TW201213655A - System and method for high efficiency power generation using a carbon dioxide circulating working fluid - Google Patents

Abstract

The present invention provides methods and system for power generation using a high efficiency combustor in combination with a CO2 circulating fluid. The methods and systems advantageously can make use of a low pressure ratio power turbine and an economizer heat exchanger in specific embodiments. Additional low grade heat from an external source can be used to provide part of an amount of heat needed for heating the recycle CO2 circulating fluid. Fuel derived CO2 can be captured and delivered at pipeline pressure. Other impurities can be captured.

Description

201213655 VI. Description of the Invention: [Technical Field of the Invention] [0001] Cross-Reference to Related Applications This patent application claims priority to US Provisional Patent Application No. 61/299, 272 filed on Jan. 28, 2010. And U.S. Patent Application Serial No. 12/714,074, filed on Feb. 26, 2010, the disclosure of which is hereby incorporated by reference. The disclosures are hereby incorporated by reference in its entirety. 〇 The present invention is directed to a power generation (e.g., electric power) system and method for transmitting energy generated by efficient combustion of fuel through the use of circulating liquid. In particular, this system and method can use carbon dioxide as a circulating liquid. [Prior Art] [0002] It is estimated that in the next 100 years, while developing and deploying carbon-free energy, petrochemical fuels will continue to provide most of the world's electricity demand. However, by burning fossil fuels and/or suitable biomass (bi〇mass)

The known power generation methods of I) are affected by an increase in energy costs and an increase in carbon dioxide (C〇2) production and other emissions. Global warming has gradually been seen as a potential firefighting consequence of developed and increased carbon emissions from developing countries. Solar energy and wind power may not replace fossil fuel combustion in the short term, and nuclear energy has a risk associated with nuclear expansion and nuclear waste disposal. Conventional devices for generating electricity from fossil fuels, or suitable biomass, are now increasingly subject to high pressure (:02 replenishment requirements for delivery to the storage site (seqUestrati〇n site). However, even for c〇 100125736 Form No. A0101 Page 3 of 134 201213655 The best design for capture, the existing technology can only provide very low thermal efficiency, so this requirement proves to be difficult to implement. Furthermore, (: 〇 2 captured The construction cost is high and this results in significantly higher power costs compared to systems that circulate <:〇2 into the atmosphere. Accordingly, the art is capable of taking into account the reduction in C0 emissions, and/or A more efficient L.L. sealed high efficiency power generation system and method has always had an increased demand. SUMMARY OF THE INVENTION [0003] The present invention provides for the use of a combined circulating liquid (eg, a (: 〇 2 circulating liquid) Power generation method and system for a high efficiency burner (for example, an evapotranspiration burner). In particular, the circulating liquid can be introduced into the combustion together with a fuel for combustion and an oxidant. The burner is such that a high pressure, high temperature liquid stream comprising the circulating liquid and any combustion products is produced. The liquid stream can be directed to a power generating device, such as a turbine. Advantageously, the liquid stream is During expansion into the turbine, it may be maintained at a relatively high pressure such that the pressure ratio across the full wheel (ie, the ratio between the pressure at the turbine inlet and the pressure at the turbine outlet) is less At about 12. The liquid stream can then be further processed to separate components of the liquid stream, which can include passing the liquid stream through a heat exchanger. In particular, the circulating liquid (at least a portion of which can be recycled From the liquid stream, the same heat exchanger can be used to heat the circulating liquid prior to being introduced into the burner. In such an embodiment, it is useful to operate the heat exchanger (e.g., by selecting a low temperature heat source) The heat exchanger has only a small temperature difference between the turbine discharge and the recovered liquid at the hot end of the heat exchanger. In certain aspects, the invention provides A power generation system that can generate high-efficiency power generation with a low construction of 100,125,736, and can also produce a general C No. in the pipeline pressure form A0101 Page 4 / 134 pages 1003441436-0 201213655 for pure C〇2 The crucible 2 can also be recycled into the power generation system. The system and method of the present invention is characterized by the ability to use a wide variety of fuel sources. For example, the high efficiency combustor used in accordance with the present invention can utilize a gaseous state ( For example, natural gas or coal-derived gas), liquid (eg, 'hydrocarbons, bitumen), and solid (eg, coal, lignite, petroleum coke) fuels. Even further fuels (as described elsewhere) can also In other aspects, the method and system of the present invention are particularly useful in that it

We can exceed the optimum efficiency of the existing coal-fired power station that does not provide (: 〇2 capture. Such an existing power station uses 1.7 吋 mercury condensing pressure to use asphalt

The coal provides an optimum efficiency of about 45% (lower calorific value, or "LHV'). The system of the present invention can exceed such efficiency while also delivering c〇 at the desired pressure for sequestration or other disposal. 2

In still another aspect, the present invention provides the ability to reduce the physical size and construction cost of a power generation system as compared to current technologies that utilize similar fuels. Thus, the method and system of the present invention can significantly reduce the cost of construction associated with a power generation system. Still further, the systems and methods of the present invention contemplate nearly 100% recovery of C〇2 used, and/or produced c尤其2, especially from carbon in the fuel. In particular, the c〇2 can be provided as a dried, purified gas at line pressure. Moreover, the present invention provides the ability to separately recover other fuels and burn derivative-derived impurities for other uses, and/or disposal. 100125736 In a particular aspect, the invention is directed to a method of power generation using a combination of, for example, c〇2). In a particular embodiment, Form No. A0101 - Circulating Liquid (The power generation method according to the fifth page of the present invention, page 3, 344, 436, 00, 00, 00, 00, 00 Specifically, the C 〇 2 is introduced at a pressure of at least about 8 MPa (preferably at least about 12 MPa) and a temperature of at least about 200 ° C (preferably at least about 400 ° C). The method still further includes combusting the fuel to provide a combustion product stream comprising c. 2. In particular, the combustion product stream can have a temperature of at least about 80 ° C. Again, the method can include The combustion product stream expands across a turbine for generating electricity, the turbine having an inlet for receiving the combustion product stream, and an outlet for releasing a turbine discharge stream comprising c〇2. Preferably, The ratio of pressure of the combustion product stream at the inlet to the turbine discharge stream at the outlet is less than about 12. In a particular embodiment, desirably, the C〇2 is at a pressure of at least about 10 MPa. At least about 2 A pressure of 0 MPa, a temperature of at least about 400 ° C, or a temperature of at least about 700 ° C is introduced into the combustor. Even further possible processing parameters are also described herein. In some embodiments, the c〇 2 circulating liquid may be introduced into the transpiration cooling burner for mixing with the crucible 2 and one or both of the carbonaceous fuel. In other embodiments, the c〇2 circulating liquid may be introduced into the evapotranspiration. The burner is cooled to be all or part of an evapotranspiration liquid that is introduced through one or more evapotranspiration supply channels formed in the evapotranspiration burner. In a particular embodiment, The c〇2 circulating liquid can be introduced into the combustor as the evaporative liquid. The combustion is characterized in particular by the actual combustion temperature. For example, combustion is carried out at a temperature of at least about 1,500 ° C. In other embodiments The combustion is carried out at a temperature of at least about 1,600 ° C to about 3,300 ° C. The invention is also characterized by the purity of c 〇 2 in the 〇 2 stream. For example, at 100125736 Form No. A010 1 Page 6 of 134 1003441436-0 201213655 Ambient air is useful in some embodiments. However, in certain embodiments, it may be beneficial to purify the oxygen content. For example, the 〇2 It can be provided as first class, wherein the molar concentration of the ruthenium 2 is at least 85%. Even further specific concentrations are also described herein. In a particular embodiment, the combustion product stream can have at least about 1, 〇〇〇 The temperature of ° C. Further, the combustion product stream has a pressure of at least about 90% of the pressure of c〇2 introduced into the burner, or a pressure of at least about 95% of the pressure of C〇2 introduced into the burner. In some embodiments, the pressure ratio of the combustion product flowing at the turbine inlet to the pressure of the turbine discharge at the turbine outlet may be from about 1.5 to about 10, or may be from about 2 to about 8. Even further possible ratios are also provided here. The invention may be characterized by the ratio of the particular material being introduced into the combustion chamber. For example, the ratio of c 〇 2 in the c 〇 2 circulating liquid to carbon in the fuel introduced into the combustor may be from about 10 to about 50, or may be from about 10 to about 30, based on the molar. . Even further possible ratios are offered here. C3 The invention may be characterized in that at least a portion c2 in the turbine discharge stream can be recovered and reintroduced into the combustor. At least a portion of c〇2 can be discharged from the system (e.g., for sequestration or other disposal), for example, through a conduit. In a particular embodiment, c〇2 in the turbine discharge stream can be in a gaseous state. In particular, the turbine discharge stream can have a pressure of less than, or equal to, 7 MPa. In other embodiments, the method of the present invention further includes passing the turbine exhaust stream through at least one heat exchanger (which cools the turbine exhaust stream), and providing 100125736 Form No. A0101 Page 7 of 134 Page 1003441436-0 201213655 The temperature is less than about 20 ° C. One of the temperatures C 〇 2 circulates the liquid stream. This may usefully provide a C〇2 circulating liquid stream under conditions that facilitate the removal of one or more subordinate components (i.e., components other than C〇2). In a particular embodiment, this can include passing the turbine discharge stream through at least two heat exchangers in series. More specifically, the first heat exchanger in the series can receive the turbine discharge stream and lower its temperature, the first heat exchanger being formed of a superalloy that can withstand at least about 900 °C. The method of the present invention may also include performing one or more separation steps on the c〇2 circulating liquid stream to remove one or more subordinate components present in the circulating liquid stream other than c〇2 ( As mentioned above). In particular, the one or more subordinate components may comprise water. The method of the present invention also includes compressing one (: 〇 2 stream. For example, after expanding the combustion product stream and cooling the turbine effluent stream, it is beneficial to compress the stream to recover it back. Specifically The method can include passing the C〇2 circulating liquid stream through one or more compressors (eg, a pump) to compress the C〇2 circulating liquid stream to a pressure of at least about 8 MPa. The method may include circulating the <:〇2 circulating liquid through at least two compressors in series to pressurize the c〇2 circulating liquid stream. In some embodiments, the C〇2 circulating liquid stream may be Pressurizing to a pressure of at least about 15 Mpa. Even further pressure ranges are desirable (as otherwise described). In other embodiments, the pressurized c〇2 circulating liquid stream is particularly Provided to be in a supercritical fluid state. In some embodiments, at least a portion c2 of the pressurized c〇2 circulating liquid stream can be directed to a pressurized line for storage ( Or other disposal, as previously mentioned). The method of the present invention also includes heating the previously cooled (: 〇 2, 100125736 Form No. A0101, page 8 / 134, page 1003441436-0 201213655 ring liquid flow to direct the burner (ie, the (: Recovery of the 循环2 circulating liquid stream. In some embodiments, this may include heating the pressurized c 〇 2 circulating liquid stream to at least about 200 ° C, at least about 400 ° C, or at least about 700 ° C. Temperature. In certain embodiments, the temperature of the pressurized c〇2 circulating liquid stream can be heated to no more than about 50 ° C less than the temperature of the turbine exhaust stream. Even further possible temperature ranges are provided herein. In particular, such heating may include passing the pressurized c〇2 circulating liquid stream through the same heat exchanger for cooling the turbine discharge stream. Such heating may also include from an external The source is input to the heat (i.e., in addition to the heat captured from the heat exchangers). In a particular embodiment, the heating may include the use of heat recovered from a separate unit. Preferably, this additional Heat in the heat exchanger The cold end of the element (or when a series connection of heat exchangers is used, in front of the heat exchanger in the series operating at the highest temperature range) is introduced.

In certain embodiments, the invention features a property that the combustion product stream can allow for selective execution of multiple turbines. For example, in some embodiments, the combustion product stream can be comprised of one or more combustible components (eg, selected from the group consisting of: H2, CO, CH4, H2S, nh3, and It combines a reducing liquid. This can be controlled by the ratio of 〇 2 to the fuel used. In some embodiments, the combustion stream may comprise fully oxidized components, for example, c〇2, H2〇, and s〇2, and the reduced components listed above. The actual composition achieved may depend on the ratio of 〇2 and the fuel used in the feed to the evapotranspiration burner. In particular, a turbine used in such an embodiment may include two or more units each having an inlet and an outlet. In a particular embodiment, the turbo units are operable such that the 100125736 form number A0101 page 9/134 pages 1003441436-0 201213655 operate at substantially the same temperature at the inlet, which may include adding some 〇2 to The liquid flow at the outlet of the first turbine unit (or the preceding turbine unit when three or more units are used). The provision of 〇2 allows for the combustion of one or more of the aforementioned combustible components which raises the temperature of the stream before entering the next turbine in the series. This results in the ability to maximize the power generated from the combustion gases in the presence of the circulating liquid. In other embodiments, the turbine discharge stream can be an oxidizing liquid. For example, the turbine discharge stream can include an excess of 〇2. In some embodiments, the invention features the state of the various streams. For example, after the step of expanding the flow of combustion products across the turbine, the turbine discharge stream can be in a gaseous state. The gas may pass through at least one heat exchanger to cool the gaseous turbine discharge stream to separate the C〇2 from any of the subordinate components. Thereafter, at least a portion of the separator has been separated (: 〇2 can be pressurized and converted to a supercritical liquid form and again passed through the same heat exchanger to recover the c into the burner 〇2 is heated. In a particular embodiment, the temperature of the turbine discharge stream entering the heat exchanger (or when using a first heat exchanger in series) from the expansion step and leaving the same heat exchanger The temperature difference between the temperatures of the heated, pressurized, supercritical fluid C〇2 recovered into the combustor may be less than about 50 ° C. As previously mentioned, the liquid exiting the fuel burner The stream may comprise the (: 〇 2 circulating liquid and one or more further components, for example, combustion products. In some embodiments, usefully recovering at least a portion of C 〇 2 and reintroducing it into the fuel The burner. Therefore, the circulating liquid can be a recovered liquid. Of course, C〇2 from an external source can be used as the circulating liquid. The turbine discharge can be in an economizer heat exchanger 100125736 Form No. A0 101 Page 10 of 134 1003441436-0 201213655 Cooling, and the recovered heat can be used to heat the high pressure recovery c〇2. The cooled turbine discharge leaving the low temperature end of the heat exchanger can be derived from β The components of the fuel or the β-combustion treatment are, for example, η 〇, s〇, NO, N 〇 2, Hg, and HCl. In other embodiments, these components can be removed from the flow by an appropriate method. Other components in this stream may include inert gaseous impurities derived from the fuel or oxidant, for example, \, argon (Ar), and excess ruthenium 2. These may be removed by suitable processing of the separation. In other embodiments, the turbine discharge must be at a pressure that is less than the condensing pressure of the 涡轮 turbine discharge C 〇 2 at the temperature of the available chiller so that there is no c 当 when the turbine discharge is cooled. 2 The liquid phase will form as this will allow liquid water to be separated from the gaseous c〇2 containing a minimum amount of water vapor to allow the water to be condensed. In a further embodiment, the purified (: 〇2 can now be compressed And together with the representative At least a portion of c液体2 in the liquid of carbon oxide (derived from the carbon fed to the fuel of the fuel) to produce a high pressure recovery c〇2 circulating liquid stream that can be introduced into a pressurized line for sequestration Due to the high pressure of the turbine discharge stream, the ability to transfer c〇2 directly into the pressurized line from the combustion process with minimal further processing, or compression, is distinctly different from conventional methods (where C〇 2 is restored to near atmospheric pressure (i.e., about 1 1 MPa) or is diverged to the atmosphere. Furthermore, the co L· for sequestration according to the present invention can be more efficient and economical than conventionally known. Mode Transfer The specific heat of the recovered C turbulent flow entering the heat exchanger (ideally, above the critical pressure u force) is high and decreases as the temperature rises. It is particularly advantageous that at least a portion of the heat at the lowest temperature level is derived from an external source, which may be, for example, a low pressure flow supply that provides heat to the condensation, in further embodiments, the heat source Derived from the adiabatic mold 100125736 Form No. A0101 Page π / Total 134 pages 1003441436-0 201213655 The operation of the air compressor used in the cryogenic air separation of the oxidant to supply the burner (which is not used) To provide heat to the closed loop stream of the heat transfer liquid of the recycle c〇2 stream for extraction of compressed heat and internal cooling). In an embodiment, the power generation method according to the present invention may include the steps of introducing a fuel, helium 2, and (:〇2 circulating liquid into a combustor, the c〇2 being at a pressure of at least about 8 Mpa, and at least about a temperature of 200 t: is introduced; burning the fuel to provide a combustion product stream comprising C 〇 2 having a temperature of at least about 800 ° C; expanding the combustion product stream across a turbine for power generation The turbine has an inlet to receive the combustion product stream, and an outlet to release a turbine discharge stream comprising c〇2, wherein the combustion product stream at the inlet is compared to the turbine discharge at the outlet The flow pressure ratio is less than about 12; the heat is recovered from the turbine discharge stream by passing the turbine discharge stream through a heat exchange unit to provide a cooled turbine discharge stream; the cooled turbine discharge stream is removed from the existing One or more subordinate components of C09 are added to the cooled full wheel discharge stream to provide a purified, L·cooled turbine discharge stream; the purified portion is purified using a first compressor The cooled turbine discharge stream is compressed to a pressure above the critical pressure of (〇2 to provide a supercritical co2 circulating liquid stream; the supercritical c〇2 circulating liquid stream is cooled to a density of at least about 200 kg/n^ One temperature, Form No. A0101 100125736 Page 12 of 134 Page 1003441436-0 201213655 The supercritical, high density c〇2 circulating liquid is passed through a second compressor to pressurize the (:〇2 circulating liquid to Entering the pressure required for the burner; passing the supercritical, high-density, high-pressure C〇2 circulating liquid through the same heat exchange unit so that the recovered heat is used to increase the temperature of the (?2 circulating liquid) Supplying an additional amount of heat to the supercritical, high density, high pressure C〇2 circulating liquid to cause the temperature of the (the 〇2 circulating liquid) and the turbine for recycling to the burner leaving the heat exchange unit The difference in temperature between the exhaust streams is less than about 50 ° C; and 已 the heated, supercritical, high density (: 〇 2 circulating liquid is recovered into the combustor. In a particular embodiment, the systems and Method is especially useful It is a combination of existing power generation systems and methods (eg, conventional coal fired power plants, nuclear energy reactors, and other systems and methods that can utilize conventional boiler systems). Thus, in some embodiments, as described above Between the expanding step and the retracting step, the method of the present invention can include passing the turbine exhaust stream through a second heat exchange unit. Such a second heat exchange unit can be derived from heating using heat from the turbine exhaust stream. One or more streams of a steam power generation system (e.g., a conventional boiler system including a coal fired power plant and a nuclear power reactor). The heated vapor stream can then be passed through one or more turbines for power generation. The flow leaving the turbines can be processed by circulating back through the parts of a conventional power generation system (e.g., a boiler). In a further embodiment, the method of the invention may be characterized by one or more of the following steps: cooling the turbine discharge stream to a temperature below its water dew point; 100125736 Form No. A0101 Page 13 of 134 pages 1003441436-0 201213655 further cooling the turbine discharge stream by an ambient temperature cooling medium; condensing water with the one or more subordinate components to form HJ0, 2 4 , HNOq, HC1, and mercury One or more solutions; u pressurizing the cooled turbine discharge stream to a pressure of less than about 15 MPa; from the supercritical, high density, high pressure c〇2 cycle before passing through the primary heat exchange unit Retrieving a product c〇2 stream in the liquid stream; using a portion of the combustion product stream as a fuel; burning a carbonaceous fuel with 〇2 in the presence of a c 〇2 circulating liquid, the carbonaceous fuel, 〇2, and C The supply ratio of the 循环2 circulating liquid is such that the carbonaceous fuel is only partially oxidized to produce one, or more, including a nonflammable component, c〇2, and H2, CO, CH, H9S, and NHq. Partial oxidation of 4 L 〇 Burning the product stream; providing the carbonaceous fuel, helium 2, and (:〇2 circulating liquid in a ratio such that the temperature of the partially oxidized combustion product stream is sufficiently low such that all incombustible components in the stream are solid particles Forming the partially oxidized combustion product stream through one, more or more filters; using the filter to reduce the remaining amount of non-combustible components by at least about 2 mg/m3 of the portion of the oxidative combustion product stream; Coal, lignite, or petroleum coke is used as a fuel; a particulate form fuel is provided as a slurry having (: 〇2. In a further embodiment, the invention is described in relation to a power generation method comprising the following steps: The carbon fuel, helium 2, and a c〇2 circulating liquid are introduced into an evapotranspiration burner, the C〇2 being introduced at a pressure of at least about 8 Mpa, and at a temperature of at least about 200 ° C; burning the fuel to provide A combustion product stream comprising c〇2, which produces 100125736 Form No. A0101 Page 14 of 134 pages 1003441436-0 201213655 The stream has a temperature of at least about 80 ° C; Crossing a turbine for generating electricity, the turbine having an inlet to receive the combustion product stream, and an outlet to release a turbine exhaust stream comprising c〇2, wherein the combustion product stream at the inlet is compared to The turbine discharge stream at the outlet has a pressure ratio of less than about 12; passing the turbine discharge stream through at least two heat exchangers in series that recover heat from the turbine discharge stream and provide the C〇 recycle liquid stream;

