CROSS-REFERENCE TO RELATED APPLICATIONS This application claims priority to copending U.S. provisional application entitled “HOT SOLIDS PROCESS SELECTIVELY OPERABLE BASED ON THE TYPE OF APPLICATION THAT IS INVOLVED” having U.S. Ser. No. 61/165,069, filed Mar. 31, 2009, which is entirely incorporated herein by reference.
TECHNICAL FIELD This invention relates generally to hot solids processes that are capable of being selectively operated for purposes of generating a predetermined output based on the nature of the specific application for which the predetermined output is being produced. More particularly, the present invention relates to such a hot solids process, which is 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, wherein such specific application is designed to be pre-selected from a group of specific applications that includes at least two of 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.
BACKGROUND The World today faces a critical challenge as all nations strive to satisfy basic human requirements—food, shelter, clothing and work—that are so dependent on adequate supplies of energy. The great increase in the use of energy has been met mostly by fossil fuels—primarily, coal, oil and gas. The belief is that environmental concerns, security of supply, and economic impacts must all be balanced as the demand for energy continues to increase. Real economic growth and energy use nevertheless still remain inextricably linked.
While the quest for ultimate solutions to provide adequate energy supplies continues, near term, interim solutions must be considered for meeting the immediate growth in demand for energy. Technological improvements in the mining, drilling, moving, processing, and using of fossil fuels can, of course, stretch energy resource reserves, as can a determined effort at conservation of energy. Similarly, the utilization of advanced clean fossil fuel technologies involving the employment of various forms of hot solids processes such as, by way of exemplification and not limitation, fossil fuel gasification, fluidized-bed combustion, or hybrid combustion-gasification fossil fuel technologies are capable of having the effect of that of widening the use of the World's vast fossil fuel resources.
In accordance with the mode of operation of electrical power generation systems, as is well known to most, the steam that is produced by steam generators, which are employed in such electrical power generation systems, from the combustion of fossil fuel therein is designed to be employed in steam turbines. Such steam, which commonly is both at a high temperature and at a high pressure, is expanded in the aforementioned steam turbine in order to thereby effect a rotation of the steam turbine. Such rotation of the steam turbine in turn is operative in a known manner to cause a generator that is suitably operatively connected to the steam turbine to rotate as well. Then, when the generator undergoes such rotation, a conductor is made to move through a magnetic field thereby causing an electric current to be generated. The aforedescribed mode of operation is fundamentally the basis upon which electrical power generation systems continue to be predicated even to this day.
In an effort to realize higher efficiencies for electrical power generation systems, attempts have been known to have been made to increase the temperatures and the pressures at which the steam generators that are employed in such electrical power generation systems are capable of being operated. Such efforts to date have resulted in steam generators being supplied commercially for employment in electrical power generation systems that are capable of being operated at subcritical pressure conditions or that are capable of being operated at supercritical pressure conditions. Improvements in the strength of the materials from which such steam generators, which are intended for employment in electrical power generation systems, are designed to be constructed have permitted such materials, and thus such steam generators, to be operated both at such higher temperatures and at such higher pressures.
Discussing further the advanced clean fossil fuel technologies to which reference has been had above previously wherein various forms of hot solids processes are employed, and in particular to that of fossil fuel gasification technologies, attention is first directed in this connection, by way of exemplification and not limitation, to U.S. Pat. No. 2,602,809, which issued on Jul. 8, 1952 to The M. W. Kellogg Company. The teachings of U.S. Pat. No. 2,602,809 are considered to be representative of an exemplification of an early development in the continuing development of fossil fuel gasification technologies of the type wherein hot solids processes are employed. To this end, in accordance with the teachings thereof, the teachings of U.S. Pat. No. 2,602,809 are directed to a process, which is said to be particularly suited for the gasification of low-grade solid carbon-containing materials. More specifically, insofar as the mode of operation of the process to which the teachings of U.S. Pat. No. 2,602,809 are directed is concerned, the solid carbon-containing materials are designed to be oxidized in order to convert such solid carbon-containing materials to carbon oxides by virtue of the indirect oxidation thereof with air in such a manner that the nitrogen of the air does not contaminate the product gas. Such gasification of the solid carbon-containing materials is accomplished by virtue of the alternate oxidation and reduction of a fluidized metal oxide. According to the teachings of U.S. Pat. No. 2,602,809, solid fuels are subjected to being converted to gases as a consequence of the contacting by a metal oxide with finely-divided solid carbon-containing materials under conditions such as to cause the metal oxide to be reduced and the carbon of the solid fuel to be oxidized to carbon oxides, with the metal oxide being the principal source of oxygen that is required for the oxidation of the carbon. Then, after the metal oxide has been reduced, the reduced metal oxide is subjected to being re-oxidized whereupon the process cycle is capable of being repeated once again.
With further regard to the fossil fuel gasification technologies of the advanced clean fossil fuel technologies to which reference has been had above previously wherein various forms of hot solids processes are employed, attention is next directed herein, by way of exemplification and not limitation, to U.S. Pat. No. 4,602,573, which issued on Jul. 29, 1986 to Combustion Engineering, Inc. The teachings of U.S. Pat. No. 4,602,573 are considered to be representative of an exemplification of a further development in the continuing evolution of fossil fuel gasification technologies of the type wherein hot solids processes are employed. To this end, in accordance with the teachings thereof, the teachings of U.S. Pat. No. 4,602,573 are stated to be directed to a method of gasifying and combusting a carbonaceous fuel and, more particularly to an integrated process wherein a sulfur and nitrogen-bearing carbonaceous fuel is gasified to produce a carbon monoxide-rich low BTU fuel gas that is designed to be subsequently combusted with additional carbonaceous fuel in a steam generator. More specifically, insofar as the mode of operation of the process to which the teachings of U.S. Pat. No. 4,602,573 are directed is concerned, a first portion of sulfur and nitrogen-bearing carbonaceous fuel is gasified in a gasification reactor in a reducing atmosphere of air to produce a hot, char-containing, carbon monoxide-rich fuel gas having a low BTU content. Thereafter, a sulfur capturing material is introduced into the gasification reactor so that the gasifying of the carbonaceous fuel is carried out in the presence of the sulfur capturing material whereby a substantial portion of the sulfur in the carbonaceous fuel being gasified is captured by the sulfur capturing material.
Attention will next be directed herein further to the advanced clean fossil fuel technologies to which reference has been had above previously wherein various forms of hot solids processes are employed and in particular to that of fluidized-bed combustion technologies. Thus, more specifically, attention is therefore directed in this connection, by way of exemplification and not limitation, to U.S. Pat. No. 4,111,158, which issued on Sep. 5, 1978 to Metallgesellschaft Aktiengesellschaft. The teachings of U.S. Pat. No. 4,111,158 are considered to be representative of an exemplification of an early development in the continuing development of the fluidized-bed combustion technologies of the type wherein hot solids processes are employed. To this end, in accordance with the teachings thereof, the teachings of U.S. Pat. No. 4,111,158 are stated to be directed to a method of and an apparatus for carrying out an exothermic process in which a solid feed contains a combustible such as, for example, carbonaceous or sulfurous compounds. Continuing, insofar as the mode of operation of the method of and the apparatus for to which the teachings of U.S. Pat. No. 4,111,158 are directed is concerned, the combustible compounds of the solid feed are designed to be burned under approximately stoichiometric conditions in a fluidized bed. Thereafter, the solids, which are produced as a consequence of such burning of the combustible compounds of the solid feed and which are withdrawn from the fluidized bed are caused to be recycled back to the fluidized bed, while the heat that is produced from such burning of the combustible compounds of the solid feed is available to be recovered.
