US20150089949A1 - Closed loop supercritical carbon dioxide power cycle - Google Patents
Closed loop supercritical carbon dioxide power cycle Download PDFInfo
- Publication number
- US20150089949A1 US20150089949A1 US14/043,321 US201314043321A US2015089949A1 US 20150089949 A1 US20150089949 A1 US 20150089949A1 US 201314043321 A US201314043321 A US 201314043321A US 2015089949 A1 US2015089949 A1 US 2015089949A1
- Authority
- US
- United States
- Prior art keywords
- stream
- carbon dioxide
- supercritical carbon
- closed loop
- expanded
- 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
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
- C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
- C01B3/384—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts the catalyst being continuously externally heated
-
- 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
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
- F02C—GAS-TURBINE PLANTS; AIR INTAKES FOR JET-PROPULSION PLANTS; CONTROLLING FUEL SUPPLY IN AIR-BREATHING JET-PROPULSION PLANTS
- F02C1/00—Gas-turbine plants characterised by the use of hot gases or unheated pressurised gases, as the working fluid
- F02C1/04—Gas-turbine plants characterised by the use of hot gases or unheated pressurised gases, as the working fluid the working fluid being heated indirectly
- F02C1/10—Closed cycles
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
- C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
- C01B2203/0233—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a steam reforming step
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/08—Methods of heating or cooling
- C01B2203/0872—Methods of cooling
- C01B2203/0883—Methods of cooling by indirect heat exchange
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/08—Methods of heating or cooling
- C01B2203/0872—Methods of cooling
- C01B2203/0888—Methods of cooling by evaporation of a fluid
- C01B2203/0894—Generation of steam
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/14—Details of the flowsheet
- C01B2203/142—At least two reforming, decomposition or partial oxidation steps in series
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/80—Aspect of integrated processes for the production of hydrogen or synthesis gas not covered by groups C01B2203/02 - C01B2203/1695
- C01B2203/84—Energy production
-
- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/54—Improvements relating to the production of bulk chemicals using solvents, e.g. supercritical solvents or ionic liquids
Definitions
- S—CO2 supercritical carbon dioxide
- HTR Helical Tube Reactor
- a closed loop supercritical carbon dioxide power generation process includes Indirectly exchanging heat between a hot gas stream and a warm supercritical carbon dioxide stream, expanding the heated supercritical carbon dioxide stream in a turbine, indirectly exchanging heat from the expanded supercritical carbon dioxide stream in a high temperature recuperator and the a temperature recuperator, thereby a cooled, expanded supercritical carbon dioxide steam, splitting the cooled, expanded supercritical carbon dioxide stream into a first stream and a second stream, compressing the first stream in a main compressor, and introducing the compressed first stream into the low temperature recuperator, and compressing the second stream in a recompressor, combining the compressed second stream with the heated first stream, and introducing the combined stream into the high temperature recuperator, wherein it indirectly exchanges heat with expanded supercritical carbon dioxide stream, thereby producing the warm supercritical carbon dioxide stream.
- FIG. 1 is a schematic representation of one embodiment of the present invention.
- FIG. 2 is a schematic representation of one embodiment of the present invention.
- FIG. 3 is an illustration of the cycle efficiency of the various cycles as a function of source temperature.
- a simple SC CO2 Brayton cycle (comprising one turbine and one compressor) has higher thermodynamic efficiency than a steam (Rankine) cycle for temperatures greater than 450 deg C.
- the more complex 3t/6c (comprising three turbines and six compressors) He Brayton cycle has higher efficiencies than the simple SC CO2 Brayton cycle for temperatures greater than 700 deg C.
- C CO2 is the optimum working fluid for heat extraction.
- the high pressure range typically 70-200 bara
- CO2 is a non-toxic, inexpensive, stable, inert, relatively non-corrosive, inflammable and well characterized fluid.
- FIG. 1 one embodiment of the present invention is presented.
- Hydrocarbon fuel stream 101 and steam stream 102 are combined into pre-reformer mixture stream 133 and introduced into pre-reformer preheating module 125 .
- pre-reformer mixture stream 133 is heated against flue gas stream 124 , thereby producing heated pre-reformer stream 134 and flue gas stream 126 .
