CN102482596A - A hot solids process selectively operable based on a type of application that is involved - Google Patents

Abstract

The present invention provides a thermal solids method that is selectively operable to generate a predetermined output based on the nature of the particular application for which the generated predetermined output is being used, and wherein such particular application can be derived from Pre-selected from a specific group of applications including new steam generator applications, retrofit steam generator applications, _CO2 capture-ready thermal solids combustion applications, _CO2 capture-ready thermal solids gasification applications, _CO2 capture thermal solids combustion applications, _CO2 capture thermal solids gasification applications, partial _CO2 capture thermal solids combustion applications and partial _CO2 capture thermal solids gasification applications.

Description

Thermal solids methods that can be selectively operated based on the type of application involved

Cross References to Related Applications

THIS APPLICATION CLAIMS PENDING OF THE MARCH 31, 2009 APPLICATION TITLE "HOT SOLIDS PROCESS SELECTIVELY OPERABLE BASED ON THE TYPE OF APPLICATION THAT IS INVOLVED" Priority to U.S. Provisional Application No. 61/165,069, which is hereby incorporated by reference in its entirety.

technical field

The present invention generally relates to a thermal solids process selectively operable to generate a predetermined output based on the properties of a particular application for which the predetermined output is generated. In particular, the present invention relates to such heat fixing methods that are selectively operable to produce a predetermined output based on the properties of the particular application for which the predetermined output is generated, and wherein such specific Applications can be pre-selected from a specific group of applications including new steam generator applications, retrofit steam generator applications, CO2 capture ready thermal solids combustion applications, CO2 capture ready thermal solids gasification applications, At least two of a CO2 capture thermal solids combustion application, a CO2 capture thermal solids gasification application, a partial CO2 capture thermal solids combustion application, and a partial CO2 capture thermal solids gasification application.

Background technique

The world today faces serious challenges as all nations struggle to meet basic human needs (ie, clothing, food, shelter, and transportation), which depend on an adequate supply of energy. The large increase in energy use has been largely met by fossil fuels, primarily coal, oil and natural gas. There is no doubt that as the demand for energy continues to grow, environmental concerns, security of supply, and economic impact must be balanced. Still, real economic growth and energy use are closely linked.

While the ultimate solution to provide sufficient energy supply is still being explored, in the short term we must consider temporary solutions to meet the immediate increase in energy demand. Of course, energy reserves could be stretched if technological improvements were made in the extraction, drilling, delivery, processing and use of fossil fuels, which could be a determined effort in energy storage. Similarly, technologies that utilize advanced and clean fossil fuels involve the use of various forms of thermal solids processes such as, but not limited to, fossil fuel gasification, fluidized bed combustion, or mixed gasification fossil fuel technologies that can scale up Use of the world's vast fossil fuel resources.

In the mode of operation of power generation systems, most people understand that the steam generators used in such power generation systems generate steam from the combustion of fossil fuels, which is used in steam turbines. This steam is usually at high temperature and pressure and is expanded in the aforementioned steam turbine, thereby turning the steam turbine. This rotation of the steam turbine will in turn operate in a known manner, causing a generator operatively connected to said steam turbine in a suitable manner to also rotate. Then, when this rotation occurs in the generator, a conductor is moved through the magnetic field, which creates an electric current. The above-mentioned mode of operation has basically been the basis of the power generation system that people assert even today.

In an effort to increase the efficiency of power generation systems, attempts have been made to increase the temperature and pressure at which steam generators used in such power generation systems can operate. These efforts to date have resulted in commercially available steam generators for use in power generation systems capable of operating at subcritical pressure conditions as well as supercritical pressure conditions. Such steam generators are intended for use in power generation systems, and improvements in the strength of the materials available for construction of such steam generators would allow such materials and thus such steam generators to operate at the higher temperatures and operate at the higher pressures mentioned.

In further discussion of the previously mentioned advanced clean fossil fuel technologies in which various forms of thermal solids processes are used, especially fossil fuel gasification, attention is first given to (eg, But not limited to) U.S. Patent No. 2,602,809 issued July 8, 1952 to The M.W. Kellogg Company. The teachings of US Patent No. 2,602,809 are considered representative of early developments in the continuing development of fossil fuel gasification technology using a thermal solids process type. To this end, according to the teachings therein, the teachings of US Patent No. 2,602,809 relate to a process which is said to be particularly suitable for the gasification of low-grade solid carbonaceous materials. Specifically, to the extent contemplated by the mode of operation of the method contemplated by the teachings of U.S. Patent No. 2,602,809, solid carbonaceous matter may be oxidized to convert such solid carbonaceous matter into carbon oxides, which conversion is It is carried out by indirect oxidation of solid carbonaceous substances and air, while preventing the nitrogen in the air from polluting the product gas. The gasification of such solid carbonaceous materials is accomplished by alternating oxidation and reduction of fluidized metal oxides. According to the teachings of U.S. Patent No. 2,602,809, solid fuels are converted to gases by contacting metal oxides with particulate solid carbonaceous matter in a manner that reduces the metal oxides and oxidizes the carbon in the solid fuel to Carbon oxides, where the metal oxide is the main source of oxygen required for carbon oxidation. Then, after the reduction of the metal oxide, the reduced metal oxide is re-oxidized, after which the method cycle can be repeated again.

A further discussion of fossil fuel gasification, previously mentioned above as an advanced clean fossil fuel technology, in which various forms of hot solid processes are used, is followed by a focus on (for example, but not limited to) the 1986 US Patent No. 4,602,573 issued July 29 to Combustion Engineering, Inc. The teaching of US Patent No. 4,602,573 is considered representative of a further development in the continuing development of fossil fuel gasification technology using a thermal solid process type. To this end, according to the teachings therein, the teachings of U.S. Patent No. 4,602,573 are stated to relate to a method of gasifying and combusting carbonaceous fuels, and in particular, to an integrated process in which carbon containing sulfur and nitrogen The carbonaceous fuel is gasified to produce a carbon monoxide rich, low BTU fuel gas which can then be combusted with other carbonaceous fuels in a steam generator. Specifically, so far as the mode of operation of the method contemplated by the teachings of US Pat. to produce a charcoal-containing, carbon monoxide-enriched hot fuel gas with a low BTU content. Thereafter, a sulfur-trapping substance is introduced into the gasification reactor so that gasification of the carbonaceous fuel can be performed in the presence of the sulfur-trapping substance, whereby the sulfur-trapping substance traps the gasified A substantial portion of sulfur in carbonaceous fuels.

Next, this patent application document will further focus on the previously mentioned advanced clean fossil fuel technologies using various forms of thermal solids processes, especially fluidized bed combustion technology. Therefore, in particular, attention is drawn in this regard to, for example, but not limited to, US Patent No. 4,111,158 issued September 5, 1978 to Metallgesellschaft Aktiengesellschaft. The teachings of US Patent No. 4,111,158 are considered representative of early developments in the continuing development of fluidized bed combustion technology of the type using a hot solids process. To this end, according to the teachings therein, the teachings of US Patent No. 4,111,158 are stated to relate to a method and apparatus for performing an exothermic process in which the solid feedstock contains flammable compounds, eg, carbonaceous or sulfur-containing compounds. Next, to the extent contemplated by the mode of operation of the method and apparatus taught by US Patent No. 4,111,158, the flammable compound of the solid feedstock can be used for combustion in the fluidized bed under approximately stoichiometric conditions. Thereafter, solids generated by the combustion of flammable compounds of such solid feedstocks will be withdrawn from the fluidized bed, which can be returned to the fluidized bed for recycling, while due to the The heat generated by the combustion of flammable compounds can be recovered.