Lt from the (:〇2 circulating liquid stream removes one or more subordinate components present in the circulating liquid stream plus c〇2 ;; causing the (:〇2 circulating liquid stream to pass through at least two compressions in series) And increasing the pressure of the C〇2 circulating liquid to at least about 8 MPa, and converting c〇2 in the circulating liquid from a gaseous state to a supercritical fluid state; and passing the supercritical C09 circulating liquid through the same At least two heat exchangers in series that use the recovered heat to increase the temperature of the C〇2 circulating liquid to at least about 200 ° C (or alternatively, increase to no more than about the temperature of the turbine discharge stream) 50 ° C. This may in particular include the introduction of additional heat from an external heat source (ie, a heat source that is not directly derived from the turbine discharge stream passing through the heat exchanger). In a further embodiment, The present invention is characterized in that it provides an efficient method of generating electricity from combustion of a carbonaceous fuel without atmospheric release of c〇2. Specifically, the method may include the following steps: the carbonaceous fuel, 〇2 Take A recycled c〇2 circulating liquid is introduced into a transpiration cooling burner at a defined stoichiometric ratio, the C 〇 2 being introduced at a pressure of at least about 8 MPa and a temperature of at least about 200 ° C. 100125736 Form No. A0101 15 pages/135 pages 1003441436-0 201213655 burning the fuel to provide a combustion product stream comprising c〇2, the combustion product stream having a temperature of at least about 800 ° C; expanding the combustion product stream across a turbine to Generating power, the turbine having an inlet to receive the combustion product stream, and an outlet to release a turbine exhaust stream comprising C〇2, wherein the combustion product stream at the inlet is compared to the outlet at the outlet The turbine discharge stream has a pressure ratio of less than about 12; the turbine discharge stream is passed through at least two heat exchangers in series, which recover heat from the turbine discharge stream and provide the c〇2 circulating liquid stream; making the CO/shield liquid Flowing through at least two compressors in series, which increases the pressure of the CO 2 circulating liquid to at least about 8 MPa, and converts c〇2 in the circulating liquid from a gaseous state to an ultra-pro a fluid state; passing the c〇2 circulating liquid stream through a separation unit, wherein the stoichiometrically required amount of c〇2 is recovered and directed to the burner, and any excess (:〇2 in the absence of atmospheric release) Retrieving in the case; and passing the recovered c〇2 circulating liquid through at least two heat exchangers in the same series, which uses the recovered heat to increase the temperature of the c〇2 circulating liquid to at least before introduction into the burner Approximately 200 ° C (or alternatively, increased to no more than about 50 ° C less than the temperature of the turbine discharge stream); wherein the combustion efficiency is greater than 50%, the efficiency of the carbon-containing fuel generated relative to combustion The ratio of the net power generated by the total low calorific value of thermal energy is calculated. In another aspect, the invention can be described as providing a power generation system. In particular, a power generation system in accordance with the present invention can include an evapotranspiration burner, a power generation turbine, at least one heat exchanger, and at least one compressor. 100125736 Form No. A0101 Page 16 of 134 1003441436-0 201213655 In a particular embodiment, the evapotranspiration burner may have at least one inlet to receive a carbonaceous fuel, helium 2, and a c〇2 circulating liquid stream . The combustor may further have at least one combustion stage that combusts the fuel in the presence of the C〇2 circulating liquid, and provides at a defined pressure (eg, at least about 8 MPa) and a temperature (eg, at least about 800 ° C). One includes (: a combustion product stream of 〇2. The power generating turbine is in fluid communication with the burner and may have an inlet to receive the combustion product stream and an outlet to release a turbine discharge stream comprising 〇〇2 The turbine may be adapted to control the pressure drop such that the ratio of the pressure of the combustion product stream at the inlet to the pressure of the turbine discharge stream at the outlet is less than about 12. The at least one heat exchanger The turbine can be in fluid communication to receive the turbine exhaust stream. The heat exchanger can transfer heat from the turbine exhaust stream to the c〇2 circulating liquid stream. The at least one compressor can be coupled to the At least one heat exchanger is in fluid communication. The (equal) compressor may be adapted to compress the (:2) circulating liquid stream to a desired pressure. In addition to the foregoing, the power generating system according to the present invention One or more separation devices may be included between the at least one heat exchanger and the at least one compressor. Such separation device(s) may be used to remove the presence of the (:〇2 circulating liquid Further, the power generation system may include one or two separate units including one or more heat generating components. Therefore, the power generation system is also One or more heat transfer components may be included that transfer heat from the 〇2 separation unit to the (up to 2 circulatory liquid) upstream of the burner. Alternatively, the power generation system may include an external heat source. For example, a hot low pressure steam supply may be provided for condensing 100125736 Form No. A0101 Page 17 of 134 pages 1003441436-0 201213655. Therefore, the power generation system may include one or more heat transfer parts that will be hot The c〇2 circulating liquid is transferred from the steam to the upstream of the combustor. In a further embodiment, the power generation system of the present invention may comprise one or more of the following: a first compressor adapted to C〇2 The circulating liquid stream is compressed to a pressure higher than the critical pressure of C〇2; a second compressor adapted to compress the C〇2 circulating liquid stream to a pressure required to be input to the burner; a cooling device adapted to The C〇2 circulating liquid stream is cooled to a temperature having a density greater than about 200 kg/m3; one or more heat transfer components, the one or more heat transfer components transferring heat from an external source to the The c〇2 circulating liquid upstream of the combustor and downstream of the second compressor; a second combustor located upstream of and in fluid communication with the evaporative cooling combustor; one or more filters or separation devices, The one or more filters or separation devices are located between the second burner and the evaporative cooling burner; a mixing device for forming a slurry of particulate fuel material and a fluidized medium; and Grinding device to atomize a solid fuel. In other embodiments, the present invention can provide a power generation system that can include the following: one or more injectors for providing fuel, a C〇2 circulating liquid, and an oxidant; an evapotranspiration burner having At least one combustion stage that combusts the fuel and provides a temperature of at least about 800 ° C. 100125736 Form No. A0101 Page 18 of 134 pages 1003441436-0 201213655 degrees and at least about 4 MPa (preferably, at least about 8 MPa) a discharge liquid flow; a power generation turbine having an inlet and an outlet, and wherein the electrical power is generated as the liquid flow expands, the turbine being designed to maintain the liquid flow at a desired pressure to Having the liquid flow at the inlet to the outlet at a pressure ratio of less than about 12; - a heat exchanger for cooling the liquid stream exiting the turbine outlet, and heating the c〇2 circulating liquid; for leaving The liquid stream of the heat exchanger is separated into (one more than one device of 〇2 and one or more further parts for recovery or disposal. In a further embodiment, The electrical system may also include one or more means for delivering at least a portion (:2) from the liquid stream to a pressurized line. In a particular embodiment, in accordance with the present invention The system may include one or more components that are trimmed as described herein with a conventional power generation system (eg, a coal fired power plant, a nuclear power reactor, or the like). For example, a power generation system may include two heat exchanges. a unit (eg, a primary heat exchange unit, and a slave heat exchange unit). The primary heat exchange unit can be substantially the other manner of unit as described above, and the slave heat exchange unit can be used to discharge the flow from the turbine The heat is transferred to one or more units of steam flow (e.g., from a boiler associated with the conventional power generation system) to superheat the steam flow. Thus, a power generation system in accordance with the present invention may include a subordinate a heat exchange unit located between the turbine and the main heat exchange unit and in fluid communication with the turbine and the main spring exchange unit. Similarly, the power generation system can be packaged a boiler in fluid communication with the slave heat exchange unit via at least one vapor stream. Further, the power generation system may include at least one further power generating turbine having to receive the at least one steam from the slave heat exchange unit Flow 100125736 Form No. A0101 Page 19 of 134 Page 1003441436-0 201213655 One entry. Therefore, the system can be described as including a primary power generating full wheel and a slave power generating turbine. The primary power generating turbine can be a combustion with the present invention. A turbine that communicates with the liquid. The slave power turbine can be a turbine that communicates with a vapor stream, in particular, a supercritical steam stream that is superheated by the heat of the exhaust stream from the main power turbine. A system trimming with one or more parts from a conventional power generation system is described herein, particularly with respect to FIG. 12 and Example 2. The use of the terms of the primary power generation turbine and the slave power generation turbine should not be construed as limiting the scope of the invention, and only to provide clarity of the description. In the concept of another aspect of the invention, an external flow to the heat The high temperature end of the exchanger is heated by heat transfer from the cooled turbine discharge stream, and as a result, the high pressure recovery stream will exit the heat exchanger and enter the burner at a low temperature. In this example, the amount of fuel burned in the burner will increase, allowing the turbine inlet temperature to be maintained. The calorific value of the additional combusted fuel is equal to the additional heat load imposed on the heat exchanger. In some embodiments, the invention features a processing plant that produces shaft power from a cycle in which C〇2 is the primary circulating liquid. In a further embodiment, the invention provides a process that can meet certain conditions. In a particular embodiment, the invention is further characterized by one or more subsequent actions, or means for performing such an action: compressing the C〇2 circulating liquid to a critical value exceeding c〇2 Pressure pressure; directly burns a solid, liquid, or gaseous hydrocarbon-containing fuel in a substantially pure crucible 2 to prepare a mixture of rich (: 2 supercritical recovery liquid to achieve a desired turbine inlet temperature, For example, greater than about 500 ° C (or other temperature ranges as described herein, such as 100125736 Form No. A0101, page 20 / 134, 1003441436-0 201213655); formed by combustion products in the full wheel generated by the shaft power a supercritical flow and a reclaimed rich (3) liquid diffusion, particularly at a pressure of about 2 MPa, and below a liquid % liquid phase when the liquid is cooled to a temperature consistent with the use of the temperature cooling device Pressure (for example, about 7. 3-7.4 MPa); discharging a turbine into a heat exchanger - the turbine is discharged from the heat exchanger to be cooled, and the heat is transferred to - the recovered rich cg2 super Liquid

Cooling off-heat exchanger-containing c〇2 flow by an ambient temperature cooling device and separating liquid phase water containing at least a small amount of (3) 2 liquid phase, and package 2 containing at least a small amount of water vapor; The water-phase separation is carried out in a manner in which the CG2 and the liquid water or weak acid phase are in close contact with each other (for example, 'up to 1G seconds), so that S〇2, s〇3, H2〇, N are involved. The reaction of 〇, N〇2, 〇2ieHg can occur and the nucleus is converted to more than 9 _ sulfur in 4

Hzs〇4, and in the first class more than 90% of the nitrogen oxides are converted to HN〇3, and in the first class more than 80% of the mercury is converted to soluble mercury compounds; by cooling the gas phase (:〇2 to The non-condensing component (for example, ^, Ar, and 〇2) is separated by the temperature of the c〇2 freezing point of the gas/liquid phase separation, leaving N2, Ar, and yttrium in the gas phase. Compressing a purified gaseous C〇2 stream to a cooling by an ambient cooling device in a gas compressor produces a high density c〇 liquid (eg, 2 having at least about 200 kg/m3, preferably a pressure of at least about 3 〇〇 kg/m or, more preferably, at least about 400 kg/m 3 ; 100125736 to cool the compressed c 〇 2 by ambient cooling means to form a high density supercritical fluid A0101 Page 21 of 134 1003441436-0 201213655 For example, the density is at least about 200 kg/m3, preferably at least 300 kg/m3' or, more preferably, at least about 400 kg/m3); in a compressor a high-density CO liquid is compressed to a pressure higher than the pressure of the L 2 boundary of the c ;; a south pressure c 〇 2 flow Divided into two splits, one entering the cold end of a heat exchanger' and the second utilizing at less than about 250. (3 available external heat source for heating; promoting efficient heat transfer (including a selective external heat source) Used) such that the temperature of a turbine discharge stream entering the hot end of a heat exchanger and the recovery from the hot end of the same heat exchanger (the difference between the temperatures of the 〇2 circulating liquid is less than about 50 °C ( Or other temperature thresholds as described herein; compressing a C〇2 circulating liquid to a pressure of from about 8 MPa to about 50 MPa (or other pressure ranges as described herein); At least a portion of the recovered C〇2 recycle liquid stream and a carbonaceous fuel stream are mixed to form a separate liquid stream (or slurry, if used in a powder, solid state, below the autoignition temperature of the fuel Fuel), and its ratio is adjusted to yield an adiabatic flame temperature of approximately 1,200 ° C to 3,500 (: (or other temperature range as described herein); at least a portion of one Recycling c 0 2 circulating liquid stream and combustion product phase Combined to produce a mixed liquid stream having a temperature ranging from about 500 t to 1,600 t (or other temperature ranges as described herein); producing from about 2 MPa to about 7.3 MPa (or other pressure range) , as described herein, one of the pressures of the turbine discharge stream; utilizing one or more compressors derived from a cryogenic helium 2 plant (in particular, in the adiabatic mode), and/or a C〇2 Compressor (especially 100125736 Form No. A0101, page 22 / 134 pages 1003441436-0 201213655, in this adiabatic mode) operates by compressing heat while externally heating a portion of a high pressure c〇2 circulating liquid stream, Heat is transferred by a suitable heat transfer liquid, including the (: 2 liquid itself); one or more external liquids are heated in a heat exchanger by equal additional fuel burned in a combustor a stream, wherein one or more of the external liquid streams may comprise steam that may be superheated in the heat exchanger; heated by external heat using heat supplied by a condensed stream provided by an external source Recycling (: 〇 2 circulating fluid a portion of the stream; cooling a (including 〇 2 stream (which exits the cold end of the heat exchanger) in a heat exchanger to provide heat for heating an externally supplied liquid stream; a 馈送2 feed stream, wherein the enthalpy 2 has a molar concentration of at least about 85% (or other concentration ranges as described herein); operating a burner such that upon exiting the burner (ie, a combustion The product stream) and the concentration of 〇2 in a total gas stream entering a turbine are greater than about 0. U mole; performing a power generation process such that only one power generating turbine is used; performing a power generation process such that only one burner Used to substantially completely burn the carbonaceous fuel input to the combustor; operating a combustor such that the amount of helium 2 in the helium stream entering the combustor is lower than the fuel stream entering the combustor The amount required for stoichiometric combustion, and thus the production of one or both of h2 and carbon monoxide (CO) in the combustion product stream; one treatment with two or more turbines, each turbine having One has been fixed Exhaust pressure, wherein one or both of H2 and CO appear to leave the first turbine (and, if applicable, in addition to vortex 100125736 Form No. A0101 Page 23 / Total 134 Page 1003441436-0 201213655 Wheel series In the exhaust stream of the succeeding turbine other than the last turbine, and some or all of H2 and C0 are burned by adding a stream of 2 to the inlet of the second and subsequent turbines to The enthalpy of the enthalpy of the effluent from the last thirsty wheel, for example, the excess is greater than about 0.1%. ear. In a further embodiment, the present invention may provide one or more of the following cooling turbine discharge streams to heat a C〇2 circulating liquid in a heat exchange system such that the turbine discharge stream is cooled to a temperature below its water dew point; cooling medium by an ambient temperature and derivatization with fuel and combustion including H2S〇4, HNOQ, HC1, and other impurities (eg, 〇

Cooling the turbine discharge stream with condensed water of Hg and other metals in the form of ionic compounds in solution; compressing the purified (:〇2 circulating liquid to above its critical pressure but below 10 in a first compressor) Pressure of Mpa; cooling the circulating liquid to a point having a density greater than 600 kg/m3; compressing the high density c〇2 circulating liquid in a compressor to overcome the pressure drop in the system and feeding the cycle c〇2 liquid into the The pressure t required to burn the chamber removes a c〇2 product stream, which (the 〇2 product stream contains substantially all C〇2 formed by burning carbon in the fuel stream, which is taken from: a discharge flow of the first compressor or the second compressor; supplying water at a temperature higher than the cooling turbine discharge stream directly to the heat exchanger or by heating a side stream including the C〇2 circulating liquid Dew point of a temperature 100125736 Form No. A0101 Page 24 / Total 134 pages 1003441436-0 Degree level for this [〇2 cycle liquid one additional amount of heat so that the cycle at the hot end of the heat exchanger c〇2 Temperature difference between liquid and the thirsty wheel discharge Less than 50 °c; using a fuel comprising a carbonaceous fuel to produce a first class comprising H2, CO, CH4, H2S, NH3, and a non-flammable residue, having an enthalpy in an evapotranial cooling burner a portion of the oxidized non-flammable residue, the burner being fed with a portion of the cycle (: 〇 2 stream to cool the partially oxidized combustion product to a temperature of 500 ° C to 900 ° C, where The ash appears as solid particles that can be completely removed from the outlet liquid stream by the filtration system; the side stream flow is remixed with the separated heated circulating co9 liquid stream

U point, providing a temperature difference between the cooling turbine discharge stream and the heating cycle 液体2 liquid flow between 10 ° C and 50 ° c; providing a pressure of the turbine discharge flow leaving the cold end of the heat exchanger to This stream is rendered liquid-free when it is cooled prior to separation of the water from the impurities (: 〇 2 is formed; a minimum portion of the turbine effluent stream is utilized to enable conventional steam power generation derived from associated boiler systems and nuclear reactors The plurality of steam streams of the system are superheated; additional low heat is provided to the cycle (: 〇2 flow to become one or more pressure levels of steam taken from an external vapor source (eg, a power station) Providing heating of at least a portion of the condensate exiting the steam condenser of the steam power generation system with a dilator discharge stream exiting the cold end of the heat exchanger system; the cycle C for heat discharge from an open cycle gas turbine 〇2 stream provides form number A0101 page 25 / 134 pages 201213655 additional low heat; part of the coal oxidized derivatized gas as fuel plus % is sent to the fuel a second burner to complete the firing; a ratio of 2 m〇2 to fuel operating _ a separate burner to oxidize the fuel to a gasification product comprising c〇2, h2〇, and s〇2: 2 = the remaining fuel is oxidized to include h2'cG, and H2S components; = the enthalpy in the discharge flow of the first turbine is operated to operate the second turbine above the total pressure ratio to reduce the combustion The component is in turn reheated the intermediate pressure stream to a higher temperature before the intermediate pressure stream is expanded through the second full wheel. Even the step-by-step implementation is included as described in relation to the various figures and / The invention disclosed in the further description of the invention is provided herein. [Embodiment] The present invention will now be described more fully hereinafter with reference to the various embodiments. This disclosure is made more complete and complete, and the scope of the present invention is fully described by those of ordinary skill in the art. The invention may be embodied in many different forms and should not be construed as being limited to the implementations set forth herein. Case These embodiments are provided so that this disclosure will satisfy the applicable legal requirements. When used in the specification and in the appended claims, the singular forms "a" Unless otherwise clearly stated in the context, the present invention provides a power generation system and method through the use of a high efficiency fuel burner (eg, an evapotranial cooling burner), and associated circulating fluids (eg, (: 〇 2 circulating liquid). The liquid is combined with the appropriate fuel, any necessary oxidant, and any related materials useful for efficient combustion. 100125736 Form No. 1010101 Page 26 of 134 Page 1003441436-0 201213655

It is provided in the burner. In a particular embodiment, the method can be implemented using a burner operating at very high temperatures (eg, in the range of about 1,600 ° C to about 3,300 ° C or other temperature ranges disclosed herein). The presence of circulating liquid can act to moderate the temperature of the liquid stream exiting the combustor so that the liquid stream can be utilized in the energy transfer generated by the electrical power. Specifically, the combustion product stream can be expanded to span at least one turbine to generate electricity. The expanded gas stream can be cooled to remove various components from the stream, such as water, and heat recovered from the expanded gas stream that can be used to heat the C〇2 circulating liquid. The purified recycle liquid stream can then be pressurized and heated for recovery via the burner. If desired, the portion c〇2 from the combustion product stream (i.e., produced by c〇2 formed by the combustion of fuel-containing carbon in the presence of oxygen) may be withdrawn for storage or other Dispose of, for example, to the C〇2 line. Systems and methods can utilize specific processing parameters and parts to maximize the efficiency of the system and method (especially while avoiding the release of C to atmospheric). As specifically recited herein, the circulating liquid is exemplified by the use of (: 02 as a circulating liquid. While the use of C02 circulating liquid in accordance with the present invention is advantageous, such disclosure should not be construed as It is a necessary limitation in the scope of the present financing that can be made to the scope of the liquid (4), unless otherwise stated. In some embodiments, the power generation system according to the present invention may use a cycle including the co2 (four). In other words, the circulating liquid The chemistry immediately prior to input to the burner is such that the circulating liquid includes a significant amount of co2. In this case, the term "significantly" means that the liquid comprises at least about 90% molar concentration, at least about 91% molar. Concentration, at least about 92% molar concentration, at least about 93% molar concentration, at least about 100125736. Table early number A0101 97 "5" / ++ 1 Qy) s 1003441436-0 201213655 94% Moer Moment At least about 95% molar, at least about 96% molar, to >, about m molar, at least about 98% molar, or at least about 99% molar. of%. Preferably, the circulating liquid comprises substantially only c〇 prior to entering the burner. In this case, the filament "substantially only, may represent at least about 29.91% molar concentration, at least about 99 25% molar concentration, at least about 99.5% molar concentration, at least about 99. 75% molar concentration to; c〇2 of about 99.8% molar concentration, or at least about 999% molar concentration. In the burner '(; 〇2 can be derived from one or more fuels The other components, any oxidant, and any fuel-burning derivative are mixed. Thus, the circulating liquid leaving the burner (herein described as a combustion product stream) may include c〇2 and a smaller amount of other materials, such as Water (h2〇), oxygen (〇2), nitrogen (n2) 'nitrogen (Ar), sulfur dioxide (s〇2), sulfur trioxide (s〇3), nitric oxide (N〇), nitrogen dioxide ( N〇2), hydrogen chloride (HC1), mercury (Hg), and traces of other components that can be derived from the combustion process (eg, particulates, such as ash, or liquefied ash), which include additional combustibles. More detailed below, the combustion process can be controlled to make the properties of the liquid stream For reduction, or oxidation, it may provide benefits that will be specifically recited. The systems and methods of the present invention may incorporate one or more burners that are useful for combustion of a suitable fuel, as described herein. Preferably, at least one burner used in accordance with the present invention is a high efficiency burner capable of providing substantially complete combustion at a relatively high combustion temperature. High temperature combustion provides substantially complete fuel combustion It is particularly useful, and thus maximizes efficiency. In various embodiments, high temperature combustion form number A0101 page 28/134 pages 1003441436-0 201213655 may represent at least about 1,200 ° C, at least about 1,300 ° C, at least about 1,400 ° C, at least about 1,500 ° C, at least about 1,600 ° C, at least about 1,750 ° C, at least about 2,000 ° C, at least about 2,500 ° C, or at least about Combustion at a temperature of 3,000 ° C. In a further embodiment, high temperature combustion can be expressed at about 1,200 t to about 5,000 ° C, about 1,500 ° C to about 4,000. (: , about ' 1,600 ° (: to Approximately 3,500 °0:, approximately 1,700. (: to approximately 3,200 ° C, approximately 1,800 ° C to approximately 3,10 0 ° C, approximately 1,900. (: to approximately 3,000 ° C, or approximately 2,000 ° C Burning to a temperature of about 3 000 t. In some embodiments, high temperature combustion according to the present invention can be achieved using an evapotranial cooling combustor. One example of an evapotranspiration burner that can be used in the present invention is described in U.S. Patent Application Serial No. 12/714,074, filed on Jan. 26, 201, the entire disclosure of which is hereby incorporated by reference. In some embodiments, an available evaporative cooling burner in accordance with the present invention may include one or more heat exchange zones, one or more cooling liquids, and one or more evapotranspiration liquids. According to the present invention, the use of an evapotranial cooling burner is particularly advantageous in terms of fuel combustion for power generation relative to conventional techniques. For example, the use of evapotranspiration can effectively prevent corrosion, dirt, and erosion in the burner. This in turn allows the burner to operate over a sufficiently high temperature range to provide complete, or at least substantially complete, combustion of the fuel used. These, as well as further advantages, are further described herein. In a particular aspect, an evapotranspiration burner useful in accordance with the present invention can include a combustion chamber at least partially defined by an evapotranspiration member, wherein the evapotranspiration member is at least partially surrounded by a pressure suppression member. The combustion 1003441436-0 100125736 Form No. A0101 Page 29 of 134 201213655 The chamber can have - part of the population - relative export section. The inlet portion of the combustion chamber is configurable to receive a carbonaceous fuel for combustion at a combustion temperature in a combustion = chamber to form a combustion product. The firing chamber may be further configured to direct combustion products to the outlet portion. The transpiration member may be configured to direct evapotranic material therethrough to the combustion chamber to buffer combustion products and interactions between the transpiration members. . Additionally, the evapotranspiration material can be introduced into the combustion chamber to achieve a desired outlet temperature for the combustion product. In a particular embodiment, the evapotranspiration can comprise at least a portion of the circulating liquid. The walls of the combustion chamber may be lined with a layer of porous material whereby the evapotrans (e.g., c2, and/or 1120) are thereby directed and flow. In other aspects, the inner transpiration member 2332 can be expanded from the inlet portion 222A of the evapotranspiration member 230 to the outlet portion 222B, and in some examples, the perforated/porous structure of the sigma internal evapotranspiration member 2332 can be substantially completely The inlet portion 222A is expanded to the outlet portion 222β such that the evapotranspiration liquid 210 is substantially introduced into the entire length of the combustion chamber 222. That is, in general, the entirety of the internal transpiration member 2332 can be configured with a perforated/porous structure to allow substantially the entire length of the combustion chamber m to be subjected to evapotranspiration. More particularly, in some aspects, the cumulative perforation/hole area can be substantially equal to the surface area of the internal evapotranspiration member 2332. In still other aspects, the perforations/holes may be spaced apart at an appropriate density such that the evapotranic material can be dispensed substantially uniformly from the internal transpiration member 2332 into the combustion chamber m (i.e., without lack of evapotranspiration) The flow of matter or the presence of "dead spots (hearts are 100125736 spots)"). In one example, the square inch of the internal transpiration component m2 may include a perforation per level of 25 〇 X 25 〇 form nickname A0101 page 30 / 134 pages 1003441436-0 201213655 The hole array 'supplied to provide approximately 62,500 holes per square inch, such perforations/holes are spaced apart by a distance of approximately 〇4 吋 (0. 1 _) "hole area and the total wall The ratio porosity of the region can be, for example, about 5%. The array of holes can vary over a wide range to suit the design parameters of other systems, such as the desired pressure drop relative to the flow rate across the evapotranspiration component. In some instances, an array size of from about 10 x 10 to about 10,000 X 10, Å per inch having a porosity of from about 10% to about 80% can be used. The flow of evapotranic material through the porous evapotranspiration layer and optionally through additional supply can be configured to achieve a desired total exit liquid outlet temperature from the burner. In some embodiments, as will be described further herein, such temperatures can range from about 500 °C to about 2,000. Within the range of (: the flow may also be used to cool the transpiration member to a temperature below the maximum allowable operating temperature of the material forming the transpiration member. The evapotranspiration may also be used to prevent possible impact, contamination, or otherwise Damage to any liquid or solid ash material, or other contaminants in the fuel of such walls. In such an example, 'evaporable components may require the use of materials with reasonable thermal conductivity so that incident radiant heat can be radial The ground is conducted outwardly through the porous evaporative component and is then intercepted by convective heat transfer from the surface of the porous layer structure to the liquid radially inward through the vaporized layer. Such an architecture may allow for being directed through the The contiguous portion of the stream of the transpiration member is heated to a temperature within the desired range, for example, from about 500 ° C to about 1, 〇〇〇 ° C, and at the same time maintaining the temperature of the porous evapotranture at its location Suitable materials for the porous evaporative component may include, for example, porous ceramics, refractory metal fiber blankets, drilled holes. Column section, and/or sintered metal 100125736 Form No. A0101 Page 31 of 134 Page 1003441436-0 201213655 Metal powder. The second function of the ET component is that it can be flat on both sides. The heat dispersing liquid is controlled to flow inwardly and longitudinally along the 'combustion ☆ to achieve the evapotranspiration liquid flow and the = mixing while simultaneously increasing the length along the combustion chamber = the body energy is available to achieve the diluent speed to provide Solid, and/or liquid particles that are buffered or otherwise blocked to burn off ash or other contaminants in the product to thereby avoid impact on the surface of the transpiration layer and to avoid enthalpy or other damage. For example, such factors It may only be possible to burn the fuel (eg, coal) with a residual flammable residue (% of the coal) to the inner wall of the burner pressure line of the transpiration component. The high temperature evapotranspiration stream in the burner. An embodiment of a burner apparatus for use in accordance with the present invention is schematically illustrated in Figure 1, which is generally indicated by numeral 220. In the example, the burner assembly 22G can be configured to combust a particulate solid (e.g., coal) to form a combustion product, although any other suitable combustible carbonaceous material (as disclosed herein) can also be used as a fuel. The combustion chamber 222 can be defined by an evaporative component 23, which is configured to feed the (4) of the money chamber 222 (i.e., to facilitate evapotranspiration cooling, and/or to buffer the combustion). The product and the interaction between the evaporative component classes. It will be appreciated by those of ordinary skill in the art that the wire 23 is cylindrical in shape to define a generally cylindrical shape with a human sigma portion And one phase 100125736 Form No. AOlOi Page 32 of 134 is a simple combustion chamber 222 for the outlet portion. The steaming component (10) can be at least partially surrounded by a pressure suppression member (four). The mouth thin A of the torn chamber can be configured to receive symbols from the general

