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INVENTION
Russian Federation Patent RU2121118
DEVICE AND METHOD FOR THE PRODUCTION OF ENERGY
OF GEOTHERMAL FLUID MEDIUM
Name of the inventor: Lucien Y.Broniki (IL); Riollet Gilbert (FR); Asher Elovikov (IL); Nadav Amir (IL); Moshe Grassianni (IL); Yoel Dzhilon (IL); Alex Moritz (IL)
The name of the patentee: The format of performance, Inc. (US)
Address for correspondence:
Starting date of the patent: 1993.10.01
The apparatus and method are designed to produce energy and can be used in geothermal power. The energy produced from geothermal high pressure fluid through the separation of high-pressure steam, and high pressure brine, expanding the high pressure vapor into the high pressure turbine generator to produce power and heat depleted vapor and liquid separation from the heat depleted steam, thereby obtaining a dried heat depleted steam at a pressure and temperature lower than the temperature and pressure of the high pressure steam. The separated liquid thus high pressure brine is combined in the evaporation chamber, which produces steam, combined with the dried heat depleted steam and expands into the low pressure turbine generator to produce additional power, with the portion of the high pressure steam is used for the intermediate heating of the dried heat depleted steam and the steam produced in the vaporization chamber before steam is expanded in a low pressure turbine generator. The invention enables a cost-effective and long-lasting power.
DESCRIPTION OF THE INVENTION
The present invention relates to a geothermal power plant operating on high pressure geothermal fluid environment.
The need for alternatives to fossil fuels for energy production and is well known geothermal resources represent a promising solution. However, in order to be economically attractive, geothermal source should be used so as to maximize the energy output in the range of good engineering practice. This requires a maximum conversion of latent and sensible heat present in geothermal liquid (fluid), and selecting the maximum efficiency of the thermodynamic cycle. This cycle should minimize the formation of scale and corrosion effects of geothermal fluids in the power supplies. Finally, environmental considerations require the return of all the extracted fluids and gases back into the ground to avoid the effects of the environment and prevent the depletion of resources.
Many geothermal sources currently being explored or exploited, producing large quantities of hot brine at moderate pressures, typically about 10.55 kg / cm 2. However, some sources make liquid mixture of steam and brine at significantly higher pressures, for example about 56.25 kg / cm 2. In the latter case, the brine is usually very corrosive and poses problems for its use and disposal. Recently Hawaii geothermal wells were drilled, extracting liquid under high pressure, consisting of about 80% steam and 20% brine. The steam is usually only saturated, and there is thus a question, and how long the well will be able to withstand a pressure of 56.25 kg / cm 2 in continuous operation for many years.
Given this uncertainty, practiced to install pressure reducing valve in the flow from the well, with the result that the system can be used low-pressure steam in the expectation that ultimately decrease high blood pressure. However, this is a conservative solution, and it is costly due to the lifetime of the plant, as a significant amount of potential energy will be lost.
It is known that when a mixture of saturated steam and high pressure supplied from a geothermal brine wells, steam is separated and fed to a steam turbine generator backpressure. The exhaust steam from the back pressure turbine is fed with a plurality of parallel modules each of which comprises a low pressure steam turbine generator. Each module contains a capacitor, which acts as an evaporator for the organic vapor to a turbogenerator.
The disadvantage of this design is that, subject to the maximum work from the high pressure steam supplied from geothermal wells, steam, extending from the back pressure turbine is wet, and this leads to the fact that it is not suitable for the input stages of the low pressure turbine.
The closest prior art known to the applicant, is disclosed in the following references, cited in the corresponding US patent application:
US Patent 4665705,
US Patent 4189923,
US Patent 3762545.
The patent '705 describes a system to minimize the formation of silica scale (silica) in steam boilers for evaporation, used in geothermal power plants. Evaporated steam turbogenerator results in an action, but crumpled (exhaust) in the vapor condenses "distilled water" and is not used for evaporating organic fluid.
Patent '923 shows the use of pressurized gas for supplying brine from the brine and geothermal wells to vapor evaporation which results in the effect of the turbogenerator.
