Clean combustion and equilibration equipment and methods are provided to progressively deliver, combust and equilibrate mixture of fuel, oxidant and aqueous diluent in a plurality of combustion regions and in one or more equilibration regions to further progress oxidation of products of incomplete c
Clean combustion and equilibration equipment and methods are provided to progressively deliver, combust and equilibrate mixture of fuel, oxidant and aqueous diluent in a plurality of combustion regions and in one or more equilibration regions to further progress oxidation of products of incomplete combustion, in a manner that sustains combustion while controlling temperatures and residence times sufficiently to reduce CO and NOx emissions to below 25 ppmvd, and preferably to below 3 ppmvd at 15% O2.
대표청구항▼
1. A method of cleanly reacting fluids in a reaction system having a compressor, a pilot region, with a pilot inlet, upstream of a plurality of reaction regions in streamwise flow upstream of an equilibration region having an equilibration region outlet feeding a turbine expander, having a multiplic
1. A method of cleanly reacting fluids in a reaction system having a compressor, a pilot region, with a pilot inlet, upstream of a plurality of reaction regions in streamwise flow upstream of an equilibration region having an equilibration region outlet feeding a turbine expander, having a multiplicity of expander stages or expanders, with a first interstage equilibration region configured between a first upstream expander stage or expander and a second downstream expander stage or expander, a downstream system outlet, and a controller controlling reactant, oxidant, and diluent delivery systems to respectively deliver reactant fluid comprising a reactant, oxidant fluid comprising an oxidant, and diluent fluid comprising a product of reaction in a higher concentration than in ambient air, into each of said reaction regions; the method comprising the steps of: delivering and heating one or more of reactant fluid, oxidant fluid, and diluent fluid to the pilot region, whereby forming a hot pilot fluid;delivering reactant fluid, oxidant fluid, and diluent fluid into each of said reaction regions other than from one of the pilot region and the reaction regions;reacting within each reaction region a portion of the reactant and the oxidant in the presence of diluent delivered into that reaction region, whereby forming hot liquid;providing into each reaction region some hot fluid from one of the pilot region and an upstream reaction region;equilibrating, in the equilibration region, a hot fluid from one of the upstream reaction regions;controlling the reactant, oxidant and diluent fluid flows entering said reaction regions;wherein maintaining in each of said reaction regions a hot reaction fluid temperature above a fluid self-ignition temperature TIGN for that reaction regions;wherein constraining a temperature of equilibrated hot fluid leaving the equilibration region outlet to within a prescribed temperature range less than about 1700° Celsius and greater than about 650° Celsius;wherein providing sufficient oxidant fluid in one or more downstream reaction zones with sufficient equilibration time in the equilibration region and in the first interstage equilibration region to reduce a residual volume concentration of residual intermediate reactant product in the equilibrated fluid leaving the system outlet to less than 50 ppmv when adjusted to a 15% oxidant basis; andwherein providing lower oxidant to reactant concentrations in an upstream portion of reaction zones than in a downstream portion of reaction zones and constraining a byproduct volume concentration of a primary diluent reaction byproduct to less than 50 ppmvd when adjusted to the 15% oxidant basis. 2. The method of reacting fluids of claim 1, comprising combusting fluids in a combustion system comprising a plurality of combustion regions in streamwise flow, wherein the reactant is a fuel comprising one of a hydrocarbon, hydrogen, carbon, or carbon monoxide, the oxidant is oxygen, and the diluent comprises one of carbon dioxide and water; the method comprising the steps of: delivering one or more of fuel fluid, oxidant fluid, and diluent fluid to the pilot region, whereby forming a hot pilot fluid;delivering fuel fluid, oxidant fluid, and diluent fluid into each combustion region other than from one of the pilot region and the combustion regions;controlling the oxidant fluid, fuel fluid, and diluent fluid flows entering said combustion regions;combusting a portion of diluted fuel-oxidant fluid formed thereby within each combustion region, whereby forming hot fluid;providing some hot fluid from the upstream region to a downstream combustion region; andequilibrating within the equilibration region, a hot combustion fluid formed upstream of the equilibration region;wherein delivery of hot pilot fluid, fuel fluid, oxidant fluid, and diluent fluid maintains the hot combustion fluid temperature above the fluid self-ignition temperature TIGN in each of said combustion regions;wherein