AU2007280834A1 - 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
- Publication number
- AU2007280834A1 AU2007280834A1 AU2007280834A AU2007280834A AU2007280834A1 AU 2007280834 A1 AU2007280834 A1 AU 2007280834A1 AU 2007280834 A AU2007280834 A AU 2007280834A AU 2007280834 A AU2007280834 A AU 2007280834A AU 2007280834 A1 AU2007280834 A1 AU 2007280834A1
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- Australia
- Prior art keywords
- heat
- process according
- carbon dioxide
- expansion
- source
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Abandoned
Links
- 238000000034 method Methods 0.000 title claims description 59
- 230000005611 electricity Effects 0.000 title description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 84
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 42
- 239000001569 carbon dioxide Substances 0.000 claims description 42
- 238000003860 storage Methods 0.000 claims description 17
- 239000007788 liquid Substances 0.000 claims description 12
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 12
- 238000009833 condensation Methods 0.000 claims description 11
- 230000005494 condensation Effects 0.000 claims description 11
- 239000007789 gas Substances 0.000 claims description 7
- 230000006835 compression Effects 0.000 claims description 6
- 238000007906 compression Methods 0.000 claims description 6
- 239000003345 natural gas Substances 0.000 claims description 6
- 239000000203 mixture Substances 0.000 claims description 5
- 239000002918 waste heat Substances 0.000 claims description 5
- 238000001816 cooling Methods 0.000 claims description 4
- 238000012432 intermediate storage Methods 0.000 claims description 4
- 238000004519 manufacturing process Methods 0.000 claims description 4
- 238000002485 combustion reaction Methods 0.000 claims description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 3
- 239000003570 air Substances 0.000 claims 3
- 150000003839 salts Chemical class 0.000 claims 3
- 239000012080 ambient air Substances 0.000 claims 2
- 230000014759 maintenance of location Effects 0.000 claims 1
- 230000003068 static effect Effects 0.000 claims 1
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 8
- 239000012530 fluid Substances 0.000 description 7
- 229910021529 ammonia Inorganic materials 0.000 description 4
- 239000000463 material Substances 0.000 description 3
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical class [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 2
- OFBQJSOFQDEBGM-UHFFFAOYSA-N Pentane Chemical compound CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
- 239000003507 refrigerant Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000006978 adaptation Effects 0.000 description 1
- 235000011114 ammonium hydroxide Nutrition 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000004035 construction material Substances 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 229910052710 silicon Inorganic materials 0.000 description 1
- 239000010703 silicon Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- 239000002912 waste gas 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)
Description
uur KeT.: bUJU t-aleni No.: VV U Zuut/l 14 1 t9 A4 Title: Method and apparatus for use of low-temperature heat for electricity generation Description The invention relates to the use of low temperature heat for the electricity generation by using supercritical carbon dioxide as working medium. State-of the-art There are two known methods for the using of low temperature heat from combustion and reaction processes as well as from solar thermal and geothermic processes essentially: 1. In the OCR (Organic-Rankine-Cycle) - process the heat is removed from the process medium via a heat exchanger and used for the production of steam. Refrigerants, mixtures of refrigerants or low boiling organic substances e.g. pentane, are used in this process, vaporized and expanded via a steam turbine, driving a generator while producing power. The expanded steam is used mainly for preheating and then condensed. The heat of condensation is emitted into the surrounding. The efficiency is determined, depending on the working medium used, the temperature of condensation (ambient temperature) and the reachable temperature of vaporization from approx. 300 K to 625 K depending of the used working fluid. As a rule, the heat transfer is realized by a silicon oil circuit. A related version of the OCR-process for low power is known as edc-process. The edc-process is working with temperatures of condensation from approx. 248 K to 350 K and is using specially adapted turbines. The efficiency of the ORC-process achievable at temperature of 100 *C is approx. 6,5 % and at a temperature of 200 *C approx. 13-14 %. 