG. 13, power leaves the system and this must cause an energy shortfall which can conveniently be compensated for by heat input along line  153 - 160 . In the absence of heating the system in FIGS. 10 to  13  cause global freezing. It delivers power without compensation. Stability is reached with heat supply. 
     FIGS. 14 and 15 are displays for preferred layouts of a number of examples applied to produce the power in a three column physical layouts. The conical shafts allow the velocity energising of fluid in, for example,  172  to store velocity energy, which reduces the physical size of the layout and the total volume. It creates a better condition of state for extracting power energy. The layout in FIG. 14 contains liquid in  173  and  175 , and vapour in the rest of the voids. FIG. 15 is a display of the preferred section through a 3 column power station. It shows a layout adapted specifically to employ catalytic actions like mixing water and ammonia fluids, water and carbon dioxide, or water and compressed air. Dispersion occurs at  187 , heat input at  188  and/or  185 , mixing, jetting and induction of velocity energy at  189 . The mixed mass  191  is pressured and accelerated before passing power generator  194 . The water component in  194  is circulated with pump  195  and the vapour, like ammonia gas rises through  198  to complete all cycles. 
     FIG. 16 illustrates a layout where horizontally flowing vapour  78  is velocity energised in  82  to increase velocity, increase pressure etc on leaving column at  81 . Velocity energy may be applied by extracting liquid at  79 , pressurising the liquid in pump  80  to change the state of condition of the vapour. 
     FIG. 17 illustrates a power generation layout operating in four working shafts,  86  containing pressurised carbon dioxide liquid from  105 , to be distributed by  90  to sprinkle upcoming R125 vapour ( 89 ) to be condensed by evaporation of carbon dioxide. The carbon dioxide vapour is heavier than the F125 vapour and flows downward shaft  87  to be condensed at  99  to form liquid  105  for recycling. Carbon dioxide forms the refrigeration cycles. The R125 forms the power cycle, by being evaporated at  100  on receiving heat from CO 2 , being of low density the vapour moves up column  89 , cools in rising, liquifies at  94 , flows down  88  to produces hydraulic power at  97  before being dispersed at  98  for re-evaporating. Since N is larger than one the generated power is more than the input power to the carbon dioxide. The power delivered must be compensated for by adding heat at  102 ,  83  and/or  101 . 
     FIG. 18 shows a known T-X loop between two fluids X 1  and X 2  which are mixed in a proportion X between 0 and 100%. If T is scaled positive downwards like z, loop line  56  is the liquid condensation equilibrium line and  57  the gas evaporation equilibrium line. In the symmetric loop in display  55 , the two boiling temperatures of the two pure fluids are the same. 
     FIG. 19 illustrates the change in the hysteresis loop of two fluids as a result of gravitational compression from  73  at the top of a column to  74  at the bottom of the column. If the rate of temperature increase for increased pressure of the two fluids are not the same, the two hysteresis loops become rotated as shown in  63 . If the loops in  63  are mirror images, and the shaft related lines pass through the centres of the loops, equal amounts of gas and liquid are formed at the top and the bottom of the shaft. Rotation may be induced as discussed later in FIG.  20 . Heating change the operating temperature from  68 - 69  to  70 - 71 . At  70  most of liquid X 1  is condensed and less of X 2  is evaporated at  71 . This cause column fluid instability which may produce power. It may also cope for unequal latent heats of the two fluids. 
     FIG. 20 is a T-X diagram to fit examples 8 or 10 with mixed fluid inside a two or four column operating systems to produce power without or with less mechanical pressurisaton. Lines  23 / 24  and  25 / 26  are not of equal length. The correct temperature interval choice as modified with velocity energy will cause the result that precisely N times of a specified fluid will evaporate at top and bottom to maximise pro duction. Apply display  77  in FIG.  16 . 
