Description:.

CHEMICAL LOOPING COMBUSTION SYSTEM

Field of the Invention

Generally, the present disclosure relates to energy production technologies. Particularly, the present disclosure relates to a chemical looping combustion system.
Background
The background description includes information that may be useful in understanding the present invention. It is not an admission that any of the information provided herein is prior art or relevant to the presently claimed invention, or that any publication specifically or implicitly referenced is prior art.
The evolution of energy systems seeks to address the global demand for cleaner energy production methods. Among various innovative approaches, the concept of chemical looping combustion has emerged as a promising technology for carbon capture and storage (CCS). This method involves the cyclic oxidation and reduction of metal oxides to facilitate combustion without direct contact between air and fuel, thereby simplifying the capture of carbon dioxide.
Traditional combustion processes typically involve the direct combustion of fossil fuels in air, leading to the production of flue gases rich in carbon dioxide. The separation of CO2 from these gases for CCS purposes is energy-intensive and costly. In contrast, chemical looping combustion offers a more efficient pathway by using metal oxides as oxygen carriers, which transport oxygen from air to fuel, thus enabling combustion in a separate environment. This process results in a stream of CO2 that is not diluted with nitrogen from the air, significantly simplifying CO2 capture.
However, the efficiency and viability of chemical looping combustion systems are hindered by several challenges. One of the primary issues is the durability and reactivity of the metal oxides used as oxygen carriers. These materials must withstand numerous oxidation and reduction cycles without significant degradation. Additionally, the design of the reactors and the mechanism for the transport of metal oxides between them play critical roles in the overall efficiency of the system. Ensuring robust and efficient transfer of materials while minimizing energy losses is crucial.
Moreover, the integration of chemical looping combustion systems with existing industrial and power generation infrastructure poses another set of challenges. These systems require significant modifications to traditional combustion systems, including the implementation of specialized reactors and material handling systems. The capital costs associated with these modifications, along with the operational complexities, limit the widespread adoption of chemical looping combustion technology.
In light of the above discussion, there exists an urgent need for solutions that overcome the challenges associated with conventional combustion methods for efficient carbon capture. The present system aims to provide an enhanced chemical looping combustion approach, incorporating a novel air reactor, fuel reactor, and transport mechanism design, to address the aforementioned issues and improve the efficiency and sustainability of carbon capture processes.
Summary
The following presents a simplified summary of various aspects of this disclosure in order to provide a basic understanding of such aspects. This summary is not an extensive overview of all contemplated aspects, and is intended to neither identify key or critical elements nor delineate the scope of such aspects. Its purpose is to present some concepts of this disclosure in a simplified form as a prelude to the more detailed description that is presented later.
The following paragraphs provide additional support for the claims of the subject application.
In a first aspect, the present disclosure aims to provide a chemical looping combustion system comprising an Air reactor designed to oxidize Metal oxide with air to produce oxygen-depleted air and reduced metal. A Fuel Reactor is configured to receive the Reduced Metal from the Air reactor and react it with a hydrocarbon fuel to produce combustion products including CO2 and H2O, and to regenerate the metal oxide. Additionally, a transport mechanism is incorporated for moving the Reduced Metal from the Air reactor to the Fuel Reactor, and the regenerated metal oxide from the Fuel Reactor back to the Air Reactor, thus creating a closed chemical loop. Such a system enables efficient energy production while facilitating carbon capture.
Furthermore, the Air reactor includes a fluidized bed with an adjustable air distributor plate to ensure even distribution of air and maximal contact with the metal oxide particles. The Fuel Reactor comprises a cyclonic separator, a mechanical agitator for thorough mixing, and a grate unit for ash collection. A dual conduit transfer line connects the Air reactor and Fuel Reactor, including a heat exchange mechanism for preheating Reduced Metal. The system also features a set of inlets and outlets in both reactors to facilitate independent or parallel operation with additional modules.
Moreover, the transport mechanism includes a rotary valve with an airtight seal to prevent backflow, a cooling unit to regulate temperature, and a vibrating feeder with a variable speed drive for controlled transfer. A separation unit is provided to capture CO2 from combustion products for sequestration or industrial use. Both the Air and Fuel Reactors include a temperature control unit with internal cooling coils and external insulation to maintain optimal reaction temperatures. The transport mechanism further comprises a screw conveyor with an adjustable pitch for controlling the transport rate.