2. In the Kalina-process the heat is removed via a heat exchanger from the process medium by means of a saturated ammonia-water mixture, while ammonia is expelled. The ammonia vapour is expanded via a turbine driving a generator while producing power. Afterwards the cold ammonia is dissolved again. According to the literature the efficiency of the Kalina process is somewhat higher approx. 18 %. The advantage is the simpler construction of the plant as well as the significantly wider range of -1- Uur KeT.: OUJU i-'atent NO.: VVU UUW/1 4 / t 4 AL effective temperatures of the working medium. The disadvantages are the problems with the construction material due to using the aggressive ammonia-water mixture which would lead to a shorter service life of the little proved method. Another disadvantage is the danger of possible emissions of the highly toxic and environmentally dangerous ammonia in case of possible leakages. Further methods, known from the patent literature, have so far not been able to be technically accomplished. The solutions coming closest to this invention are according to the publications DE 196 32 019 C2 and US 4,765,143. In the publication DE 196 32 019 C2 supercritical carbon dioxide is used as working medium to utilise low temperature heat in the temperature range of 40 to 65 *C. At the same time the pressure range is so chosen that it will not fall below the critical pressure. The reverse compressing is taking place exclusively in the fluid range. The cost of compression for the production of higher working pressure is relatively high for this reason. Disadvantageous is also the separation into a working circuit and a flow circuit which are coupled by a heat exchanger. Consequently there are higher losses. In the US 4,765,143 patent the use of a storage with carbon dioxide at the triple point is described; its solid-liquid mixture is produced by a refrigerator by using overcapacities, said storage during the operation as peak-current power station carrying out the liquefaction of the carbon dioxide. In this manner load fluctuations in the electrical network e.g. in the day-night cycle can be equalised. Carbon dioxide is used also in the actual working circuit. No data is available regarding the efficiency achieved. Disadvantage of this method is the relatively high minimum temperature of over 2000C in the case of low temperature heat usage and from the point of energy the relatively low working pressure. Thus according to our experience no high degrees of efficiency can be achieved during the production of electrical energy. Likewise, a process for using of geothermal heat also operates with carbon dioxide as working medium, that is known from the patent US 3,875,749. This process is working -2uUr KeT.: bU3U ti-'enl NO.: VVU ZUU/l 141 P /A only in the fluid and gas range, wherein the carbon dioxide serves as working medium, in the compressed state it absorbs heat in an underground storage and is then expanded in a turbine producing power. Afterwards a renewed compression takes place in the fluid range. The complicated construction of the underground heat exchanger is a disadvantage in this process and the danger of exhausting the geothermal potential in the vicinity of the cavern by cooling. Task of the invention The task of the invention is to develop a process and a plant to use the process with a higher efficiency than known methods and a broader working range of temperatures and consequently range of control, that allow an optimal modus operandi depending on local conditions and climate, e.g. summer and winter operation without constructional changes with a low material effort and with a low environmental hazard. At the same time the emission of carbon dioxide should be reduced. According to the invention the task is solved by using high-pressured supercritical carbon dioxide as heat carrier, which absorbs low temperature heat from a heat source, afterwards is expanded via an expansion turbine which is connected with a generator while producing power, as a result it is cooled, wherein the carbon dioxide acts also as working medium, subsequently by using a cold source it is liquefied and in liquid state is compressed to the working pressure. As essential element the process has at least one external heat source, at least one expansion machine connected with a generator, at least one heat exchanger with liquefier and a pump for compressing the liquid carbon dioxide to supercritical pressures, at least one carbon dioxide storage as well as control devices and valves belonging to it. It is characterized in that carbon dioxide under pressure is used as the heat carrier, while this carbon dioxide will be liquefied at low temperatures, then compressed in the liquid state up to high supercritical