Patent Application
20240279820
This disclosure relates to green power production technology, especially processing carbon dioxide and other greenhouse gases. More particularly, the inventive concepts presented herein relate to arc-discharge powered reactors and affiliated techniques for high-efficiency carbon capture for fuel power production that also yields useful carbon-based by-products, resulting in an overall negative emissions profile.
One approach to address global climate change involves isolating greenhouse gases (GHGs) such as methane, carbon dioxide, etc. from the atmosphere by deploying air-to-GHG removal plants around the world, and then sequestering the GHGs, e.g., in deep underground reservoirs. To appreciate the scale necessary to achieve carbon reduction goals, approximately 40,000 installations of air-to-GHG removal plants that correspond to the over 40,000 or more fossil fuel-fired electricity generation plants around the world would be required to isolate the GHGs generated by these fossil fuel-fired electricity generation plants.
Even if these air-to-GHG removal plants were able to operate at an economic efficiency level of few hundred dollars per ton, the significant problems associated with moving the GHGs to storage sites makes the GHG sequestration approach virtually unachievable. At the scale necessary to achieve proposed carbon reduction goals, moving GHGs to sequestration sites would require an estimated 65,000 miles of pipeline for the United States alone. Unfortunately, geopolitical pressures render sequestration approaches impractical, even if the cost of the pipelines were to be borne by sovereign nation government entities.
Moreover still, ongoing efforts to reduce environmental impact of modern human activities (including but not limited to power production) rely increasingly on the ability to replace fossil fuels as a primary power source. A large proportion of green technologies and research propose using electrical power generated from “clean” sources as a primary alternative. However, in order to enable continuous operation of these electric-focused approaches, a massive amount of energy storage is required. In plain terms, this means we need more efficient and more numerous batteries, which often require rare and difficult-to-produce materials such as “pristine” carbon products (graphene, 3D graphene, nanotubes, etc.).
Accordingly, what is needed are systems and techniques for preventing the GHGs generated from combustion at fossil fuel-fired electricity generation plants from entering the biosphere in the first place. In addition, new and improved technology is required to mitigate release of GHGs currently locked up in the environment. Such systems and techniques should also ideally be capable of permanently reincorporating any, and preferably all, released GHGs into useful products and materials for green technologies and applications such as energy storage, construction, industrial, textiles, transportation, sensors, etc. as will be appreciated by those having ordinary skill in the art upon reading the present disclosure. Furthermore, suitable systems will be highly scalable, simple to operate, easily accessible, entirely portable, and broadly applicable to a wide variety of practical uses including but not limited to those stated hereinabove. The inventive concepts presented herein address problems associated with greenhouse gases at the source, but also extend to recapturing and utilizing released GHGs in practical applications.
A processing reactor receives an effluent exhaust gas stream (e.g., from a coal-fired or natural gas-fired electricity generation facility). The effluent exhaust gas stream is directed through a high frequency, atmospheric pressure, non-equilibrium plasma to break apart target GHG molecules such as methane, carbon dioxide, carbon monoxide, nitrous oxide, nitrogen oxides (NOx), sulfoxides (SOx) and unspent hydrocarbons.
The elements released from these cracked molecules are then controlled by an electromotive force to maintain separation, modulate ion lifetimes, and allow for recombination of oxygen, nitrogen, and hydrogen atoms into H2, O2, N2, and H2O. These benign (or in the case of oxygen, beneficial) resultant gases can then be released into the surrounding environment or used for other purposes.
Meanwhile, carbon and/or sulfur solids are captured and collected for industrial and manufacturing uses. Notably, the processing reactor facilitates tuning of the plasma such that desired species of carbon solids (e.g., graphene) are produced as by-products.
These carbon solid by-products may be employed directly in a variety of applications, including but not limited to production of advanced composite materials, industrial diamond, carbon fiber, carbon-based building materials, polymer and chemical synthesis, etc., as well as in energy storage applications, sensor technology, and aerospace applications, among others.
According to one aspect, a system for producing solid carbon from carbon dioxide gas and water includes: one or more flow inlets configured to direct carbon dioxide and water into a reactor configured to dissociate the carbon dioxide and the water into one or more dissociated species using a plasma generated by the reactor; a voltage generator configured to generate a pulsed electric field that facilitates one or more chemical reactions between the dissociated species; and a receptacle configured to receive solid carbon generated by some or all of the one or more chemical reactions.
According to another aspect, a system for producing solid carbon from one or more greenhouse gases (GHGs) includes: one or more flow inlets configured to direct a supply gas comprising GHGs into a reactor configured to dissociate at least some of the GHGs into one or more dissociated species using a plasma generated within a volume of the reactor; a voltage generator configured to generate a pulsed electric field within the volume of the reactor; and at least one receptacle configured to receive solid carbon generated within the volume of the reactor via the dissociating and the pulsed electric field.
According to yet another aspect, a system for producing solid carbon and/or hydrogen from one or more greenhouse gases (GHGs) includes: a DC power supply coupled to a reactor via a primary anode and a primary cathode; and one or more dielectrics positioned within the reactor between the primary anode and the primary cathode. The DC power supply and the one or more dielectrics are cooperatively configured to generate an arc discharge plasma within the reactor; and the plasma is configured to dissociate at least some of the GHGs into one or more dissociated species upon contact with the plasma. The system further comprises one or more secondary electrodes coupled to the reactor and configured to generate a pulsed electric field within the reaction chamber to control one or more chemical reactions occurring therein, where at least one of the chemical reactions creates solid carbon and gaseous hydrogen from one or more of the dissociated species.
According to still yet another aspect, a method for producing solid carbon and/or hydrogen from one or more greenhouse gases (GHGs) includes: receiving, at a dissociating reactor, a supply gas comprising one or more GHGs; dissociating, using the dissociating reactor, some or all of the GHGs into the one or more dissociated species; controlling, using a pulsed electric field generated within a volume of the dissociating reactor, one or more chemical reactions involving some or all of the one or more dissociated species to generate one or more desired output species; and collecting the some or all of the one or more desired output species.
Further details of aspects, objectives, and advantages of the technological aspects are described herein, and in the drawings and claims.
The drawings described below are for illustration purposes only. The drawings are not intended to limit the scope of the present disclosure. This patent or application file contains at least one drawing executed in color. Copies of this patent or patent application publication with color drawings will be provided by the U.S. Patent and Trademark Office upon request and payment of the necessary fee.
Many long-term strategies for combating climate change count heavily on the ability to capture and sequester the huge amounts of carbon dioxide that result from burning fossil fuels. The intent is to sequester it permanently in deep underground rock formations. Unfortunately, high costs of sequestration and lingering technical uncertainties mean the foregoing carbon capture and storage (CCS) strategies may not contribute significantly in reducing global carbon dioxide emissions into the environment.
A recent report from the International Energy Agency (IEA) warns that the development and deployment of CCS is “seriously off pace” as a way to prevent the average global temperature from rising more than 2° C. The window to begin applying CCS toward consequential emissions reduction is “shrinking fast,” and the IEA has declared that CCS must supply over a fifth of the emissions reductions needed by the year 2050 to keep the temperature rise below 2° C.
All told, today's sequestration capture technologies sequester only about 20 million metric tons of carbon dioxide per year. By comparison, coal burning in the United States and China alone accounts for approximately 7 billion metric tons of carbon dioxide emissions each year.
To meet the 2° C. goal, the IEA states a minimum of 110 additional projects at power plants and industrial facilities should be brought online by 2020—with at least enough capacity to capture and store 269 million metric tons of carbon dioxide that year. Although many large-scale projects are in planning or construction phases, it can take more than a decade to build a new CCS project. The conventional CCS strategy presents a colossal example of “too little too late”.
Even worse, the foregoing problems with the CCS strategy are further complicated by the fact that techniques for chemically and/or mechanically separating carbon dioxide from plant exhaust or natural gas streams are expensive and fraught with complex processing logistics. Firstly, before the gas can be buried, it must be compressed to a supercritical state and then transported (e.g., via pipeline) to the injection site-both of which are very expensive processes. As such, CCS adds too much to the price of power production for CCS to serve as a cost-effective solution.
Additional details regarding separating carbon solids from gases can be found in U.S. Pat. No. 10,781,103, filed Feb. 22, 2019 and entitled “Microwave Reactor System with Gas-Solids Separation,” the contents of which are herein incorporated by reference.
Secondly, traditional carbon sequestration technologies rely on the availability of sequestration locations for permanent storage of the emitted carbon dioxide. Many sequestration locations have not proven to be viable and/or have not lived up to the hope. For example, many proposed underground sequestration sites have been met with political challenges by the public. As another example, the permeability of deep saline cavities is very low, making it hard to get the fluid into the rock. Furthermore, studies have shown that delivering sufficiently large volumes into these cavities is not feasible without the potential for triggering earthquakes. Worse, such earthquakes that might occur on faults could let the sequestered gas escape.
Even if the technological and political problems associated with securing and maintaining sequestration sites are solved, current carbon capture/sequestration methods simply divert CO2 into these sites. Unfortunately, this merely postpones dealing with the existence of super-large volumes of greenhouse gasses phase and other pollutants.
Indeed, long term prospects for sequestration and plasma-based solid carbon capture contrast starkly. While sequestration costs tend to rise over time, e.g., due to limited availability of sequestration sites, and increasing regulations on carbon, plasma-based solid carbon capture is projected to exhibit continuing cost decreases due to improved efficiency and growing maturity of resale markets for the solid carbon products.
To take full advantage of these projected cost decreases, carbon capture must be deployed on a large scale. To illustrate this scale, consider that on a typical summer day, the greater Los Angeles area demands well over 5 GW of peak power from its fossil fuel fired electric generation plants. If implementing carbon capture at a 5 GW power plant, approximately 500 MW of input electricity is required to dissociate greenhouse gases into capturable carbon solids. This can be implemented using about seven 75 MW klystron-based microwave energy emitters. Optionally, a larger number of lesser-powered microwave energy emitters may be used.
Application of the disclosed techniques eliminates sequestration by chemically deconstructing the pollutant species into benign constituents. Additionally, application of the disclosed techniques provides many environmental and economic benefits by returning the captured constituent elements (e.g., C and O2) for use in other applications. Still further advantages of plasma-based solid carbon capture techniques over traditional sequestration are given in Table 1.
An improved approach—and one that avoids leaving an unwelcome inheritance to future generations—is to process carbon dioxide and other greenhouse gasses into solid carbons, thus completely avoiding the problems associated with traditional carbon dioxide capture and storage techniques.