Discussing further the previously mentioned fluidized bed combustion technology for advanced clean fossil fuel technology in which various forms of hot solids processes are used, this patent application document subsequently focuses on (for example, but not Limited to) U.S. Patent No. 5,533,471 issued Jul. 9, 1996 to A. Ahlstrom Corporation. The teaching of US Patent No. 5,533,471 is considered representative of further developments in the ongoing development of fluidized bed combustion technology of the type using hot solids processes. To this end, according to the teachings therein, the teachings of U.S. Patent No. 5,533,471 are stated to relate to a system and a method that allow the temperature of a fluidized bed reactor to be effectively controlled to allow sufficient heat transfer for cooling the solid matter surface area. Specifically, to the extent contemplated by the mode of operation of the system and method taught by US Patent No. 5,533,471, both circulating (fast) fluidized beds and bubbling (slow) fluidized beds are used. Next, the two (2) fluidized beds are installed adjacent to each other with a first interconnection and a second interconnection between the two (2) fluidized beds, wherein the fluidization gas input to the bubbling fluidized bed grid Typically lower than the fluidization gas input to the circulating fluidized bed grid. Because the density of the bubbling fluidized beds as a whole is substantially constant, with a clear demarcation line at the top, a first interconnection is provided above the top of the bubbling fluidized beds so that between two (2) fluidized beds The pressure and density conditions cause the particles to flow from the circulating fluidized bed to the bubbling fluidized bed through the first interconnection. However, since the average density of a bubbling fluidized bed is higher than that of a circulating fluidized bed, the pressure and density conditions can result in the particles being treated in the bubbling fluidized bed (e.g., after cooling the particles therein) ) is returned to the circulating fluidized bed through the second interconnection.

With regard to further discussion of advanced clean fossil fuel technologies, previously mentioned above, using various forms of hot solids processes, especially co-combustion-gasification, attention is first given to (e.g., but Without limitation) U.S. Patent No. 4,272,399 issued June 8, 1981 to the Monsanto Company. The teachings of US Patent No. 4,272,399 are considered representative of early developments in the continuing development of co-combustion-gasification technology of the type using a hot solids process. To this end, according to the teachings therein, the teachings of US Patent No. 4,272,399 are stated to relate to a unified method for generating high purity synthesis gas from carbonaceous materials. Specifically, to the extent contemplated by the teachings of U.S. Patent No. 4,272,399 regarding the mode of operation of the unified process, metal-oxygen containing substances may be described as carriers of heat and oxygen and generally may be referred to as oxidizing agents, referred to as The metal-oxygen-containing substances are used as transfer agents for oxygen and heat, thereby gasifying carbonaceous substances in an oxidative manner. The oxidant may then be fluidized and delivered through an upflow co-current system using steam, carbon dioxide, forming gas, or mixtures thereof. Thus, according to the mode of operation of the unified process of the present invention, the synthesis gas is first oxidized and heated by the oxidant, thereby forming water and carbon in the oxidant reduction zone, before the oxidant and gas contact the carbonaceous material in the gasification zone. In addition, carbonaceous species are oxidized primarily to carbon monoxide and hydrogen without allowing atmospheric nitrogen to contaminate the product synthesis gas. In addition, the gasification of carbonaceous materials is accomplished by alternate oxidation and reduction of fluidized oxidants. Then, after such gasification, the reduced oxides, possibly in the form of elemental metal or in a lower oxidation state, are re-oxidized in the oxidation zone, so that the cycle repeats.

Discussing further the previously mentioned co-combustion-gasification of advanced clean fossil fuel technology, in which various forms of hot solid processes are used, this patent application document subsequently focuses on (eg, but Without limitation) US Patent No. 7,083,658 issued to ALSTOM Technology Ltd (ALSTOM Technology Ltd) on August 1, 2006, which is incorporated herein by reference. The teaching of US Patent No. 7,083,658 is considered representative of further developments in the ongoing development of co-combustion-gasification technology of the type using a hot solids process. To this end, according to the teachings therein, the teachings of U.S. Patent No. 7,083,658 are stated to relate to an apparatus for generating hydrogen from fossil fuels, biofuels, petroleum coke, or any other carbonaceous fuel for use in generating electricity, such that minimal Minimize or eliminate the release of carbon dioxide (CO2). Specifically, to the extent contemplated by the mode of operation of the apparatus covered by the teachings of U.S. Patent No. 7,083,658, there is provided a gasifier for generating gaseous products from carbonaceous fuels, the gasifier comprising A first chemical process cycle comprising an exothermic oxidant reactor and an endothermic reductant reactor. Next, the exothermic oxidant reactor has a CaS inlet, a hot air inlet and a CaSO4/waste gas outlet. Whereas the endothermic reductant reactor has a CaSO4 inlet that is in fluid communication with the exothermic oxidant reactor CaSO4/waste gas outlet and a CaS/gas product outlet that reacts with the exothermic oxidant a CaS inlet in fluid communication; and a material inlet for receiving carbonaceous fuel. Also, CaS is oxidized in air in the exothermic oxidizer reactor to form hot CaSO4, which is then discharged to the endothermic reductant reactor. In addition, the hot CaSO4 received in the endothermic reductant reactor and the carbonaceous fuel undergo an endothermic reaction that utilizes the heat generated by CaSO4 deoxygenating CaSO4 with the carbonaceous fuel to form CaS and gaseous products. Thereafter, the CaS is vented to the exothermic oxidant reactor, while gaseous products are vented from the first chemical process cycle.

It is therefore an object of the present invention to provide a thermal solids process which can be selectively operated based on the type of application involved.

Another object of the present invention is to provide a thermal solids process which is selectively operable to produce a predetermined output.

It is another object of the present invention to provide such a thermal solids method which is selectively operable to generate such a predetermined output based on the nature of the particular application for which the generated predetermined output is used.

It is another object of the present invention to provide such a thermal solids method which is selectively operable to generate said predetermined output based on the nature of the particular application for which said generated predetermined output is being used, And wherein such specific application can be pre-selected from a set of specific applications.

It is a further object of the present invention to provide a thermal solids method that is selectively operable to produce a predetermined output based on the properties of the particular application being used to generate such predetermined output, and wherein such Specific applications can be pre-selected from a group of specific applications including new steam generator application, retrofit steam generator application, CO2 capture ready thermal solid combustion application (CO2 capture ready Hot Solids Combustion application), CO2 capture ready Hot Solids Gasification application (CO2 capture readyHot Solids Gasification application), CO2 capture ready Hot Solids Combustion application (CO2 capture readyHot Solids Combustion application), CO2 capture hot solids gasification application gasification applications, partial CO2 capture thermal solids combustion applications and partial CO2 capture thermal solids gasification applications.

Yet another object of the present invention is to provide such a thermal solids method that is relatively low cost, relatively low complexity to use, and characterized by versatility, taking into account the particular application involved To the extent that a predetermined output can be generated using the thermal solids method of the present invention, wherein said predetermined output is generated for said particular application.