- Pre-reformer mixture stream 133 may have a temperature of between 275 and 350 C, preferably 310 C.
- Heated pre-reformer stream 134 may have a temperature of between 475 and 525 C, preferably 490 C.
- Flue gas stream 124 may have a temperature of between 825 and 875 C, preferably 850 F. Flue gas stream 126 thus exits module 125 with a reduced temperature of between 725 and 775 C, preferably 750 C.
- Reformer mixture 110 may have a temperature of between 575 and 625 C, preferably 600 C.
- Reformer mixture 110 is then introduced into reformer preheating module 109 .
- reformer mixture stream 110 is heated against flue gas stream 114 , thereby producing heated reformer stream 136 and flue gas stream 111 .
- Heated reformer stream 136 is then combined with steam stream 137 thereby forming reformer mixture stream 138 .
- Reformer mixture stream 138 is further heated in reformer pre-heating module 107 .
- reformer mixture 138 is heated against flue gas stream 111 , thereby producing heated reformer stream 108 and flue gas stream 124 .
- Flue gas stream 111 may have a temperature of between 875 and 925 C, preferably 900 C.
- Flue gas stream 114 may have a temperature of between 1025 and 1075 C, preferably 1057 C.
- Heated reformer stream 108 may have a temperature of between 625 and 675 C, preferably 652 F.
- Heated reformer stream 108 then enters reformer 113 , wherein it is heated and catalytically produces process gas stream 115 .
- Fuel stream 112 and heated air stream 130 are introduced into reformer 113 , where they combust, thereby providing heat for the above catalytic reaction, and producing flue gas stream 114 .
- Process gas stream 115 enters heat recovery boiler 116 , wherein condensate stream 118 is heated to produce process boiler steam stream 117 , and syngas stream 119 .
- Process boiler steam stream may have a temperature of between 250 and 300 C, preferably 270 C.
- Flue gas stream 126 splits into flue gas stream 128 and flue gas stream 127 .
- Flue gas stream 128 may comprise between 50 and 70%, preferably 60% of flue gas stream 126 .
- At least a portion 121 of process boiler steam stream 117 enters superheater module 122 , wherein it exchanges heat with flue gas stream 127 , thereby producing flue gas stream 135 and super heated steam stream 123 .
- Steam stream 123 is then split into at least stream 102 , 104 , and 137 .
- Excess steam stream 120 may comprise less than 20% of the total process boil steam stream 117 .
- Excess steam stream 120 may comprise between 10 and 15%, preferably 12% of the total process boil steam stream 117 .
- Superheated steam stream 123 may have a temperature of between 300 and 350 C, preferably 335 C.
- Flue gas steam 135 may have a temperature of between 600 and 650 C, preferably 630 C.
- Flue gas stream 135 is recombined with flue gas stream 128 , thus producing flue gas stream 201 .
- Flue gas stream 201 may have a temperature of between 675 and 725 C, preferably 700C.
- Flue gas stream 201 enters power cycle reheat module 202 , wherein it indirectly exchanges heat with warm supercritical carbon dioxide stream 204 , thereby producing heated supercritical carbon dioxide stream 205 , and flue gas stream 203 .
- Cooled combined flue gas stream 203 may further indirectly exchange heat with process streams, such as ambient air stream 114 , thereby producing hot air stream 116 and exhaust gas stream 117 .
- Cooled combined flue gas stream 203 may have a temperature of between 435 and 485 C, preferably 460 C.
- Exhaust gas stream 117 may have a temperature of between 100 and 200 C, preferably between 125 and 175 C, more preferably 150 C.
- Flue gas stream 203 then enters air heater module 129 , wherein it indirectly exchanges heat with inlet air stream 130 , thereby producing heated air stream 131 and stack stream 132 .
- Inlet air stream 130 may be ambient temperature.
- Inlet air stream 130 may have a temperature of between 0 and 40 C. preferably between 10 and 30, more preferably 20 C.
- Stack stream 132 may have a temperature of between 125 and 175 C, preferably 150 C.