Amm «Γ on . _ 1003441436-0 201213655 This fueling mixture of this mixing arrangement. In other embodiments, such a mixing arrangement may be absent, and one or more of the materials input into the burner may be separately added via separate inlets. According to a particular embodiment, the fuel mixture can be combusted in the combustion chamber 222 at a particular combustion temperature to form a combustion product, wherein 'the combustion chamber 222 can be configured further to direct the combustion product to the outlet Part 222B. A heat removal device 2350 (see, for example, 'Fig. 2) can be associated with the pressure suppression component 2338 and configured to control its temperature. In a particular example, the heat removal device 2350 can include a heat transfer jacket defined at least in part by a wall 2336 relative to the pressure suppression member 2338, wherein a liquid can be defined by a water cycle therebetween The jacket 2337 circulates. In an embodiment, the circulating liquid can be water. In a particular aspect, the porous internal evapotranspiration member 2332 is thus configured to introduce the non-dispersive liquid into the combustion chamber 222 such that the evapotranspiration 210 is present in an interior surface that is generally offset relative to the internal evapotranspiration member 2. A right angle (9G) angle into the combustion chamber 222 » in addition to these advantages β, the diffusion of the substance 210 at a right angle relative to the internal transpiration member 2332 also facilitates, or otherwise enhances, the furnace /Check liquid ~ "Solid solid droplets, or other contaminants, or hot combustion liquid swirls from the inner surface of the internal evapotranspiration member 2332. When there is no contact between the slag liquid or the mouth droplets, the droplets can be prevented from coalescing into larger droplets or groups, which are known in the prior art to be between droplets or particles and solid walls. It happens immediately after contact. The evapotranspiration material guide 1003441436-0 is generally at a right angle to the diverging member 2332. This helps to <in other ways enhances the possible impact and damages 100125736 Form No. A0101 Page 33 / Total 134 pages 201213655 The internal transpiration member has the effect of forming a turbulent flow of combustion liquid at a sufficient velocity perpendicular to and adjacent to the internal transpiration member. In such an example, the external transpiration member 2331, the pressure suppression member 2338, the heat transfer jacket 2336, and/or the insulation layer 2339 can be configured (individually, or collectively) to provide an associated evapotranible substance/liquid The various effects of the delivery of 21 〇 reaching and over the internal distracting component 2332 and entering the combustion chamber 222 (i.e., providing a substantially evenly distributed supply). That is, the substantially uniform supply of the evapotranspiration material 21〇 into the combustion chamber 222 (according to flow rate, pressure, or any other suitable and appropriate measurement) can be configured by configuring the external evapotranspiration component 2331, the pressure suppression component 2338, the heat transfer jacket 2336, and/or the heat insulating layer 2339 is achieved, thereby providing a uniformly supplied evapotranspiration 21 〇 to the internal loose component 2332, or the effluent f21() is related to the internal transpiration component The supply of the outer surface of the 2 3 3 2 may be specifically customized and configured to achieve a substantially uniform distribution of the evapotranspiration 21 in the combustion chamber 222. Such a substantially uniform distribution avoids the formation of hot combustion liquid vortices that otherwise form and possibly impinge and damage internal transpiration components by the interaction of the non-uniform evapotranic liquid with the flow of the combustion liquid. The mixing arrangement 250, when present, can be configured to mix the carbonaceous fuel 254 with enriched oxygen 242 and a circulating liquid 236 to form a fuel mixture. The carbonaceous fuel 254 can be provided in the form of a solid carbonaceous fuel, a liquid carbonaceous fuel, and/or a gaseous carbonaceous fuel. The oxygen enriched 242 can be oxygen having a molar purity greater than about 85%. The supply of oxygen-enriched 242, for example, can be performed by any air known in the art as a system/technique, such as, for example, a cryogenic air separation process, or a temperature ion-permeable membrane oxygenation can be performed. Separation process (from the air 100125736 form number A0101 page 34 / 134 page ιηΜ /) gas). As described herein, the circulating liquid 236 can be carbon dioxide. In the example where the carbonaceous fuel 254 is particulate solids (e.g., pulverized coal 254A)', the mixing arrangement 250 can be further configured to mix the particulate solid carbonaceous fuel 254A and a liquefied material 255. According to one aspect, the particulate solid carbon fuel 254A can have an average particle size of between about 50 microns and about 200 microns, and according to still another aspect, the liquefied material 255 can comprise water, and/or liquid C〇2, Its density is between about 450 kg/m3 and about 11 〇〇kg/m3. More specifically, the liquefied material 255 can be formed in conjunction with the particulate solid carbonaceous fuel 254A, for example, slurry 250A between about 25 and about 55 percent by weight of the particulate solid carbonaceous fuel 254A. Although in FIG. 1, the oxygen 242 is shown to be mixed with the fuel 254 and the circulating liquid 236 prior to introduction into the combustion chamber 222, those of ordinary skill in the art will understand that, in some instances, The oxygen 242 is detachably introduced into the combustion chamber 222 when necessary or desired. The mixing arrangement 250, in some aspects, can include, for example, an array of spaced apart injection nozzles (not shown) that can be disposed in the evapotranspiration associated with the inlet portion 222A of the cylindrical combustion chamber 222. Near the end wall 223 of the component 230. Injecting the fuel/fuel mixture into the combustion chamber 222 in this manner can provide, for example, a large surface area injected fuel mixed inlet stream, which in turn facilitates mixing the injected fuel inlet stream by irradiation Perform fast heat transfer. Thus the temperature of the injected fuel mixture can be rapidly increased to the ignition temperature of the fuel, and thus can result in tight combustion. Although these values are dependent on a number of factors, such as the architecture of a particular injection nozzle, the injection rate of the fuel mixture can fall, for example, from about 1 〇 m/sec to about 40 m / Form No. A0101, page 35 / Total 134 pages 1〇〇201213655

The range between Sec. This way. For example, the note 2 = can be used in a number of different forms. 5 (d) is about, for example, 'spinning between about a fuel of about i / coffee U_' where it has been noted. A velocity of ms to about 40 m/s is injected through the positive: the stripping member 230, which is more particularly shown in Fig. 2, is subjected to a constant value, and the pressure reducing member 230 is at least partially suppressed. The part 2338 can be surrounded by 1 & in some examples 'the pressure is surrounded, wherein the secret part is subjected to a heat transfer jacket such as 6 gamma fit and the Pb1 transfer sleeve 2336 can be pressed with the pressure suppression member The water stream can be fed or more channels 2337 whereby the low level can therefore be used to control and/or transmit through an evaporation mechanism, the degree of water of the cycle, for example, at the selected temperature of the pressure suppression component 2338. In some respects, J100 W. . And within the scope of the magic suppression member 2338a 2339 can be disposed on the evapotranspiration member 230 with :::::: 21, the outer member 2332 is disposed as; the internal evapotranspiration member 2332, and the internal evapotranspiration member The pressure suppression member 2338 is operative from any suitable firing chamber 222 relative to the outer member. The external transpiration portion, steel, and steel alloy, includes: a material composition, for example, including stainless steel and a nickel alloy. In some instances, the outer evapotranspiration member is configurable to define a first evapotranspiration supply passage 2333A extending therebetween from its adjacent surface to the surface of the internal evapotranspiration member 2332. In some examples - 100125736, the first evapotranspiration supply may correspond to the embossed surface number 36 pages/total 34 pages 10034^201213655 force suppression component 2338, the heat transfer jacket 2336, and/or the thermal insulation The second evapotranspiration liquid supply passage 233 3B defined by the layer 233 9 . The first and second evapotranspiration liquid supply passages 2333A, 2333B can thus be configured to cooperate to direct an evapotranspiration liquid therebetween through the internal evapotranspiration member 2332. In some examples, as shown in FIG. 1, for example, the squirting liquid 210 can include the circulated liquid 236, and the same source from which it can be associated with the first and second evapotranspiration liquids. Supply passages 2333A, 2333B, if necessary, may be adiabatic for delivering sufficient supply and sufficient pressure of the evapotranspiration liquid 21〇 (ie, ^coo, such that the evapotranspiration liquid 21〇 is directed through the interior Evaporating component 2332 and entering combustion chamber 222. The method involving the evaporative component 230 and associated evapotranspiration 21 (as disclosed herein) may allow the burner assembly 22 to be relatively high. The pressure and relatively high temperatures operate in different ways as disclosed herein. In this regard, the internal transpiration member 2332 can be constructed of, for example, a porous (tetra) material, a perforated material, a layer ride, in two dimensions. (4) Orientation ^ ☆ a three-dimensional porous carpet composed of sequential fibers, or any other suitable material, or a combination thereof that exhibits the desired features as disclosed herein, ie A plurality of flow passages or holes or other suitable openings 23 to receive and guide the porous ware through the internal evapotranspiration member 2332 and other suitable limitations for such evapotranspiration cooling systems include alumina, yttria, conversion Toughened zirconia (trans_ formation-t〇Ughened zirc〇nium), steel, molybdenum,:, copper-plated tungsten (C〇Pper-infiltrated tungsten), tungsten coated (tungSten-C〇ated m〇lybdenum), tungsten Coated copper (100125736 Form No. A0101, page 37 / 134 pages, 201213655 tungsten-coated copper), various high temperature nickel alloys, rhenium-sheathed or coated materials. Suitable sources of materials, for example Package Inc. (Golden, CO) (^) ; UltraMet Advanced

Materials Solutions (Pacoima, CA) (refractory metal coating), 0rsam Sylvania (Danvers, MA) (tungsten/copper); and MarkeTech International, lnc. (port Townsend, WA) (tungsten). Examples of perforated materials suitable for use in such an evapotranspiration cooling system include all of the materials described above, as well as suppliers (wherein the perforated end structures can be obtained by perforating the initial non-porous structure using methods known in the art of fabrication). Examples of suitable laminates include all of the materials described above, as well as the supplier (wherein the laminated end structure can be achieved by, for example, using known methods of manufacturing techniques) to achieve the desired end aperture. This is obtained by laminating a non-porous or partially perforated structure.) 100125736 Form No. A0101, page 38/134, pp. 3A and 3B illustrate the definition of the combustion in an aspect of the burner assembly 22〇 The structure of the chamber 222 is permeable to the evapotranspiration member 23 and the surrounding force suppression member 2338 or the heat insulating layer 2339 (for example, disposed between the transpiration member 23{) and the pressure suppression portion (4) 38. The :::thermal" interface is formed. For example, when relatively cold, the size of the heat dissipating component 230 can be more relative to the surrounding pressure suppressing component 2338. In the radial direction, and/or in the axial direction, when inserted into the pressure suppressing member 2338, a radial, and/or axial gap may occur therebetween (see, for example, Fig. 3A). Of course, such a difference in the inch can help the evapotranspiration component to intervene in the force-suppressing component. However, 'for example, when heating toward the operating temperature, the flute can be used as the scatter component 23Q can be configured. For backwards and/or axial extension, see , μ % 例如 例如 例如 例如 例如 例如 例如 例如 例如 例如 例如 例如 以及 以及 以及 以及 以及 以及 以及 以及 以及 以及 以及 以及 以及 以及 以及 以及 以及 以及 以及 以及 以及 以及 以及 以及 以及 以及 以及 以及In this case, the money component 230 relates to the "heart" of the evapotranspiration component 23 and the internal evapotranspiration, which is placed under compression. Thus, a suitable high temperature "^ resistant fragile material (e.g., porous ceramics can be used to form the internal evapotranspiration 2332).

With such an arrangement of the internal transpiration member 2332, the evapotranspiration 210 can include, for example, carbon dioxide directed through the internal transpiration member 2332 (i.e., from the same source as the circulated liquid 236) to cause the evapotranspiration. Substance 2U) immediately forms a buffer layer 231 adjacent to the internal evapotranspiration member 2332 within the combustion chamber milk (i.e., - "Steam Wall

The buffer layer 231 can be configured to buffer the interaction between the internal evapotranspiration component 2332 and the liquefied non-combustible component associated with the combustion product and heat. That is, in some examples, the evapotranspiration liquid 210 can be delivered through the internal evapotranspiration component 2332, for example, at least under pressure within the combustion chamber 222, wherein the evapotranspiration liquid 21 〇 enters the combustion The flow rate of chamber 222 (i.e., c〇2 flow) is sufficient to mix the effluent liquid 210 with the combustion product and to cool the combustion product to form an exiting liquid mixture at a sufficient temperature for the inlet demand for subsequent downstream processing. (i.e., a turbine may require an inlet temperature of, for example, about 1 '225 C), but wherein the leaving liquid mixture is still sufficiently south to maintain slag droplets or other contaminants in the fluid, or liquid state of the fuel. The liquid state of the non-combustible elements of the fuel may contribute, for example, to the separation of such contaminants from the liquid form of the combustion 100125736 Form No. A0101 Page 39 / Total 134 pages 1003441436-0 201213655 Preferably, in a free flowing, low viscosity form, it will be less likely to impede or otherwise damage any removal system performed for such separation. In practice, such a demand may depend on various factors, such as the type of solid carbonaceous fuel (i.e., coal) used, and the particular characteristics of the slag formed in the combustion process. That is, the combustion temperature in the combustion chamber 222 can cause any non-combustible elements in the carbonaceous fuel to be liquefied in the combustion products. In a particular aspect, the porous internal transpiration member 2332 is thus configured to direct the evapotranic liquid into the combustion chamber 222 in a radially inward manner, thereby forming a liquid barrier wall, or buffer layer 231, the liquid barrier wall The buffer layer 231 is associated with the surface of the internal evapotranspiration member 2332 that defines the combustion chamber 222 (see, for example, Figure 2). The surface of the internal evapotranspiration member 2 3 3 2 is also heated by the products of combustion. In this connection, the porous internal transpiration member 2332 can be configured to have suitable thermal conductivity such that the evapotranspiration liquid 210 passing through the internal transpiration member 2332 is heated while the porous internal transpiration member 2332 is simultaneously cooled, resulting in a definition The temperature of the surface of the internal transpiration member 2332 of the combustion chamber 222 falls within the highest combustion temperature range, approximately, for example, 1,000 °C. The liquid barrier wall or buffer layer 2 31 formed by the combination of the evapotranspiration liquid 210 and the internal esteam component 2332 thus buffers the interaction of the internal evapotranspiration component 2332 with the high temperature combustion products and slag or other contaminant particles, And thus the internal transpiration member 2332 is buffered from contact, contamination, or other damage. Furthermore, the evapotranspiration liquid 210 can be introduced into the combustion chamber 222 via the internal esteam component 2332 in a manner to adjust the combustion chamber at a desired temperature (eg, from about 500 ° C to about 2,000 ° C). The evapotranspiration liquid 100125736 around the outlet portion 222B of 222 is shown in Form No. A0101, page 40 of 134, 1003441436-0 201213655 210, and an exiting mixture of the combustion products. In a particular embodiment, the burner assembly 220 can thus be configured to provide a relatively complete combustion of a fuel 254 at a relatively high operating temperature as described herein - efficient burning Device. In some examples, such a burner burner - 'or more cooling liquid' and / or - or more evapotranspiration 21 〇 . Additional parts can also be (4) connected to the burning brain | set 22 (four) is executed. For example, an air separation unit may be provided to separate % and enthalpy, and - a fuel injector device may provide for the collection of the unit from the air separation unit 2 and the circulation of the liquid and the gas, _Liquid, 2 - supercritical liquid, or - a fuel stream of solid particulate fuel in the form of high density CG2_t combined. In another aspect, the evapotranspiration burner set 22 can include a fuel injector to inject a pressurized fuel stream into the combustion chamber 222 of the burner assembly 22, wherein the fuel The stream may include a treated carbonaceous fuel 254, a fluidizing medium 255 (which may include the circulating liquid coffee 'as discussed herein), and oxygen 242 1 (rich) oxygen such as the Cl circulating liquid 236 may be combined Become a homogeneous supercritical mixture. The amount of oxygen present is sufficient to combust the fuel and produce a combustion product having the desired composition. The burner assembly 220 can also include a combustion chamber 222 configured to - a high pressure, high temperature combustion volume to receive the fuel stream, and enter the porous venting member 23 by defining a combustion chamber 222 Combustion volume - evapotranic liquid 210. The feed rate of the evapotranspiration liquid 21〇 can be used to control the temperature of the burner unit outlet portion/turbine inlet portion to a desired value, and/or to cool the evapotranspiration member 23 to be compatible with forming the evapotranspiration The temperature of the material of component 230. The evapotranspiration liquid 210 directed through the evapotranspiration 100125736 Form No. Λ0101, page 41/134, 1003441436-0 201213655 component 230 provides a liquid/buffer at the surface of the evapotranspiration member 230 defining the combustion chamber 222. a layer, wherein the liquid/buffer layer prevents particles of ash or liquid slag from interacting with the exposed walls of the evaporative component 230 due to combustion of certain fuels. The combustion chamber 222 can be further configured to The fuel stream (and the circulating liquid 236) may be injected at a pressure greater than the pressure at which the combustion occurs, or otherwise introduced into the combustion chamber 222. The burner assembly 220 can include a pressure suppression component 2338 that at least partially surrounds the evapotranspiration member 230 defining the combustion chamber 222, wherein a thermal insulation component 2339 can be disposed to the pressure suppression component 2338 and the evapotranspiration component 230 between. In some examples, a heat removal device 2350, for example, a jacketed water cooling system defining a water circulation jacket 2337, can be combined with the pressure suppression member 2338 (i.e., circumscribed to the "shell" forming the burner assembly 220. The pressure suppression member 2338), the evapotranspiration liquid 210 to which the transpiration member 230 of the burner device 220 is coupled, may be, for example, a small amount of Η0, and/or an inert gas (for example, \or U Ld argon mixed C 〇 2, the transpiration member 230 may comprise, for example, a porous metal, a terrarium, a composite matrix, a layered manifold, any other suitable Structure, or a combination thereof. In some aspects, combustion within the combustion chamber 222 can produce a high pressure, high temperature combustion product stream that can be subsequently directed to a power generating device, such as a turbine, for expansion associated therewith, as in A more comprehensive description of this. The relatively higher pressure performed by the embodiment of a burner apparatus disclosed herein can be applied to generate a 100125736 form number A0101 in a minimum volume. Page 42 of 134 pages 1003441436- 0 201213655 Energy concentration is a relatively high intensity which essentially results in a relatively high energy density. This relatively high energy density enables downstream processing of this energy to be performed in a more efficient manner than at lower pressures, and thus provides a feasibility factor for the technology. Thus, aspects of this disclosure provide a level of strength greater than that of an existing power plant (i.e., 10-100 times). This higher energy density increases the efficiency of the process, but also reduces the cost of the equipment required to perform the energy conversion from self-heating to electrical power (by reducing the size and quality of the device, thereby reducing the cost of the device). As discussed herein in other ways, the burner apparatus used in the method and system of the present invention can be used to combust a variety of different carbonaceous fuel sources. In a particular embodiment, the carbonaceous fuel can be substantially completely combusted such that the combustion product stream does not include a liquid, or solid, incombustible material. However, in some embodiments, a solid carbonaceous fuel (e.g., coal) useful in the present invention may result in the appearance of non-combustible materials. In a particular embodiment, the burner assembly can include the ability to achieve a combustion temperature that causes the non-combustible elements in the solid carbonaceous fuel to be liquefied during the combustion process. In such an example, the manner in which the liquefied non-combustible component is removed can be applied. The completion of the removal may, for example, utilize a cyclonic separator, an impact separator, or a graded refractory particulate filter bed disposed in a toroidal configuration, or a combination thereof. In a particular embodiment, the droplets may be removed from the high temperature circulating liquid stream by a series of cyclonic separators (e.g., a separator device 2340 shown in Figure 4). . In general, aspects of such a cyclonic separator as disclosed herein may include a plurality of centrifugal separators 1 in series (including an inlet centrifugal separator device 100A, 100125736, Form No. A0101, page 43 / 134 pages 1003441436-0 201213655 which are configured to receive the combustion product/outflow liquid stream and associated liquefied non-combustible elements thereof, and an outlet centrifugal separator device 008 configured to discharge combustion products/ Leaving the liquid stream, the combustion product/exit liquid stream has such liquefied non-combustible elements that are substantially removed therefrom. Each centrifugal separator device 100 includes a plurality of centrifugal separator elements, or a cyclone 1, operatively disposed in parallel with a central collection line 2, wherein each centrifugal separator element, or cyclone 1, is configured to be self-contained The combustion product/exit liquid stream removes at least a portion of the liquefied non-combustible elements and directs the removed portions of the liquefied non-combustible elements to a sump 20. Such a separator device 2340 can be configured to operate at an elevated pressure and, thus, can further include a pressure-containing housing configured to collect the centrifugal separators The device and the sump. According to such an aspect, the pressure bearing housing 125 can be an extension of the pressure suppression member 238 (which also surrounds the burner assembly 220), or the pressure bearing housing 125 can be associated with the burner device 2 2 A pressure separating member 2338 of 0 is combined with a separate member. In either case, due to the elevated temperature experienced by the separator device 2340 via the exiting liquid stream, the pressure bearing housing 125 can also include a operatively coupled therewith to remove heat generated therefrom. A heat dissipation system, for example, a heat transfer jacket (not shown) having a liquid circulating therein. In some aspects, a heat recovery device (not shown) can be operatively coupled to the heat transfer jacket, wherein the heat recovery device can be configured to receive liquid circulated in the heat transfer jacket and regain Thermal energy from the liquid. In a particular embodiment, the (slag removal) separation gas unit 2340 (shown in Figure 4) can be configured to be around its outlet portion 222B and with 100125736 Form No. A0101 Page 44 of 134 Page 1003441436 -0 201213655 The combustion station 220 is placed in series to receive the dew flow/combustion product therefrom. The effluent from the burner unit 22 is cooled to exit the liquid stream, and the liquid slag (non-combustible elements) therein can be guided to enter the inlet centrifugal separator via a conical reducer 1 The central collection of device 10GA provides 2A. In the aspect, the separator device 2340 can include three centrifugal separator devices 1A, i〇〇b, 100C (although it will be understood by those of ordinary skill in the art that a separation

The device may include one, two, three, or more centrifugal separator devices when necessary or desired. In this example, the three centrifugal separator devices 1A, 1B, 1A operatively arranged in series provide a 3-stage cyclone separation unit. Each of the centrifugal separator devices includes, by way of example, a plurality of centrifugal separator elements (cyclonic n, which are disposed in the phase

Corresponding to the central collection line 2, the central collection of the inlet centrifugal separator device 10A provides 2A and the central collection line 2, and the intermediate centrifugal separator device stores each (4) at its outlet end The place is sealed. In these examples, the exiting liquid stream is directed into a branch passage 11 of each of the centrifugal separator elements (cyclones) corresponding to the respective centrifugal separator devices UO. The branch channels 11 are configured to be combined with the inlet ends of the respective cyclones 1 to form a tangentiai inlet (which causes, for example, the exiting liquid flow into the cyclone 1 in the spiral flow) The wall of the cyclone i interacts). The outlet passage 3 from each of the cyclones 1 then enters the inlet portion of the central collection line 2 of the respective centrifugal separator device 1 in accordance with the route. At the outlet centrifugal separator I, at the outlet, the exiting liquid stream (having a substantially non-combustible element separated therefrom) from the outlet 100125736, the central collection line of the centrifugal separator device 100A, Α0101, page 45/total Page 134 and via a collection 1003441436-0 201213655 collection line 12 and an outlet nozzle 5 are directed such that the "clean" exit liquid stream can then be directed to a subsequent process, for example, associated with the conversion device. Thus, an exemplary three-stage cyclonic separation arrangement allows the slag in the exiting liquid stream to be removed and reduced, for example, by less than 5 ppm by mass. At each stage of the separator device 2340, the separated liquid slag is guided from each of the cyclones 1 via an outlet pipe 4 extending to a sump 20. The separated liquid slag is then introduced into an outlet nozzle or line 14 extending from the sump 20 and the pressure bearing housing 125 to remove, and/or re-acquire, components therefrom. In effecting the removal of the slag, the liquid slag may be directed through a water-cooled section 6, or otherwise through a section having a high pressure, cold water connection, wherein the interaction with water causes the liquid slag to solidify, and/ Or form granular. The mixture of solidified slag and water can then be separated into a slag/water liquid mixture in a line (collection provided) 7, which can be removed by a suitable valve 9, especially after the pressure drop, at the same time Any remaining gas can be removed via a separate line 8. In some embodiments, one of the sequential operational phase pairs may allow for continuous operation of the system. Since the separator device 2340 can be executed with a relatively higher temperature combustion product stream (i.e., at a temperature sufficient to maintain the non-flammable elements at a lower viscosity in liquid form), in some instances it may be desirable It is desirable that the surface of the separator device 2340 exposed to the combustion product/outflow liquid stream and one of the liquefied non-combustible elements associated therewith can be configured to have high temperature resistance, high corrosion resistance, And a material composed of one of low thermal conductivity. Examples of such materials may include cerium oxide and aluminum oxide, although such an example is not intended to be 100125736 Form No. A0101 Page 46 of 134 1003441436-0 201213655 as a limitation of any type. Thus, in certain aspects, the separator device 2340 can be configured to substantially remove the liquefied non-combustible elements from the combustion product/exit liquid stream and maintain the non-combustible elements in a low viscosity liquid state Form, at least until it is removed from the sump. Of course, in embodiments where a non-solid fuel is used and the non-combustible material is not included in the combustion product stream, there is no need to additionally add the slag separator.

ϋ In some embodiments, the separator device 2340 can be used to separate particulate solid ash residues from the combustion of any fuel (eg, coal) that produces a non-combustible solid residue. For example, the coal can be Grinding to a desired size (for example, such that less than 1% by weight of the particulate or powdered coal may include the size of the particles having a size greater than 100 μm) and using a liquid (: 〇 2 to form a slurry. The embodiment may have a temperature of from about -40 C to about -18 C. The slurry may include from about 40% to about 60% by weight of coal. The slurry may then be subjected to Pressurized to the desired combustion pressure. Referring to Figure 1, the recovery stream 236 can be separated in relation to the mode of entering the burner 220. A first portion (stream 236a) can be input via the mixing arrangement 250. A second portion (stream 236b) of the combustor 220 can be introduced into the combustor 220 by traversing the evaporative cooling layer 230. As mentioned above, it is possible to cause a reducing gas.

