WO2014043029A1 - Exothermic and endothermic cycling power generation - Google Patents

Exothermic and endothermic cycling power generation Download PDF

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Publication number
WO2014043029A1
WO2014043029A1 PCT/US2013/058756 US2013058756W WO2014043029A1 WO 2014043029 A1 WO2014043029 A1 WO 2014043029A1 US 2013058756 W US2013058756 W US 2013058756W WO 2014043029 A1 WO2014043029 A1 WO 2014043029A1
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Prior art keywords
exothermic
power generation
generation system
endothermic
working fluid
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PCT/US2013/058756
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French (fr)
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Michael Gurin
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Michael Gurin
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Publication of WO2014043029A1 publication Critical patent/WO2014043029A1/en

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    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01KSTEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K25/00Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for
    • F01K25/08Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for using special vapours
    • F01K25/10Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for using special vapours the vapours being cold, e.g. ammonia, carbon dioxide, ether
    • F01K25/103Carbon dioxide

Definitions

  • the present invention generally relates to power generation systems that utilize multiple reactor beds that cycle between exothermic thermal generation and endothermic loading devices (reactor) preferably within highly recuperated thermodynamic cycles to provide tightly controlled temperature regulation and thermal recovery.
  • the present invention relates to a reactor comprised of at least two reactor beds cycling between exothermic and endothermic mode to operate a thermodynamic cycle at high efficiency and ensuring safe operation of reactor in both modes for optimal energy production.
  • the present invention generally relates to power generation systems that have multiple reactors (beds) and that utilize the reactor beds in alternating exothermic and endothermic modes.
  • the present invention relates to a power generation system having at least two beds comprised of beds that alternate between one exothermic reaction mode (power) and an endothermic reaction mode (loading).
  • Figure 1 is a flow chart process illustration of multiple embodiments of an exothermic reactor in accordance with the present invention
  • Figure 2 is a flow chart process illustration of multiple embodiments of an exothermic reactor in accordance with the present invention.
  • Figure 3 is a flow chart process illustration of a parallel configuration of reactor stages in accordance with one embodiment of the present invention
  • Figure 4 is a flow chart process illustration of multiple embodiments of an exothermic reactor in a highly recuperated power generating cycle in accordance with the present invention
  • Figure 5 is a flow chart process illustration of multiple embodiments of an exothermic reactor in a highly recuperated power generating cycle in accordance with the present invention
  • Figure 6 is a flow chart process illustration of multiple embodiments of an exothermic reactor in a recuperated power generating cycle having multiple recuperators in accordance with the present invention
  • Figure 7 is another flow chart process illustration of multiple embodiments of an exothermic reactor in a recuperated power generating cycle having multiple recuperators in accordance with the present invention
  • Figure 8 is a schematic diagram of multiple embodiments of a reactor stage highly integrated to a phonon-electron coupling layer with both components further subjected to an electromagnetic (or electrostatic) field for voltage bias.
  • reactor bed includes any bed as known in the art (and preferably a simulated moving bed) in which a reaction or chemical interaction takes place that either produces thermal energy or consumes thermal energy. It is understood in the context of this invention that it further includes the process of adsorption, absorption, and desorption as exemplary chemical interactions that technically aren't reactions. It is understood that the reactor bed has at two types of reactants being consumable (i.e., a large percentage greater than 50 percent and preferably greater than 90%) of reactant is consumed within other reactants within reactor bed that aren't consumed) and reactants being reversible (i.e., a large percentage less than 50 percent and preferably less than 10 percent).
  • reactants being consumable (i.e., a large percentage greater than 50 percent and preferably greater than 90%) of reactant is consumed within other reactants within reactor bed that aren't consumed) and reactants being reversible (i.e., a large percentage less than 50 percent and preferably less than 10 percent).
  • reversible reactants are switched between the exothermic mode to the endothermic mode for the principle objective of protecting the reactant from irreversible damage.
  • consumable reactants are switched between the exothermic mode and the endothermic mode for the principle objective of protecting the reactor bed and any additional reversible reactants (or substrates) remaining within the reactor bed.
  • cycles between is used interchangeably with “switch” and “switches”, as used herein, to indicate a change from one mode to another mode.
  • the reference of “between” does not enable an intermediary state between endothermic and exothermic modes beyond a brief transition between the two modes (i.e., there is not a mode of 1 ⁇ 2 exothermic and 1 ⁇ 2 endothermic).
  • exothermic includes any reaction type that produces thermal energy as a result of such reaction. It is understood in the context of this invention that exothermic is broadly utilized as operating in a mode that adds from the bed into the power generation working fluid (i.e., heat the working fluid).
  • endothermic includes any reaction type that utilizes thermal energy during such reaction. It is understood in the context of this invention that endothermic is broadly utilized as operating in a mode that removes heat from the bed into the power generation working fluid (i.e., cool the working fluid).
  • endothermic loading includes any reaction type that utilizes thermal energy to preheat (beyond an initial temperature) reactants (such as prior to entering an exothermic reaction mode).
  • thermal continuity includes the direct connection between the heat source and the heat sink whether or not a thermal interface material is used.
  • heat spreader includes a heat sink having the ability to extend the surface area of heat transfer.
  • fluid inlet or "fluid inlet header”, as used herein, includes the portion of a heat exchanger where the fluid flows into the heat exchanger.
  • fluid discharge includes the portion of a heat exchanger where the fluid exits the heat exchanger.
  • expandable fluid includes the all fluids that have a decreasing density at increasing temperature at a specific pressure of at least a 0.1% decrease in density per degree C.
  • heat transfer fluid is a liquid medium utilized to convey thermal energy from one location to another.
  • the terms heat transfer fluid, working fluid, and expandable fluid are used interchangeably.
  • recuperator is a method of recovering waste heat downstream of an expander and transferring the thermal energy upstream of either a compressor, turbocompressor or pump.
  • a thermodynamic cycle that recovers at least 50% of the post expander thermal energy is hereinafter referred to as a "highly recuperated cycle”.
  • exital heater is a method of heating (i.e., increasing enthalpy) of a working fluid utilizing a heat exchanger as opposed to in-situ combustion of the working fluid.
  • condenser and “condensor”, interchangeable spellings in this invention, is utilized to remove thermal energy from a working fluid within the condenser and further understood to not always result in the working fluid being condensed (but always cooled).
  • electrostatic and “electrostatic” are interchangeable in this invention, in that an electron flow bias is achieved particularly for free electrons.
  • high-side is the portion of the thermodynamic cycle having a higher pressure than the "low-side”, which is the portion of the thermodynamic cycle downstream of the pump (or compressor) and upstream of the expander.