Patent '545 discloses boiling brine from geothermal wells to vapor expansion in steam turbine generator and a condensate compound of the turbine exhaust steam from the concentrated brine evaporation after surgery before the brine is returned to the ground.
Steam pressure turbine driving the generator, an alternative approach may be to the effect that the high-pressure steam from the well may be converted into low-pressure steam turbine and fed in parallel to a large number of modules that can operate at low pressure steam. Each module can use low-pressure steam turbine generator and a capacitor that acts as an evaporator for the liquid organic vapor turbogenerator. When the geothermal fluid only produces high pressure saturated steam, the steam expansion in the turbine takes place in the wet steam on the TS-diagram, generating exhaust steam containing water droplets, and therefore not suitable for use in the input stages of the low-pressure steam turbines of different modules.
Thus, the present invention is to provide a new and improved geothermal power plant capable of operating at high pressure geothermal fluid without the disadvantages inherent in the known constructions described above.
In accordance with the present invention, energy is obtained from the geothermal fluid high pressure by dividing it into a high-pressure steam, and high pressure brine, expanding the high pressure vapor into the high pressure turbine generator to produce power and heat depleted vapor, and separating the liquid from the heat depleted steam, thereby obtaining dried heat depleted steam at a pressure and temperature lower than the temperature and pressure of high pressure steam. The liquid thus separated and combined high pressure brine in the evaporation chamber, which produces steam, blending with the dried heat depleted steam and expands to lower pressure turbogenerator for the production of more energy. Optionally, the high pressure part of the steam is used to reheat the dried heat depleted steam and vapor produced the evaporation chamber, before the couples will be expanded to lower pressure turbogenerator.
In a modification of the high pressure geothermal fluid is supplied to a non-contact heat exchanger or preferably several heat exchangers serving as the evaporator and the heater for a closed steam system in which steam is expanded in a high pressure stage of the turbine generator to produce power and heat depleted steam. moisture separator separates the liquid from the heat depleted steam, producing dried heat depleted steam. The separated liquid is supplied to the evaporation chamber, which is supplied and heated water from the heater and which produces steam is combined with the dried heat depleted steam and sent to the lower pressure turbogenerator.
Embodiments of the present invention are shown in the accompanying drawings, wherein:
FIG. 1 - block diagram of a first embodiment of the present invention, which provides a maximum recovery of geothermal energy from a high pressure source directly using geothermal fluid produced by the source.
FIG. 2 - block diagram of a modification of the embodiment shown in FIG. 1, but using the heater.
FIG. 3 - block diagram of a second embodiment of the present invention similar to the first embodiment,
but indirectly using geothermal fluid.
FIG. 4 - block diagram of a modification of the embodiment shown in FIG. 3.
As shown in the drawings, the numeral 10 designates one embodiment of a geothermal power plant in accordance with the present invention operating at high pressure geothermal liquid. The geothermal fluid is supplied from production well 12, and it is usually produced at a pressure of 56.25 kg / cm 2 and consists of a mixture of about 80% vapor and 20% concentrated brine. Composite liquid produced from well 12 is directed into the first vaporization chamber 14 in which the liquid is divided in two channels, the channel having a high vapor pressure, indicated at 15, and the channel containing the high-pressure brine is designated numeral 16. High pressure saturated steam channel 15 is fed to the high pressure stage 18 of the steam turbine 17 directly connected to the generator 19 so that the expansion in the high pressure steam turbine stage 18 leads to a generator 19 that produces electric energy flowing into the power system (not shown).
Stage turbine 18 produces heat depleted high pressure vapor in the moisture separator 20 where water is separated from the exhaust steam of steam, producing a dried vapor at intermediate pressure. Water is drained from the moisture separator to the sump of the second evaporation chamber 21 connected to the pipeline 16 of the first separator 14 performing fluid evaporation to steam at temperatures and pressures consistent with the temperature and pressure of the dried vapor produced from the moisture separator 2. The steam produced within the chamber 21 is combined with the steam produced in the separator 20, and sent to the stage 22 of the intermediate pressure turbine generator 17. The steam that was placed in step 22, it is expanded by activating generator 19 and producing heat depleted steam at the outlet of stage 22.
