Process for utilizing energy produced by the phase change of liquid

The present invention relates to a process for utilizing energy produced by the phase change of liquid, such as fluoronated hydrocarbon, light fraction hydrocarbon, lower alcohol and ethers using the heat coming from unused heat sources for example, the heat of the earth, the heat of hot springs, the heat of the warm waste water of factory and power plant. The present invention is applicable to transfer the heat of the unused heat source from the low place to the high place in order to use said heat for farming and cultivation at the high and cold places. The present invention is also applicable to transfer of the mass energy of the liquid from the low place to the high place by uniformly mixing the said liquid with the ascending saturated or super-saturated vapor of the said liquid.

BACKGROUND OF THE INVENTION 
The present invention relates to a process and an apparatus for utilizing 
energy produced by the phase change of a liquid. Generally speaking, the 
liquid possesses the characteristic properties that the saturated vapor 
pressure of the liquid increases with the temperature increasement in the 
range of temperature between the freezing point of the liquid and the 
critical temperature thereof, while the saturated vapor pressure of the 
liquid decreases with the temperature decreasement thereof. The saturated 
vapor of the liquid condenses, when a pressure higher than the saturated 
vapor pressure of the liquid is added to the saturated vapor of the 
liquid, while the saturated vapor of the liquid is liquefied with the 
temperature decreasement of the liquid. The phase change either of the 
liquefaction of the vapor or the gasification of the liquid occurs 
depending on the interrelationship between the temperature change and the 
pressure change, the saturated vapor pressure of the liquid being the 
border therebetween. It is necessary to give the latent heat of gasifying 
the liquid in order to cause the phase change of gasifying the liquid and 
to remove the condensation heat from the vapor of the liquid to liquefy 
the vapor. The present invention relates to the process utilizing energy 
in which the principle mentioned above is applied, namely, the process 
relates to the process utilizing energy characterized by forming the 
circulating circuit comprising (a) the step of ascending the vapor of the 
liquid from the low place to the high place utilizing the pressure 
difference between the vapor pressure of the liquid generated when the 
liquid is vaporized by being heated at the low place and that generated 
when said ascending vapor of the liquid is cooled to be liquefied at the 
high place; (b) the step of cooling said ascending vapor at the high place 
to be liquefied and preferably, utilizing the heat energy of the ascending 
vapor when said vapor is liquefied; (c) the step of utilizing the 
potential energy of the liquid which has been liquefied at the high place 
and (d) the step of vaporizing the liquid after it has descended by 
repeated heating of the said liquid. The specific substance, for example, 
Fron-22 and Fron-500, which are the trademarks of fluoro-carbon polymers 
manufactured by Daikin Industrial Co. of Osaka, Japan, are vaporized 
within the vaporizer by the aid of the heat coming from the unused heat 
source, for example, the heat of the earth, the heat of hot springs, the 
atmospheric temperature, the solar heat, the heat of the sea water and/or 
the heat of the warm waste water of factory and power plant. The vapor of 
the specific substance ascends from the low place to the high place 
through the conduit connecting said high and low places by the pressure 
difference between the vapor pressure generated at the low place and that 
generated at the high place. The vapor pressure of the ascending vapor at 
the high place depends on the vapor pressure generated at the low place, 
the weight of the vapor which is the product of the height of the conduit 
and the density of the vapor, the loss of the vapor pressure caused by the 
inner resistance of the conduit and the depression of the temperature 
within the conduit. At that time, the phase state of the fluid within the 
conduit is the liquid state, the wet vapor state, the super-heated vapor 
state or the gaseous state, depending on both the temperature and pressure 
influences. The ascending vapor within the conduit at the high place is 
led to the heat exchanger or the cooling apparatus to be cooled by means 
of the atmospheric temperature, the water temperature, the wind 
temperature and the latent heat of evaporation of water, whereby said 
vapor is cooled and liquefied, the heat of the condensation being taken 
away through the heat exchanger or the cooling apparatus. 