Brief Description of the Drawings

The features and advantages of the present disclosure would be more clearly understood from the following description taken in conjunction with the accompanying drawings in which:
FIG. 1 illustrates a block diagram of a chemical looping combustion system (100), in accordance with the embodiments of the present disclosure.
FIG. 2 illustrates two line graphs marked as (a) and (b), which quantify the mole fraction of three chemical species – methane (CH4), carbon dioxide (CO2), and water (H2O) – in a chemical looping combustion system, in accordance with the embodiments of the present disclosure.
FIG. 3 illustrates a sequence of snapshots captured from a simulation of bubble dynamics within the chemical looping combustion system, in accordance with the embodiments of the present disclosure.
FIG. 4 illustrates the relationship between the particle size of the fuel used in the chemical looping combustion process and the fuel conversion rate, in accordance with the embodiments of the present disclosure.
FIG. 5 illustrates details of time correlating the fuel conversion rate with the temperature of the system, in accordance with the embodiments of the present disclosure.
FIG. 6 illustrates effect of mass flow rate on fuel conversion, in accordance with the embodiments of the present disclosure.
FIG. 7 illustrates a detailed view of the transient fluctuations in molar concentrations for the gaseous reactant methane (CH4) and the products carbon dioxide (CO2) and water (H2O) in a chemical looping combustion system, in accordance with the embodiments of the present disclosure.
FIG. 8 illustrates a mole fraction of reactant and products at both the interface and the outlet at various inlet temperatures, in accordance with the embodiments of the present disclosure.
FIG. 9 illustrates the rate of conversion of the fuel (methane) using different ratios of CuO and NiO as oxygen carriers at a range of temperatures from 923 K to 1323 K, in accordance with the embodiments of the present disclosure.