     FIG.  21 : Shafts  117  and  111  are vertical, the first to collect gravitationally driven fluid to produce power at  115 . Latter shaft  111  conveys heated vapour which is not condensing vertically, to loose temperature and joins skew shaft  109 . Condensing liquid in  109  is collected and stepwise transferred by a series of pipes numbered  116  to the vertical column  117  for drenching and accelerating fluid. Each duct is equipped with a partial filled U-tube loop to eliminate vapour gas pressure equalising in shafts  117  and  109 . 
     In the layout in FIG. 21 gasses like CO 2  and R125 will produce power without pumping since R125 will rise in  111  and  109  to cool, liquify and drench mixed fluid. The dense CO 2  vapour will complete the two cycles for delivering power by distillation as shown in FIG.  20 . 
     FIG. 22 shows two working vapour columns  203  and  202 . The gas rotates on being heated at  206  and power is drawn off at  201 . A velocity energy system sucks liquid from  204  apply jet energy at  205  and controls production. 
     FIG. 23 shows curves of temperature, pressure and ammonia solution in water ratio which are applied in examples. The fluid mixture cycle starts at  165  and it may be pressurised isothermally in a shaft to state of condition  164 . The pressurised mixture expels heat in the transition. If the expelled heat is consumed at constat pressure the fluid will change its condition of state from that at  165  to  168  or to a condition between  168  and  164  according to the handling of expelled heat. 
    
    
     SUMMARY 
     The invention applies the theory of thermodynamics, based on two laws. The first law was redefined to include mass to energy conversion in atomic reactions. The second law holds exactly when applied as defined e.g. a Camot cycle or a single temperature entropy diagram (T-s diagram). No reference to the second law could be traced which refers to T-s countercyles. New investigations were conducted on the influence of energy other than heat and work energy together with a T-s diagram, like it&#39;s combination with velocity energy etc, acting simultaneously. The state of art is shown in FIGS. 1,  2  and  3 . Countercycles are shown in FIG.  4  and multiple countercycles in FIG.  5 . T-s cycles with temperature plotted on a positive scale and negative scale are shown in FIGS. 6 and 8 to illustrate that a component of the state of condition of the T-s diagram can simulate fluid in a column ( 48 ). The common T-s diagram in FIG. 6 is inappropriate. 
     Heat, temperature, pressure and work specifications can split a T-s cycles as shown in FIG.  10 . The two fractional cycles together with gravity and catalistic vapour solution are shown in FIGS. 11 and 12, and the combination of two fractional diagrams in combination with gravity in FIG.  13 . The oversupply work  135 - 152  minus input can be withdrawn with no additional reference to heat demand and supply. This work is gravitational and chemical work tendered with the implementation of thermodynamics. Running the diagrams in FIG. 13 shows that work can be delivered with no heat supply. This must freeze the system. To reach stability, heat must be supplied. This heat input, can be supplied at any workable position in FIG.  13 . If input heat comes from the surround the application of the invention will freeze the surround. 
     Heat mass is applied in recirculation of at least one cycle of a system of countercycles in at least two working columns to convert heat energy into work energy by applying gravity and chemistry. The heat mass of the two fluid systems may be equal. One of the cycles may dominate the thermodynamic behaviour of the other. One of the fluids may liquefy when moving upwardly along one of the columns. The fluid in liquid form in the one column may drench the fluid in the other column and may evaporate the condensed fluid. The difference in the fluid densities may cause a pressure difference at the bottom of the columns. The arrangement may be such that the pressure difference may yield output power and may require heat input. 
     The combined mass of multi-cycles may enforce excessive enthalpy in fluid at an enforced intermediate entropy level of fluid(s) in shafts to enable heat to be converted to power. 
     The system may apply carbon dioxide or mostly carbon dioxide to form a countercycle converter and/or a recycling countercycle to change heat energy into work energy. 
     The system may operate with column(s) and fluid(s) at drenching as well as preheating of very high orders, which may equal or exceed 50%, on condition that drenching plus preheating does not exceed 100%. 
     The system may recirculate energy in one or more cycles in countercycles to convert heat energy into power at an efficiency of up to 100%. 