The temperature and the pressure of the liquid vapor to be liquefied are 
determined on the basis of the characteristic feature of said liquid, when 
the said liquid is selected taking in account of the sort of the heat 
source to be utilized, the temperature and the amount thereof, the cooling 
capacity of the heat exchanger, the diameter of the conduit, the height 
and the length thereof and the capacity of the heat insulation of the 
conduit. The more the pressure difference between the vapor pressure 
corresponding to the temperature of the condensed liquid at the high place 
and that of the ascending vapor coming from the low place becomes large, 
the more the amount of the ascending vapor increases. The liquid liquefied 
by removing the heat of the condensation through the heat exchanger or the 
cooling apparatus at the high place is gathered into the liquid storage 
tank positioned beneath the heat exchanger and then the potential energy 
of the descending liquid is utilized to the power source for driving the 
turbine while descending within the conduit, and finally the said liquid 
enters into the vaporizer using the unused heat source. The pressure of 
the liquid at the inlet of the vaporizer, after driving the turbine, is 
determined by the sum of (A) the product of (a) the difference of the 
height between the position of the liquid storage tank provided below the 
turbine and that of the inlet of the vaporizer and (b) the density of the 
liquid, and (B) the inner pressure of the said storage tank corresponding 
to the vapor pressure of the liquid within the liquid storage tank. As the 
pressure of the liquid at the inlet of the vaporizer is necessary to be 
higher than that within the vaporizer in order to feed the liquid into the 
vaporizer, it is important to determine the position of the liquid storage 
tank provided beneath the power plant. As occasion demands, the liquid 
liquefied may be fed under the pressure into the vaporizer to raise the 
liquid pressure by the aid of a pump. 
The liquid suitable for use in the present invention demands the following 
phase change characteristics, from the efficiency standpoint: 
(1) The relatively small latent heat of the vaporization of the liquid. 
(2) The high vapor pressure, the low density and the low viscosity at the 
temperature of the vaporization. 
(3) The low vapor pressure, the high liquid density and the low viscosity 
of the liquid at the temperature of the liquefaction. 
(4) The high chemical and thermal stability of the liquid. 
In case that the circulation circuit of the present invention for utilizing 
energy is used to transfer the heat energy from the low place to the high 
place, that is one of the objects of the present invention, it is suitable 
to use the liquid having the high latent heat of the vaporization. 
Moreover, it is necessary to take the following characteristics (the 
capacity and the construction) of the apparatus of the present invention 
into consideration in order to select, with the good efficiency, the 
liquid having the characteristics suitable to the arrangement of the 
apparatus of the present invention, the heating medium and the amount of 
energy to be absorbed. 
(1) The heat value to be absorbed and the temperature of the vapor in the 
vaporizer depending on the temperature and the amount of the heating 
medium in the heating and vaporizing apparatus. 
(2) The heat value to be cooled and the temperature of the liquid liquefied 
depending on the mass and the temperature of the liquid in the cooling and 
liquefying apparatus. 
(3) The difference of the height between the position of the vaporizer and 
that of the cooling and liquefaction apparatus, the diameter of the 
conduit, the root, the total length of the inclined conduit, the inner 
resistance and the heat insulating capacity of the conduit. 
(4) The amount of energy to be utilized. 
(5) Variations of the various factors and the surrounding conditions during 
all the year. 
The liquid suitable to be used in the present invention comprises, for 
example, fluoronated hydrocarbon, chlorinated hydrocarbon, brominated 
hydrocarbon, fluorochloro hydrocarbon, fluorobromo hydrocarbon, light 
fraction hydrocarbon, lower alcohol, lower thioalcohol, lower alkyl ether, 
lower alkylthioether, alkylsulfoxide, toluene, xylene, or the mixture 
thereof and ammonia. 
The circulation circuit of the present invention is used to transfer the 
potential energy from the low place to the high place, that is another 
object of the present invention. 
