CA2662463A1 - Method and apparatus for use of low-temperature heat for electricity generation - Google Patents
Method and apparatus for use of low-temperature heat for electricity generation Download PDFInfo
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- CA2662463A1 CA2662463A1 CA002662463A CA2662463A CA2662463A1 CA 2662463 A1 CA2662463 A1 CA 2662463A1 CA 002662463 A CA002662463 A CA 002662463A CA 2662463 A CA2662463 A CA 2662463A CA 2662463 A1 CA2662463 A1 CA 2662463A1
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- carbon dioxide
- heat
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- pressure
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- 238000000034 method Methods 0.000 title claims abstract description 56
- 230000005611 electricity Effects 0.000 title abstract description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 96
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 48
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 48
- 239000007788 liquid Substances 0.000 claims abstract description 17
- 239000012530 fluid Substances 0.000 claims description 14
- 238000003860 storage Methods 0.000 claims description 14
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 12
- 238000009833 condensation Methods 0.000 claims description 8
- 230000005494 condensation Effects 0.000 claims description 8
- 239000000872 buffer Substances 0.000 claims description 7
- 238000001816 cooling Methods 0.000 claims description 7
- 239000007789 gas Substances 0.000 claims description 6
- 238000004519 manufacturing process Methods 0.000 claims description 6
- 239000003345 natural gas Substances 0.000 claims description 6
- 230000006835 compression Effects 0.000 claims description 5
- 238000007906 compression Methods 0.000 claims description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 5
- 239000000203 mixture Substances 0.000 claims description 4
- 239000002918 waste heat Substances 0.000 claims description 4
- 230000014759 maintenance of location Effects 0.000 claims description 3
- 239000000126 substance Substances 0.000 claims description 3
- 239000003570 air Substances 0.000 claims 3
- 239000012080 ambient air Substances 0.000 claims 2
- 150000003839 salts Chemical class 0.000 claims 2
- 239000013529 heat transfer fluid Substances 0.000 claims 1
- 239000005445 natural material Substances 0.000 claims 1
- 230000003068 static effect Effects 0.000 claims 1
- 239000000383 hazardous chemical Substances 0.000 abstract 1
- 238000009434 installation Methods 0.000 abstract 1
- 238000005057 refrigeration Methods 0.000 abstract 1
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 8
- 229910021529 ammonia Inorganic materials 0.000 description 4
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical class [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- OFBQJSOFQDEBGM-UHFFFAOYSA-N Pentane Chemical compound CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 2
- 235000011114 ammonium hydroxide Nutrition 0.000 description 2
- 238000009834 vaporization Methods 0.000 description 2
- 230000008016 vaporization Effects 0.000 description 2
- YTOPFCCWCSOHFV-UHFFFAOYSA-N 2,6-dimethyl-4-tridecylmorpholine Chemical compound CCCCCCCCCCCCCN1CC(C)OC(C)C1 YTOPFCCWCSOHFV-UHFFFAOYSA-N 0.000 description 1
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 239000004035 construction material Substances 0.000 description 1
- 230000001351 cycling effect Effects 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000007710 freezing Methods 0.000 description 1
- 230000008014 freezing Effects 0.000 description 1
- 108010028309 kalinin Proteins 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000003507 refrigerant Substances 0.000 description 1
- 229910052710 silicon Inorganic materials 0.000 description 1
- 239000010703 silicon Substances 0.000 description 1
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
- F01K25/00—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for
- F01K25/08—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for using special vapours
- F01K25/10—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for using special vapours the vapours being cold, e.g. ammonia, carbon dioxide, ether
- F01K25/103—Carbon dioxide
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/14—Combined heat and power generation [CHP]
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Combustion & Propulsion (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Engine Equipment That Uses Special Cycles (AREA)
Abstract
The invention relates to the additional use of low-temperature heat for electricity generation using supercritical carbon dioxide as the working medium. The invention includes a method and an installation for use of the method, by means of which higher efficiency is achieved than with known methods and whose operating range covers a broader temperature band and thus a control range which makes it possible to ensure optimum driving during summer and winter without any design changes, with a simple physical design at the same time and without additional environmental hazards, with comparatively little hardwave complexity. At the same time, a reduction in the carbon dioxide emission is achieved. In order to implement the method, low-temperature heat is received from an existing heat source (1) by means of carbon dioxide, which is at a high supercritical pressure, as the heat carrier, and is then expanded, carrying out work, via an expansion machine (2) which is coupled to a generator (3) with the heat carrier being cooled down, then being liquefied using a refrigeration source (4) and being compressed again to the working pressure, in liquid form.
Description
METHOD AND APPARATUS FOR USE OF LOW-TEMPERATURE HEAT FOR ELECTRICITY GENERATION
FIELD OF THE INVENTION
The invention relates to the use of low temperature heat for the production of electrical energy by using of supercritical carbon dioxide as working fluid.
BACKGROUND OF THE INVENTION
There known two methods for the using of low temperature heat from burning and reaction processes as well as from solar thermal and geothermic processes essentially:
1. In the OCR (Organic-Rankine-Cycle) - process the heat is taking away from the process medium by a heat exchanger and using for the production of steam.