  • low-side is the portion of the thermodynamic cycle having a lower pressure than the "high-side”, which is the portion of the thermodynamic cycle downstream of the expander and upstream of the pump (or compressor).
  • the present invention generally relates to highly recuperated power generation cycles and/or high to low-pressure ratio power generation cycles preferably having at least one thermal source that cycles between an exothermic and endothermic reaction mode.
  • the recuperator has an effectiveness of at least 30% between the working fluid downstream of the expansion stage to upstream of the pressure increasing device, though it is understood that any level of effectiveness including transfer of thermal energy to secondary distributed energy functions (e.g., absorption or adsorption chillers) in order to keep working fluid temperatures to less than 800 degrees Celsius (and preferentially less than 600, 300, or 200 degrees Celsius, and particularly preferred to less than 100 degrees Celsius).
  • secondary distributed energy functions e.g., absorption or adsorption chillers
  • the utilization of an individual or multiple distinct expanders with or without a variable area nozzle is envisioned. Exemplary embodiments of the present invention will now be discussed with reference to the attached Figures. Such embodiments are merely exemplary in nature and not to be construed as limiting the scope of the present invention in any manner.
  • ScC02 Pump 30 or simply pump, operable to increase the pressure of the working fluid.
  • the working fluid is preferably supercritical C02 such that the discharge pressure from the pump is above the supercritical pressure of the carbon dioxide "C02". It is understood that any working fluid can be substituted, though the operation of a supercritical fluid is distinct and preferred.
  • the particularly preferred working fluid is selected from C02 or ammonia (even when component name contains ScC02), with the specifically preferred working fluid being C02.
  • the working fluid can include combinations of fluid, notably hydrogen containing molecules such as H2, NH4, CH4 in which case the hydrogen becomes one of the reactants within exothermic reactor stage.
  • the addition of hydrogen molecules can simply occur such that an increased presence of moles of hydrogen within the exothermic stage (at least during the initial stages of the exothermic stage), as compared to the beginning of the endothermic stage directly within the reactor bed.
  • the hydrogen loading in the exothermic stage is at an exothermic power level, and respectively in the endothermic stage is at an endothermic loading level.
  • the exothermic power level has a hydrogen loading that is at least 10% greater than the endothermic loading level, and preferably at least 50% greater than the endothermic loading level.
  • Figure 1 is comprised of 2 different scenarios A and B that depict thermodynamic cycles.
  • the cycle begins with a ScC02 Pump 30 discharging the working fluid, preferably at a pressure above the supercritical pressure of the working fluid.
  • the now (relatively) high pressure working fluid is heated by thermal energy from the Reactor Exothermic Stage HX 20 ,whether directly through heat exchangers as known in the art or as depicted indirectly through a Heat Pipe 11.
  • the now superheated working fluid enters the ScC02 Expander 40, which transforms the thermal energy into mechanical, and optionally into electrical energy through a generator as known in the art.
  • the now (relatively) low pressure working fluid has thermal energy dissipated through the ScC02 Condenser 60 such that the working fluid is preferably again a liquid (or alternatively can remain as a cooler gas for Brayton cycles) when the thermodynamic cycle is a Rankine cycle.
  • the cycle is identical to Scenario A with the exception of the further inclusion of a Reactor Endothermic Stage HX 20.1 downstream of the ScC02 Expander 40, with thermal energy removed from the Reactor Endothermic Stage HX 20.1 into the working fluid as depicted through a Heat Pipe 11.
  • the Reactor Endothermic Stage HX 20.1 can be positioned downstream of the ScC02 Pump 30 and upstream of the Reactor Exothermic Stage HX 20.
  • the fundamental principle in this depiction, and in all of the subsequent depictions is that the endothermic stage is operating at a lower temperature than the exothermic stage, and is core to the invention is such that an exothermic stage capable of increasing the temperature within the exothermic reactor bed is best controlled by using a supercritical fluid having a relatively high mass flow rate (at least in comparison to steam cycle) per kW of energy produced operable to greatly reduce or eliminate hot spots within the reactor bed (most likely to occur at interface between reactants, including localized defect points which have surface areas significantly higher than 30 meter square per gram, preferably higher than 300 meter square per gram, and specifically preferred higher than 2000 meter square per gram) so as to not permanently damage the reactor, the reactants, or the catalysts within the reactor bed.
  • the embodiments throughout the invention notably first within Figure 1 Scenario B, has the counterpart in which the Reactor Exothermic Stage HX 20 upon reaching (i.e., operating temperature) within 10 degrees Celsius, or preferably within 5 degrees Celsius, or specifically preferred within 1 degrees Celsius of the "Damaged Temperature Limit" (which is defined as the temperature at which permanent damage occurs within the reactor, reactants, or catalysts within the reactor bed; notably the point at which subsequent reactions produce reduced thermal energy for the same mass of reactants and catalysts are at most 10 percent lower than the prior exothermic reactor stage, preferably at most 5 percent lower than the prior exothermic reactor stage, or specifically at most 1 percent lower than the prior exothermic reactor stage) rapidly cycles to the Reactor Endothermic Stage HX 20.1 operable to rapidly decrease the reactor bed temperature to less than the Damaged Temperature Limit.
  • the "Damaged Temperature Limit" which is defined as the temperature at which permanent damage occurs within the reactor, reactants, or catalysts within the reactor bed; notably the point at which subsequent reactions produce reduced thermal energy for
  • Figure 2 - Scenario A is identical to Figure 1 - Scenario B with the exception of the addition of a Recuperator 390.1 downstream of the Reactor Endothermic Stage HX 20.1 such that thermal energy removed from the endothermic stage is at least partially used to produce increased (by at least 2 percent, preferably at least 5 percent, and specifically preferred at least 10 percent as without recuperation) power by the expander.
  • the placement of the Recuperator 390.1 is alternatively upstream of the Reactor Endothermic Stage HX 20.1 operable to increase the temperature differential between the operating temperature within the reactor bed while operating as exothermic stage versus the endothermic stage.
  • Figure 2 - Scenario B is another embodiment of the invention that includes both additional uses of the various endothermic and exothermic reactor stages, in addition to additional functionality for the endothermic and exothermic reactor stages.
  • a core aspect of the invention is the use of a series of reactor beds that operate as a simulated moving bed, such that a tight band of operating temperatures is within each bed and that the order of flow by the working fluid into each bed is sequentially cycled to achieve temperature control in addition to heat recovery such that waste heat is used in the endothermic stages, and subsequently used as preheat to the exothermic stages.