Disclosed herein are highly innovative approaches for high-efficiency solid carbon capture. The various approaches can be applied in a manner that completely eliminates polluting emissions that are a byproduct of fossil fuel combustion. The technique can capture and remove carbon from exhaust streams of any fossil fuel processes such as are operated by, for instance, coal-fired or natural gas-fired electricity generation utilities and other big greenhouse gas producers.
As hereinabove indicated, a processing reactor receives an effluent exhaust gas stream (e.g., from a coal-fired or natural gas-fired electricity generation facility). The effluent exhaust gas stream is directed through a high frequency, atmospheric pressure, non-equilibrium plasma to break apart target molecules such as carbon dioxide, carbon monoxide, and unspent hydrocarbons. Additional details regarding general approaches to maintaining a non-equilibrium plasma can be found in U.S. Pat. No. 11,107,662, filed Sep. 30, 2020, and entitled “Reactor System Coupled to an Energy Emitter Control Circuit,” the contents of which are herein incorporated by reference.
According to preferred embodiments, reactors utilized in the context of the presently described inventive embodiments include arc discharge reactors, in which a supply gas (such as methane, or a mixture of greenhouse gases or other suitable supply materials as described herein) is fed into a reactor, e.g. via one or more inlets (which may include inlets reintroducing supply gas or recycled supply gas into the reactor for additional processing) and passed along a length of a reaction chamber where a high current (e.g., characterized by a magnitude of 100 amperes or more) electrical arc is generated, e.g. using a DC power supply operatively coupled to a control circuit and receiving control signal(s) from said control circuit. The DC power supply preferably operates at constant current to provide the high current, and generates arc(s) (equivalently referred to herein as “arc discharge(s)” of electrical current) within the reaction zone. The arcing electricity has voltage and current characteristics that are sufficient to generate a plasma within the reaction zone. The arcing phenomenon may be facilitated by presence of one or more insulators or dielectrics (e.g. hollow or cylindrical ceramic dielectric monoliths) placed within the reaction chamber and between opposing electrodes of the DC power supply. More specifically, the arc generates an equilibrium plasma that may have a temperature on the order of about 6000 K or more. The specific amount of current, and corresponding plasma temperature, may be controlled to maintain desired input energies within the reaction chamber and drive dissociation of input materials into constituent components, followed by reconstitution of desired output materials (preferably including but in no way being limited to pristine carbons, graphene, 3D graphene, etc. as would be understood by a person having ordinary skill in the art upon reading the present disclosure). For instance, in one general approach the DC power supply may operate in constant current mode and generate power in a range from several kW/hr to several GW/hr. Advantageously, according to various embodiments, the reactor is operable under ambient pressure conditions.
Additional details regarding an exemplary implementation of an arc discharge plasma reactor and operation thereof in accordance with the presently described inventive concepts are set forth and described with reference to
The elements released from these cracked molecules are then controlled by an electromotive force to maintain separation, modulate ion lifetimes, and allow for recombination of oxygen, nitrogen, and hydrogen atoms into O2, N2, and H2O. These benign (or in the case of oxygen, beneficial) resultant gases can then be released into the surrounding environment or used for other purposes.
The solid carbons are formed in a plasma. The plasma is generated by combining a specific arrangement of active electrodes with energy-optimized electromagnetic radiation and high intensity electric fields. Formed on the active electrodes are arrangements wrapped around the gas stream to precisely create the necessary frequencies and energy levels for breaking apart the molecules. Efficiency is partially dependent on the precision with which the electrodes are arranged in the reactor and on the type and magnitude of energy supplied to the system. Control of these variables dominates the morphology of the carbons produced (e.g., graphene, carbon nano-onions, mixed phase graphenes, etc.).
In some approaches, the arc-discharge reactors implemented in the context of the presently described inventive concepts may be characterized by an individual output power in a range from about 2 MW to about 10 MW, or any value therebetween, such as about 2.5 MW, about 3.33 MW, about 5 MW, about 6.66 MW, about 7.5 MW, about 8 MW, about 9 MW, etc. Moreover, multiple reactors may be coupled or multiplexed to generate a total power output sufficient to drive dissociation of methane into solid carbon and hydrogen gas, according to the operating characteristics and requirements of the particular implementation in question, as would be understood by those having ordinary skill in the art upon reading the present disclosure.
These non-polluting solid carbon capture processes provide a highly efficient means for elemental carbon removal from electricity generation plant exhaust streams while only using an estimated 10-15% of the electricity generated by that plant. Moreover, by incorporating the captured carbon into these solids, subsequent release into the atmosphere is extremely unlikely, particularly less so than when employing conventional carbon sequestration techniques. Accordingly, the presently disclosed inventive concepts represent a revolutionary approach to CCS, while also providing economically useful by-products.
Some of the terms used in this description are defined below for easy reference. The presented terms and their respective definitions are not rigidly restricted to these definitions—a term may be further defined by the term's use within this disclosure. The term “exemplary” is used herein to mean serving as an example, instance, or illustration. Any aspect or design described herein as “exemplary” is not necessarily to be construed as preferred or advantageous over other aspects or designs. Rather, use of the word exemplary is intended to present concepts in a concrete fashion. As used in this application and the appended claims, the term “or” is intended to mean an inclusive “or” rather than an exclusive “or”. That is, unless specified otherwise, or is clear from the context, “X employs A or B” is intended to mean any of the natural inclusive permutations. That is, if X employs A, X employs B, or X employs both A and B, then “X employs A or B” is satisfied under any of the foregoing instances. As used herein, at least one of A or B means at least one of A, or at least one of B, or at least one of both A and B. In other words, this phrase is disjunctive. The articles “a” and “an” as used in this application and the appended claims should generally be construed to mean “one or more” unless specified otherwise or is clear from the context to be directed to a singular form.
Various aspects are described herein with reference to the figures. It should be noted that the figures are not necessarily drawn to scale, and that elements of similar structures or functions are sometimes represented by like reference characters throughout the figures. It should also be noted that the figures are only intended to facilitate the description of the disclosed aspects-they are not representative of an exhaustive treatment of all possible aspects, and they are not intended to impute any limitation as to the scope of the claims. In addition, an illustrated aspect need not portray all aspects or advantages of usage in any particular environment.
An aspect or an advantage described in conjunction with a particular aspect is not necessarily limited to that aspect and can be practiced in any other aspects even if not so illustrated. References throughout this specification to “some aspects” or “other aspects” refer to a particular feature, structure, material or characteristic described in connection with the aspects as being included in at least one aspect. Thus, the appearance of the phrases “in some aspects” or “in other aspects” in various places throughout this specification are not necessarily referring to the same aspect or aspects. The disclosed aspects are not intended to be limiting of the claims.
According to one aspect, a method for producing solid carbon from carbon dioxide gas and water includes: receiving carbon dioxide and water in a reactor configured to generate a plasma; dissociating the carbon dioxide and the water using the plasma to form one or more dissociated species; exposing the dissociated species to an electric field configured to facilitate one or more chemical reactions; generating solid carbon via the chemical reactions; and outputting the solid carbon from the reactor.
According to another general aspect, a system includes: a waveguide comprising a plasma zone extending along a length of the first waveguide; a microwave energy source coupled to the waveguide; a first flow inlet configured to flow carbon dioxide gas into the plasma zone; and a gas-solid separator system coupled to the microwave plasma reactor. The microwave energy source is configured to propagate microwave energy into the waveguide. The microwave energy is configured to generate a plasma within the plasma zone. The plasma within the plasma zone is configured to dissociate the carbon dioxide gas into a plurality of components including oxygen gas and solid carbon particles. The gas-solid separator (GSS) system is configured to receive the plurality of components.
According to yet another general aspect, a system includes: a plurality of reaction chambers, wherein each reaction chamber is coupled, directly or indirectly, to at least one microwave energy source, at least one amplifier, and at least one receptacle. Each reaction chamber comprises a waveguide coupled to the microwave energy source. Each waveguide respectively includes a plasma zone configured to generate a plasma in response to the microwave energy; at least one inlet configured to deliver raw material into the plasma zone; and an outlet configured to output a powder based on the raw material.
According to still yet another general aspect, a composition of matter includes a carbonaceous material having physical characteristics of being formed from dissociation of carbon dioxide and water using a plasma and an electric field.
To illustrate,
These products are fed directly into the REACTOR, and exposed to one or more plasmas (not shown) that are tuned/controlled in order to produce desired solid carbon by products (SOLID CARBON), such as graphene (GRAPHENE), three-dimensional carbon structures (3D CARBON), and/or more conventional carbon based materials (CONVENTIONAL MATERIALS) suitable for, e.g., incorporation into building materials, tires, etc. as would be understood by a person having ordinary skill in the art upon reading the present disclosure.
Meanwhile, other by-products of the reaction(s) performed in the REACTOR include molecular oxygen and/or nitrogen, according to one various aspects and generally depending on the type of input provided to/combusted in the FACILITY. Preferably, at least some of the oxygen (O2) produced is released into the BIOSPHERE, providing additional environmental benefits beyond mere capture of carbon from the FOSSIL FUEL. Optionally, oxygen produced in the REACTOR may be returned to the FACILITY to help drive combustion of further fuel.
FACILITY and REACTOR each preferably include a cap or other mechanism for preventing emissions from escaping. In this manner, aside from beneficial oxygen release (and/or release of benign products such as molecular nitrogen), the REACTOR enables power generation with zero emissions. By capturing carbon in more-or-less permanent form via the solid carbon products, overall emissions from generating power according to an arrangement as shown in
As will be appreciated by persons having ordinary skill in the art, generating solid carbon, and especially particular desired species of carbon products, requires much more than simply exposing carbon dioxide to plasma. As indicated previously, the plasma is controlled and tuned to yield specific conditions necessary for efficiently converting carbon dioxide gas into solid carbon, according to a two-reaction scheme described in greater detail hereinbelow with reference to
To appreciate the impact of the plasma energy curve 202, consider the well-known Bosch reaction (shown in Eq. 1 and Eq. 2). The Bosch reaction is a chemical reaction between carbon dioxide and hydrogen that produces elemental carbon (graphite), water, and a 10% return of invested heat. The Bosch reaction requires the introduction of a catalyst and requires a temperature level of 530-730° Celsius. The first reaction, known as water shift-gas reaction (Eq. 1), is very fast while the second reaction (Eq. 2) is slow and is, therefore, the controlling reaction:
Systems that carry out the foregoing chemical reactions have been used to remove carbon dioxide from the atmosphere of space capsules. One such system exploits a high temperature (600° Celsius) catalytic reaction to convert carbon dioxide into elemental carbon dust and water. Such a system can be very effective with respect to removal of carbon dioxide from the atmosphere, however such systems suffer two critical deficiencies: (1) carrying out the second reaction in which the elemental carbon is extracted from the carbon monoxide causes fouling of the catalytic surfaces by forming a solid-solid solution, which is the result of the metallurgical reaction in which the carbon atoms dissolve in the metal catalyst, thus resulting in a severely limited operational lifetime of the system; and (2) causing and controlling the foregoing chemical reactions is very inefficient from an energy cost perspective.