Refrigerants, freezing or low boiling substances as e.g. pentane are used in this process, vaporized and labor-producing expanded due a expansion turbine connecting with a generator. The expanded vapor is used for preheating and then condensed. The heat of condensation will be delivered into the surrounding. The efficiency is estimated by the difference between the temperature of condensation (temperature of the surrounding) and the reachable temperature of vaporization from 300 K to 625 K
depending of the used working fluid. The heat transfer is realized by a silicon oil cycle normally. A changed version of the OCR-process for low power is known as edc-process. The edc-process is working with temperatures of condensation from nearly 248 K to 350 K and is using special constructed turbines. The efficiency of the ORC-process is reaching at a temperatures level of 100 C nearly 6,5 % and at a temperature level of 200 C nearly 13-14 %.
FIELD OF THE INVENTION
The invention relates to the use of low temperature heat for the production of electrical energy by using of supercritical carbon dioxide as working fluid.
BACKGROUND OF THE INVENTION
There known two methods for the using of low temperature heat from burning and reaction processes as well as from solar thermal and geothermic processes essentially:
1. In the OCR (Organic-Rankine-Cycle) - process the heat is taking away from the process medium by a heat exchanger and using for the production of steam.
Refrigerants, freezing or low boiling substances as e.g. pentane are used in this process, vaporized and labor-producing expanded due a expansion turbine connecting with a generator. The expanded vapor is used for preheating and then condensed. The heat of condensation will be delivered into the surrounding. The efficiency is estimated by the difference between the temperature of condensation (temperature of the surrounding) and the reachable temperature of vaporization from 300 K to 625 K
depending of the used working fluid. The heat transfer is realized by a silicon oil cycle normally. A changed version of the OCR-process for low power is known as edc-process. The edc-process is working with temperatures of condensation from nearly 248 K to 350 K and is using special constructed turbines. The efficiency of the ORC-process is reaching at a temperatures level of 100 C nearly 6,5 % and at a temperature level of 200 C nearly 13-14 %.
2. In the Kalina-process the heat is taking away from the process medium by a saturated ammonia-water mixture, in which ammonia is desorbed. The ammonia is labor-producing expanded due an expansion turbine which is connected with a generator. After them the cold ammonia is reabsorbed in the ammonia-water mixture.
The efficiency of the Kalinin process is with 18 % (brutto) a little higher than the ORC-process, according to the literature. Profitable is the simpler construction of the plant as well as the significant wider range of temperatures of the working fluid.
Disadvantageous are the problems with the construction material by using of the aggressive ammonia-water mixture which is leading to a lowering of the cycling time of the little proved plant. Another disadvantage is the danger of possible emissions of the high-toxic and environmentally dangerous ammonia at possible leakages or disturbances.
Task Invention Task invention is developing a process for using low temperature heat for the production of electric power with a higher efficiency and a broader working range as known processes and a simple device for the realization of this process with a low material effort and with a low environmental hazard.
The wider working range and wider adjustment range are loading to optimal processing in relation to local conditions and climate, e.g. summer or winter operation without constructive changes and minimization of the production of carbon dioxide.
According to the invention the task is solved by using high-pressured supercritical carbon dioxide as heat transfer medium, which takes off low temperature heat from a heat source, after them is expanded labor-producing in an expansion turbine, which is connected with a generator, as a result is cooled, then by using of a cold source is liquefied and in liquid state is pressured to the working pressure.
The process implied at least an external heat source (1), an expansion machine (2) connected with a generator (3), a heat exchanger with liquefier (4) and a pump (5) for compressing liquid carbon dioxide to supercritical pressures and a carbon dioxide storage (6) as soon as control devices and valves belonging to it, characterized in that carbon dioxide is used as the heat transfer medium and working fluid. The carbon dioxide will be liquefied at low temperatures, compressed in the liquid state to high supercritical pressures, at these pressures buffered for heat exchange process, taken off the thermal energy at this pressure from a heat source (1) and labor-producing expanded due an expansion machine (2) with an connected generator (3). In the expanding process carbon dioxide will be cooled and the final temperature will be controlled by the wanted pressure for the liquefaction. After them the carbon dioxide will be liquefied at this pressure by heat exchange a cold source due the discharge of the heat of condensation. The compression of the liquid carbon dioxide by a liquid pump (5) needs relatively few energy and a possible increase of temperature is acting in the increase of the efficiency.
In relation to the use of steam there are many advantages. First an expensive water purification plant will be not needed and then the relatively high losses in the waste heat boiler are avoided, which are resulted by the big temperature differences between the cooling-down curve of the exhaust gas and the warming-up curve of the steam through the vaporization of the water. The often used two-pressure and three-pressure cycles for a better adaption are causing a higher effort in material and control.
These difficulties will be avoided by the alternative use of the supercritical region for the heat transfer. The region is very interest too because their easy thermodynamic terms for the heat exchange by using of low temperature heat. That is caused by relatively high values of the heat capacity, low values of the viscosity and a heat conductivity comparable to steam.
The thermodynamic usable range of state is limited to low temperatures by the triple point of carbon dioxide at temperature of nearly 217 K and a pressure of 0,55 MPa.
To higher temperatures and pressures there are no limitations for thermodynamic reasons, but for the practical use in relation to the material of the expansion machines and the heat exchangers.
An additional advantage to the OCR-process is given by the fact that the heat transfer and working fluid are not differently, carbon dioxide is used for both tasks.