  • exothermic reactors as noted earlier has to remain below the Damage Temperature Limit, and yet thermodynamic cycles have higher efficiency therefore an exothermic thermal energy source (which doesn't cycle between exothermic and endothermic stages) such as combustion (i.e., oxidation exothermic reaction).
  • the utilization of the cyclic exothermic to endothermic as a thermal source within the inventive thermodynamic cycle comprised of reactor beds is effective to reduce the amount of fuel oxidized in the combustion (as known in the art using any traditional fuel source ranging from biomass, biofuel, petroleum, to natural gas) and notably to reduce the operating costs of the thermodynamic cycle.
  • the working fluid is heated by the downstream Reactor Exothermic Stage HX 20 prior to entering the Recuperator 390.1.
  • Exothermic Stage HX 20 is principally done when the operating cost of the reactor bed (i.e., reactants) is less than US$1 per MMBTU (i.e., essentially free) as incremental temperature gain is achieved beyond working fluid temperature downstream of the Recuperator 390.1.
  • Another aspect of this scenario is the inclusion of the aforementioned exothermic oxidation reaction within the External Combustor HX 220 to transfer thermal energy to the working fluid upstream of the ScC02 Expander 40.
  • the preferred expander inlet temperature is greater than 400 Celsius, particularly preferred greater than 600 Celsius, and specifically preferred greater than 800 Celsius.
  • the combustion exhaust from the External Combustor HX 220 is utilized to support endothermic loading within at least one of the reactor beds (depicted as Reactor Endothermic Stage HX 20.2) that cycles between exothermic stage and endothermic stage.
  • the concurrent preheating of fuel (reduces fuel consumption as known in the art) used in the External Combustor HX 220 through a Fuel Atomizer 230 has the further benefit of more rapidly reducing the operating temperature within the Reactor Endothermic Stage HX 20.1.
  • the ability to rapidly reduce the operating temperature within a reactor bed is of particular importance when switching between the exothermic stage to the endothermic stage (operable to eliminate a runaway reaction condition of the exothermic stage, such that otherwise the Damage Temperature Limit is reached).
  • the ScC02 Condenser 60 is operable in the same manner as Scenario B also downstream of the Recuperator 390.1.
  • Figure 3 is identical to Figure 2 Scenario B with the addition of an Oxidant Compressor 250 (preferably through a ceramic compressor, particularly a ceramic ramjet, and specifically preferred an inside-out ceramic ramjet), which can be ambient air compressor, oxygen enriched ambient air to high purity oxygen source.
  • an Oxidant Compressor 250 preferably through a ceramic compressor, particularly a ceramic ramjet, and specifically preferred an inside-out ceramic ramjet
  • the now compressed oxidant is preheated as known in the art through a heat exchanger recovering waste heat from the combustion exhaust upstream of the External Combustor HX 220.
  • Figure 4 is comprised of 2 different scenarios A and B that depict alternative thermodynamic cycles.
  • two distinct reactor beds operating within the exothermic stage as a thermal input for increased energy efficiency of the thermodynamic to power generation (or just thermal energy).
  • the working fluid is first heated using thermal energy from first Reactor Exothermic Stage HX 20.3 operable at a lower temperature (by greater than 300 Celsius as compared to the second Reactor Exothermic Stage HX 20, preferably less than 200 Celsius, and specifically preferred less than 100 Celsius) prior to further heating of the working fluid through the Recuperator 390.1.
  • the working fluid is subsequently further heated through the second Exothermic Stage HX 20 upstream of the ScC02 Expander 40.
  • An important element of the invention is the alternating cycling of the at least two exothermic reactor beds between a high temperature operating range approaching the Damage Temperature Limit, and a low temperature operating range of at least 100 Celsius less than the Damage Temperature Limit. This cycling of reactor beds between high and low temperature operating ranges rapidly prevents runaway exothermic reactions, greatly reduces hot spots, and importantly enabling thermal energy removed during the transition between high and low temperature operating ranges to be utilized as a thermal energy source for the thermodynamic cycle.
  • the now high pressure working fluid is heated first by the Recuperator 390.2 followed by a subsequent heat transfer (i.e., working fluid is cooled) to the Reactor Endothermic Stage HX 20.1.
  • the working fluid continues to the second Recuperator 390.1 to increase the working fluid enthalpy, and then further increase in enthalpy through the third reactor bed Reactor Exothermic Stage HX 20 prior to reaching the ScC02 Expander for conversion into mechanical/electrical energy.
  • the splitting of the thermal energy recuperation downstream of the expander enables three distinct temperature operating regions (one for each reactor bed).
  • the preferred embodiment is such that a high mass flow rate, at least 25 percent greater than a steam cycle, preferably at least 50 percent greater than a steam cycle (of the same kW rating), and specifically preferred at least 100 percent greater than a steam cycle of the same kW rating.
  • the temperature differential between inlet and discharge temperature within a reactor bed is less than 200 Celsius, particularly preferred less than 120 Celsius, and specifically preferred less than 100 Celsius.
  • the fundamental objective of the high mass flow rate is to obtain a heat transfer rate that is corresponding to a heat transfer rate of at least 25 percent greater than a steam cycle, preferably at least 50 percent greater than a steam cycle (of the same kW rating), and specifically preferred at least 100 percent greater than a steam cycle of the same kW rating.
  • Figure 5 Scenario B is similar to Figure 5 Scenario A with the primary difference being the placement of the endothermic stage in relationship to the thermodynamic cycle, plus the elimination of a second exothermic stage reactor bed.
  • This configuration such that the Reactor Endothermic Stage HX 20.1 between the first Recuperator 390.1 and the second Recuperator 390.2 reduces the operating temperature of the endothermic stage relative to the exothermic stage enabling at least a 10 percent, preferably at least a 20 percent, and specifically preferred at least a 30% faster thermal decrease rate during transition of a reactor bed from exothermic stage to endothermic stage by working fluid have a higher temperature differential with the exothermic stage peak temperature.
  • Figure 6 introduces a second parallel expander stage.
  • This embodiment has one of the parallel stages beginning with the ScC02 Pump 30 (depicted here as a common pump and condenser for both loops, though it is understood that each loop can have either a separate pump or condenser as envisioned in this invention) with working fluid first heated by a first Recuperator 390.2 with subsequent superheating by the Reactor Exothermic Stage HX 20 prior to being expanded ScC02 Expander 40.1 to generate mechanical/electrical energy.
  • the now expanded working fluid returns through the Recuperator 390.2 as noted before reaching the ScC02 Condenser 60 as known in the art.