The turbogenerator 17 includes a low pressure stage, operating similarly to the intermediate stage 22. Thus, the steam coming from stage 22 is directed to the moisture separator 23 in which the water in the spent steam from the steam is separated, dried producing low pressure steam. Water from the separator water is drained into the sump of the third evaporation chamber 24 connected to the pipeline 25, which in turn is connected to the sump of the second chamber 21, carrying out the evaporation of the brine contained therein to steam at temperatures and pressures that are consistent with the temperature and pressure of the dried vapor obtained a moisture separator 23. The steam produced in chamber 24 is combined with steam produced in the separator 23, and sent to the low pressure stage 17. The steam turbogenerator 26 that was placed in step 26, it is expanded by activating generator 19 and producing heat depleted steam in line 27 from the output stage 26.
Backbone 27 is connected to a condenser 28, cooled air shown as the device which condenses the exhaust gas, producing condensate which is pumped by pump 29 into the borehole receding. In the same borehole sent concentrated brine from settler evaporative separator 24, and a non-condensable gas removed from the condenser 28 which has been compressed before it is fed into the well.
Moisture separators 20 and 21 between the stages of turbine generator supports moisture vapor at the entrance and in each stage at acceptable levels, and results in greater efficiency of the turbine. In addition, the instantaneous vaporization of water between steps allows for maximum cooling of the working fluid / water /, ensuring maximum extraction of sensible heat. Moreover, the use of the condensate from the moisture separator to the evaporator chamber serves to dilute the brine in the separators of sumps, thereby reducing the concentration of, and preventing precipitation when cooled brine. This influences the optimum low temperature evaporation. Without the addition of brine such low temperatures could not be achieved.
Modification of the invention shown in FIG. 2, provides the superheat between stages. As shown in the embodiment of 10A, a part of high-pressure steam obtained in the first vapor separator bypasses step 18A high pressure and is sent into the superheater 35, where the steam gives both latent and sensible heat before it enters the clarifier second separator 21A evaporation.
Following expansion of the steam in 18A-stage high pressure actuation 19A generator heat depleted high pressure steam is sent to 20A moisture separator, where the water is removed from the vapor, producing a dried low pressure steam, which is combined with the steam produced in the 21A cell, which is combined with brine from settler evaporative separator 14A. Instead of direct steam at low pressure stage 26A, it is first superheated in superheater 35, where high pressure steam is cooled in the superheater.
In the embodiment of FIG. 3 10B represents a steam-closed cycle in which the high pressure geothermal fluid is not in direct contact with the working fluid (water). As shown, the high pressure geothermal fluid from production well 12B is supplied noncontact heat exchanger 40 that functions as an evaporator for the heated water supplied thereto. After evaporation of the water in the heat exchanger cooled geothermal liquid is directed to a heat exchanger 41 functioning as a preheater for the fed in condensate. Further cooled geothermal fluid, mostly liquid, the receding back hole 30B. As the geothermal liquid pressure is maintained at a relatively high level, the deposition of minerals from the fluid is reduced to a minimum and does not require creating additional pressure for its injection into the ground.
If the quantity of non-condensable gases, including hydrogen sulfide, in the geothermal fluid is so large that deteriorates the heat transfer in the evaporator 40, these gases may be removed from the evaporator and combined with the cooled liquid geothermal liquid exiting the preheater 41, before the mixture goes into the abductor hole 30B . This operation is facilitated by the increased solubility of non-condensable gases in the liquid cooled geothermal fluid coming out of the heater. Moreover, the high pressure non-condensable gases in the evaporator facilitates removal of entrained with the minimum number of geothermal steam.