pressures, at these pressures intermediately stored and prepared for the process, then expanded via an expansion machine that drives a generator while producing power, the carbon dioxide -3- Our Ref.: 6030 Patent No.: WU ZUU$/14( /4 AZ cools off in this process and the final temperature will be controlled according to the required pressure for the liquefaction. Afterwards the carbon dioxide will be liquefied at appropriate pressure by a cold source to remove the heat of condensation. The following pressure increase of the working pressure by a liquid pump needs relatively little energy. The possible increase of temperature in the intermediate storage causes a further increase of the efficiency. Compared with the use of steam there are many advantages. First an expensive water preparation will be not needed. Then the relatively high losses in the waste heat boiler are avoided due to the supercritical modus operandi, which are resulted due to the big temperature differences between the cooling-down curve of the gas and the warming-up curve of the steam by evaporating the water. The often used two-pressure and three pressure steam processes for a better adaption of the steam curve to the waste gas curve lead to higher costs of material and control. These difficulties will be avoided due to the use of the supercritical region for the heat absorption. and is also of interest because their favourable thermodynamic terms for the heat exchange by using of low energy heat. That is also caused by high values of the heat capacity, low values of the viscosity in conjunction with the heat conductivity comparable to steam. The thermodynamically available range is limited by the triple point of the carbon dioxide at approx. 217 K corresponding to a pressure of 0.55 MPa. There are thermodynamic upper limits for pressures or usable temperatures. However, there are limits for practical use and material reasons. An additional advantage of using carbon dioxide when compared with the OCR-process is given by the fact that additional heat exchanger is required because the heat carrier medium is working in a closed circuit while it is at the same time the working medium in the same circuit. Further advantages of the chosen heat carrier and working medium are given by its relatively low danger potential for people and environment and its easy availability. In addition, the possibility of storing larger amounts of carbon dioxide and its use as working medium relieves the atmosphere and the environment. Additional economy is obtained by credits in the carbon trade. Due to this it is considerably more advantageous when compared with the OCR and Kalina processes. Further advantages are given by a higher efficiency of the process and the possibility to combine problem free the process with other heat and cold potentials thus further increasing its efficiency. That is possible by using cold potentials in the earth near the surface of the earth, as -4- Our Ret.: b030 Patent NO.: VVU ZUUU/14, / 4 AZ well as by using cold potentials, which are created by expansion processes from other gases, in particular of natural gas by lowering the temperature and make the necessary cold energy for the liquefaction of the carbon dioxide available in the desired temperature range below 283 K. The process will be used preferably in combination with a natural gas power station with natural heat and cold potentials already available and thus allows, in addition to the intermediate storing of large amounts of carbon dioxide, a problem-free discontinuous operation also in a strongly fluctuating operation without significant start-up and adaptation times. At the same time the storage is built up with carbon dioxide used for the heat transfer, with the side effect that larger quantities of the carbon dioxide occurring during the combustion are stored in an environmentally friendly manner and can be fed to a sensible application. The storage of carbon dioxide is carried out by initial compression of the scrubbed power plant gases and their drying and cooling, while liquid carbon dioxide formed in the pipelines in the ground layers near to the surface at 281 to 283 K and pressures over 5 MPa is collected and conveyed to underground caverns. When this pressure is exceeded in the cavern, the liquid carbon dioxide has to be further compressed to build up the storage until the desired final pressure is achieved. In an advantageous manner the build up of the carbon dioxide storage is carried out during the winter months, when air coolers can be used also on the ground surface when at an operating pressure of 5 MPa the outside temperature falls below 283 K. Examples of application Further advantages are given by the description of examples of application of the invention as well as the associated drawing and a table. The fundamental principle of the application of the process and the device for using the heat potential of the earth for the condensation of the working medium, the carbon dioxide, is shown in the drawing. 