  • the parallel loops can be intertwined by alternative placement of the recuperators as known in the art.
  • the second loop has the working fluid leave the ScC02 Pump 30 before being first heated by the Recuperator 390.1 and then entering a photon enhanced thermionic emission "PETE" cell as known in the art to increase the working fluid peak temperature by at least 100 Celsius greater than the first loop peak temperature (and preferably at least 200 Celsius greater, and specifically preferred at least 300 Celsius greater).
  • PETE photon enhanced thermionic emission
  • Figure 7 is one embodiment of two parallel though intertwined loops such that at least two reactor beds that cycle between exothermic and endothermic stages.
  • the first loop working fluid enters the first Recuperator 390.1 and then is subsequently superheated through the first reactor bed Reactor Exothermic Stage HX 20 at an operating peak temperature less than Damage Temperature Limit.
  • the working fluid then enters the first ScC02 Expander 40 to produce mechanical/electrical energy.
  • the now low pressure working fluid is either reheated, which also concurrently provides "cooling" of the Reactor Endothermic Stage HX 20.1 to provide endothermic loading, or simply cooling by transfer thermal energy to the endothermic stage.
  • Figure 8 Scenario A depicts one embodiment operable to reduce the creation of hot spots within the reactor bed operating in the exothermic stage.
  • the Reactor (Bed) Exothermic Stage HX 20 is in thermal communication directly with a Phonon - Electron Coupling 200 layer (operable as known in the art) necessary to create ballistic transmission of free electrons for rapid "dissipation" of thermal (i.e., phonon) energy.
  • the reactor and phonon/electron coupling components are "sandwiched" between an Electromagnetic Field 210.1 and 210.2 such as to create a bias for electron emission.
  • the particularly preferred embodiment is such that the operating voltage field when a phonon to electron coupling event takes place, the voltage becomes greater than dielectric breakdown voltage to yield free electron(s).
  • the operating voltage can be pulsed at high frequency, preferably in the terahertz range.
  • Figure 8 Scenario B is another embodiment of Scenario A such that multiple layers of alternating layers of Reactor Exothermic Stage HX 20 and Phonon Electron Coupling 200 perpendicular to the electromagnetic field (cathode and anode) 210.1 and 210.2.
  • the invention reactor beds are preferably comprised of at least one of Boron 10 Hydride, Palladium, Lithium 6, and Nickel. It is understood that the nature of exothermic reactions also includes LENR and LANR as known in the art. A wide range of triggers can be used to switch between endothermic loading and exothermic stages including switching of operating voltage across the reactor, and plasmon generators.
  • the phonon to electron coupling layer is preferably within the mean free path of phonons from reactant voids/defects.

Abstract

Provided herein are power generating systems utilizing exothermic and endothermic cycling of simulated moving beds, preferentially utilizing supercritical carbon dioxide as a working fluid, to increase enthalpy and thermodynamic cycle efficiency while providing long-term operating life by utilizing the high heat transfer rate of supercritical fluids to maintain precise temperature control of each bed. Methods for producing power are also provided.

Description

EXOTHERMIC AND ENDOTHERMIC CYCLING POWER GENERATION
CROSS-REFERENCE TO RELATED APPLICATIONS
This application claims the benefit of provisional patent application US No.
61/534,387 titled "Exothermic and Endothermic Cycling Power Generation" filed on September 14, 2011, and hereby incorporated by reference in its entirety.
FIELD OF THE INVENTION
The present invention generally relates to power generation systems that utilize multiple reactor beds that cycle between exothermic thermal generation and endothermic loading devices (reactor) preferably within highly recuperated thermodynamic cycles to provide tightly controlled temperature regulation and thermal recovery. In one embodiment, the present invention relates to a reactor comprised of at least two reactor beds cycling between exothermic and endothermic mode to operate a thermodynamic cycle at high efficiency and ensuring safe operation of reactor in both modes for optimal energy production.
BACKGROUND OF THE INVENTION
Due to a variety of factors including, but not limited to, global warming issues, fossil fuel availability and environmental impacts, crude oil price and availability issues, alternative energy sources are becoming more popular today. One such source of alternative and/or renewable energy are hybrid exothermic reactions/mode operating in conjunction with endothermic reactions/mode. The most efficient thermodynamic cycles have high temperatures (in excess of 500 °C, and preferably in excess of 800 °C) presenting significant challenges for exothermic reactions that have upper limit temperature constraints. SUMMARY OF THE INVENTION
The present invention generally relates to power generation systems that have multiple reactors (beds) and that utilize the reactor beds in alternating exothermic and endothermic modes. In one embodiment, the present invention relates to a power generation system having at least two beds comprised of beds that alternate between one exothermic reaction mode (power) and an endothermic reaction mode (loading).
BRIEF DESCRIPTION OF THE DRAWINGS
Figure 1 is a flow chart process illustration of multiple embodiments of an exothermic reactor in accordance with the present invention;
Figure 2 is a flow chart process illustration of multiple embodiments of an exothermic reactor in accordance with the present invention;
Figure 3 is a flow chart process illustration of a parallel configuration of reactor stages in accordance with one embodiment of the present invention; Figure 4 is a flow chart process illustration of multiple embodiments of an exothermic reactor in a highly recuperated power generating cycle in accordance with the present invention;
Figure 5 is a flow chart process illustration of multiple embodiments of an exothermic reactor in a highly recuperated power generating cycle in accordance with the present invention;
Figure 6 is a flow chart process illustration of multiple embodiments of an exothermic reactor in a recuperated power generating cycle having multiple recuperators in accordance with the present invention;
Figure 7 is another flow chart process illustration of multiple embodiments of an exothermic reactor in a recuperated power generating cycle having multiple recuperators in accordance with the present invention;
Figure 8 is a schematic diagram of multiple embodiments of a reactor stage highly integrated to a phonon-electron coupling layer with both components further subjected to an electromagnetic (or electrostatic) field for voltage bias. DETAILED DESCRIPTION OF THE INVENTION
The term "reactor bed", as used herein, includes any bed as known in the art (and preferably a simulated moving bed) in which a reaction or chemical interaction takes place that either produces thermal energy or consumes thermal energy. It is understood in the context of this invention that it further includes the process of adsorption, absorption, and desorption as exemplary chemical interactions that technically aren't reactions. It is understood that the reactor bed has at two types of reactants being consumable (i.e., a large percentage greater than 50 percent and preferably greater than 90%) of reactant is consumed within other reactants within reactor bed that aren't consumed) and reactants being reversible (i.e., a large percentage less than 50 percent and preferably less than 10 percent). The use of reversible reactants are switched between the exothermic mode to the endothermic mode for the principle objective of protecting the reactant from irreversible damage. The use of consumable reactants are switched between the exothermic mode and the endothermic mode for the principle objective of protecting the reactor bed and any additional reversible reactants (or substrates) remaining within the reactor bed.
