BACKGROUND OF THE INVENTION

Beginning from ancient times when prehistoric peoples began using fire, humankind has relied on the use of thermal energy to keep warm, cook food, and make tools. Thermal energy derived from combustion or oxidation of fuel materials or obtained from the sun’s rays has proven essential to human flourishing. The transfer of thermal energy from one substance to another provides heat for warming objects and spaces, for altering the chemical properties of materials, and for changing then- shapes. Certain devices for producing thermal energy (each, a “thermal device”), including without limitation equipment such as furnaces, boilers, heaters, warmers, ovens, stoves, dryers, annealers, bakers, cookers, sealers, smelters, solderers, torches, cutting torches, welders, melters, kilns, autoclaves, sterilizers, and the like are well-known in everyday life, while others are familiar to artisans of ordinary skill in more specialized fields.

Thermal energy is the total kinetic energy of a solid or fluid object or material medium due to the random motion of its atoms and molecules. Temperature is the average kinetic energy within the object. Heat is the transfer or flow of thermal energy due to differences in temperature between one object/material medium and another, with the heat flowing from the higher-temperature object/material medium to the one with a lower temperature. Thermal energy is transferred by conduction, convection, and radiation.

Thermochemical principles, whereby chemical reactions are incited to produce thermal energy, are employed routinely for residential or industrial purposes. In many cases, the thermal energy is captured by another medium or mechanism to produce useful work, as is seen in internal or external combustion engines, in which the heat produced by combustion expands fluids (gases or liquids) to drive a prime mover mechanical part, thereby producing useful work, i.e., the displacement of the mechanical part. In other cases, however, the production of heat is itself the goal of the chemical reaction. For example, the chemical reaction of combustion in fireplaces and stoves produces thermal energy that is used to heat spaces and to heat food; in these situations, the beneficial effect of the chemical reaction is not measurable secondarily as work (i.e., the displacement of an object produced by a force acting on it), but rather is quantified primarily as heat. Thermal energy used to produce heat for residential and industrial applications is most commonly derived either directly or indirectly from conventional fossil fuel sources. This results in the production of CO2, which subsequently enters the atmosphere as a greenhouse gas.

It is estimated that heating an average American home with natural gas produces about 6,400 pounds of carbon dioxide, and heating with electricity produces about 4,700 pounds. In colder regions, however, the average amount of CO2 for home heating can double. Commercial settings have additional needs for thermal energy besides what is required for environmental heating. For example, industrial processes use thermal energy to transform materials into other useful shapes or substances, or to initiate or sustain chemical reactions that yield valuable products. Exemplary commercial processes using heat include, without limitation, operations such as metalworking, glassblowing, soldering, drying, baking, hardening, thermosetting, and further including the multitude of heat-requiring reactions in industrial chemistry. In these settings, too, thermal energy is typically provided by conventional processes employing fossil fuel combustion, resulting in the substantial production of carbon dioxide. Industrial heat requirements, including cement production, steel production, and chemical production, are responsible for about 10% of all global greenhouse gas emissions, greater than that of cars and airplanes combined.

The Haber-Bosch process exemplifies a crucial industrial process that requires considerable thermal energy and that produces substantial CO2. The Haber-Bosch process for ammonia formation has revolutionized agriculture over the past century, allowing unreactive diatomic nitrogen to be transformed into a major feedstock for fertilizer synthesis. While the forward reaction of the Haber- Bosch process is exothermic (N ₂ +3H ₂ 2NH ₃ , AH° = -91.8 kJ/mol), it needs to be carried out under high-temperature and high-pressure conditions, including temperatures between 400 - 600 °C. Thus, to produce the conditions required for Haber-Bosch reactions, considerable thermal energy is required, which is mainly produced directly or indirectly by combustion of fossil fuels. It is estimated that the Haber-Bosch process worldwide consumes about 2% of the world’s total energy production, uses about 2% of the world’s natural gas output, and emits 300 million metric tons of CO2 annually: about 1.87 tons of CO2 is released per ton of ammonia produced.

With increasing awareness of the environmental consequences of greenhouse gas emissions, there is a recognized need for alternatives for generating thermal energy for residential and industrial heating purposes that avoid or minimize the production of CO2. There is a further need for convenient and modular systems to produce thermal energy and heat that avoid the complexities, capital expenditures, and logistics of fossil-fuel-based sources of such energy and heat. Advantageously, such systems should be economical and efficient to use, and adaptable to a variety of settings.