Contents of the invention

The present invention provides a thermal solids method that is selectively operable to generate a predetermined output based on the properties of the particular application for which the predetermined output is generated, and wherein such particular application can be derived from a Preselected from a group of specific applications including new steam generator applications, retrofit steam generator applications, CO2 capture ready heat solid combustion applications, CO2 capture ready heat solid gasification applications, CO2 capture heat At least two of a solids combustion application, a CO2 capture thermal solids gasification application, a partial CO2 capture thermal solids combustion application, and a partial CO2 capture thermal solids gasification application. To this end, the mode of operation of such a thermal solids process according to the present invention is to combust a preferred limestone-based sorbent (such as, but not limited to, CaS) in an oxidation reactor, such an oxidation reactor preferably (such as, but not limited to limited to) circulating bed reactors in order thereby to generate hot CaSO4 by burning such limestone-based sorbents. This hot CaSO is then in turn used in a reduction reactor, such as, but not limited to, a circulating bed reactor, to produce a predetermined output based on pre-selected properties for a particular application, Wherein said pre-selected specific application is being used to generate such predetermined output.

A second exemplary embodiment of the mode of operation of the hot solids process according to the present invention, wherein the fuel for combustion thereby comprises a solid carbonaceous fuel such as, but not limited to, coal, and wherein the pre-selected specific application is improved steam generator application, and in this case an existing steam generator used as an oxidation reactor, wherein said pre-selected specific application is being used to generate a predetermined output, and said predetermined output is passed through the thermal solids method of the present invention This second exemplary embodiment of the mode of operation results. For this reason, for the second exemplary embodiment of the mode of operation of the thermal solids process of the present invention, in order to be able to be used as such an oxidation reactor, the existing steam generator needs to be modified so as to be implemented in order to be able to use A cyclone operating in the manner of a reactor or likewise a curvilinear separator capable of operating in the manner of a reactor.

A second exemplary embodiment of the mode of operation of the hot solids process of the present invention will now be discussed further, when the existing steam generator is suitably modified to implement a curve splitter for operation as an oxidation reactor From the reduction reactor used in the second exemplary embodiment of the mode of operation of the hot solids process of the invention to the curve separator, the oxides can be conveyed by excess air with the purpose of achieving therein the combustion of the oxides. Gases generated from the combustion of oxides with air in an oxidation reactor (i.e., a curvilinear separator) are in turn passed through an existing steam generator where heat can be absorbed from such gases . Simultaneously, any ash particles and/or solid particles resulting from the combustion of oxidant and air in the oxidation reactor (i.e., a curvilinear splitter, existing steam generators suitably modified to implement such a curvilinear splitter) can be removed from the Collected at the bottom of the existing steam generator, the ash particles and/or solid particles do not entrain the above-mentioned gas used to flow through the existing steam generator.

Description of drawings

Figure 1 is a schematic diagram of a hot solids process operating in accordance with the present invention;

Figure 2 is a schematic diagram of a first exemplary embodiment of a mode of operation of a hot solids process operating in accordance with the present invention;

According to the second exemplary embodiment of the mode of operation of the hot solid method operating according to the present invention, Fig. 3a and Fig. 3b are respectively schematic diagrams illustrating different configurations of said second exemplary embodiment;

Figure 4 is a schematic diagram of a third exemplary embodiment of a mode of operation of a hot solids process operating in accordance with the present invention;

Figure 5 is a schematic diagram of a fourth exemplary embodiment of a mode of operation of a hot solids process operating in accordance with the present invention;

Figure 6 is a schematic diagram of a fifth exemplary embodiment of a mode of operation of a hot solids process operating in accordance with the present invention;

Figure 7 is a schematic diagram of a sixth exemplary embodiment of a mode of operation of a hot solids process operating in accordance with the present invention;

Figure 8 is a schematic diagram of a seventh exemplary embodiment of a mode of operation of a hot solids process operating in accordance with the present invention; and

9 is a schematic diagram of an eighth exemplary embodiment of a mode of operation of a hot solids process operating in accordance with the present invention.

Detailed ways

Referring now to FIG. 1, there is depicted a schematic diagram of a thermal solids process, generally indicated by reference numeral 10 in FIG. The predetermined output of is for the specific application, and the latter mentioned predetermined output is indicated by arrow 12 in FIG. 1 . According to the mode of operation of the thermal solids method of the present invention schematically depicted in FIG. Including new steam generator application, improved steam generator application, CO2 capture reserved thermal solid combustion application, CO2 capture reserved thermal solid gasification application, CO2 capture thermal solid combustion application, CO2 capture thermal solid gasification At least two of applications, partial CO2 capture thermal solids combustion applications, and partial CO2 capture thermal solids gasification applications.

The hot solids process 10 of the present invention according to the preferred mode of operation can use air; solid carbonaceous fuels such as, but not limited to, coal; a source of calcium (e.g., calcium oxide); Therein such predetermined output 12 is generated, wherein said pre-selected particular application is being used to generate such predetermined output 12 . To this end, such predetermined output 12 generated in accordance with the mode of operation of the thermal solids process 10 of the present invention may be, for example, CO capture reserved after being so generated, based on the nature of the particular application that may be preselected in accordance with the present invention. , or CO2 capable of being captured after being so generated or CO2 capable of being partially captured after being so generated. Furthermore, the heat generated by using the hot solids method 10 of the present invention according to the preferred mode of operation can be used to generate steam, which is suitable for generating electricity.

With further reference to FIG. 1 , according to the preferred mode of operation, the reduction reactor generally indicated by reference numeral 14 in FIG. 1 and the oxidation reactor generally indicated by reference numeral 16 in FIG. 1 are used in the hot solids process 10 of the present invention used in . Next, according to a preferred embodiment of the hot solids process 10 of the present invention, the solid carbonaceous fuel supplied as input to the reduction reactor 14 (such as, but not limited to, coal, the latter being indicated by arrow 18 in FIG. 1 Indicates) for indirect use of air for combustion. To this end, the calcium source for addition to the hot solids process 10 of the present invention according to the preferred mode of operation is also (for example, but not limited to) supplied as input to the reduction reactor 14, and the latter mentioned calcium source is shown in FIG. 1 Indicated by arrow 20 . However, such a calcium source 20 may be provided to other parts of the hot solids process 10 of the present invention other than as an input to the reduction reactor 14 without departing from the spirit of the invention. This calcium source 20 (i.e., calcium oxide) may be selected from calcium sources such as limestone (CaCO3), lime (CaO), gypsum, or waste bed material from circulating bed boilers, preferably (e.g., but not limited to) contains limestone (CaCO3). With further reference to this figure, such limestone (CaCO3) 20 added to said thermal solids process 10 for operation to capture solid carbonaceous in reduction reactor 14 according to the preferred mode of operation of the thermal solids process 10 Sulfur (S) contained in the fuel 18 thereby generates calcium sulfide (CaS) in the reduction reactor 14 . Such calcium sulphide (CaS), represented by arrow 22 in FIG. In the oxidation reactor 16, such calcium sulfide (CaS) 22 is combusted in an exothermic reaction with air, and the latter air is indicated by arrow 24 in FIG. 16 to generate calcium sulfate (CaSO4) in the oxidation reactor 16. Subsequently, this calcium sulfate (CaSO 4 ) represented by arrow 26 in FIG. Thereby, the oxygen and heat required to burn the solid carbonaceous fuel 18 and reduce the calcium sulfate (CaSO4) 26 to calcium sulfide (CaS) 22 in the reduction reactor 14 are thereby provided, thereby enabling continuous recirculation. The combustion of the solid carbonaceous fuel 18 in the reduction reactor 14 is used to cause the predetermined output 12 to be produced in the reduction reactor 14, and the carbon and hydrogen contained in the solid carbonaceous fuel 18 during the combustion of such solid carbonaceous fuel 18 converted into a product gas consisting of CO2 and H2O. This H2O can then be removed from such product gas so that the residue of such product gas is in a suitable form so that it can be used as a predetermined output 12 based on a pre-selected specific the nature of the application produced by using the thermal solids method 10 of the present invention, wherein said pre-selected specific application is being used to generate such predetermined output 12, and such pre-selected specific application is a new steam generator application, or Retrofit steam generator applications, or CO2 capture ready thermal solids combustion applications, or CO2 capture ready thermal solids gasification applications, or CO2 capture thermal solids combustion applications, or CO2 capture thermal solids gasification applications, or Partial CO2 capture thermal solids combustion applications, or partial CO2 capture thermal solids gasification applications.