The term "cycles between" is used interchangeably with "switch" and "switches", as used herein, to indicate a change from one mode to another mode. The reference of "between" does not enable an intermediary state between endothermic and exothermic modes beyond a brief transition between the two modes (i.e., there is not a mode of ½ exothermic and ½ endothermic).
The term "exothermic", as used herein, includes any reaction type that produces thermal energy as a result of such reaction. It is understood in the context of this invention that exothermic is broadly utilized as operating in a mode that adds from the bed into the power generation working fluid (i.e., heat the working fluid).
The term "endothermic", as used herein, includes any reaction type that utilizes thermal energy during such reaction. It is understood in the context of this invention that endothermic is broadly utilized as operating in a mode that removes heat from the bed into the power generation working fluid (i.e., cool the working fluid). The term "endothermic loading", as used herein, includes any reaction type that utilizes thermal energy to preheat (beyond an initial temperature) reactants (such as prior to entering an exothermic reaction mode).
The term "in thermal continuity", as used herein, includes the direct connection between the heat source and the heat sink whether or not a thermal interface material is used.
The term "heat spreader", as used herein, includes a heat sink having the ability to extend the surface area of heat transfer.
The term "fluid inlet" or "fluid inlet header", as used herein, includes the portion of a heat exchanger where the fluid flows into the heat exchanger.
The term "fluid discharge", as used herein, includes the portion of a heat exchanger where the fluid exits the heat exchanger.
The term "expandable fluid", as used herein, includes the all fluids that have a decreasing density at increasing temperature at a specific pressure of at least a 0.1% decrease in density per degree C.
The term "heat transfer fluid" is a liquid medium utilized to convey thermal energy from one location to another. The terms heat transfer fluid, working fluid, and expandable fluid are used interchangeably.
The term "recuperator" is a method of recovering waste heat downstream of an expander and transferring the thermal energy upstream of either a compressor, turbocompressor or pump. A thermodynamic cycle that recovers at least 50% of the post expander thermal energy is hereinafter referred to as a "highly recuperated cycle".
The term "external heater" is a method of heating (i.e., increasing enthalpy) of a working fluid utilizing a heat exchanger as opposed to in-situ combustion of the working fluid.
The term "condenser" and "condensor", interchangeable spellings in this invention, is utilized to remove thermal energy from a working fluid within the condenser and further understood to not always result in the working fluid being condensed (but always cooled). The term "electromagnetic" and "electrostatic" are interchangeable in this invention, in that an electron flow bias is achieved particularly for free electrons.
The term "high-side" is the portion of the thermodynamic cycle having a higher pressure than the "low-side", which is the portion of the thermodynamic cycle downstream of the pump (or compressor) and upstream of the expander.
The term "low-side" is the portion of the thermodynamic cycle having a lower pressure than the "high-side", which is the portion of the thermodynamic cycle downstream of the expander and upstream of the pump (or compressor).
The present invention generally relates to highly recuperated power generation cycles and/or high to low-pressure ratio power generation cycles preferably having at least one thermal source that cycles between an exothermic and endothermic reaction mode.
Here, as well as elsewhere in the specification and claims, individual numerical values and/or individual range limits can be combined to form non-disclosed ranges. It is understood that methods as known in the art to increase pressure of a working fluid include a pump, compressor, turbo-pump, or turbo-compressor. In this invention, the pressure increasing device(s) discharge the working fluid into a common high pressure discharge header. It is also understood as known in the art that power is generated by reducing pressure of a working fluid through an expansion stage. The preferred expansion stage is a single stage device but under all circumstances the invention has one high pressure discharge header providing working fluid to at least two parallel expanders and a recuperator for each of the at least two parallel expanders. The recuperator has an effectiveness of at least 30% between the working fluid downstream of the expansion stage to upstream of the pressure increasing device, though it is understood that any level of effectiveness including transfer of thermal energy to secondary distributed energy functions (e.g., absorption or adsorption chillers) in order to keep working fluid temperatures to less than 800 degrees Celsius (and preferentially less than 600, 300, or 200 degrees Celsius, and particularly preferred to less than 100 degrees Celsius). The utilization of an individual or multiple distinct expanders with or without a variable area nozzle is envisioned. Exemplary embodiments of the present invention will now be discussed with reference to the attached Figures. Such embodiments are merely exemplary in nature and not to be construed as limiting the scope of the present invention in any manner. With regard to Figures 1 through 8, like reference numerals refer to like parts. Additionally throughout the invention, it is understood that the ScC02 Pump, Turbopump or Turbocompressor 30 is hereinafter referred to as ScC02 Pump 30 or simply pump, operable to increase the pressure of the working fluid. The working fluid is preferably supercritical C02 such that the discharge pressure from the pump is above the supercritical pressure of the carbon dioxide "C02". It is understood that any working fluid can be substituted, though the operation of a supercritical fluid is distinct and preferred. The particularly preferred working fluid is selected from C02 or ammonia (even when component name contains ScC02), with the specifically preferred working fluid being C02. Additionally, the working fluid can include combinations of fluid, notably hydrogen containing molecules such as H2, NH4, CH4 in which case the hydrogen becomes one of the reactants within exothermic reactor stage. Alternatively, it is understood that the addition of hydrogen molecules can simply occur such that an increased presence of moles of hydrogen within the exothermic stage (at least during the initial stages of the exothermic stage), as compared to the beginning of the endothermic stage directly within the reactor bed. The hydrogen loading in the exothermic stage is at an exothermic power level, and respectively in the endothermic stage is at an endothermic loading level. The exothermic power level has a hydrogen loading that is at least 10% greater than the endothermic loading level, and preferably at least 50% greater than the endothermic loading level.