     The first aspect of the invention produces power generation by combining thermodynamics, catalysts and gravity in T-s Internal countercycles and gravitational work as shown in FIGS. 10 to  13 . The variable catalyst action is not displayed. The preferred layout is shown in FIG. 15, including the positions where appropriate state of conditions numbers  134 ,  135 ,  152 ,  159  and  160  of FIG. 13 apply. State of condition point  134  in the figures does not pre-specify the entropy of point  134 . The percentages drenching and preheating are therefore not pre-specified. Apply liquid in column  193  and vapour in columns  192  and  199  of FIG.  15 . The state of condition points  159  and  106  apply in column  199  to simulate low entropy fluid. To produce power the pump  195  must be applied. 
     EXAMPLE 1 
     Process Scarel Apply the internal T-s countercycle process on the fluid consisting of “pure” CO 2  and water as a catalyst operating at −8° C. at a pressure of 2.8 MPa and 60% drench plus 40% preheat in a 286 m vertical column. The calculated results show that the minimum power yield is 1.52 kJ/kg CO 2  (4 kg cycle). To obtain “120 megawatt” it will be required to circulate 315.2 Ton/sec of CO 2  and the total mass of fluid in the three shafts in FIG. 15 must be 30047 tons of CO 2  flowing at an average speed of 3 meters per second. As shown in FIG. 2 the three columns fit in a circular shaft of 28.4 m diameters. 
     EXAMPLE 2 
     Process Fanie To produce 120 megawatt power in example 1 it requires heat input at −8° C. equivalent to 120 megawatt. The input heat may be withdrawn from water stored at 10° C. and cooled to become ice at 0° C. A kilogram water delivers 352 kilojoules heat to become ice. At full capacity process Fanie will produce 1225.2 ton ice per hour which becomes 0.882 million kiloliters potable water per month, on top of the power delivery of example 1. 
     The second aspect of the invention specifies that heat must be supplied somewhere in FIGS. 14 and 15 otherwise the first aspect will create operations of indefinite freezing. The heat may be supplied at any temperature above the state of condition points of FIG.  13 . Most of the examples calculated start at temperatures below freezing point. The heat may originate from running water which may be frozen. If polluted water or sea water is frozen the ice is not chemically polluted. Pollution components may be separated and exploited. The ice, when melton, is consumable water to be sterilised to be potable in general. 
     An extension of the second aspect shows that the system in the first aspect produces a global freezer applicable in all applications of freezing. 
     The Third aspect of the invention claims that the power required for sprinkler irrigation may be withdrawn from the water to be sprinkled, that sprinkling with cooled irrigation water causes less evaporation from the sprinkled water and provides better quality water to the soil being sprinkled. 
     EXAMPLE 3 
     Withdraw heat from flowing water applied at a sprinkler or a township to deliver 300 kilowatt in a shaft of 40 meter depth. The 300 kilowatt is sufficient to drive a sprinkler irrigation spill point system or a township&#39;s power demand. Lowering of the temperature of the flowing water by 5° C. reduces the spill point water evaporation during sprinkling. More than 5° C. lowering may be applied. The column diameters for power from the sprinkler system are: 1.8 m for compressed air, 1.5 m for the mix column, 0.29 m for the water column and if the two smaller columns are contained in the large column its diameter must be 2.2 m. 
     The Fourth aspect of the invention claims that principally the layout in FIGS. 14,  15  and  17  implies that energy is recirculated. To create stability in FIG. 13 it is required that power may be withdrawn at  135 - 152  in FIG.  13  and the same amount of heat returned, to complete the internal countercycle associated with gravitational acceleration. 
     Fluid following the T-s thermal path of a theoretically closed thermodynamic cycle is in fact ideally a circulating system with specification for the boundary value input and output. 
     In other professions and trades the continued use of matter is called recycling. This often happens without a change in substance. In thermodynamics countercycles recycling, may yield more work without consuming proportionally more heat. The rate off flowing of one or both cycles in FIG. 13 may be changed. 