Referring next to FIG. 2, there is depicted a schematic diagram of a first exemplary embodiment of the mode of operation of the hot solids method 10 of the present invention, generally indicated by reference numeral 28 in FIG. The first exemplary embodiment is adapted to operate in accordance with the present invention to generate predetermined outputs based on preselected application-specific properties, the latter mentioned predetermined outputs being represented in FIG. 2 by arrows 30 and 31, wherein the preselected A specific application is being used to generate the predetermined outputs 30 and 31, and the pre-selected specific application is a new steam generator application. Referring further to FIG. 2, a reduction reactor, generally indicated by reference numeral 32 in FIG. 2, and an oxidation reactor, generally indicated by reference numeral 34 in FIG. An exemplary embodiment 28 is used in the thermal solids method 10 of the present invention, said first exemplary embodiment being operable in accordance with the present invention to produce predetermined outputs 30 and 31 based on preselected application-specific properties, wherein the The pre-selected specific application is being used to generate the predetermined outputs 30 and 31, and the pre-selected specific application is a new steam generator application. For the oxidation reactor 34 used in this first exemplary embodiment 28 of the mode of operation of the hot solids process 10 of the present invention, when the fuel for use therewith comprises a solid carbonaceous fuel such as, but not limited to Coal, and when the pre-selected specific application is a fresh steam generator application, the input to the oxidation reactor 34 includes CaS, the latter being indicated by arrow 36 in Figure 2, and air, the latter Air is represented by arrow 38 in FIG. 2, wherein said pre-selected particular application is being used to generate predetermined outputs 30 and 31, and said predetermined outputs pass through this first exemplary mode of operation of the thermal solids method 10 of the present invention. Example 28 was produced. Then, in this case, the output of such an oxidation reactor 34 comprises ash, the latter mentioned ash indicated by arrow 48 in FIG. 2 ; CaSO4; and N2, the latter N2 is indicated by arrow 50 in FIG. 2 .

However, for the reduction reactor 32 used in the first exemplary embodiment 28 of the mode of operation of the hot solids process 10 of the present invention, when the fuel for use therewith comprises a solid carbonaceous fuel, such as, but not When limited to coal, and when the pre-selected specific application is a fresh steam generator application, the input to the reduction reactor 32 includes a solid carbonaceous fuel, the latter being indicated by arrow 40 in FIG. 2 ; CaCO3, the latter mentioned CaCO3 is indicated by arrow 42 in FIG. 2; steam, the latter mentioned steam is indicated by arrow 44 in FIG. The preselected particular application is being used to generate the predetermined outputs 30 and 31 produced by this first exemplary embodiment 28 of the mode of operation of the hot solids method 10 of the present invention. The steam 44 added to the reduction reactor 32 is used to operate to effect the oxidation of CO to CO in the product gas that can be used according to the first exemplary embodiment of the mode of operation of the hot solids process 10 of the present invention 28 is produced in the reduction reactor 32 while reducing H2O in such product gas to H2. Such CO2 can then be captured by the excess CaO contained in the solids, which is circulated within the reduction reactor 32 in order thereby to form CaCO3 therein. Such CaCO3 is intended to be withdrawn from the reduction reactor 32 as a predetermined output 30 and then to the calciner, and the latter mentioned calciner is generally indicated by the reference numeral 52 in FIG. 2 . The calciner 52 is adapted to operate such that CO2 is released from a predetermined output 30 in the form of CaCO3 flowing from the reduction reactor 32 to the calciner 52 and such release of CO2 from the CaCO3 is effected The required heat is provided by the hot solids supplied from the oxidation reactor 34 to the calciner 52 , and the latter mentioned hot solids are indicated by arrow 54 in FIG. 2 . CaO remaining after CO2 release from CaCO3 is achieved in calciner 52 is then recycled to reduction reactor 32 for reuse, and such recycling is indicated by arrow 56 in FIG. 2 . According to the first exemplary embodiment 28 of the mode of operation of the hot solids process 10 according to the invention, the residue of the product gas produced in the reduction reactor 32 is intended to be discharged from the reduction reactor 32 as a predetermined output 31, the following predetermined output 31 takes the form of CO2-free steam generator fuel, and said CO2-free steam generator fuel is then supplied to a live steam generator (generally indicated by reference numeral 58 in FIG. Fuel for steam generator 58.

Referring next to Figures 3a and 3b, both of which contain a schematic diagram illustrating, by way of example and not limitation, a second exemplary implementation of the mode of operation of the hot solids method 10 of the present invention A different configuration of the second exemplary embodiment, generally indicated by reference numeral 60 in FIGS. 3a and 3b, wherein the fuel combusted thereby comprises a solid carbonaceous fuel such as, but not limited to, coal, and Where the pre-selected specific application is a retrofit steam generator application, said pre-selected specific application is being used to generate a predetermined output indicated by arrow 62 in FIGS. A second exemplary embodiment 60 of the mode of operation of the method 10 results. In this case, the existing steam generator generally indicated by reference numeral 64 in Figure 3a and the existing steam generator generally indicated by reference numeral 66 in Figure 3b are used as oxidation reactors. For this reason, for the second exemplary embodiment 60 of the mode of operation of the hot solids process 10 of the present invention, in order thereby to be used as such an oxidation reactor, the existing steam generator 64 needs to be suitably modified so that A cyclone is thereby implemented, the latter being indicated by reference numeral 68 in FIG. Appropriate modifications are required in order thereby to implement a curve splitter, the latter mentioned with reference numeral 70 in Figure 3b, which is suitably designed to be able to operate as a reactor.

A second exemplary embodiment 60 of the mode of operation of the hot solids process 10 of the present invention is discussed next, when an existing steam generator 64 has been suitably modified (as shown schematically in FIG. 3 a ) to thereby implement a cyclone 68 , such cyclone 68 is suitably designed to be able to operate as an oxidation reactor in order to burn CaS therein (the later mentioned CaS is indicated by arrow 72 in FIG. The excess air mentioned is indicated by arrow 74 in FIG. 3 a ) together as input into the cyclone 68 . The reduction reactor, generally indicated by reference numeral 76 in Figures 3a and 3b, is suitably designed to be able to improve the specific application based on the fact that the fuel for combustion is a solid carbonaceous fuel, and that the specific application preselected is A steam generator application is used to generate a predetermined output 62 therein, wherein the preselected particular application is being used to generate the predetermined output 62 . The solid mainly composed of CaSO4 is separated from the gas generated by the combustion of CaS 72 and air 74 in the cyclone 68, and the CaSO4 is formed by the combustion of CaS 72 and air 74 in the cyclone 68, and as shown in Figure 3a, the existing The steam generator 64 has been modified to implement the cyclone. As indicated by arrow 78 in Figure 3a, such CaSO4 is used for subsequent recycling from cyclone 68 to reduction reactor 76, wherein such CaSO4 78 can be combined with solid carbonaceous fuel (such as, but not limited to, coal, mentioned later) The coal is indicated by arrow 80 in Figure 3a) and CaCO3 (the later mentioned CaCO3 is indicated by arrow 82 in Figure 3a) is used together, and both the solid carbonaceous fuel and CaCO3 are used as the input of reduction reactor 76 supplied to produce a predetermined output 62 within the reduction reactor 76 based on the properties of a preselected particular application, which is an improved steam generator application. In addition, the gas generated in cyclone 68 by the combustion of CaS 72 with air 74 in cyclone 68 (as shown in FIG. There is a steam generator 64 (shown by arrow 84 in FIG. 3a ) in order to absorb heat from such gas 84 within the existing steam generator 64 . At the same time, any ash particles and/or solid particles that may be generated by the combustion of CaS 72 and air 74 in the cyclone 68 can be collected at the bottom of the existing steam generator 64 (as shown by arrow 86 in Figure 3a), where As shown in FIG. 3 a , the existing steam generator 64 has been suitably modified to thereby implement such a cyclone 68 without entraining the gas 84 intended to flow through the existing steam generator 64 .