Turning to Figure 1, Figure 1 is comprised of 2 different scenarios A and B that depict thermodynamic cycles. In the embodiment of Figure 1 - Scenario A, the cycle begins with a ScC02 Pump 30 discharging the working fluid, preferably at a pressure above the supercritical pressure of the working fluid. The now (relatively) high pressure working fluid is heated by thermal energy from the Reactor Exothermic Stage HX 20 ,whether directly through heat exchangers as known in the art or as depicted indirectly through a Heat Pipe 11. The now superheated working fluid enters the ScC02 Expander 40, which transforms the thermal energy into mechanical, and optionally into electrical energy through a generator as known in the art. The now (relatively) low pressure working fluid has thermal energy dissipated through the ScC02 Condenser 60 such that the working fluid is preferably again a liquid (or alternatively can remain as a cooler gas for Brayton cycles) when the thermodynamic cycle is a Rankine cycle. In the embodiment of Figure 1 - Scenario B, the cycle is identical to Scenario A with the exception of the further inclusion of a Reactor Endothermic Stage HX 20.1 downstream of the ScC02 Expander 40, with thermal energy removed from the Reactor Endothermic Stage HX 20.1 into the working fluid as depicted through a Heat Pipe 11. Though not depicted, the Reactor Endothermic Stage HX 20.1 can be positioned downstream of the ScC02 Pump 30 and upstream of the Reactor Exothermic Stage HX 20. The fundamental principle in this depiction, and in all of the subsequent depictions is that the endothermic stage is operating at a lower temperature than the exothermic stage, and is core to the invention is such that an exothermic stage capable of increasing the temperature within the exothermic reactor bed is best controlled by using a supercritical fluid having a relatively high mass flow rate (at least in comparison to steam cycle) per kW of energy produced operable to greatly reduce or eliminate hot spots within the reactor bed (most likely to occur at interface between reactants, including localized defect points which have surface areas significantly higher than 30 meter square per gram, preferably higher than 300 meter square per gram, and specifically preferred higher than 2000 meter square per gram) so as to not permanently damage the reactor, the reactants, or the catalysts within the reactor bed. The embodiments throughout the invention, notably first within Figure 1 Scenario B, has the counterpart in which the Reactor Exothermic Stage HX 20 upon reaching (i.e., operating temperature) within 10 degrees Celsius, or preferably within 5 degrees Celsius, or specifically preferred within 1 degrees Celsius of the "Damaged Temperature Limit" (which is defined as the temperature at which permanent damage occurs within the reactor, reactants, or catalysts within the reactor bed; notably the point at which subsequent reactions produce reduced thermal energy for the same mass of reactants and catalysts are at most 10 percent lower than the prior exothermic reactor stage, preferably at most 5 percent lower than the prior exothermic reactor stage, or specifically at most 1 percent lower than the prior exothermic reactor stage) rapidly cycles to the Reactor Endothermic Stage HX 20.1 operable to rapidly decrease the reactor bed temperature to less than the Damaged Temperature Limit. Turning to Figure 2, Figure 2 - Scenario A is identical to Figure 1 - Scenario B with the exception of the addition of a Recuperator 390.1 downstream of the Reactor Endothermic Stage HX 20.1 such that thermal energy removed from the endothermic stage is at least partially used to produce increased (by at least 2 percent, preferably at least 5 percent, and specifically preferred at least 10 percent as without recuperation) power by the expander. The placement of the Recuperator 390.1 is alternatively upstream of the Reactor Endothermic Stage HX 20.1 operable to increase the temperature differential between the operating temperature within the reactor bed while operating as exothermic stage versus the endothermic stage. Turning to Figure 2, Figure 2 - Scenario B is another embodiment of the invention that includes both additional uses of the various endothermic and exothermic reactor stages, in addition to additional functionality for the endothermic and exothermic reactor stages. A core aspect of the invention is the use of a series of reactor beds that operate as a simulated moving bed, such that a tight band of operating temperatures is within each bed and that the order of flow by the working fluid into each bed is sequentially cycled to achieve temperature control in addition to heat recovery such that waste heat is used in the endothermic stages, and subsequently used as preheat to the exothermic stages. Furthermore, exothermic reactors as noted earlier has to remain below the Damage Temperature Limit, and yet thermodynamic cycles have higher efficiency therefore an exothermic thermal energy source (which doesn't cycle between exothermic and endothermic stages) such as combustion (i.e., oxidation exothermic reaction). The utilization of the cyclic exothermic to endothermic as a thermal source within the inventive thermodynamic cycle comprised of reactor beds is effective to reduce the amount of fuel oxidized in the combustion (as known in the art using any traditional fuel source ranging from biomass, biofuel, petroleum, to natural gas) and notably to reduce the operating costs of the thermodynamic cycle. Beginning the cycle at the ScC02 pump 30 the working fluid is heated by the downstream Reactor Exothermic Stage HX 20 prior to entering the Recuperator 390.1. This use of Exothermic Stage HX 20 is principally done when the operating cost of the reactor bed (i.e., reactants) is less than US$1 per MMBTU (i.e., essentially free) as incremental temperature gain is achieved beyond working fluid temperature downstream of the Recuperator 390.1. Another aspect of this scenario is the inclusion of the aforementioned exothermic oxidation reaction within the External Combustor HX 220 to transfer thermal energy to the working fluid upstream of the ScC02 Expander 40. The preferred expander inlet temperature is greater than 400 Celsius, particularly preferred greater than 600 Celsius, and specifically preferred greater than 800 Celsius. The combustion exhaust from the External Combustor HX 220 is utilized to support endothermic loading within at least one of the reactor beds (depicted as Reactor Endothermic Stage HX 20.2) that cycles between exothermic stage and endothermic stage. The concurrent preheating of fuel (reduces fuel consumption as known in the art) used in the External Combustor HX 220 through a Fuel Atomizer 230 has the further benefit of more rapidly reducing the operating temperature within the Reactor Endothermic Stage HX 20.1. The ability to rapidly reduce the operating temperature within a reactor bed is of particular importance when switching between the exothermic stage to the endothermic stage (operable to eliminate a runaway reaction condition of the exothermic stage, such that otherwise the Damage Temperature Limit is reached). The ScC02 Condenser 60 is operable in the same manner as Scenario B also downstream of the Recuperator 390.1.
Turning to Figure 3, Figure 3 is identical to Figure 2 Scenario B with the addition of an Oxidant Compressor 250 (preferably through a ceramic compressor, particularly a ceramic ramjet, and specifically preferred an inside-out ceramic ramjet), which can be ambient air compressor, oxygen enriched ambient air to high purity oxygen source. The now compressed oxidant is preheated as known in the art through a heat exchanger recovering waste heat from the combustion exhaust upstream of the External Combustor HX 220.