     Instability caused by oversupplying input heat and/or producing less power will systematically increase the global temperature like a heater. Stability can be reached by disposing of heat, similar to thermal power stations. 
     An operating layout may be unstable and satisfying boundary conditions temporary. Recycling may be over driving power production without sufficient increases of input heat, like a refrigerator or like closing a thermal power station. The temperature level of the whole layout will then decrease, operating as a global freezing unit. Stability is reached by any of: 
     consuming heat from the exterior 
     input heat leaking to the set up 
     cooling another layout 
     stopping. 
     It is obvious that the fluid of an internal countercycle power station, as described above, can be recirculated or one cycle may be recycled according to design specifications and boundary conditions. Between the conditions described above, stable energy recycling, nominal heat input and power output will cause conversion of heat into power at efficiencies approaching 100%. 
     The Fifth aspect of the invention is to operate preceding aspects with fluids which are not hostile to life. The most common fluids in life are water and air which are applied in example 4. Ammonia is a good catalyst which is not human friendly. For the example assume that 120 Megawatt must be produced in three columns of 96 m length, that the heat intake temperature is 4° C. and drenching is 60%. 
     EXAMPLE 4 
     Process Jaja: Apply the preferred layout in FIG. 15 to circulate air catalysts and water compressed to 3.0 MPa. Water is contained in  196 ,  193  and  187 , and the air flows in  199  across heat supply  185 . It becomes mixed with water in  187 , compressed in  192 , and delivers power in  194 . The starting temperature at  187  is 4° C., allowing for heat input at  185  from reject heat at thermal power stations, water or mine ventilation. Calculations apply a 10 m/sec flow rate to show that 120 Megawatt is generated by re-circulating 2 931 ton of water and 1 961 ton of air filling the 96 m tall columns. The column excavation volume is 55.3×10 3  m 3 . In this example the increase in operating pressure from 3.0 MPa to 3.084 MPa apply at the 96 meter shaft bottom. The layout can be fitted in 3 shafts of average diameter 23.3 m (air), 192 m (mix) and 3.7 m (water), or the 3 columns in one shaft of 28 m diameter. To reduce the diameters the shaft lengths may be extended. 
     The Sixth aspect is that example 4 may be scaled down to be installed in operating mines for the provision of power and simultaneously airconditioning the mine. 
     EXAMPLE 5 
     Process Fanie: Compare the power delivered by hydraulic means with power delivered by one of the invented methods. The latter consumes energy by lowering the temperature of the water by 5° C. Given: Vanderkloof dam delivers 120 Megawatt hydroelectricity on consuming up to 217 m 3 /s water at a hydraulic head approaching 96 m. The invented method tested here, applies 20% drenching to R125 CFC gas mixed with carbon dioxide in four columns of 96 m. Heat extracted to lower the temperature of 217 m 3 /s water by 5° C. equals 4542 megawatt. This is 37.85 times more than the delivery capacity of the hydroelectric installation at Vanderkloof dam. 
     The compared invented method applies 20% drenching to R125 to improve the output according to FIG. 17, and applies velocity energy to regulate the process. 
     The seventh aspect of the invention is to apply catalytic action in the production of power. It improves the efficiency of the layout as shown in examples 6 and 7. 
     EXAMPLE 6 
     Show that catalytic action can be applied together with internal countercycle power generation. With reference to FIG. 23, start at state of conduction  165  for the mass composed of 15% ammonia gas at 0.3 MPa and 290 K, 35% liquid water and 50% nitrogen gas or other non-reacting fluid at 8.0 MPa and 290 K. According to Dalton&#39;s law the total pressure should be 8.3 MPa and after lowering by 250 m as shown in FIG. 15 the pressure at  198  should be 8.4 MPa. Isothermally the 15% ammonia gas should dissolve completely in the water and release 180 kilojoule heat for 1 kg fluid. According to the design most of this heat will be consumed in ammonia gas forming after power delivery. In the heated intermediate stage the heat can produce power. The liquid is recycled with pump  195  and the ammonia gas will circulate along  198  and  199  to be drenched again at  187  to complete the cycles. The exact output power at  194  will be more than 10 kJ/kg fluid,-depending on the design. 