Regarding further the fluidized-bed combustion technologies of the advanced clean fossil fuel technologies to which reference has been had above previously wherein various forms of hot solids processes are employed, attention is next directed herein, by way of exemplification and not limitation, to U.S. Pat. No. 5,533,471, which issued on Jul. 9, 1996 to A. Ahlstrom Corporation. The teachings of U.S. Pat. No. 5,533,471 are considered to be representative of an exemplification of a further development in the continuing evolution of fluidized-bed combustion technologies of the type wherein hot solids processes are employed. To this end, in accordance with the teachings thereof, the teachings of U.S. Pat. No. 5,533,471 are stated to be directed to a system and to a method that allow the temperature of the fluidized bed reactor to be controlled efficiently, allowing adequate heat transfer surface area for cooling of solid materials. More specifically, insofar as the mode of operation of the system and of the method to which the teachings of U.S. Pat. No. 5,533,471 are directed is concerned, a circulating (fast) fluidized bed and a bubbling (slow) fluidized bed are utilized. Continuing, these two (2) fluidized beds are mounted adjacent each other with first and second interconnections between them, typically with the fluidizing gas introducing grid of the bubbling fluidized bed being below that of the circulating fluidized bed. Because the bubbling fluidized bed has a substantially constant density throughout, with a clear demarcation line at the top thereof, the first interconnection is provided above the top of the bubbling fluidized bed so that the pressure and density conditions between the two (2) fluidized beds result in a flow of particles from the circulating fluidized bed to the bubbling fluidized bed through the first interconnection. However, since the average density in the bubbling fluidized bed is higher than the density in the circulating fluidized bed, the pressure and density conditions cause the particles after treatment in the bubbling fluidized bed (e.g., after the cooling of the particles therein) to return to the circulating fluidized bed through the second interconnection.
Discussing further the advanced clean fossil fuel technologies to which reference has been had above previously wherein various forms of hot solids processes are employed, and in particular that of hybrid combustion-gasification technologies, attention is first directed in this connection, by way of exemplification and not limitation, to U.S. Pat. No. 4,272,399, which issued on Jun. 8, 1981 to the Monsanto Company. The teachings of U.S. Pat. No. 4,272,399 are considered to be representative of an exemplification of an early development in the continuing evolution of the hybrid combustion-gasification technologies of the type wherein hot solids processes are employed. To this end, in accordance with the teachings thereof, the teachings of U.S. Pat. No. 4,272,399 are stated to be directed to a unified process for producing high purity synthesis gas from carbon-containing materials. More specifically, insofar as the mode of operation of the unified process to which the teachings of U.S. Pat. No. 4,272,399 are directed is concerned, a metal-oxygen containing material, which can be characterized as a heat and oxygen carrier and which can be referred to generally as an oxidant, is used as the transfer agent of oxygen and heat for oxidatively gasifying carbon-containing material. Continuing, steam, carbon dioxide, synthesis gas or mixtures thereof are employed to fluidize and transport the oxidant through an up-flow, co-current system. Thus, in accordance with the mode of operation of the subject unified process, synthesis gas is first oxidized and heated by the oxidant to form water and carbon dioxide in an oxidant reducing zone prior to contact of the oxidant and gases with the carbon-containing material in a gasifying zone. In addition, the carbon-containing materials are oxidized to predominately carbon monoxide and hydrogen in a manner such that the nitrogen contained in the air does not contaminate the product synthesis gas. Furthermore, the gasification of the carbon-containing material is accomplished by the alternate oxidation and reduction of a fluidized oxidant. Then, after such gasification, the reduced oxidant, which may be in the form of the elemental metal or lower oxidized state is re-oxidized in an oxidizing zone and the cycle is then repeated.
Regarding further the hybrid combustion-gasification technologies of the advanced clean fossil fuel technologies to which reference has been had above previously wherein various forms of hot solids processes are employed, attention is next directed herein, by way of exemplification and not limitation, to U.S. Pat. No. 7,083,658, which issued on Aug. 1, 2006 to ALSTOM Technology Ltd., which is incorporated herein by reference. The teachings of U.S. Pat. No. 7,083,658 are considered to be representative of an exemplification of a further development in the continuing evolution of hybrid combustion-gasification technologies of the type wherein hot solids processes are employed. To this end, in accordance with the teachings thereof, the teachings of U.S. Pat. No. 7,083,658 are stated to be directed to apparatus utilizing fossil fuels, biomass, petroleum coke, or any other carbon bearing fuel to produce hydrogen for power generation, which minimizes or eliminates the release of carbon dioxide (CO2). More specifically, insofar as the mode of operation of the apparatus to which the teachings of U.S. Pat. No. 7,083,658 are directed is concerned, a gasifier is provided for producing a gas product from a carbonaceous fuel, which comprises a first chemical process loop including an exothermic oxidizer reactor and an endothermic reducer reactor. Continuing, the exothermic oxidizer reactor has a CaS inlet, a hot air inlet and a CaSO4/waste gas outlet. Whereas, the endothermic reducer reactor has a CaSO4 inlet in fluid communication with the exothermic oxidation reactor CaSO4/waste gas outlet, a CaS/gas product outlet in fluid communication with the exothermic oxidizer reactor CaS inlet, and a materials inlet for receiving the carbonaceous fuel. Moreover, CaS is oxidized in air in the exothermic oxidizer reactor to form hot CaSO4, which is discharged to the endothermic reducer reactor. Furthermore, hot CaSO4 and carbonaceous fuel that is received in the endothermic reducer reactor undergo an endothermic reaction utilizing the heat content of the CaSO4 with the carbonaceous fuel stripping the oxygen from the CaSO4 to form CaS and the gas product. Thereafter, the CaS is discharged to the exothermic oxidizer reactor, and with the gas product being discharged from the first chemical process loop.
It is, therefore, an object of the present invention to provide a hot solids process that is selectively operable based on the type of application that is involved.
It is also an object of the present invention to provide such a hot solids process that is capable of being selectively operated for purposes of generating a predetermined output.
It is another object of the present invention to provide such a hot solids process that is capable of being selectively operated based on the nature of the specific application for which a predetermined output is being produced for purposes of generating such a predetermined output.
It is still another object of the present invention to provide such a hot solids process, which is capable of being selectively operated 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.
A further object of the present invention is to provide such a hot solids process that is capable of being selectively operated for purposes of generating a predetermined output based on the nature of the specific application for which such a predetermined output is being produced, and wherein such specific application is designed to be pre-selected from a group of specific applications included in which are 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.
Yet another object of the present invention is to provide such a hot solids process that is relatively inexpensive to provide, that is relatively uncomplicated to employ, and that is characterized by the great versatility, which such a hot solids process embodies, insofar as concerns the specific application for which a predetermined output, which it is desired to produce for such a specific application, is capable of being generated through the use of the hot solids process of the present invention.
SUMMARY OF THE INVENTION In accordance with the present invention a hot solids process is provided, which is 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 included in which are at least two of 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. To this end, the mode of operation in accordance with the present invention of such a hot solids process is such that preferably a limestone based sorbent, such as, by way of exemplification and not limitation, CaS, is designed to be combusted in an oxidizing reactor, such oxidizing reactor preferably, by way of exemplification and not limitation, being a circulating bed reactor, in order to thereby produce hot CaSO4 from the combustion of such limestone based sorbent. This hot CaSO4 is then in turn designed to be employed in a reducing reactor, such reducing reactor preferably, by way of exemplification and not limitation, being a circulating bed reactor, for purposes of generating a predetermined output based on the nature of the pre-selected specific application for which such predetermined output is being produced.