Detailed Description
In the following detailed description of the invention, reference is made to the accompanying drawings that form a part hereof, and in which is shown, by way of illustration, specific embodiments in which the invention may be practiced. In the drawings, like numerals describe substantially similar components throughout the several views. These embodiments are described in sufficient detail to claim those skilled in the art to practice the invention. Other embodiments may be utilized and structural, logical, and electrical changes may be made without departing from the scope of the present invention. The following detailed description is, therefore, not to be taken in a limiting sense, and the scope of the present invention is defined only by the appended claims and equivalents thereof.
The use of the terms “a” and “an” and “the” and “at least one” and similar referents in the context of describing the invention (especially in the context of the following claims) are to be construed to cover both the singular and the plural, unless otherwise indicated herein or clearly contradicted by context. The use of the term “at least one” followed by a list of one or more items (for example, “at least one of A and B”) is to be construed to mean one item selected from the listed items (A or B) or any combination of two or more of the listed items (A and B), unless otherwise indicated herein or clearly contradicted by context. The terms “comprising,” “having,” “including,” and “containing” are to be construed as open-ended terms (i.e., meaning “including, but not limited to,”) unless otherwise noted. Recitation of ranges of values herein are merely intended to serve as a shorthand method of referring individually to each separate value falling within the range, unless otherwise indicated herein, and each separate value is incorporated into the specification as if it were individually recited herein. All methods described herein can be performed in any suitable order unless otherwise indicated herein or otherwise clearly contradicted by context. The use of any and all examples, or exemplary language (e.g., “such as”) provided herein, is intended merely to better illuminate the invention and does not pose a limitation on the scope of the invention unless otherwise claimed. No language in the specification should be construed as indicating any non-claimed element as essential to the practice of the invention.
Pursuant to the "Detailed Description" section herein, whenever an element is explicitly associated with a specific numeral for the first time, such association shall be deemed consistent and applicable throughout the entirety of the "Detailed Description" section, unless otherwise expressly stated or contradicted by the context.
The term "chemical looping combustion system" as used throughout the present disclosure relates to a system designed for energy production through the combustion of fuels in a manner that facilitates carbon capture. This system employs a cyclic process involving the oxidation and reduction of metal oxides to separate combustion air from fuel, preventing direct contact and thus enabling efficient capture of carbon dioxide.
The term "Air Reactor" as used throughout the present disclosure relates to a component of the chemical looping combustion system that is responsible for the oxidation of metal oxide using an inflow of air. This reactor produces oxygen-depleted air and reduced metal as outputs, playing a critical role in the system's operation by preparing the metal oxide for subsequent reaction in the fuel reactor.
The term "fuel reactor" as used throughout the present disclosure relates to a component configured to receive reduced metal from the Air Reactor. Upon receiving the reduced metal, the fuel reactor facilitates its reaction with a hydrocarbon fuel. This reaction produces combustion products, including CO2 and H2O, and regenerates the metal oxide for recirculation back to the Air Reactor, thus contributing to the closed-loop operation of the system.
The term "transport mechanism" as used throughout the present disclosure relates to the system component responsible for moving the reduced metal from the Air reactor to the Fuel Reactor and the regenerated metal oxide from the Fuel Reactor back to the Air Reactor. This mechanism ensures the continuous flow of materials necessary for the sustained operation of the chemical looping combustion process, thereby maintaining a closed chemical loop within the system.
FIG. 1 illustrates a block diagram of a chemical looping combustion system (100), in accordance with the embodiments of the present disclosure. The chemical looping combustion system (100), adapted for energy production with integrated carbon capture capabilities. In the depicted system, an Air reactor (102) is configured to receive an inflow of air and oxidize Metal oxide. The oxidation process conducted within said Air reactor (102) results in the production of oxygen depleted air and reduced metal, critical for the looping combustion process. Adjacent to the Air reactor (102), a Fuel Reactor (104) is illustrated, which is configured to accept the Reduced Metal from the Air reactor (102). Said Fuel Reactor (104) is designed to react said Reduced Metal with a hydrocarbon fuel, thereby producing combustion products that include, but are not limited to, CO2 and H2O. The reaction within the Fuel Reactor (104) also facilitates the regeneration of metal oxide, which is an essential component of the closed-loop system. Additionally, the block diagram shows a Transport Mechanism (106), strategically positioned to facilitate the movement of the Reduced Metal from the Air reactor (102) to the Fuel Reactor (104), and to transport the regenerated metal oxide from the Fuel Reactor (104) back to the Air reactor (102). Said Transport Mechanism (106) is critical in maintaining a closed chemical loop, which is a fundamental feature of the system (100) for continuous operation and improved efficiency of the combustion process.
In an embodiment, the air reactor (102) of the chemical looping combustion system (100) is enhanced by the inclusion of a fluidized bed. This fluidized bed is engineered to optimize the distribution and maximal contact of air with the metal oxide particles, essential for efficient oxygen transfer. An adjustable air distributor plate is incorporated within the fluidized bed to control the fluidization rate. Such control is pivotal in ensuring a uniform temperature distribution across the reactor, which in turn, significantly enhances the efficiency of the oxidation process within the air reactor (102). This adjustment capability allows for the adaptation of the reactor's conditions to various operational requirements, thus improving the overall performance of the chemical looping combustion system (100).
In another embodiment, the fuel reactor (104) of the system (100) comprises several critical components. A cyclonic separator is utilized to effectively separate the regenerated metal oxide from the combustion products before these are recirculated to the air reactor (102). This ensures the purity of the metal oxide for efficient oxidation. Additionally, a mechanical agitator is employed to enable thorough mixing of the reduced metal with the hydrocarbon fuel, facilitating complete combustion. A grate unit supports a packed bed of reduced metal, allowing ash from the combustion process to fall for easy collection and removal. These features collectively enhance the combustion efficiency and ease the maintenance of the fuel reactor (104), contributing significantly to the system’s (100) overall functionality.
