Abstract: A gasifier 10 includes a first chemical process loop 12 having an exothermic oxidizer reactor 14 and an endothermic reducer reactor 16. CaS is oxidized in air in the oxidizer reactor 14 to form hot CaSO4 which is discharged to the reducer reactor 16. Hot CaSO4 and carbonaceous fuel received in the reducer reactor 16 undergo an endothermic reaction utilizing the heat content of the CaSO4, the carbonaceous fuel stripping the oxygen from the CaSO4 to form CaS and a CO rich syngas. The CaS is discharged to the oxidizer reactor 14 and the syngas is discharged to a second chemical process loop 52. The second chemical process loop 52 has a water-gas shift reactor 54 and a calciner 42. The CO of the syngas reacts with gaseous H2O in the shift reactor 54 to produce H2 and CO2. The CO2 is captured by CaO to form hot CaCO3 in an exothermic reaction.

Abstract: A gasifier 10 includes a first chemical process loop 12 having an exothermic oxidizer reactor 14 and an endothermic reducer reactor 16. CaS is oxidized in air in the oxidizer reactor 14 to form hot CaSO4 which is discharged to the reducer reactor 16. Hot CaSO4 and carbonaceous fuel received in the reducer reactor 16 undergo an endothermic reaction utilizing the heat content of the CaSO4, the carbonaceous fuel stripping the oxygen from the CaSO4 to form CaS and a CO rich syngas. The CaS is discharged to the oxidizer reactor 14 and the syngas is discharged to a second chemical process loop 52. The second chemical process loop 52 has a water-gas shift reactor 54 and a calciner 42. The CO of the syngas reacts with gaseous H2O in the shift reactor 54 to produce H2 and CO2. The CO2 is captured by CaO to form hot CaCO3 in an exothermic reaction.

Abstract: A gasifier 10 includes a first chemical process loop 12 having an exothermic oxidizer reactor 14 and an endothermic reducer reactor 16. CaS is oxidized in air in the oxidizer reactor 14 to form hot CaSO4 which is discharged to the reducer reactor 16. Hot CaSO4 and carbonaceous fuel received in the reducer reactor 16 undergo an endothermic reaction utilizing the heat content of the CaSO4, the carbonaceous fuel stripping the oxygen from the CaSO4 to form CaS and a CO rich syngas. The CaS is discharged to the oxidizer reactor 14 and the syngas is discharged to a second chemical process loop 52. The second chemical process loop 52 has a water-gas shift reactor 54 and a calciner 42. The CO of the syngas reacts with gaseous H2O in the shift reactor 54 to produce H2 and CO2. The CO2 is captured by CaO to form hot CaCO3 in an exothermic reaction.

Abstract: A system for reducing carbon dioxide emissions from gasses generated in burning fossil fuel, includes a vessel, separator and reheater. The upper portion of the vessel receives downward flowing, first type solid particles capable of absorbing heat from upward flowing gasses and second type solid particles capable of capturing carbon dioxide from the gasses. The separator separates the second type solid particles with the captured carbon dioxide from the gasses discharged from the first vessel discharge, and directs the separated second type solid particles with the captured carbon dioxide to a separator discharge. The reheater directs the first type solid particles and the second type solid particles with the captured carbon dioxide in a downwardly flow to a first reheater discharge, such that heat from the first type solid particles causes the captured carbon dioxide to be released from the second type solid particles.

Abstract: A system for reducing carbon dioxide emissions from gasses generated in burning fossil fuel, includes a vessel, separator and reheater. The upper portion of the vessel receives downward flowing, first type solid particles capable of absorbing heat from upward flowing gasses and second type solid particles capable of capturing carbon dioxide from the gasses. The separator separates the second type solid particles with the captured carbon dioxide from the gasses discharged from the first vessel discharge, and directs the separated second type solid particles with the captured carbon dioxide to a separator discharge. The reheater directs the first type solid particles and the second type solid particles with the captured carbon dioxide in a downwardly flow to a first reheater discharge, such that heat from the first type solid particles causes the captured carbon dioxide to be released from the second type solid particles.

Abstract: A gasifier 10 includes a first chemical process loop 12 having an exothermic oxidizer reactor 14 and an endothermic reducer reactor 16. CaS is oxidized in air in the oxidizer reactor 14 to form hot CaSO4 which is discharged to the reducer reactor 16. Hot CaSO4 and carbonaceous fuel received in the reducer reactor 16 undergo an endothermic reaction utilizing the heat content of the CaSO4, the carbonaceous fuel stripping the oxygen from the CaSO4 to form CaS and a CO rich syngas. The CaS is discharged to the oxidizer reactor 14 and the syngas is discharged to a second chemical process loop 52. The second chemical process loop 52 has a water-gas shift reactor 54 and a calciner 42. The CO of the syngas reacts with gaseous H2O in the shift reactor 54 to produce H2 and CO2. The CO2 is captured by CaO to form hot CaCO3 in an exothermic reaction.