The fluid is working in a closed circuit and an additional heat exchanger is not needed.
The efficiency of the Kalinin process is with 18 % (brutto) a little higher than the ORC-process, according to the literature. Profitable is the simpler construction of the plant as well as the significant wider range of temperatures of the working fluid.
Disadvantageous are the problems with the construction material by using of the aggressive ammonia-water mixture which is leading to a lowering of the cycling time of the little proved plant. Another disadvantage is the danger of possible emissions of the high-toxic and environmentally dangerous ammonia at possible leakages or disturbances.
Task Invention Task invention is developing a process for using low temperature heat for the production of electric power with a higher efficiency and a broader working range as known processes and a simple device for the realization of this process with a low material effort and with a low environmental hazard.
The wider working range and wider adjustment range are loading to optimal processing in relation to local conditions and climate, e.g. summer or winter operation without constructive changes and minimization of the production of carbon dioxide.
According to the invention the task is solved by using high-pressured supercritical carbon dioxide as heat transfer medium, which takes off low temperature heat from a heat source, after them is expanded labor-producing in an expansion turbine, which is connected with a generator, as a result is cooled, then by using of a cold source is liquefied and in liquid state is pressured to the working pressure.
The process implied at least an external heat source (1), an expansion machine (2) connected with a generator (3), a heat exchanger with liquefier (4) and a pump (5) for compressing liquid carbon dioxide to supercritical pressures and a carbon dioxide storage (6) as soon as control devices and valves belonging to it, characterized in that carbon dioxide is used as the heat transfer medium and working fluid. The carbon dioxide will be liquefied at low temperatures, compressed in the liquid state to high supercritical pressures, at these pressures buffered for heat exchange process, taken off the thermal energy at this pressure from a heat source (1) and labor-producing expanded due an expansion machine (2) with an connected generator (3). In the expanding process carbon dioxide will be cooled and the final temperature will be controlled by the wanted pressure for the liquefaction. After them the carbon dioxide will be liquefied at this pressure by heat exchange a cold source due the discharge of the heat of condensation. The compression of the liquid carbon dioxide by a liquid pump (5) needs relatively few energy and a possible increase of temperature is acting in the increase of the efficiency.
In relation to the use of steam there are many advantages. First an expensive water purification plant will be not needed and then the relatively high losses in the waste heat boiler are avoided, which are resulted by the big temperature differences between the cooling-down curve of the exhaust gas and the warming-up curve of the steam through the vaporization of the water. The often used two-pressure and three-pressure cycles for a better adaption are causing a higher effort in material and control.
These difficulties will be avoided by the alternative use of the supercritical region for the heat transfer. The region is very interest too because their easy thermodynamic terms for the heat exchange by using of low temperature heat. That is caused by relatively high values of the heat capacity, low values of the viscosity and a heat conductivity comparable to steam.
The thermodynamic usable range of state is limited to low temperatures by the triple point of carbon dioxide at temperature of nearly 217 K and a pressure of 0,55 MPa.
To higher temperatures and pressures there are no limitations for thermodynamic reasons, but for the practical use in relation to the material of the expansion machines and the heat exchangers.
An additional advantage to the OCR-process is given by the fact that the heat transfer and working fluid are not differently, carbon dioxide is used for both tasks.
The fluid is working in a closed circuit and an additional heat exchanger is not needed.
Other advantages of this medium are given by its relatively low danger potential for people and environment and its high availability.
Besides them the storage of bigger amounts of carbon dioxide under control and its use as working fluid relieves the atmosphere and the environment and gives credits by the carbon dioxide trade. Other advantages are given by a higher efficiency of the process and in the possibility to combine the process with other heat and cold potentials increasing real efficiency. That is possible by using cold potentials in the earth near the surface of the earth in low depths, as well as by using cold potentials, which are created by expansion processes from other gases as natural gas and air and are delivering wanted low temperatures.
The process will be used as a combination of a gas power station with natural heat and cold potentials. Big amounts of carbon dioxide will be stored in the buffers of carbon dioxide and used immediately in a discontinuous working and by expansion for the production of electrical power too without significant start-up and shut-down periods.
The start of development of the storage for carbon dioxide is made by winning carbon dioxide from the exhaust air by condensation of water for removing (drying) first and after then the carbon dioxide by compression over 5 MPa, cooling to a temperature of 281 to 283 K and condensing. Cooling is made by the earth temperature in 3 to 30 meters depth.
The liquid carbon dioxide is collected and given through the buffer storage into the underground storage. A part of this can be used for substituting losses of the circuit in the liquid range. For commissioning the plant the carbon dioxide circuit must be filled with carbon dioxide from other sources. In the winter time can be used the surrounding air temperature for cooling when the temperature is below 278 K. Then can be is used a lower pressure for the liquefaction, depending from the real air temperature.
Examples of Application Further advantages are given by the description of examples of application of the invention as well as the connected picture and table.
Besides them the storage of bigger amounts of carbon dioxide under control and its use as working fluid relieves the atmosphere and the environment and gives credits by the carbon dioxide trade. Other advantages are given by a higher efficiency of the process and in the possibility to combine the process with other heat and cold potentials increasing real efficiency. That is possible by using cold potentials in the earth near the surface of the earth in low depths, as well as by using cold potentials, which are created by expansion processes from other gases as natural gas and air and are delivering wanted low temperatures.