In accordance with a second exemplary embodiment of the mode of operation of the hot solids process of the present invention, wherein the fuel that is designed to be combusted in accordance therewith comprises a solid carbonaceous fuel, such as, by way of exemplification and not limitation, coal, and wherein the pre-selected specific application for which the predetermined output that is being generated from this second exemplary embodiment of the mode of operation of the hot solids process of the present invention, which is being produced, is a retrofit steam generator application, and with, in such a case, the existing steam generator being made to function in the role of an oxidizing reactor. To this end, in order to thereby be able to function in the role of such an oxidizing reactor for purposes of the second exemplary embodiment of the mode of operation of the hot solids process of the present invention, the existing steam generator preferably is modified so as to thereby embody either a cyclone, which is designed to be capable of operating in the manner of a reactor, or a curvilinear separator, which is also designed to be capable of operating in the manner of a reactor.
With further regard to the discussion of the second exemplary embodiment of the mode of operation of the hot solids process of the present invention, when the existing steam generator is so suitably modified in order to thereby embody a curvilinear separator, such curvilinear separator is designed to be operative in the manner of an oxidizing reactor for purposes of effecting the combustion therewithin of an oxide, which is designed to be transported with excess air to the curvilinear separator from the reducing reactor that is employed in this second exemplary embodiment of the mode of operation of the hot solids process of the present invention. The gas, which is produced in the oxidizing reactor, i.e., the curvilinear separator, from the combustion of the oxide and the air therewithin, in turn is made to flow through the existing steam generator so as to thereby enable heat to be absorbed within the existing steam generator from such gas. While, any ash and/or solid particles, which may be produced from the combustion of the oxide and the air in the oxidizing reactor, i.e., in the curvilinear separator with which the existing steam generator has been suitably modified so as to thereby embody such curvilinear separator, that do not become entrained with the aforementioned gas, which is made to flow through the existing steam generator, are designed to be collected at the bottom of the existing steam generator.
BRIEF DESCRIPTION OF THE DRAWINGS FIG. 1 is a schematic diagram of a hot solids process that functions in accordance with the present invention;
FIG. 2 is a schematic diagram of a first exemplary embodiment of the mode of operation of a hot solids process that functions in accordance with the present invention;
FIGS. 3a and 3b are each a schematic diagram embodying a different form of construction of a second exemplary embodiment of the mode of operation of a hot solids process that functions in accordance with the present invention;
FIG. 4 is a schematic diagram of a third exemplary embodiment of the mode of operation of a hot solids process that functions in accordance with the present invention;
FIG. 5 is a schematic diagram of a fourth exemplary embodiment of the mode of operation of a hot solids process that functions in accordance with the present invention;
FIG. 6 is a schematic diagram of a fifth exemplary embodiment of the mode of operation of a hot solids process that functions in accordance with the present invention;
FIG. 7 is a schematic diagram of a sixth exemplary embodiment of the mode of operation of a hot solids process that functions in accordance with the present invention;
FIG. 8 is a schematic diagram of a seventh exemplary embodiment of the mode of operation of a hot solids process that functions in accordance with the present invention; and
FIG. 9 is a schematic diagram of an eighth exemplary embodiment of the mode of operation of a hot solids process that functions in accordance with the present invention.
DETAILED DESCRIPTION Referring now to FIG. 1 of the drawings, there is depicted therein a schematic diagram of a hot solids process, generally denoted by the reference numeral 10 in FIG. 1 of the drawings, that is designed to be operable in accordance with the present invention for purposes of generating a predetermined output, and with the latter predetermined output being denoted by the arrow 12 in FIG. 1 of the drawings, based on the nature of the specific application for which the predetermined output is being produced. In accordance with the mode of operation of the hot solids process of the present invention that is schematically depicted in FIG. 1 of the drawings, the specific application, based upon the nature of which the predetermined output is being produced, is designed to be pre-selected from a group of specific applications included in which are at least two of 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.
The hot solids process 10 of the present invention in accordance with the preferred mode of operation thereof is designed to utilize air; a solid carbonaceous fuel, such as, by way of exemplification and not limitation, coal; a source of calcium (e.g., calcium oxide); and steam to effect therewith the generation of the predetermined output 12, based on the nature of the pre-selected specific application for which such predetermined output 12 is being produced. To this end, based on the nature of the specific application that in accordance with the present invention is designed to be pre-selected, such predetermined output 12, which is produced in accordance with the mode of operation of the hot solids process 10 of the present invention, is designed such as to be either CO2 that after being so produced is capture ready or CO2 that after being so produced is capable of being captured or CO2 that after being so produced is capable of being partially captured. Moreover, the heat, which is generated through the use of the hot solids process 10 of the present invention in accordance with the preferred mode of operation thereof, is in addition capable of being employed to make steam, which is suitable for use for power generation purposes.
With further reference to FIG. 1 of the drawings, a reducing reactor, denoted generally by the reference numeral 14 in FIG. 1, and an oxidizing reactor, denoted generally by the reference numeral 16 in FIG. 1, are each designed to be employed in the hot solids process 10 of the present invention, in accordance with the preferred mode of operation thereof. Continuing, in accordance with the preferred embodiment of the hot solids process 10 of the present invention, solid carbonaceous fuel, such as, by way of exemplification and not limitation, coal, and with the latter coal being denoted by the arrow 18 in FIG. 1, which is supplied as an input to the reducing reactor 14, is designed to be burned using air indirectly. To this end, a source of calcium, and with the latter source of calcium being denoted by the arrow 20 in FIG. 1, which is designed to be added, in accordance with the preferred mode of operation, to the hot solids process 10 of the present invention, is also supplied, by way of exemplification and not limitation, as an input to the reducing reactor 14. However, such source of calcium 20 could equally well be supplied elsewhere in the hot solids process 10 of the present invention other than as an input to the reducing reactor 14, without departing from the essence of the present invention. Such source of calcium 20 (i.e., calcium oxide), which may be selected from sources of calcium, such as, limestone (CaCO3), or lime (CaO), or gypsum, or the spent bed material from a circulating bed boiler, preferably, by way of exemplification and not limitation, comprises limestone (CaCO3). With further reference thereto, such limestone (CaCO3) 20, which in accordance with the preferred mode of operation of the hot solids process 10 of the present invention is added to the hot solids process 10, is designed to be operative to capture in the reducing reactor 14 the sulfur (S), which is contained in the solid carbonaceous fuel 18, such as to thereby produce calcium sulfide (CaS) therefrom in the reducing reactor 14. Such calcium sulfide (CaS), as denoted by the arrow 22 in FIG. 1, is then made to exit from the reducing reactor 14 as an output therefrom, whereupon such calcium sulfide (CaS) 22 is designed to be supplied as an input to the oxidizing reactor 16. In the oxidizing reactor 16, this calcium sulfide (CaS) 22 is burned in a heat liberating reaction with air, and with the latter air being denoted by the arrow 24 in FIG. 1, which is designed to be supplied as an input to the oxidizing reactor 16, such as to thereby effect the production of calcium sulfate (CaSO4) in the oxidizing reactor 16. This calcium sulfate (CaSO4), as is denoted by the arrow 26 in FIG. 1, is then made to exit as an output from the oxidizing reactor 16, whereupon this calcium sulfate (CaSO4) 26 is designed to be cycled to the reducing reactor 14 as an input thereto for purposes of thereby providing therefrom the supply of oxygen and of heat that is required both in order to burn the solid carbonaceous fuel 18 and in order to reduce the calcium sulfate (CaSO4) 26 to calcium sulfide (CaS) 22 in the reducing reactor 14 such as to thereby permit a continuous recycling thereof to be had. The burning of the solid carbonaceous fuel 18 in the reducing reactor 14 is designed to be such that the predetermined output 12 is thus generated in the reducing reactor 14, and with the carbon and the hydrogen contained in the solid carbonaceous fuel 18 being converted, in the course of such burning of the solid carbonaceous fuel 18, to a product gas consisting of CO2 and H2O. This H2O is then capable of being removed from such product gas thereby leaving the remainder of such product gas in a suitable form so as to be capable of functioning as the predetermined output 12, which through the use of the hot solids process 10 of the present invention is generated, based on the nature of the pre-selected specific application for which such predetermined output 12 is being produced, be such pre-selected specific application a new steam generator application or a retrofit steam generator application or a CO2 capture ready Hot Solids Combustion application or a CO2 capture ready Hot Solids Gasification application or a CO2 capture Hot Solids Combustion application or a CO2 capture Hot Solids Gasification application or a partial CO2 capture Hot Solids Combustion application or a partial CO2 capture Hot Solids Gasification application.