To mainly utilize the potential energy, the liquid or the heated liquid is 
uniformly mixed with the saturated vapor or the super-heated vapor of the 
said liquid generated in the vaporizer positioned at the low place. The 
wet-vapor stream containing the mist of the liquid ascends from the low 
place to the high place by the vapor pressure of the ascending vapor. The 
ascending of the wet vapor stream containing the mist of the liquid is 
carried out by the pressure difference between the vapor pressure of said 
stream ascending from the low place and that of said stream at the 
liquifying temperature when it is liquified at the high place. The energy 
of the ascending vapor is converted to the potential energy by selecting 
and regulating the degree of drying of the ascending dry vapor to the 
optimum value by means of uniformly mixing the liquid or the heated liquid 
with the ascending dry vapor taking the said height and the temperature or 
pressure difference of the vapors therebetween into consideration thereby 
effectively utilizing energy of the ascending dry vapor at the low place, 
economizing energy required to condense the wet-vapor at high place, 
producing the large amount of the potential energy of the liquid and 
enhancing the utilizing efficiency of the energy held in the ascending 
vapor. Namely, in case that it is unneccessary to utilize the heat energy 
of the ascending vapor at the high place, as the process for effectively 
utilizing the heat energy and the ascending energy of the ascending vapor, 
the said liquid is uniformly mixed with the vapor coming from the 
vaporizer to make the wet-vapor thereby increasing the amount of 
transferring the liquid from the low place to the high place and 
relatively reducing the cooling energy for condensing the wet-vapor at the 
high place and producing the potential energy with good efficiency. 
According to the process as mentioned above, it makes possible to obtain 
the large potential energy in case that the distance between the low place 
and the high place is short, namely in said case, the utilization 
efficiency of the potential energy of the ascending vapor is greatly 
impvoed by using the wet vapor containing the mist of liquid instead of 
the dry vapor of liquid. 
SUMMARY OF THE INVENTION 
The present invention relates to a process for utilizing the heat energy 
and the potential energy produced by the phase change of liquid such as 
fluoronated hydrocarbon, light fraction hydrocarbon, lower alcohol and 
ethers using the heat coming from the unused heat sources such as the heat 
of earth, the heat of hot springs, or the heat of the warm waste water of 
factory and power plant.

DESCRIPTION OF THE PREFERRED EMBODIMENT 
The present invention is explained by virtue of the figure as follows: 
The liquid enters into the liquid storage tank 5 descending along the 
conduit 42, after driving several generators 1, through the flow control 
valve 2 and the check valve 3 provided the output of the turbine 
(generator) 1. There is arranged the detecting and controlling mechanism 
for controlling the liquid temperature, the pressure and the liquid 
surface within the tank 5 which consists of the thermoelectric couple 6, 
the pressure transmitter 4 and the differential pressure transmitter 27. 
The liquid pressure within the conduit 7 generally increased while 
descending the conduit 7 due to the difference in height between the 
height 44 of the tank 5 positioned below the turbine and the height 45 of 
the liquid inlet of the heating apparatus 17 and the density of the liquid 
and finally becomes higher than the vapor pressures generated within the 
heating apparatus 17 and the vaporizer 23 thereby feeding the liquid into 
the heating apparatus 17. The liquid descending within the conduit 7 
enters into the heating apparatus 17 through the flow controlling valve 15 
and the by-pass valves 11, detecting the liquid pressure within the 
conduit 7 by the pressure transmitter 8 and the flow rate of the liquid 
within the conduit 7 by means of the flow transmitter 14. 
When the liquid pressure is lower than the predetermined pressure, the 
liquid is introduced into the heating apparatus 17 through the check valve 
13 after raising the liquid pressure at the predetermined level by means 
of the booster 10 which is operated by closing the by-pass valve 11 and 
opening the control valves 9, 12 and 13. The flow rate of the liquid 
within the liquid storage tank 5 is controlled so as to maintain the 
liquid level within the tank 5 to the constant level by the linkage of the 
differential transmitter 27 and the flow regulating valve 15 arranged at 
the inlet of the heating apparatus 17. The liquid entering into the 
heating apparatus 17 is heated to the requisite temperature by the warm 
waste water exhausted from the factory and the power plant, the hot steam 
spouting out from the earth, the heat of the hot springs and/or the warm 
wind. The temperature of the wet steam spouting out from the outlet of the 
heating apparatus 17 is controlled to be the predetermined level by 
regulating the flow rate of the heating medium which is fed into the 
heating apparatus 17 by means of the control valve 18 according to the 
indication of the thermocouple 19. 