     EXAMPLE 7 
     The catalytic action in example 6 will operate in a mechanical layout consisting of a compressor(s) and/or centrifuge(s) for compression, an expander(s) to produce power and heat exchanger(s) for heat input to complete the internal counteracting T-s diagram in FIG.  13 . 
     The examples 6 and 7 demonstrate that the pressure and temperature sensitivity of the solubility of ammonia in water (FIG. 23) can be applied as shown in FIG.  14 . The evaporation and condensation heat is successively conveyed to compressed nitrogen or other fluid to do the additional work. 
     The eight aspect of the invention expands on the fifth aspect, in so far as the combination of gravitational energy plus catalytically produced energy is more than gravitational energy. Catalytically supplied heat may be withdrawn by applying centrifuges and expanders to produce power. 
     The ninth aspect of the invention modifies the power T-s cycle to produce and deliver more power from the combined countercycles. Preheating and drenching reduce the entropy interval of the power cycle, and consequently more power cycles fit inside the refrigeration cycle. The reduced power cycles individually yield less power. The total output is the product of individual power cycles times N, the number of cycles. This product increases as shown in FIG.  9 . 
     The tenth aspect of the invention applies the well known hysteresis loop between evaporation and condensation of a varying mixture of two fluids as shown in FIG. 18, together with the distortion of loops by gravitational action in shafts as shown in FIG.  19 . On regulating the temperature in two shafts the distorted loop displayed in FIG. 19 yields various percentages of the mixed fluids X 1  and X 2 , as shown by analyzing line  68  to  69  in relation with line  70  to  71 . Skew displays, to advance power production as shown in FIG. 20, are obtained by regulating the temperature related via the velocity of flow to the pressure. The tenth aspect is implemented in preferred layout displays shown in FIGS. 21 and 22. 
     EXAMPLE 8 
     Demonstrate that power production operates in two columns as shown in FIG.  21 . Consider CO 2  and CFC called HP80 on the assumption that no chemical reaction occurs between the fluids. To obtain equal heat masses mix CO 2  and HP80 (20% drench on 20% preheat) in the ratio 28% CO 2  and 72% HP80. Let X 1  be CO 2  and X 2  be HP80. FIG. 20 shows that the vapour will contain more R125 at the bottom of the shaft and less at the top of the shaft. The fluid specific volumes of 18 and 11 l/kg confirms that CO 2  gas will move down and HP80 gas will move up, to condense and avail HP80 liquid at the top of the column to a much bigger extent than CO 2  liquid. When applied in a display as shown in FIG. 21 the CO 2  will be highly drenched to accelerate the operation of the system. 
     No formula or experience avails to calculate the output. Nominal estimates show that a mass of 269 ton in a 96 m column will produce about 1.4 megawatt power production. 
     EXAMPLE 9 
     Apply fluids carbon dioxide and R125 (chemically CHF 2 CF 3 ) in four columns of 10 m length and fluid mixing, as displayed in FIG.  17 . Regulation occurs at  93  by velocity energy and power is generated at  97  from R125 and CO 2  fluid mix as well as at  83  from high entropy fluid. The R125 and CO 2  gas is self circulating due to densities. Production is regulated by liquid pump  103 , power production pump  83 , generator  97  and velocity pump  93 , at a temperature of 280K. Calculations show equal heat masses for 1 kg CO 2  and 1.65 kg R125 if not drenched. Drenching will increase production as shown in FIG.  9 . Full cycle power production is 72 J/kg of CO 2  circulated or 13.5 J/kg from the total mass of circulated gas and z=10 m: It can be increased by drenching. At 10% preheat, 10% drenching and fluid flow velocity 20 m/sec the power production increases to 129 J/kg total mass or 24.2 per kg of cycle mass. A practical application of the latter case shows that 3 kilowatt can be generated in a column of 10 m long and 2.2 m diameter. An enlarged layout of 120 megawatt at column height of 48 m requires an encircling shaft of 77 m diameter, which is impractical. For this capacity a column of 300 m long and diameter of 30.8 m is more proportional. 
