Abstract: A chemical looping system that contains an oxidizer and a reducer is in fluid communication with a gas purification unit. The gas purification unit has at least one compressor, at least one dryer; and at least one distillation purification system; where the gas purification unit is operative to separate carbon dioxide from other contaminants present in the flue gas stream; and where the gas purification unit is operative to recycle the contaminants to the chemical looping system in the form of a vent gas that provides lift for reactants in the reducer.

Abstract: A chemical looping system that contains an oxidizer and a reducer is in fluid communication with a gas purification unit. The gas purification unit has at least one compressor, at least one dryer; and at least one distillation purification system; where the gas purification unit is operative to separate carbon dioxide from other contaminants present in the flue gas stream; and where the gas purification unit is operative to recycle the contaminants to the chemical looping system in the form of a vent gas that provides lift for reactants in the reducer.

Abstract: An air infiltration abatement system (300) for a power plant (10) includes a recirculated flue gas source (175), a recirculated flue gas supply line (310) connected to the recirculated flue gas source (175) and a power plant component. The power plant component has a leakage area in fluid communication with the recirculated flue gas supply line (310). The recirculated flue gas source (175) receives a combustion flue gas (75) from an oxygen fired boiler (20) of the power plant (10), and provides the combustion flue gas (75) to the recirculated flue gas supply line (310). The recirculated flue gas supply line (310) supplies the combustion flue gas (75) as a recirculated flue gas (330) to the oxygen fired boiler (20) via the leakage area of the power plant component.

Abstract: A hot solids process selectively operable for purposes of generating at least one predetermined output based on what the specific nature of the primary purpose of the hot solids process is for which the at least one predetermined output that is selected from a multiplicity of predetermined outputs, such as H2 and CO2, is being produced, and wherein such primary purpose of the hot solids process is designed to be pre-selected from a group of primary purposes of the hot solids process that includes at least two of the generation of H2 for electric power purposes, the generation of SynGas for electric power production as well as for other industrial uses, the production of steam for electric power generation as well as for other uses, the production of process heat, the production of CO2 for agricultural purposes, and the generation of a feedstock such as H2 for use for the production of liquid hydrocarbons.

Abstract: A combustor 110 is operative to effect therewith the combustion of fossil fuel 114? in order to thereby both heat to a working fluid 102 and generate a flue gas 104. An air preheater 144 receives the flue gas 104 generated in the combustor 110. A blower 180 causes air 188 to flow to the air preheater 144 when operating in an air fired mode, and causes both O2 and recycled flue gas 188? to flow when operating in the O2 firing mode. The air preheater 144 is operative to transfer heat from the flue gas 150 received thereby to the air 188 that is received when operating in an air fired mode or to both the received O2 and the recycled flue gas 188? that is received when operating in the O2 firing mode in order to thereby effect a preheating of the air 188 or of both the O2 and recycled flue gas, 188? depending upon the specific nature of the mode of operation thereof, and to thereby effect therewith a cooling of the flue gas received thereby.

Abstract: A combustor 110 combust a fluidized bed of fossil fuel 114, 114? to heat a working fluid 102 and generate flue gas 104. An air preheater 144 has first and second gas passageways 144a, 144b for respectively directing the generated flue gas 150 and another gas 250 with captured CO2 generated by combustion outside of the combustor 110. When operated in a non-CO2 capture, the air preheater 144 receives the flue gas 150, but not the other gas 250, and the first gas passageway 144a directs the flue gas 150 so as to preheat the air 188. However, when operated in the CO2 capture mode, the air preheater 144 receives the flue gas 150 and the other gas 250, and the second gas passageway 144b also directs the other gas 250 so as to preheat the air 188?. In either mode, the preheated air 188, 188? is applied by the combustor 110 to fluidize a bed of fossil fuel 114, 114?.