The liquid heated to the predetermined temperature enters into the 
vaporizer 23 through the flow controlling valve 52 and the check valve 20 
detecting the flow rate of the liquid within the conduit 16 by means of 
the flow transmitter 51 and vaporizes. The temperature and the pressure of 
the vaporizing liquid are detected by means of the thermocouple 24 and the 
pressure transmitter 22 provided at the outlet of the vaporizer 23 is 
controlled so as to become the requisite pressure by means of the control 
valves 24, 25 and 53. 
The surface of the liquid within the vaporizer 23 is detected by the 
differential transmitter 26, and the flow rate of the vaporizing liquid at 
the outlet of the vaporizer 23 is detected by means of the flow 
transmitter 21. The vaporizing liquid coming from the vaporizer 23 ascends 
to the predetermined level within the conduit 28 by the aid of the 
pressure of the vaporizing liquid. 
In order to mainly utilize the potential energy of the liquid, the liquid 
coming from the heating apparatus 17 is fed into the gas-liquid mixer 58 
through the conduit 60 andthe check valve 56 in order to uniformly mix the 
said liquid with the ascending dry vapor coming from the vaporizer 23. The 
amount of the liquid fed to the said mixer 58 is regulated by means of the 
flow transmitter 54, the flow control valve 55 and the thermo-electric 
couple 57 provided at the outlet of the mixer 58. The liquid condensed in 
the mixer 58 is recycled into the vaporizer 23 through the conduit 59. The 
wet vapor containing the mist of the liquid ascends to the predetermined 
level within the conduit 28 and then condenses by means of the cooling 
apparatus 31 thereby making it possible to transfer the large amount of 
the liquid accompanied by the ascending dry vapor from the low place to 
the high place. 
The conduit 28 is the conduit having the double structure in which the 
vapor passage of the liquid is provided in the inside of said double 
structure and the adiabatic heat insulator is provided outside of said 
double structure and further the means for keeping it warm is provided at 
the outside of the conduit 28. The temperature and the pressure of the 
vapor of the liquid at the predetermined level within the inside passage 
of the double structure of the conduit 28 are detected by means of the 
thermocouple 29 and the pressure transmitter 30 respectively. The conduit 
28 is connected with the cooling apparatus 31 by means of the naked pipe 
which generally descends toward the cooling apparatus 31 from the top of 
the conduit 28. 
The cooling apparatus 31 is constructed, for example, so as to raise the 
cold atmospheric air from the bottom thereof and spread the cooling water 
from the top thereof through the pipe 33, thereby cooling the temperature 
of the gas-liquid mixture flowing within the pipe provided within the said 
cooling apparatus and liquefying said mixture by removing the condensation 
heat and then introducing the liquid into the tank 37. The temperature, 
the pressure and the surface of the liquid are detected by the means of 
the thermocouple 39, the pressure transmitter 34 and the differential 
pressure transmitter 35. 
The liquid temperature within the tank 37 is regulated through the 
thermo-electric couple 39 and the control valve 32 to control the flow 
rate of the cooling water. As the cooling water flows out as the warm 
water from the outlets 36, 38 provided at the bottom of the cooling 
apparatus 31 after having passed through the cooling apparatus 31, the 
said warm water is used for another service or recycle as to heat an 
object 37. The liquid pressure at the inlet of the turbine is determined 
according to the difference of the height between the position 43 of the 
tank 37 and that 44 of the generator 1, the density of the liquid and the 
pressure within the tank 37. The amount of the liquid entering into the 
turbine of the generator 1 is determined so as to be the predetermined 
level by regulating the amount of the liquid entering into the tank 37 and 
the surface of the liquid within the tank 37 and is controlled by the 
linkage of the control valve 41 provided at below the tank 37 and the 
differential transmitter 35 for detecting the liquid surface within the 
tank 35. The flow rate of the liquid is detected through the flow 
transmitter 40, and the number of the operative generator (or the turbine 
1) is determined according to the flow rate of the liquid which is fed to 
the generator 1. 