SUMMARY OF THE INVENTION

The present invention relates to the discovery that apparatuses containing carbon matrices can be used to produce reactant chemicals useful as fuels and chemical feedstocks. The processes of the invention include the application of electromagnetic radiation, directly and/or indirectly, to gases, nano-porous carbon, or compositions and combinations thereof, thereby pre-treating the gas, and exposing a carbon matrix to pre-treated gas in an apparatus of the invention and recovering those reactant chemicals useful as fuels and chemical feedstocks produced therein. The invention relates to apparatuses for instantiating materials, and processes for using such apparatuses. The invention includes processes comprising the steps of contacting a bed comprising nanoporous carbon with an activated gas while applying electromagnetic radiation to the nanoporous carbon for a time sufficient to cause instantiation of the fuel substance or feedstock substance and collecting the fuel substance or feedstock substance. The invention further relates to the fuel substance or feedstock substance produced by the process.

More specifically, the invention includes a process of instantiating a chemical reactant within a nanoporous carbon powder comprising the steps of:

(i) adding a nanoporous carbon powder into a reactor assembly (RA), as described below,

(ii) adding a feedgas composition to the reactor assembly, wherein the feedgas composition is free of the desired fuel substance or feedstock substance;

(iii) powering one or more RA coils to a first electromagnetic energy level;

(iv) subjecting the nanoporous carbon powder (the terms nanoporous carbon powder, nanoporous carbon material and nanoporous carbon are used herein interchangeably) to harmonic patterning to instantiate the chemical reactant in product compositions;

(v) collecting the product compositions comprising the chemical reactant; and

(vi) optionally isolating the chemical reactant from the product compositions.

In one embodiment, the RA coil surrounds a nanoporous carbon bed to establish a harmonic electromagnetic resonance in ultramicropores of the nanoporous carbon powder. The feed gas composition can be, for example, air, oxygen, hydrogen, helium, nitrogen, neon, argon, krypton, xenon, carbon monoxide, carbon dioxide or mixtures thereof, preferably nitrogen or air. Preferably, the nanoporous carbon powder comprises graphene having at least 99.9% wt. carbon (metals basis), a mass mean diameter between 1 pm and 5 mm, and an ultramicropore surface area between about 100 and 3000 m ² /g. More specifically, the invention includes a reactor assembly comprising:

A reactor chamber containing a nanoporous carbon material;

A second porous frit defining the ceiling of the reactor chamber; wherein each porous frit has a porosity that is sufficient to allow a gas to permeate into the reactor chamber and contain a nanoporous carbon material;

A reactor head space disposed above the reactor cap;

1, 2, 3, 4, 5 or more RA coils surrounding the reactor chamber and/or reactor head space operably connected to one or more RA frequency generators and/or one or more power supplies;

0, 1, 2, 3, 4, 5 or more pairs of RA lamps wherein the pairs of RA lamps are disposed circumferentially around the RA coils and define a space between the pairs of RA lamps and the RA coils, when present;

An optional x-ray source configured to expose the reactor chamber to x-rays; One or more optional lasers configured to direct a laser towards (e.g., through or across) the reactor chamber or the gas within the reactor assembly, when present; and

A computer processing unit (CPU) configured to control the power supply, frequency generator, x-ray source, lamps and/or lasers.

As will be described in more detail below, the gas inlet of the reactor assembly can be in fluid connection with at least one gas supply selected from the group consisting of air, oxygen, hydrogen, helium, nitrogen, neon, argon, krypton, xenon, carbon monoxide, carbon dioxide and mixtures thereof; and/or (iii) the gas supply is directed through a gas manifold controlled by mass flow meters.

As will be described in more detail below, the nanoporous carbon powder charged to the reactor assembly can comprise graphene having at least 95% wt. carbon (metals basis), a mass mean diameter between 1 pm and 5 mm, and an ultramicropore surface area between about 100 and 3000 m ² /g. The nanoporous carbon powder is preferably characterized by acid conditioning, wherein the acid is selected from the group consisting, without limitation, of HC1, HF, HBr, HI, sulfuric acid, phosphoric acid, carbonic acid, and nitric acid, and a residual water content of less than that achieved upon exposure to a relative humidity (RH) of less than 40% RH at room temperature. In a preferred embodiment, the process contemplates degassing the nanoporous carbon powder prior to the process.

As will be described in more detail below, the reactor assembly can include a plurality of devices that can impart electromagnetic fields, including x-ray sources, coils, lasers and lamps or lights, including pencil lamps, short wave and long wave lamps. The wavelengths generated by each device (e.g., lamps or lasers) can be independently selected.

As will be described in more detail below, the RA coils can be made from the same or different electrically conducting materials. For example, a first RA coil comprises a copper wire winding, a second RA coil comprises a braiding of copper wire and silver wire, and a third RA coil is a platinum wire winding, and each RA coil is configured to create a magnetic field and wherein each power supply independently provides AC and/or DC current.