A second exemplary embodiment 60 of the mode of operation of the hot solids process 10 of the present invention is discussed next, when an existing steam generator 66 has been suitably modified (as shown schematically in Figure 3b) to thereby implement a curve splitter 70, such a curve splitter 70 is suitably designed to operate as an oxidation reactor to burn CaS therein (the later mentioned CaS is indicated by arrow 86 in FIG. Excess air (the excess air mentioned later is indicated by arrow 88 in FIG. 3 b ) is fed together as input into the curve separator 70 . The reduction reactor, generally indicated by reference numeral 76 in Figures 3a and 3b, is suitably designed to be able to improve the specific application based on the fact that the fuel for combustion is a solid carbonaceous fuel, and that the specific application preselected is A steam generator application is used to generate a predetermined output 62 therein, wherein the preselected particular application is being used to generate the predetermined output 62 . The solids consisting mainly of CaSO4 are separated from the gas formed by the combustion of CaS 86 and air 88 in the curvilinear separator 70, which is formed by the combustion of CaS 86 and air 88 in the curvilinear separator 70, and as shown in Figure 3b , the existing steam generator 66 has been modified to implement the curve splitter. Such CaSO4 is used for subsequent recycling from curve separator 70 to reduction reactor 76, as indicated by arrow 90 in FIG. The coal mentioned later is represented by arrow 92 in Fig. 3b) and CaCO (the CaCO mentioned later is represented by arrow 94 in Fig. is supplied to produce a predetermined output 62 within the reduction reactor 76 based on the properties of a preselected particular application, where the preselected particular application is an improved steam generator application. In addition, the gases generated in curvilinear separator 70 by the combustion of CaS 86 and air 88 in curvilinear separator 70 (as shown in FIG. 70) in turn through the existing steam generator 66 (as indicated by arrow 96 in FIG. 3b) to absorb heat from such gas 96 within the existing steam generator 66. At the same time, any ash particles and/or solid particles that may be generated by the combustion of CaS 86 and air 88 in the curve separator 70 can be collected at the bottom of the existing steam generator 66 (shown by arrow 98 in Figure 3b) , where as shown in FIG. 3 b , the existing steam generator 66 has been suitably modified to thereby implement such a curvilinear separator 70 that does not take away the gas 96 intended to flow through the existing steam generator 66 .

Referring next to FIG. 4 of this patent application document, there is depicted a schematic diagram of a third exemplary embodiment of the mode of operation of the hot solids method 10 of the present invention, generally indicated by the reference numerals in FIG. 4 100 indicates that said third embodiment is adapted to operate in accordance with the present invention to generate a predetermined output based on the properties of a pre-selected specific application, the latter mentioned predetermined output being represented by arrow 102 in FIG. 4 , wherein said pre-selected specific application An application is being used to generate the predetermined output 102, and the pre-selected particular application is a CO2 capture-ready thermal solids combustion application. With further reference to FIG. 4, a reduction reactor, generally indicated by reference numeral 104 in FIG. 4, and an oxidation reactor, generally indicated by reference numeral 106 in FIG. Three exemplary embodiments 100 are used in the thermal solids method 10 of the present invention, said third exemplary embodiment being operable in accordance with the present invention to generate a predetermined output 102 based on pre-selected application-specific properties, wherein said pre-selected The selected specific application is being used to generate the predetermined output 102, and the pre-selected specific application is a CO2 capture-ready thermal solid combustion application. Next, according to the third exemplary embodiment 100 of the mode of operation of the hot solid process 10 of the present invention, the solid carbonaceous fuel (such as, but not limited to, coal, the latter mentioned coal in the Indicated by arrow 108 in FIG. 4 ) for indirect combustion with air. For this reason, the CaCO3 added for the third exemplary embodiment 100 of the mode of operation of the hot solid process 10 according to the invention (the latter mentioned CaCO3 is indicated by the arrow 110 in FIG. 4 ) is also input to the reduction reactor 104 And supply. Such CaCO 110 added according to the third exemplary embodiment 100 of the mode of operation of the hot solid process 10 of the present invention is used to operate to capture the sulfur contained in the solid carbonaceous fuel 108 in the reduction reactor 104, In order to thereby generate CaS therefrom in the reduction reactor 104 . The latter CaS (indicated by arrow 112 in FIG. 4 ) is then withdrawn therefrom as output from the reduction reactor 104, after which such CaS 112 will be supplied as input to the oxidation reactor 106. In the oxidation reactor 106, such CaS 112 burns in an exothermic reaction with air, indicated by arrow 114 in FIG. CaSO4 is generated in the oxidation reactor 106 .

With further reference to this figure, the CaSO4 (indicated by arrow 116 in FIG. 4) is intended to be subsequently withdrawn as the output of the oxidation reactor 106, after which the CaSO4 is intended to be recycled into the reduction reactor 104 as an input to provide Combustion of the solid carbonaceous fuel 108, and the oxygen and heat required for the reduction of CaSO 116 to CaS 112 are simultaneously achieved in the reduction reactor 104, thereby achieving continuous recirculation therein. Combustion of solid carbonaceous fuel 108 in reduction reactor 104 is used to cause predetermined output 102 to be produced in reduction reactor 104, and the carbon and hydrogen contained in solid carbonaceous fuel 108 in the combustion of such solid carbonaceous fuel 108 process, whereby a product gas consisting of CO2 and H2O is generated therefrom. H2O can then be removed from such product gas, so that the residue of such product gas is in a suitable form so that the residue can be used as a predetermined output 102 by using the hot solid process 10 of the present invention A third exemplary embodiment of the mode of operation 100 produces such that reservations are captured based on the nature of a pre-selected specific application that is being used to generate such a capture reservation predetermined output 102 , and the pre-selected specific application is a thermal solid combustion application reserved for CO2 capture.