The steam produced in the evaporator 40 is supplied to the high-pressure stage turbine generator 18B 17B, where it is expanded by activating generator 19B connected to the power system (not shown). The vapor exiting the stage 18B, 20B flows into the moisture separator which separates the wet steam to dry steam and fluid at an intermediate pressure. The liquid component of this separator is discharged into the evaporator sump chamber 21B, which is fed heated water from the heater 41. The water in the evaporation chamber 21B vaporizes into steam at a temperature and pressure commensurate with the temperature and pressure of the steam produced in the separator 20B. The steam produced in chamber 21B and 20B separator, combined and fed to an intermediate stage 22B turbogenerator 17B, which expands activating generator 19B.
The vapor exiting the stage 22B, 22B is fed into the moisture separator, which separates the wet steam into a liquid component and a dry steam at low pressure. The liquid component of this separator is fed into the evaporator sump chamber 24B, which receives water from the sump and the chamber 21B. The water in the chamber 24B vaporizes into steam at a temperature and pressure similar to the pressure and temperature of steam obtained in the separator 23B. The steam produced in the separator chamber 23B and 24B, blended and fed into the low-pressure stage turbine generator 26B 17B, which expands activating generator 19B.
Steam is removed from stage 28B, is condensed in air cooled condenser 28B and condensate is compressed to a pressure fluid located in the sump chamber 24B is combined with this liquid and is then returned to the heater 41. After heating of the water leaving the heater 41 is directed into the chamber 21B. but most of it is sent to the evaporator 40 to produce high pressure steam for a turbine stage 18B. Distribution of water between the evaporator and the heater chamber 21B is produced so that only a sufficient amount of water is supplied to a separator, which is required for the production of steam, a pair of similar to that produced in the separator 20B.
Preferably, the flow rate of water in the preheater 41 is similar geothermal fluid flow rate, which is mostly liquid in the preheater. This enhances the extraction of heat from the geothermal fluid. Fluctuations in the flow rate of the geothermal liquid at ambient dry bulb that affect the air-cooled condenser or other parameters that influence the heat source or a heat power plant, can be brought into conformity by adjusting the flow rate of water in the water heater 41. The amount of supplied to the heater 41, the necessary excess equilibration geothermal liquid flow rate in the heater may deviate from the vaporization chamber 21B. This provides a convenient way to regulate and stabilize the operation of power plants. The embodiment of FIG 10C. 4 shows a steam power plant, in which the high pressure geothermal fluid is in indirect contact with the working fluid (water) and performed reheating. As shown, the high pressure geothermal fluid from production well 12C is supplied to a non-contact heat exchanger 50 functioning as an evaporator for the heated water supplied thereto. After evaporation of the water in the heat exchanger cooled geothermal liquid is directed to a heat exchanger 50 that functions as an intermediate heater for heating up the intermediate working fluid supplied thereto (water). Further cooled geothermal liquid is then fed to heat exchanger 52 functioning as a preheater of the working fluid (water), and then returns back into the discharge hole 30C. Because the geothermal liquid pressure is maintained at a relatively high level, then there is little precipitation of minerals in the liquid without creating additional pressure required for injection into the ground.
The vapor generated in the evaporator 50 is sent to the high-pressure stage turbine generator 18C 17C, where it is an extension powering a generator 19C coupled to the power system (not shown). Steam is removed from stage 18C, 20C directed to a moisture separator, which separates the wet steam into a liquid component and a dry steam at an intermediate pressure. The liquid component of this separator is discharged into the evaporator sump chamber 21C, which is fed from the heated water 52. Water heater 21C to the chamber evaporates into steam, which is combined with the steam produced in the separator 23C, and supplied to the heater 51. After heating steam fed to the input 22C 17C-stage turbo-generator, which is expanding, powering a generator 19C.
Steam escaping from the step 22C, the cooled air condensed in condenser 28C and condensate liquid is compressed to a pressure in the sump of the separator 21C, combined with this liquid and is then returned to the heater 52. After heating the water discharged from heater 52 is directed into a separator 21C.
Although the embodiments shown in FIGS. 2 and 4 are two-stage turbine generators, the present invention is applicable to turbogenerators with a large number of steps.
Furthermore, although a single generator is shown, which is driven by all the stages of the turbine, separate generators can be provided for each stage. Furthermore, although the capacitor shown in various embodiments as a cooled air, but according to the present invention can be used with water-cooled condensers.