Plasma-based techniques address both deficiencies, specifically: (1) when using plasma-based techniques, there is no need for catalysts, and as such, there is no fouling of the catalytic surfaces; and (2) the energy efficiency of the process is much higher when using the herein-disclosed techniques.
To further explain this latter point, the energy efficiency in the conversion of carbon dioxide into elemental carbon is directly tied to the reaction rates of the necessary chemical pathways. To understand where major efficiency loss mechanisms exist in a thermal, catalytic thermal, and plasma catalytic-based systems, the energetic particle densities and their associated energies for each system must be examined.
As shown in
As the plot of
Now, referring to the plasma catalysis curve 202, virtually all particles actively participate in the chemical reaction process, providing a much more efficient process. Notably, using plasma catalysis enables approximately all of the particles to participate in conversion chemistry, ultimately producing solid carbon. In addition, plasma catalysis does not require the use of a separate catalyst to lower the activation energy, avoiding contamination and consumption problems associated therewith.
One possible pathway is shown and discussed as pertains to
As shown, this scheme operates by directing an exhaust gas stream through a high-frequency atmospheric pressure non-equilibrium plasma to break apart pollutant molecules (e.g., silanes, siloxanes, polysiloxanes, cadmium oxides, NOx, SOx, COx, hydrocarbons, etc. as would be understood by a person having ordinary skill in the art upon reading the present disclosure). The elements released from these dissociated molecules are then controlled by an electromotive force to maintain separation of the dissociated constituents and to facilitate disposition (e.g., collection or release) of the resultant substances. As shown, free oxygen and hydrogen atoms are permitted to recombine into O2, and H2O, and are released into the air. (Those having ordinary skill in the art will appreciate other products, such as molecular nitrogen, may be produced when other pollutant molecules are present.) Other elements (primarily carbon, but also including sulfur, silicon, etc. according to some approaches) are captured as solids, and then collected for industrial and manufacturing uses such as heretofore discussed.
Referring again to
In addition, it is preferable to remove oxygen from the system quickly, so as to avoid recombination and improve overall conversion efficiency.
An important aspect of
To address this shortcoming, the presently described inventive concepts leverage water (and various dissociated species thereof) to provide additional dissociation pathways and chemical reaction pathways to convert carbon dioxide (and various dissociated species thereof) or methane into solid carbon. While
Accordingly, the presently disclosed inventive concepts take advantage of a second reaction pathway, denoted by the dashed lines in
If the impacting electron has energy greater than the activation energy, the surplus energy will be scattered or re-radiated as electrons. These secondary electrons might have sufficient energy to cause further reactions within the plasma chemistry system such that one electron of sufficiently high energy could result in the dissociation of many states. For example, one 100 eV electron could take part in a three-step dissociation process to produce C+, as shown in the second reaction pathway of
As will be appreciated by persons having ordinary skill in the art upon reading the present disclosure, these reaction pathways (particularly the second reaction pathway) requires input energy on a scale that prohibits use of thermal energy sources to achieve the desired dissociation states and corresponding conversion of CO2 into solid carbon at desired efficiency (e.g., conversion efficiency up to about 85%, up to about 90%, up to about 95%, up to about 98%, up to about 99%, or up to about 100%, according to various aspects).
Accordingly, the presently disclosed inventive concepts employ ultra high frequency energy sources, such as one or more magnetron(s), one or more klystron(s), or any other suitable source for generating ultra high frequency radiation (preferably microwave radiation) sufficient to generate a plasma, most preferably a plasma characterized by an energy of approximately 100 electron volts (eV) (which requires about 1 gigawatt of input energy), and/or a frequency in a range from about one gigahertz to about five gigahertz, in various aspects. Preferably, the energy sources (and/or corresponding reactors) are configured so that energy output can be accumulated from among a plurality of sources/reactors chained together, e.g., so as to facilitate amplification and/or multiplexing of power generated by the series.
For instance, again considering a plasma characterized by an energy of approximately 100 eV, in various aspects suitable energy sources may include 100 one-megawatt reactors, 50 two-megawatt reactors, 25 four-megawatt reactors, or any other suitable combination of reactors connected together so as to output a total of 1 gigawatt energy to drive the plasma. In preferred aspects, the reactors may include LYTEN® klystron reactors. Of course, in alternative aspects, different energy output requirements may be met using different combinations and types of reactors, as would be appreciated by a person having ordinary skill in the art upon reading the present disclosure.
In more embodiments, particularly those employing arc discharge reactor(s) as the dissociating reactor, the energy of the plasma may be anywhere in a range from about 1.0 eV to about 5.0 eV.
It should be noted that the foregoing exemplary plasma energies may be scaled according to the particular needs of the application to which the reactor is employed. For instance, a multitude of reactors may each provide a plasma characterized by an energy in a range from about 1.0 eV to about 5.0 eV, allowing for cumulative plasma energy beyond 5.0 eV, as would be understood by those having ordinary skill in the art upon reading the present descriptions.
Moreover, and again with particular regard to implementations involving arc discharge reactors, the frequency of the electric field created within the plasma may depend on the type of power source.
For instance, an alternating current power source may generate a field having a frequency anywhere in a range from about 0 Hz to about 500 kHz (including values and subranges therebetween, such as a frequency of about 1 Hz, about 10 Hz, about 25 Hz, about 33 Hz, about 50 Hz, about 66 Hz, about 75 Hz, about 80 Hz, about 90 Hz, about 95 Hz, about 100 Hz, about 125 Hz, about 133 Hz, about 150 Hz, about 166 Hz, about 175 Hz, about 190 Hz, about 200 Hz, about 250 Hz, about 275 Hz, about 300 Hz, about 333 Hz, about 350 Hz, about 400 Hz, about 425 Hz, about 450 Hz, about 475 Hz, about 490 Hz, about 500 Hz, about 666 Hz, about 750 Hz, about 1 kHz, about 2.5 kHz, about 3.33 kHz, about 5 kHz, about 6.66 kHz, about 7.5 kHz, about 9 kHz, about 10 kHz, about 25 kHz, about 33 kHz, about 50 kHz, about 66 kHz, about 75 kHz, about 100 kHz, about 250 kHz, about 333 kHz, about 400 kHz, about 500 kHz, or any value or subrange therebetween falling within the broad range from about 0 Hz to about 500 kHz.
By contrast, the frequency of the electric field when implementing a direct current power source is 0 kHz.
However, whether using an AC or a DC field, the field may be pulsed, and pulsing may be performed at a frequency anywhere in a range from about 0 Hz to about 200 kHz (including values and subranges therebetween, such as a frequency of about 1 Hz, about 10 Hz, about 25 Hz, about 33 Hz, about 50 Hz, about 66 Hz, about 75 Hz, about 80 Hz, about 90 Hz, about 95 Hz, about 100 Hz, about 125 Hz, about 133 Hz, about 150 Hz, about 166 Hz, about 175 Hz, about 190 Hz, about 200 Hz, about 250 Hz, about 275 Hz, about 300 Hz, about 333 Hz, about 350 Hz, about 400 Hz, about 425 Hz, about 450 Hz, about 475 Hz, about 490 Hz, about 500 Hz, about 666 Hz, about 750 Hz, about 1 kHz, about 2.5 kHz, about 3.33 kHz, about 5 kHz, about 6.66 kHz, about 7.5 kHz, about 9 kHz, about 10 kHz, about 25 kHz, about 33 kHz, about 50 kHz, about 66 kHz, about 75 kHz, about 100 kHz, about 200 kHz, or any value or subrange therebetween falling within the broad range from about 0 Hz to about 200 kHz.
Additional details regarding suitable energy source configurations (or equivalently, “reactors”) are provided herein with reference to
As shown in
Accordingly,
From inspection of
With continuing reference to
From inspection of
The above dissociation species' cross-sectional areas are a percentage of the total cross-sectional area versus impacting electron energy for carbon dioxide. Specifically, if an electron at 50 eV impacts a CO2 molecule, there is a 62.2% probability that CO2+ would be created. Moreover, these dissociation states have a necessary activation energy which needs to be overcome. In the case of CO2+ this required energy is 13.8 eV, again assuming presence/use of water to facilitate the various dissociation and conversion pathways.
In addition to the dissociation pathways (thick, solid black lines) shown in
Further still,
As discussed in greater detail herein, controlling the conditions of the plasma allows control over the specific dissociated species, and corresponding chemical reactions, that take place. Also disclosed herein are systems and techniques to tune the plasma energy distribution for optimum reaction pathways to be achieved. It shall be understood that the various features, components, and arrangements shown in
As will be appreciated by persons having ordinary skill in the art upon reading the present disclosure, certain tuning parameters depend from the input energy of the electrons. As one tuning example, the input energy of the electrons can derive from the nature (e.g., shape, duty cycle, etc.) of the pulsed power (e.g., AC and/or DC field(s)) in conjunction with the frequency, phase and propagation mode of the microwave radiation. Thus, reaction sequences are tunable, which tunability provides the means for efficient, low cost carbon removal.
For instance, and referring to
In addition, the extended length plasma region 404 may be controlled so as to facilitate fine-tuned control of radical generation and/or to facilitate introduction of additional materials. Specifically, and as shown, a first set of thermal plume energy sources 410 (such as ohmic heating device 412, dielectric heating device 414, phonon heating device 418) are positioned along the length of extended length plasma zone 402, whereas a second set of thermal plume energy sources 1023 (such as electromagnetic energy source 416, and/or an optional light energy source (not shown)) are positioned along the length of the extended length afterglow zone 430. Though not shown in
As shown, the length of extended length plasma zone 402 is sufficiently long so as to accommodate a three flow inlets 4081, 4082, and 4083 to provide material to the reactor 400.
In use, according to preferred aspects, flow inlets 4081 and 4082 may provide materials such as water and carbon dioxide to the reactor 400. Of course, additional or different materials may be provided via flow inlets 4081 and 4082 without departing from the scope of the presently disclosed inventive concepts.