Abstract: A gasifier 10 includes a first chemical process loop 12 having an exothermic oxidizer reactor 14 and an endothermic reducer reactor 16. CaS is oxidized in air in the oxidizer reactor 14 to form hot CaSO4 which is discharged to the reducer reactor 16. Hot CaSO4 and carbonaceous fuel received in the reducer reactor 16 undergo an endothermic reaction utilizing the heat content of the CaSO4, the carbonaceous fuel stripping the oxygen from the CaSO4 to form CaS and a CO rich syngas. The CaS is discharged to the oxidizer reactor 14 and the syngas is discharged to a second chemical process loop 52. The second chemical process loop 52 has a water-gas shift reactor 54 and a calciner 42. The CO of the syngas reacts with gaseous H2O in the shift reactor 54 to produce H2 and CO2. The CO2 is captured by CaO to form hot CaCO3 in an exothermic reaction.

Abstract: A gasifier 10 includes a first chemical process loop 12 having an exothermic oxidizer reactor 14 and an endothermic reducer reactor 16. CaS is oxidized in air in the oxidizer reactor 14 to form hot CaSO4 which is discharged to the reducer reactor 16. Hot CaSO4 and carbonaceous fuel received in the reducer reactor 16 undergo an endothermic reaction utilizing the heat content of the CaSO4, the carbonaceous fuel stripping the oxygen from the CaSO4 to form CaS and a CO rich syngas. The CaS is discharged to the oxidizer reactor 14 and the syngas is discharged to a second chemical process loop 52. The second chemical process loop 52 has a water-gas shift reactor 54 and a calciner 42. The CO of the syngas reacts with gaseous H2O in the shift reactor 54 to produce H2 and CO2. The CO2 is captured by CaO to form hot CaCO3 in an exothermic reaction.

Abstract: A gasifier 10 includes a first chemical process loop 12 having an exothermic oxidizer reactor 14 and an endothermic reducer reactor 16. CaS is oxidized in air in the oxidizer reactor 14 to form hot CaSO4 which is discharged to the reducer reactor 16. Hot CaSO4 and carbonaceous fuel received in the reducer reactor 16 undergo an endothermic reaction utilizing the heat content of the CaSO4, the carbonaceous fuel stripping the oxygen from the CaSO4 to form CaS and a CO rich syngas. The CaS is discharged to the oxidizer reactor 14 and the syngas is discharged to a second chemical process loop 52. The second chemical process loop 52 has a water-gas shift reactor 54 and a calciner 42. The CO of the syngas reacts with gaseous H2O in the shift reactor 54 to produce H2 and CO2. The CO2 is captured by CaO to form hot CaCO3 in an exothermic reaction.

Abstract: A furnace (10) includes a series of lower compartments (18) extending in a vertical arrangement, with at least one of the lower compartments (18) having one or more fuel nozzles (20) which tangentially fires fuel into the combustion chamber at an offset from a diagonal (DD) passing through opposed corners of the combustion chamber. At least one of the lower compartments (18) has one or more air nozzles (22) which tangentially introduces air into the combustion chamber along an offset direction which is offset from the diagonal (DD) to the same side as the fuel firing offset direction. The tangentially fired air and the offset fired fuel create a swirling fireball (RB) in the combustion chamber.

Abstract: A recuperative and conductive heat transfer system (10, 10′) that is operative to effect therewith the heating within the second portion (20, 20′) of the heat transfer system (10, 10′) of a “working fluid” flowing through the heat s transfer surfaces (32, 32′) as a consequence of the transfer thereto by conduction of heat from a multiplicity of regenerative solids (24, 24′). The multiplicity of regenerative solids (24, 24′) derive their heat from a recuperation thereby within the first portion (12, 12′) of the heat transfer system (10, 10′) from either an internally generated or an externally generated source of heat (22, 22′).