In a further embodiment, the air reactor (102) and fuel reactor (104) of the system (100) are interconnected by a dual conduit transfer line. This innovative design enables the simultaneous transfer of reduced metal to the fuel reactor (104) and metal oxide to the air reactor (102). The dual conduit transfer line serves as a crucial component in maintaining the continuity of the chemical looping process, ensuring the efficient recycling of materials between the reactors. Such a configuration not only optimizes the system’s operational efficiency but also minimizes the time required for the transfer of materials, thereby enhancing the overall productivity of the system (100).
In yet another embodiment, the dual conduit transfer line of the system (100) incorporates a heat exchange mechanism situated between the two conduits. This mechanism facilitates the preheating of reduced metal en route to the fuel reactor (104) by utilizing the heat from the hotter metal oxide coming from the fuel reactor (104). The inclusion of this heat exchange mechanism significantly improves the energy efficiency of the system by recovering and reusing heat that would otherwise be lost. This not only reduces the energy requirement for heating the reduced metal but also contributes to a more sustainable operation of the chemical looping combustion system (100).
In an embodiment, both the air reactor (102) and fuel reactor (104) of the system (100) are designed with sets of inlets and outlets for air, fuel, and exhaust gases. These components are engineered to operate independently or in parallel with additional modules, offering versatility in the system’s configuration. Such design considerations enable the system (100) to be adapted for various scales of operation, from small to large capacities. This flexibility is critical for the integration of the system (100) into different industrial applications, thereby broadening its applicability and utility in the energy sector.
In another embodiment, the transport mechanism (106) of the system (100) comprises a rotary valve equipped with an airtight seal to prevent backflow of gases. This rotary valve, actuated by a motorized unit, controls the flow of reduced metal between the air reactor (102) and the fuel reactor (104). Additionally, a cooling unit is incorporated to regulate the temperature of the reduced metal during transportation, ensuring optimal conditions are maintained. A vibrating feeder, associated with a variable speed drive, enables the controlled transfer of metal oxide and reduced metal particles. These components collectively ensure the efficient, controlled, and safe transportation of materials within the system (100), contributing to its operational integrity and reliability.
In a further embodiment, the system (100) includes a separation unit designed to capture CO2 from the combustion products for sequestration or industrial use. This unit plays a vital role in the environmental performance of the system (100), enabling the capture and reuse or safe storage of CO2, thereby significantly reducing the greenhouse gas emissions associated with the combustion process. The inclusion of this separation unit enhances the sustainability of the system (100), aligning it with global efforts to combat climate change through carbon capture and storage technologies.
In yet another embodiment, both the Air reactor (102) and Fuel Reactor (104) of the system (100) include a temperature control unit. This unit comprises internal cooling coils and external insulation designed to maintain optimal reaction temperatures and prevent heat loss to the environment. The precise control of reaction temperatures is crucial for the efficiency and safety of the chemical looping combustion process. The temperature control unit ensures that the reactors operate within their optimal temperature ranges, maximizing the system’s efficiency while minimizing energy consumption and environmental impact.
In an embodiment, the transport mechanism (106) of the system (100) includes a screw conveyor with an adjustable pitch. This feature allows for the precise control of the transport rate of the reduced metal and metal oxide, ensuring that the flow of materials is synchronized with the operational demands of the reactors. The ability to adjust the pitch of the screw conveyor provides a high level of control over the material transfer rates, optimizing the efficiency of the chemical looping combustion process. This contributes to the system’s (100) overall operational flexibility and efficiency, enabling it to accommodate variations in fuel supply and process conditions.
FIG. 2 illustrates two line graphs marked as (a) and (b), which quantify the mole fraction of three chemical species – methane (CH4), carbon dioxide (CO2), and water (H2O) – in a chemical looping combustion system, in accordance with the embodiments of the present disclosure. The first graph (a) tracks the mole fraction at the reaction interface, while the second graph (b) measures at the outlet of the system. In graph (a), methane displays a high mole fraction that remains relatively constant, signifying it as a primary reactant. In contrast, carbon dioxide and water, likely products of the reaction, are present in lower and fluctuating concentrations. In graph (b), the outlet, there is a sharp decrease in methane indicating combustion or reaction, and corresponding increases in carbon dioxide and water, signifying their generation as a part of the process.
FIG. 3 illustrates a sequence of snapshots captured from a simulation of bubble dynamics within the chemical looping combustion system, in accordance with the embodiments of the present disclosure. Each frame is labeled with a time stamp from t=0 to t=2 seconds, illustrating how the system evolves over time. The color gradients represent the density of the materials within the system, with different colors signifying varying densities. The dynamics captured show the formation, rise, and collapse of gas bubbles through the medium, highlighting the unsteady and turbulent nature of the reaction environment.
FIG. 4 illustrates the relationship between the particle size of the fuel used in the chemical looping combustion process and the fuel conversion rate, in accordance with the embodiments of the present disclosure. The trend indicates slopes downward, indicating that larger particles correlate with a lower rate of conversion. This suggests that the size of the particles has a significant impact on the efficiency of the conversion process, with smaller particles being more favorable for conversion.
FIG. 5 illustrates details of time correlating the fuel conversion rate with the temperature of the system, in accordance with the embodiments of the present disclosure. The trend line in this graph moves upward, showing that as the temperature increases, the conversion rate also increases. This positive relationship underscores the importance of temperature as a key factor influencing the efficiency of the chemical looping combustion process, with higher temperatures enhancing the conversion rate.