- Hot gas stream 201 indirectly exchanges heat with warm supercritical carbon dioxide stream 204 , thereby producing heated supercritical carbon dioxide stream 205 , and cooled combined flue gas stream 203 .
- Heated supercritical carbon dioxide stream 205 then enters turbine 206 , wherein it is expanded, thus producing energy.
- the energy is mechanically introduced into shaft 223 , wherein it powers main compressor 216 and re-compressor 218 , with excess mechanical energy being converted to electricity in generator 222 .
- heated supercritical carbon dioxide stream 205 is expanded, it exits turbine 206 as expanded supercritical carbon dioxide stream 207 .
- Expanded supercritical carbon dioxide stream 207 then enters high temperature recuperator 208 , wherein it indirectly exchanges heat with combined stream 221 (described below).
- the first stream 212 may comprise between 50% and 70%, preferably between 55% and 65%, more preferably 60% of cooled, expanded supercritical carbon dioxide stream 211 .
- First stream 212 may enter reject heat exchanger 214 , wherein it is cooled, thereby producing cooled first stream 215 . Cooled first stream 215 then enters main compressor 216 , wherein it is compressed into compressed first stream 217 .
- Second stream 213 enters re-compressor 218 , wherein it is compressed into compressed second stream 219 .
- Compressed second stream 219 is then combined with heated first stream, to produce combined stream 221 .
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Combustion & Propulsion (AREA)
- Organic Chemistry (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Health & Medical Sciences (AREA)
- General Health & Medical Sciences (AREA)
- Inorganic Chemistry (AREA)
- Engine Equipment That Uses Special Cycles (AREA)
Abstract
Description
- In the interest of maximizing thermal efficiency in a standard Steam Methane Reformer (SMR) plant, steam is typically generated from two sources: flue gas waste heat and process heat. This inevitably leads to excess steam generation, more than required internally for the reforming process. In the absence of a steam customer, this results in the last resort measure of installing a steam turbine for realizing economic value.
- The concept of supercritical carbon dioxide (S—CO2), as a promising heat extraction working fluid for cool down of nuclear reactors, has been in existence for more than a decade. Most of the technological developments in this area have occurred from a nuclear power perspective. The proof of concept has been well established experimentally. Under the DOE GEN-IV nuclear program, Sandia National lab has developed two small S-CO2 loops (˜1 MW): Compression loop (at Sandia) and Brayton loop (at Barber Nichols). In the past few years, the idea of using S-CO2 cycle for non-nuclear applications has gained traction. Because of a lesser footprint, lower operating and capital costs, it has been proposed to be integrated in solar plants, molten carbonate fuel cells and as first bottoming cycle in combined cycle plants followed by steam as second bottoming cycle. Under the DOE Sunshot initiative (for solar applications), a 10 MWe scale up is currently under development along with industry partners. It is to be noted that for a standard SMR (120 MMSCFD), power generation is ˜19 MW.
- In SMR's, for good thermal efficiency purposes, the following ideas have been proposed/implemented. As discussed earlier, installation of a steam turbine to realize economic value out of excess steam. Multiple pre-reformers may be impleented to minimize excess steam. Helical Tube Reactor (HTR) technology has been developed to lower the temperature out of the reformer on the process side.
- To date, no prior art exists which advocates the integration of S—CO2 in an SMR in the configuration as proposed herein for significant reduction or, possibly, an elimination of export steam.
- One embodiment of a closed loop supercritical carbon dioxide power generation process is disclosed. This process includes Indirectly exchanging heat between a hot gas stream and a warm supercritical carbon dioxide stream, expanding the heated supercritical carbon dioxide stream in a turbine, indirectly exchanging heat from the expanded supercritical carbon dioxide stream in a high temperature recuperator and the a temperature recuperator, thereby a cooled, expanded supercritical carbon dioxide steam, splitting the cooled, expanded supercritical carbon dioxide stream into a first stream and a second stream, compressing the first stream in a main compressor, and introducing the compressed first stream into the low temperature recuperator, and compressing the second stream in a recompressor, combining the compressed second stream with the heated first stream, and introducing the combined stream into the high temperature recuperator, wherein it indirectly exchanges heat with expanded supercritical carbon dioxide stream, thereby producing the warm supercritical carbon dioxide stream.