Reference will next be had herein to FIG. 2 of the drawings wherein there is depicted therein a schematic diagram of a first exemplary embodiment, generally denoted by the reference numeral 28 in FIG. 2 of the drawings, of the mode of operation of the hot solids process 10 of the present invention that is designed to be operable in accordance with the present invention for purposes of generating a predetermined output, and with the latter predetermined output being denoted by the arrows 30 and 31 in FIG. 2 of the drawings, based on the nature of the pre-selected specific application for which the predetermined outputs 30 and 31 are being produced being a new steam generator application. With further reference to FIG. 2 of the drawings, a reducing reactor, denoted generally by the reference numeral 32 in FIG. 2, and an oxidizing reactor, denoted generally by the reference numeral 34 in FIG. 2, are each designed to be employed in the hot solids process 10 of the present invention, in accordance with the first exemplary embodiment 28 of the mode of operation of the hot solids process 10 of the present invention that is operable in accordance with the present invention for purposes of generating the predetermined outputs 30 and 31, based on the nature of the pre-selected specific application for which the predetermined outputs 30 and 31 are being produced being a new steam generator application. The inputs to the oxidizing reactor 34, which is employed in this first exemplary embodiment 28 of the mode of operation of the hot solids process 10 of the present invention when the fuel that is designed to be employed in accordance therewith comprises a solid carbonaceous fuel, such as, by way of exemplification and not limitation, coal, and when the pre-selected specific application for which the predetermined outputs 30 and 31, which are being generated from this first exemplary embodiment 28 of the mode of operation of the hot solids process 10 of the present invention, are being produced is a new steam generator application, includes CaS, and with the latter CaS being denoted by the arrow 36 in FIG. 2, and air, and with the latter air being denoted by the arrow 38 in FIG. 2. Continuing, the outputs from such an oxidizing reactor 34 in such a case include ash, and with the latter ash being denoted by the arrow 48 in FIG. 2; CaSO4, to which reference will be had further hereinafter that is denoted by the arrow 46 in FIG. 2; and N2, and with the latter N2 being denoted by the arrow 50 in FIG. 2.
Whereas, the inputs to the reducing reactor 32 that is employed in this first exemplary embodiment 28 of the mode of operation of the hot solids process 10 of the present invention when the fuel that is designed to be employed in accordance therewith comprises a solid carbonaceous fuel, such as, by way of exemplification and not limitation, coal, and when the pre-selected specific application, for which the predetermined outputs 30 and 31 that are being generated from this first exemplary embodiment 28 of the mode of operation of the hot solids process 10 of the present invention are being produced, is a new steam generator application, include the solid carbonaceous fuel, and with the latter solid carbonaceous fuel being denoted by the arrow 40 in FIG. 2; CaCO3, and with the latter CaCO3 being denoted by the arrow 42 in FIG. 2; steam, and with the latter steam being denoted by the arrow 44 in FIG. 2; and CaSO4, to which reference has been had hereinbefore that is denoted by the arrow 46. The steam 44, which is added to the reducing reactor 32, is designed to be operative to effect the oxidation of the CO in the product gas that is designed to be generated in the reducing reactor 32, in accordance with the first exemplary embodiment 28 of the mode of operation of the hot solids process 10 of the present invention, to CO2, while concomitantly the H2O in such product gas is reduced to H2. Thereafter, such CO2 is designed to be captured by the excess CaO that is contained in the solids, which circulate within the reducing reactor 32, so as to thereby form CaCO3 therefrom. Such CaCO3 is designed to be made to exit as the predetermined output 30 from the reducing reactor 32, and is caused to flow to the calciner, and with the latter calciner being denoted generally by the reference numeral 52 in FIG. 2. The calciner 52 is designed to be operative to cause the CO2 to be released from the predetermined output 30, wherein the predetermined output 30 is in the form of CaCO3, which is caused to flow to the calciner 52 from the reducing reactor 32, and with the heat, which is required in order to effect such release of the CO2 from the CaCO3, being supplied by the hot solids, and with the latter hot solids being denoted by the arrow 54 in FIG. 2, which are supplied to the calciner 52 from the oxidizing reactor 34. The CaO, which remains after such release of the CO2 is effected from the CaCO3 in the calciner 52, is then designed to be recycled, and with such recycling being denoted by the arrow 56 in FIG. 2, to the reducing reactor 32 for reuse therein. The remainder of the product gas, which is generated in the reducing reactor 32, in accordance with the first exemplary embodiment 28 of the mode of operation of the hot solids process 10 of the present invention, is designed to be made to exit from the reducing reactor 32 as the predetermined output 31, the latter predetermined output 31 being in the form of a CO2-free steam generator fuel, and with said CO2-free steam generator fuel then being supplied to the new steam generator, which is denoted generally by the reference numeral 58 in FIG. 2, for use therein as the fuel for the new steam generator 58.
Reference will next be had herein to FIGS. 3a and 3b of the drawings wherein there is depicted in each of these Figures a schematic diagram embodying, by way of exemplification and not limitation, a different form of construction of a second exemplary embodiment, generally denoted by the reference numeral 60 in each of FIGS. 3a and 3b of the drawings, of the mode of operation of the hot solids process 10 of the present invention, wherein the fuel that is designed to be combusted in accordance therewith comprises a solid carbonaceous fuel, such as, by way of exemplification and not limitation, coal, and wherein the pre-selected specific application, for which the predetermined output denoted by the arrow 62 in each of FIGS. 3a and 3b that is being generated from this second exemplary embodiment 60 of the mode of operation of the hot solids process 10 of the present invention is being produced, is a retrofit steam generator application. In such a case, the existing steam generator that is denoted generally by the reference numeral 64 in FIG. 3a, and the existing steam generator that is denoted generally by the reference numeral 66 in FIG. 3b, are each designed to be made to function as an oxidizing reactor. To this end, in order to thereby function as such an oxidizing reactor for purposes of the second exemplary embodiment 60 of the mode of operation of the hot solids process 10 of the present invention, the existing steam generator 64 is designed to be suitably modified so as to thereby embody a cyclone, the latter cyclone being denoted by the reference numeral 68 in FIG. 3a, which is suitably designed so as to be capable of operating in the manner of a reactor, while the existing steam generator 66 is designed to be suitably modified so as to thereby embody a curvilinear separator, the latter curvilinear separator being denoted by the reference numeral 70 in FIG. 3b, which is suitably designed so as to be capable of operating in the manner of a reactor.