As occasion demands, the thermal insulating processing can be applied to 
the descending conduit 42 connected from the tank 37 to the generator 1 in 
order to prevent the influence of the temperature variation due to the 
atmosphere. The liquid within the tank 37 does not gasify since the 
pressure within the tank 37 is balanced with the vapor pressure of the 
liquid corresponding to the temperature of the liquid entering into the 
tank 37. 
As the liquid pressure descending within the conduit 42 increases, even if 
the liquid within the conduit 42 is heated, the liquid does not gasify 
within the tank 5 since the inner pressure of the tank 5 is balanced with 
the vapor pressure of the liquid corresponding to the temperature of the 
liquid entering into the tank 5, but the pressure of the tank 5 acts upon 
the outlet of the turbine or generator 1. The present invention is 
explained by way of the following examples but not to be limited to the 
examples. 
EXAMPLE 1 
Fron-500 (Dichlorodifluoro methane-Difluoro ethane mixture) (CCl.sub.2 
F.sub.2 --C.sub.2 H.sub.4 F.sub.2 :73.8/26.2 wt%) is used as the liquid in 
the example 1. 
The thermodynamics properties of Fron-500 are shown as follows: 
______________________________________ 
Molecular weight 
99.31 
Boiling point -33.3 
Freezing point -158.9 
Critical temperature 
105.1 
Critical pressure 
44.4 atm. 
Critical density 
0.498 
Specific heat liquid (25.degree. C.) 0.29 Cal/g. 
vapor (30.degree. C.) 0.13 Cal/g. 
Viscosity liquid (-15.degree. C.) 0.292 Centipoise 
vapor (30.degree. C., latm) 0.222 Centipoise 
______________________________________ 
(1) One of the trial balances is shown as follows: 
Fron-500 was introduced into the vaporizer at the temperature of 20.degree. 
C. and vaporized by the warm water of 90.degree. C. to obtain the vapor of 
50.degree. C. The necessary amount of the heat was 43.81 Kcal/kg. The 
vapor pressure of the saturated vapor at the temperature of 50.degree. C. 
was 14,793 kg/cm.sup.2 abs. Now, when the vapor of Fron-500 ascends to 700 
m in height within the straight conduit having vacuum room between the 
walls of the double structure of the conduit and the heat insulating layer 
around the outside of the said conduit, the vapor density of the liquid at 
50.degree. C. was 70.1 kg/cm.sup.2. The weight of the vapor of the liquid 
within the conduit amounts to 4.907 kg/cm.sup.2 (70.1 kg/cm.sup.3 
.times.700 m). The vapor pressure of the liquid at 700 m in height 
depresses to 9.886 kg/cm.sup.2 abs. While, when the vapor of Fron-500 is 
cooled to 20.degree. C. and liquefied at 700 m in height by means of the 
cooling apparatus, the vapor pressures within the cooling apparatus and 
the liquid storage tank depresses to 6.849 kg/cm.sup.2 abs. which 
corresponds to the pressure lower than that of the ascending vapor (namely 
9.886 kg/cm.sup.2) by that of more than 2 kg/cm.sup.2 at the high place, 
whereby the vapor of the liquid ascends to 700 m in height within the 
conduit. There is discharged the necessary amount of the heat of 43.79 
kcal/kg which corresponds to the amount of the heat necessary to cool the 
vapor of Fron-500 to the liquid of 20.degree. C. at 700 m in height. 
Namely, it results in transfering from the low place to the high place of 
the amount of the heat which is almost same to that given at the low 
place. As is continuously transfered from the low place to the high place 
the heat coming from the unused heat source having far lower temperature 
than that necessary to utilize to the conventional geothermal generator 
according to the process for utilizing energy of the present invention, it 
makes it possible to effectively utilize the heat of said unused heat 
source to farming and cultivation at the high and cold places. 