The process will be used as a combination of a gas power station with natural heat and cold potentials. Big amounts of carbon dioxide will be stored in the buffers of carbon dioxide and used immediately in a discontinuous working and by expansion for the production of electrical power too without significant start-up and shut-down periods.
The start of development of the storage for carbon dioxide is made by winning carbon dioxide from the exhaust air by condensation of water for removing (drying) first and after then the carbon dioxide by compression over 5 MPa, cooling to a temperature of 281 to 283 K and condensing. Cooling is made by the earth temperature in 3 to 30 meters depth.
The liquid carbon dioxide is collected and given through the buffer storage into the underground storage. A part of this can be used for substituting losses of the circuit in the liquid range. For commissioning the plant the carbon dioxide circuit must be filled with carbon dioxide from other sources. In the winter time can be used the surrounding air temperature for cooling when the temperature is below 278 K. Then can be is used a lower pressure for the liquefaction, depending from the real air temperature.
Examples of Application Further advantages are given by the description of examples of application of the invention as well as the connected picture and table.
The fundamental principle of the application of the process and the device for using of the waste energy of an energy generation plant by using the earth as cooling source for condensation of the working fluid carbon dioxide is shown in the picture.
Three different heat potentials at 363 K, 373 K und 623 K are used exemplary as heat sources at the working pressure at 15 MPa in the examples I to III. As expansion machine (2) is used an expansion turbine. The earth heat potential in the depths of 8 to 30 meters is used as cold source (4) for the condensation of the working fluid carbon dioxide which was expanded to 4.5 MPa. A pressure chamber (6) will used as a temporary storage.
The pipes for the carbon dioxide circuit are the lines 7 to 11 according to the picture.
The calculation of the examples was made with the program EBSILON
Professional. In example IV of the second part of the table is calculated the situation of example li (heat source at 373 K) with a lower air temperature of 271 K, which is characteristic for the winter, as cold source (4) and their using by air coolers. For this it is given a lower turbine output pressure of 3.7 MPa. By using of the broader ranges of temperature and pressure the efficiency of energy generation plant is 1.3 % better than in example II.
This result is important especially of regions with low temperatures as well as for using of geothermic energy and power stations.
The low temperatures are causing a relatively low efficiency but in all cases the efficiency of this process was more than 2 % higher than in comparable processes.
In a co-generation the heat source (1) of the process was the waste energy. In the examples I to IV the waste energy is used at the given temperature levels 363 K, 373 K, and 623 K and should be used energetically. The fluid carbon dioxide is streaming from the underground buffer (6) with a pressure of 15 MPa and temperatures of 293.5 K
(examples I to Iit) and 284,5 K(example IV) through the heat exchanger (1), heated at the given temperatures to 363 K (example I), 373 K (example II and IV), and (example III), streaming through a control valve to an expansion turbine (2), expanding labor-producing from 15 MPa to 4.5 MPa (examples I to III) or rather 3.7 MPa (example IV) and driving on this way a with the turbine connected generator (3). The carbon dioxide was expanded into an underground pipe network as the cold source (4) to a temperature of 281 K in the examples I to Ill. The carbon dioxide is liquefied at this temperature because the long retention period of the carbon dioxide in the pipe network.An air cooler was used as the cold source (4) at 271 K in the example IV and the carbon dioxide was expanded to a pressure of 3.7 MPa. The liquid carbon dioxide is going through a heat isolated pipe (9) to the liquid pump (5), compressed to a pressure of 15 MPa, and stored in the buffer (6). The work for the compression of the liquid carbon dioxide is lower than 30 % of the produced energy. The netto-efficiency of the process is given in the table. The efficiency is increased at higher heat potentials and lower cold sources are usable, e.g. by using of the expansion cold of natural gas and can reach at 373 K efficiencies of nearly 25 %.
Three different heat potentials at 363 K, 373 K und 623 K are used exemplary as heat sources at the working pressure at 15 MPa in the examples I to III. As expansion machine (2) is used an expansion turbine. The earth heat potential in the depths of 8 to 30 meters is used as cold source (4) for the condensation of the working fluid carbon dioxide which was expanded to 4.5 MPa. A pressure chamber (6) will used as a temporary storage.
The pipes for the carbon dioxide circuit are the lines 7 to 11 according to the picture.
The calculation of the examples was made with the program EBSILON
Professional. In example IV of the second part of the table is calculated the situation of example li (heat source at 373 K) with a lower air temperature of 271 K, which is characteristic for the winter, as cold source (4) and their using by air coolers. For this it is given a lower turbine output pressure of 3.7 MPa. By using of the broader ranges of temperature and pressure the efficiency of energy generation plant is 1.3 % better than in example II.
This result is important especially of regions with low temperatures as well as for using of geothermic energy and power stations.
The low temperatures are causing a relatively low efficiency but in all cases the efficiency of this process was more than 2 % higher than in comparable processes.