According to still more aspects, third flow inlet 4083 can be configured to provide additional material into a FEWG, such as FEWG 505 shown in
The thermal plume energy sources 410 may be modular such that the various thermal plume energy sources can be positioned in any location along the FEWG. For example, the ohmic heating device 402 can be swapped with electromagnetic energy source 416. Moreover, such modularity can include signaling to/from one or more reactor controllers. One example of such a configuration is described hereinbelow.
Energy sources (such as ohmic heating device 412, dielectric heating device 404, electromagnetic energy source 416, phonon heating device 418, and/or an optional light energy source (not shown)) are coupled to a pan-reactor temperature and flow controller (not shown). The flow controller is in turn coupled with a bank of pan-reactor flow actuators coupled to flow inlets 4081, 4082, and 4083. Moreover, a series of temperature measurements are coupled to the pan-reactor temperature and flow controller and can control any one or more of the energy sources based at least in part on the temperature measurements. As such, temperatures within the reactor can be controlled to a fine degree across all zones, and within all regions of the reactor. Moreover, pulsing of the plasma field, e.g., by modulating parameters including the duty cycle and frequency, allows precise control of the plasma field.
According to additional aspects, a reactor such as reactor 400 enables atmospheric pressure plasma reduction chemistry facilitated using microwave radiation to generate pathways towards the energy efficient and low-cost removal of carbon from carbon dioxide. The formed carbon solids can be collected at various points of the reactor. The shown reactor (which may include an applicator such as waveguide 406 shown in
Accordingly,
In some aspects, the plasma plume may be extended such as is shown by the thermal afterglow that extends substantially through the shown extended length of the reactor 400. The extended length may be long enough, and the flow rate through extended length may be controlled so as to facilitate particle resonance times that allow for the re-nucleation and growth off of other grown platelets. Various energy sources (e.g., phonon heating device 418, electromagnetic energy source 416, optional light energy source (not shown), etc.) can be controlled in a manner that leads to a complex clustering of covalently bonded carbon-to-carbon connected nano platelets (e.g., such as shown in
There may be many zones that are defined by various corresponding lengths of the FEWG 505. Strictly as one example,
The ability to independently control the material flows while at the same time controlling the thermal plume energy sources along plasma column length leads to the ability to control the energy levels within the plasma region 502, which in turn leads to controllable selection of one or more reaction pathways that occur during conversion of the introduced materials into specific separated components. However, certain reaction pathways that occur during conversion of the introduced materials into specific separated components need a longer pathway and/or longer times being spent in the pathway and/or different temperature ranges along the pathway such that the plasma column length needs to be extended. This is accommodated by provision of the shown reaction zone 596 having an extended length. This is further accommodated by control of a set of thermal plume energy sources. In particular, temperature control of regions throughout the entire length of the FEWG 505 can be accommodated by selection, control, and positioning any of a variety of thermal plume energy sources. Strictly as an illustrative example, temperatures in plasma region 502 can be at least partially controlled by energy input1, while temperatures in afterglow region 503 can be at least partially controlled by energy input2, and while temperatures in any of the shown secondary zones can be at least partially controlled by additional thermal plume energy sources (not shown)
As such, the pathways and temperature contours through the FEWG 505 can be controlled, at least in part by selection and design of the FEWG, and at least in part by control of flows through the inlets, and at least in part by control of additional thermal plume energy inputs.
As used herein, the term ‘thermal plume’ refers to a region or regions within the reactor where plasma is formed and/or where chemical reactions are taking place. In exemplary aspects, two or more different, independently-controllable energy sources are provided in proximity to two or more regions within the reactor. Further, in exemplary aspects the average temperature in a first region (e.g., in plasma region 502) are higher than the average temperature in a second region (e.g., in afterglow region 503).
Control of the specific chemical reactions of the introduced materials can be facilitated at least in part by controlling the temperature contours in and between the plasma region and the afterglow region. Control of the plasma and neutral gas temperatures can allow for optimization of the flux of building precursors, such as C2 radicals. For example, too much C2 in a small region can lead to formation of amorphous carbon and additional graphene layers; however, smaller concentrations of C2 over a longer region lead to controlled growth of graphene platelets which is advantageous for growing longer platelets, typically sought after in many applications. Therefore, rather than having an intense source of C2 over a small distance, having a controlled concentration of C2 over a longer period is advantageous to growth kinetics.
For further materials processing within the reactor, the FEWG 505 can be fitted with any number of components that define secondary intra-reactor zones 515 (e.g., secondary zone1, secondary zone2, secondary zone3, secondary zone4, . . . secondary zoneN). Each secondary zone can be independently sized by in a first dimension (as shown) and/or in a second dimension (not shown) by sizing its corresponding component. In some aspects, the order of the secondary zones can be determined based on a particular desired pathway. For example, secondary zone1 might be followed by secondary zone3, followed by secondary zone2, followed by secondary zone4, etc. In some aspects, a selection of secondary zones can be determined based on a particular desired pathway. For example, secondary zone1 might be followed by secondary zone3, without any further secondary zones. In some aspects, components that define any one or more of the secondary zones can be removably attached to a previous component and/or successive component(s). For example, a component that defines secondary zone1 can be removably attached to the FEWG 505 (as shown), and/or a component that defines secondary zoneN can be removably attached to any other component, including the FEWG 505 itself.
The depiction of the apparatus of
The physical shape of length L1 and length L2 can be designed to cause a longer or shorter residence time as materials pass through length L1 and length L2 of the reactor. Moreover, the different and independently-controllable energy inputs (e.g., energy input1, energy input2) serve to control the temperatures and temperature variations that materials passing through length L1 and length L2 of the reactor are subjected to.
The two separate flow inlets (flow inlet 5081 and flow inlet 5082) permit two or more materials to be mixed, either before or after entering the FEWG 505. Mixtures of materials that include, for example, an active material component and an electrically conductive material component are useful in many applications such as electronics, automotive and aerospace. Such mixtures of materials often benefit from some underlying structure. For example, some structural composites utilize a fibrous web or weave of material with high tensile strength to provide strength in one or two directions. Such a fibrous web or weave of material is embedded in a matrix material with a lower elastic modulus to provide flexibility. Another application that benefits from an underlying structure within a mixture of active and conductive materials are battery electrodes, where the active material is an energy storage material and metallic or carbon-based particles provide electrical conductivity.
Related to the underlying structure of such mixtures, the surface area of the active material or the conductive component can also be important. A high surface area can provide a high interfacial area either between the active material and the conductive material, or upon which reactions can take place. In many applications, carbon allotropes are attractive for the conductive material component in such mixed structured materials because they can be produced with high electrical and thermal conductivities, and with high surface areas.
Conventional approaches to making such composite materials include growing structured carbon allotropes (e.g., nanostructured graphene) on a substrate, and then depositing the active material component into the pores of the structured carbon material. However, while high quality carbon allotropes require high growth temperatures (e.g., greater than 500° C.), many other materials cannot withstand these high processing temperatures. Accordingly, the zone-segregated reactor 501 can be configured with an extended length of the FEWG 505 such that chemical processing at lower temperatures within afterglow region 503 can be carried out. Additional energy inputs (e.g., energy input2) may be provided and controlled so as to maintain a temperature or temperature contours at least though length L2.
The configuration 600 is shown as an example. Additional or fewer components may be coupled together to achieve specific output quantities of a carbonaceous material. For example, in some implementations, ten or more reaction chambers may be coupled to one amplifier. In addition, multiple amplifiers may be combined using a power combiner (not shown in
Additional details regarding general approaches to powering multiple reaction chambers using a single microwave emitter can be found in U.S. Pat. No. 10,937,632, filed Aug. 14, 2017 and entitled “Microwave Chemical Processing Reactor,” the contents of which are herein incorporated by reference.
The reactor system 700A may be coupled to a control circuit and/or an amplifier, e.g. amplifier 602 of
The reaction chamber 732 of the reactor system 700A of
For example, in one implementation, the first pressure barrier 722 and/or the second pressure barrier 724 may be positioned within the waveguide 730 within the electromagnetic field-enhancing zone 731 as shown in
To activate and operate the reaction system 700A of
In this way, the microwave radiation 736 emitted by the amplifier 601 may be concentrated in the direction “A” within the electromagnetic field-enhancing zone 731 due to the incremental decrease of the cross-sectional area 750 along section length L0. The concentrated microwave radiation 736 may electromagnetically excite the supply gas 733 in the reaction zone 770 to ignite and thereby self-generate the plasma 737 within the plasma region 735. In addition, electrodes E1 and E2 are preferably located on opposite sides of the reaction zone 770, and used to generate electrical fields that influence chemical reactions taking place within reaction zone 770. Most preferably, in operation, an approximately 180 degree phase difference is maintained between electrodes E1 and E2, whether the corresponding field is generated using direct current or alternating current.
The plasma may include carbon-containing free radicals, such as methyl radicals 771, which may combine and recombine within the plasma region 735 when further electromagnetically excited by the microwave radiation 736. This combination and recombination of the methyl radicals 771 may include self-nucleation to produce the carbonaceous material 780. In this way, the carbonaceous material 780 may be output from the reaction chamber 732 by the outlet 738.
In one implementation, the reaction chamber may have an overall length L, which may be further sub-divided into multiple section lengths including LA, L0, LB, L2, and L1, any one or more of which may be reconfigured as shown in
In one implementation, the reaction chamber 732 may have a total length L, section length LA, and section length LB as shown in
One or more of the reaction chambers 732 of the reactor systems 700A-700B may be made from innately conductive materials and/or materials including electrically-conductive coated layers to, for example, facilitate emission of greater than 90% of the microwave radiation 736 emitted by the amplifier 601. Suitable example may include metals, metal-containing materials, metal with a conductive coating, ceramics, ceramic-containing materials, ceramic material with a conductive coating, stainless steel, stainless steel coated with a conductive layer including aluminum, nickel, silver, or a nickel-silver alloy, stainless steel having an aluminum liner, and/or a ceramic material coated with a conductive layer.