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 111. As expansion machine 2 an expansion turbine is used. The earth heat potential in the depths of 8 to 30 m is available as cold source 4 and is used for the condensation of the working medium which was expanded to 4.5 MPa. A pressure -5uur Ket.: busu patent NO.: VVU ZUU/l (41/ A4 chamber 6 is used as a temporary storage. The pipes for the carbon dioxide circuit are the lines 7 to 11 according to the drawing. The calculation of the examples was carried out with the program EBSILON Professional. In the second part of the table as example IV the operation of the plant with a cold source 4 at outside temperatures of 273 K and the use of air coolers is illustrated instead of the earth potential as heat source described in examples I to Ill. By using the broader range of temperature with the now feasible lower output pressure of the turbine the efficiency is improved by approx. 1.3%. This result is important especially for regions with low temperatures all year round as well as for using of geothermic energy and when using low temperature heat for power stations. In the case of this method and the assumed conditions of the method one can assume only relatively low degrees of efficiency. They are, however, at least 2% higher than in the case of comparable methods. In a system power station in examples I to IV as heat source 1 waste heat is used at determined temperature levels and it is to be used for energy. For this purpose the fluid carbon dioxide is removed from an underground storage, constructed as an intermediate storage 6, with the temperatures specified in the Table and at a pressure of 15 MPa and heated in a system power station also to the also specified temperature. The carbon dioxide is expanded via a control valve 12 in an expansion machine 2 to 4.5 MPa and drives a generator 3. The expansion is carried out in a system of pipes as cold source 4 close to the surface and pressurised to 4.5 MPa with an ambient temperature of 281 K. Due to the relatively long dwell time and the surrounding earth potential a liquefaction takes place at these temperatures. The liquid carbon dioxide is conveyed via an insulated line 9 to a fluid pump 5, also described as a fluid compressor, and compressed here to 15 MPa and stored in an intermediate storage 6. The energy use for compression is less than a third of the energy obtained. The net degree of efficiency of the process is 12.5 %. If an additional or independent lower temperature potential is available, then depending on the available cold energy at the specified temperature of 373 K degrees of efficiency of up to 25 % may be achieved. -6- Table Working Unit Tempe- Press Power Elt Elt Netto, Examp medium rature ure KW Gross Net Efficien le flow ____ K MPa Therm. Electr. ____ _ _ _ __ 7 363 15 2,3 _ _ __ _ _ 328 _ _ _ _ _ _ 8 1 _ __ 283 4,5_ _ _ _ _ _ _ _ 4 __ _ _ _ _ _-1809 _ _ _ _ _ 9 1 _ __ 283 4,5 __ _ __ _ _____ 1____ 5 ____ ____ -119 _ _______ 10,11 __ _ _ 293,5 15 1 _ _ __ _ _ _____ ___ __ _ _ 1 1___ 2018 1__ _ _ _ _ _ _ _ _ _ _ _ ___328 209 110,4% 1_ 7 373 15 2,3 _ _ _450__ _ _ _ _ _ _ _ 8 _ _ _ _ 283 4,5 _ _ _ _ _ __ _ _ _ _ _ _ _ _ _ _ 4 __ _ _-1902 __ _ __ _ _ _ _ __ _ _ _ 9 283 4,5____ 1__ _ 5 _ _ -119 _ _ _ _ _ _ _ _ 10,11 ____ 293,5 15____ 1 _______ 12243_ _ _ _ ___ _ _ ___450 331 114,4% ___ 7 623 15 1___ 2,3 1__ _ _ _1230 _ _ _ 8 1493 4,5__ _ _ _ _ _ __ _ _ 1__ _ 4 __ _ _ _ _ _ -4486 _ _ _ _ _ _ _ _ _ _ _ 9 1283 4,5 _ _ _ ___ ___ 10,11 __ __ 293,5 15 ____ __ ___ ___ _______ 1 _____15598 _ _ _ 11230 1112 19,9% 7 373 15 I 2,3 1_ _ _ _ _ 5i4 j__ _air 84 1__ 275,5 3,7 1___ ____ coolin _ _ _ _4 __ _ _ _ _ _ -2049 _ _ __ _ _ _ 9 _ _ _ 271,5 3,7__ _ _ _ ___ _ _ _ _ _ _ 5 ._ _ 121_ _ _ _ 10,11 __ _ _ 284,5 15__ _ _ _ _ _ _ _ _ __ ___ 1__ _ I _ _ _ ___ 2442 _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ 514 1393 16,1 % __ -7-
Claims (17)
1. Process for using of low temperature heat for the production of electric power by using of supercritical carbon dioxide as working medium, characterised in that low temperature heat of a heat source (1) is absorbed as heat carrier, while the carbon dioxide acts as working medium, afterwards it is expanded in an expansion machine (2) which is connected with a generator (3) while producing power, it is cooled in this process and subsequently liquefied by means of a cold source (4), then compressed in liquid form to the working pressure and stored in a high pressure interim storage (6).