Referring next to Figure 5 of this patent application document, there is depicted a schematic diagram of a fourth exemplary embodiment of the mode of operation of the hot solids method 10 of the present invention, generally indicated by the reference numerals in Figure 5 118 indicates that said fourth embodiment is used to operate in accordance with the present invention to generate a predetermined output based on the properties of a pre-selected specific application, the latter mentioned predetermined output being represented by arrow 120 in FIG. 5 , wherein said pre-selected specific application An application is being used to generate the predetermined output 120, and the pre-selected particular application is reserved for a thermal solids gasification application for CO2 capture. With further reference to FIG. 5, a reduction reactor, generally indicated by reference numeral 122 in FIG. 5, and an oxidation reactor, generally indicated by reference numeral 124 in FIG. Four exemplary embodiments 118 are used in the thermal solids method 10 of the present invention, the fourth exemplary embodiment being operable in accordance with the present invention to produce a predetermined output 120 based on preselected application-specific properties, wherein the pre-selected The selected specific application is being used to generate the predetermined output 120, and the pre-selected specific application is a CO2 capture-ready thermal solids gasification application. Next, according to the fourth exemplary embodiment 118 of the mode of operation of the hot solid process 10 of the present invention, the solid carbonaceous fuel (such as, but not limited to, coal, the latter mentioned coal in the Indicated by arrow 126 in Figure 5) is used to effect gasification. For this reason, the CaCO3 added for the fourth exemplary embodiment 118 of the mode of operation of the hot solid process 10 according to the invention (the latter CaCO3 is indicated by arrow 128 in FIG. 5 ) is also used as input to the reduction reactor 122 And supply. Such CaCO 128 added according to the fourth exemplary embodiment 118 of the mode of operation of the hot solid process 10 of the present invention is used to operate to capture the sulfur contained in the solid carbonaceous fuel 126 in the reduction reactor 122, In order to thereby generate CaS therefrom in the reduction reactor 122 . The latter CaS (indicated by arrow 130 in FIG. 5 ) is then intended to be withdrawn therefrom as output from the reduction reactor 122, after which such CaS 130 will be supplied as input to the oxidation reactor 124. In the oxidation reactor 124, such CaS 130 is used to carry out the reaction. Air (the latter air is indicated by arrow 132 in FIG. 5 ) is supplied as input to the oxidation reactor 124 in order thereby to be able to generate CaSO by reaction of CaS 130 in the oxidation reactor 124.

Referring further to this figure, such CaSO4, indicated by arrow 134 in FIG. To provide the oxygen and heat required for simultaneous gasification of solid carbonaceous fuel 126 and reduction of CaSO 134 to CaS 130 in reduction reactor 122, thereby achieving continuous recirculation therein. The gasification of the solid carbonaceous fuel 126 in the reduction reactor 122 is used to cause the predetermined output 120 to be produced in the reduction reactor 122, after which the carbon and hydrogen contained in the solid carbonaceous fuel converted during the gasification process to generate product gases including CO2 and H2O as well as CO and H2. HO can then be removed from such product gas so that the residue of such product gas is in a suitable form so that it can be used as a predetermined output 120 by using the hot solids process 10 of the present invention A fourth exemplary embodiment 118 of the mode of operation produces such that reservations are captured based on the nature of a pre-selected specific application that is being used to generate such a capture reservation predetermined output 120, And the pre-selected specific application is a thermal solid gasification application reserved for CO2 capture.

Referring next to FIG. 6 of this patent application document, there is depicted a schematic diagram of a fifth exemplary embodiment of the mode of operation of the hot solids method 10 of the present invention, generally indicated by the reference numerals in FIG. 6 136 indicates that said fifth embodiment is intended to operate in accordance with the present invention to generate a predetermined output based on pre-selected properties of a particular application, the latter mentioned predetermined output being indicated by reference numeral 138 in FIG. 6 , wherein said pre-selected The specific application selected is being used to generate the predetermined output 138 and the pre-selected specific application is a CO2 capture thermal solids combustion application. With further reference to FIG. 6, a reduction reactor, generally indicated by reference numeral 140 in FIG. 6, and an oxidation reactor, generally indicated by reference numeral 142 in FIG. A fifth exemplary embodiment 136 for use in the thermal solids method 10 of the present invention is operable in accordance with the present invention to produce a predetermined output 138 based on preselected application-specific properties, wherein the A preselected particular application is being used to generate the predetermined output 138 and the preselected particular application is a CO2 capture thermal solids combustion application. Next, according to the fifth exemplary embodiment 136 of the mode of operation of the hot solid process 10 of the present invention, the solid carbonaceous fuel (such as, but not limited to, coal, the latter mentioned coal in the Indicated by arrow 144 in FIG. 6 ) for indirect combustion with air. For this reason, the CaCO3 added for the fifth exemplary embodiment 136 of the mode of operation of the hot solid process 10 according to the invention (the latter mentioned CaCO3 is indicated by arrow 146 in FIG. 6 ) is also input to the reduction reactor 140 And supply. Such CaCO 146 added according to the fifth exemplary embodiment 136 of the mode of operation of the hot solid process 10 of the present invention is used to operate to capture the sulfur contained in the solid carbonaceous fuel 144 in the reduction reactor 140, In order to thereby generate CaS therefrom in the reduction reactor 140 . The latter CaS (indicated by arrow 148 in FIG. 6 ) is then intended to be withdrawn therefrom as output from the reduction reactor 140, after which such CaS 148 is intended to be supplied as input to the oxidation reactor 142. In the oxidation reactor 142, such CaS 148 burns in an exothermic reaction with air, indicated by arrow 150 in FIG. CaSO4 is generated in the oxidation reactor 142 .

Referring further to this figure, such CaSO4 (shown by arrow 152 in FIG. 6) is then intended to be discharged as an output of the oxidation reactor 142, after which such CaSO4 is intended to be recycled into the reduction reactor 140 as an input , to provide the oxygen and heat required for simultaneous combustion of solid carbonaceous fuel 144 and reduction of CaSO 152 to CaS 148 in reduction reactor 140, thereby achieving continuous recirculation therein. The combustion of the solid carbonaceous fuel 144 in the reduction reactor 140 is used to cause the predetermined output 138 to be produced in the reduction reactor 140, after which the carbon and hydrogen contained in the solid carbonaceous fuel 144 in such solid carbonaceous fuel 144 During the combustion process, it is converted into a product gas containing CO2 and H2O. HO can then be removed from such product gas so that the residue of such product gas is in a suitable form so that it can be used as a predetermined output 138 by using the hot solids method 10 of the present invention A fifth exemplary embodiment 136 of the mode of operation of , produced so that trapping is performed on the basis of preselected application-specific properties by any trapping means suitable for such use, which trapping means is schematically shown in FIG. depicting, wherein a schematic depiction of such capture components is indicated by reference numeral 154, said preselected particular application being used to generate such predetermined output 138, and said preselected particular application being a CO2 capture thermal solids combustion application .