In a co-generation the heat source (1) of the process was the waste energy. In the examples I to IV the waste energy is used at the given temperature levels 363 K, 373 K, and 623 K and should be used energetically. The fluid carbon dioxide is streaming from the underground buffer (6) with a pressure of 15 MPa and temperatures of 293.5 K
(examples I to Iit) and 284,5 K(example IV) through the heat exchanger (1), heated at the given temperatures to 363 K (example I), 373 K (example II and IV), and (example III), streaming through a control valve to an expansion turbine (2), expanding labor-producing from 15 MPa to 4.5 MPa (examples I to III) or rather 3.7 MPa (example IV) and driving on this way a with the turbine connected generator (3). The carbon dioxide was expanded into an underground pipe network as the cold source (4) to a temperature of 281 K in the examples I to Ill. The carbon dioxide is liquefied at this temperature because the long retention period of the carbon dioxide in the pipe network.An air cooler was used as the cold source (4) at 271 K in the example IV and the carbon dioxide was expanded to a pressure of 3.7 MPa. The liquid carbon dioxide is going through a heat isolated pipe (9) to the liquid pump (5), compressed to a pressure of 15 MPa, and stored in the buffer (6). The work for the compression of the liquid carbon dioxide is lower than 30 % of the produced energy. The netto-efficiency of the process is given in the table. The efficiency is increased at higher heat potentials and lower cold sources are usable, e.g. by using of the expansion cold of natural gas and can reach at 373 K efficiencies of nearly 25 %.
Table Fluid Unit Tempe- Press Power Elt Elt Netto Examp flow rature ure KW Brutto Netto Efficien le K MPa Therm. Electr. cy I
2 , 3 328 8 283 4,5 9 283 4,5 10,11 293,5 15 328 209 10,4%
II
2,3 450 8 283 4,5 9 283 4,5 10,11 293,5 15 450 331 14,4%
III
2,3 1230 8 493 4,5 9 283 4,5 10,11 293,5 15 1230 1112 19,9%
IV
2 , 3 514 air 8 275,5 3,7 cooling 9 271,5 3,7 10,11 284,5 15 514 393 16,1 %
2 , 3 328 8 283 4,5 9 283 4,5 10,11 293,5 15 328 209 10,4%
II
2,3 450 8 283 4,5 9 283 4,5 10,11 293,5 15 450 331 14,4%
III
2,3 1230 8 493 4,5 9 283 4,5 10,11 293,5 15 1230 1112 19,9%
IV
2 , 3 514 air 8 275,5 3,7 cooling 9 271,5 3,7 10,11 284,5 15 514 393 16,1 %
Claims (17)
1. Process for using of low temperature heat for the production of electric power by using of supercritical carbon dioxide as working fluid, in which high compressed supercritical carbon dioxide as heat transfer fluid takes off low temperature heat of a heat source (1) and then is expanded in a labor-producing expansion machine (2), which is connected with a generator (3), is cooled in this process and liquefied by means of a cold source (4), then increased of pressure by a pump for liquids (5) to the working pressure and stored in a high pressure interim storage (6).
2. A process is claimed in claim 1, wherein the labor-producing expansion is made into the range of vapor-liquid-equilibrium with a partial condensation of carbon dioxide and the vapor-liquid-mixture is liquefied totally by means of a cold source (4), then increased of pressure by a pump for liquids (5) to the working pressure and stored in a high pressure interim storage (6).
3. A process is claimed in claim 1 and 2, wherein as interim storages (6) are used salt caverns in big depth.
4. A process is claimed in claim 1 to 3, wherein the waste heat of a power station is used as heat source (1).
5. A process is claimed in claim 1 to 3, wherein the waste heat of motors is used as heat source (1).
6. A process is claimed in claim 1 to 3, wherein the waste heat of machines and plants is used as heat source (1).
7. A process is claimed in claim 1 to 3, wherein geothermal energy is used as heat source (1).
8. A process is claimed in claim 1 to 3, wherein solar energy is used as heat source (1).
9. A process is claimed in claim 1 to 8, wherein the geothermal potential in depth of to 30 meters is used as cold source (4) for the liquefaction of the carbon dioxide at last partially.
10. A process is claimed in claim 1 to 9, wherein the ambient air or substances which are tempered by the ambient air are used as cold source (4) for the liquefaction of the carbon dioxide at last partially.
11. A process is claimed in claim 1 to 10, wherein deep water of seas, rivers or oceans or substances which are tempered by deep water are used as cold source (4) for the liquefaction of the carbon dioxide at last partially.
12. A process is claimed in claim 1 to 11, wherein the cold energy of the expansion of compressed air or natural gas or substances which are tempered by the cold energy of the expansion are used as cold source (4) for the liquefaction of the carbon dioxide at last partially.
13. A process is claimed in claim 1 to 12, wherein the labor-producing two-stage expansion is characterized by an expansion into the two-phase region in the first step by separating of the gas part and using of a liquid part of this stream for cooling of the whole stream for the expansion, in this process will be the stream heated and then in a second step expanded to lower pressures, then used for the cooling and liquefying of the first gas stream and after them compressed and assembled with the liquefied first gas part and in the liquid form compressed to the working pressure.
14. A process is claimed in claim 1 to 13, wherein the salt caverns in the process are used both storages for carbon dioxide in the supercritical high pressure state and geothermic heat sources and heat exchanger, through which the potential of the carbon dioxide emission is lowered additional
15. A process is claimed in claim 1 to 14, wherein the liquefaction takes place in the earth near the surface of the earth and the depth storage in more than 400 meters because the high pressure of the carbon dioxide of 10 MPa at least by safety reasons and the high static pressure the costs of the compression reduces.