-
FIG. 1 is a schematic representation of one embodiment of the present invention. -
FIG. 2 is a schematic representation of one embodiment of the present invention. -
FIG. 3 is an illustration of the cycle efficiency of the various cycles as a function of source temperature. - Illustrative embodiments of the invention are described below. While the invention is susceptible to various modifications and alternative forms, specific embodiments thereof have been shown by way of example in the drawings and are herein described in detail. It should be understood, however, that the description herein of specific embodiments is not intended to limit the invention to the particular forms disclosed, but on the contrary, the intention is to cover all modifications, equivalents, and alternatives falling within the spirit and scope of the invention as defined by the appended claims.
- It will of course be appreciated that in the development of any such actual embodiment, numerous implementation-specific decisions must be made to achieve the developer's specific goals, such as compliance with system-related and business-related constraints, which will vary from one implementation to another.
- Moreover, it will be appreciated that such a development effort might be complex and time-consuming, but would nevertheless be a routine undertaking for those of ordinary skill in the art having the benefit of this disclosure.
- In the present innovation, it is proposed to use the S—CO2 closed power loop for better exploiting the waste heat in the SMR flue gas section by splitting the flue gas outlet (T˜750 deg C) of the pre-reformer super-heater in the following fashion:
- Since the integration is deliberately done in the 450-700° C. range, all the key SMR process parameters (i.e. pre-reformer S/C, pre-reformer inlet T, reformer S/C, reformer inlet T and WGS inlet T), input natural gas feed and hydrogen production have not been effected. It is anticipated that excess steam may still be generated, but this excess steam will be 12% of the original stream production, or less. The 12% excess steam can either be directly sold or used for electricity generation by installing a small steam turbine (which will be ⅛th size of the steam turbine in a typical standard SMR).
- In a supercritical cycle the working fluid is maintained above the critical point during the compression phase of the cycle.
- As shown in
FIG. 3 , a simple SC CO2 Brayton cycle (comprising one turbine and one compressor) has higher thermodynamic efficiency than a steam (Rankine) cycle for temperatures greater than 450 deg C. The more complex 3t/6c (comprising three turbines and six compressors) He Brayton cycle has higher efficiencies than the simple SC CO2 Brayton cycle for temperatures greater than 700 deg C. Hence, in the temperature range 450-700 deg C., C CO2 is the optimum working fluid for heat extraction. - By adding an extra compressor and, the SC CO2 cycle achieves a thermodynamic efficiency of 50% in the same temperature range. The gain in efficiency, as compared to steam, is primarily because of
-
- a) a significant reduction in compression work due to the liquid like density near the critical point,
- b) there are no pinch limitations as encountered in steam generation, since SC CO2 behaves like a single phase fluid in supercritical region, and
- c) the critical point (31 deg C.) is near the desired heat rejection temperature of 20 deg C.
- An added benefit, as compared to a steam cycle for same power output, is that the overall footprint is significantly reduced. The high pressure range (typically 70-200 bara) helps in reducing the size of the compressors, turbines and heat exchangers by orders of magnitude. Further, CO2 is a non-toxic, inexpensive, stable, inert, relatively non-corrosive, inflammable and well characterized fluid.
- Following are the key advantages realized from the proposed integration with an SMR:
-
- a) the ability to minimize or, possibly, eliminate export steam generation
- b) due to the higher efficiency of SC CO2 cycle, there is approximately a 12% gain in power generation when compared with a steam cycle. This is assuming a small steam turbine (˜⅛th size of the steam turbine in a pure steam cycle, 80% efficiency and condensing) is installed.
- c) the flue gas steam generator is eliminated and there is approximately a 35% reduction in boiler feed water requirement.
- d) as previously mentioned, the overall footprint, as compared to steam cycle for the same power output, is significantly reduced.