Referring next to Figure 7 of this patent application document, there is depicted a schematic diagram of a sixth exemplary embodiment of the mode of operation of the hot solids method 10 of the present invention, generally indicated by the reference numerals in Figure 7 156 indicates that said sixth exemplary embodiment is adapted to operate in accordance with the present invention to generate a predetermined output based on preselected application-specific properties, the latter mentioned predetermined output being indicated by reference numeral 158 in FIG. 7 , wherein said A preselected particular application is being used to generate the predetermined output 158 and the preselected particular application is a CO2 capture thermal solids gasification application. With further reference to FIG. 7, a reduction reactor, generally indicated by reference numeral 160 in FIG. 7, and an oxidation reactor, generally indicated by reference numeral 162 in FIG. Six exemplary embodiments 156 are used in the thermal solids method 10 of the present invention, the sixth exemplary embodiment is operable in accordance with the present invention to produce a predetermined output 158 based on preselected application-specific properties, the preselected The specific application of is being used to generate the predetermined output 158, and the pre-selected specific application is a CO2 capture thermal solids gasification application. Next, according to the sixth exemplary embodiment 156 of the mode of operation of the hot solid process 10 of the present invention, the solid carbonaceous fuel (such as, but not limited to, coal, the latter mentioned coal in the Indicated by arrow 164 in FIG. 7 ) is used to perform gasification. To this end, the CaCO 3 added for the sixth exemplary embodiment 156 of the mode of operation of the hot solid process 10 according to the invention (the latter mentioned CaCO 3 is indicated by arrow 166 in FIG. 7 ) is also supplied to the reduction reactor 160 . Such CaCO3166 added according to the sixth exemplary embodiment 156 of the mode of operation of the hot solid process 10 of the present invention is used to operate to capture the sulfur contained in the solid carbonaceous fuel 164 in the reduction reactor 160 so that CaS is thereby generated therefrom in the reduction reactor 160 . The latter CaS (indicated by arrow 168 in FIG. 7 ) is then used to withdraw therefrom as output of reduction reactor 160, after which such CaS 168 is supplied as input to oxidation reactor 162. In the oxidation reactor 162, such CaS 168 is used to carry out the reaction. Air is used as an input to the oxidation reactor 162 to be supplied to thereby generate CaSO by the reaction of CaS 168 in the oxidation reactor 162, the latter air being indicated by arrow 170 in FIG. 7 .

With further reference to this figure, such CaSO4 represented by arrow 172 in FIG. To provide the oxygen and heat required for simultaneous gasification of the solid carbonaceous fuel 164 and reduction of CaSO 172 to CaS 168 in the reduction reactor 160, thereby achieving continuous recirculation therein. The gasification of the solid carbonaceous fuel 164 in the reduction reactor 160 is used to cause the predetermined output 158 to be produced in the reduction reactor 160, after which the carbon and hydrogen contained in the solid carbonaceous fuel During the gasification process, it is converted into product gases including CO2 and H2O as well as CO and H2. HO can then be removed from such product gas so that the residue of such product gas is in a suitable form so that it can be used as a predetermined output 158 by using the hot solids process 10 of the present invention A sixth exemplary embodiment 156 of the mode of operation of , produced so as to be capable of trapping based on pre-selected application-specific properties by any trapping member suitable for such use, such trapping member being schematically illustrated in FIG. 7 wherein a schematic depiction of such capture components is indicated by reference numeral 174, and wherein said preselected specific application is being used to generate a predetermined output 158, said preselected specific application being CO2 capture of hot solids gas application.

Referring next to FIG. 8 of this patent application document, there is depicted a schematic diagram of a seventh exemplary embodiment of the mode of operation of the hot solids method 10 of the present invention, generally indicated by the reference numerals in FIG. 8 176 indicates that said seventh embodiment is adapted to operate in accordance with the present invention to generate a predetermined output based on preselected application-specific properties, the latter mentioned predetermined output being indicated by reference numeral 178 in FIG. 8 , wherein said preselected The specific application of is being used to generate the predetermined output 178, and the pre-selected specific application is a partial CO2 capture thermal solid combustion application. With further reference to FIG. 8, a reduction reactor, generally indicated by reference numeral 180 in FIG. 8, and an oxidation reactor, generally indicated by reference numeral 182 in FIG. Seven exemplary embodiments 176 for use in the thermal solids method 10 of the present invention are operable in accordance with the present invention to produce predetermined outputs 178 based on preselected application-specific properties, the preselected The specific application of is being used to generate the predetermined output 178, and the pre-selected specific application is a partial CO2 capture thermal solid combustion application. Next, according to the seventh exemplary embodiment 176 of the mode of operation of the hot solids process 10 of the present invention, the solid carbonaceous fuel (such as, but not limited to, coal, the latter mentioned coal in Indicated by arrow 184 in Figure 8) for indirect combustion with air. For this reason, the CaCO3 added for the seventh exemplary embodiment 176 of the mode of operation of the hot solid process 10 according to the invention (the latter mentioned CaCO3 is indicated by arrow 186 in FIG. 8 ) is also used as input to the reduction reactor 180 And supply. Such CaCO 186 added according to the seventh exemplary embodiment 176 of the mode of operation of the hot solid process 10 of the present invention is used to operate to capture the sulfur contained in the solid carbonaceous fuel 184 in the reduction reactor 180, In order to thereby generate CaS therefrom in the reduction reactor 180 . The latter CaS (indicated by arrow 188 in FIG. 8 ) is then used to withdraw therefrom as output of reduction reactor 180, after which such CaS 188 is supplied as input to oxidation reactor 182. In the oxidation reactor 182, such CaS 188 burns in an exothermic reaction with air, the latter air being indicated by arrow 190 in FIG. In order to be able to thereby generate CaSO4 in the oxidation reactor 182 .

Referring further to this figure, such CaSO4 (shown by arrow 192 in FIG. 8 ) is then used for discharge as output of oxidation reactor 182, after which such CaSO4 192 is used for recycling as input of reduction reactor 190 to Wherein, to provide in the reduction reactor 180 simultaneously the combustion of the solid carbonaceous fuel 184, and the required oxygen and heat for the reduction of CaSO 192 to CaS 188, thereby realizing continuous recirculation therein. The combustion of the solid carbonaceous fuel 184 in the reduction reactor 180 is used to cause the predetermined output 178 to be produced in the reduction reactor 180, after which the carbon and hydrogen contained in the solid carbonaceous fuel 184 The combustion process converts to product gases including CO2 and H2O. HO can then be removed from such product gas so that the residue of such product gas is in a suitable form so that it can be used as a predetermined output 178 by using the hot solids method 10 of the present invention A seventh exemplary embodiment 176 of the mode of operation is generated so that partial capture can be performed by any partial capture member suitable for such use based on preselected application-specific properties, such partial capture member being shown in FIG. 8 wherein a schematic depiction of such a partial capture member is indicated by reference numeral 194, and wherein said preselected particular application is being used to generate such predetermined output 178, said preselected particular application being partial CO2 Capture heat for solid combustion applications.

Referring next to FIG. 9 of this patent application document, there is depicted a schematic diagram of an eighth exemplary embodiment of the mode of operation of the hot solids method 10 of the present invention, said eighth exemplary embodiment being generally indicated by reference numerals in FIG. 9 196 indicates that said eighth exemplary embodiment is adapted to operate in accordance with the present invention to generate a predetermined output based on pre-selected application-specific properties, the latter mentioned predetermined output being indicated by reference numeral 198 in FIG. 9 , said pre-selected The specific application selected is being used to generate the predetermined output 198 and the pre-selected specific application is a partial CO2 capture thermal solids gasification application. With further reference to FIG. 9, a reduction reactor, generally indicated by reference numeral 200 in FIG. 9, and an oxidation reactor, generally indicated by reference numeral 202 in FIG. An eighth exemplary embodiment 196 for use in the thermal solids method 10 of the present invention is operable in accordance with the present invention to produce a predetermined output 198 based on preselected application-specific properties, wherein the pre-selected The specific application selected is being used to generate the predetermined output 198 and the pre-selected specific application is a partial CO2 capture thermal solids gasification application. Next, according to the eighth exemplary embodiment 196 of the mode of operation of the hot solid process 10 of the present invention, for the solid carbonaceous fuel (such as, but not limited to, coal, mentioned later) supplied as input to the reduction reactor 200 Coal is indicated by arrow 204 in Figure 9) for gasification. To this end, the CaCO 3 added for the eighth exemplary embodiment 196 of the mode of operation of the hot solids method 10 according to the invention (indicated by arrow 206 in FIG. 9 ) is also supplied to the reduction reactor 200 . Such CaCO 206 added according to the eighth exemplary embodiment 196 of the mode of operation of the hot solid process 10 of the present invention is used to operate to capture the sulfur contained in the solid carbonaceous fuel 204 in the reduction reactor 200, In order to thereby generate CaS therefrom in the reduction reactor 200 . The latter CaS (indicated by arrow 208 in FIG. 9 ) is then used to withdraw therefrom as an output of the reduction reactor 200, after which such CaS 208 is supplied as input to the oxidation reactor 202. In the oxidation reactor 202, such CaS 208 is used to carry out the reaction. Air (the latter air is indicated by arrow 210 in FIG. 9 ) is supplied as an input to the oxidation reactor 202 in order thereby to be able to generate CaSO in the oxidation reactor 202 by the reaction of CaS 208 .