FIG. 6 illustrates effect of mass flow rate on fuel conversion, in accordance with the embodiments of the present disclosure. The line graph first ascends, reaching a peak conversion rate at a certain mass flow rate, before descending again, forming a peaked curve. This indicates that there is an optimal mass flow rate at which the fuel conversion is maximized. Above and below this optimal rate, the efficiency of the conversion process diminishes. As represents the conversion rate of CH4 at the reactor outlet with CuO as a metal oxide for different mass flow rates. Depending on the overall mixture of solid and gaseous elements, the mean mole fraction value of CH4 at the outlet has been found to gradually increase for different rates of flow mass like 0.03 kg/s to 0.1 kg/s. This indicates that the conversion rate increases for a rate of flow mass between 0.01 kg/s - 0.03 kg/s where better mixing of gaseous-solid particles is noticeable. However, the conversion rate decreases gradually for other mass-flow rates above 0.03 kg/s.
FIG. 7 illustrates a detailed view of the transient fluctuations in molar concentrations for the gaseous reactant methane (CH4) and the products carbon dioxide (CO2) and water (H2O) in a chemical looping combustion system, in accordance with the embodiments of the present disclosure. These fluctuations are presented at both the interface and the reactor outlet for varying proportions of Copper Oxide (CuO) and Nickel Oxide (NiO) used as oxygen carriers. Specifically, the first row of graphs represents a 30% CuO and 70% NiO composition, the second row 50% CuO and 50% NiO, and the third row 70% CuO and 30% NiO. At the interface, approximately 20%, 25%, and 30% of fuel conversion is achieved respectively, indicating that the proportion of CuO has a direct impact on conversion efficiency at this stage. Conversely, at the reactor outlet, nearly 50%, 45%, and 40% of the fuel undergoes conversion for the corresponding mixtures. These numbers suggest that different ratios of CuO and NiO influence the combustion efficiency, with a higher percentage of CuO leading to a slight decrease in conversion at the outlet.
FIG. 8 illustrates a mole fraction of reactant and products at both the interface and the outlet at various inlet temperatures, in accordance with the embodiments of the present disclosure. The first two charts examine the interface and outlet at base temperatures, the third and fourth charts increase this temperature, and the fifth and sixth charts present further elevated temperatures. These charts showcase unsteady perturbance of molar fractions, particularly for methane, as the inlet temperature of the fuel reactor is varied. It can be inferred that higher temperatures lead to more pronounced fluctuations and possibly higher reactivity in the system, affecting the combustion process and the distribution of products and reactants throughout.
FIG. 9 illustrates the rate of conversion of the fuel (methane) using different ratios of CuO and NiO as oxygen carriers at a range of temperatures from 923 K to 1323 K, in accordance with the embodiments of the present disclosure. The conversion rate observed varies with the proportion of CuO and NiO as well as with temperature, indicating that both the composition of the metal oxides and the operational temperature play significant roles in the chemical looping combustion process. For CuO ratios of 0.3, 0.5, and 0.7, and corresponding NiO ratios of 0.7, 0.5, and 0.3, the conversion rates span between 0.45 to 0.75, 0.35 to 0.75, and 0.40 to 0.70 respectively across the temperature range. This trend suggests that an increase in temperature leads to an enhanced reaction rate within the reactor, with the highest conversion rates being observed at the highest temperatures for all compositions.
Example embodiments herein have been described above with reference to block diagrams and flowchart illustrations of methods and apparatuses. It will be understood that each block of the block diagrams and flowchart illustrations, and combinations of blocks in the block diagrams and flowchart illustrations, respectively, can be implemented by various means including hardware, software, firmware, and a combination thereof. For example, in one embodiment, each block of the block diagrams and flowchart illustrations, and combinations of blocks in the block diagrams and flowchart illustrations can be implemented by computer program instructions. These computer program instructions may be loaded onto a general purpose computer, special purpose computer, or other programmable data processing apparatus to produce a machine, such that the instructions which execute on the computer or other programmable data processing apparatus create means for implementing the functions specified in the flowchart block or blocks.
Throughout the present disclosure, the term ‘processing means’ or ‘microprocessor’ or ‘processor’ or ‘processors’ includes, but is not limited to, a general purpose processor (such as, for example, a complex instruction set computing (CISC) microprocessor, a reduced instruction set computing (RISC) microprocessor, a very long instruction word (VLIW) microprocessor, a microprocessor implementing other types of instruction sets, or a microprocessor implementing a combination of types of instruction sets) or a specialized processor (such as, for example, an application specific integrated circuit (ASIC), a field programmable gate array (FPGA), a digital signal processor (DSP), or a network processor).
The term “non-transitory storage device” or “storage” or “memory,” as used herein relates to a random access memory, read only memory and variants thereof, in which a computer can store data or software for any duration.
Operations in accordance with a variety of aspects of the disclosure is described above would not have to be performed in the precise order described. Rather, various steps can be handled in reverse order or simultaneously or not at all.
While several implementations have been described and illustrated herein, a variety of other means and/or structures for performing the function and/or obtaining the results and/or one or more of the advantages described herein may be utilized, and each of such variations and/or modifications is deemed to be within the scope of the implementations described herein. More generally, all parameters, dimensions, materials, and configurations described herein are meant to be exemplary and that the actual parameters, dimensions, materials, and/or configurations will depend upon the specific application or applications for which the teachings is/are used. Those skilled in the art will recognize, or be able to ascertain using no more than routine experimentation, many equivalents to the specific implementations described herein. It is, therefore, to be understood that the foregoing implementations are presented by way of example only and that, within the scope of the appended claims and equivalents thereto, implementations may be practiced otherwise than as specifically described and claimed. Implementations of the present disclosure are directed to each individual feature, system, article, material, kit, and/or method described herein. In addition, any combination of two or more such features, systems, articles, materials, kits, and/or methods, if such features, systems, articles, materials, kits, and/or methods are not mutually inconsistent, is included within the scope of the present disclosure.