16. A process is claimed in claim 1 to 15, wherein the process is operating in joint with a peak load power station of natural gas basis and operating discontinuously, through which the excess energy is used to load natural gas, compressed air and carbon dioxide in underground buffers (6) under high pressure and, when needed, to take off air and natural gas discontinuously and the storage for carbon dioxide to use both as buffer storage and as geothermal heat source for the working fluid.
17. Device realizing the process is claimed in claim 1 to 16, wherein is used at least a given heat source, a heat exchanger with liquefying function, a medium for the heat transfer, an expansion machine (2), a generator (5) which ist connected with the expansion machine (2), a pump (6) for the compression of the liquid carbon dioxide, a buffer for the storage of the liquid working fluid, control devices and valves.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE102006035272A DE102006035272B4 (en) | 2006-07-31 | 2006-07-31 | Method and device for using low-temperature heat for power generation |
| DE102006035272.6 | 2006-07-31 | ||
| PCT/DE2007/001351 WO2008014774A2 (en) | 2006-07-31 | 2007-07-31 | Method and apparatus for use of low-temperature heat for electricity generation |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA2662463A1 true CA2662463A1 (en) | 2008-02-07 |
Family
ID=38521920
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA002662463A Abandoned CA2662463A1 (en) | 2006-07-31 | 2007-07-31 | Method and apparatus for use of low-temperature heat for electricity generation |
Country Status (8)
| Country | Link |
|---|---|
| US (1) | US20090266075A1 (en) |
| EP (1) | EP2078140A2 (en) |
| KR (1) | KR20090035735A (en) |
| AU (1) | AU2007280834A1 (en) |
| CA (1) | CA2662463A1 (en) |
| DE (1) | DE102006035272B4 (en) |
| RU (1) | RU2009106716A (en) |
| WO (1) | WO2008014774A2 (en) |
Families Citing this family (62)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US8940265B2 (en) * | 2009-02-17 | 2015-01-27 | Mcalister Technologies, Llc | Sustainable economic development through integrated production of renewable energy, materials resources, and nutrient regimes |
| US8063511B2 (en) * | 2008-05-27 | 2011-11-22 | Expansion Energy, Llc | System and method for liquid air production, power storage and power release |
| US8814983B2 (en) | 2009-02-17 | 2014-08-26 | Mcalister Technologies, Llc | Delivery systems with in-line selective extraction devices and associated methods of operation |
| US9231267B2 (en) * | 2009-02-17 | 2016-01-05 | Mcalister Technologies, Llc | Systems and methods for sustainable economic development through integrated full spectrum production of renewable energy |
| US9097152B2 (en) | 2009-02-17 | 2015-08-04 | Mcalister Technologies, Llc | Energy system for dwelling support |
| US8808529B2 (en) | 2009-02-17 | 2014-08-19 | Mcalister Technologies, Llc | Systems and methods for sustainable economic development through integrated full spectrum production of renewable material resources using solar thermal |
| US8616323B1 (en) | 2009-03-11 | 2013-12-31 | Echogen Power Systems | Hybrid power systems |
| US9014791B2 (en) | 2009-04-17 | 2015-04-21 | Echogen Power Systems, Llc | System and method for managing thermal issues in gas turbine engines |
| CA2766637A1 (en) | 2009-06-22 | 2010-12-29 | Echogen Power Systems Inc. | System and method for managing thermal issues in one or more industrial processes |
| WO2011017476A1 (en) | 2009-08-04 | 2011-02-10 | Echogen Power Systems Inc. | Heat pump with integral solar collector |
| US8869531B2 (en) | 2009-09-17 | 2014-10-28 | Echogen Power Systems, Llc | Heat engines with cascade cycles |
| US8794002B2 (en) * | 2009-09-17 | 2014-08-05 | Echogen Power Systems | Thermal energy conversion method |
| US8613195B2 (en) | 2009-09-17 | 2013-12-24 | Echogen Power Systems, Llc | Heat engine and heat to electricity systems and methods with working fluid mass management control |
| US8813497B2 (en) | 2009-09-17 | 2014-08-26 | Echogen Power Systems, Llc | Automated mass management control |
| IT1397145B1 (en) * | 2009-11-30 | 2013-01-04 | Nuovo Pignone Spa | DIRECT EVAPORATOR SYSTEM AND METHOD FOR RANKINE ORGANIC CYCLE SYSTEMS. |
| FR2956153B1 (en) * | 2010-02-11 | 2015-07-17 | Inst Francais Du Petrole | DEVICE FOR MONITORING A LOW FREEZING WORK FLUID CIRCULATING IN A CLOSED CIRCUIT OPERATING ACCORDING TO A RANKINE CYCLE AND METHOD USING SUCH A DEVICE |
| CN102906393B (en) | 2010-03-30 | 2015-04-22 | 斯蒂芬·李·坎宁安 | Oscillating piston engine |