Continuing with the discussion regarding the second exemplary embodiment 60 of the mode of operation of the hot solids process 10 of the present invention, when the existing steam generator 64 is suitable modified, as schematically depicted in FIG. 3a, so as to thereby embody the cyclone 68, such cyclone 68 is suitably designed so as to be operative in the manner of an oxidizing reactor for purposes of effecting therewithin the combustion of CaS, the latter CaS being denoted by the arrow 72 in FIG. 3a, which is designed so as to be capable of being transported along with excess air, the latter excess air being denoted by the arrow 74 in FIG. 3a, as inputs to the cyclone 68. The reducing reactor, which is denoted generally in each of FIGS. 3a and 3b by the reference numeral 76, is suitably designed so as to be capable of being employed for purposes of effecting in a manner, which will be described herein more fully subsequently, the generation therewithin of the predetermined output 62, based both on the fuel that is designed to be combusted being a solid carbonaceous fuel and on the pre-selected specific application, for which the predetermined output 62 is being generated, being a retrofit steam generator application. The solids, which consist mainly of CaSO4, that are produced from the combustion of the CaS 72 and the air 74 within the cyclone 68, which as depicted in FIG. 3a the existing steam generator 64 has been modified to embody, are separated from the gas, which is produced from the combustion in the cyclone 68 of the CaS 72 and the air 74. Such CaSO4 is then designed to be recycled, as denoted by the arrow 78 in FIG. 3a, from the cyclone 68 to the reducing reactor 76, wherein such CaSO4 78 is designed to be utilized along with both the solid carbonaceous fuel, such as, by way of exemplification and not limitation, coal, the latter coal being denoted by the arrow 80 in FIG. 3a, and the CaCO3, the latter CaCO3 being denoted by the arrow 82 in FIG. 3a, that are each designed to be supplied as inputs to the reducing reactor 76, for purposes of effecting the generation within the reducing reactor 76 of the predetermined output 62, based on the nature of the pre-selected specific application, being a retrofit steam generator application. Further, the gas that is produced in the cyclone 68, which as depicted in FIG. 3a the existing steam generator 64 has been suitably modified so as to thereby embody the cyclone 68, from the combustion of the CaS 72 and the air 74 in the cyclone 68, is made to flow in turn through the existing steam generator 64, as is denoted by the arrow 84 in FIG. 3a, such as to enable heat to be absorbed within the existing steam generator 64 from such gas 84. While, any ash and/or solid particles, which may be produced from the combustion of the CaS 72 and the air 74 in the cyclone 68 with which the existing steam generator 64 has been suitably modified, as is depicted in FIG. 3a, so as to thereby embody such cyclone 68, that do not become entrained with the gas 84, which is made to flow through the existing steam generator 64, are designed to be collected, as is denoted by the arrow 86 in FIG. 3a, at the bottom of the existing steam generator 64.
With further regard to the discussion of the second exemplary embodiment 60 of the mode of operation of the hot solids process 10 of the present invention, when the existing steam generator 66 is suitably modified, as schematically depicted in FIG. 3b, so as to thereby embody the curvilinear separator 70, such curvilinear separator 70 is suitably designed so as to be operative in the manner of an oxidizing reactor for purposes of effecting therewithin the combustion of CaS, the latter CaS being denoted by the arrow 86 in FIG. 3b, which is designed so as to be capable of being transported along with excess air, the latter excess air being denoted by the arrow 88 in FIG. 3b, as inputs to the curvilinear separator 70. The reducing reactor, which is denoted generally in each of FIGS. 3a and 3b by the reference numeral 76, is suitably designed so as to be capable of being employed for purposes of effecting in a manner, which will be described herein more fully subsequently, the generation therewithin of the predetermined output 62, based both on the fuel that is designed to be combusted being a solid carbonaceous fuel and on the pre-selected specific application, for which the predetermined output 62 is being generated, being a retrofit steam generator application. The solids, which consist mainly of CaSO4, that are produced from the combustion of the CaS 86 and the air 88 within the curvilinear separator 70, which as depicted in FIG. 3b the existing steam generator 66 has been modified to embody, are separated from the gas, which is produced from the combustion in the curvilinear separator 70 of the CaS 86 and the air 88. Such CaSO4 is then designed to be recycled, as is denoted by the arrow 90 in FIG. 3b, from the curvilinear separator 70 to the reducing reactor 76, wherein such CaSO4 90 is designed to be utilized along with both the solid carbonaceous fuel, such as, by way of exemplification and not limitation, coal, the latter coal being denoted by the arrow 92 in FIG. 3b, and the CaCO3, the latter CaCO3 being denoted by the arrow 94 in FIG. 3b, that are each designed to be supplied as inputs to the reducing reactor 76, for purposes of effecting the generation within the reducing reactor 76 of the predetermined output 62, based on the nature of the pre-selected specific application, being a retrofit steam generator application. Further, the gas that is produced in the curvilinear separator 70, which as depicted in FIG. 3b the existing steam generator 66 has been suitably modified so as to thereby embody the curvilinear separator 70, from the combustion of the CaS 86 and the air 88 in the curvilinear separator 70, is made to flow in turn through the existing steam generator 66, as is denoted by the arrow 96 in FIG. 3b, such as to enable heat to be absorbed within the existing steam generator 66 from such gas 96. While, any ash and/or solid particles, which may be produced from the combustion of the CaS 86 and the air 88 in the curvilinear separator 70 with which the existing steam generator 66 has been suitably modified, as is depicted in FIG. 3b, so as to thereby embody such curvilinear separator 70, that do not become entrained with the gas 96, which is made to flow through the existing steam generator 66, are designed to be collected, as is denoted by the arrow 98 in FIG. 3b, at the bottom of the existing steam generator 66.
Reference will next be had herein to FIG. 4 of the drawings wherein there is depicted therein a schematic diagram of a third exemplary embodiment, generally denoted by the reference numeral 100 in FIG. 4 of the drawings, of the mode of operation of the hot solids process 10 of the present invention that is designed to be operable in accordance with the present invention for purposes of generating a predetermined output, and with the latter predetermined output being denoted by the arrow 102 in FIG. 4 of the drawings, based on the nature of the pre-selected specific application, for which the predetermined output 102 is being produced, being a CO2 capture ready Hot Solids Combustion application. With further reference to FIG. 4 of the drawings, a reducing reactor, denoted generally by the reference numeral 104 in FIG. 4, and an oxidizing reactor, denoted generally by the reference numeral 106 in FIG. 4, are each designed to be employed in the hot solids process 10 of the present invention, in accordance with the third exemplary embodiment 100 of the mode of operation of the hot solids process 10 of the present invention that is operable in accordance with the present invention for purposes of generating the predetermined output 102, based on the nature of the pre-selected specific application, for which the predetermined output 102 is being produced, being a CO2 capture ready Hot Solids Combustion application. Continuing, in accordance with the third exemplary embodiment 100 of the mode of operation of the hot solids process 10 of the present invention, solid carbonaceous fuel, such as, by way of exemplification and not limitation, coal, the latter coal being denoted by the arrow 108 in FIG. 4, which is supplied as an input to the reducing reactor 104, is designed to be combusted using air indirectly. To this end, CaCO3, the latter CaCO3 being denoted by the arrow 110 in FIG. 4, which is designed to be added in accordance with the third exemplary embodiment 100 of the mode of operation of the hot solids process 10 of the present invention, is also supplied as an input to the reducing reactor 104. Such CaCO3 110, which is added in accordance with the third exemplary embodiment 100 of the mode of operation of the hot solids process 10 of the present invention, is designed to be operative to capture in the reducing reactor 104 the sulfur, which is contained in the solid carbonaceous fuel 108, such as to thereby produce CaS therefrom in the reducing reactor 104. The latter CaS, as is denoted by the arrow 112 in FIG. 4, is then made to exit from the reducing reactor 104 as an output therefrom, whereupon such CaS 112 is supplied as an input to the oxidizing reactor 106. In the oxidizing reactor 106 this CaS 112 is combusted in a heat liberating reaction with air, denoted by the arrow 114 in FIG. 4, which is supplied as an input to the oxidizing reactor 106, such as to thereby produce CaSO4 in the oxidizing reactor 106.