Claims

I/We claim:

A chemical looping combustion system (100) comprising:
an air reactor (102) configured to oxidize Metal oxide with an inflow of air, thereby producing oxygen depleted air and reduced metal;
a fuel reactor (104) configured to receive the Reduced Metal from the Air reactor (102) and react it with a hydrocarbon fuel to produce combustion products, including CO2 and H2O, and to regenerate the metal oxide; and
a transport mechanism (106) for moving the Reduced Metal from the air reactor (102) to the fuel reactor (104), and the regenerated metal oxide from the fuel reactor (104) to the air reactor (102), thus creating a closed chemical loop.
The system (100) of claim 1, wherein the air reactor (102) comprises a fluidized bed to facilitate even distribution and maximal contact of air with the metal oxide particles for oxygen transfer, wherein the fluidized bed in the air reactor (102) comprises an adjustable air distributor plate for controlling the fluidization rate and ensuring uniform temperature distribution across the reactor.
The system (100) of claim 1, wherein the fuel reactor (104) comprises:
a cyclonic separator to separate the regenerated metal oxide from the combustion products before recirculation to the air reactor (102);
mechanical agitator that enable thorough mixing of the reduced metal with the hydrocarbon fuel for complete combustion; and
a grate unit to support a packed bed of reduced metal and allowing the ash from the combustion of hydrocarbon fuels to fall for easy collection and removal.
The system (100) of claim 1, wherein the air reactor (102) and fuel reactor (104) are connected by a dual conduit transfer line allowing for the simultaneous transfer of reduced metal to the fuel reactor (104) and metal oxide to the air reactor (102).
The system (100) of claim 5, wherein the dual conduit transfer line includes a heat exchange mechanism between the two conduits, allowing for the preheating of reduced metal en route to the fuel reactor (104) by the hotter metal oxide coming from the fuel reactor (104).
The system (100) of claim 1, wherein each of air reactor (102) and fuel reactor (104) comprises set of inlets and outlets for air, fuel, and exhaust gases, and are designed to operate independently or in parallel with additional modules.
The system (100) of claim 1, wherein the transport mechanism (106) comprises:
a rotary valve to control the flow of reduced metal between the air reactor (102) and the fuel reactor (104), wherein the rotary valve is actuated by a motorized unit, wherein the rotary valve comprise an airtight seal to prevent backflow of gases;
a cooling unit to regulate the temperature of the reduced metal during transportation; and
a vibrating feeder to enable flow of the metal oxide and reduced metal particles, wherein the vibrating feeder is associated with a variable speed drive to control the transfer rate of metal oxide and reduced metal particles.
The system (100) of claim 1, further comprising a separation unit to capture CO2 from the Combustion Products for sequestration or industrial use.
The system (100) of claim 1, wherein the Air reactor (102) and Fuel Reactor (104) both include a temperature control unit comprising internal cooling coils and external insulation to maintain optimal reaction temperatures and prevent heat loss to the environment.
The system (100) of claim 1, wherein the transport mechanism (106) comprises a screw conveyor with an adjustable pitch, allowing for the control of the transport rate of the reduced metal and metal oxide.