The burner 220 is operated at a ratio of 〇2 to fuel in the form of a bulk mixture (eg, 'including, Η, CHj, CO, H„S, and/or NH Z 4 2 3 ). The chilled cooling layer is passed through the burner The portion of stream 236 can be used to cool the mixture of combustion gases and the co2 circulating liquid to a temperature substantially below the solidification temperature of the ash (eg, falling between about 500 ° C and about 900 ° 0) In the range), the total gas flow 5 from the separator device 2340 can pass 100125736 Form No. A0101 Page 47 / Total 134 pages 1003441436-0 201213655 After a single pass, it can lower the level of the remaining solid ash particles To a very low value (for example, about 2 mg/m below the gas passing through the filter). This clean gas is then burned in a second burner 'here' it can be recycled with another part The liquid stream 236 is diluted. In the illustrated embodiment, the recovered liquid stream 236 can be distributed between two burners as desired. Any carbonaceous material can be used as a fuel in accordance with the present invention. 'Because of the method in the present invention And the high pressure and high temperature maintained by the oxygen-fueled burner unit used in the system. The available fuels include, but are not limited to, various grades and types of coal, wood, oil, fuel oil, natural gas, coal. Fuel gas for the base, tar from the tar sand, bitumen, biomass, algae, classified flammable solid waste, tar (aSpha 11), used tires, diesel, gasoline, jet fuel ( JP-5, JP-4), vaporized, or pyrolyzed gas, ethanol, solid and liquid biomass fuels derived from hydrocarbonaceous materials. This can be considered as an important difference from conventional systems and methods. It is known that conventional systems for burning solid fuels (e.g., coal) require quite different designs than systems for burning non-solid fuels (e.g., natural gas). The fuel can be properly treated to allow for adequate The velocity is injected into the combustion apparatus at a higher pressure than the combustion chamber. Such a fuel may be suitably fluid at ambient or elevated temperatures. And a liquid, slurry, gel, or paste form of viscosity. For example, the fuel can be supplied from about 30 ° C to about 500. (:, about 40 ° C to about 450 ° C, about 50 ° C to approximately 425. (3, or a temperature of approximately 75 ° C to approximately 400 ° C. Any solid fuel material can be ground 100125736 Form No. A0101 Page 48 / Total 134 pages 1003441436-0 201213655 Grinding, or Shredding, or otherwise, processing to properly reduce the particle size. Fluidization, or slurrying media may be added as needed to achieve the proper form and to meet the flow requirements of the high pressure pump. Of course, depending on the form of the fuel (i.e., liquid, or gaseous), a fluidized medium may not be needed. Likewise, in some embodiments, recycled circulating liquid can be used as the fluidizing medium. Ο

In accordance with the present invention, an effluent liquid suitable for use in a combustor can include any liquid that can flow through the liner in a sufficient amount and pressure to form the vapor wall. In the present embodiment, c 〇 2 may be an ideal evapotran liquid because the formed vapor wall has good thermal insulating properties as well as visible light and UV light absorbing properties. C〇2 can be used as a supercritical liquid. Other examples of effluent liquids include \0, cooled combustion product gases recovered from downstream, oxygen, helium, natural gas, helium, and other light hydrocarbons. The fuel can be used, inter alia, as an effluent liquid during the initial period of the burner to achieve an appropriate operating temperature and pressure at the burner 10 prior to injection of the primary fuel source. Fuel can also be used as an effluent liquid to adjust the operating temperature and pressure of the burner during switching between primary fuel sources (e.g., when switching from coal to biomass as the primary fuel). In some embodiments, two or more evapotranible liquids can be used. Furthermore, different effluent liquids can be used at different locations along the burner. For example, a first evapotranspiration liquid can be used in a high temperature heat exchange zone, and a second evapotranspiration liquid can be used in a lower temperature heat exchange zone. The effluent liquid can be optimized for the temperature and pressure conditions of the combustion chamber from which the vapor wall forms the vapor wall. In this example, the effluent liquid is a preheated recovery C 〇 2 . In one aspect, the invention provides a method of generating electricity. In particular, these 100125736 Form No. A0101 Page 49 of 134 1003441436-0 201213655 The method uses a c〇2 circulating liquid which is preferably recovered as such by the method. The method of the present invention also uses a high efficiency burner, such as, for example, the evapotranspiration burner described above. In some embodiments, the method is generally described in relation to the flow chart shown in Figure 5. As can be seen therein, a burner 220 is provided and various inputs are also provided therein. A carbonaceous fuel 254 and 02242 (as needed) may be introduced into the burner 22(R) together with a circulating liquid 236 (in this embodiment, (3)^. A hybrid arrangement 250 as indicated by the dashed line indicates the part. It is optional to occur. In particular, any combination of two or all three materials (fuel, and c〇2 circulating liquid) can be combined in the mixing arrangement 250 prior to introduction into the burner 220. Various embodiments A, it is desirable that the material entering the burner exhibits specific physical characteristics that are desirable for efficient operation of the power generation method. For example, in some embodiments, It is desirable that (in the C 〇 2 circulating liquid (: 〇 2 is introduced into the burner at a defined pressure, and/or temperature. In particular, it is beneficial to the C that is introduced into the burner) 〇 2 ' has a pressure of at least about 8 MPa. In further embodiments, the 被 2 can be introduced into the burner (: 〇 2 can be at least about 1 MPa, at least about 12 MPa, at least about 14 MPa, at least about 1 5 MPa, at least approximately 16 MPa, Less than about 18 MPa, at least about 20 MPa, at least about 22 MPa, at least about 24 MPa, or at least about 25 Mpa. In other embodiments, the pressure can be from about 8 MPa to about 50 MPa, about 12 MPa. Up to about 50 MPa, from about 15 MPa to about 50 MPa, from about 20 MPa to about 50 MPa, from about 22 MPa to about 50 MPa, from about 22 MPa to about 45 MPa, from about 22 MPa to about 40 MPa, from about 25 MPa to about 40 MPa, or approximately 100125736 Form No. A0101 Page 50 of 134 Page 1003441436-0 201213655 25 MPa to approximately 35 MPa. Further, for the C〇2 introduced into the burner, it is beneficial to have a temperature of at least about 200 ° C. In further embodiments, (: 〇 2 may be at least about 250 2, at least about 30 0 2 , at least about 350 2, at least about 400 e, at least About 450 2 , at least about 500 2, at least about 550 Q, at least about 600 2 , at least about 650 2, at least about 700 2, at least about 750 2 , at least about 800 2, at least about 850 Q, or at least about 900 2 Temperature. In some In an embodiment, it is desirable that the fuel introduced into the combustor is provided under specific conditions. For example, in certain embodiments, it is desirable that the carbonaceous fuel is in a The pressure, and/or temperature has been defined to be introduced into the combustor. In some embodiments, the carbonaceous fuel is introduced under conditions that are equal to, or substantially similar to, the conditions of the (2) circulating liquid. In the burner. The term "substantially similar conditions" may mean that a conditional parameter falls within 5%, within 4%, within 3% of the reference condition parameter (eg, the condition parameter of the C〇2 circulating liquid) as recited herein. Within 2%, or within 1%. In certain embodiments, the carbonaceous fuel may be first mixed with the (?2) circulating liquid prior to introduction into the combustor. In such an embodiment, it is contemplated that the carbonaceous fuel and the (: The 〇2 circulating liquid may be in the same, or substantially similar, condition (which may specifically include conditions described in relation to the c〇2 circulating liquid). In other embodiments, the carbonaceous fuel may be cycled with the c〇2 The liquid is separated and introduced into the burner. In such a case, the carbonaceous fuel will still be introduced at a pressure as described in relation to the c〇2 circulating liquid. In some embodiments, it is useful, The carbonaceous fuel is maintained at a different temperature than the (?2) circulating liquid prior to introduction into the burner. For example, the carbonaceous fuel can range from about 30 ° C to a large 100125736 Form No. A0101 Page 51 / A total of 134 pages 1003441436-0 201213655 about 800 t:, about 35 ° C to about 700 ° C 'about 40. <: to about 600 ° C, about 45 ° C to about 500 ° C, about 50. (: to About 400 ° C, about 55 ° C to about 300 t:, about 60 ° C to large 200 ° C, about 65 ° C to about 175 ° C, or about 70. (: to a temperature of about 150 C is introduced into the burner. In other embodiments, desirably, is introduced into the burner The 〇2 疋 is provided under a specific condition. Such a condition may be accompanied by the method of providing 〇 2. For example, it is desirable to provide 02 at a specific pressure. Specifically, the pair is introduced into the For the crucible 2 in the combustor, it is beneficial to have a pressure of at least about 8 MPa. In a further embodiment, the crucible 2 introduced into the combustor can be at a pressure of at least about 1 〇Mpa, at least About 12 MPa, at least about 14 MPa, at least about 15 MPa, at least about 16 MPa, at least about 18 MPa, at least about 2 MPa, at least about 22 MPa, at least about 24 MPa, at least about 25 MPa, at least about 30 MPa. Providing at least about 35 MPa, at least about 4 MPa, at least about 45 MPa, or at least about 50 MPp 〇 2 may comprise using an air separator (or oxygen separator), such as a cryogenic 02 concentrator, -〇2 Transfer separator 'or any similar device For example, 'the ion transport separator used to separate the air from the ambient air. As provided in the foregoing & the <RTI ID=0.0> Heating, in some embodiments, it is desirable that the crucible 2 is at a temperature that is different from the inherent temperature of the pressurized gas. For example, it is desirable to provide (d) to the g2 of the burner. The temperature is about 3Q about _t, about 35 °C to about 800. (:, about 40 r to about 7 〇〇 it, about 100125736 45 ° C to about 600 ° C 'about 5Q 〇 c to about coffee t 'about 1003441436-0 Form No. A0101 Page 52 / Total 134 pages 201213655 Ο 55 From °C to about 400 ° C, about 60 it to about 3 〇〇 it, about 65 ° C to about 250 ° C, or about 70 〇 c to about 2 〇〇. Further, in some embodiments, & can be introduced into the burner under conditions equivalent to, or substantially similar to, the (3) circulating liquid, and/or the carbonaceous fuel. This may result from various components prior to introduction into the burner. Mixing, or may result from a particular method of preparing to introduce the burner. In a particular embodiment, the crucible 2 may be combined with a defined molar ratio of C〇2 to provide a temperature of the crucible 2 It may be the same as the c〇 circulating liquid. For example, when the combustion can be carried out at a temperature lower than 100 r, the C〇2 can be at a supercritical pressure. This eliminates the correlation due to the C〇2 dilution effect. The danger of burning purely 〇2 heating alone. Such a mixture can be large A ratio of CO / 0 of from about 1:2 to about 5:1, from about 1:1 to about 4:1, or from about 1:1 to about 3:1. 2 2 Ο In some embodiments, usefully, supply The crucible 2 to the burner is substantially purified (i.e., elevated in relation to the molar content of other components naturally present in the air). In certain embodiments, the crucible 2 Having a purity greater than about 50% molar, greater than about 60% molar, greater than about 70% molar, greater than about 80% molar, greater than about 85% molar, greater than about 90% molar, greater than about 95% Moth, greater than about 96% Mo, greater than about 97% Mo, greater than about 98% Mo, greater than about 99% Mo, or greater than about 99.5% Mo. In other embodiments, the 〇 2 may have a molar purity of from about 85% to about 99.6%, from about 85% to about 99%, from about 90% to about 99%, from about 90% to about 98%, or from about 90% to about 97. %. All C〇2 recovered from the carbon in the fuel contributes to higher purity in the range of at least about 99.5% Mo. 100125736 The (:〇2 circulating liquid can be at the inlet of the burner with The crucible 2 and the carbonaceous table No. A0101 Page 53 of 134 201213655 Fuel - starting from the conductor. n As described in the previous cooling burner, the c〇2 circulating liquid can also pass through the ^ evapotranspiration cooler - or more The evapotranspiration supply is introduced into the evapotranspiration, and the effluent is ignited by all or part of the evapotranspiration liquid. In some embodiments according to this I, the 液体The burner of the burner of the burner (i.e., together with the crucible 2 and the fuel), and the introduction of the loop liquid may also be introduced into the burner 2 through the evaporative component to make all or part of the burner Evapotranspiration of the cooling liquid. In other embodiments, the circulating liquid may be passed through the transpiration member (4) as a whole or part (4) evapotranspiration cooling (4) (ie, no C and 02 and the fuel is introduced into the burner inlet) . 2 In some embodiments, the invention features a variety of tt rates associated with being introduced into the combustion chamber. In order to achieve the most efficient burning efficiency, it is useful to burn the carbonaceous fuel at a high temperature. However, the temperature of the combustion and the temperature of the combustion product stream leaving the combustor may need to be controlled within defined parameters. To this end, it is useful to provide a special ratio of this (: 〇 2 circulatory liquid) to the fuel so that the combustion temperature, and/or the turbine inlet temperature can be controlled within the desired range, while also maximizing the conversion The amount of energy that is electrical. In a particular embodiment, this can be achieved by adjusting the ratio of the liquid flow to the carbon in the fuel. As described more fully herein, the desired The ratio may be affected by the desired turbine inlet temperature and the temperature difference between the inlet and outlet streams at the hot end of the heat exchanger. This ratio may be specifically recited as being in the (〇2 circulating liquid) The ratio of C〇2 to carbon present in the carbonaceous fuel 'in order to determine the amount of moles of C〇2 introduced into the burner, in some embodiments 100125736 Form No. A0101 Page 54 of 134 In 201213655, the overall c〇2 content supplied to the burner (ie, the fuel and the inlet at the inlet, and any C〇2 used as an esteam cooling liquid) are included in the calculation. However, in a particular embodiment This calculation may be separately introduced based on C0 in the burner inlet 2 Ο

A quantity of 100,125,736 (ie, excluding any c〇2 used as an evapotranspiration cooling liquid). In the embodiment in which c〇2 is introduced into the burner as only one evaporative cooling liquid, the measurement is based on the content of C〇2 introduced into the burner as the evaporative cooling liquid. Thus, the ratio can be described as the molar content of c 〇 2 associated with the input of carbon into the fuel entering the combustor to the burner inlet. Alternatively, the ratio can also be described as the molar content of C 〇 2 that is input to the burner through the chilled cooling liquid through the carbon in the fuel input to the burner. In certain embodiments, the ratio of C 〇 2 circulating liquid to carbon in the fuel introduced into the combustor (on a molar basis) may be from about 10 to about 50 (ie, about 1 mole per carbon pair in the fuel) 10 moles of C0 to about 50 moles of C〇2) per i mole of carbon in the fuel. In a further embodiment, the ratio of c〇2 to carbon in the fuel in the circulating liquid can be from about 15 to about 5, about 20 to about 50, about 25 to about 50, about 30 to about 50. From about 15 to about 45, from about 20 to about 45, from about 25 to about 45, from about 30 to about 45, from about 15 to about 40, from about 20 to about 40, from about 25 to about 40, or from about 30 to about 40. In other embodiments 'the ratio of (〇2 to carbon in the fuel in the circulating liquid may be at least about 5, at least about 10, at least about 15, at least about 2, at least about 25, or at least about 30. The ratio of c〇2 introduced into the burner to the molar ratio of carbon present in the carbonaceous fuel can have an important impact on the thermal efficiency of the overall system. This is the effect of the form A0101, page 55 of 134 The impact of the 201213655 rate was also impacted by the design and function of further parts of the system, including heat exchangers, water separation ~ «and pressurizing units. The combination of the various components of the systems and methods described herein resulted in the banknotes The ability of the special CO/c ratio to have high thermal efficiency. The systems and methods previously described that do not include the various elements described herein typically would require a c〇2/c molar ratio that would be significantly lower than in the present invention. The (3) 2/c molar ratio is used to achieve efficiencies similar to those described herein. However, the present invention has identified an efficient system and method for recovering C〇2 that far exceeds that of the prior art. C〇2/C molar ratio Use is feasible. A further advantage of the use of the high C〇2/C# molar ratio according to the present invention is the dilution of impurities in the combustion stream. Corrosion or erosion effects of impurities (eg, vapors and sulfur) on system parts It can therefore be greatly reduced. Today, high-chlorine, and/or still-sulphur coal cannot be used in known systems because of the combustion products from such coals (which include HC1 and H/0) for power plant parts. Corrosion and erosion are too large to withstand. Many other impurities (for example, solid ash particles and volatile materials containing components such as lead, iodine, antimony, and mercury #) can also cause serious internal damage to power generation parts at high temperatures. The dilution effect of recycling C〇2 can greatly improve, or eliminate, the harmful effects of such impurities on power plant components. Next, the choice of c〇2/c molar ratio can involve complex considerations regarding efficiency and plant The effects of parts erosion and corrosion, as well as the design of the parts and functions of the c〇2 recycling system. The present invention is not accompanied by conventional techniques. In the case of high thermal efficiency, 'Efficient recovery of c〇2, and thus increased CO/c molar ratio is feasible. The high c〇/c molar ratio thus conveys at least the advantages described first. Similarly, usefully Is to control the amount of cesium that is introduced into the burner. 100125736 Form nickname A0101 Page 56 of 1 134 Page 2 ι〇〇3441436-〇201213655

This may depend in particular on the operational nature of the burner. As described more fully herein, the method and system of the present invention may allow for a full oxidation mode, a full reduction mode, or both. In the fully oxidized mode, the amount of ruthenium 2 provided to the burner is preferably at least the stoichiometric amount necessary to achieve complete oxidation of the carbonaceous fuel. In some embodiments, the amount of 〇2 provided may exceed at least about 01% mole of the stoichiometric amount, at least about 0.25% Moir' at least about 5. 5 % mole, at least about 1% molar, at least about 2% molar, at least about 3% molar, at least about 4% molar, or at least about 5% molar, in other embodiments 'the amount of 〇2 provided may exceed A stoichiometric amount of from about 1% by mole to about 5% by mole, from about 25% by mole to about 4% by mole, or from about 5% by mole to about 3% by mole. In the full reduction mode, the amount of helium 2 supplied to the burner is preferably converted to a component of the carbonaceous fuel!] CO, CH Z 4

The stoichiometric amount necessary for H2S, and NH3 plus at least about 0.1% Mo, at least about 0.25% Mo, at least about 〇. 5% Mo, at least about 1% Mo, at least about 2% Mohr, at least about 3% molar, at least about 4% molar, or at least about 5% molar excess. The amount of 02 provided in other embodiments may exceed the mentioned stoichiometry from about 0.1% molar to about 5% molar, about 0.25% molar to about 4% molar, or about 0. 5% mol to about 3% Mo in some embodiments 'The method of the invention is characterized by a physical state of C (^) from the beginning to the end of each step in the process. c〇2 may depend on The material condition of the material is recognized as being present in various states. C〇 has a triple point at 2 〇. 518 MPa and 56.6 °C, but (: 〇2 also has a critical pressure at 7.38 MPa and 31.1 C And the temperature. After crossing this critical point, 'c〇2 exists as a supercritical liquid, and the present invention has been implemented by 100125736 Form No. A0101 Page 57/134 Page 1043441436-0 201213655 At a special point in % Keeping % in a special state to maximize the power of the power generation. In a particular embodiment, the (3) introduced into the burner is preferably in the form of a supercritical liquid. 2 ^ Also for power generation systems or methods The understanding of efficiency lies in the monthly output and input system or method of the narrative system or method. Ratio of energy between methods In the case of a power generation system or method, efficiency is often described as the power or power output to the burner grid (eg, megawatts or

Mw) The ratio between the total l发热wer heating value thermal en_ergy of the fuel that is burned to produce electricity (or power). This ratio is then referred to as the net system or method efficiency (based on LHV). This efficiency may take into account all of the energy required for internal system or method processing, including the production of purified oxygen (eg, via an air separation unit), pressurization to deliver co2 to a C〇2 pressurized line, and energy required. Other system or method conditions entered. In various embodiments, the system and method of the present invention utilizes c〇 primarily as a working fluid in a cycle in which a carbonaceous fuel is substantially pure at a pressure exceeding a critical pressure of c〇2. Combustion (i.e., in a combustor) is carried out in crucible 2 to produce a combustion product stream. This stream expands across the first/nine round and then passes through a recuperator heat exchanger. In the heat exchanger, the turbine discharges a recovery (: 〇 2 circulating liquid) that is preheated in a supercritical state. The preheated, recovered c 〇 2 circulating liquid is introduced into the burner. In the burner And mixing with the product from the combustion of the carbonaceous fuel to provide a total flow at a defined maximum thirst inlet temperature, as it is confirmed that the temperature difference at the hot end of the complex heat exchanger is minimized. The advantages of the present invention, therefore, at least partially provide excellent efficiency. This minimization can be achieved by using a low temperature level heat source prior to introduction into the burner by 100125736 Form No. A0101 Page 58 / Total 134 Page 1003441436-0 201213655 Heat recovery of part c. At these low temperature levels, the specific heat of the supercritical c〇2 and the twist are very positive, and this additional heating allows the turbine to flow out the p Λ

100125736 2 preheats to a much higher temperature, and this can significantly reduce the temperature difference at the hot end of the helium complex heat exchanger. The useful low heat source in certain embodiments is used in thermal insulation operations. An air compressor in a cryogenic air separation plant' or a hot exhaust stream from a conventional gas turbine. In a particular embodiment of the invention, the temperature difference at the hot end of the multiple heat exchanger can be less than about 50. (:, and preferably falls within the range of about 10 ° C to about 30 ° C. The use of a low pressure ratio (eg, less than about 1 2 ) is a further factor that can increase efficiency. The coupled c〇2 is used as a working fluid to reduce energy consumption when the pressure discharged from the cooling turbine is raised to the recovery pressure. A further advantage is that a very small additional parasitic power source is used with nearly 100% carbon capture from the fuel. Consumption of a high pressure liquid that is converted to c〇2t-quantitative in the fuel (: 〇2 is produced as a supercritical pressure (typically, about 1 MPa to about 20 MPa) above C管路2 of the line pressure) The system and method parameters are further described in more detail herein. Returning to Figure 5, the carbonaceous fuel introduced into the burner 220 along with the crucible 2242 and the (2) circulating liquid 254 is combusted to provide a combustion product stream. In a particular embodiment, such as previously described, the burner 220 is an evapotranspiration burner. The combustion temperature may vary depending on particular processing parameters, for example, The type of carbonaceous fuel used, such as the fuel introduced into the burner (the Mohr ratio of 〇2 to carbon, and/or the Mohr ratio of 0〇2 and 〇2 introduced into the burner. In the embodiment, as described above, the combustion temperature is described in relation to the transpiration-cooling burner. Form No. A0101, page 59 / 134, 1 〇〇 201213655, in a particularly preferred embodiment As described herein, a combustion temperature in excess of about ° C is advantageous. It is also useful to control the combustion temperature such that the fuel I product exiting the burner has a desired temperature. For example, useful Yes, the combustion product stream exiting the combustor has a temperature of at least about 7 Torr, to about 750. 〇 at least about 800. 〇 at least about 850 ° C, at least about 900 ° C, at least about 950 ° C. At least about 1000 C, at least about 1〇5〇.^, at least about 11〇〇.匚, at least about 1200 °C, at least about 1300 fly, at least about 1400 «C, at least about 1,500. (:, or at least Approximately 16 〇〇〇 c. In some embodiments The combustion product stream can have a temperature of from about 7 〇〇t to about 丨, 6 〇{) C, from about 800 ° C to about 1,6 〇〇. (:, about 850 t to about 1,500 C, approximately 900 ° C to about 1,400 t, about 950 ° C to about 1,350 ° C, or about looo °c to about 1300 ° C. As mentioned above, the pressure of the c〇 can be 2 during the entire power generation cycle It is a key parameter to maximize power cycle efficiency. While it is important to have a specifically defined pressure for the material introduced into the burner, it is equally important to have a defined pressure for the combustion product stream. In particular, the pressure of the combustion product stream can be related to the pressure of the C〇2 circulating liquid introduced into the combustor. In a particular embodiment, the pressure of the combustion stream can be at least about 90% of the pressure of the CO 2 introduced into the burner, i.e., in the circulating liquid. In a further embodiment, the pressure of the combustion product stream can be at least about 91%, at least about 92%, at least about 93%, at least about 94%, at least about 95 of the pressure of c〇2 introduced into the combustor. %, at least about 96%, at least about 97%, at least about 98% 'or at least about 99%. 100125736 Form No. A0101 Page 60 of 134 1003441436-0 201213655 The chemical replenishment of the combustor product stream exiting the combustor may vary depending on the type of carbonaceous fuel used. Importantly, the combustion product stream will include c〇2 that is recovered and reintroduced into the burner or further cycle. Furthermore, an excess of c〇2 (including c〇2 produced by the combustion of the fuel) may be taken from other treatments used for sequestration or not including release to the atmosphere (: 〇2 circulating liquid (especially in a suitable direct Passed to a pressure of a c〇2 line. In a further embodiment, the combustion product stream may include water vapor, S〇2, S〇3, HCI, NO, N〇2.