With further reference thereto, this CaSO4, as is denoted by the arrow 116 in FIG. 4, is then designed to be made to exit as an output from the oxidizing reactor 106, whereupon this CaSO4 116 is designed to be recycled to the reducing reactor 104 as an input thereto, for purposes of supplying the oxygen and the heat that is required in order to effect both the combustion of the solid carbonaceous fuel 108 and the reduction of the CaSO4 116 to CaS 112 in the reducing reactor 104 so as to thereby permit a continuous recycling thereof to be had. The combustion of the solid carbonaceous fuel 108 in the reducing reactor 104 is designed to be such that the predetermined output 102 is thus generated in the reducing reactor 104, whereby the carbon and the hydrogen that is contained in the solid carbonaceous fuel 108 is designed to be converted in the course of such combustion of the solid carbonaceous fuel 108 so as to thereby produce a product gas therefrom consisting of CO2 and H2O. The H2O is then capable of being removed from such product gas leaving the remainder of such product gas in a suitable form so as to, therefore, be capable of functioning as the predetermined output 102, which is generated through the use of the third exemplary embodiment 100 of the mode of operation of the hot solids process 10 of the present invention, such as to thus be capture ready, based on the nature of the pre-selected specific application, for which such capture ready predetermined output 102 is being produced, being a CO2 capture ready Hot Solids Combustion application.
Reference will next be had herein to FIG. 5 of the drawings wherein there is depicted therein a schematic diagram of a fourth exemplary embodiment, generally denoted by the reference numeral 118 in FIG. 5 of the drawings, of the mode of operation of the hot solids process 10 of the present invention that is designed to be operable in accordance with the present invention for purposes of generating a predetermined output, and with the latter predetermined output being denoted by the arrow 120 in FIG. 5 of the drawings, based on the nature of the pre-selected specific application, for which the predetermined output 120 is being produced, being a CO2 capture ready Hot Solids Gasification application. With further reference to FIG. 5 of the drawings, a reducing reactor, denoted generally by the reference numeral 122 in FIG. 5, and an oxidizing reactor, denoted generally by the reference numeral 124 in FIG. 5, are each designed to be employed in the hot solids process 10 of the present invention, in accordance with the fourth exemplary embodiment 118 of the mode of operation of the hot solids process 10 of the present invention that is operable in accordance with the present invention for purposes of generating the predetermined output 120, based on the nature of the pre-selected specific application, for which the predetermined output 120 is being produced, being a CO2 capture ready Hot Solids Gasification application. Continuing, in accordance with the fourth exemplary embodiment 118 of the mode of operation of the hot solids process 10 of the present invention, solid carbonaceous fuel, such as, by way of exemplification and not limitation, coal, the latter coal being denoted by the arrow 126 in FIG. 5, which is supplied as an input to the reducing reactor 122, is designed to be gasified. To this end, CaCO3, the latter CaCO3 being denoted by the arrow 128 in FIG. 5, which is designed to be added in accordance with the fourth exemplary embodiment 118 of the mode of operation of the hot solids process 10 of the present invention, is also supplied as an input to the reducing reactor 122. Such CaCO3 128, which is added in accordance with the fourth exemplary embodiment 118 of the mode of operation of the hot solids process 10 of the present invention, is designed to be operative to capture in the reducing reactor 122 the sulfur, which is contained in the solid carbonaceous fuel 126, such as to thereby produce CaS therefrom in the reducing reactor 122. The latter CaS, as is denoted by the arrow 130 in FIG. 5, is then designed to be made to exit from the reducing reactor 122 as an output therefrom, whereupon such CaS 130 is supplied as an input to the oxidizing reactor 124. In the oxidizing reactor 124 this CaS 130 is designed to be reacted. Air, the latter air being denoted by the arrow 132 in FIG. 5 is designed to be supplied as an input to the oxidizing reactor 124, so as to thereby be capable of producing CaSO4 from the reaction of the CaS 130 in the oxidizing reactor 124.
With further reference thereto, this CaSO4, as is denoted by the arrow 134 in FIG. 5, is then designed to be made to exit as an output from the oxidizing reactor 124, whereupon this CaSO4 134 is designed to be recycled to the reducing reactor 122 as an input thereto for purposes of supplying the oxygen and the heat that is required in order to effect both the gasification of the solid carbonaceous fuel 126 and the reduction of the CaSO4 134 to CaS 130 in the reducing reactor 122 so as to thereby permit a continuous recycling thereof to be had. The gasification of the solid carbonaceous fuel 126 in the reducing reactor 122 is designed to be such that the predetermined output 120 is thus generated in the reducing reactor 122, whereupon the carbon and the hydrogen that is contained in the solid carbonaceous fuel 126 is designed to be converted in the course of such gasification of the solid carbonaceous fuel 126 to a product gas including CO2 and H2O as well as CO and H2. The H2O is then capable of being removed from such product gas leaving the remainder of such product gas in a suitable form so as to, therefore, be capable of functioning as the predetermined output 120, which is generated through the use of the fourth exemplary embodiment 118 of the mode of operation of the hot solids process 10 of the present invention, such as to thus be capture ready, based on the nature of the pre-selected specific application, for which such capture ready predetermined output 120 is being produced, being a CO2 capture ready Hot Solids Gasification application.
Reference will next be had herein to FIG. 6 of the drawings wherein there is depicted therein a schematic diagram of a fifth exemplary embodiment, generally denoted by the reference numeral 136 in FIG. 6 of the drawings, of the mode of operation of the hot solids process 10 of the present invention that is designed to be operable in accordance with the present invention for purposes of generating a predetermined output, and with the latter predetermined output being denoted by the reference numeral 138 in FIG. 6 of the drawings, based on the nature of the pre-selected specific application, for which the predetermined output 138 is being produced, being a CO2 capture Hot Solids Combustion application. With further reference to FIG. 6 of the drawings, a reducing reactor, denoted generally by the reference numeral 140 in FIG. 6, and an oxidizing reactor, denoted generally by the reference numeral 142 in FIG. 6, are each designed to be employed in the hot solids process 10 of the present invention, in accordance with the fifth exemplary embodiment 136 of the mode of operation of the hot solids process 10 of the present invention that is operable in accordance with the present invention for purposes of generating the predetermined output 138, based on the nature of the pre-selected specific application, for which the predetermined output 138 is being produced, being a CO2 capture Hot Solids Combustion application. Continuing, in accordance with the fifth exemplary embodiment 136 of the mode of operation of the hot solids process 10 of the present invention, solid carbonaceous fuel, such as, by way of exemplification and not limitation, coal, the latter coal being denoted by the arrow 144 in FIG. 6, which is supplied as an input to the reducing reactor 140, is designed to be combusted using air indirectly. To this end, CaCO3, the latter CaCO3 being denoted by the arrow 146 in FIG. 6, which is designed to be added in accordance with the fifth exemplary embodiment 136 of the mode of operation of the hot solids process 10 of the present invention, is also supplied as an input to the reducing reactor 140. Such CaCO3 146, which is added in accordance with the fifth exemplary embodiment 136 of the mode of operation of the hot solids process 10 of the present invention, is designed to be operative to capture in the reducing reactor 140 the sulfur, which is contained in the solid carbonaceous fuel 144, such as to thereby produce CaS therefrom in the reducing reactor 140. The latter CaS, as is denoted by the arrow 148 in FIG. 6, is then designed to be made to exit from the reducing reactor 140 as an output therefrom, whereupon such CaS 148 is designed to be supplied as an input to the oxidizing reactor 142. In the oxidizing reactor 142, this CaS 148 is combusted in a heat liberating reaction with air, the latter air being denoted by the arrow 150 in FIG. 6, which is designed to be supplied as an input to the oxidizing reactor 142, so as to thereby be capable of producing CaSO4 in the oxidizing reactor 142.