Turning to Figure 4, Figure 4 is comprised of 2 different scenarios A and B that depict alternative thermodynamic cycles. In the embodiment of Figure 4 - Scenario A, two distinct reactor beds operating within the exothermic stage as a thermal input for increased energy efficiency of the thermodynamic to power generation (or just thermal energy). Beginning at the ScC02 pump 30, the working fluid is first heated using thermal energy from first Reactor Exothermic Stage HX 20.3 operable at a lower temperature (by greater than 300 Celsius as compared to the second Reactor Exothermic Stage HX 20, preferably less than 200 Celsius, and specifically preferred less than 100 Celsius) prior to further heating of the working fluid through the Recuperator 390.1. The working fluid is subsequently further heated through the second Exothermic Stage HX 20 upstream of the ScC02 Expander 40. An important element of the invention is the alternating cycling of the at least two exothermic reactor beds between a high temperature operating range approaching the Damage Temperature Limit, and a low temperature operating range of at least 100 Celsius less than the Damage Temperature Limit. This cycling of reactor beds between high and low temperature operating ranges rapidly prevents runaway exothermic reactions, greatly reduces hot spots, and importantly enabling thermal energy removed during the transition between high and low temperature operating ranges to be utilized as a thermal energy source for the thermodynamic cycle.
In the embodiment of Figure 4 - Scenario B, everything is the same as Figure 4 - Scenario A with the addition a third reactor bed Reactor Endothermic Stage HX 20.1 such that as envisioned the three reactor beds cycle through operating regions interchanging with each other, where the third reactor bed Reactor Endothermic Stage HX 20.1 has thermal energy removed by the working fluid downstream of the ScC02 Expander 40 with subsequent dissipation from the working fluid to a Waste Heat Recovery 395 system as known in the art such as domestic hot water, absorption/adsorption heat pump, industrial processes, etc.
It is understood that operating the at least two reactor beds in sequential operation of exothermic stages followed by endothermic stages (on a repeated manner) maximizes energy efficiency while preventing the exothermic stage reactor bed from exceeding the Damage Temperature Limit, such that thermal energy from the late stages of operation of the first exothermic stage is "recovered" for the endothermic loading of the second reactor bed. Turning to Figure 5, Figure 5 Scenario A is similar to Figure 4 Scenario B with the primary difference being the placement of the endothermic stage in relationship to the thermodynamic cycle, plus the addition of a second recuperator. Beginning at the ScC02 Pump 30, the now high pressure working fluid is heated first by the Recuperator 390.2 followed by a subsequent heat transfer (i.e., working fluid is cooled) to the Reactor Endothermic Stage HX 20.1. The working fluid continues to the second Recuperator 390.1 to increase the working fluid enthalpy, and then further increase in enthalpy through the third reactor bed Reactor Exothermic Stage HX 20 prior to reaching the ScC02 Expander for conversion into mechanical/electrical energy. The splitting of the thermal energy recuperation downstream of the expander enables three distinct temperature operating regions (one for each reactor bed). It is a primary intent of the invention to minimize the temperature gradient within each reactor bed, which occurs by limiting (or eliminating) non-linear phase transitions within the heat exchangers of each reactor bed (e.g., steam systems as working fluid, or traditional non- recuperated ORC cycles). In particular, the preferred embodiment is such that a high mass flow rate, at least 25 percent greater than a steam cycle, preferably at least 50 percent greater than a steam cycle (of the same kW rating), and specifically preferred at least 100 percent greater than a steam cycle of the same kW rating. It is further preferred such that the temperature differential between inlet and discharge temperature within a reactor bed, particularly the reactor bed operating in exothermic stage with temperature closest to the Damage Temperature Limit of all of the reactor beds (cycling at the moment), is less than 200 Celsius, particularly preferred less than 120 Celsius, and specifically preferred less than 100 Celsius. The fundamental objective of the high mass flow rate is to obtain a heat transfer rate that is corresponding to a heat transfer rate of at least 25 percent greater than a steam cycle, preferably at least 50 percent greater than a steam cycle (of the same kW rating), and specifically preferred at least 100 percent greater than a steam cycle of the same kW rating. Turning to Figure 5, Figure 5 Scenario B is similar to Figure 5 Scenario A with the primary difference being the placement of the endothermic stage in relationship to the thermodynamic cycle, plus the elimination of a second exothermic stage reactor bed. This configuration such that the Reactor Endothermic Stage HX 20.1 between the first Recuperator 390.1 and the second Recuperator 390.2 reduces the operating temperature of the endothermic stage relative to the exothermic stage enabling at least a 10 percent, preferably at least a 20 percent, and specifically preferred at least a 30% faster thermal decrease rate during transition of a reactor bed from exothermic stage to endothermic stage by working fluid have a higher temperature differential with the exothermic stage peak temperature. Turning to Figure 6, Figure 6 introduces a second parallel expander stage.
Operating an exothermic reactor bed below its corresponding Damage Temperature Limit yields a significantly lower peak temperature as compared to many other thermal energy sources (e.g., combustion and solar thermal). This embodiment has one of the parallel stages beginning with the ScC02 Pump 30 (depicted here as a common pump and condenser for both loops, though it is understood that each loop can have either a separate pump or condenser as envisioned in this invention) with working fluid first heated by a first Recuperator 390.2 with subsequent superheating by the Reactor Exothermic Stage HX 20 prior to being expanded ScC02 Expander 40.1 to generate mechanical/electrical energy. The now expanded working fluid returns through the Recuperator 390.2 as noted before reaching the ScC02 Condenser 60 as known in the art. It is known in the art that the parallel loops can be intertwined by alternative placement of the recuperators as known in the art. The second loop has the working fluid leave the ScC02 Pump 30 before being first heated by the Recuperator 390.1 and then entering a photon enhanced thermionic emission "PETE" cell as known in the art to increase the working fluid peak temperature by at least 100 Celsius greater than the first loop peak temperature (and preferably at least 200 Celsius greater, and specifically preferred at least 300 Celsius greater). The now superheated working fluid is expanded through the second ScC02 Expander 40 with the now expanded working fluid making its return through the aforementioned recuperator then to the aforementioned condenser.