Hg 'excess 〇 2, N 2 , Ar, and one or more of the possible other contaminants present in the fuel being burned. Unless removed (e.g., by the treatments described herein), the materials present in the combustion product stream may continue in the c〇2 circulating liquid stream. Such a material with the appearance of C 0 2 may be referred to herein as a "subordinate component." As can be seen in Figure 5, the combustion product stream 40 can be directed to a turbine 320 where the combustion product stream 40 expands to produce a power source (e.g., via a generator to generate electricity, which is not shown in the legend). ). The turbine 320 can have an inlet to receive the combustion product stream 40 and an outlet to release a turbine discharge stream 50 comprising C〇2. Although a single turbine 320 is shown in FIG. 5, it will be appreciated that more than one turbine may be used, multiple turbines may be connected in series, or alternatively separated by one or more further parts. For example, a further burning part, a compression part, a separator part, or the like. Again, processing parameters can be tightly controlled in this step to maximize cycle efficiency. The efficiency of current natural gas power plants is critically dependent on the turbine inlet temperature. For example, extensive work has been carried out at a significant cost to achieve a turbine technology that allows an inlet temperature of up to approximately 1,350 °C. 100125736 Form No. A0101 Page 61 of 134 Page 1003441436-0 201213655. The higher the temperature at the entrance to the thirsty wheel, the higher the efficiency of power generation waste, but the more expensive the thirsty wheel, and potentially the shorter the shot edge. Some companies are afraid to pay higher prices and have a short period of validity. Although in some embodiments the invention may utilize such a turbine to further increase efficiency ', this is not required. In a particular embodiment, the system and method of the present invention achieves the desired efficiency while producing a turbine population temperature that is at a much lower temperature range. Thus, the features of the present invention can be achieved as described above - a specific efficiency while providing a combustion product stream to a turbine σ at a defined temperature (as described herein) which can be significantly smaller than conventional techniques The temperature required to achieve the same efficiency with the same fuel. As previously mentioned, the combustion product stream 4's exiting the combustor 220 preferably has a pressure that closely matches the pressure of the c2 circulating fluid 236 entering the combustor 22''. Thus, in a particular embodiment 2, the temperature and pressure of the combustion stream 40 is such that the (3)^ present in the stream is in a supercritical liquid state. As the combustion product stream expands across the turbine 32, the pressure of the stream is reduced. Preferably, the pressure drop is controlled such that the pressure of the combustion product stream 40 is at a depreciated ratio to the pressure of the turbine discharge stream 5〇. In certain embodiments, the ratio of the 6 Hz combustion product stream at the inlet of the turbine to the turbine effluent stream at the outlet of the turbine is less than about 12 ^. This can be defined as the inlet pressure. (Ip) to π pressure (〇p) ratio (ie, /(^). In other embodiments, the pressure ratio may be less than about 丨丨, less than about 1 〇, less than about 9, less At about 8, or less than about 7. In other embodiments, the inlet pressure to outlet pressure ratio at the turbine can be from about 15 to about 12, from about 2 to about 12, from about 3 to about 12, about 4 to 100125736 Form Number Α 0101 Page 62 / Total 134 Page 1003441436-0 201213655 About 12, about 2 to about 11, about 2 to about ι, about 2 to about 9, about 2 to about 8, about 3 to about 11 About 3 to about 1 Torr, about 3 to about 9, about 3 to about 8, about 4 to about π, about 4 to about 10, about 4 to about 9, or about 4 to about 8.

In a particular embodiment, it is desirable that the turbine discharge stream be at a condition such that c 〇 2 in the flow is no longer in a supercritical liquid state but in a gaseous state. For example, providing a gaseous state can help remove any dependent components. In some embodiments, the turbine discharge stream has a pressure that is lower than the pressure at which C〇2 can be in a supercritical state. Preferably, the turbine discharge stream has a pressure of less than about 7.3 MPa, less than or equal to about 7 MPa, less than or equal to about 6.5 MPa, less than or equal to about 6 MPa, less than or 5 MPa。 Less than or equal to about 4.5 MPa, less than or equal to about 4 MPa, less than or equal to about 3. 5 MPa, less than or equal to about 3 MPa. Less than or equal to about 2.5 MPa, less than or equal to about 2 MPa, or less than or equal to about is MPa, in other embodiments,

G The full wheel discharge stream may have a pressure of from about 1.5 MPa to about 7 MPa, from about 3 MPa to about 7 MPa or from about 4 MPa to about 7 MPa. Preferably, the pressure of the turbine discharge stream is less than c〇 when the cooling temperature of the stream is encountered.

The condensing pressure of U (e.g., ambient cooling), therefore, in accordance with the present invention, C 〇 2 downstream of the turbine 320 (and, preferably, C 〇 2 upstream of the pressurizing unit 620) is maintained. In the gaseous state, conditions that can form liquid CO are not allowed to be reached. L. While the combustion product stream passing through the turbine may cause some temperature reduction' but the wheel discharge stream will typically have a temperature that prevents removal of any subordinate components that are present in the combustion stream. For example, the vortex 100125736 Form No. A0101 Page 63 / Total 134 Page 1003441436-0 201213655 The wheel discharge stream can have a temperature of from about 500 ° C to about 1 000 ° C 'about 600 ° C to about 1 000 ° C, about 700. (: to about 1000 ° C, or about 800 ° C to about 1 000 ° C. Because of the relatively high temperature of the combustion product stream, it is beneficial that the material used to form the turbine can withstand such temperatures. It may also be useful that the turbine includes a material that provides good chemical resistance to the pattern of dependent materials present in the combustion product stream. Thus, in some embodiments, usefully, the turbine discharge stream 5 〇 passing through at least one heat exchanger 420, which cools the turbine discharge stream 5 〇 and provides a C 〇 circulating liquid stream 60 having a temperature falling within a defined range, L· in a particular embodiment, leaving the heat exchange The CO/shield ring liquid 60 of the 420 (or the last heat exchanger in series when two or more heat exchangers are used) has a temperature of less than about 2 ,, less than about 150 °. C, less than about 125 ° C, less than about 1 ° C, less than about 95 ° C, less than about 90 ° C, less than about 85 t, less than about 80 ° C, less than about 75 ° C, less than about 70 ° C, less than about 65 ° C 'less than about 60 ° C Less than about 5 5 ° C, less than about 50. 〇, less than about 45 ° C, or less than about 40 t: As mentioned in the face, it is beneficial that the pressure of the turbine discharges and the combustion The pressure of the product stream has a specific ratio. In a particular embodiment, the thirsty wheel discharge stream will pass through one or more of the heat exchanges described herein without passing through any additional parts of the system. Thus, the pressure ratio can also be described as the pressure at which the combustion product stream exits the burner as compared to the hot end of the stream entering the heat exchanger (or the first heat when using a series heat exchanger) The ratio of the pressure at the time of the exchanger. Again 'this pressure is better than less than about 12, in the other implementation 100125736 1003441436-0 Form No. A0101 Page 64 / Total 134 pages 201213655 Order 'The combustion product flow and entry The inter-flow pressure ratio of the heat exchanger can be less than about 11, less than about 10, less than about 9, less than about 8, or less than about 7'. In other embodiments, the pressure ratio can be about 1. 5 to about 1 〇 'about 2 to large 9, from about 2 to about 8, from about 3 to about 8 'or from about 4 to about 8.

While the use of an evapotranial cooling burner allows for high heat combustion, the system and method of the present invention is characterized by the ability to provide a turbine exhaust stream to a temperature that is sufficiently low to reduce the cost associated with the system, increasing the Heat exchangers, as well as heat exchangers that improve the efficiency and stability of the system. In a particular embodiment, the heat exchanger has a hottest operating temperature of less than about Ο 1,100 ° C, less than about 1, 〇〇〇 in the system or method according to the present invention. Oh, less than about 975. (:, less than about 950 ° C, less than about 925. (:, or less than about 900 ° C. In certain embodiments, it is particularly useful that the heat exchanger 42 includes at least one in series A heat exchanger to receive the full wheel discharge stream 5 〇 and to cool it to a desired temperature, the type of heat exchanger used may vary depending on the conditions of the stream entering the heat exchanger. The turbine discharge stream 50 can be at a relatively high temperature, as described above, and, therefore, usefully, the heat exchanger designed to withstand harsh conditions is Turbine discharge stream 5 举例 ^ For example, the first heat exchanger in the heat exchanger train may comprise an IN_CONEL alloy or similar material. Preferably, the first heat exchange in the series connection The material included is capable of continuously withstanding an operating temperature of at least about 700 ° C 'at least about 750 t, at least about 800, at least about 850 ° C 'at least about 900. (:, at least about 95 〇. (:, to 100125736 Less than 1 000 °C 'at least about 1 1〇〇乞, or at least approximately form number A0101, page 65 / 134 pages 1003441436-0 201213655 1,200 ° C. It is also useful that one or more of the heat exchangers are included in the combustion The material of the subordinate material in the stream is a chemically resistant material, INCONEL® alloy is available from Special Metals Corporation, and some embodiments may include austenitic nickel-chromium-based alloys, which may be used. Examples of alloys include INCONEL'OO, INC0NEL®6 (H, INCONEL® 601GC, INCONEL® 603C〇9I, INCONEL® 617, INCONEL® 625, INCONEL® 625LCF, IN-CONEL® 686, INCONEL® 690, INC0NEL® 693 , INCONEL® 706 , INC0NEL®718 , INC0NEL®718SPFTM , INCONEL® 722, INCONEL®725, INCONEL® 740, INCONEL® C〇2-750, INC0NEL®751 , INC0NEL®MA754 , INCONEL® MA758 , INC0NEL®783 , INCONEL®903 , INCONEL® N06230 , INC0NEL®C-276 , INC0NEL®G-3 , INCONEL® HC〇2, INCONEL®22. An example of an advantageous heat exchanger design is a diffusion bonded compact plate heat exchanger made of a high temperature material with chemically ground fins in the plate. Suitable heat exchangers can be included under the trade name HEAT-RIC® (available from Meggitt USA, Houston, TC 〇 2). Preferably, the first of the series exchangers is sufficient to transfer heat from the turbine discharge stream such that one or more other exchangers present in the series exchanger may be made of more conventional materials. For example, stainless steel, in a particular embodiment, at least two heat exchangers, or at least three heat exchangers, are used in series to cool the turbine discharge stream to a desired temperature. In particular, the use of multiple heat exchangers in series can be used in the next 100125736 Form No. A0101 Page 66 / Total 134 pages 1003441436-0 201213655 Regarding the transfer of heat from the turbine discharge stream to the c〇2 circulating liquid It is seen in the description that the circulating liquid is reheated before being introduced into the burner.

In some embodiments, the method and system are characterized in that they can be a staged combustion method or system. This can be achieved by using a high efficiency burner, such as the aforementioned transpiration cooling burner. It is essential that the dip can be substantially completely combusted in the separate combustor such that it is not necessary to provide a combustor in series to completely combust the fuel. Accordingly, in some embodiments, the method and system of the present invention can be described as the sole burner of the evapotranspiration burner. In further embodiments, the methods and systems can be described as passing the effluent stream into the heat exchanger, the combustion occurring only in the separate evapotranial cooling combustor. In still other embodiments, the method and method can be described as the turbine exhaust stream passing directly into the heat exchanger without passing through another burner. , ...

100125736 After cooling, the c〇2 circulating liquid stream exiting the at least one heat exchanger may undergo further processing to separate any subordinates remaining in the C〇2 circulating liquid stream 60 from the combustion of the fuel. Ingredients. As shown in Figure 5, the C〇2 circulating liquid stream 60 can be directed to one or more separation units 520. As will be discussed in more detail later, in particular, the present invention features the ability to provide an efficient power generation method utilizing combustion of a carbonaceous fuel without releasing c〇2 to the atmosphere, which may be at least partially formed by The CO in combustion of a carbon-containing fuel is achieved as a circulating liquid in a power generation cycle. In some embodiments, although continuous combustion and recovery of C〇2 as the circulating liquid may cause accumulation of c〇2 in the system, in such cases, it is useful to abandon at least part of the form from the 1003441436-0 No. A0101, page 67 of 134, with 201213655 circulating liquid c〇2 (for example, the amount is approximately equal to the (:~ amount) derived from the combustion of the carbonaceous fuel' so the % waived by any suitable The method is carried out. In a particular embodiment, the c〇2 can be directed to a line that is sealed or disposed of in an appropriate manner, as described below. The required (: 〇 2 piping system specification is that When c〇2 enters the pipeline, water is generally not needed to avoid eroding the carbon steel used in the pipeline, although the wet ''c〇2 can be directly introduced into the stainless steel c〇2 pipeline, but not always In fact, based on cost considerations, it may be more desirable to use a carbon steel pipe. According to this, in certain embodiments, water present in the co2 circulating liquid (eg, formed during combustion of the carbonaceous fuel, and Maintain burning The product stream, the thirsty wheel discharge stream, and the water in the CO 2 recycle liquid stream may be largely removed as a liquid '4 phase from the cooled (3) helium circulating liquid machine, in a particular embodiment By providing a 匸〇2 circulating liquid at a pressure lower than the pressure point at which c〇2 occurs in the gas phase mixture when the gas phase mixture is cooled to the lowest temperature by the ambient temperature cooling method (for example) , in a gaseous state, for example, in particular, the C〇2 circulating liquid can be supplied at a pressure of less than 7.38 MPa during the separation of the subordinate components. If a low ambient temperature range is used, or substantially At lower temperatures than ambient temperatures, even lower pressures may be required. This allows water to be separated in liquid form and, to minimize, the purified (3) fading contaminants leaving the separation unit, This may also limit the turbine discharge pressure to at least the value of the critical pressure of the turbine exhaust gas. The true magical power may depend on the temperature at which the ambient cooling mode is available. For example, if the water is separated At (10) τ, a pressure of 7 MPa allows a limit of 〇 38 Mpa for the C 〇 2 condensing pressure. In some embodiments, leaving the heat exchanger and entering the separation unit 100125736 Form No. A0101 Page 68 of 134 Page 1003441436-0 201213655 忒C〇2 circulating liquid can be supplied at a pressure of about 2 Mpa to about 7 MPa ' 2. 25 MPa to about 7 MPa, 2. 5 MPa to about 7 Mpa, 75 MPa to about 7 MPa , 3 MPa to about 7 MPa, 3.5 MPa to about 7 MPa, 4 MPa to about 7 MPa, or 4 MPa to about 6. In another embodiment, the pressure may be substantially the same as the pressure at the turbine outlet.

In a particular embodiment, the purified c〇2 recycle stream 65 after separation of water, which does not include water vapor, or substantially does not include water vapor. In some embodiments, the purified (: 〇 2 recycle stream is characterized by a water vapor comprising less than 1.5% under the Mohr base, less than 125% under the Mohr base, less than Mohr 1% under the foundation, less than 9% under the Mohr foundation, less than 0.8% under the Mohr base, less than the 〇.7% under the Mohr foundation, less than the 莫. 5% under 莫. 5%, less than 莫. 4% under Mohr's foundation, less than 〇 under 莫. 3%, less than 莫 under Mohr.

‘or less than 莫. 1% under Mohr’s foundation. In some embodiments, the amount of water vapor included in the purified C〇2 circulating liquid stream may be only about G.Q1% to Dashe 5% under the Mohr basis, and the large shape m to about Mohr. 1%, about 〇.〇1% to about 〇75% under the Mohr base, about Gm to about 〇.5% under the Mohr base, and 1% to about 〇25% under the Mohr base. 'About U5% to about 〇.5% under Mohr's base, or about 0. 05% to about 〇. 25% under Mohr's base. 100125736 may be superior in that it provides 'c〇2 a viewant' at the above defined temperature and pressure conditions to aid in the subordinate composition (eg, a magical separation of the circulating liquid to provide for maintaining the C0 under the desired conditions). = 2 Circulating Fluid Zhao Zhong C 〇 2 and water in separation :::: Help ?:: state, provide - ^ Page 69 / Total 134 pages of 1003441436-0 201213655 This (: 〇 2 circulating liquid, the The temperature of the liquid stream can be lowered to a point where the water in the stream will be in a liquid state and thus more readily separated from the gaseous C〇2. In certain embodiments, it is desirable to provide further drying. The conditions are such that the purified C〇2 circulating liquid can be completely, or substantially anhydrous, as previously mentioned, water may be separated from the C〇2 circulating liquid depending on the phase in the material (: A small portion (i.e., low concentration) of water is left in the 循环2 circulating liquid. In some embodiments, it is acceptable to have the C〇2 circulating liquid continue to have a small portion of water remaining therein. In other implementations In an example, it is useful to make the C〇2 circulating fluid Further processing is performed to help remove all or part of the remaining water. For example, low concentrations of water may be by a desiccant dryer or other means suitable in accordance with the disclosure herein. In particular, providing this at a defined pressure (: 〇 2 circulating liquid to the separate units may help to maximize the efficiency of the power cycle again. Specifically, providing the defined pressure range (: 〇 2 circulating liquid can cause the purified c 〇 2 circulating liquid in the gas phase to be compressed to a high pressure with a minimum total power consumption. As previously described, such pressurization is required to make part of The purified (: 〇 2 circulating liquid is recovered to the burner and is partially supplied at the required line pressure (eg, from about 10 MPa to about 20 MPa). This further clarifies that the inlet of the diffusion turbine is minimized. The benefit of the ratio to the outlet pressure, as mentioned above. This effect increases the overall cycle efficiency and also allows the discharge pressure from the turbine to fall within the aforementioned range for use in The C〇2 separating the circulating liquid water, and other ingredients slave The circulating liquid C〇2 Form Number 100125736 elucidated by way of example a flow separation unit 520 A0101 page 70/134 Total 201 213 655 1003441436-0

Figure 6 Figure 1 ί7. As can be seen, the c〇2 circulating liquid stream 60 from the heat exchanger can be further removed from the C〇2 circulating liquid 6〇 by using water to further remove the hot cold water heat father 530 (or any similar function). The apparatus), and the C〇2 circulating liquid 61 discharging the mixed phase, wherein the c〇 is maintained as a gas, and the water in the c〇2 circulating liquid has been converted into a liquid phase. For example, the C〇2 circulating liquid 60 can be cooled by the cold water heat exchanger 53 to a temperature of less than about 50 ° C, less than about 55 t, less than about 40 ° C, less than about 50 ° C. About 45 t, less than about 4 〇. (:, or less than about 30 ° C. Preferably, the pressure of the C 〇 2 circulating liquid is substantially not changed by the cold water heat exchanger 530. The c 〇 circulating liquid 61 of the mixed phase is directed to a water Separation unit 540, wherein liquid water stream 62a is discharged from the separator 520. Also, leaving the water separation unit "o is an enriched C02 circulating liquid stream 62b, which may exit the separator 520 directly, As a purified C〇2 circulating liquid stream 65. In an alternative embodiment (as indicated by the dotted line)

And as illustrated by the part, the carbon dioxide rich recycle liquid stream 62b can be directed to one or more additional separation units 55A to remove more subordinate components, as described more fully below. In a particular embodiment, any more subordinate components of the c〇2 circulating liquid can be removed after removal of the water. Next, the c〇2 circulating liquid leaves the one or more additional separator units as the purified CO 2 circulating liquid 65. However, in some embodiments, the mixed phase C〇2 circulating liquid 61 may be first directed to remove one or more dependent components prior to removal of water, and the partially purified stream may then be directed to the The water is separated by 4Q. It will be appreciated that those skilled in the art disclosed herein will be able to imagine various combinations of separators as desired, and all such combinations are incorporated in the present invention by 100125736 1003441436-0 Form No. A0101 Page 71 of 134 pages 201213655 As mentioned previously, in addition to water, the c〇2 circulating liquid may also contain other subordinate components, such as fuel-derived, combustion-derived, and oxygen-derived impurities, such subordinate components may also be And when the moisture is separated, it is removed from the cooled, gas phase (: 〇 2 circulating liquid. For the four columns, in addition to water II · gas, such as S09, S0q, HCI, NO, N〇 2. The subordinate components of Hg and excess 〇2, N2 and Ar may also be removed. These subordinate components of the c〇2 circulating liquid (usually considered as impurities or contaminants) may be extracted from the appropriate method. The cooling c〇2 circulating liquid is completely removed (for example, the method defined in US Patent Application Publication No. 2008/02265 No. 5 and European Patent Application No. EP 1 952 874 and EP 1 953 486, the entire This is incorporated herein by reference.) While S09 and 801 can be 100% converted to sulfuric acid, >95% of NO and rib 2 can be converted to nitric acid. Any excess in this (:〇2 circulating liquid) The oxygen can be separated as an oxygen-rich stream for selective recovery to the burner. Any inert gases present (e.g., N2 and Ar) can be vented to the atmosphere at low pressure, in some embodiments, The 〇2 circulating liquid can thus be purified such that c 〇 2 derived from the carbon in the fuel for combustion can be ultimately delivered in a high density, purified stream. In a particular embodiment, the purified c 液体The 循环 液体 包括 2 2 2 2 2 2 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 2 Circulating liquid can be supplied at the desired pressure to be directly fed into a C〇2 line, for example, at least about 10 MPa, at least about 15 MPa, or at least about 20 MPa. As a summary of the foregoing, the carbonaceous fuel 254 in the presence of helium 2242 and a C〇2 circulating liquid 236 in an evapotranspiration burner The combustion can be formed into 100125736 Form No. A0101 Page 72 / Total 134 Page 1003441436-0 201213655 Ο A combustion product flow with a relatively high temperature and pressure is 4〇. This includes the combustion of the relatively large amount of C〇2 The stream 4 can be passed through a turbine 320 to expand the combustion product stream 40, thereby reducing the pressure of the stream and generating electricity. The turbine discharge stream 5Q exiting the turbine 320 is at a reduced pressure but still at Relatively high temperature. Due to the contaminants and impurities in the combustion product stream, it is beneficial to separate such contaminants as well as impurities prior to recycling the c〇2 recycle liquid to the human system. To achieve this separation, the turbine discharge stream 5Q is cooled by passing the one or more heats. Separation of the product (e. g., water and any other contaminants as well as impurities) can be achieved. As described above, in order to recover the (3), the ring liquid is returned to the burner and the C02 circulating liquid must be reheated by reheating. In a certain embodiment, the invention is characterized in that, while performing a special processing step - to maximize the efficiency of the power generation cycle, it also avoids the emission of pollution, such as CO 2 ), to the atmosphere. The cooled and purified CO of the single crucible, the reheating of the liquid liquid Zhao and the re-heating

The purified C〇2 circulating liquid 65 leaving the - or more separation units 520 may be added by _ or more pressure units 62G (eg, 'pumps, compressors, or the like). C〇2 The pressure of the circulating liquid 65. In some embodiments, the purified recycle liquid 65 can be compressed to at least about 7.5. The pressure of about 8 MPa. In some embodiments, a separate large is used to increase the pressure of the purified c〇2 circulating liquid to the force required to introduce the burner 220 at *. Extending 100125736 Form Α Α 0101 Page 73 / 134 pages. λα απι m — - 1〇〇3441436~〇201213655 In a special embodiment, 'pressurization can be used in series in the pressurizing unit 62〇 Two or more compressors (eg, pumps) are implemented. One such embodiment is not shown in Figure 7, wherein the purified c〇2 circulating liquid 65 is passed through a first compressor 63 to compress the purified circulating liquid 65 to a first pressure (which is Preferably, the critical pressure is above (3) ,, and thus the stream 66 is formed. Stream 66 can be directed to recoverable heat (e.g., heat formed by the pressurization of the first compressor) and thus a cooling water heat exchanger 64() that forms stream 67, preferably in proximity to the environment. At temperature. Stream 67 can be directed to a second compressor 65A that is used to pressurize the c〇2 circulating liquid to a second pressure greater than the first pressure. As previously mentioned, the second pressure can be substantially similar to the pressure required to input (or retract) the c〇2 circulating liquid to the burner. In a particular embodiment, the first compressor 63 can be used to increase the pressure of the purified (?2) circulating liquid 65 such that the purified c〇2 circulating liquid can be converted from a gaseous state to a supercritical 5 MPa至约15。 The singularity of the singularity of the singularity of the singly MPa, from about 7.5 MPa to about 12 MPa, from about 7.5 MPa to about 1 MPa, or from about 8 MPa to about 1 MPa. Then, the stream 66 exiting the first compressor 630 (which is in the super Critical liquid state) by cooling the (:〇2 circulating liquid to a temperature sufficient to form a high-density liquid that can be pumped more efficiently to even higher pressures. Similar to the effect of the device.) According to the large volume of c〇2 used as the circulating liquid, it is important to pump the large volume of co2 in the superfluid state, which is important in the system. Energy harvesting, however, the present invention can be achieved by densifying 100125736 Form No. A0101 Page 74 of 134 Page 1003441436-0 201213655 C〇2 and therefore the superior efficiency provided by reducing the total volume of supercritical C〇2 (which is pumped back to the burner for recovery) Increased. In a particular embodiment, after being discharged from the chilled water heat exchanger 640 (and

The C09 circulating liquid can provide a density of at least about 200 kg/m3, at least about 250 kg/m3, at least about 300 kg/m3, at least about 350 kg/m3, prior to passing through the heat exchange unit 420. At least about 400 kg/m3, at least about 450 kg/m3, at least about 500 kg/m3, at least about 550 kg/m3, at least about 600 kg/m3, at least about 650 kg/m3, at least about 700 kg/m3, at least Approximately 750 kg/m3, at least approximately 800 kg/m3, at least approximately 850 kg/m3, at least approximately 900 kg/m3, at least approximately 950 kg/m3, or at least approximately 1000 kg/m. In further embodiments, the density may range from about 150 kg/m3 to about 1,100 kg/m3, from about 200 kg/m3 to about 1,000 kg/m, from about 400 kg/m3 to about 950 kg/m3. , from about 500 kg/m3 to about 900 kg/m3, or from about 500 kg/m3 to about 800 kg/m3.