CHEMICAL LOOPING COMBUSTION SYSTEM

An innovative chemical looping combustion system is disclosed, aimed at enhancing carbon capture and energy efficiency. This system encompasses an Air reactor for oxidizing Metal oxide with air to yield oxygen depleted air and reduced metal. It also includes a Fuel Reactor that receives Reduced Metal from the Air Reactor, facilitating its reaction with a hydrocarbon fuel to generate combustion products like CO2 and H2O, while regenerating the metal oxide. A transport mechanism efficiently moves Reduced Metal and regenerated metal oxide between the Air reactor and Fuel Reactor, thereby maintaining a closed chemical loop. This system is designed to improve the capture of carbon dioxide, thus contributing to cleaner energy production methods.

Drawings
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FIG. 1
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FIG. 2
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FIG. 3
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FIG. 4
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FIG. 5
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FIG. 6
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FIG. 7
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FIG. 8
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FIG. 9
, Claims:I/We claim:

A chemical looping combustion system (100) comprising:
an air reactor (102) configured to oxidize Metal oxide with an inflow of air, thereby producing oxygen depleted air and reduced metal;
a fuel reactor (104) configured to receive the Reduced Metal from the Air reactor (102) and react it with a hydrocarbon fuel to produce combustion products, including CO2 and H2O, and to regenerate the metal oxide; and
a transport mechanism (106) for moving the Reduced Metal from the air reactor (102) to the fuel reactor (104), and the regenerated metal oxide from the fuel reactor (104) to the air reactor (102), thus creating a closed chemical loop.
The system (100) of claim 1, wherein the air reactor (102) comprises a fluidized bed to facilitate even distribution and maximal contact of air with the metal oxide particles for oxygen transfer, wherein the fluidized bed in the air reactor (102) comprises an adjustable air distributor plate for controlling the fluidization rate and ensuring uniform temperature distribution across the reactor.
The system (100) of claim 1, wherein the fuel reactor (104) comprises:
a cyclonic separator to separate the regenerated metal oxide from the combustion products before recirculation to the air reactor (102);
mechanical agitator that enable thorough mixing of the reduced metal with the hydrocarbon fuel for complete combustion; and
a grate unit to support a packed bed of reduced metal and allowing the ash from the combustion of hydrocarbon fuels to fall for easy collection and removal.
The system (100) of claim 1, wherein the air reactor (102) and fuel reactor (104) are connected by a dual conduit transfer line allowing for the simultaneous transfer of reduced metal to the fuel reactor (104) and metal oxide to the air reactor (102).
The system (100) of claim 5, wherein the dual conduit transfer line includes a heat exchange mechanism between the two conduits, allowing for the preheating of reduced metal en route to the fuel reactor (104) by the hotter metal oxide coming from the fuel reactor (104).
The system (100) of claim 1, wherein each of air reactor (102) and fuel reactor (104) comprises set of inlets and outlets for air, fuel, and exhaust gases, and are designed to operate independently or in parallel with additional modules.
The system (100) of claim 1, wherein the transport mechanism (106) comprises:
a rotary valve to control the flow of reduced metal between the air reactor (102) and the fuel reactor (104), wherein the rotary valve is actuated by a motorized unit, wherein the rotary valve comprise an airtight seal to prevent backflow of gases;
a cooling unit to regulate the temperature of the reduced metal during transportation; and
a vibrating feeder to enable flow of the metal oxide and reduced metal particles, wherein the vibrating feeder is associated with a variable speed drive to control the transfer rate of metal oxide and reduced metal particles.
The system (100) of claim 1, further comprising a separation unit to capture CO2 from the Combustion Products for sequestration or industrial use.
The system (100) of claim 1, wherein the Air reactor (102) and Fuel Reactor (104) both include a temperature control unit comprising internal cooling coils and external insulation to maintain optimal reaction temperatures and prevent heat loss to the environment.
The system (100) of claim 1, wherein the transport mechanism (106) comprises a screw conveyor with an adjustable pitch, allowing for the control of the transport rate of the reduced metal and metal oxide.

CHEMICAL LOOPING COMBUSTION SYSTEM