Turning to Figure 7, Figure 7 is one embodiment of two parallel though intertwined loops such that at least two reactor beds that cycle between exothermic and endothermic stages. Beginning at the ScC02 Pump 30, the first loop working fluid enters the first Recuperator 390.1 and then is subsequently superheated through the first reactor bed Reactor Exothermic Stage HX 20 at an operating peak temperature less than Damage Temperature Limit. The working fluid then enters the first ScC02 Expander 40 to produce mechanical/electrical energy. The now low pressure working fluid is either reheated, which also concurrently provides "cooling" of the Reactor Endothermic Stage HX 20.1 to provide endothermic loading, or simply cooling by transfer thermal energy to the endothermic stage. The second loop working fluid leaves the ScC02 Pump 30 to be heated by the second Recuperator 390.2 which is then subsequently expanded through the second ScC02 Expander 40.1 prior to returning through the recuperator and condenser. Turning to Figure 8, Figure 8 Scenario A depicts one embodiment operable to reduce the creation of hot spots within the reactor bed operating in the exothermic stage. The Reactor (Bed) Exothermic Stage HX 20 is in thermal communication directly with a Phonon - Electron Coupling 200 layer (operable as known in the art) necessary to create ballistic transmission of free electrons for rapid "dissipation" of thermal (i.e., phonon) energy. The reactor and phonon/electron coupling components are "sandwiched" between an Electromagnetic Field 210.1 and 210.2 such as to create a bias for electron emission. The particularly preferred embodiment is such that the operating voltage field when a phonon to electron coupling event takes place, the voltage becomes greater than dielectric breakdown voltage to yield free electron(s). The operating voltage can be pulsed at high frequency, preferably in the terahertz range.
Turning to Figure 8, Figure 8 Scenario B is another embodiment of Scenario A such that multiple layers of alternating layers of Reactor Exothermic Stage HX 20 and Phonon Electron Coupling 200 perpendicular to the electromagnetic field (cathode and anode) 210.1 and 210.2.
The invention reactor beds are preferably comprised of at least one of Boron 10 Hydride, Palladium, Lithium 6, and Nickel. It is understood that the nature of exothermic reactions also includes LENR and LANR as known in the art. A wide range of triggers can be used to switch between endothermic loading and exothermic stages including switching of operating voltage across the reactor, and plasmon generators. The phonon to electron coupling layer is preferably within the mean free path of phonons from reactant voids/defects.
Although the invention has been described in detail with particular reference to certain embodiments detailed herein, other embodiments can achieve the same results. Variations and modifications of the present invention will be obvious to those skilled in the art and the present invention is intended to cover in the appended claims all such modifications and equivalents.

Claims

EXOTHERMIC AND ENDOTHERMIC CYCLING POWER GENERATION
What is claimed is: 1. A power generation system comprising a thermodynamic cycle having a high- side and a low-side, a working fluid having a high-side pressure and a low-side pressure, a reaction bed wherein the reaction bed cycles between an exothermic mode and endothermic mode, and wherein the reaction bed is comprised of at least one reactant.
2. The power generation system according to claim 1 wherein the working fluid is a supercritical fluid at the high-side pressure.
3. The power generation system according to claim 1 wherein the working fluid is carbon dioxide or ammonia.
4. The power generation system according to claim 1 wherein the reaction bed in the exothermic mode is further comprised of hydrogen at an exothermic power level at least 10 percent greater than an endothermic loading level.
5. The power generation system according to claim 1 wherein the reaction bed in the exothermic mode is further comprised of hydrogen at an exothermic power level at least 50% greater than an endothermic loading level.
6. The power generation system according to claim 2 wherein the working fluid has a heat transfer rate at least 25 percent greater than a working fluid of steam.
7. The power generation system according to claim 2 wherein the working fluid has a mass flow rate at least 25 percent greater than a working fluid of steam.
8. The power generation system according to claim 1 wherein the reaction bed has an operating temperature and a damaged temperature limit and whereby the reaction bed switches from the exothermic mode to the endothermic mode when the operating temperature is at the damaged temperature limit.
9. The power generation system according to claim 8 wherein the reaction bed has an operating temperature and a damaged temperature limit and whereby the reaction bed switches from the exothermic mode to the endothermic mode when the operating temperature is at least 100 degrees Celsius less than the damaged temperature limit.
10. The power generation system according to claim 1 wherein the reaction bed is comprised of at least one reactant wherein the at least one reactant is consumed while operating in the exothermic mode.
11. The power generation system according to claim 1 wherein the reaction bed is comprised of at least one reactant wherein the at least one reactant is a reversible reactant whereby at least 90 percent of the reactant remains within the reactor bed while operating in the exothermic mode.
12. The power generation system according to claim 1 wherein the reaction bed is comprised of at least one reversible reactant wherein the at least one reactant has a surface area of greater than 2000 square meters per gram.
13. The power generation system according to claim 1 wherein the reaction bed is comprised of at least two beds operating as a simulated moving bed wherein at least one of the at least two beds is operated in exothermic mode and at least one of the at least two beds is operated in endothermic mode.
14. The power generation system according to claim 13 further comprised of a recuperator operable to recover waste heat, wherein the waste heat is utilized as a thermal source for the at least one of the at least two beds in endothermic mode.
15. The power generation system according to claim 13 wherein the at least one of the at least two beds in endothermic mode transfers thermal energy into the working fluid operable as a preheat.
16. The power generation system according to claim 13 further comprised of a second recuperator and a third reactor bed operable to have at least a distinct temperature region for each of the at least two beds and the third reactor bed.
17. A power generation system comprising a thermodynamic cycle having a high- side and a low-side, a working fluid having a high-side pressure and a low-side pressure, an exothermic reaction bed, a photon enhanced thermionic emission cell, at least one recuperator, and wherein the working fluid is a supercritical fluid at the high-side pressure.
18. The power generation system according to claim 17 further comprised of an expander and a pump, and wherein the at least one recuperator is comprised of a first recuperator downstream of the expander and upstream of the photon enhanced thermionic emission cell, and a second recuperator downstream of the pump.
19. The power generation system according to claim 18 further comprised of at least one of a phonon to electron coupling layer, and a terahertz electromagnetic frequency field.
20. A method of producing power from an exothermic source, a thermodynamic cycle having a high-side and a low-side, a working fluid having a high-side pressure and a low-side pressure, a reaction bed wherein the reaction bed cycles between an exothermic mode and endothermic mode, and wherein the reaction bed is comprised of at least one reactant.
PCT/US2013/058756 2012-09-14 2013-09-09 Exothermic and endothermic cycling power generation WO2014043029A1 (en)

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US20090139234A1 (en) * 2006-01-16 2009-06-04 Gurin Michael H Carbon dioxide as fuel for power generation and sequestration system
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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3871179A (en) * 1974-03-13 1975-03-18 Reginald B Bland Stirling cycle engine with catalytic regenerator
US4009575A (en) * 1975-05-12 1977-03-01 said Thomas L. Hartman, Jr. Multi-use absorption/regeneration power cycle
US20090139234A1 (en) * 2006-01-16 2009-06-04 Gurin Michael H Carbon dioxide as fuel for power generation and sequestration system
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US20120186219A1 (en) * 2011-01-23 2012-07-26 Michael Gurin Hybrid Supercritical Power Cycle with Decoupled High-side and Low-side Pressures

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