With further reference thereto, this CaSO4, as is denoted by the arrow 152 in FIG. 6, is then designed to be made to exit as an output from the oxidizing reactor 142, whereupon this CaSO4 152 is designed to be recycled to the reducing reactor 140 as an input thereto for purposes of supplying the oxygen and the heat that is required in order to effect both the combustion of the solid carbonaceous fuel 144 and the reduction of the CaSO4 152 to CaS 148 in the reducing reactor 140 so as to thereby permit a continuous recycling thereof to be had. The combusting of the solid carbonaceous fuel 144 in the reducing reactor 140 is designed to be such that the predetermined output 138 is thus generated in the reducing reactor 140, whereupon the carbon and the hydrogen that is contained in the solid carbonaceous fuel 144 is designed to be converted in the course of such combusting of the solid carbonaceous fuel 144 to a product gas including CO2 and H2O. The H2O is then capable of being removed from such product gas leaving the remainder of such product gas in a suitable form so as to, therefore, be capable of functioning as the predetermined output 138, which is generated through the use of the fifth exemplary embodiment 136 of the mode of operation of the hot solids process 10 of the present invention, such as to thus be capable of being captured by any capture means that is suitable for use for such a purpose, such capture means being schematically illustrated in FIG. 6, wherein the schematic illustration of such capture means is denoted by the reference numeral 154, based on the nature of the pre-selected specific application, for which such predetermined output 138 is being produced, being a CO2 capture Hot Solids Combustion application.
Reference will next be had herein to FIG. 7 of the drawings wherein there is depicted therein a schematic diagram of a sixth exemplary embodiment, generally denoted by the reference numeral 156 in FIG. 7 of the drawings, of the mode of operation of the hot solids process 10 of the present invention that is designed to be operable in accordance with the present invention for purposes of generating a predetermined output, and with the latter predetermined output being denoted by the reference numeral 158 in FIG. 7 of the drawings, based on the nature of the pre-selected specific application, for which the predetermined output 158 is being produced, being a CO2 capture Hot Solids Gasification application. With further reference to FIG. 7 of the drawings, a reducing reactor, denoted generally by the reference numeral 160 in FIG. 7, and an oxidizing reactor, denoted generally by the reference numeral 162 in FIG. 7, are each designed to be employed in the hot solids process 10 of the present invention, in accordance with the sixth exemplary embodiment 156 of the mode of operation of the hot solids process 10 of the present invention that is operable in accordance with the present invention for purposes of generating the predetermined output 158, based on the nature of the pre-selected specific application, for which the predetermined output 158 is being produced, being a CO2 capture Hot Solids Gasification application. Continuing, in accordance with the sixth exemplary embodiment 156 of the mode of operation of the hot solids process 10 of the present invention, solid carbonaceous fuel, such as, by way of exemplification and not limitation, coal, the latter coal being denoted by the arrow 164 in FIG. 7, which is supplied as an input to the reducing reactor 160, is designed to be gasified. To this end, CaCO3, the latter CaCO3 being denoted by the arrow 166 in FIG. 7, which is designed to be added in accordance with the sixth exemplary embodiment 156 of the mode of operation of the hot solids process 10 of the present invention, is also supplied to the reducing reactor 160. Such CaCO3 166, which is added in accordance with the sixth exemplary embodiment 156 of the mode of operation of the hot solids process 10 of the present invention, is designed to be operative to capture in the reducing reactor 160 the sulfur, which is contained in the solid carbonaceous fuel 164, such as to thereby produce CaS therefrom in the reducing reactor 160. The latter CaS, as is denoted by the arrow 168 in FIG. 7, is then designed to be made to exit from the reducing reactor 160 as an output therefrom, whereupon such CaS 168 is supplied as an input to the oxidizing reactor 162. In the oxidizing reactor 162, this CaS 168 is designed to be reacted. Air, the latter air being denoted by the arrow 170 in FIG. 7, is designed to be supplied as an input to the oxidizing reactor 162, so that CaSO4 is thereby capable of being produced from the reacting of the CaS 168 in the oxidizing reactor 162.
With further reference thereto, this CaSO4, as is denoted by the arrow 172 in FIG. 7, is then designed to be made to exit as an output from the oxidizing reactor 162, whereupon this CaSO4 172 is designed to be recycled to the reducing reactor 160 as an input thereto for purposes of supplying the oxygen and the heat that is required in order to effect both the gasification of the solid carbonaceous fuel 164 and the reduction of the CaSO4 172 to CaS 168 in the reducing reactor 160 so as to thereby permit a continuous recycling thereof to be had. The gasification of the solid carbonaceous fuel 164 in the reducing reactor 160 is designed to be such that the predetermined output 158 is thus generated in the reducing reactor 160, whereupon the carbon and the hydrogen that is contained in the solid carbonaceous fuel 164 is designed to be converted in the course of such gasification of the solid carbonaceous fuel 164 to a product gas including CO2 and H2O as well as CO and H2. The H2O is then capable of being removed from such product gas leaving the remainder of such product gas in a suitable form so as to, therefore, be capable of functioning as the predetermined output 158, which is generated through the use of the sixth exemplary embodiment 156 of the mode of operation of the hot solids process 10 of the present invention, such as to thus be capable of being captured by any capture means that is suitable for use for such a purpose, such capture means being schematically illustrated in FIG. 7, wherein the schematic illustration of such capture means is denoted by the reference numeral 174, based on the nature of the pre-selected specific application, for which such predetermined output 158 is being produced, being a CO2 capture Hot Solids Gasification application.