(2) The second one of the trial balances is shown as follows: 
When the cooling and liquefying temperature of the liquid amounts to 
40.degree. C., since the environment temperature at the high place ascends 
in the summer, the vapor pressure of the liquid amounts to 22.910 
kg/cm.sup.2 at the vaporizing temperature of 70.degree. C. at the low 
place (the ground), while the vapor pressure of the liquid descends to 
14.678 kg/cm.sup.2 at the high place of 700 m. When the vapor of the 
liquid was cooled to 40.degree. C. and liquefied, the vapor pressure of 
the liquid amounts to 11.639 kg/cm.sup.2. Therefore, the differential 
pressure between the vapor pressure (14.678 kg/cm.sup.2) and that (11.639 
kg/cm.sup.2) at the temperature of 40.degree. C. reaches to more than 3 
kg/cm.sup.2 thereby making it possible to ascend the large amount of the 
vapor of the liquid to the high place. As shown above, it makes possible 
to alter and regulate the temperature of the vaporization according to the 
cooling temperature, the cooling capacity and the amount of the liquid to 
be treated, the environment temperature, the wind temperature and the 
water temperature. When Fron-500, which has entered into the liquid 
storage tank at the high place after liquefying, descends within the 
conduit 42, since the density of the liquid is 1.175 kg/l at 20.degree. 
C., 1.103 kg/l at 40.degree. C. respectively, the amount of the work for 
driving the turbine is determined on the basis of the height of the 
descending liquid, the density of the liquid, the inner pressure of the 
liquid storage tank at the high place and the liquid flow rate. The liquid 
of Fron-500 enters into the liquid storage tank at the low place after 
driving the turbine. At that time, the inner pressure of the liquid 
storage tank amounts to 6.849 kg/cm.sup.2 at the liquid temperature of 
20.degree. C., 11.639 kg/cm.sup.2 at 40.degree. C. respectively, while 
the inner pressure of the vaporizer amounts to 14.793 kg/cm.sup.2 at 
50.degree. C., 22.91 kg/cm.sup.2 at 20.degree. C. respectively, so that 
the differential pressure between the inner pressure of the vaporizer and 
that of the liquid storage tank results in 7.944 kg/cm.sup.2 and 11.271 
kg/cm.sup.2 respectively. The distance or the height (7) between the 
position of the vaporizer 23 and that of the liquid storage tank 5 
provided at the outlet of the turbine 1 is necessary to be 67.6 m at 
20.degree. C., and more than 102 m at 40.degree. C. respectively whereby 
the available height for driving the turbine results in less than 632.4 m 
and 598 m respectively. If the pump 10 for ascending the pressure is used 
to increase the pressure difference, it is possible to use the head of 600 
m and the liquid pressure of 70 kg/cm.sup.2 -63 kg/cm.sup.2 at the inlet 
of the turbine to drive the turbine. 
(3) The third one of the trial balances is shown as follows: 
Now Fron-500 (liquid) is vaporized at the rate of 1,000 kg/sec. giving the 
amount of the heat to the liquid at the rate of about 43,810 k cal/sec. by 
means of the heating apparatus 17 provided on the ground. When the liquid 
ascends to the height of 700 m within the straight conduit 28 having the 
inner diameter of 100 cm as the liquid vapor of 50.degree. C., the flow 
rate of the vapor reaches to 18.2 m/sec. and the head loss due to the 
internal resistance of the conduit reaches to 500 mm aq. In order to 
ascend the liquid to the height of 700 m, the pressure difference of more 
than 5 kg/cm.sup.2 is required taking account of the weight of the vapor 
due to the height of 700 m and the said head loss. As mentioned above, 
when the vapor of the liquid is cooled to 20.degree. C. and liquefied at 
the high place of 700 m, taking the amount of the heat by force at the 
rate of about 43,790 kcal/sec., the vapor pressure at the high place 
reaches to 6.849 kg/cm.sup.2, while the inner pressure of the vaporizer 23 
at 50.degree. C. amounts to 14.793 kg/cm.sup.2, so that the pressure 
difference between the high place and the outlet of the vaporizer amounts 
to 7.944 kg/cm.sup.2. The effective pressure difference amounts to 2.944 
kg/cm.sup.2 after deducting the head loss of 5 kg/cm.sup.2 thereby 
sufficiently compensating the head loss within the cooling apparatus 31. 