In a particular embodiment, the stream 66 can be cooled by the chilled water heat exchanger 640 to a temperature of less than about 6 Torr, less than about 50 ° C, less than about 40 Torr, or Less than about 30 ° C. In other embodiments, the temperature of the C 〇 2 circulating liquid leaving the chilled water heat exchanger 640 to stream 67 may range from about 15 ° C to about 5 ° C, about 2 (TC). Up to about 45 ° C ' or about 2 ° C to about 4 (TC. Preferably, the C 〇 2 circulating liquid in the stream 67 entering the second compressor 650 is in a condition that contributes to energy efficiency. 'The pump is pumped to the desired pressure to introduce the c〇2 circulating liquid into the burner. For example, the pressurized, supercritical (3) circulating fluid 2 stream 70 can be further pressurized to pressure At least about 12 Mpa, to 100125736 Form No. A0101, page 75, 134, 1003441436-0 201213655, less than about 15 MPa, at least about 16 MPa, at least about 18 MPa, at least about 20 MPa, or at least about 25 MPa. In some embodiments, the pressurized supercritical C〇2 circulating liquid stream 70 can be repressurized to a pressure of approximately 15 MP. a to about 50 MPa, from about 20 MPa to about 45 MPa, or from about 25 MPa to about 40 MPa. Any type of compressor that can operate at the pressures mentioned and that can achieve the pressure can be used, for example, a high pressure multi-stage pump. The pressurized (the 〇2 circulating liquid stream 70 exiting the one or more pressurizing units 620 can be directed back to the heat exchangers previously used to cool the turbine exhaust stream 50 As shown in Figure 5, the pressurized C〇2 circulating liquid stream 70 is first passed through a splitter 720 to form a C〇2 line liquid stream 80 and a C〇2 circulating liquid stream 85 (generally Equal to C 〇 2 circulating liquid stream 70, except for the actual amount of C 〇 2 present in the stream. Thus, in some embodiments, at least one of the pressurized c 〇 2 circulating liquid streams Part (: 〇 2 will be introduced into a pressurized line for storage. From this (: 〇 2 circulating liquid flow removed and directed to the pipeline (or other storage or disposal device) c The amount of 〇2 may vary depending on the desired content of c〇2 introduced into the burner to control The combustion temperature and the true amount of 〇2 present in the combustion effluent stream exiting the burner. In some embodiments, the amount of c 〇 2 recovered, as previously described, may generally be at the burner In the combustion of the carbonaceous fuel formed (: 〇 2 amount. To achieve high efficiency operation, it is helpful that the CO/shield ring liquid leaving the pressurized unit 620 is heated to the supercritical liquid A temperature that is much lower than the heat of the heat. This is equivalent to providing a very large heat input in a relatively low temperature range. Using an external heat source (eg, a relatively low temperature heat source) to provide additional heating for a portion of the recovered C〇2 circulating fluid 100125736 Form No. A0101 Page 76 of 134 pages 1003441436-0 201213655 The heat exchanger unit 42 can be recovered in the turbine discharge stream 50 and at the hot end of the heat exchanger unit 420 (or when using a two or more heat exchangers in series) 〇L· Operates in the case where the temperature difference between the circulating liquid streams 236 is small. In a particular embodiment, the pressurized c〇2 circulating liquid is heated by the one or more heat exchanger pairs to pressurize the pressurized C〇2 circulating liquid stream to the pressurized c〇2 circulating liquid stream It is useful to enter the temperature required for the burner. In certain embodiments, the pressurized C〇2 circulating liquid stream is heated to a temperature of at least about 2 Torr, at least about 300 ° C ' at least before the c 〇 2 circulating liquid stream is fed to the burner. About 4 inches, at least about 5 inches. (:, at least about 600 ° C 'at least about 7 〇〇 t, or at least about 8 ° C. In some embodiments, it can be heated to a temperature of about 5 〇〇 to about 1,200 ° C, about 550 ° C to about 1, 〇〇〇 ° c, or about 6 〇〇 ° c to about 950 〇 C. Ο Figure 8 illustrates an embodiment of a heat exchanger unit 420 in which three individual heat exchangers Used in series to recover heat from the turbine discharge stream 50 to provide a 〇〇2 circulating liquid stream 60' in a condition suitable for removing subordinate components and to simultaneously recover the c〇2 circulating liquid stream 236 and to Heating is introduced to the pressurized, supercritical c〇2 circulating liquid stream 70 (or 85) prior to introduction into the burner. As described further above, the systems and methods of the present invention can be used with conventional power systems (e.g., , a coal-fired power plant) is trimmed to increase efficiency, and/or its output. In some embodiments, the heat exchanger unit 420, as described below, may thus be referred to as primary in such a trim. Heat exchange unit, here also uses a subordinate heat exchange The unit (as illustrated in Figure 12). The secondary heat exchange unit can, for example, be used for overheating (super-100125736 Form No. A0101 Page 77 / Total 134 Page 1003441436-0 201213655 heat) - Steam The use of the terms primary heat exchange unit and the dependent heat exchange unit is not to be construed as limiting the scope of the invention, and only to provide a clear description. The embodiment included in Fig. 8 The turbine exhaust stream 5〇 first enters the heat exchanger series 42〇 through the first heat exchanger 430 to provide a stream 52 that will have a lower temperature than the turbine discharge stream 5〇. When the first hot parent converter 430 receives the hottest stream in the series (ie, the turbine exhaust stream 50) and thus transfers heat in the heat exchanger series 42 落 in the most extreme temperature range, Illustrated as a high temperature heat exchanger. As previously mentioned, the first heat exchanger 430 receiving a relatively higher temperature turbine discharge stream 5 can include a heat exchanger that can be used to adapt the heat exchanger to recover the temperature mentioned. Special alloy Or other materials, the temperature of the turbine discharge stream 5 显 can be significantly reduced by passing through the first heat exchanger 43 (which can also be applied to the use of less than three, or more than three individual heat exchangers) Other embodiments). In certain embodiments, the temperature of the stream 52 from the first heat exchanger 43 may be at least about 100 ° C lower than the temperature of the turbine exhaust stream 5 ,, at least about 200 It is at least about 30 Torr, at least about 400 ° C, at least about 450 t, at least about 500. (:, at least about 550 ° C 'at least about 575 ° C, or at least about 600 t, in a particular embodiment, The temperature of stream 52 can range from about 10 〇〇c to about 8 Torr. (:, about 150 ° C to about 600 ° C, or about 200. (: to about 500 C. In a preferred embodiment, the pressure of the stream 52 exiting the first heat exchanger 43 is substantially similar The pressure of the turbine discharge stream 5 。. In particular, the pressure of the stream 52 exiting the first heat exchanger 430 may be at least 9%, at least 91%, at least 92 压力 of the pressure of the turbine discharge stream 50. /0, at least 93%, at least 94%, at least 95%, at least 96%, at least 97%, 1003441436-0 100125736 Form No. A0101 Page 78 of 134 pages 201213655 At least 98%, at least 99%, at least 99. 5 %, or at least 99.8%. 该 该 the stream 52 leaving the first heat exchanger 430 passes through the second heat exchanger 440' to produce a stream 56 having a temperature less than entering the second heat exchanger The temperature of the stream 52 of 440. When the second heat exchanger 440 transfers heat within an intermediate temperature range (i.e., less than the first heat exchanger 430 but larger than the third heat exchanger 450) , which can be described as an intermediate temperature heat exchanger. In some embodiments, the first stream 52 and the second stream 56 The temperature difference between the two may be substantially less than the temperature difference between the turbine discharge stream 50 and the stream 52 exiting the first heat exchanger 430. In some embodiments, the stream 56 exiting the second heat exchanger 440 The temperature may be about 10 ° C to about 200 ° C lower than the temperature of the stream 52 entering the second heat exchanger 440, about 20 ° C to about 175 ° C, about 30 ° C to about 150 t, or about From 40 ° C to about 140 t. In a particular embodiment, the temperature of stream 56 can range from about 75 ° C to about 600 ° C, from about 100 ° C to about 400 ° C, or from about 10 ° C to about 300 ° C. Again, it may be preferred that the pressure of the stream 56 exiting the second heat exchanger 440 is substantially similar to the pressure of the stream 52 entering the second heat exchanger 440. In particular, leaving The pressure of the stream 56 of the second heat exchanger 440 may be at least 90%, at least 91%, at least 92%, at least 93%, at least 94% 'at least 95% of the pressure of the stream 52 entering the second heat exchanger 440. % 。 。 The second heat exchanger 440, at least 96%, at least 97%, at least 98% 'to the less than 99%', at least 99.5%, or at least 99.8%. The stream 56 passes through the third heat exchanger 450 to produce the C09 circulating liquid stream 60 having a temperature lower than the temperature of the stream 56 entering the third heat exchanger 450. When the third heat exchanger 450 passes

U 100125736 is the heat in the lowest temperature range of the heat exchanger series 420. It can be described as Form No. A0101, page 79 / 134 pages 1003441436-0 201213655, which is described as 'a low ba hot father change. In some embodiments, the temperature of the C〇2 circulating liquid stream 60 exiting the third heat exchanger 450 may be about 1 〇 to about 2 5 lower than the temperature of the stream 56 entering the third heat exchanger 450. 〇, about 15 ° C to about 20 ° C 'about 20 ° C to about 175 ° C, or about 25 ° C to about 150 ° C. In a particular embodiment, stream 60 may have a temperature of from about 40 ° C to about 200 ° C, from about 40 ° C to about 1 ° t, or from about 40 ° C to about 90 ° C. Again, it may be preferred that the pressure of the C〇2 circulating liquid stream 6〇 exiting the third heat exchanger 450 is substantially similar to the pressure of the stream 56 entering the third heat exchanger 450. In particular, the pressure of the C〇2 circulating liquid stream exiting the third heat exchanger 450 may be at least 90%, at least 91%, at least 92% of the pressure of the stream 56 entering the third heat exchanger 450, At least 93%, at least 94%, at least 95%, at least 96%, at least 97% 'at least 98%', at least 99%, at least 99.5%, or at least 99.8% ° entering the third heat exchanger 450 ( And thus the C〇2 circulating liquid stream 60, which generally exits the heat exchanger unit 420, can be directed to one or more separation units 520. As also described above, the (3) circulating liquid stream can be separated by one or more types of L· to remove the subordinate component from the stream, and then pressurized to return to the combustor as the recycled cycle. Liquid (optionally separated (: part of 02 to enter a C〇2 line or other storage or disposal device without discharge to the atmosphere). Back to Figure 8, the added The pressure C 〇 2 circulating liquid stream 70 (or 85, if first passed through a separation device, as shown in Figure 5) can be directed back through the same three heat exchangers in series, thus, originally through the heat The heat recovered by the exchanger can be used to impart heat to the pressurized C〇2 circulating liquid stream 7 进入 prior to entering the burner 22. Typically, the number is 1 * 8 by the number through the three 100125736 forms. 〇S/* 134 ^ 1003441436-0 201213655 heat exchangers (450, 440, and 430) and the heat imparted to the pressurized C〇2 circulating liquid stream 70 may be relatively opposite to the heat exchangers The amount of heat recovered (as described above) is proportional. In certain embodiments, the invention is The difference in temperature between the flow leaving and entering the thermal converter (or the last heat exchanger in the series). See Figure 8, which is specifically related to the temperature difference between streams 60 and 70. In particular, the temperature difference at the cold end of the heat exchanger (of the last heat exchanger in the series) is greater than zero' and the range may be from about 2 ° C to about 50. (:, approximately 3. (: to about 4 ° C 'about 4 ° C to about 30. 0, or about 5 to about 20 ° C. In some embodiments, the pressurized CO circulating liquid stream 70 can be directly passed through 2 in series The three heat exchangers, for example, the pressurized C〇2 circulating liquid stream 70 (i.e., at a relatively lower temperature) can pass through the third heat exchanger 450 to form Stream 71 at an increased temperature, which may pass directly through the second heat exchanger 440 to form a stream 73' at an increased temperature that may pass directly through the first heat exchanger 430 to form an extractable burner 220 The high temperature, pressurized CO recycle liquid stream 236. However, in a particular embodiment The invention is characterized in that an external heat source is used to further increase the temperature of the recovered (: 〇 2 circulating liquid. For example, as illustrated in Figure 8, the pressurized CO circulating liquid stream 70 passes After the third heat exchanger 450, the formed stream 71, instead of passing directly through the second heat exchanger 440, can be split into a splitting portion 460 of the two streams 71b and 72a by splitting the stream 71. The stream 71b can pass through Second heat exchanger 440. As previously described, stream 72a may be passed through the heat imparted by the heat exchangers themselves, in addition to the pressurized C〇2 circulating liquid stream 70, 100125736 Form No. A0101 81 pages / total 134 pages 1003441436-0 201213655 Additional amount of hot side heaters 4 7 0. The amount of the pressurized (: 〇 2 circulating liquid stream directed to the second 埶**, , the exchanger 440, and the side heater 470 from the stream 71 may depend on the operating conditions of the system and the The pressurized c〇2 circulating liquid stream changes in order to enter the desired final temperature of the combustor 220. In some embodiments, the flow 71匕 is directed to c〇2 of the second heat exchanger 440 and the stream 72a The molar ratio between C02 directed to the side heater 470 can be from about 1:2 to about 2 〇:1 (i.e., about every 2 moles of c〇2 in stream 72a versus C of the upper streamer) 2, to approximately 2 耳 C 〇 2 of the flow 72a to 2 〇 的 c 〇 2) of the upper flow 71b. In a further embodiment, the flow 71b is directed to the second heat exchanger 440 002 And the molar ratio between c〇2 of the stream 72a directed to the side heater 47() can be from about 1:1 to about 20:1, from about 21 to about 16:1, from about 2:1 to about 12 :1, from about 2:1 to about 1〇:1, from about 2:1 to about 8:1, or from about 4:1 to about 6:1. The side heater can include a heat that can be used to impart heat to the circulating liquid Any device. In some embodiments, The energy (i.e., heat) provided by the side heater can be input into the system from an external source. However, in a particular embodiment in accordance with the invention, the efficiency of the cycle can be generated in the cycle by utilization. The increase in waste heat at one or more points is increased. For example, the generation of crucible 2 for input to the burner can generate heat. Known air separation units can generate heat as a by-product of the separation process. Usefully, the helium 2 can be provided with increased pressure, such as described above, and such pressurization of the gas can also generate heat as a by-product. For example, '〇2 can be produced by operating a cryogenic air separation process, wherein Oxygen is pumped to save the cooled liquid oxygen during processing (it has been fully pressurized by adding 100125736 heat to ambient temperature form number A0101. Such a low temperature oxygen pumping work can be page 82 / 134 pages 1003441436 - 0 has two air compressors, all of which can be operated adiabatically in a no inter-stage cooling manner, so that the temperature of the hot, pressurized air can be cooled down But approaching and/or above the temperature of the stream (e.g., stream 72a, in Figure 8) heated by the external source. In the prior art settings, when the secondary cooling system is needed to eliminate the byproduct When hot, such heat is not utilized, or can be practically consumed as a system. However, in the present invention, a coolant can be used to recover the heat generated from the air separation process, and to provide the heat. To the side heater illustrated in FIG. 8, in other embodiments, the side heater itself may be the air separation unit (or an associated device), and the CO/shield ring liquid ( For example, stream 72a) in Figure 8 can itself be circulated directly through a coolant system on or associated with the air separation unit to recover heat generated in the air separation process, more particularly The added heat can be obtained by adiabatically operating the C〇2 compressor and removing the heat of compression in an after-cooler against the transfer of heat of compression to heat a portion of the high pressure c〇2 circulating liquid. One cycle heat transfer fluid And reached, or passed directly to the high pressure heat recovered by circulating the liquid C09 stream (e.g., FIG. 8 on stream 72a)

U is achieved. Furthermore, such hot addition enthalpy need not be limited to the position described in relation to Figure 8, but may be after the sub-components are separated from the c〇2 circulating liquid (but preferably in the C0 circulating liquid) By directly in the

Any point at the upstream of the heat exchanger at the upstream of the U burner input is input to the cycle. Of course, any similar method that utilizes the waste generated in the power generation cycle can also be included in the disclosure of this case. For example, 'utilize a supply stream at an appropriate temperature, or a hot exhaust gas from a conventional open-cycle gas turbine. Form No. A0101 Page 83 of 134 201213655 The amount of heat imparted by this side heater 470 may depend on the materials and equipment used and the CO2 circulating liquid stream 2 3 6 in order to enter the burner 2 2 〇 It varies with the final temperature that needs to be achieved. In some embodiments, the side heater 470 effectively increases the temperature of the stream 72 a by at least about 1 〇 ° C, at least about 20 ° C, at least about 30 ° C, at least about 40. (:, at least about 50 ° C 'at least about 60 ° C, at least about 70 ° C, at least about 80 ° C 'at least about 90 ° C, or at least about l 〇 (TC. In other embodiments 'the side The heater 470 effectively increases the temperature of the stream 72a by at least about 10 ° C to about 200 ° C, at least about 50 r to about 175 ° C ' or at least about 75 ° C to about 150 ° C. In a particular embodiment The side heater 470 causes the temperature increase of the stream 72a to fall within at least about 15 seconds of the temperature of the stream 73 exiting the heat exchanger 440, at least about 12 ° C, at least about 10 ° C, at least about 7. (within, or at least about 5 ° C. By this additional heat source, if the amount of c〇2 in the flow is directed through the second heat exchanger 440, then the third heat exchange is exited Stream 71 of vessel 450 may additionally be heated in addition to the ability of heat convection 71 available in the second heat exchanger 440. By splitting the stream, it may be obtained in the second heat exchanger 440 The heat can be completely granted to the portion of the 〇〇2 circulatory liquid in stream 71b, which is available at the same time. The heat of the side heater 470 can also be fully delegated to a portion of the contents of the CO circulating liquid in stream 72a. Thus, it can be seen that if all of the amount in stream 71 (: 〇2 circulating liquid is directed to the The second heat exchanger 440, rather than being shunted and separately heated (as described above), may have a temperature greater than the exiting second when entering the first heat exchanger 430 when utilizing an alternate splitting method The temperature of stream 73 of heat exchanger 440. In some embodiments, borrowing 100125736 Form No. A0101 Page 84 / Total 134 Page 1003441436-0 201213655 The importance of the increase in heat obtained by the S-Side shunt method is sufficient to limit the c〇 Whether the uncoiled liquid stream 236 has been sufficiently heated prior to entering the burner. As can be seen in Figure 8, the stream 7 lb exiting the splitter 46 通过 passes through the second heat exchanger 440 to form a stream 73 which is directed Mixer 480 to combine stream 73 with stream 72b discharged from the side heater 47. Next, combined stream 74 passes through the first heat exchanger 430 to enter the first heat exchanger 430 The temperature of the c〇2 circulating liquid plus To a temperature substantially close to the turbine discharge stream. The proximity of the liquid stream at the hot end of the first heat exchanger can be applied to other embodiments of the invention that use less than three or more than three heat exchangers. And can be applied to the first heat exchanger through which the c〇2 circulating liquid exits the turbine. The ability to achieve a liquid near the temperature at the hot end of the first heat exchanger can be the present invention. A key feature that achieves the desired efficiency level. In some embodiments, the turbine discharge stream from the turbine enters the temperature of the first heat exchanger in the array (i.e., after expansion into the turbine) and : 〇 2 circulating liquid leaving the heat exchanger to recover the difference between the temperatures entering the burner may be less than about 80 ° C, less than about 75 ° C, less than about ° C, less than about 65 ° C, less At about 60 t, less than about 55 ° C, less than about 50 ° C 'less than about 45 ° C, less than about 40 ° C, less than about 35. (:, less than about 30 ° C, less than about 25 ° C, less than about 20. (:, or less than about 15 ° C » As can be seen from the foregoing, the efficiency of the system and method of the present invention can be borrowed The turbine discharge stream 50 and the recovered C〇2 circulating liquid stream 236 are precisely controlled at the hot end of the heat exchanger 420 (or the first heat exchanger 430 in the series illustrated in Figure 8). Significantly benefiting from the difference. In the preferred embodiment, this temperature difference is less than 50 t. Although it is not desirable to be bound by the theory of 100125736 Form No. A0101, page 85 / 134, 1003441436-0 201213655, It has been found that, according to the present invention, the heat available for heating the recovered (: 2 circulated liquid (eg, heat recovered from the turbine discharge stream in one or more heat exchangers) may not be sufficient The entire stream of recycled c〇2 circulating liquid is sufficiently heated. It is understood that the present invention can be overcome by splitting the convection 71 so that stream 71b enters the heat exchanger 440 and stream 72a enters the exterior. a heat source 470, wherein the external heat source 470 provides The external and external sources of heat cause the temperature of stream 72b exiting the external heat source 470 to rise to a temperature substantially close to stream 73 exiting heat exchanger 440, as previously described. Next, streams 72b and 73 combine to form a stream. 74, the flow rate of stream 71b (and stream 72a) can be controlled by the temperature difference at the cold end of heat exchanger 440. The amount of external heat required to overcome the aforementioned heat deficiency can be achieved by allowing the temperature of stream 56 to be as high as possible. Minimizing and minimizing the difference in cold junction temperature of the heat exchanger 440. The water vapor generated in the stream 56 from the combustion products will reach its dew point at a temperature that depends on the composition of the stream 56 and its pressure. At this temperature, water condensation greatly increases the effective mCp of stream 56 to stream 60, as well as providing all of the heat required to heat the total recovered stream 70 to stream 71. The temperature of stream 56 leaving the heat exchanger 410 is preferably preferred. The ground may be in the range of about 5 ° C of the dew point of stream 56. Preferably, the difference in temperature between streams 56 and 71 at the cold end of heat exchanger 440 may be at least about 3 ° C, at least about 6 °. C, at least about 9 ° C, at least about 12 ° C, Less than about 15 ° C, at least about 18 ° C, or at least about 20 ° C. Returning to Figure 5, the (: 〇 2 circulating liquid 236 can be preheated before being recycled into the combustor 220, such as Illustrated by the at least one heat exchanger 420 of the hot turbine discharge stream 50 after passing through the diffusion turbine 320. To maximize the efficiency of the cycle, usefully, in conjunction with the composition of heat 100125736, Form No. A0101, page 86 / 134 pages 1003441436-0 201213655 The gas inlet path and the material available for the highly stressed turbine blades are as high as possible at the inlet temperature and at the maximum temperature allowed in the heat exchanger 420 consistent with the system operating pressure, The diffusion turbine 320 is operated. The hot inlet path of the turbine inlet stream and the first row of turbine blades can be cooled by any useful means. In some embodiments, the efficiency can be maximized by using a portion of the high pressure, recovery (: 〇 2 circulating liquid. In particular, the lower temperature (: 〇 2 circulating liquid (eg, falling at about 50 t to about The cycle may be from the cold end of the heat exchanger 420 before the cold end of the heat exchanger 420, or from the intermediate point of the heat exchanger 420 when multiple heat exchanger units in series are used (eg, from Figure 8 The stream 71, 72a, 71b, 72b, 73, or 74) is withdrawn. The blade cooling liquid can be drained from the holes in the turbine blade and can be directly fed into the turbine stream. High efficiency burners (eg, here) The operation of the evapotranial cooling burner can produce an oxidizing gas having an excess oxygen concentration (for example, in the range of about 0.1% to about 5% mole). Alternatively, the burner can produce The combustion gas is a reducing gas having certain concentrations of h2, CO, ch4, h2s, and one or more of 〇3. It is particularly advantageous that, according to the present invention, it becomes possible to use Only one turbine unit, or a series vortex An electric turbine of a wheel unit (eg, 2, 3 or more units). Advantageously, in a particular embodiment using a series unit, all units can operate at the same inlet temperature, and this makes the first The power output of the turbine feed pressure to the overall pressure ratio can be maximized. An example of a turbine unit 320 in a reduction mode utilizing two turbines 330, 340 operating in series is shown in Figure 9. As seen herein, the combustion The product stream 40 is directed to the first turbine 330. In such an embodiment, 100125736 Form No. A0101 Page 87 of 134 Page 1003441436-0 201213655 The combustion product stream 40 is designed (eg, by controlling the fuel used) The amount of helium used, and the operating conditions of the combustor, are reducing gases having one or more combustion components therein, as previously described, the combustion product stream 40 expands across the first turbine 330 to produce electricity ( For example, a related generator is not shown in this illustration), and a first exhaust stream 42 is formed. Before being introduced into the second turbine 340, Quantitative helium 2 may be added to the first turbine exhaust stream 42 to combust combustible components present in the first turbine exhaust stream 42 which may also leave the second turbine while leaving excess oxygen The inlet temperature of unit 340 rises to substantially the same value as the first turbine unit 330. For example, the temperature of the exhaust stream 42 from the first turbine unit 330 can fall from about 500 °C to about 1,000 °C. The range of addition of 〇2 to the effluent stream 42 at this temperature can cause the gas in the stream to be heated to a temperature of from about 700 ° C to about 1,600 ° C by combustion of excess fuel gas while in the reduction mode. The range is substantially the same as the temperature range of the combustion product stream 40 that exits the combustion chamber 220 and enters the first turbine unit 330. In other words, the operating temperatures at the inlet of each of the two turbines are substantially the same. In a particular embodiment, the difference in operating temperatures at the inlets of the turbines is no more than about 10%, no more than about 9%, no more than about 8%, no more than about 7%, no more than about 6%. More than about 5°/〇, no more than about 4%, no more than about 3%, no more than about 2%, or no more than about 1%. A similar reheating step for the additional turbine unit can also be carried out to the extent remaining fuel remaining. If desired, combustion can be enhanced by the use of a suitable catalyst in the oxygen feed combustion space. In some embodiments, the power cycle as described herein can be used to repair 100125736 Form No. A0101 Page 88 / Total 134 Page 1003441436-0 201213655 Complete existing power station, for example, by heating at high temperature and high pressure The liquid, such as the turbine discharge stream described herein, is introduced into the steam superheat cycle of a conventional Rank-ine cycle power plant. This may be a coal fired, or nuclear power plant with a boiling water reactor (BWR), or a pressurized water reactor (PWR) thermal cycle. This is effective in increasing the efficiency and power output of the steaming power plant by superheating the steam to a temperature much higher than the temperature of the superheated steam generated in the prior system. If a pulverized coal fired boiler is used, the steam conditions in a nuclear power plant are typically as high as about 320 °C, up to a maximum of about 600 °C before the steam temperature target. The steam temperature can rise above 700 °C using superheating that may be accompanied by heat exchange in the systems and methods of the present invention. This causes the thermal energy to be directly converted into additional shaft power, which is the additional fuel that is converted to a steam-based power station without increasing the amount of condensed steam due to the extra fuel that is superheated by the combustion. This can be achieved by providing a slave heat exchange unit. For example, as further described herein, the turbine discharge stream described in connection with the method and system of the present invention can be directed through the slave heat exchanger prior to passage through the primary heat exchange unit. The heat obtained in the slave heat exchange unit can be used to superheat steam from the boiler. As previously mentioned, the superheated steam can be directed to one or more turbines for power generation. After passing through the slave heat exchange unit, the turbine discharge stream can then be directed to the primary heat exchange unit, as otherwise described herein. Such systems and methods are described in Example 2 and illustrated in Figure 12. Furthermore, it is possible to take the low pressure steam from the inlet of the final steam turbine and use it to heat part of the recovered (: 〇 2 circulating liquid, as mentioned above. 100125736 Form No. A0101 Page 89 / 134 pages 1003441436 -0 201213655 In a particular embodiment, condensate from the steam power plant may be heated to before de-aeration with the c〇2 circulating liquid stream leaving the cold end of the heat exchange unit - intermediate temperature (for example, in some embodiments, at a temperature of about 80 ° C.) This heating normally uses bleed steam from the inlet of the final LP steam turbine stage 'so' for today The net effect of the efficiency of the steam power station with insufficient side steam heating can be compensated by preheating the condensation, which preserves the partial steam supply. The above general power generation method (ie, power generation cycle) can be utilized in accordance with the present invention. The appropriate power generation system described herein is implemented. In general, the power generation system according to the present invention may include any of the zeros described herein in relation to the power generation method. For example, a power generation system can include a combustor for burning a carbonaceous fuel in the presence of a helium 2 and c〇2 circulating liquid. In particular, the burner can be an evapotranspiration burner as described herein. 'However, other burners that can operate under otherwise described conditions may also be used. In particular, the characteristics of the burner may be related to the combustion conditions in which it operates and the particular parts of the burner itself. In embodiments, the system can include one or more injectors for providing the carbon dioxide fuel (and, optionally, a fluidization medium) the helium 2 and the C〇2 circulating liquid. The system can include Removing the parts of the liquid slag. The burner generates a fuel gas at a temperature at which solid ash particles can be effectively filtered out of the gas, and the gas can be mixed with quenching (: 02) Burning in a second burner. The burner may include at least one combustion stage in which the carbonaceous fuel is combusted in the presence of the :02 circulating liquid to provide inclusion including A combustion product stream of pressure C 〇 2 of 100125736 and temperature. Form No. A0101 Page 90 of 134 1003441436-0 201213655 The system may further comprise a power generating turbine in fluid communication with the burner, the thirst The wheel may have an inlet for receiving the flow of combustion products and an outlet for releasing a turbine discharge stream of: (〇2). The electricity may be generated as the liquid stream expands. The turbine is designed to maintain the liquid flow At a desired pressure ratio (I / 0), as described herein.