     The eleventh aspect of the invention applies fluid mixing and fluid selections to eliminate two large heat exchangers of the state of the art displayed in FIG.  1 . The selection of fluids yield power at  83  in FIG. 17 from density differences between vapours as shown in example 9. This is a further aspect of producing power, additive to liquid induced power production at  97  and in FIG.  17 . 
     EXAMPLE 10 
     Apply the display in FIG. 22 to generate power. The display shows two independently acting mechanisms. The first is liquid store  204 , liquid pump  207  and at  205  a generator of velocity energy which is mostly recoverable. The second mechanism consists of heat source  206  supplying energy to vapour  203  which, as a result of heating, is of smaller density than vapour  202 . In the columns the difference in density causes circulation and therefore deliver power at  201 . If the rotation speed is increased from (say) 1 to 10 m/s by velocity energy, the vapour power delivery will increase ten times. Given the vapour ethylene (C 2 H 4 ) at 265 K, 3.35 MPa having S=−1.519 which is combustible but not fired. Operations run at about −8° C. and the liquid in  204  is also ethylene. Create an entropy level on leaving  205  to be on the liquid saturation line. Energy from  206  will expand the fluid gas to cause a light density in column  203 . On withdrawing power at  201  the temperature and pressure drops and the gas in  203  will be drenched by fog in  202 , which enhances the vapour power production induced by gravity in the columns. No data for sample calculations avail. 
     EXAMPLE 11 
     Apply the reject heat of the thermal power station Lethaba (heat from coal) on applying the process described in example 4, operating at −8° C. according to the example. The reject heat from the thermal process can be converted to power in total. Assume the six times 618 Megawatt Lethaba power station runs at 45% efficiency then the example referred to, will deliver an extra 4532 Megawatt and on top it will save about 58 million cubic meter water from Vaaldam applied to evaporate the power station reject heat. 
     The twelfth aspect of the invention involves a system to run countercycle power production inside two only columns for fluid flow. The columns are coupled intermediately with liquid conveyance pipes for drenching and pressure isolation, as shown in FIG.  21 . In example 8 it was shown that the T-x behaviour in FIG. 20 dominates evaporation and delivers high density CO 2 , well drenched, to reach power converter  115  and yield output power. The rate of power production will be influenced by velocity inducer  121 . The heat input  113  in FIG.  21  and the velocity generator  121  dominate the production of the system. 
     The thirteenth aspect of the invention applies internal fluid drenching in 2 columns as shown in FIG.  22 . The condition of state of the two fluids in  203  and  202  impel circulation and output power generator  201  and heat input  206  establish a temperature according to production. 
     Display  208  is designed to operate near the vapour saturation line of a fluid and operates well if the vapour density is high, e.g. for CO 2  which can be applied to operate between +30° C. and −100° C., depending on the quality of the input heat source. 
     The Fourteenth aspect of the invention relates to the residues left over after water extraction by freezing. This is a field by itself. Reference may be made to mineral extraction from the dead sea and to sea salt extraction at Port Elizabeth, both as a result of water removal. 
     The Fifteenth aspect of the invention relates to a practical design and application of the invention operating in water. The entire power station may float in water. The mass of air in the power station, functioning for example on water heat, water, a catalyst and air, can be increased to reach the air pressure required for optimal functioning. The air mass increases the density of the global power station. Consequently the power station will sink down the water and stabilise at the bottom of the water. On stabilisation the production of power may commence. Being stable at the bottom the power station cannot move round as a result of waves or water current during operation. If repairs have to be made, the high pressure air and/or water masses are released, the power station will float like a ship and normal open air repairs can be applied to the power station as a whole. The external water pressure counters internal pressure of the power station, yielding an economical design. 