Referring further to this figure, such CaSO4 (shown by arrow 212 in FIG. 9 ) is then used for discharge as an output of the oxidation reactor 202, after which such CaSO4 is used for recycling as an input of the reduction reactor 200 to Wherein, to provide the gasification of the solid carbonaceous fuel 204 simultaneously in the reduction reactor 200, and the required oxygen and heat for the reduction of the CaSO 212 to the CaS 208, thereby realizing continuous recirculation therein. The gasification of the solid carbonaceous fuel 204 in the reduction reactor 200 is used to cause the predetermined output 198 to be produced in the reduction reactor 200, after which the carbon and hydrogen contained in the solid carbonaceous fuel During the gasification process, it is converted into product gases including CO2 and H2O as well as CO and H2. HO can then be removed from such product gas so that the residue of such product gas is in a suitable form so that it can be used as a predetermined output 198 by using the hot solids method 10 of the present invention The eighth exemplary embodiment 196 of the mode of operation is generated so that partial trapping can be performed by any partial trapping member suitable for such use based on pre-selected application-specific properties, such partial trapping member being shown in FIG. 9 wherein a schematic depiction of such a partial capture member is indicated by reference numeral 214, and wherein said preselected particular application is being used to generate such predetermined output 198, said preselected particular application being partial CO2 Capture heat for solids gasification applications.

While the above-mentioned embodiments of the invention include calcium oxide, the invention contemplates that the oxides may include, for example, metal oxides composed of iron such as FeO.

While preferred embodiments of the invention have been shown and described in the present application, it should be understood that various changes may be made thereto without departing from the spirit and scope of the invention as set forth in the appended claims. Modify and replace. Therefore, it should be further understood that, according to the description of the present invention in this patent application document, the present invention is described by way of example and not limitation.

Claims (12)

1. hot solids method, the alternative operation of said hot solids method is to produce predetermined output based on the character of application-specific, and the predetermined output of wherein said generation is used for said application-specific, and said method comprises:

Preliminary election goes out application-specific from one group of application-specific; Said application-specific group comprises that the live steam producer is used, the improvement type vapour generator is used, CO2 capture reserve hot solids burn application, CO2 capture reserve that the hot solids gasification is used, CO2 captures the hot solids burn application, CO2 capture that the hot solids gasification is used, portion C O2 captures the hot solids burn application and portion C O2 capture the hot solids gasification in using at least both, the said predetermined output that wherein generates is used for said application-specific;

First reactor drum as the reduction reactor running is provided;

Second reactor drum as the oxidation reactor running is provided;

Sulfur-containing solid carbonaceous fuel and calcium source are fed to said reduction reactor as input;

Air is fed to said oxidation reactor as input;

In said reduction reactor, capture the sulphur in the said sulfur-containing solid carbonaceous fuel, thereby in said reduction reactor, generate CaS with said calcium source;

Said CaS as the output of said reduction reactor and discharge, and is fed to said oxidation reactor with this type of CaS as input subsequently;

In said oxidation reactor, generate CaSO4 with said CaS;

Said CaSO4 as the output of said oxidation reactor and discharge, and is fed to said reduction reactor with this type of CaSO4 as input subsequently;

Said CaSO4 in the said reduction reactor is originated and origin of heat as oxygen; Thereby in said reduction reactor, from said sulfur-containing solid carbonaceous fuel, produce said predetermined output based on the character of said application-specific, the said predetermined output that wherein generates is used for said application-specific; And

Said predetermined output is discharged from said reduction reactor.

2. hot solids method according to claim 1 is characterized in that the said application-specific of selecting in advance is the application of improvement type vapour generator.

3. hot solids method according to claim 2 is characterized in that said oxidation reactor is included in the cyclone of implementing in the existing vapour generator, and said existing vapour generator has been transformed to implement said cyclone.

4. hot solids method according to claim 2 is characterized in that said oxidation reactor is included in the curve separator of implementing in the existing vapour generator, and said existing vapour generator has been transformed to implement said curve separator.

5. hot solids method according to claim 1 is characterized in that the said application-specific of selecting in advance is that CO2 captures the hot solids burn application.

6. hot solids method according to claim 5 is characterized in that further comprising and provides exercisable capture member to capture the step of the said predetermined output of from said reduction reactor, discharging therein.

7. hot solids method according to claim 1; It is characterized in that the said application-specific of selecting in advance is that CO2 captures hot solids gasification application; And said method further comprises provides exercisable capture member, to capture the said predetermined output of from said reduction reactor, discharging therein.

8. hot solids method according to claim 1; It is characterized in that the said application-specific of selecting in advance captures the hot solids burn application for portion C O2; And said method further comprises provides exercisable part to capture member, partly to capture the said predetermined output of from said reduction reactor, discharging therein.

9. hot solids method according to claim 1; It is characterized in that the said application-specific of selecting in advance captures hot solids gasification application for portion C O2; And said method further comprises provides exercisable part to capture member, partly to capture the said predetermined output of from said reduction reactor, discharging therein.

10. hot solids method according to claim 1 is characterized in that being fed to as input the preferred CaCO3 in said calcium source of said reduction reactor.

11. an alternative operation is to produce the hot solids method of predetermined output based on the character of application-specific, the said predetermined output that wherein generates is used for said application-specific, and said method comprises:

Preliminary election goes out application-specific from one group of application-specific; Said application-specific group comprises that the live steam producer is used, the improvement type vapour generator is used, CO2 capture reserve hot solids burn application, CO2 capture reserve that the hot solids gasification is used, CO2 captures the hot solids burn application, CO2 capture that the hot solids gasification is used, portion C O2 captures the hot solids burn application and portion C O2 capture the hot solids gasification in using at least both, the said predetermined output that wherein generates is used for said application-specific;

First reactor drum as the reduction reactor running is provided;

Second reactor drum as the oxidation reactor running is provided;

Sulfur-containing solid carbonaceous fuel and oxide compound are fed to said reduction reactor as input;

Air is fed to said oxidation reactor as input;

In said reduction reactor, capture the sulphur in the said sulfur-containing solid carbonaceous fuel with said oxide compound;

In said oxidation reactor, generate oxide compound;

Said oxide compound as the output of said oxidation reactor and discharge, and is fed to said reduction reactor with this type oxide as input subsequently;

Said oxide compound in the said reduction reactor is originated and origin of heat as oxygen; Thereby in said reduction reactor, from said sulfur-containing solid carbonaceous fuel, produce said predetermined output based on the character of said application-specific, the said predetermined output that wherein generates is used for said application-specific; And

Let said predetermined output from said reduction reactor, discharge.

12. hot solids method according to claim 11 is characterized in that said oxide compound is a kind of in quicklime and the MOX.

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