| KR101138223B1 (en) * | 2010-04-30 | 2012-04-24 | 한국과학기술원 | System for increasing supercritical Brayton cycle efficiency through shift of critical point using gas mixture |
| US20120255312A1 (en) * | 2010-09-27 | 2012-10-11 | Air Products And Chemicals, Inc. | Method and System to Produce Electric Power |
| EP2627876B1 (en) * | 2010-10-14 | 2015-03-11 | Energreen Heat Recovery AS | Method and system for the utilization of an energy source of relatively low temperature |
| US8857186B2 (en) | 2010-11-29 | 2014-10-14 | Echogen Power Systems, L.L.C. | Heat engine cycles for high ambient conditions |
| US8616001B2 (en) | 2010-11-29 | 2013-12-31 | Echogen Power Systems, Llc | Driven starter pump and start sequence |
| US8783034B2 (en) | 2011-11-07 | 2014-07-22 | Echogen Power Systems, Llc | Hot day cycle |
| US9869272B1 (en) * | 2011-04-20 | 2018-01-16 | Martin A. Stuart | Performance of a transcritical or supercritical CO2 Rankin cycle engine |
| EP2710086A4 (en) * | 2011-04-21 | 2015-03-11 | Emmtech Energy Ab | Working fluid for rankine cycle |
| CN102146814A (en) * | 2011-04-28 | 2011-08-10 | 罗良宜 | Supercritical low-temperature air energy power generator |
| DE102011101788A1 (en) * | 2011-05-17 | 2012-11-22 | Alexander Oberhof | Method for generating electrical energy using solar energy, involves condensing warm vapor to temperature below specific value, and refilling vapor-producing medium in closed chamber, if pressure in chamber is lower than that in condenser |
| DE102011107284A1 (en) * | 2011-07-06 | 2013-01-10 | Rwe Technology Gmbh | Device for emergency cooling of a plant for exothermic processes |
| US9062898B2 (en) | 2011-10-03 | 2015-06-23 | Echogen Power Systems, Llc | Carbon dioxide refrigeration cycle |
| DE102011119977A1 (en) | 2011-12-02 | 2013-06-06 | Alena von Lavante | Device and method for using the waste heat of an internal combustion engine, in particular for using the waste heat of a vehicle engine |
| DE102011122271A1 (en) * | 2011-12-23 | 2013-06-27 | Interimo GmbH | Power plant arrangement for producing energy for building, has low temperature or cooling power plant operating with cyclic process and including evaporator thermally coupled with low caloric waste heat flow of combined heat and power plant |
| US9038391B2 (en) * | 2012-03-24 | 2015-05-26 | General Electric Company | System and method for recovery of waste heat from dual heat sources |
| CN102606240A (en) * | 2012-03-27 | 2012-07-25 | 中国科学院微电子研究所 | By using CO2System and method for generating power |
| JP6276753B2 (en) | 2012-04-18 | 2018-02-07 | スチュアート，マーティン，エー． | Polygonal vibrating piston engine |
| DE102012009459A1 (en) * | 2012-05-11 | 2013-11-14 | Peter Kreuter | Apparatus for converting thermal energy into mechanical energy by Rankine cycle process, comprises circulating line for guiding working fluid, evaporator, working machine and capacitor, where working fluid is carbon dioxide |
| BR112015003646A2 (en) | 2012-08-20 | 2017-07-04 | Echogen Power Systems Llc | supercritical working fluid circuit with one turbo pump and one starter pump in configuration series |
| US9118226B2 (en) | 2012-10-12 | 2015-08-25 | Echogen Power Systems, Llc | Heat engine system with a supercritical working fluid and processes thereof |
| US9341084B2 (en) | 2012-10-12 | 2016-05-17 | Echogen Power Systems, Llc | Supercritical carbon dioxide power cycle for waste heat recovery |
| WO2014063810A2 (en) | 2012-10-24 | 2014-05-01 | Peter Kreuter | Device for converting thermal energy into mechanical energy and motor vehicle comprising a device of this type |
| WO2014081329A1 (en) * | 2012-11-20 | 2014-05-30 | Siemens Aktiengesellschaft | Method for creating electrical energy |
| WO2014117074A1 (en) | 2013-01-28 | 2014-07-31 | Echogen Power Systems, L.L.C. | Process for controlling a power turbine throttle valve during a supercritical carbon dioxide rankine cycle |
| WO2014117068A1 (en) | 2013-01-28 | 2014-07-31 | Echogen Power Systems, L.L.C. | Methods for reducing wear on components of a heat engine system at startup |
| WO2014138035A1 (en) | 2013-03-04 | 2014-09-12 | Echogen Power Systems, L.L.C. | Heat engine systems with high net power supercritical carbon dioxide circuits |
| WO2014171892A1 (en) * | 2013-04-18 | 2014-10-23 | Lien Chiow Tan | Green engine |
| KR101588929B1 (en) * | 2013-09-02 | 2016-01-27 | 서울대학교산학협력단 | Rankine cycle apparatus and Power generating system comprising the same |
| KR102084796B1 (en) * | 2013-09-30 | 2020-03-04 | 한국전력공사 | A system for saving and generating the electric power using supercritical carbon dioxide |