constraining the temperature of the hot combustion fluid to within a prescribed temperature range less than about 1700° C., and greater than about 800° C. as it exits the equilibration region;wherein reducing the residual volume concentration of carbon monoxide (CO) in the equilibrated fluid leaving the system outlet to less than nine (9) ppmvd when adjusted to a 15% O2 basis; andwherein providing lower oxidant to fuel concentrations in an upstream portion of combustion regions than in a downstream portion of combustion regions and constraining the byproduct volume concentration of nitrogen oxides (NOx) formed within the combustion system to less than twenty five (25) ppmvd when adjusted to the 15% O2 basis in the equilibrated fluid leaving the system outlet. 3. The method of claim 2, further comprising recovering a portion of water from exhausted combustion fluid downstream of the turbine expander after start-up, and delivering a portion of recovered water as liquid water diluent upstream of the equilibration region outlet. 4. The method of claim 2, further comprising heating a portion of one or more of reactant fluid, oxidant fluid, and diluent fluid being delivered to the pilot inlet with one of: contacting fluid with a hot surface; electromagnetically heating the fluid; or adding a spontaneously reacting fluid. 5. The method of claim 2, wherein controlling delivery of hot pilot fluid, fuel fluid, oxidant fluid, and diluent fluid to maintain a fuel rich composition above soot formation in one or more upstream combustion regions, wherein constraining the volume concentration of NOx formed within the combustion regions to less than 5 ppmvd when adjusted to the 15% O2 basis. 6. The method of claim 2, wherein delivering oxidant fluid in a downstream combustion region or within the equilibration region sufficient to exceed a relative oxidant/fuel stoichiometric ratio Lambda equal to one, and diluting and equilibrating the resultant hot fluid sufficient to reduce the volume concentration of residual carbon monoxide (CO) in the equilibrated fluid leaving the system outlet to less than 5 ppmvd when adjusted to the 15% O2 basis. 7. The method of claim 2, wherein configuring the combustion and equilibration regions, and controlling delivery of hot pilot fluid and of fuel, oxidant and diluent fluids comprise controlling the residence time of the hot combustion fluid from the pilot inlet to the equilibration region outlet to between 1 millisecond and 100 milliseconds. 8. The method of claim 7, wherein controlling delivery of hot pilot fluid, fuel fluid, oxidant fluid, and diluent fluid to control the temperature of the hot combustion fluid to greater than 850° Celsius in said combustion regions, and to control the temperature of hot combustion fluid to less than about 1450° Celsius as it exits the equilibration system. 9. The method of claim 2, wherein, when a temperature of an upstream combustion region is below the critical temperature TCRIT, then the step of combusting fluid within a downstream combustion region of said combustion regions, comprises controlling a mass delivery flow rate of one or more of diluent fluid, oxidant fluid, and fuel fluid, such that a mean temperature of the hot combustion fluid exiting said downstream combustion region is maintained above a critical temperature TCRIT defining neutrally stable combustion. 10. The method of claim 2, wherein the step of combusting fluid within said combustion regions comprises controlling a mass delivery flow rate of one or more of diluent fluid, oxidant fluid, and fuel fluid such that a mass delivery flow rate delivery ratio R of said delivered fluid to hot combustion fluid into each of the combustion regions is maintained between 25% and 150% of a critical delivery flow ratio RCRIT. 11. The method of claim 10, wherein the fluid flow rate of each of fuel fluid, oxidant fluid and diluent fluid, delivered to a downstream combustion region is greater than the respective fuel fluid flows delivered to an upstream combustion region. 12. The method of claim 2, wherein the step of delivering fuel fluid, oxidant fluid, and diluent fluid comprises: premixing with diluent fluid one of fuel fluid, oxidant fluid, and premixed fuel-oxidant-fluid, before delivering the mixed fluid into one of the combustion regions downstream of the pilot region. 13. The method of claim 2, wherein the step of delivering fuel fluid, oxidant fluid, and diluent fluid comprises premixing fuel fluid, oxidant fluid, and diluent fluid, and delivering uncombusted premix fluid and hot pilot fluid into one of said combustion regions downstream of the pilot region. 14. The method of claim 2, wherein delivering one of oxidant fluid, and diluent fluid to the hot combustion fluid in the equilibration region downstream of the plurality of combustion regions to reduce a carbon monoxide concentration. 