P P goes further' The system may include at least fluid communication with the turbine

100125736 A hot parent exchanger to receive the turbine discharge stream and to cool the stream to form a cooled c〇2 recycle liquid stream. Similarly, the at least one heat exchanger can be used to heat the CD (2) circulating liquid of the burner, in particular, the heat exchanger is characterized by being allowed to be subjected to the special conditions so described. Construction material for operation. The offending system may also include separating the (3) 2 circulating liquid stream exiting the heat exchanger into 〇) 2 and - or more other additional components for recovery or disposal. A special job may include (iv) a device for separating water (or other pure material described herein) from the (3) ring liquid. The I system can progress to include one or more devices (eg, compressors) that communicate with the at least one heat exchanger (and/or with - or more of the multiple separation devices) for compression and purification 〇) 2 circulating liquid. Furthermore, the system may include a device for separating the circulating liquid of the product 2 into two streams, wherein one stream passes through the heat exchanger and enters the burner, and the second stream is delivered into the I-pressurized line (or other In an embodiment of the apparatus for sequestering and/or disposing of the c〇2, an even more step-wise part may be included in the system by way of example, δ, the system may include a separation unit to 02 Delivered into a burner (or ~ - an injector or a similar device that mixes or licks two materials). In some embodiments 1003441436-0 Form Compilation Α0101 Page 91 of 134 201213655, the air separation unit can generate heat. Thus, it is useful for the system to further include one or more heat transfer components to transfer heat from the air separation unit to the paste 2 circulating liquid stream upstream of the service. In other embodiments, the system according to the present invention may include any and all of the components described herein separately with respect to the power generation cycle and the power generation method. In other embodiments, the present invention encompasses systems and methods that are particularly useful in power generation for use in fuels that leave incombustible residues upon combustion. In certain embodiments, such non-combustible material can be removed from the combustion product stream using a suitable device, such as a contaminant removal device illustrated in Figure 4. However, in other embodiments, it is useful to manage the non-combustible material by using a multi-burner system and method, such as illustrated in Figure 10. As shown in Figure 10, the coal fuel 254 can be passed through a grinding device 900 to <a powdered coal. In other embodiments, the coal fuel 254 can be provided under a particular condition. In a particular embodiment, the coal may have an average particle size of from about 1 Torr (10) to about 5 Å μηη, from about 25 μηη to about 400 μηι' or from about 5 η to about 2 〇〇 μηη. In other embodiments, the coal may be described as having an average size of less than about 500 μηη « 450 μη, » 400 Mra , 350 μπι > 300 μιη · 250 μ m ' 200 _ ' 150 μιη, or 1 〇〇 μιη Coal particles larger than 5〇%, 60%, 70%, 80% '90%, 91%, 92%, 93%, 94%, 95%, 96% '97% ' 98% '99% ' or 99 .5%. The pulverized coal may be mixed with a liquefied material to provide coal in the form of a slurry. In the figure, the pulverized coal is in a mixer 910 and a c 来自 from the recycled c 〇 circulating liquid 2 2 side draw (side draw) 68 combination. In the first diagram, the c〇 side 100125736 1003441436-0 Form No. A0101 Page 92 of 134 201213655

Extract 68 from,! The stream 67 which has been subjected to the treatment of the (3) 2 circulating liquid in a supercritical, high density state is recovered. In a particular embodiment 2, the C〇2 used to form the coal slurry may have a volume of about 45 〇 kg/ M3 to a twist of about 1,100 kg/m. More particularly, the c〇2 side draw 68 can be mated with the particulate coal to form, for example, between about 10 weight percent to about 75 weight percent, or about 25 weights of the particulate coal. Percentage to between about 55 weight percent - slurry 225. Further, the temperature at which the c〇2 from the side draw 68 is used to form the slurry may be less than about 〇 ° C, less than about -1 〇 ' less than about -20 ° C, or less. At about -30. (: In other embodiments, the C〇2 from the side draw 68 used to form the slurry may be at a temperature of from about 0 °C to about -60 °C, about -10 °C. To about -50 ° C, or about -18 ° C to about -40 ° C.

The pulverized coal/C 2 slurry 255 is transferred from the mixer 910 to a portion of the oxidation burner 930 via the pump 920. As described herein, one 〇 2 stream can be formed using an air separation unit 30 that separates air 241 into purified enthalpy 2. The 〇 2 stream is separated into 0 which is directed to the partial oxidation burner 930. Stream 243, and 09 stream 242 directed to the combustor 220. In the embodiment of Fig. 10, a stream 2 of 86 is withdrawn from the recovered C2 circulating liquid stream 85 for cooling the partial oxidation burner 930. In other embodiments, CO 2 for cooling the partial oxidation burner 930 may be taken from stream 236 to replace stream 86 ' or both 0 and 2 may be taken from stream 86 and stream 236. Preferably, it is retrieved. The amount of 〇2 is sufficient to cool the temperature of stream 256 such that the ash presents a solid form that can be safely removed' as otherwise described. The ratio of the c〇2 coal and the crucible 2 being supplied to the partial oxidation burner 930 is such that the coal is only partially oxidized to produce a composition including CO 2 at 100125736 Form No. A0101 Page 93/134 pages 1003441436-0 201213655 and H2, CO, CH4, H'2S, and a portion of the oxidized combustion product stream 256 of one or more of NH3. The CO, coal, and ο are also introduced into the partial oxidation burner 930 at a necessary Ζ 2 ratio such that the temperature of the partially oxidized combustion product stream 256 is sufficiently low to allow all of the occurrences in the stream 256 The ash is in the form of solid particles that can be removed simply by one or more cyclone separators, and/or filters. The embodiment of Figure 1 illustrates the removal of ash via filter 940. In a particular embodiment, the temperature of the partially oxidized combustion stream 2 5 6 can be less than about 1,1 〇〇, less than about 1,000 ° C, less than about 900 ° C 'less than about 8 〇〇 °c, or less than about 700 °C. In other embodiments, the temperature of the partially oxidized combustion stream 256 can range from about 300 °C to about 1, 〇〇〇^, about 4 Torr. 〇 to about 950 ° C, or about 500 ° C to about 9 〇〇 ^. The filtered, partially oxidized combustion stream 257 can be directly introduced into the second combustor 220, which can be an evapotranspiration combustor, as described herein. This input is with this 0. Stream 242 and the recovered C0 μ with + 2 2 pour % < liquid stream 236 are provided. The combustion at this point can be carried out in a manner similar to that described additionally in + & The combustor 220 is ignited in the presence of the oxidative combustion stream 2 5 6 in the presence of the sulphur-like combustion stream 256 and the enthalpy combustion stream 40. This stream is expanded across a turbine 320, which produces electricity (e.g., via generator 1209). The turbine discharge stream 5 passes through a stack of exchanger units 420 (which may be heat exchangers in series, such as ^, 'as described in relation to Figure 8). The C〇2 circulating liquid stream 60 is passed through the cooling water heat 530 to form a stream 61 which is passed through the slave component for removing the w, again, and the gas in the stream 62 (for example, Η20 'S02 'S04, ν〇 2, ν 〇 3 ' and Hg) mouth 540. The separator 540 can be substantially similar to the tubular string 1330 in the description of Fig. 12. Preferably, the separation form number A0101 page 94/134 pages from ^40 includes a counter 100125736 1003441436-0 201213655, which provides a contactor with sufficient dwell time to allow such impurities to be The water reacts to form a material that is easily removed (eg, an acid).

The purified C〇2 circulating liquid stream 65 is passed through a first compressor 630 to form a stream 66 which is cooled by a cooling water heat exchanger 6040 to provide the supercritical, high density C〇2 circulating liquid. Stream 67. As previously described, a portion of stream 67 can be withdrawn as stream 68 for use as a fluidized medium in the mixer 910 to form the coal slurry stream 2 5 5 . Further, the supercritical, high density C〇2 circulating liquid stream 67 is additionally pressurized in a compressor 650 to form the pressurized, high critical, high density C〇2 circulating liquid stream 70. A portion of stream C of stream 70 will be withdrawn at point 720, as described herein with respect to Figures 5 and 11, to provide stream 80 to a C〇2 conduit, or other storage device. The remainder of the c〇2 continues to be a pressurized, supercritical, high density C〇2 circulating liquid stream 85, a portion of which can be withdrawn as stream 86 for cooling the partial oxidation burner 930, as described above . Additionally, the stream 85 is returned to the heat exchanger 420 (or series of heat exchangers, as described in relation to Figure 8) to heat the stream and ultimately form the recovered input to the burner 220. C 〇 2 circulates liquid stream 236. As previously mentioned, an external heat source can be used in conjunction with the heat exchanger unit 420 to provide the necessary efficiency. Similarly, other systems and method parameters, as described herein, may be applied to the system and method according to FIG. 10, such as flow temperature and pressure, and the turbine unit 320, the heat exchanger unit 420, Separation unit 520, as well as other operating conditions of the compressor unit 630. EXPERIMENTAL Next, the present invention will be further described with respect to specific examples which are provided to clarify an embodiment of the present invention and should not be 100125736 Form No. A0101 Page 95 / Total 134 Page 1003441436-0 201213655 It is to be understood that the invention is limited. Example 1 Using a recovered (: 2 circulatory liquid decane combustion power generation system and method A specific example of the system and method according to the present invention is illustrated in Figure 11, and the following description relates to the use of a computer A special cycle system under special conditions of the simulation. In this method, before introducing an evapotranspiration burner 220, a temperature of 134 ° C and a pressure of 30.5 MPa of a decane (CH,) fuel stream 254 and temperature A recovered C〇2 circulating liquid stream 236 at 860 ° C and a pressure of 30.3 MPa (and thus in a supercritical fluid state) is combined in a mixer 252. An air separation unit 30 is used to provide a temperature of 105 ° C and Concentrated crucible 2242 at a pressure of 30.5 MPa. The air separation unit also generates heat (Q) which is extracted for processing. The crucible 2242 is in the combustor 22 with the decane fuel stream 254 and The (: 循环 2 circulating liquid 236 combines and is combusted there to provide a combustion product stream 40 at a temperature of 1189 ° C and a pressure of 30 MPa. The C 〇 2, 〇 2, and methane are provided at a molar ratio of about 35:2:1 (ie, lbmol/hr, each Pound moles per hour. The energy input used in this embodiment is 344,935 Btu/hr (363,932 kJ/hr). The combustion product stream 40 is expanded across the turbine 320 to produce The turbine discharge stream 50 at a temperature of 885 ° 0 and a pressure of 5 MPa (where C 〇 2 in the turbine discharge stream 50 is in a gaseous state), the rate at which the combustion product stream 40 expands across the turbine 320 to generate electricity is 83.5 per hour. Kilowatts (kW/hr) Next, the turbine discharge stream 50 passes through three heat exchangers in series to continuously cool the stream, thereby removing the subordinate components. The first heat exchanger 430 can generate a temperature of 237 ° C. And the flow 52 of the pressure 5 MPa, the flow 52 pass 100125736 Form No. A0101 page 96 / 134 pages 1003441436-0 201213655 Pass the second heat exchanger 440 ' to generate a flow of i23 ° C and a pressure of 5 MPa flow 56 'flow 56 passes through the third heat exchanger 450 to produce a stream 60 having a temperature of 80 ° C and a pressure of 5 MPa. After the C 〇 2 circulating liquid passes through the series of heat exchangers, the stream 60 can be heated by a cooling water The exchanger 530 is further cooled. The temperature is 24 ° C Water (C) is circulated through the chilled water heat exchanger 530 to cool the C 〇 2 circulating liquid stream 60 to a temperature of 27 ° C, and thus condense any water present in the 〇 2 circulating liquid stream The cooled c〇2 circulating liquid stream 61 is then passed through a water separation unit 540 such that the liquid water is removed and discharged into stream 62a. Discharged from the water separation unit 540 is the "dried" C〇2 circulating liquid stream 65 at a temperature of 34 ° C and a pressure of 3 MPa. The dry C 〇 2 circulating liquid stream 65 (which is still in a gaseous state) Next, a first compression unit 630 is passed through the two-step pressurization plan. The C 〇 2 circulating liquid stream was pressurized to 8 MPa, which likewise raised the temperature of the 〇〇 2 circulating liquid stream to 78 °C. This requires 5.22 kW/hr of power input. Next, the supercritical liquid CO recycle liquid stream 66 is passed through a second cooled 〇2 V water heat exchanger 640 where the supercritical liquid CO 2 recycle liquid stream 66 is cooled by water at a temperature of 24 ° C to produce a temperature. A cooled supercritical liquid CO at a temperature of 27 ° C, a pressure of 8 MPa, and a density of 762 kg/m 3 follows the L·ring liquid stream 67. This stream is then passed through a second compression unit 650 to form the pressurized C〇2 circulating liquid stream 70 at a temperature of 69 ° C and a pressure of 30.5 MPa. This requires an electrical input of 8.23 kW/hr. This flow is passed through a line splitter 720' whereby a 1 1 bmo 1 CO is directed to a pressurized line via a stream, and 34.1 lbmol of C09 is directed as stream 85 and back to ί* to the series Three heat exchangers to re-add 100125736 before entering the burner 220 Form No. A0101 Page 97 / Total 134 pages 1003441436-0 201213655 Heat the c〇2 circulating liquid stream. The flow of the filtered liquid C 〇 2 circulating liquid stream 85 through the third heat exchanger 450 to form a temperature of 114 ° C and a pressure of 3 0. 5 Μ P a, the flow 71 through the shunt 460, so that 27. 3 The CO/sheath of Ibmol is directed to flow 71b to the second heat exchanger 440, and 〇1 of 6.8 1 bmo 1 is directed through stream 7 2 a of one side heater 470. Stream 71 b and Each of the streams 7 2 a has a temperature of 114 ° C and a pressure of 30.5 MPa. The side heater 470 uses heat (Q) from the air separation unit 30 to provide additional flow to the C 〇 2 circulating liquid stream. The stream 71b can generate a stream 73 having a temperature of 224 ° C and a pressure of 30.5 MPa through the second heat exchanger 440. The stream 72a forms a stream 72b through the side heater 470, which is also at a temperature of 224 ° C and pressure. 30. 4 MPa. Streams 73 and 72b combine in a mixer 480 to form a stream 74 having a temperature of 224 ° C and a pressure of 30.3 MPa, and then stream 74 passes through the first heat exchanger 430 to return to the The inlet of the burner 220 provides a temperature of 860 ° C and a pressure of 30. 0 MPa of the recovered (: 〇 2 circulating liquid stream 236. Calculation of the efficiency of the aforementioned simulated cycle Based on the comparison between the generated energy and the LHV of the methane fuel and the additional energy input to the system, as described above, an efficiency of about 53.9% can be achieved under the simulated conditions, which is particularly surprising in that This excellent efficiency also avoids any atmospheric emissions of C 0 2 (especially due to any CO 2 produced by the combustion of the carbonaceous fuel). Example 2 Pulverized coal power station finishing with recycled c〇2 circulating liquid Power Generation System and Method Another special example of a system and method in accordance with the present invention is set forth in the first 1 2 100125736 Form No. A0101, page 98 / 134, page 1003441436-0 201213655, the following description describes A special cycle system under special conditions simulated by a computer. In this simulation, the trimming ability of the system and method for a conventional pulverized coal power station is illustrated. The pressure of 30.5 MPa is 1 〇 2 flow 1 056 and a pressure of 30. 5 MPa of a carbon-containing fuel 10 5 5 (for example, a coal-derived gas produced by partial oxidation) and a pressure of 30. 5 MPa of a C 〇 2 circulating liquid stream 1 053 Evaporatively cooling the burner 220. The crucible 2 can be received from an air separator, or a similar device that can generate heat (Q) that can be extracted for use in the system, for example, to produce an expanded stream, or The heat is increased to a cooled c〇2 circulating liquid stream. The combustion of the fuel in the combustor 220 produces a combustion product stream 1054 at a temperature of 1,150 ° C and a pressure of 30.0 MPa, which flow expands over a turbine 320 ( It may be referred to as a primary power generating turbine in general to generate electricity by driving a generator 1 029. The diffusion turbine discharge stream 1001 at a temperature of 775 ° C and a pressure of about 3.0 MPa is introduced into the hot end of a heat exchanger 110 where the heat from the turbine discharge stream 1001 is used to superheat the conventional coal-fired power generation. The high pressure stream generated in station 1 800 flows 1 031 and the medium pressure stream flows 1 032. Boiler fed water 1810 and coal 1810 are input to the power station 1800 to generate flow flows 1031 and 1032 by burning the coal 1810. The heat transfer in the heat exchanger causes the equal stream flows 1031 and 1 032 to be superheated from a temperature of about 550 ° C to a temperature of about 750 ° C to form flow streams 1 033 and 1 034 which will return to the power station. (described below). This method achieves a very high steam temperature without the need for a conventional power station to use expensive high temperature alloys in large steam boilers that burn coal near atmospheric pressure. The flow streams 1033 and 1034 are expanded into a three-stage turbine 1200 (generally 100125736 Form No. A0101 Page 99 / Total 134 pages 1003441436-0 201213655 called. Subordinate power thirteen) to drive a generator m. Stream 1 〇 35 leaving the turbine 1 200 is condensed in condenser crucible 220. The treated condensate 1 036 is pumped to a high pressure using a feed water pump 123, and then vaporized and superheated in the coal-fired boiler 1800 to be discharged into the 5 Xuan heat exchanger 1 00, As mentioned above. This system is used to increase the power rotation and efficiency of an existing coal-fired power station. The heat exchanger 100 is a Heatric type diffusion bonded plate heat exchanger having a chemical polishing channel typically constructed of a high temperature, high nickel content alloy (eg, '617 alloy), wherein the alloy is capable of control This heat exchanger is a high-efficiency heat transfer unit with a high heat transfer coefficient for all liquids, enabling significant overheating and operation under oxidizing conditions, as well as pressure and high temperatures. The remainder of the systems and methods illustrated in Figure 12 are similar in construction and operation to the systems and methods described herein. In particular, the diffusion turbine discharge stream 1001 is cooled in the heat exchanger 11 and exits the cold end of the heat exchanger 1100 as a discharge stream 1 037 having a temperature of 575 C. This stream 1037 is then passed through a second heat exchanger, where it is cooled to a temperature of 90 ° C and a pressure of 2.9 MPa to form a stream 1 0 3 8 . This stream is further cooled to a temperature of 40 C in a third heat exchanger crucible 31 by virtue of a portion of the condensate 1057 from the condenser 丨2 3 该 of the power station to form a stream 10 3 之间。 Further, it is further cooled by a cooling water in a cooling water heat exchanger 1 3 2 0 to a temperature of 27 ° C, to form a pressure of 1. 8 7 MPa of 1 0 4 0. The heat exchanger 13 〇〇 may be a Heatric 310 stainless steel diffusion bonded unit ° 30 ° C. The cooled flow 1 040 is fed into a packaged column 丨 330 100125736 Form No. A0101 Page 100 of 134 pages 1003441436-0 201213655 Base, equipped with a circulation pump 1340, which provides a countercurrent weak acid circulation stream to supply countercurrent contact between the incoming gas and the weak acid wash . S〇2, S〇3, NO, and NO are converted to HN〇3 and H2S04, and are absorbed by the liquid together with the condensed water and any other water-soluble components, and the net liquid product from the column 1330 is removed in line 1042. And the pressure is reduced to atmospheric pressure and then enters a separator 1360. Dissolved (: 〇2 is flashed off in line 1043, compressed to a pressure of 2.85 MPa using a pump 1350, and flowed into stream 1044' to join the stream exiting the top of column 1 330. 45. Ο The combined flow formation will re-recycle the liquid into the burner (1 〇 2 circulating liquid. 1125 〇 4 and HN 〇 3 diluted in water exit from the base of the separator 1360 to flow 1046, depending on the concentration The fuel composition and temperature in the contactor column 1 330. It is noted that, preferably, nitric acid is present in the acid stream 1 046 because nitric acid will react with any mercury present and is completely Remove this impurity.