2. A process according to claim 1, characterised in that the power-producing expansion is carried out up to the condensation range with a partial liquefaction and the gas liquid-mixture is further liquefied totally by using a cold source (4) and compressed in the liquid form to the working pressure and intermediately stored.
3. A process according to claim 1 and 2, characterised in that as interim storage (6) very deep salt caverns are used.
4. A process according to claim 1 to 3, characterised in that the waste heat of a power station is used as heat source (1).
5. A process according to claim 1 to 3, characterised in that the waste heat of motors is used as heat source (1).
6. A process according to claim 1 to 3, characterised in that the waste heat of machines and plants is used as heat source (1).
7. A process according to claim 1 to 3, characterised in that geothermal energy is used as heat source (1). -8-
8. A process according to claim 1 to 3, characterised in that solar thermal energy is used as heat source (1).
9. A process according to claim 1 to 8, characterised in that the geothermal potential in depth of 5 to 30 meters is used as cold source (4) for the liquefaction of the carbon dioxide at last partially.
10. A process according to claim 1 to 9, characterised in that at least partially the ambient air and other media tempered by the ambient air are used as cold source (4) for the removal of the condensation heat.
11. A process according to claim 1 to 10, characterised in that at least partially deep water of seas and oceans are used as cold source (4) to remove the condensation heat.
12. A process according to claim 1 to 11, characterised in that at least partially the cold energy of the expansion process of compressed air or natural gas is used as cold source (4) for the removal of the condensation heat.
13. A process according to claim 1 to 12, characterised in that the power-producing expansion is a two-stage one, characterised in that a first expansion takes place in the two-stage operation, the gas portion is separated, one part is used for the cooling of the total stream before the expansion and is heated by this, afterwards is subjected to a renewed expansion at lower pressures, afterwards it is used for the cooling and condensation of the gaseous first part stream and is subsequently precompressed and returned to the branched gas stream for further comparison.
14. A process according to claim 1 to 13, characterised in that in this process salt caverns act both as mass storages for compressed supercritical carbon dioxide and as heat exchanger while they additionally reduce the potential of possible emission of carbon dioxide into the environment. -9-
15. A process according to claim 1 to 14, characterised in that the liquefaction is carried out at in the vicinity of the surface of the earth, while the deep storage due to the high pressure of the carbon dioxide of at least at 10 MPa is carried out due to safety considerations at a depth of at least 400 m, while the static pressure of the liquefied carbon dioxide reduces the cost of the compression.
16. A process according to claim 1 to 15, characterised in that the process is operated in conjunction with a peak-load power plant based on natural gas and operates discontinuously, thus constructed that temporarily excess energy is used to store natural gas, combustion air and the working medium carbon dioxide in underground intermediate storages (6) in salt caverns under high pressure and continuously remove the air and the natural gas as required to use the carbon dioxide storage both as a supplier of geothermal heat and as buffer storage for the working medium.
17. Device to be used for the process according to claim 1 to 16, characterised in that it comprises at least one existing heat source, one heat exchanger with a liquefier, a medium for the heat transfer, one expansion machine (2), one generator (5) which is connected with the expansion machine (2), one pump (6) for the compression of the liquid carbon dioxide, one buffer for the storage of the liquid working medium, control devices and valves. - 10 -
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 |
|---|---|
| AU2007280834A1 true AU2007280834A1 (en) | 2008-02-07 |
Family
ID=38521920
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| AU2007280834A Abandoned AU2007280834A1 (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) |
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| DK2627876T3 (en) * | 2010-10-14 | 2015-06-15 | Energreen Heat Recovery As | A method and system for utilizing a power source of relatively low temperature |
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2006
- 2006-07-31 DE DE102006035272A patent/DE102006035272B4/en not_active Expired - Fee Related
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- 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 CA CA002662463A patent/CA2662463A1/en not_active Abandoned
- 2007-07-31 RU RU2009106716/06A patent/RU2009106716A/en unknown
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| WO2008014774A3 (en) | 2009-08-20 |
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| CA2662463A1 (en) | 2008-02-07 |
| WO2008014774A2 (en) | 2008-02-07 |
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