The waveguide 730 and/or the reaction zone 770 of the reaction chamber 732 of one or more of the reactor systems 700A-700B may facilitate generation of the plasma 737 within the plasma region 735. In this way, the reaction chamber 732 may not require an additional or separate waveguide and/or quartz reaction chamber to generate the plasma 737. In addition, configurations of the waveguide 730 and/or the reaction zone 770 facilitating ignition of the plasma 737 may enable processing of larger volumes of the supply gas 733 up to 1,000 liters (L). For example, in some implementations, the raw material 745, such as particulate matter suspended in an inert gas flow stream, and/or the supply gas 733 may be flowed through the inlet 760 and/or the supply gas inlet 734, respectively, at one or more approximate flow rate ranges, such as 1 slm (standard liters per minute) to 1,000 slm, and/or any smaller ranges within 1 slm and 1,000 slm
In other implementations, as the raw material 745 may be a liquid delivered into the reaction zone 770 of the reaction chamber 732 through the raw material inlet 760. The raw material 745 may be or include water, alkanes, alkenes, alkynes, aromatic hydrocarbons, saturated and/or unsaturated hydrocarbons, including alkanes, alkenes, alkynes, or aromatic hydrocarbons, ethanol, methanol, isopropyl alcohol (such as isopropanol), etc. In this way, the raw material may produce carbon and hydrogen as separated components. The flow rate of the raw material 745 in liquid-phase may be a percentage of the supply gas 733 flowed into the reactor, including from 0.001% to 1,000%, or from 0.001% to 100%, or from 0.001% to 10%, or from 0.001% to 1%, or from 0.001% to 0.1%, or from 0.01% to 1000%, or from 0.01% to 100%, or from 0.01% to 10%, or from 0.01% to 1%, or from 0.01% to 0.1%.
In some implementations, the raw material 745 may be a colloidal dispersion delivered through the raw material inlet 760 into the reaction chamber 732. For example, colloidal dispersions may include various unprocessed carbonaceous materials. Some examples of colloidal dispersions that can be used as the raw material 745 include one or more of solid particles from the Group 16, Group 14, Group 10, Group 9, Group 5, Group 2, Group 1, alloys thereof, mixtures thereof, and/or may be mixed with a liquid or a gas. Solid particles used in colloidal dispersions in the raw material 745 may be mixed with liquids, such as water, alkanes, alkenes, alkynes, aromatic hydrocarbons, saturated and unsaturated hydrocarbons, such as of alkanes, alkenes, alkynes, or aromatic hydrocarbons), ethanol, methanol, isopropyl alcohol, or mixtures thereof, such as a 50/50 mixture of ethanol/methanol.
In some aspects, the supply gas 733 and/or the raw material 745 may include one or more gas-phase substances, such as gases from Group 1 and Group 15-18, as well as inorganic compounds, such as a group 14 hydride. In this way, the raw material 745 may be processed within the reaction chamber 732 and produce the carbonaceous material 780, as well as one or more separated components including solid inorganic materials coated in organic materials, and composite materials with interlayers of organic/inorganic materials. The raw material 745, when prepared as a colloidal dispersion as presented above, may be flowed into the reaction chamber 732 as a percentage of the supply gas 733 flowed into the reactor, such as from 0.001% to 1000%, or from 0.001% to 100%, or from 0.001% to 10%, or from 0.001% to 1%, or from 0.001% to 0.1%, or from 0.01% to 1,000%, or from 0.01% to 100%, or from 0.01% to 10%, or from 0.01% to 1%, or from 0.01% to 0.1%.
In addition, the raw material 745 may be only a gas without particulate matter suspended in the gas. For example, in one implementation, the supply gas 733 may be an inert gas, such as argon, and the raw material may be a hydrocarbon-containing gas, such as C2H2, C2H4, C2H6. In addition, the raw material 745 may be methane (CH4), and thereby be separated into components including hydrogen and nanoparticulate carbon. In other implementations, the raw material 745 may be carbon dioxide (CO2) bubbled in water to yield separated components including oxygen, carbon, and water. In some aspects, the raw material 745 may be or include hydrogen sulfide (H2S) to yield separated components can include hydrogen gas and sulfur. In some implementations, the raw material 745 may not contain carbon dioxide. In some other implementations, the raw material can be a complex gas-based material, such as silane (SiH4), trimethylaluminum (TMA), trimethylgallium (TMG), glycidyl methacrylate (GMA), SF6, and/or other substances and/or materials commonly used in the semiconductor industry for deposition and etching of metals and dielectrics.
In some aspects, one or more of the reaction chambers 732 of the reactor systems 700A-700C of
The plasma region 735 may be tuned in terms of various physical parameters including temperature, pressure, and/or density of the plasma 737 by the microwave radiation 736 output by the amplifier 601 to correspondingly tune the carbonaceous material 780 in terms of physical properties or characteristics. For example, the control circuit 710 may control the amplifier 601 to pulse emission of the microwave radiation 736 into the reaction chamber 732. Additional details of tuning the microwave radiation 736 in microwave chemical processing systems are disclosed in U.S. Pat. No. 9,812,295, which is assigned to the assignee of the present application and incorporated by reference herein in its entirety.
In some implementations, an average energy in the plasma 737 may be controlled by the control circuit 710 by, for example, altering a pulse period and/or by selecting a pulsing frequency to achieve a desired plasma energy. In addition, or the alternative, the average energy of the plasma 737 may be controlled by adjusting the duty cycle of the control signal 715. For example, time-averaged input power and the pulse period of the amplifier 601 may both be held constant, while the duty cycle of the control signal 715 may be varied. In some aspects, a shorter duty cycle may increase a magnitude of the power of the microwave radiation 736 emitted into the reaction chamber 732. In this way, a relatively low amount of power may be used to generate the carbonaceous material 780 at rates that may not be feasible at similar power settings and/or with continuous waveforms of the microwave radiation 736.
In some implementations, reaction pathways occurring within the plasma 737 in the plasma region 735 may be selected by controlling time-averaged power input into the plasma 737. For example, holding the duty cycle and pulse frequency of the amplifier 601 while increasing power input into the amplifier may cause an overall energy level of the plasma 737 to increase. In another example, more effective emission of the microwave radiation 736 into the reaction chamber 732 may also cause overall energy levels of the plasma 737 to increase at a constant duty cycle and pulse frequency, etc. In one implementation, the supply gas 733 and/or the raw material 745 may include methane, which may be separated into hydrogen and nanoparticulate carbon by the gas-solid separator 795. Generally, 4-6 eV may be required to dissociate methane, which is undesirable in circumstances where energy levels of the plasma 737 may settle at approximately 1.5 eV after an initial ignition energy spike. The control circuit 710 may cause the amplifier 601 to pulse emission of the microwave radiation 736 to maintain average plasma energy at relatively higher levels.
The plasma 737 in the plasma region 735 of the reaction chamber 732 may be a non-thermal equilibrium plasma and thereby constant change one or more physical or chemical parameters including temperature to allow the microwave radiation 736 to penetrate deeper and/or more fully into the plasma 737. For example, in some implementations, average energy of the plasma 737 over an entire pulse period may be from 0.9 eV to 20 eV, or from 0.9 to 10 eV, or from 1.5 eV to 20 eV, or from 1.5 eV to 10 eV, or greater than 0.9 eV, or greater than 1.5 eV. Energy of the plasma 737 may be tuned based on preferences of the carbonaceous material 780 as controlled by the control circuit 710. For example, the control circuit 710 may cause the amplifier to emit the microwave radiation 736 at one or more defined frequencies including 915 MHz, 2.45 GHz, or 5.8 GHz. The control circuit 710 may enable a pulse frequency from 500 Hz to 1000 kHz, or from 1 kHz to 1000 kHz, or from 10 kHz to 1000 kHz, or from 40 kHz to 80 kHz, or from 60 kHz to 70 kHz, or greater than 10 kHz, or greater than 50 kHz, or greater than 100 kHz.
The amplifier 601 may emit the microwave radiation 736 as a continuous wave or in a pulsed manner with a time-average power from 1 to 100 kW, or from 1 kW to 500 kW, or from 1 kW to 1 MW, or from 10 kW to 5 MW, or greater than 10 kW, or greater than 100 kW, or greater than 500 kW, or greater than 1 MW, or greater than 2 MW. In some aspects, the pulse period has a first duration where the microwave power is on, and a second duration where the microwave radiation 736 is off or at a lower power than during the first duration. The second duration can be longer than the first duration. The optimal duty cycle for a given system depends on many factors including the microwave power, pulse frequency, and pulse shape. The duty cycle (such as the fraction of the pulse period where the microwave radiation 736 is on, expressed as a percentage) can be from 1% to 99%, or from 1% to 95%, or from 10% to 95%, or from 20% to 80%, or from 50% to 95%, or from 1% to 50%, or from 1% to 40%, or from 1% to 30%, or from 1% to 20%, or from 1% to 10%, or less than 99%, or less than 95%, or less than 80%, or less than 60%, or less than 50%, or less than 40%, or less than 30%, or less than 20%, or less than 10%.
The reaction chamber 732 may or may not include a dielectric barrier, such as a quartz window. During operation of reactor systems with dielectric barriers, intensity of microwave radiation emitted through the dielectric barrier may be reduced. In this way, lower amounts of microwave radiation may be available to electromagnetically excite supply gas, resulting in the ignition of correspondingly lower quantities of plasma. In addition, the parallel orientation of delivery of supply gas from the supply gas inlet 734 with emission of the microwave radiation 736 may prevent against unwanted build-up of byproducts on various internal surfaces of the reaction chamber 732. In some aspects, the reaction chamber 732 may include a plasma backstop 746, which may prevent plasma in the plasma region 735 from backflowing toward the amplifier 601 and/or the supply gas inlet 734. The plasma backstop 746 may be formed from a ceramic or as a metallic filter including holes, which may permit passage of the microwave radiation 736 while preventing more than 80% of plasma from backflowing as so described.
The raw material inlet 760 maybe positioned as shown in
In other implementations, the unconverted greenhouse gases 782 may be recycled back into the reaction chamber 732 through a conduit 785 into the recycled supply gas inlet 790 to be used as the precursor gas 784. Recycling of the unconverted greenhouse gases 782 may add energy to the plasma 737, and may also thermally crack the raw material. For example, in one implementation, the unconverted greenhouse gases 782 can be 2 standard liters per minute (slm) to 10 slm of hydrogen gas (H2), which may be recycled back into the waveguide 730 of the reaction chamber 732 through the conduit 785. In this way, the reaction chamber 732 may output a total of 150 to 200 slm of H2. In addition, or the alternative, an amount less than the entirety of the unconverted greenhouse gases 782 may be recycled to meet specific output requirements of the reaction chamber 732.