Abstract: A recuperative and conductive heat transfer system (10, 10′) that is operative to effect therewith the heating within the second portion (20, 20′) of the heat transfer system (10, 10′) of a “working fluid” flowing through the heat transfer surfaces (32, 32′) as a consequence of the transfer thereto by conduction of heat from a multiplicity of regenerative solids (24, 24′). The multiplicity of regenerative solids (24, 24′) derive their heat from a recuperation thereby within the first portion (12, 12′) of the heat transfer system (10, 10′) from either an internally generated or an externally generated source of heat (22, 22′).

Abstract: A method of separating unburned Carbon, as particulate matter, from the flyash produced as a result of the combustion process occurring in a pulverized-coal fired steam generating power plant is disclosed. More particularly the invention separates the flyash into a coarse product group and a fine product group by utilizing the differences in specific gravity between the Carbon particles and remaining flyash as well as utilization of the dynamic classification characteristics of a rotary classifier to effect the separation whereby at least one of the two product groups comprises a relatively low weight percentage of unburned Carbon while yet comprising a relatively high percentage of the total mass of product recovered after separation.

Abstract: A steam generator apparatus which includes an enclosure comprising vertically extending front and back waterwalls joined by opposed spaced first and second waterwalls, The enclosure also includes a plurality of spaced vertically extending windboxes, each of the windboxes faces the interior of the enclosure. Each of the windboxes comprises a plurality of modules that are configured for installation at respective elevations, each of the modules being dimensioned and configured for shipment to the installation site. Some forms of the invention further includes a vertically extending truss assembly and the ignitor and auxiliary air compartments are supported on the truss assembly. Other forms of the invention include air ducting supplying air to air compartments and the truss assembly extends within the ducting. Still other forms of the invention may utilize the truss assembly without the modular windbox.

Abstract: A clustered concentric tangential firing system (12) particularly suited for use in fossil fuel-fired furnaces (10) and a method of operating such furnaces (10) equipped with a clustered concentric tangential firing system (12).

Abstract: An incinerator, or furnace, receives low-level radiation waste from a nuclear installation in varying volumes and calorific values. A supplemental, conventional fuel is concomitantly supplied under the control of the exhaust temperature of the products of combustion. The low-level radiation waste and supplemental fuel are mixed with combustion air in a first stage where combustion is initiated, the products of combustion being flowed downward into a second stage where the combustion is complete prior to exhaust.

Abstract: A tangentially-fired furnace is disclosed in enough detail to illustrate the location of injection ports for excess air above the fireball of the combustion chamber to eliminate the swirl of the flue gases as the flue gases flow into the convection section, in order to produce a uniform mass flow and temperature pattern of the flue gases over the cross section of the furnace exit.

Abstract: A method for the cold start of a pulverized coal-fired furnace (10) without prior warm-up of the furnace wherein a supply of microfine pulverized coal (64) supplied from a micropulverizer (60) is combusted to generate a hot gas which is passed to a load-carrying mill (20) as the drying media for the coal pulverized therein. Pulverized coal entrained in the hot gas passes from the load-carrying mill to the load-carrying burner (18) of the furnace (10) and is ignited therein to produce a warm-up flame. A portion of the microfine pulverized coal (68) may also be admixed with the pulverized coal from the load carrying mill (20) to enhance the reactivity thereof. An additional portion (66) of the microfine pulverized coal may be used to fire a pilot igniter to ignite the pulverized coal supplied to the load-carrying burners (18) from the load-carrying mill (20).

Abstract: An improved nozzle tip (10) for a burner on a pulverized coal-fired furnace for receiving a stream of pulverized coal and air discharging from the coal delivery pipe (50) of the burner and directing the pulverized fuel and air stream into the furnace, is comprised of a base body (20), a replaceable highly abrasion resistant insert (30), and a replaceable highly temperature resistant end cap (40) which is readily attachable by mechanical means (28, 48) to the base body with the abrasion resistant insert disposed therein. The insert defines a highly abrasion resistant flow conduit through the nozzle tip from the discharge end of the base body to the receiving end of the end cap through which the pulverized fuel and air stream passes from the burner into the furnace.

Abstract: A tangentially-fired, pulverized coal burning furnace (10) having overfire air (OFA) introduced into the upper portion of the furnace. The fuel and air are introduced (36, 38) into the furnace at the burner level tangentially of an imaginary circle, so that the resultant fireball moves upwardly within the furnace with a rotational spin. The OFA is introduced (40, 42) tangentially of an imaginary circle, in the reverse rotational direction to that of the fireball, so that the exhaust gases flowing from the furnace to the rear gas pass (16) flows in a straight line, with little or no spin. The OFA is made up of a mixture of low pressure air and high pressure air of sufficient volume and pressure to nullify the spin of the fireball.