The recovered liquid entering the compressor 1 380 (: 〇 2 circulating liquid stream is first dried in a desiccant dryer to a dew point of about -60 ° C, and then purified to remove the hydrazine using a cryogenic separation scheme 2, N2 and Ar, as shown in, for example, European Patent Application No. EP 1 952 874 A1, which is hereby incorporated by reference. ??? ??? ??? ??? ??? ??? ??? 5 MPa和温度74°。 The pumping is carried out in a pump 1390 to a pressure of 30. 5 MPa and a temperature of 74 ° by means of a cooling water in a cooling water heat exchanger 1370 for cooling, and then forming a dense, supercritical co2 circulating liquid 1048, which is pumped to a pressure of 30. 5 MPa and a temperature of 74 ° C, to form a high pressure, recovered CO 2 circulating liquid stream 1050 ° 100125736 (: a part of 〇 2 is removed from the stream 1 〇 50, as a c 〇 2 product stream form number A0101 page 101 / A total of 134 pages 1003441436-0 201213655 1049, which will be stored or otherwise disposed of without being released to the atmosphere. In this embodiment, the pressure of the % product stream 1〇49 is reduced to approximately 20 MPa. Line pressure and pass through a (3) 2 line The remainder of the high pressure, recovered helium 2 circulating liquid stream (now stream 1〇51) 2 enters the cold end of the heat exchanger 1 300. This stream is at 74<> (: dense supercritical liquid) A relatively large amount of low-grade heat must be received to convert it to a temperature of 237 Q, which has a much lower specific heat. In this embodiment, such low heat is taken from the conventional The steam flow of the low-pressure steam turbine of the power station has a pressure of 〇65 Mpa, an LP steam stream 1 052, and a compressed adiabatic heat derived from an air compressor in a low-temperature oxygen plant supplying the stream 1〇56. Provided. The low pressure stream exits the heat exchanger 13 and becomes a stream 1301. Optionally, all of the heat may be provided by using some of the available steam streams from the coal-fired power station at a pressure of up to 3.8 MPa. This energy can also provide the heat (Q) formed from the air separation unit, as previously described. The side stream that heats a portion of the recovered c〇2 stream provides for the cold end of the heat exchanger 1 300. Most of the heat and allowed in the hot The hot end of the 1300 has a small temperature difference of only about 25 ° C, which increases overall efficiency. The high pressure, high temperature, recovered C 〇 2 circulating liquid stream 1053 leaves the heat exchanger 1 300 at a temperature of 550 ° C ' and enters A burner 220 is used to cool the combustion gases (in this embodiment) derived from the combustion-natural gas stream 1 055 and the 97% molar oxygen stream 1 056 to produce a combustion product stream 1 054, as described above. In this embodiment, the turbine heat path and the first row of turbine blades are cooled using a stream 2 〇 58 taken from the pump discharge stream 1 050 at a temperature of 74 °C. 100125736 Form No. A0101 Page 102 of 134 Page 1003441436-0 201213655 If the above system is operated to utilize a separate power station consisting of pure (: 114 simulated natural gas fuel, then the recovered () 〇 2 flow 1〇53 The temperature is about 750 ° C into the burner, and the turbine discharges 1 〇〇 1 into the heat exchanger 1300 at a temperature of about 775 ° C. The efficiency of the single power generation system in this embodiment is 53.9% ( LHV). This composition includes the low temperature 〇2 plant and the power consumption of the natural gas feed and the helium compressor. If the fuel is simulated as coal with a calorific value of 27.92 Mj/kg (for example, using the first burner and the filter unit) The partial oxidation of the ash furnace followed by the combustion of the fuel gas and the C 〇 2 mixture in the second burner will result in an efficiency of 54% (LHV). In both cases, 'derived from the fuel Almost 100% of the carbon c2 in the carbon can be generated as a line pressure of 20 MPa. The above-described system and method using coal fuel in Fig. 12 is characterized in that it can be applied to power generation with the following special parameters. Station, according to the invention The effect of converting the burning coal power station is as follows: · Steam condition HP steam: 16.6 MPa, 565 °C ’ Flow: 473 14 kg/sec

LP steam: 4. 02 MPa, 565 °C ' Flow: 371.62 kg/sec Net power output: 493. 7.Mw Coal used in existing power stations: 1256.1 Mw Net efficiency: 39. 31% c〇2 capture %: 0 Existing power plant incorporating the system and method disclosed in the present invention and upgraded factory: 100125736 Form No. A0101 Page 1 of 3 / Total 134 Page 1003441436-0 201213655 cc^Power System Net Power Output: 371. 7 Mw Existing power station net power: 639.1

Mw Total net power: 1010. 8Mw Coal for c〇2 power system: 1053.6 Mw Coal for existing power stations: 1 256. 1

Mw Overall net worth: 43. 76°/〇 C〇2 capture %: 45. 6% * * Note that in this example, no c〇2 was captured from the existing power station. Numerous modifications and other embodiments of the invention will be apparent to those of ordinary skill in the art. Therefore, it is understood that the invention is not limited to the specific embodiments disclosed, and the modifications and other embodiments are intended to be included in the scope of the appended claims. Although specific terms are used herein, they are used in a generic and statistic format and not for the purpose of limitation. BRIEF DESCRIPTION OF THE DRAWINGS [0005] Having described the invention in a general term, reference will now be made to the accompanying drawings, which Schematic diagram of the evapotranspiration burner device used; 100125736

Figure 2 is an exemplary cross-sectional view of a wall of an evapotranable part that can be used in a burner apparatus in some embodiments of the present disclosure, Form No. A0101, page 104, 134, pp. 1003441436-0 201213655; Figure 3A and Section 3B The figure schematically illustrates a hot fit process that can be used for a collection of evapotranic components of a burner apparatus in certain embodiments of the present disclosure; FIG. 4 is a schematic illustration of that available in accordance with certain embodiments of the present disclosure. Combustion product pollution removal device; FIG. 5 is a flow chart showing power cycling according to an embodiment of the present disclosure; FIG. 6 is a diagram showing flow of CO/shield ring liquid through a separation unit according to an embodiment of the present disclosure; Flow chart

7 is a flow chart showing the pressurization of two or more compressors or pumps connected in series in a pressurizing unit according to an embodiment of the present disclosure; FIG. 8 is a view showing one according to the present disclosure. A flow chart of a heat exchanger unit of an embodiment, wherein three individual heat exchangers are used in series; and FIG. 9 is a diagram showing operation in series in a reduction mode in accordance with an embodiment of the present disclosure. Flowchart of a turbo unit of a turbine; FIG. 10 is a flow chart showing a power generation system and method using a two burner according to an embodiment of the present disclosure;

FIG. 11 is a flow chart showing a specific example of a power generation system and method according to an embodiment of the present disclosure; and FIG. 12 is a view showing a coal fired boiler according to an embodiment of the present disclosure. A flow chart of another example of a power generation system and method. [Main component symbol description] [0006] 220 burner device 222 combustion chamber 100125736 222A inlet portion form number A0101 page 105 / 134 pages 1003441436-0 201213655 2 2 2 B outlet portion 223 end wall 2338 pressure suppression member 236, 61, 65 circulating liquids 236a, 236b, 52, 56, 62, 74, 73, 71, 71b, 72a, 72b, 1044, 1045, 1039, 1038, 1301, 1035 stream 254, 1 055 carbon fuel 250A slurry Feed 254A pulverized coal 255 liquefied material 250 mixed set 242 oxygen 230 evapotranspiration 2331 external transpiration member 2332 internal transpiration member 231 buffer layer 2339 heat insulating member 2350 heat removal device 2336 wall 210 evapotranspiration 2337 channel 2333A first evapotranspiration liquid supply passage 2333B Second Evapotranic Liquid Supply Path 2335 Multiple Flow Paths or Holes or Other Suitable Openings 2A Central Collection Provide 100, 100A, 100B, 100C Centrifugal Separator Unit 100125736 Form No. A0101 Page 106 / Total 134 Page 1003441436-0 201213655 2 Central Collection line 4 outlet tube 12 collection line 5 outlet nozzle 6 water-cooled section 9 valve

7 line 8 separated line 14 outlet nozzle or line 20 sump 1 cyclone 3 outlet channel 11 branch channel 125 pressure housing 2340 separator device 85, 60, 62b, 70, 67 ' 66 circulating liquid stream 80 pipe liquid flow

720 line splitter 620 pressurizing unit 520 separation unit 420 heat exchanger 50 turbine discharge stream 320 diffusion turbine 530, 640, 1 370, 1 320 cooling water heat exchanger 540, 1 360 separator 550 separation unit 100125736 Form No. A0101 Page 107 / 134 pages 1003441436-0 201213655 6 2 a liquid water stream 650, 1 380 compressor 630 first compressor 430 first heat exchanger 440 second heat exchanger 450, 1310 third heat exchanger 480, 910 252 mixer 460 splitter 470 side heater 40, 1 054 combustion product stream 330, 340 turbine 42 first exhaust stream 30 air separation unit 241 air 900 grinding device 256 cooling stream 930 oxidation burner 920, 1 390, 1 350 Pump 68 side extraction 940 filter 86, 1 058 (: 〇 2 flow 257 combustion flow 80 C09 pipeline liquid flow 1 209, 1210 generator Q heat 1 056 oxygen flow 100125736 Form No. A0101 Page 108 / 134 pages 1003441436 -0 201213655 1 053, 1051, 1 047C〇2 circulating liquid stream 1049 C〇2 product stream 1050 pump discharge stream 1048 (: 〇 2 circulating liquid 1042, 1043 line 1 046 acid stream 1340 cycle pump 1 330 column 1 040 has cooled flow 1001 1100 expansion Turbine discharge stream 1037 discharge stream 1031 high pressure flow 1 800 power station 1 057, 1 036 condensate 1052 LP steam flow 1 032 medium pressure flow 10 3 3 flow 1 200 three-stage turbine 1220 condenser 1230 feed water pump 1810 Coal 100125736 Form No. A0101 Page 109 / Total 134 Page 1003441436-0

Claims (1)

201213655 VII. Patent application scope: 1. A power generation method comprising: introducing a fuel, helium 2, and a helium 2 circulating liquid into a burner having a pressure of at least about 12 MPa and at least about 400 a temperature of °C is introduced; the fuel is combusted to provide a combustion product stream comprising: (〇2, the combustion product stream having a temperature of at least about 800 ° C; expanding the combustion product stream across a turbine to Generating electricity, the turbine having an inlet for receiving the combustion product stream, and an outlet for releasing a turbine discharge stream comprising: (〇2, wherein the combustion product stream at the inlet is compared to The turbine discharge stream at the outlet has a pressure ratio of less than about 12; recovering heat from the turbine discharge stream by passing the turbine discharge stream through a primary heat exchange unit to provide a cooled turbine discharge stream; The cooled turbine exhaust stream removes one or more subordinate components present in the cooled turbine exhaust stream other than c〇2 to provide a purified, cooled turbine exhaust stream Compressing the purified, cooled turbine discharge stream to a pressure above the critical pressure of c〇2 using a first compressor to provide a supercritical c〇2 circulating liquid stream; circulating the supercritical C〇2 liquid Cooling to a temperature having a density of at least about 200 kg/m3; passing the supercritical, high-density c〇2 circulating liquid through a second compressor to pressurize the c〇2 circulating liquid to the burner The required pressure; the supercritical, high-density, high-pressure c〇2 circulating liquid is passed through the same main 100125736 Form No. A0101, page 110 / 134 pages 1003441436-0 201213655 heat exchange unit, so that the recovered heat is used To increase the temperature of the c〇2 circulating liquid; to supply an additional amount of heat to the supercritical, high-density, high-pressure c-ring liquid L body, thus leaving the main heat exchange unit for recovery to the burner 6 The difference between the temperature of the circulating fluid and the temperature of the turbine discharge stream is less than about 50 ° C; and recovering the heated, supercritical, high-density c〇2 circulating liquid to the burner D. The method of claim 1, wherein the retracting step cools the turbine discharge stream to a temperature below its water dew point. The method of claim i, wherein the removing step further comprises 'Through the ambient temperature cooling medium to further cool the thirsty wheel discharge stream. For example, the method described in the third paragraph of the full-time application, wherein the further cold part condenses with the multi-subordinate component of the money Water to form a solution comprising 1^.4, HN〇3, HC1, and _ or more of which are collected, such as the method described in the application for the hometown, wherein the first The compressor shrinks the cold (four) wheel discharge stream to a pressure of at least about 12 MPa. The method of claim 1, wherein a product CO stream is withdrawn from the supercritical, high-money, high (10) body stream by the primary heat exchange unit. 2 The method of claim 6, wherein the carbon combustion in the carbonaceous fuel is formed by the method 100125736 as described in claim 6 wherein the product (the 〇2 stream package is substantially All CO. L· 'Where, the product co9 flow is 1003441436-0 Form No. A0101 Page m / 134 pages 201213655 ίο 12 13 14 15 16 17 100125736 Compatible with direct input to high pressure (3) #路The method of claim 1, wherein the combustion is carried out at a temperature of from about 00 ° C to about 5 shoulders t. The method of claim 1 Wherein the _ includes a portion of the combustion product stream. 11. The method of claim 10, comprising combusting a carbonaceous fuel together with hydrazine 2 in the presence of a (3) corpse liquid, the carbonaceous ", and the supply ratio of the C〇2 circulating liquid is such that the carbonaceous fuel is only partially oxidized to produce a non-component, ΓΛ, silk co2, and H2, co, CH, (4), and (10)3 - Or more partial oxidation combustion The method of claim 2, wherein the carbonaceous material, 〇2, and oy« liquid provide a temperature that is low enough to allow the portion of the recorded combustion product stream to be All non-combustible components in the stream are in the form of solid particles. As in the method of claim 12, 1^ π/ίΓ 'where the temperature of the portion of the cerium oxide product stream is from about 500 t to about 9 〇〇. The method of claim 4, wherein the fourth embodiment of the flammable combustion product is less than the A method of partially oxidizing a combustion product; mg/m3, as described in the first aspect of the patent application, lignite or petroleum coke. In the middle, the fuel includes the method of applying the full-time application of the coal, wherein The material is in the form of a particle and is supplied as a slurry together with C〇2. For the method described in the scope of the patent, item 1 of the form number page, please refer to the page (total) (3) 201213655 Ο 19 . 20 . 21 22 . 23 . 24 . 25 . More than 90% of the particles have an average size of less than about 5 〇〇 _. The method of claim 18, wherein more than 99% of the particles have less than about The method of claim i, wherein the % circulating liquid is introduced at a pressure of at least about 15 MPa, as in the method of claim No. The circulating liquid is introduced at a pressure of at least about 20 MPa. The method of claim 2, wherein the ring liquid is introduced at a temperature of at least about 6,000 C. Such as applying for a patent! The method of item wherein the foot-ring liquid is introduced at a temperature of at least about 700 °C. The method of claim 4, wherein the combustion product stream has a temperature of at least about 1, 〇 〇 °C. The method of claim 1, wherein the combustion product stream has a pressure of at least about 90% of the pressure of the CO 2 introduced into the burner. The method of claim 25 is disclosed in claim 25. Wherein the combustion product stream has a pressure of at least about a pressure of C〇2 introduced into the burner. 5至约1〇。 The pressure ratio of the pressure of the combustion product to the inlet of the turbine is about 1.5 to about 1 〇. 28. The method of claim 27, wherein the pressure ratio of the combustion product to the inlet is from about 2 to about 8 compared to the pressure of the turbine discharge at the outlet. 100125736, as described in the scope of claim 1 of the patent application form No. A0101, page 113 / page 134 'where the fuel is one containing 1003441436-0 29 . 201213655 rabbit fuel 'and therein, % in the % circulating liquid The ratio of carbon to the fuel introduced into the burner is from about 1 Torr to about 30 31 32 33 34 35 as described in the application of the subject matter (10), wherein in the paste circulating liquid (3) The ratio of the sound of the burner to the burner is about 10 to about 30 based on the mole. For example, if you apply for the special listening section (4), the CO2 in the (four) round of discharge is a gaseous state. For example, if the application is specifically (4), the New Zealand, as described in Item 31, has a magical power of less than or equal to 7 MPa. The method of claim 4, wherein the primary heat exchange unit comprises at least three heat exchangers in series. For example, applying for the green of the 33rd item of the full-time division, wherein the first heat exchanger in the series receives the turbine discharge flow and lowers the temperature thereof, the first heat exchanger is capable of withstanding at least about 7 〇 () A high temperature alloy of gas is formed at a temperature. The method of claim 1, wherein the supercritical, high density c〇2 circulating liquid stream has a pressure of at least about 15 MPa after passing through the second compressor. The method of claim 35, wherein the supercritical, high density C 02 circulating liquid stream has a pressure of at least about 25 MPa after passing through the second compressor. The method of claim 1, wherein the supercritical (3) 卩 circulating liquid stream is cooled to a temperature having a density of at least about 4 〇〇 kg/ms. The method of claim 1, wherein the additional amount of heat comprises heat recovered from the separation unit. 1003441436 Form No. A0] 01 Page / Total] Page 34 201213655 159 ·If you apply for the patent scope! The method of the present invention, wherein the supply amount is such that the fuel of the part is oxidized to include - or more of oxidation products of (3) 2, % 〇, and S 〇 2, and the remainder of the fuel is oxidized For one or more combustible components, the one or more combustible components are selected from the group consisting of ^, 0 CH4, H2S, NH3, and combinations thereof. 40. The method of claim 4, wherein the (four) wheel comprises two units, each of which has an inlet and an outlet, and wherein the operating temperature at the inlet of each unit is substantially the same. 41 · The method described in the full-time division (4), including adding -% to the liquid stream at the outlet of the first turbine unit. 2 42 · If you apply for a patent scope! The method of item wherein the turbine discharge stream is an oxidizing liquid comprising an excess of cerium 2 . The method of claim 1, wherein the c〇2 circulating liquid is introduced into the evaporative cooling burner to mix with the crucible 2 and the fuel or both. 44 . 45 . The method of claim 1, wherein the burner comprises an evapotranspiration burner, such as the method of claim 1, wherein the (3) 2 circulating liquid is introduced into the money-dissipating cold. The burner 'is taken as all or part of the evapotranspiration cooling liquid, and is then guided through a 46.47. 48. 100125736 or more evapotranspiration supply channels formed in the evapotranspiration burner. The method of claim 1, wherein a temperature of about 1,300 ° C is applied. The method of claim 1, wherein the method is from 1200 ° C to about 5,000. (A temperature of (:) is implemented as in the method of claim 1, wherein Form No. A0101, page 115/134, the combustion is at least, the combustion is about, and the 〇2 is provided as 1003441436-0 8%。 The method of the method of the present invention, wherein the molar concentration is from about 85% to about 99. 8%. 5. The method of claim 2, wherein the turbine discharge stream passes directly into the primary heat exchange unit without passing through an additional burner. 51. The method according to the item, wherein the efficiency of the combustion is greater than 50%, and the efficiency is calculated as a ratio of net electric power generated in relation to the total low calorific value heat energy of the carbonaceous fuel for combustion generation. The method of clause 3, comprising, between the burning step and the expanding step, passing the combustion product stream through at least one means for removing a contaminant in a solid or liquid state. The method of claim 5, comprising: passing the turbine discharge stream through a subordinate heat exchange unit between the expansion step and the retracting step. 54. The method of claim 53, wherein The slave heat exchange unit utilizes heat from the turbine discharge stream to heat one or more streams derived from a steam power generation system. 55. The method of claim 54, wherein the steam power generation system The method of claim 55, wherein the method of claim 55, wherein the conventional steel furnace system comprises a coal-fired power station, wherein the method of claim 54 wherein The conventional pin furnace system includes a nuclear energy reactor.. The method of claim 54, wherein the one or more heated steam streams pass through one or more turbines for power generation. 100125736 1003441436-0 Form No. A0101 Page 116 of 134 201213655 59. A method of generating electricity, comprising: introducing a carbonaceous fuel, 0, a (^. circulating liquid into a steaming Cooling the combustion engine L, the C〇2 being introduced at a pressure of at least about 8 Mpa, and a temperature of at least about 200 ° C; burning the fuel to provide a combustion product stream comprising: (〇2, The combustion product stream has a temperature of at least about 80 ° C; and the combustion product stream is expanded across a turbine for power generation, the turbine having an inlet for receiving the combustion product stream, and an outlet for Release a turbine exhaust stream comprising CO wherein the combustion calcination at the inlet is less than about 12 60 61 62 〇 63 64 compared to the turbine discharge stream at the outlet. The method of claim 59, wherein the c〇 circulating fluid 2 is introduced at a pressure of at least about 2 MPa. The method of claim 59, wherein the c〇2 circulating liquid is introduced at a temperature of at least about 700 °C. The method of claim 5, wherein the combustion product stream has a temperature of at least about 1, 〇 〇乞. The method of the present invention, wherein the pressure ratio of the sigma (four) force to the pressure of the turbine discharge to the outlet is from about 1.5 to about 1 Torr. The method of claim 4, wherein the ratio of 〇2 in the liquid to carbon in the fuel to be introduced to the burner is from about 10 to about 50 based on the molar. 100125736 6566 The method of claim 59, wherein c〇2 in the stream is in a gaseous state. The method of claim 65, wherein Form No. A0101, Page 1 of 134, is discharged at the turbine. The turbine discharge stream 1003441436-0 201213655 has a pressure of less than or equal to 7 MPa. 67. The method of claim 59, further comprising passing the full wheel discharger through a primary heat exchange unit to recover heat from the thirsty wheel discharge stream and providing less than about 200. A cycle of temperature is a cycle. 68. The method of claim 67, wherein the primary heat exchange unit comprises at least two heat exchangers in series. Μ The method of claim 67, further comprising performing - or more separating steps on the % helium ring liquid stream to remove the liquid stream present in the ring liquid except (: 〇 2 One or more subordinate components. The method of claim 69, further comprising compressing the purified, C〇2 circulating liquid stream above the % critical pressure using a „first-restrictor a pressure to provide a supercritical c〇^ shield ring liquid stream. 71. The method of claim 7, further comprising cooling the supercritical CO? circulating liquid stream to a density of at least about a temperature of 2 〇〇kg/m3. 72. The method of claim 7, wherein the supercritical, still dense C〇2 circulating liquid is passed through a second compressor to The (3) cycle liquid is pressurized to the pressure required to be input to the burner. 73. The method of claim 72, further comprising: making the supercritical, helium density, high pressure (: 〇 2 cycle The liquid passes through the same main heat exchange unit so that the recovered heat is used Increasing the temperature of the C〇2 circulating liquid. 74. The method of claim 73, further comprising supplying an additional amount of heat to the supercritical, high-density, high-pressure c〇2 circulating liquid, , the difference between the temperature of the circulating fluid and the temperature of the turbine discharge stream for recycling to the burner is less than about 100125736 Form No. A0101 Page 118 / Total 134 pages 50 ° C » 201213655 75. The method of claim 74, further comprising recovering the heated, supercritical, high density (: 〇 2 circulating liquid to the burner. 76. as claimed in claim 74 The method of the present invention, wherein the step of supplying an additional amount of heat comprises the use of heat recovered from a separation unit. 77. The method of claim 67, wherein the turbine discharge stream passes through the The method of claim 77, wherein the slave heat exchange unit utilizes from the turbine row, before the primary heat exchange unit, the turbine discharge stream is passed through a slave heat exchange unit. The heat of the discharge heats one or more streams derived from a steam power generation system. The method of claim 78, wherein the steam power generation system comprises a conventional boiler system. The method of claim 79, wherein the conventional boiler system comprises a coal-fired power station. The method of claim 78, wherein the conventional boiler system comprises a nuclear energy reaction The method of claim 78, wherein the one or more heated steam streams pass through one or more turbines for power generation. 83. As claimed in claim 59 The method wherein at least a portion of the c〇2 circulating liquid is introduced into the evaporative cooling combustor to mix with one or both of the crucible 2 and the carbonaceous fuel. 84. The method of claim 59, wherein the C〇2 circulating liquid is introduced into the evapotranial cooling burner as all or part of an evapotranspiration cooling liquid, thereby being guided through the evapotranspiration. Cooling one or more evapotranspiration supply channels in the combustor. 100125736 Form No. A0101 Page 119 of 134 1003441436-0 201213655 8. The method of claim 59, wherein the combustion is carried out at a temperature of at least about 1,300 °C. 86. The method of claim 59, wherein the combustion is between about 1300 C and about 5,0 Torr. A temperature of 〇 is carried out. The method of claim 59, wherein the crucible 2 is provided as a stream wherein the crucible 2 has a molar concentration of at least 85 Å/〇. 88. The method of claim 59, wherein the efficiency of the combustion is greater than 50%, the efficiency being calculated as net power generated in relation to the total low calorific value thermal energy of the carbonaceous fuel for combustion generation. The ratio. 89 power generation systems, comprising: an evapotranspiration burner configured to receive a fuel, 〇, and c〇 a 2 2 ring liquid stream, and having at least one combustion stage to be present in the presence of the c 〇 circulating fluid 2 The fuel is combusted, and at a pressure of at least about 8 Mpa and at least about 800. a temperature of (: a combustion product stream comprising c〇; a primary power generating turbine in fluid communication with the burner, the primary thirsty wheel having an inlet for receiving the combustion product stream, and an outlet for Release a turbine discharge stream comprising: (〇2, the primary turbine being adapted to control the pressure drop such that the pressure of the combustion product stream at the inlet is less than the pressure ratio of the turbine discharge stream at the outlet At about 12; a primary heat exchange unit in fluid communication with the primary turbine for receiving a beta thirsty wheel discharge stream and transferring heat from the thirsty wheel discharge stream to the c〇2 circulating liquid stream; At least one compressor is in fluid communication with the at least one heat exchanger for compressing the C〇2 circulating liquid stream. 90 100125736 The power generating system of claim 89, further comprising one or more forms No. A0101 Page 120 of 134, nn. 201213655 Separating devices, located between the heat exchange unit and the at least one compressor 'to be removed from the (: 〇 2 circulating liquid) One or more subordinate components other than C〇2. 91. The power generation system of claim 89, further comprising a first-compressor adapted to compress the c〇2 circulating liquid stream to be higher than A pressure of the C0 critical pressure 2 force. 92. The power generation system of claim 91, further comprising a cooling device adapted to cool the (by 〇2 circulating liquid stream) leaving the first compressor To a temperature having a density greater than about 200 kg/m3. 93. The power generation system of claim g2, further comprising a second compressor adapted to compress the cooled c〇2 circulating liquid stream to A pressure required to input the burner. 94. The power generation system of claim 92, further comprising one or more heat transfer components for transferring heat from an external source to the upstream of the burner And the C〇2 circulating liquid flowing down the second compressor. The power generating system of claim 94, wherein the heat transfer components are associated with a single generating device. Range 89 The power generation system further includes a second burner located upstream of and in fluid communication with the evapotranspiration burner. 97. The power generation system of claim 96, further comprising - or more A power generation system according to claim 97, wherein the second burner is an evapotranspiration. The power generation system of claim 97, wherein the second burner is an evapotranspiration. Cooling the burner. The power generation system of claim 96, further comprising a mixing device to form a slurry of particulate fuel material and fluidized medium. Form No. A0101 Page 121 of 134 1003441436-0 201213655 100 101 102 103 The power generation system of claim 96, further comprising a grinding device for atomizing a solid fuel. The power generation system of claim 89, wherein the heat exchange unit comprises at least two heat exchangers. The power generation system of claim 101, wherein the heat exchange unit comprises at least three heat exchangers connected in series. A power generation system according to claim 101, wherein the first heat exchanger in series is adapted to receive the primary turbine discharge stream and is capable of withstanding at least about 700. A power generation system according to claim 89, wherein the main power generation turbine includes at least two turbines connected in series. 105. The power generation system further includes a slave heat exchange unit positioned between the main power generation turbine and the main heat exchange unit, and in liquid communication with the main power generation turbine and the main heat exchange unit. The power generation system of the first aspect, further comprising a money furnace, is in liquid communication with the subordinate heat exchange via at least one steam flow. 107. The power generation system according to claim 106, further comprising A slave power generating turbine having an inlet for receiving at least one steam stream from the slave heat exchange unit. 100125736 Form No. A0101 Page 122 of 134 Page 1003441436-0