For example, in one implementation, approximately 50% of the 2-10 slm of H2 may be recycled back to the waveguide 730 as shown, with the balance output from the gas-solid separator 795. In other implementations, the amount or proportion of the unconverted greenhouse gases 782 may be based on the identity of the supply gas 733. For example, in one implementation, the supply gas 733 may be hydrogen gas and the raw material 745 may be methane (CH4). In this way, the methane may be exposed to and electromagnetically excited by the microwave radiation 736 emitted by the amplifier 601 as controlled by the control circuit 710. The plasma 737 may be a hydrogen-based plasma generated in the plasma region 735 of the reaction chamber 732 based on excitation of some of the methane by the microwave radiation. Remaining portions of the methane may be cracked upon exposure to the microwave radiation 736 to generate the methyl radicals 771 and hydrogen gas. In this way, at least some of the hydrogen produced from cracking the methane may be recycled as the unconverted greenhouse gases 782 and form the precursor gas 784 input into the recycled supply gas inlet 790. This recycled gas may then be used to further crack methane prevalent in the plasma region to enhance operational efficiency of the reaction chamber 732. In addition, recycled hydrogen may be at a relatively high temperature, thereby warming methane in the plasma region and requiring lower energy input from the microwave radiation 736.
Instead, and one major factor contributing to the scalability and simplicity of the presently described inventive arc-discharge based dissociation approaches, the reactor 700C requires a reaction chamber 732 configured (e.g., as otherwise described herein) to contain a plasma 737 within a plasma region 735 and control environmental conditions within the reaction chamber 732 to facilitate desired physical (dissociation) and chemical (reconstitution) reactions and dictate the composition and morphology of desired output materials, preferably including hydrogen and various forms of carbon as described herein.
The plasma, rather than being generated using a microwave source, amplifier, waveguide, etc. as described hereinabove regarding
In response to appropriate control signal(s) 715 received from a control circuit 710 operatively coupled to the power supply 760 generates high current (e.g. >100 A) arcs 765 in the region of the reaction chamber 732 between or within the ceramics 750 and, in combination with components of the supply gas 733 and/or raw material 745 (preferably including methane), to ignite plasma 737 within a plasma zone 735 of the reaction chamber 732. The plasma 737 is characterized by a temperature in a range from about 6,000 K to about 20,000 K, which may be tuned to exhibit any temperature therebetween in order to facilitate formation and recovery of desired output material compositions and morphologies.
The wide tunability of this plasma allows a precise control over morphology (characteristics) of products which leads to wider applicability of the reactor. On the other side, the wide tunability of plasma temperature enables 100% conversion efficiency of various feedstock compositions, including different gas species, different concentrations thereof, different flow rate of feedstock, and/or different pressures, the latter of which is preferably and advantageously maintained at about atmospheric pressure, e.g., in a range from about 0.5 atm to about 1.5 atm, including any value(s) or subrange(s) therebetween, such as about 0.6 atm, about 0.66 atm, about 0.7 atm, about 0.75 atm, about 0.8 atm, about 0.9 atm, about 0.95 atm, about 0.99 atm, about 1.1 atm, about 1.2 atm, about 1.25 atm, about 1.33 atm, about 1.4 atm, etc., and any range between these values or other values falling within the broad range of about 0.5 atm to about 1.5 atm, as would be understood by those having ordinary skill in the art upon reading the present disclosures.
Moreover, in select approaches the electrodes used to generate the plasma may be, and preferably are, characterized by a hollow configuration. Advantageously, a hollow electrode plasma torch such as shown in
Accordingly, in an exemplary implementation, approximately 100% conversion efficiency was achieved using an arc discharge dissociating reactor and methane supply gas, by tuning current and eliminating bypass flow within the reaction chamber 732. This exemplary embodiment leads to high yield of desired carbon species, as well as zero production/retention of methane during dissociation. Accordingly, in some approaches the gas mixture output through outlet 738 to the gas-solid separator 795 may exclude one or more input supply gas components, preferably at least including methane, carbon monoxide, carbon dioxide, or combinations thereof.
To facilitate desired chemical reactions occurring in the reaction chamber 732 (e.g., reactions that produce desired species and/or morphologies of output material), optional electrode(s) E1, E2 may be operatively coupled to the reaction chamber 732, as well as to a suitable power supply such as voltage generator 770. As described with reference to
One particular advantage of working with either or both AC and DC electric fields is the reliability of this plasma source operating with various power sources. AC power sources and fields are preferable due to the ability to alternatively change polarity of the electrodes, which can improve the life time of electrodes.
With respect to dissociation of methane into solid carbon and gaseous hydrogen using arc discharge reactors, however, there is no general preference between AC and DC from the perspective of controlling the underlying chemical reactions, since the magnitude of the field can be same for either power source.
On the other hand, controlling the pulse operation can provide additional control over conversion of species within the plasma and electric field, since in pulse mode, at same total power consumption, the peak strength of the field is higher. This controllability desirably enables creation of unique feature within the resulting product which can be only achieved in a very high field strength or plasma energy. For instance, according to various embodiments, and particularly with regard to implementations utilizing arc discharge reactors, a very high field strength and/or plasma energy may be considered to include field strength(s) and plasma energies within the upper 50% of suitable ranges disclosed herein. In more embodiments, a very high field strength and/or plasma energy may be considered to include field strength(s) and plasma energies within the upper 66% of suitable ranges disclosed herein. In still more embodiments, a very high field strength and/or plasma energy may be considered to include field strength(s) and plasma energies within the upper 75% of suitable ranges disclosed herein. In still yet more embodiments, a very high field strength and/or plasma energy may be considered to include field strength(s) and plasma energies within the upper 90% of suitable ranges disclosed herein. In still yet further embodiments, a very high field strength and/or plasma energy may be considered to include field strength(s) and plasma energies within the upper 95% of suitable ranges disclosed herein. Of course, as will be appreciated by those having ordinary skill in the art upon reading the instantly disclosed inventive concepts, “very high” field strength and/or plasma energy may include values or ranges between the foregoing exemplary values, again anywhere within a broad range from about 50% to about 100% of the suitable field strength and/or plasma energy as described elsewhere herein.
In addition, it shall be understood that a given exemplary arc discharge dissociating reactor 700C may include multiple arc discharge heat sources (also referred to in the art as “torches”), which advantageously allows for increased plasma volume within the reaction chamber 732, and correspondingly an increased amount of supply gas 733 and/or raw material 745. In some approaches, the output materials may pass through the plasma region 735 and be fed to a processing and recycling stage, e.g., including an outlet 738 and gas-solid-separator 795, to facilitate further processing of unconverted greenhouse gases 782 and/or precursor gases 784, e.g. by reintroducing the gas mixture back into the reaction chamber 732 via a recycled supply gas inlet 790.
For example, and referring now to
As shown in
Moreover, though not shown in
Referring now to
Now, returning to discussion of the plasma zone, the plasma zone in this configuration supports a large volume plasma that is characterized as having a portion of the large volume where a first greenhouse gas such as GHG1 (e.g., CO2) and a second green-house gas GHG2 (e.g., CH4) are subjected to sufficient energies (e.g., at least at the shown point of ignition) such that the gasses dissociate into their constituent elemental components (e.g., carbon, oxygen, hydrogen, nitrogen, sulfur, etc., shown as D1, D2, etc.). During, or at the end of the lifetime of an atom or molecule in a dissociated state, a finite number of molecular species are predictable, and in some cases are formed in situ within the reactor. For example, a single dissociated carbon atom might combine with a single dissociated oxygen atom to form a carbon-monoxide molecule. In some cases the dissociated atoms/molecules recombine in varying ratios back into the greenhouse gasses. To control the formation of unwanted species, and more specifically, to keep the dissociated atoms/molecules separated for a time as they move downstream through the plasma, electromagnetic forces are introduced at various lengths of the reactor. Such electromagnetic forces are applied across a sufficiently long dimension of the reactor tube, and for a sufficiently long duration such that the dissociated atoms/molecules cool to sub-plasma temperatures. This in turn results in the carbon atoms being cool enough so as not to recombine with the gasses (e.g., oxygen, hydrogen) and moreover this in turn results in the carbon atoms self nucleating into carbon allotropes. Some allotropes have a slight amount of attractive forces such that solid carbons agglomerate (e.g., in the shown solid carbon agglomeration zone 12433) as well as in the cooling zone 12363. The specific characteristics of the aforementioned self-nucleating as well as the specific characteristics of the agglomerations can be controlled in secondary zone1 and secondary zone2 respectively.
In some deployments, the reactor is configured with a solid carbon functionalization zone 1232 such that the solid carbons can be functionalized by being subjected to selected gasses (e.g., gas G1, gas G2). The flow of such selected gasses can be controlled by the shown valves. More specifically, the flow of such selected gasses into the reactor tube can be controlled in part by the shown valves, and in part by a back pressure controller 1244. In any of a wide range of combinations of inflows and backpressures, solid carbons as well as the selected gasses (e.g., oxygen, hydrogen, gas G1, gas G2, etc.) flow into outlet 738 where they are then separated via gas/solid separator 795. Gasses are routed to post processing for abatement and/or release, while the solids are routed to a capture facility.
Now returning to the discussion of the gliding arc, and more specifically, regarding the function of the shown gliding arc electrode adapter 1240, it is known that a gliding arc discharge is particularly efficient for generating a non-equilibrium plasma, which in turn is particularly efficient for dissociation of CO2 as well as other greenhouse gasses.
A gliding arc discharge (GAD) in a plasma reactor occurs due to arcing between two diverging electrodes and results in a non-equilibrium plasma being generated. Such a plasma reactor can operate at atmospheric pressure and in some cases, the plasma exhibits high electron density, making it suitable for CO2 and methane dissociation.
Electrodes: In some embodiments, a gliding arc reactor consists of two or more diverging electrodes. These electrodes create the electric field necessary for the arc to form. A gas nozzle (not shown so as not to occlude the GAD apparatus) injects the carrier gas (in this case, CO2) into the reactor.
In a repeating cycle, the arc initiates at the shortest electrode gap and is then pushed downstream by the gas stream until it extinguishes. The cycle then repeats.
Voltage: The power supply should provide a voltage suitable for arc initiation. Typically, gliding arcs operate with voltages in the range of several kilovolts.
Frequency: The AC frequency affects the arc behavior. Common frequencies range from near DC to tens of kilohertz range.
Waveform: The voltage waveform can be sinusoidal or pulsed, depending on the specific application.