Abstract: A method for managing an amount of energy utilized by a carbon dioxide capture system that includes providing a fuel and a feed stream including oxygen to a combustion system. The feed stream includes a portion of a flue gas stream generated upon combustion of the fuel in the combustion system. The flue gas stream is subjected to a carbon dioxide capture system to remove carbon dioxide therefrom and an amount of at least one of an oxygen stream or the portion of the flue gas stream introduced to the feed stream is adjusted such that the feed stream maintains an oxygen concentration in a range of between 10% to 90% by volume and the carbon dioxide capture system operates at an energy load between about 1.4 GJ/ton of carbon dioxide and about 3.0 GJ/ton of carbon dioxide.

Abstract: In a retrofit system for hot solids combustion and gasification, a chemical looping system includes an endothermic reducer reactor 12 having at least one materials inlet 22 for introducing carbonaceous fuel and CaCO3 therein and a CaS/gas outlet 26. A first CaS inlet 40 and a first CaSO4 inlet 64 are also defined by the reducer reactor 12. An oxidizer reactor 14 is provided and includes an air inlet 68, a CaSO4/gas outlet 46, a second CaS inlet 44, and a second CaSO4 inlet 66. A first separator 30 is in fluid communication with the CaS/gas outlet 26 and includes a product gas and a CaS/gas outlet 32 and 34 from which CaS is introduced into said first and second CaS inlets. A second separator 50 is in fluid communication with the CaSO4/gas outlet 46 and has an outlet 52 for discharging gas therefrom, and a CaSO4 outlet from which CaSO4 is introduced into the first and second CaSO4 inlets 62, 66.

Abstract: An air infiltration abatement system (300) for a power plant (10) includes a recirculated flue gas source (175), a recirculated flue gas supply line (310) connected to the recirculated flue gas source (175) and a power plant component. The power plant component has a leakage area in fluid communication with the recirculated flue gas supply line (310). The recirculated flue gas source (175) receives a combustion flue gas (75) from an oxygen fired boiler (20) of the power plant (10), and provides the combustion flue gas (75) to the recirculated flue gas supply line (310). The recirculated flue gas supply line (310) supplies the combustion flue gas (75) as a recirculated flue gas (330) to the oxygen fired boiler (20) via the leakage area of the power plant component.

Abstract: A hot solids process wherein a predetermined output, which is designed to be suitable for use as an input to a petrochemical process, is capable of being generated through the use of the hot solids process. The mode of operation of such a hot solids process is designed to be such that preferably a portion of the otherwise normally unusable product output, which is produced from a petrochemical process, is designed to be utilized as an input to the hot solids process for purposes of generating from the hot solids process the predetermined output that is suitable for use as an input to a petrochemical process.

Abstract: A hot solids process operable selectively for combustion purposes and gasification purposes wherein a pre-identified product is selected from a group of products to be generated through the use of the hot solids process. Based on the nature of the pre-identified product, which is to be generated through the use of the hot solids process, a specific fuel from which the pre-identified product is capable of being derived is selected from a group of fuels. Then, from a group of reactors there is selected a first reactor, which is operable for generating in the first reactor the pre-identified product as an output from the first reactor. Thereafter, from a group of reactors, there is selected a second reactor, which is operable for effecting in the second reactor the conversion of air and of a predetermined carrier selected from a group of carriers to produce a predefined output from the second reactor.

Abstract: A hot solids process selectively operable for purposes of generating a predetermined output based on the nature of the specific application for which the predetermined output is being produced, and wherein such specific application is designed to be pre-selected from a group of specific applications that includes a new steam generator application, a retrofit steam generator application, a CO2 capture ready Hot Solids Combustion application, a CO2 capture ready hot solids gasification application, a CO2 capture hot solids combustion application, a CO2 capture hot solids gasification application, a partial CO2 capture hot solids combustion application, and a partial CO2 capture hot solids gasification application.

Abstract: A hot solids process selectively operable for purposes of generating at least one predetermined output based on what the specific nature of the primary purpose of the hot solids process is for which the at least one predetermined output that is selected from a multiplicity of predetermined outputs, such as H2 and CO2, is being produced, and wherein such primary purpose of the hot solids process is designed to be pre-selected from a group of primary purposes of the hot solids process that includes at least two of the generation of H2 for electric power purposes, the generation of SynGas for electric power production as well as for other industrial uses, the production of steam for electric power generation as well as for other uses, the production of process heat, the production of CO2 for agricultural purposes, and the generation of a feedstock such as H2 for use for the production of liquid hydrocarbons.