| DE102014101263B3 (en) * | 2014-02-03 | 2015-07-02 | Stephan Leyer | Apparatus and method for storing energy using supercritical carbon dioxide |
| US10570777B2 (en) | 2014-11-03 | 2020-02-25 | Echogen Power Systems, Llc | Active thrust management of a turbopump within a supercritical working fluid circuit in a heat engine system |
| KR101665687B1 (en) * | 2014-12-09 | 2016-10-12 | 연세대학교 산학협력단 | Super Critical Fluid Generating System Having Super Critical Fluid Storage |
| CN104863653B (en) * | 2015-04-21 | 2016-02-24 | 中国石油大学(华东) | A kind of carbon dioxide heat generating device and method |
| CN105971678B (en) * | 2016-05-10 | 2018-09-28 | 石家庄新华能源环保科技股份有限公司 | A kind of system energized using supercritical carbon dioxide |
| CN107939621B (en) * | 2017-12-01 | 2024-04-02 | 西安交通大学 | S-CO based on geothermal energy of heating dry rock of fin sleeve 2 Power generation system and method |
| US11187112B2 (en) | 2018-06-27 | 2021-11-30 | Echogen Power Systems Llc | Systems and methods for generating electricity via a pumped thermal energy storage system |
| EP3804100A1 (en) * | 2018-07-09 | 2021-04-14 | Siemens Energy, Inc. | Supercritical co2 cooled electrical machine |
| US11396828B2 (en) * | 2019-03-13 | 2022-07-26 | Dylan M. Chase | Heat and power cogeneration system |
| US10975697B2 (en) | 2019-09-05 | 2021-04-13 | Karl Peter Mulligan | Systems and methods for a piston engine including a recirculating system using supercritical carbon dioxide |
| CN110748391A (en) * | 2019-10-10 | 2020-02-04 | 东方电气集团东方汽轮机有限公司 | Supercritical carbon dioxide coupled LNG cold energy power generation system and method |
| CN111306017A (en) * | 2020-04-03 | 2020-06-19 | 南京天加热能技术有限公司 | Geothermal energy and solar energy organic Rankine cycle combined heat and power system |
| US11435120B2 (en) | 2020-05-05 | 2022-09-06 | Echogen Power Systems (Delaware), Inc. | Split expansion heat pump cycle |
| CN112211688A (en) * | 2020-09-22 | 2021-01-12 | 崔静思 | Extremely cold region power driving system and driving method thereof |
| MA61232A1 (en) | 2020-12-09 | 2024-05-31 | Supercritical Storage Company Inc | THREE-TANK ELECTRIC THERMAL ENERGY STORAGE SYSTEM |
| CN117622438B (en) * | 2023-12-15 | 2024-04-30 | 中国科学院上海高等研究院 | Autonomous underwater vehicle power supply system based on ocean temperature difference |
Family Cites Families (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3875749A (en) * | 1972-11-17 | 1975-04-08 | Petru Baciu | Geothermal power plant with high efficiency |
| DE3116308A1 (en) * | 1981-04-24 | 1982-11-18 | Wilhelm 2391 Oeversee Behnemann | Power plant utilizing environmental heat |
| US4765143A (en) * | 1987-02-04 | 1988-08-23 | Cbi Research Corporation | Power plant using CO2 as a working fluid |
| DE19632019C1 (en) * | 1996-08-08 | 1997-11-20 | Thomas Sturm | Heat engine operation method |
| DE10228865A1 (en) * | 2002-06-27 | 2004-01-15 | Uehlin, Jürgen, Dipl.-Ing. | Collector with integrated expansion machine, generator for converting thermal solar radiation into electricity has internal heat sink, uses carbon dioxide as heat carrying medium in several circuits |
| JP4321095B2 (en) * | 2003-04-09 | 2009-08-26 | 日立アプライアンス株式会社 | Refrigeration cycle equipment |
| FR2881482B1 (en) * | 2005-02-02 | 2007-04-06 | Inst Francais Du Petrole | METHOD FOR PRODUCING MECHANICAL ENERGY FROM GEOTHERMAL ENERGY |
| DE102006035273B4 (en) * | 2006-07-31 | 2010-03-04 | Siegfried Dr. Westmeier | Process for effective and low-emission operation of power plants, as well as for energy storage and energy conversion |
-
2006
- 2006-07-31 DE DE102006035272A patent/DE102006035272B4/en not_active Expired - Fee Related
-
2007
- 2007-07-31 WO PCT/DE2007/001351 patent/WO2008014774A2/en active Application Filing
- 2007-07-31 CA CA002662463A patent/CA2662463A1/en not_active Abandoned
- 2007-07-31 KR KR1020097004451A patent/KR20090035735A/en not_active Application Discontinuation
- 2007-07-31 AU AU2007280834A patent/AU2007280834A1/en not_active Abandoned
- 2007-07-31 RU RU2009106716/06A patent/RU2009106716A/en unknown
- 2007-07-31 US US12/375,980 patent/US20090266075A1/en not_active Abandoned
- 2007-07-31 EP EP07785679A patent/EP2078140A2/en not_active Withdrawn
Also Published As
| Publication number | Publication date |
|---|---|
| KR20090035735A (en) | 2009-04-10 |
| DE102006035272B4 (en) | 2008-04-10 |
| RU2009106716A (en) | 2010-09-10 |
| WO2008014774A2 (en) | 2008-02-07 |
| DE102006035272A1 (en) | 2008-02-07 |
| EP2078140A2 (en) | 2009-07-15 |
| US20090266075A1 (en) | 2009-10-29 |
| AU2007280834A1 (en) | 2008-02-07 |
| WO2008014774A3 (en) | 2009-08-20 |
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