15. The method of claim 2, wherein the turbine expander further comprises a third expander stage or expander downstream of the second expander stage or expander, and a second interstage equilibrium region between the second and third expansion stages or expanders, downstream of and having a larger equilibration volume than the first interstage equilibration region, in streamwise communication with said combustion regions and the system outlet, the method further comprising controlling the temperature of the hot combustion fluid entering the expander to greater than 950° Celsius, expanding the hot combustion fluid and equilibrating the expanded fluid within the first and second interstage equilibration regions, sufficiently, to reduce the concentration of carbon monoxide (CO) in expanded fluid exiting the turbine outlet to below 5 ppmvd when adjusted to the 15% O2 basis. 16. The method of claim 1, wherein controlling the relative oxidant to reactant stoichiometric ratio Lambda of the hot reaction fluid to less than one in an upstream majority of reaction regions. 17. The method of claim 16, further comprising delivering oxidant fluid and diluent fluid into a downstream equilibration region, wherein controlling the relative stoichiometric ratio Lambda to greater than one, controlling the temperature within a prescribed range, and providing sufficient residence time to reduce an intermediate reaction product to less than a prescribed concentration. 18. The method of claim 1, wherein the step of reacting the fluid within one or more of said reaction regions comprises controlling the delivery of one of diluent fluid, oxidant fluid, and reactant fluid, such that a mass delivery flow rate delivery ratio R, of said delivered fluid to hot reaction fluid into that reaction region, is between 33% and 99% of a critical delivery ratio RCRIT, while maintaining a relative oxidant/fuel stoichiometric ratio Lambda less than 1.66 in said pilot region and in said reaction regions; whereby maintaining a stable reaction. 19. The method of claim 1, wherein controlling the hot reaction fluid residence time upstream of the system outlet to between 1 millisecond and 1 second, wherein reducing a residual volume concentration of residual intermediate reactant product in the equilibrated fluid leaving the system outlet to less than 3 ppmvd when adjusted to a 15% oxidant basis; andwherein constraining a byproduct volume concentration of a primary diluent reaction byproduct to less than 3 ppmvd when adjusted to the 15% oxidant basis. 20. The method of claim 1, wherein the step of controlling delivery of diluent, reactant and oxidant fluids into one of said reaction regions comprises controlling a mass delivery flow ratio of diluent to reactant fluid to greater than 300%. 21. The method of claim 1, wherein the turbine expander further comprises a second equilibration stage being configured between the second upstream and a third downstream expander stage or expander, in streamwise communication with said reaction regions and the system outlet, the method further comprising, expanding the hot reaction fluid and equilibrating the expanded fluid within the second equilibration stage for at least half a millisecond (0.5 ms), and controlling the temperature of hot reaction fluid entering the second equilibration stage to greater than 900° Celsius, sufficient to reduce the concentration of residual intermediate reactant product leaving the system outlet to below 3 ppmvd adjusted to the 15% oxidant basis. 22. The method of claim 1, wherein delivering oxidant fluid within the equilibration region sufficient to exceed a relative oxidant/reactant stoichiometric ratio Lambda equal to one, and diluting and equilibrating the resultant hot fluid sufficient to reduce the volume concentration of residual intermediate reactant product in the equilibrated fluid leaving the system outlet to less than 5 ppmvd when adjusted to 15% O2. 23. The method of claim 21, wherein the turbine expander comprises a shaft configured between one of the first and second expander stages or expanders and between the second and third expander stages or expanders, having a stabilization bearing, and wherein the method further comprises controlling vibrations of said shaft, and one of protecting said stabilization bearing and cooling said stabilization bearing with diluent. 24. The method of claim 1, wherein the reaction system comprises a shaft configured between the compressor and the first expander stage or expander, having a stabilization bearing, and wherein the method further comprises controlling vibrations of said connecting shaft, and one of protecting said stabilization bearing and cooling said stabilization bearing with diluent. 25. The method of claim 1, wherein the reaction system comprises a shaft configured between the compressor and the first expander stage or expander, having a thrust bearing, and wherein the method further comprises controlling oxidant fluid and diluent fluid delivery to control a relative oxidant/fuel stoichiometric ratio Lambda entering the turbine expander to less than about 2.5, controlling vibrations of shaft, and one of protecting said thrust bearing and cooling said thrust bearing with diluent.
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