Arc Initiation: The gliding arc ignites at the narrowest gap between the diverging electrodes. The voltage required for arc initiation depends on factors like gas composition, electrode material, and gap distance. Generally, a few kilovolts (e.g., 2-5 kV) are sufficient for arc formation. However, the exact voltage range depends on the specific reactor design and gas conditions.
Arc Lifetime: The average arc lifetime is typically around 2 milliseconds. This duration includes the entire cycle of arc breakdown, elongation, disappearance, and re-breakdown.
Modulating Duration: To control the arc duration, a resistive-capacitive (RC) circuit connected to the power supply can be deployed. The arc's behavior is influenced by adjusting the RC time constant.
A gliding arc electrode, driven by an appropriate power supply, can dissociate CO2 into solid carbon and oxygen and/or methane into solid carbon and hydrogen. The arc's characteristics, voltage range, and duration play crucial roles in achieving efficient dissociation. By carefully configuring the power supply and controlling the RC circuit, one can tailor the gliding arc's behavior to your desired outcomes.
Advantages of using an arc discharge dissociating reactor 700C or gliding arc discharge dissociating reactor as shown in
For instance, regarding simplicity, first as noted above the illustrative arc discharge dissociating reactor does not require any waveguide or other related complicated components, making the system less prone to breakdown and requiring less extensive or less frequent maintenance procedures. In addition, DC power supply technology is a well-established field with reliable power sources having a wide range of operating characteristics readily available on the market. As a result of the foregoing practical considerations, arc discharge plasma reactors can generate plasma having desired characteristics with much greater stability, improved sustainability of operations, lower power requirements, and other advantages relating to simplicity of the system (even compared to microwave reactor configurations as described herein).
Atmospheric pressure plasma conditions have been demonstrated utilizing microwave radiation superimposed upon a modulated electric field. The superposition of microwave radiation serves to increase electron density and lower the requirements for Paschen's breakdown (dissociation) due to the modulated electric field. Atmospheric pressure plasma formation from gases including argon, nitrogen, carbon dioxide, oxygen, and helium has been investigated experimentally and some configurations and tunings achieve dissociation fractions approaching 0.95.
An electron impacting a molecule at a given energy (eV) has an effective cross-sectional area for dissociation. For instance, a 100 eV electron impacting a nitrogen gas molecule will have an effective dissociation cross-section of 2.19E−16 cm2. If the dissociating molecule has multiple dissociation states, such as depicted in the two charts of
As can be seen from
Referring now to the lower portion of
From the plots shown in
As shown and discussed hereinabove, particularly with reference to
The materials shown in
The schematic shows a molecular flow progression from consumption of fossil fuels to generation of non-polluting resultants. Operation of components of the producer-consumer ecosystem facilitate practice of methods for high-efficiency solid carbon capture for clean fossil fuel power production. Specifically, the component labeled as the carbon dioxide processing facility 1030 includes piping or other means for directing a stream of exhaust from a power plant 1004 into a carbon dioxide processing facility 1030 having a microwave reactor therein. Optionally, water may be present in the Exhaust, and/or water may be provided to the carbon dioxide processing facility 1030 from a supplemental H2O Source. The microwave reactor is configured to dissociate the carbon dioxide of the exhaust into gaseous oxygen and particulate carbon solids 1032. The carbon dioxide processing facility 1030 is configured for (1) releasing gaseous oxygen and water into the environment; and (2) is further configured for (2) capturing the particulate solid carbon into a containment vessel.
In some cases, the carbon dioxide processing facility 1030 receives outputs (e.g., water vapor H2O) from the power plant 1004, and methane decarbonization refinery 1006 receives outputs (e.g., methane) from an oil refinery 1002. As shown, the oil refinery 1002 and/or the methane decarbonization refinery 1006 also produces heavy petroleum products 1022 (e.g., diesel oil, gasoline, petroleum coke, etc.) and hydrogen 1024. In some cases, the methane refinery is configured to produce powdered carbon products 1026.
As depicted, all of the molecules of the inputs and outputs are consumed (e.g., to produce electricity), or are released a clean gaseous oxygen, or are captured as solid particulate carbon. In some ecosystems, the oil refinery produces many products other than the shown methane and heavy petroleum products 1022. For example, the oil refinery may produce other products such as naphtha and butane. Further, the oil refinery may produce by-products (e.g., H2S) that is processed in additional downstream facilities (e.g., in a sour water steam stripper).
More illustrative information will now be set forth regarding various optional architectures and uses in which the foregoing method may or may not be implemented, per the desires of the user. It should be strongly noted that the following information is set forth for illustrative purposes and should not be construed as limiting in any manner. Any of the following features may be optionally incorporated with or without the exclusion of other features described.
As shown in
With continuing reference to
In operation 1106 of
Method 1100 also includes operation 1108, where solid carbon is generated via the chemical reactions. As described in greater detail hereinabove, efficiently generating solid carbon involves the use of water as an input material, as well as fine tuning of the plasma and/or electric field to generate appropriate thermal and/or kinetic conditions for the chemical reactions to occur. For instance, optimal parameters reduce the activation energy required for dissociation and facilitate creation of desired species for participation in subsequent chemical reactions to form the desired final product, e.g., solid carbon in various forms described herein.
In operation 1110, method 1100 involves outputting the solid carbon from the reactor. The solid carbon may be output in any suitable manner that would be appreciated by a person having ordinary skill in the art upon reading the instant disclosure. Preferably, prior to output, the solid carbon is separated from other raw materials (e.g. gases), for example using a gas-solid separator, and is output to an appropriate receptacle.
According to various approaches, method 1100 may include additional or alternative operations and/or features than described immediately above.
For instance, in one aspect facilitating the chemical reactions using the electric field may include modulating a frequency and/or a duty cycle of a control signal generated by a control circuit coupled to the reactor. Moreover, the chemical reactions may include a first reaction configured to generate solid carbon from carbon monoxide and water in a single step; and a second reaction configured to generate solid carbon from carbon monoxide and water in two steps.
Preferably, but by no means necessarily, the carbon dioxide and the water are components of an effluent exhaust stream received from a power generation facility coupled to the reactor, and generating the solid carbon reduces a carbon footprint of the power generation facility.
In various approaches, the solid carbon may be or include one or more materials such as: carbon black, carbon nano-onions (CNOs), necked CNOs, carbon nanospheres, graphite, pyrolytic graphite, graphene, graphene nanoparticles, graphene platelets, fullerenes, hybrid fullerenes, single-walled nanotubes, multi-walled nanotubes, and combinations thereof.
With continuing reference to method 1100, and as noted above, it is advantageous to remove oxygen from the reactor to avoid recombination of various dissociated species therewith in pathways that do not lead to production of solid carbon (or other desired product).
In a related approach, and referring now to
In operation 1202, method 1200 includes receiving, at a dissociating reactor, a supply gas including methane. The methane in the supply gas may originate from any source, such as atmospheric methane, methane from agricultural sources (e.g. bovine emissions), industrial sources, environmental sources (e.g., thawing tundra or other historically “frozen” sources of methane), etc. according to various embodiments. The methane may be captured and included in the supply gas according to any known techniques that will be appreciated by those having ordinary skill in the art upon reading the present disclosure.
In operation 1204, at least some of the methane is dissociated into one or more dissociated species using the dissociating reactor. The dissociating reactor is accordingly configured to dissociate the methane into the dissociated species, preferably using a plasma generated using one or more arc discharge heat sources as described herein. Moreover, characteristics of the plasma, including duty cycle, temperature, pressure, frequency, energy, etc. as would be appreciated by those having ordinary skill in the art upon reading the present disclosure, may be tuned or controlled as described herein to preferentially or selectively drive the dissociation of methane into solid carbon and hydrogen gas (or precursors thereof, which may be recombined into solid carbon and/or hydrogen gas in whole or in part via chemical reactions taking place within the volume of the reactor, as described herein and referenced in operation 1206 below), rather than other dissociated species that may be generated upon exposing methane to a plasma, particularly an arc discharge plasma, although the inventive concepts presented herein shall be understood as including embodiments where dissociated species other than solid carbon, hydrogen gas, and precursors thereof, are generated within the volume of the reactor.
Turning now to operation 1206, method 1200 includes controlling, using a pulsed electric field generated within a volume of the dissociating reactor, one or more chemical reactions involving some or all of the dissociated species to generate one or more desired output species. In preferred approaches, the desired output species include solid carbon and hydrogen gas. More preferably, the desired output species consist of solid carbon and hydrogen gas. The solid carbon may include various allotropes, isotopes, etc. of carbon, and preferably includes one or more of: carbon black, carbon nano-onions (CNOs), necked CNOs, carbon nanospheres, graphite, pyrolytic graphite, graphene, graphene nanoparticles, graphene platelets, 3D graphene, fullerenes, hybrid fullerenes, single-walled nanotubes, and multi-walled nanotubes, or any permutation or combination thereof, according to select implementations. The pulsed electric field may be generated and modulated as described hereinabove, e.g., with reference to
With continuing reference to method 1200, operation 1208 involves collecting some or all of the one or more desired output species. Collection may be performed according to any suitable technique and using any suitable components, mechanisms, devices, etc. as described herein or as would be understood as suitable by a person having ordinary skill in the art upon reading the instant disclosure. In some approaches, collection may be preceded by a separation operation to segregate desired species from undesired species, to separate gases from solids, or otherwise isolate different output species from one another.
The presently described invention may be embodied as a system, a method, a composition of matter, or combinations thereof, according to various aspects. These aspects may be combined in any suitable manner, and various permutations of features disclosed herein may be included (or excluded) according to different implementations, without departing from the scope of the invention. Exemplary inventive concepts presented in this description include the following, without limitation.