When the liquid Fron-500 descends to the inlet of the turbine 1 which is 
positioned beneath 600 m from the tank positioned at the high place at the 
rate of 1000 kg/sec., if the liquid temperature of the said tank 37 
provided at the high place is the same as that of the tank 5 provided at 
the outlet of the turbine, the electric power generated by driving the 
turbine 1 due to the balance of the pressure difference between the said 
both tanks is estimated to be about 5,000 kw/hr at the efficiency of 85%. 
EXAMPLE 2 
In case that Fron-22 (Monochlorodifluoromethane) is used as the liquid, 
when Fron-22 is vaporized by heating at 5.degree. C. using the heat of the 
sea water in which the average temperature of the sea water in the Japan 
Black warm stream is +10.degree. C., the saturated vapor pressure of 
Fron-22 is 5.953 kg/cm.sup.2 abs. If said saturated vapor ascends to the 
high place of 500 m from the ground within the conduit 28, the total head 
loss resulted from the ascent of the vapor within the conduit 28 amounts 
to 1.24 kg/cm.sup.2 due to the vapor density of 24.76 kg/m.sup.3 and the 
difference of the height and the head loss within the conduit. 
Assuming that the temperature of the ascending vapor does not change while 
ascending, the vapor pressure at the height of 500 m amounts to 4.713 
kg/cm.sup.2 (5,953 kg/cm.sup.2 -1.24 kg/cm.sup.2). 
If the ascending vapor is cooled to -10.degree. C. in the cooling apparatus 
by means of the cold wind of -20.degree. C. at the wind velocity of 10 
m/sec. the vapor pressure of the cold fluid amounts to 3.613 kg/cm.sup.2. 
As the pressure difference between the vapor pressure within the vaporizer 
and that within the cooling apparatus amounts to 1.1 kg/cm.sup.2 after 
deducting the head loss of 1.24 kg/cm.sup.2 resulted from the inner 
resistance of the fluid within the conduit, it makes possible to cycle the 
fluid into the circulating system of the present invention. 
Now, if the liquid Fron-22 lying at the height of 500 m descends to the 
place below the distance of 480 m in order to introduce it to the turbine 
positioned at 20 m in height from the ground, the liquid pressure results 
in 63.2 kg/cm.sup.2 thereby driving the turbine. If the liquid temperature 
within the tank positioned at the outlet of the turbine is -10.degree. C., 
the inner pressure within the tank positioned at 20 m in height from the 
ground amounts to 3.613 kg/cm.sup.2. 
If the said liquid pressure is calculated on the basis of the surface of 
the sea water, the liquid pressure within the liquid storage tank amounts 
to 6.249 kg/cm.sup.2 adding the liquid pressure of 2.636 kg/cm.sup.2 which 
corresponds to the liquid pressure existing between the positions of the 
tank on the ground and the surface of the sea water. While, as the inner 
pressure within the vaporizer positioned into the sea water is 5.953 
kg/cm.sup.2, it makes possible to feed the liquid into the vaporizer 
thereby completing the circulation. 
The effects of the present invention are explained as follows: 
(1) In the practice of the present invention, by selecting the appropriate 
liquid to be used and utilizing the temperature difference between the 
temperature of the sea water in the Japan Black warm stream of about 
10.degree. C. and that of the cold wind of less than -20.degree. C. with 
the wind velocity of more than 10 m/sec. which blows at the top of the 
Japan Alps, the turbine generator will be driven according to the 
circulating circuit of the present invention. 
(2) As the heating sources, the steam, the warm water, the heat of the 
earth, the solar heat, the heat of the hot springs, the atmospheric 
temperature and/or the wind temperature are used. 
(3) By selecting the liquid to be used, various kinds of the heating source 
and the cooling source are utilized. 
(4) If the heat energy is transfered from the low place to the high place 
to raise the temperature of the river water and the lake water indicated 
at 37, existing at the high place, it contributes to rear and cultivate 
the agricultural products and the fish farming. 
(5) It can be utilized the natural phenomena of the cold temperature and 
the minor temperature difference between the natural phenomena and the 
atmospheric temperature.