Abstract: In a retrofit system for hot solids combustion and gasification, a chemical looping system includes an endothermic reducer reactor 12 having at least one materials inlet 22 for introducing carbonaceous fuel and CaCO3 therein and a CaS/gas outlet 26. A first CaS inlet 40 and a first CaSO4 inlet 64 are also defined by the reducer reactor 12. An oxidizer reactor 14 is provided and includes an air inlet 68, a CaSO4/gas outlet 46, a second CaS inlet 44, and a second CaSO4 inlet 66. A first separator 30 is in fluid communication with the CaS/gas outlet 26 and includes a product gas and a CaS/gas outlet 32 and 34 from which CaS is introduced into said first and second CaS inlets. A second separator 50 is in fluid communication with the CaSO4/gas outlet 46 and has an outlet 52 for discharging gas therefrom, and a CaSO4 outlet from which CaSO4 is introduced into the first and second CaSO4 inlets 62, 66.

Abstract: A combustor 110 is operative to effect therewith the combustion of fossil fuel 114? in order to thereby both heat to a working fluid 102 and generate a flue gas 104. An air preheater 144 receives the flue gas 104 generated in the combustor 110. A blower 180 causes air 188 to flow to the air preheater 144 when operating in an air fired mode, and causes both O2 and recycled flue gas 188? to flow when operating in the O2 firing mode. The air preheater 144 is operative to transfer heat from the flue gas 150 received thereby to the air 188 that is received when operating in an air fired mode or to both the received O2 and the recycled flue gas 188? that is received when operating in the O2 firing mode in order to thereby effect a preheating of the air 188 or of both the O2 and recycled flue gas, 188? depending upon the specific nature of the mode of operation thereof, and to thereby effect therewith a cooling of the flue gas received thereby.

Abstract: A combustor 110 combust a fluidized bed of fossil fuel 114, 114? to heat a working fluid 102 and generate flue gas 104. An air preheater 144 has first and second gas passageways 144a, 144b for respectively directing the generated flue gas 150 and another gas 250 with captured CO2 generated by combustion outside of the combustor 110. When operated in a non-CO2 capture, the air preheater 144 receives the flue gas 150, but not the other gas 250, and the first gas passageway 144a directs the flue gas 150 so as to preheat the air 188. However, when operated in the CO2 capture mode, the air preheater 144 receives the flue gas 150 and the other gas 250, and the second gas passageway 144b also directs the other gas 250 so as to preheat the air 188?. In either mode, the preheated air 188, 188? is applied by the combustor 110 to fluidize a bed of fossil fuel 114, 114?.

Abstract: A system (100) for regenerating an absorbent solution, including: steam (128) produced by a boiler (130); a set of pressure turbines (132) fluidly coupled to the boiler; a siphoning mechanism (134) for siphoning at least a portion of the steam produced by the boiler; and a regenerating system (118) fluidly coupled to the siphoning mechanism, wherein siphoned steam is utilized as a heat source for the regenerating system.

Abstract: A fossil fuel fired combustion apparatus and a method for operating the fossil fuel fired combustion apparatus are provided which offer the flexibility to use carbon dioxide (CO2) both as a desirable end product and as support to the combustion process. The method includes the step of introducing a substantially pure oxygen feed stream into the fossil fuel fired combustion apparatus and the step of combusting a fossil fuel in the presence of the substantially pure oxygen feed stream to produce a flue gas having carbon dioxide and water vapor as its two largest constituent elements by volume. The method also includes the step of passing the flue gas through an oxygen feed stream pre-heater at which heat from the flue gas is transferred to the oxygen feed stream. Furthermore, the method includes the step of separating the flue gas into an end product portion and a recycling portion.

Abstract: A combined cycle power plant incorporating a coal gasifier as the energy source. The gases leaving the coal gasifier pass through a liquid couplant heat exchanger before being used to drive a gas turbine. The exhaust gases of the gas turbine are used to generate both high pressure and low pressure steam for driving a steam turbine, before being exhausted to the atmosphere.