- Turning now to
FIG. 1 , one embodiment of the present invention is presented. Hydrocarbonfuel stream 101 andsteam stream 102 are combined into pre-reformer mixture stream 133 and introduced intopre-reformer preheating module 125. Withinmodule 125, pre-reformer mixture stream 133 is heated againstflue gas stream 124, thereby producing heated pre-reformerstream 134 andflue gas stream 126. - Pre-reformer mixture stream 133 may have a temperature of between 275 and 350 C, preferably 310 C. Heated pre-reformer
stream 134 may have a temperature of between 475 and 525 C, preferably 490 C.Flue gas stream 124 may have a temperature of between 825 and 875 C, preferably 850 F.Flue gas stream 126 thusexits module 125 with a reduced temperature of between 725 and 775 C, preferably 750 C. - Heated pre-reformer
stream 134 is then introduced into pre-reformer 103, thereby producingreformer mixture 105.Reformer mixture 105 is then combined withsteam stream 104 thereby formingreformer mixture 110.Reformer mixture 110 may have a temperature of between 575 and 625 C, preferably 600 C. -
Reformer mixture 110 is then introduced intoreformer preheating module 109. - Within
module 109reformer mixture stream 110 is heated againstflue gas stream 114, thereby producing heatedreformer stream 136 andflue gas stream 111. - Heated
reformer stream 136 is then combined withsteam stream 137 thereby formingreformer mixture stream 138.Reformer mixture stream 138 is further heated in reformer pre-heatingmodule 107. Withinmodule 107,reformer mixture 138 is heated againstflue gas stream 111, thereby producing heatedreformer stream 108 andflue gas stream 124. -
Flue gas stream 111 may have a temperature of between 875 and 925 C, preferably 900 C.Flue gas stream 114 may have a temperature of between 1025 and 1075 C, preferably 1057 C. Heatedreformer stream 108 may have a temperature of between 625 and 675 C, preferably 652 F. - Heated
reformer stream 108 then entersreformer 113, wherein it is heated and catalytically producesprocess gas stream 115.Fuel stream 112 and heatedair stream 130 are introduced intoreformer 113, where they combust, thereby providing heat for the above catalytic reaction, and producingflue gas stream 114.Process gas stream 115 entersheat recovery boiler 116, whereincondensate stream 118 is heated to produce processboiler steam stream 117, andsyngas stream 119. Process boiler steam stream may have a temperature of between 250 and 300 C, preferably 270 C. -
Flue gas stream 126 splits intoflue gas stream 128 andflue gas stream 127.Flue gas stream 128 may comprise between 50 and 70%, preferably 60% offlue gas stream 126. At least aportion 121 of processboiler steam stream 117 enterssuperheater module 122, wherein it exchanges heat withflue gas stream 127, thereby producingflue gas stream 135 and superheated steam stream 123.Steam stream 123 is then split into at leaststream Excess steam stream 120 may comprise less than 20% of the total processboil steam stream 117.Excess steam stream 120 may comprise between 10 and 15%, preferably 12% of the total processboil steam stream 117.Superheated steam stream 123 may have a temperature of between 300 and 350 C, preferably 335 C.Flue gas steam 135 may have a temperature of between 600 and 650 C, preferably 630 C. -
Flue gas stream 135 is recombined withflue gas stream 128, thus producingflue gas stream 201.Flue gas stream 201 may have a temperature of between 675 and 725 C, preferably 700C. -
Flue gas stream 201 enters powercycle reheat module 202, wherein it indirectly exchanges heat with warm supercriticalcarbon dioxide stream 204, thereby producing heated supercriticalcarbon dioxide stream 205, andflue gas stream 203. Cooled combinedflue gas stream 203 may further indirectly exchange heat with process streams, such asambient air stream 114, thereby producinghot air stream 116 andexhaust gas stream 117. Cooled combinedflue gas stream 203 may have a temperature of between 435 and 485 C, preferably 460 C.Exhaust gas stream 117 may have a temperature of between 100 and 200 C, preferably between 125 and 175 C, more preferably 150 C. -