Reference will next be had herein to FIG. 8 of the drawings wherein there is depicted therein a schematic diagram of a seventh exemplary embodiment, generally denoted by the reference numeral 176 in FIG. 8 of the drawings, of the mode of operation of the hot solids process 10 of the present invention that is designed to be operable in accordance with the present invention for purposes of generating a predetermined output, and with the latter predetermined output being denoted by the reference numeral 178 in FIG. 8 of the drawings, based on the nature of the pre-selected specific application, for which the predetermined output 178 is being produced, being a partial CO2 capture Hot Solids Combustion application. With further reference to FIG. 8 of the drawings, a reducing reactor, denoted generally by the reference numeral 180 in FIG. 8, and an oxidizing reactor, denoted generally by the reference numeral 182 in FIG. 8, are each designed to be employed in the hot solids process 10 of the present invention, in accordance with the seventh exemplary embodiment 176 of the mode of operation of the hot solids process 10 of the present invention that is operable in accordance with the present invention for purposes of generating the predetermined output 178, based on the nature of the pre-selected specific application, for which the predetermined output 178 is being produced, being a partial CO2 capture Hot Solids Combustion application. Continuing, in accordance with the seventh exemplary embodiment 176 of the mode of operation of the hot solids process 10 of the present invention, solid carbonaceous fuel, such as, by way of exemplification and not limitation, coal, the latter coal being denoted by the arrow 184 in FIG. 8, which is supplied as an input to the reducing reactor 180, is designed to be combusted using air indirectly. To this end, CaCO3, the latter CaCO3 being denoted by the arrow 186 in FIG. 8, which is designed to be added in accordance with the seventh exemplary embodiment 176 of the mode of operation of the hot solids process 10 of the present invention, is also supplied as an input to the reducing reactor 180. Such CaCO3 186, which is added in accordance with the seventh exemplary embodiment 176 of the mode of operation of the hot solids process 10 of the present invention, is designed to be operative to capture in the reducing reactor 180 the sulfur, which is contained in the solid carbonaceous fuel 184, such as to thereby produce CaS therefrom in the reducing reactor 180. The latter CaS, as is denoted by the arrow 188 in FIG. 8, is then designed to be made to exit from the reducing reactor 180 as an output therefrom, whereupon such CaS 188 is supplied as an input to the oxidizing reactor 182. In the oxidizing reactor 182, this CaS 188 is combusted in a heat liberating reaction with air, the latter air being denoted by the arrow 190 in FIG. 8, which is designed to be supplied as an input to the oxidizing reactor 182, so as to thereby be capable of producing CaSO4 in the oxidizing reactor 182.
With further reference thereto, this CaSO4, as is denoted by the arrow 192 in FIG. 8, is then designed to be made to exit as an output from the oxidizing reactor 182, whereupon this CaSO4 192 is designed to be recycled to the reducing reactor 190 as an input thereto for purposes of supplying the oxygen and the heat that is required in order to effect both the combustion of the solid carbonaceous fuel 184 and the reduction of the CaSO4 192 to CaS 188 in the reducing reactor 180 so as to thereby permit a continuous recycling thereof to be had. The combusting of the solid carbonaceous fuel 184 in the reducing reactor 180 is designed to be such that the predetermined output 178 is thus generated in the reducing reactor 180, whereupon the carbon and the hydrogen that is contained in the solid carbonaceous fuel 184 is designed to be converted in the course of such combusting of the solid carbonaceous fuel 184 to a product gas including CO2 and H2O. The H2O is then capable of being removed from such product gas leaving the remainder of such product gas in a suitable form so as to, therefore, be capable of functioning as the predetermined output 178, which is generated through the use of the seventh exemplary embodiment 176 of the mode of operation of the hot solids process 10 of the present invention, such as to thus be capable of being partially captured by any partial capture means that is suitable for use for such a purpose, such partial capture means being schematically illustrated in FIG. 8, wherein the schematic illustration of such partial capture means is denoted by the reference numeral 194, based on the nature of the pre-selected specific application, for which such predetermined output 178 is being produced, being a partial CO2 capture Hot Solids Combustion application.
Reference will next be had herein to FIG. 9 of the drawings wherein there is depicted therein a schematic diagram of an eighth exemplary embodiment, generally denoted by the reference numeral 196 in FIG. 9 of the drawings, of the mode of operation of the hot solids process 10 of the present invention that is designed to be operable in accordance with the present invention for purposes of generating a predetermined output, and with the latter predetermined output being denoted by the reference numeral 198 in FIG. 9 of the drawings, based on the nature of the pre-selected specific application, for which the predetermined output 198 is being produced, being a partial CO2 capture Hot Solids Gasification application. With further reference to FIG. 9 of the drawings, a reducing reactor, denoted generally by the reference numeral 200 in FIG. 9, and an oxidizing reactor, denoted generally by the reference numeral 202 in FIG. 9, are each designed to be employed in the hot solids process 10 of the present invention, in accordance with the eighth exemplary embodiment 196 of the mode of operation of the hot solids process 10 of the present invention that is operable in accordance with the present invention for purposes of generating the predetermined output 198, based on the nature of the pre-selected specific application, for which the predetermined output 198 is being produced, being a partial CO2 capture Hot Solids Gasification application. Continuing, in accordance with the eighth exemplary embodiment 196 of the mode of operation of the hot solids process 10 of the present invention, solid carbonaceous fuel, such as, by way of exemplification and not limitation, coal, the latter coal being denoted by the arrow 204 in FIG. 9, which is designed to be supplied as an input to the reducing reactor 200, is designed to be gasified. To this end, CaCO3, denoted by the arrow 206 in FIG. 9, which is designed to be added in accordance with the eighth exemplary embodiment 196 of the mode of operation of the hot solids process 10 of the present invention, is also supplied to the reducing reactor 200. Such CaCO3 206, which is added in accordance with the eighth exemplary embodiment 196 of the mode of operation of the hot solids process 10 of the present invention, is designed to be operative to capture in the reducing reactor 200 the sulfur, which is contained in the solid carbonaceous fuel 204, such as to thereby produce CaS therefrom in the reducing reactor 200. The latter CaS, as is denoted by the arrow 208 in FIG. 9, is then designed to be made to exit from the reducing reactor 200 as an output therefrom, whereupon such CaS 208 is supplied as an input to the oxidizing reactor 202. In the oxidizing reactor 202, this CaS 208 is designed to be reacted. Air, the latter air being denoted by the arrow 210 in FIG. 9 is supplied as an input to the oxidizing reactor 202, so that CaSO4 is thereby capable of being produced from the reaction of the CaS 208 in the oxidizing reactor 202.
With further reference thereto, this CaSO4, as denoted by the arrow 212 in FIG. 9, is then designed to be made to exit as an output from the oxidizing reactor 202, whereupon this CaSO4 212 is designed to be recycled to the reducing reactor 200 as an input thereto for purposes of supplying the oxygen and the heat that is required in order to effect both the gasification of the solid carbonaceous fuel 204 and the reduction of the CaSO4 212 to CaS 208 in the reducing reactor 200 so as to thereby permit a continuous recycling thereof to be had. The gasification of the solid carbonaceous fuel 204 in the reducing reactor 200 is designed to be such that the predetermined output 198 is thus generated in the reducing reactor 200, whereupon the carbon and the hydrogen that is contained in the solid carbonaceous fuel 204 is designed to be converted in the course of such gasification of the solid carbonaceous fuel 204 to a product gas including CO2 and H2O as well as CO and H2. The H2O is then capable of being removed from such product gas leaving the remainder of such product gas in a suitable form so as to, therefore, be capable of functioning as the predetermined output 198, which is generated through the use of the eighth exemplary embodiment 196 of the mode of operation of the hot solids process 10 of the present invention, such as to thus be capable of being partially captured by any partial capture means that is suitable for use for such a purpose, such partial capture means being schematically illustrated in FIG. 9, wherein the schematic illustration of such partial capture means is denoted by the reference numeral 214, based on the nature of the pre-selected specific application, for which such predetermined output 198 is being produced, being a partial CO2 capture Hot Solids Gasification application.
While the embodiments of the present invention described hereinbefore included a calcium oxide, the invention contemplates that the oxide may include a metal oxide, for example, formed of iron such as FeO.
While preferred embodiments of the present invention have been shown and described in the instant application, it is to be understood that various modifications and substitutions may be made thereto without departing from the spirit and scope of the present invention as set forth in the claims that are appended hereto. Accordingly, it is to be further understood that the present invention, as the present invention has been described herein, has been described by way of illustration and not limitation.