Finally, although not shown, the Rankine turbine on an organic liquid, preferably using pentane or isopentane in accordance with the ambient conditions, can operate in conjunction with low-pressure steam turbines. In this case, a condenser for the steam turbine is cooled by the organic liquid. Although the above single-stage turbines have been described, can be used parallel to the turbine stage or if it is convenient.
In the embodiments of FIGS. 1 and 3 describes the three stages of the turbine, and it is convenient when the geothermal fluid has a relatively high pressure, such as 56/25 kg / cm 2.
In this case, the steam supplied to the intermediate pressure level may be about 7.03 - 10.55 kg / cm 2, and the steam supplied to the low pressure stage of the order of 1.4 - 2.8 kg / cm 2. When the pressure of the geothermal fluid from the production well below the intermediate stage and only low pressure can be used.
heaters may be used for fossil fuel overheating, steam drying or other purposes, thereby improving the efficiency and the ability of the present invention in various conditions. Most of the advantages mentioned in connection with the embodiment of FIG. 1, and applicable to other embodiments of the present invention shown in the other figures.
The resulting improvements and advantages provided by the method and apparatus of the present invention are apparent from the above description of a preferred embodiment of the present invention. However, there may be changes and modifications without departing from the scope of the present invention as defined by the appended claims.
CLAIM
1. An apparatus for generating power from geothermal fluid by high pressure steam generating high pressure and high pressure brine from geothermal fluid and expanding the high pressure vapor into high pressure stage of the turbine to produce power and heat depleted steam, characterized in that it comprises
a) the separator heat depleted steam produced in the high pressure turbine, to the aqueous component and dried pairs
b) a source of another fluid at a temperature higher than the temperature of the aqueous component,
c) evaporating water separator for receiving a part of said liquid separator and the other from the source to form a combined (connected) to obtain a liquid and a vapor and residual liquid
d) another steam turbine,
d) means for supplying a vapor of steam and dried in another steam turbine, where there is an expansion, produces energy and other heat depleted steam.
2. Device according to claim 1, characterized in that it comprises
a) the other separator from heat depleted steam turbine on the other component, and the dried aqueous vapor,
b) a further steam turbine,
c) means for feeding the dried vapor from the separator to another another turbine.
3. The apparatus of claim. 1 and 2, characterized in that the fluid is brine from the source of geothermal fluid.
4. The apparatus according to claim 1, characterized in that it comprises
a) the other separator from heat depleted steam turbine on the other component, and the dried aqueous vapor,
b) other evaporative separator for receiving water from another part of the separator, and the residual liquid from the evaporative separator to form another combined liquid and obtaining other vapors and other residual water,
c) still another steam turbine,
g) means for feeding a vapor from the other evaporative separator and dried steam from another separator in still another turbine, where there is an expansion, produces energy and other heat depleted steam.
5. Apparatus according to claim 4, characterized in that the brine fluid is a source of geothermal fluid.
6. Device according to claim 1, characterized in that there is overheating the superheater for steam vapors and dried before they are fed to another steam turbine.
7. Apparatus according to claim 6, characterized in that the high pressure steam supplied to the superheater where the steam is cooled.
8. Apparatus according to claim 7, characterized in that the cooled steam from the superheater is fed to an expander.
9. A process for the production of geothermal energy from the high pressure fluid through the fluid separation at the high-pressure steam, and high pressure brine and expanding the high pressure vapor into the high pressure turbine generator to produce power and heat depleted steam, characterized in that the following operations:
a) separating the liquid from the heat depleted steam, thereby obtaining a dried heat depleted steam at a pressure and temperature lower than the temperature and pressure of the high pressure steam,
b) combining the liquid thus separated from the high-pressure brine to the mixture,
c) evaporation to obtain a vapor mixture,
g) extension of vapors and dried heat depleted steam turbogenerator at low pressure for more energy.
10. The method of claim 9, wherein the portion of the high pressure steam is used for heating the dried heat depleted steam and vapors prior to expansion in the low pressure turbine generator.
print version
Publication date 07.01.2007gg
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