Flue gas stream 203 then entersair heater module 129, wherein it indirectly exchanges heat withinlet air stream 130, thereby producingheated air stream 131 andstack stream 132.Inlet air stream 130 may be ambient temperature.Inlet air stream 130 may have a temperature of between 0 and 40 C. preferably between 10 and 30, more preferably 20C. Stack stream 132 may have a temperature of between 125 and 175 C, preferably 150 C. - Turning now to
FIG. 2 , one embodiment of the present invention is presented.Hot gas stream 201 indirectly exchanges heat with warm supercriticalcarbon dioxide stream 204, thereby producing heated supercriticalcarbon dioxide stream 205, and cooled combinedflue gas stream 203. - Heated supercritical
carbon dioxide stream 205 then entersturbine 206, wherein it is expanded, thus producing energy. The energy is mechanically introduced intoshaft 223, wherein it powersmain compressor 216 and re-compressor 218, with excess mechanical energy being converted to electricity ingenerator 222. As heated supercriticalcarbon dioxide stream 205 is expanded, it exitsturbine 206 as expanded supercriticalcarbon dioxide stream 207. Expanded supercriticalcarbon dioxide stream 207 then entershigh temperature recuperator 208, wherein it indirectly exchanges heat with combined stream 221 (described below). - This produces cooled expand supercritical
carbon dioxide stream 109, and warm supercriticalcarbon dioxide stream 204. Cooled expand supercriticalcarbon dioxide stream 109 is then introduced intolow temperature recuperator 210, wherein it indirectly exchanges heat with compressed first stream 217 (described below). This produces heatedfirst stream 220 and cooled, expanded supercriticalcarbon dioxide stream 211. Cooled, expanded supercriticalcarbon dioxide stream 211 is then divided intofirst stream 212 andsecond stream 213. Thefirst stream 212 may comprise between 50% and 70%, preferably between 55% and 65%, more preferably 60% of cooled, expanded supercriticalcarbon dioxide stream 211. -
First stream 212 may enter rejectheat exchanger 214, wherein it is cooled, thereby producing cooledfirst stream 215. Cooledfirst stream 215 then entersmain compressor 216, wherein it is compressed into compressedfirst stream 217. -
Second stream 213 enters re-compressor 218, wherein it is compressed into compressedsecond stream 219. Compressedsecond stream 219 is then combined with heated first stream, to produce combinedstream 221.
Claims (7)
Priority Applications (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US14/043,321 US20150089949A1 (en) | 2013-10-01 | 2013-10-01 | Closed loop supercritical carbon dioxide power cycle |
PCT/US2014/058180 WO2015050839A1 (en) | 2013-10-01 | 2014-09-30 | A closed loop supercritical carbon dioxide power cycle |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US14/043,321 US20150089949A1 (en) | 2013-10-01 | 2013-10-01 | Closed loop supercritical carbon dioxide power cycle |
Publications (1)
Publication Number | Publication Date |
---|---|
US20150089949A1 true US20150089949A1 (en) | 2015-04-02 |
Family
ID=51794953
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US14/043,321 Abandoned US20150089949A1 (en) | 2013-10-01 | 2013-10-01 | Closed loop supercritical carbon dioxide power cycle |
Country Status (2)
Country | Link |
---|---|
US (1) | US20150089949A1 (en) |
WO (1) | WO2015050839A1 (en) |
Cited By (10)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US20140009887A1 (en) * | 2011-03-25 | 2014-01-09 | 3M Innovative Properties Company | Fluorinated oxiranes as heat transfer fluids |
CN107420931A (en) * | 2017-08-25 | 2017-12-01 | 西安热工研究院有限公司 | Coal-fired supercritical carbon dioxide generating flue gas can be with working medium energy sub-prime classified utilization method and system |
CN108798811A (en) * | 2018-07-04 | 2018-11-13 | 西安热工研究院有限公司 | A kind of compression supercritical carbon dioxide energy-storage system and method |