In one aspect, a method for producing solid carbon from carbon dioxide gas and water includes: receiving carbon dioxide and water in a reactor configured to generate a plasma; dissociating the carbon dioxide and the water using the plasma to form one or more dissociated species; exposing the dissociated species to an electric field configured to facilitate one or more chemical reactions; generating solid carbon via the chemical reactions; and outputting the solid carbon from the reactor. The system may additionally or alternatively include any one or more of the following operations/features, according to various approaches. In one approach, The system includes separating the solid carbon from one or more byproducts of dissociating the carbon dioxide and the water, and/or from one or more byproducts of the one or more chemical reactions. In another approach, facilitating the chemical reactions using the electric field comprises modulating a frequency and/or a duty cycle of a control signal generated by a control circuit coupled to the reactor. Moreover, the chemical reactions may include: a first reaction configured to generate solid carbon from carbon monoxide and water in a single step; and/or a second reaction configured to generate solid carbon from carbon monoxide and water in two steps. Generating the solid carbon using the plasma involves causing electron(s) to impact the carbon dioxide and the water, and optionally corresponding dissociated species thereof. Preferably, the carbon dioxide and the water are components of an effluent exhaust stream received from a power generation facility coupled to the reactor. More preferably, generating the solid carbon reduces a carbon footprint of the power generation facility. The solid carbon may include one or more materials selected from the group consisting of: carbon black, carbon nano-onions (CNOs), necked CNOs, carbon nanospheres, graphite, pyrolytic graphite, graphene, graphene nanoparticles, graphene platelets, fullerenes, hybrid fullerenes, single-walled nanotubes, and multi-walled nanotubes. In some approaches, the plasma is characterized by an energy of approximately 100 electron volts (eV), and/or a frequency in a range from about one gigahertz to about five gigahertz. The system may include generating an electric field, e.g., an alternating current and/or a pulsed direct current (DC) field, within the plasma zone and/or the reaction zone. The electric field may be generated using a plurality of electrodes coupled to the reactor, preferably positioned on opposite sides of the plasma zone. The electrodes may be characterized by an approximately 180-degree phase difference. The electric field may be characterized by having a variable strength along a length of the reactor, e.g., due to differing distance between respective electrode(s) and the plasma zone along the length of the reactor. Oxygen may be removed from the reactor during performance of The system, in order to avoid recombination with other species to form products other than the desired output, e.g., solid carbon, sulfur, silicon, etc.
According to another aspect, a system includes a waveguide comprising a plasma zone extending along a length of the first waveguide; a microwave energy source coupled to the waveguide; a first flow inlet configured to flow carbon dioxide gas into the plasma zone; and a gas-solid separator system coupled to the microwave plasma reactor. The microwave energy source is configured to propagate microwave energy into the waveguide; and the microwave energy is configured to generate a plasma within the plasma zone. The plasma within the plasma zone is configured to dissociate the carbon dioxide gas into a plurality of components including oxygen gas and solid carbon particles. Dissociation using the plasma involves causing electron(s) to impact the carbon dioxide and the water, and optionally corresponding dissociated species thereof. The gas-solid separator (GSS) system is configured to receive the plurality of components. Additionally or alternatively, the system may include any combination or permutation of the following components/features, according to various aspects of the inventive concepts presented herein. For instance, the waveguide preferably also includes a reaction zone configured to facilitate one or more chemical reactions for converting the carbon dioxide into the plurality of components. Optionally, an electromagnetic energy source, an ohmic heating device, a dielectric heating device, and/or a phonon heating device may be coupled to the plasma zone, wherein temperature contours in the plasma zone are controlled using the ohmic heating device, the dielectric heating device, the microwave energy device, and/or the phonon heating device. The waveguide may optionally include a second flow inlet configured to deliver carbon dioxide into the plasma zone, and/or a third flow inlet configured to deliver one or more additional materials into a reaction zone of the waveguide, where the one or more additional materials are configured to functionalize the carbon dioxide and/or the plurality of components. Preferably, the plurality of components includes solid carbon. More preferably, the carbon dioxide gas is provided to the first flow inlet from an effluent exhaust stream of a power generation facility. The gas-solid separator (GSS) may be configured to separate gaseous components from the solid carbon particles prior to outputting the solid carbon particles. The system may additionally include at least one receptacle coupled to the gas-solid separator system, where the at least one receptacle is configured to receive the solid carbon particles. The system also may include a plurality of electrodes coupled to the waveguide, wherein the plurality of electrodes is configured to cooperatively generate either or both of an alternating current (AC) field and a pulsed direct current (DC) field. Whether generated using AC or DC, an approximately 180 degree phase difference is preferably maintained between the electrodes. The first flow inlet may be configured to flow the carbon dioxide gas into the plasma zone in a direction parallel to the waveguide.
According to yet another aspect, a system includes a plurality of reaction chambers such as the system described hereinabove. The plurality of reaction chambers are coupled (e.g., in parallel or in series), directly or indirectly, to at least one microwave energy source, at least one amplifier, and at least one receptacle. Each reaction chambers includes a waveguide coupled to the microwave energy source, and each waveguide independently comprises: a plasma zone configured to generate a plasma in response to the microwave energy; at least one inlet configured to deliver raw material into the plasma zone; and an outlet configured to output a powder based on the raw material. Preferably, each reaction chambers comprises or is part of a klystron. The plasma preferably causes electron(s) to impact carbon dioxide and water within the reaction chamber(s), in turn causing dissociation thereof, and optionally the dissociation involves causing electron(s) to impact dissociated species of carbon dioxide and/or water. It shall be understood that systems including a plurality of reaction chambers may include any combination or permutation of components/features/capabilities described hereinabove regarding a single reaction chamber.
According to still yet another aspect of the presently described inventive concepts, a composition of matter includes a carbonaceous material having physical characteristics of being formed from dissociation of carbon dioxide and water using a plasma and an electric field. Preferably, the dissociation is driven by electron(s) impacting chemical species present in a reaction chamber configured to generate a (e.g., microwave) plasma.
The physical characteristics of being formed from dissociation of carbon dioxide and water using at least one plasma may include the carbonaceous material comprising carbonaceous aggregates characterized by a principal dimension having a length in a range from about 1 micron to about 1000 microns. The physical characteristics of being formed from dissociation of carbon dioxide and water using at least one plasma may additionally or alternatively include the carbonaceous material comprising one or more materials selected from the group consisting of: carbon black, carbon nano-onions (CNOs), necked CNOs, carbon nanospheres, graphite, pyrolytic graphite, graphene, graphene nanoparticles, graphene platelets, fullerenes, hybrid fullerenes, single-walled nanotubes, and multi-walled nanotubes. The plasma conferring the physical characteristics is characterized by a frequency in a range from about one gigahertz to about five gigahertz. The plasma may be a microwave plasma; and/or the electric field is either an alternating current (AC) field or a pulsed direct current (DC) field, though AC fields and DC fields may be used in combination, according to various aspects of the invention.
It should be understood that the arrangement of components illustrated in the Figures described are exemplary and that other arrangements are possible. It should also be understood that the various system components (and means) defined by the claims, described below, and illustrated in the various block diagrams represent logical components in some systems configured according to the subject matter disclosed herein.
For example, one or more of these system components (and means) may be realized, in whole or in part, by at least some of the components illustrated in the arrangements illustrated in the described Figures. In addition, while at least one of these components are implemented at least partially as an electronic hardware component, and therefore constitutes a machine, the other components may be implemented in software that when included in an execution environment constitutes a machine, hardware, or a combination of software and hardware.
More particularly, at least one component defined by the claims is implemented at least partially as an electronic hardware component, such as an instruction execution machine (e.g., a processor-based or processor-containing machine) and/or as specialized circuits or circuitry (e.g., discreet logic gates interconnected to perform a specialized function). Other components may be implemented in software, hardware, or a combination of software and hardware. Moreover, some or all of these other components may be combined, some may be omitted altogether, and additional components may be added while still achieving the functionality described herein. Thus, the subject matter described herein may be embodied in many different variations, and all such variations are contemplated to be within the scope of what is claimed.
In the description above, the subject matter is described with reference to acts and symbolic representations of operations that are performed by one or more devices, unless indicated otherwise. As such, it will be understood that such acts and operations, which are at times referred to as being computer-executed, include the manipulation by the processor of data in a structured form. This manipulation transforms the data or maintains it at locations in the memory system of the computer, which reconfigures or otherwise alters the operation of the device in a manner well understood by those skilled in the art. The data is maintained at physical locations of the memory as data structures that have particular properties defined by the format of the data. However, while the subject matter is being described in the foregoing context, it is not meant to be limiting as those of skill in the art will appreciate that various of the acts and operations described hereinafter may also be implemented in hardware.
To facilitate an understanding of the subject matter described herein, many aspects are described in terms of sequences of actions. The description herein of any sequence of actions is not intended to imply that the specific order described for performing that sequence must be followed. All methods described herein may be performed in any suitable order unless otherwise indicated herein or otherwise clearly contradicted by context.
The use of the terms “a” and “an” and “the” and similar referents in the context of describing the subject matter (particularly 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. 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. Furthermore, the foregoing description is for the purpose of illustration only, and not for the purpose of limitation, as the scope of protection sought is defined by the claims as set forth hereinafter together with any equivalents thereof entitled to. The use of any and all examples, or exemplary language (e.g., “such as”) provided herein, is intended merely to better illustrate the subject matter and does not pose a limitation on the scope of the subject matter unless otherwise claimed. The use of the term “based on” and other like phrases indicating a condition for bringing about a result, both in the claims and in the written description, is not intended to foreclose any other conditions that bring about that result. No language in the specification should be construed as indicating any non-claimed element as essential to the practice of the invention as claimed.
The aspects described herein included the one or more modes known to the inventor for carrying out the claimed subject matter. Of course, variations of those aspects will become apparent to those of ordinary skill in the art upon reading the foregoing description. The inventor expects skilled artisans to employ such variations as appropriate, and the inventor intends for the claimed subject matter to be practiced otherwise than as specifically described herein. Accordingly, this claimed subject matter includes all modifications and equivalents of the subject matter recited in the claims appended hereto as permitted by applicable law. Moreover, any combination of the above-described elements in all possible variations thereof is encompassed unless otherwise indicated herein or otherwise clearly contradicted by context.
The present application is a continuation in part of U.S. patent application Ser. No. 18/110,306, filed Feb. 15, 2023 and entitled “Negative Emission, Large Scale Carbon Capture for Clean Fossil Fuel Power Generation”, which is a continuation of U.S. patent application Ser. No. 17/889,120, filed Aug. 16, 2022, granted Mar. 28, 2023 as U.S. Pat. No. 11,613,817, and entitled “Negative Emission, Large Scale Carbon Capture for Clean Fossil Fuel Power Generation”, which claims priority to U.S. Provisional Patent Application No. 63/234,322, filed Aug. 18, 2021 and entitled “High-Efficiency Carbon Capture for Clean Fossil Fuel Power Production”. The contents of all applications to which the present application claims priority are herein incorporated by reference in entirety.
| Number | Date | Country | |
|---|---|---|---|
| 63234322 | Aug 2021 | US |
| Number | Date | Country | |
|---|---|---|---|
| Parent | 17889120 | Aug 2022 | US |
| Child | 18110306 | US |
| Number | Date | Country | |
|---|---|---|---|
| Parent | 18110306 | Feb 2023 | US |
| Child | 18625094 | US |