     The design is normally tested at twice the open air operational pressure. If the external water pressure is three times the operational pressure the internal air pressure can be raised to (1+3)=4 times the open air design pressure, eg, design the power station for one MPa, cover the power station with 300 m of water (supplying operating heat) and operate the power station at four MPa. This reduces the physical size of the power station to a fraction of the equivalent size of a 4 MPa open air power station. 
     The sixteenth aspect of the invention relates to the stability of an under water power station and the stability of power generating equipment in the power station. Displays  12  in FIG. 2 shows high entropy fluid(s) in a fraction of the circumferential column area and low entropy fluid(s) in the other fraction of the column area. This is thermally well in rock but will cause tilting in water. Under water the circumferential column can be prevented from tilting by placing columns  14  and  15  in opposing positions in column  13  and by choosing column flow speeds in  14  and  15  to equalize the mass distribution in column  13 . 
     DESCRIPTION OF PREFERRED EMBODIMENT OF THE INVENTION 
     The layout  186  in FIG. 15 is the preferred layout. It lends itself to scaling, power production and the freezing of water to yield potable water. An appreciable advantage of the three column layout compared to the two and four column layouts vests in the fact that evaporation and condensation of the two fluids are mechanically enforced. 
     The system  186  comprises three columns namely  191 ,  193  and  199 . Column  199  contains gas, drenched vapour and/or vapour. Column  193  contains liquid, preheated liquid and/or low entropy vapour. Column  191  contains a fluid mixture consisting of liquid plus vapour and/or gas. The system  186  further includes a pump  195  for circulating liquid or low entropy fluid by force; an electric power generator  194 ; a drenching disperser  187  a fluid mixer  134 ; a heat input  185 . If required velocity energy for circulation may be applied at  187  by over pressurising pump  195 . 
     The three columns  191 ,  193  and  199  are filled with a mixture of a suitable fluid or pure fluid such as a refrigerants HP80 and F125 mixture or pure carbon dioxide. For ease of calculation purposes, it is assumed that column  193  and sump  196  contain liquid only. 
     To produce power the liquefied fluid of high density  196  is elevated with pump  195  along  193  and dispersed in  187  and  134 . Partly or wholly gasified fluid  199  of low density is elevated against gravity by induced vacuum or mechanical circulation if necessary and mixed in  189 , providing mechanical circulation. At  134  the action may include jetting and/or drenching. 
     Note that the division line  134  to  149  in FIG. 12 depicts a refrigeration cycle component and lines  134  to  141  in FIG. 11 depict a power cycle component. The fluid state of condition points of FIG. 13 are indicated in FIG. 15 showing the work output cancelled by gravity in  159  to  160  in column  199 . 
     The input work against gravity in FIGS. 13 and 15 extends from  153  through pump  195  to the high pressure stage  155  and pressure is decreased by flowing against gravity to state of condition  135  to  134  at the top of column  191 . For ease of calculation assume a 50% mass mixture of gas and liquid at disperser  187 . One kilogram per second fluid in columns  193  and  199  result in 2 kilogram fluid per second in column  191 . The state of condition of fluid in column  191  change from  134  to  152 . In passing through power generation  194  the state of condition becomes  135  to be separated into liquid  154  and gas  159 . This completes the power generation countercycle in FIG. 15 as well as the thermodynamic cycle in FIG.  13 . Assume a shaft length of z o  from h=mgz o  in which h is enthalpy change of gas from  159  to  160 . 
     If m 1  is the mass flow rate of liquid, m 2  the mass flow rate of vapour and/or gas and z o  the column depth the analysis of work in FIG. 13 shows. 
     Work input in column  193  ( 153  to  187 )=−m 1 gz o    
     Work input in column  199  ( 155  to  153 )=−m 2 gz o +hm 2 =0 
     Work output in column  191 =m 1 gz o +m 2 gz o −hm 2    
     Netto work output=hm 2 +m 2 gz o =0 
     The theoretical analysis does not explain why work can be withdrawn from  152  to  135  in FIG.  13 . If a catalyst is included in the fluid it will decrease the temperature of  134  d increase the temperature of  152 , to produce more output power.