CN109538320A (en) * | 2019-01-11 | 2019-03-29 | 哈尔滨电气股份有限公司 | Simple-part cooling cycle close-coupled supercritical carbon dioxide of small-sized sodium heap recycles energy supplying system |
EP3628722A1 (en) * | 2018-09-28 | 2020-04-01 | Siemens Aktiengesellschaft | Crack gas generator, method for crack gas generation |
CN111219218A (en) * | 2020-03-11 | 2020-06-02 | 西安热工研究院有限公司 | Coal-based supercritical carbon dioxide power generation system with waste heat recovery function and method |
CN111237023A (en) * | 2020-03-20 | 2020-06-05 | 杭州汽轮机股份有限公司 | Rotating mechanical shafting structure based on supercritical carbon dioxide and working method |
CN111928289A (en) * | 2020-07-23 | 2020-11-13 | 西安交通大学 | System and method for power cycle low-NOx blue carbon doped combustion |
CN114508396A (en) * | 2022-01-12 | 2022-05-17 | 中南大学 | Ultrahigh-temperature helium-supercritical carbon dioxide combined Brayton cycle system |
CN114592971A (en) * | 2022-03-30 | 2022-06-07 | 西安热工研究院有限公司 | Biomass micro gas turbine and supercritical carbon dioxide coupling power generation system and method |
Families Citing this family (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN110836131B (en) * | 2019-11-05 | 2021-03-23 | 西安交通大学 | Supercritical carbon dioxide recompression circulating turbine mechanical system |
Citations (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2012145092A (en) * | 2011-01-12 | 2012-08-02 | Shintaro Ishiyama | Centrifugal blower (compressor) for compressing supercritical carbon dioxide (co2), supercritical co2 gas turbine, and supercritical co2 gas turbine electric power generation technique including electric power generator |
Family Cites Families (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US20120216536A1 (en) * | 2011-02-25 | 2012-08-30 | Alliance For Sustainable Energy, Llc | Supercritical carbon dioxide power cycle configuration for use in concentrating solar power systems |
WO2013094196A1 (en) * | 2011-12-20 | 2013-06-27 | 日本ネイチャーセル株式会社 | Compact nuclear power generation system |
-
2013
- 2013-10-01 US US14/043,321 patent/US20150089949A1/en not_active Abandoned
-
2014
- 2014-09-30 WO PCT/US2014/058180 patent/WO2015050839A1/en active Application Filing
Patent Citations (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2012145092A (en) * | 2011-01-12 | 2012-08-02 | Shintaro Ishiyama | Centrifugal blower (compressor) for compressing supercritical carbon dioxide (co2), supercritical co2 gas turbine, and supercritical co2 gas turbine electric power generation technique including electric power generator |
Cited By (11)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US20140009887A1 (en) * | 2011-03-25 | 2014-01-09 | 3M Innovative Properties Company | Fluorinated oxiranes as heat transfer fluids |
CN107420931A (en) * | 2017-08-25 | 2017-12-01 | 西安热工研究院有限公司 | Coal-fired supercritical carbon dioxide generating flue gas can be with working medium energy sub-prime classified utilization method and system |
CN108798811A (en) * | 2018-07-04 | 2018-11-13 | 西安热工研究院有限公司 | A kind of compression supercritical carbon dioxide energy-storage system and method |
EP3628722A1 (en) * | 2018-09-28 | 2020-04-01 | Siemens Aktiengesellschaft | Crack gas generator, method for crack gas generation |
WO2020064238A1 (en) | 2018-09-28 | 2020-04-02 | Siemens Aktiengesellschaft | Crack gas generator, method for crack gas generation |
CN109538320A (en) * | 2019-01-11 | 2019-03-29 | 哈尔滨电气股份有限公司 | Simple-part cooling cycle close-coupled supercritical carbon dioxide of small-sized sodium heap recycles energy supplying system |
CN111219218A (en) * | 2020-03-11 | 2020-06-02 | 西安热工研究院有限公司 | Coal-based supercritical carbon dioxide power generation system with waste heat recovery function and method |
CN111237023A (en) * | 2020-03-20 | 2020-06-05 | 杭州汽轮机股份有限公司 | Rotating mechanical shafting structure based on supercritical carbon dioxide and working method |
CN111928289A (en) * | 2020-07-23 | 2020-11-13 | 西安交通大学 | System and method for power cycle low-NOx blue carbon doped combustion |
CN114508396A (en) * | 2022-01-12 | 2022-05-17 | 中南大学 | Ultrahigh-temperature helium-supercritical carbon dioxide combined Brayton cycle system |
CN114592971A (en) * | 2022-03-30 | 2022-06-07 | 西安热工研究院有限公司 | Biomass micro gas turbine and supercritical carbon dioxide coupling power generation system and method |
Also Published As
Publication number | Publication date |
---|---|
WO2015050839A1 (en) | 2015-04-09 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
US20150089949A1 (en) | Closed loop supercritical carbon dioxide power cycle | |
Meng et al. | Thermodynamic analysis of combined power generation system based on SOFC/GT and transcritical carbon dioxide cycle | |
US7926292B2 (en) | Partial oxidation gas turbine cooling | |
US8375725B2 (en) | Integrated pressurized steam hydrocarbon reformer and combined cycle process | |
US7718159B2 (en) | Process for co-production of electricity and hydrogen-rich gas steam reforming of a hydrocarbon fraction with input of calories by combustion with hydrogen in situ | |
NO318511B1 (en) | Process for generating power by means of an advanced thermochemical recovery cycle | |
WO2009057939A3 (en) | Hydrogen generator with easy start-up and stable operation and high efficiency | |
CN102797650A (en) | Low-CO2-emisison solar energy and methanol complementary thermodynamic cycle system and method | |
Rabbani et al. | Energetic and exergetic assessments of glycerol steam reforming in a combined power plant for hydrogen production | |
US9067785B2 (en) | Integration of a closed loop supercritical carbon dioxide power cycle in a steam methane reformer | |
Wang et al. | 4E Analysis of a novel combined cooling, heating and power system coupled with solar thermochemical process and energy storage | |
KR102029421B1 (en) | Fuel cell hybrid generation system | |
CN103373705A (en) | Method and device for improving grade of medium-and-low-temperature solar thermal power and integrally separating CO2 | |
Campanari et al. | Thermodynamic Analysis of Integrated Molten Carbon Fuel Cell–Gas Turbine Cycles for Sub-MW and Multi-MW Scale Power Generation | |
Yu et al. | Thermodynamic and economic analysis of a revised Graz cycle using pure oxygen and hydrogen fuel | |
JP2018500726A5 (en) | ||
US8733109B2 (en) | Combined fuel and air staged power generation system | |
JP7381631B2 (en) | Supercritical CO2 power cycle using methane dry reforming | |
US4239693A (en) | Process for production of methanol | |
Liu et al. | Off-design performance analysis for an integrated system of solid oxide fuel cell and supercritical carbon dioxide Brayton cycle with CO2 capture | |
Yue et al. | Thermodynamic analysis of solar-assisted hybrid power generation systems integrated with thermochemical fuel conversion | |
WO2021121762A1 (en) | Energy conversion system | |
Chen et al. | Performance Comparison of Internal and External Reforming for Hybrid SOFC-GT Applications by Using 1D Real-Time Fuel Cell Mode | |
Martelli et al. | Design criteria and optimization of heat recovery steam cycles for high-efficiency, coal-fired, Fischer-Tropsch plants | |
Rudra et al. | A performance analysis of integrated solid oxide fuel cell and heat recovery steam generator for IGFC system |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
AS | Assignment |
Owner name: AIR LIQUIDE PROCESS & CONSTRUCTION, INC., TEXAS Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNOR:ENG, BRUCE;REEL/FRAME:031869/0149 Effective date: 20131218 |
|
AS | Assignment |
Owner name: AIR LIQUIDE, SOCIETE ANONYME POUR L'ETUDE ET L'EXP Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNOR:AIR LIQUIDE PROCESS & CONSTRUCTION, INC.;REEL/FRAME:031847/0535 Effective date: 20131003 |
|
AS | Assignment |
Owner name: L'AIR LIQUIDE, SOCIETE ANONYME POUR L'ETUDE ET L'E Free format text: CORRECT SPELLING OF ASSIGNEE NAME AT REEL: 031847, FRAME: 0535;ASSIGNOR:AIR LIQUIDE PROCESS & CONSTRUCTION, INC.;REEL/FRAME:032138/0107 Effective date: 20131003 |
|
STCB | Information on status: application discontinuation |
Free format text: ABANDONED -- FAILURE TO RESPOND TO AN OFFICE ACTION |