As will be described in more detail below, the reactor assembly can be characterized by (i) a first pair of RA lamps configured in a first plane defined by a center axis and a first radius of the reactor chamber, (ii) a second pair of RA lamps configured in a second plane defined by the center axis and a second radius of the reactor chamber and (iii) a third pair of RA lamps configured in a third plane defined by the center axis and a third radius of the reactor chamber. Preferably, each RA lamp is a pencil lamp characterized by a tip substantially equidistant from the central axis and each pair of RA lamps comprises a vertical RA lamp and a horizontal RA lamp. Preferably each pair of lamps is equidistantly spaced around the circumference of the reactor chamber. As will be described in more detail below, the reactor assembly further comprises an electromagnetic embedding enclosure (E/MEE or EMEE), as defined more specifically below. The E/MEE is typically located along a gas line upstream of the reactor assembly gas inlet. Typically, an electromagnetic embedding enclosure located upstream of the gas inlet comprises:

(a) a gas inlet;

(b) at least one E/MEE pencil lamp positioned below the internal gas line, at least one E/MEE pencil lamp positioned above the internal gas line and at least one E/MEE pencil lamp positioned to the side of the internal gas line; wherein each E/MEE pencil lamp is independently rotatably mounted, located along the length of the internal gas line, and the lamps and/or coil(s) are powered by a power supply, preferably the power supply of the reactor assembly; the gas flow, lamps and/or coil(s) are preferably independently controlled by one or more central processing units, preferably the central processing unit (CPU) of the reactor assembly.

Typically, a CPU independently controls powering each E/MEE pencil lamp and a rotation position of each E/MEE pencil lamp. It is to be understood that the term “independently” is not meant to be absolute but is used to optimize results. Rather, controlling each RA coil, lamp and/or laser (each a device) such that it is powered (or rotated) at the same time or at a time specified before and/or after another device is meant to be “independently” controlled. Thus, assigning two or more devices to a power supply and control unit in series is contemplated by the term. The term is intended to exclude simply powering (or rotating) all devices simultaneously.

As will be described in more detail below, the E/MEE housing can be typically closed and opaque, the internal gas line can be transparent and external gas line in fluid connection with the housing outlet and gas inlet can be opaque. Typically, the internal gas line is between 50 cm and 5 meters or more and has a diameter between 2 mm and 25 cm or more.

As will be described in more detail below, the apparatus can have at least 5 E/MEE pencil lamps located along the internal gas line. Each E/MEE pencil lamp can be independently placed such that its longitudinal axis is (i) parallel to the internal gas line, (ii) disposed radially in a vertical plane to the internal gas line, or (iii) perpendicular to the plane created along the longitudinal axis of the internal gas line or along the vertical axis of the internal gas line. Each E/MEE pencil lamp can be independently affixed to one or more pivots that permit rotation, such as, between about 0 and 360 degrees (such as, between 0 and 90 degrees, between 0 and 180 degrees, between 0 and 270 degrees and any angle there between) with respect to the x, y, and/or z axis wherein (i) the x-axis is defined as the axis parallel to the gas line and its vertical plane, (ii) the y-axis defining the axis perpendicular to the gas line and parallel to its horizontal plane, and (iii) the z-axis is defined as the axis perpendicular to the gas line and parallel to its vertical plane.

As will be described in more detail below, at least one E/MEE pencil lamp can be a neon lamp, at least one E/MEE pencil lamp can be a krypton lamp, and at least one E/MEE pencil lamp can be an argon lamp. It can be desirable to match, or pair, one or more E/MEE pencil lamps with one or more (e.g., a pair) of RA lamps. Accordingly, at least one pair of RA pencil lamps can be selected from the group consisting of a neon lamp, a krypton lamp, and an argon lamp.

As will be described in more detail below, the invention also includes nanoporous carbon powder compositions, gas compositions, and fluid (preferably gaseous) compositions produced in accordance with the claimed methods and processes.

As will be described in more detail below, the invention includes a process of producing a nanoporous carbon composition comprising the steps of: (a) initiating a gas flow in a reactor assembly as described herein; (b) independently powering each RA coil to a first electromagnetic energy level; (c) powering the one or more RA frequency generators and applying a frequency to each RA coil; (d) independently powering each RA lamp; (e) independently powering each laser; (f) powering the x-ray source; and (g) subjecting the nanoporous carbon powder to harmonic electromagnetic resonance in ultramicropores of the nanoporous carbon powder to instantiate a fluid (preferably gaseous), or solid chemical reactant in a nanopore.

The invention also includes a process of producing a nanoporous carbon composition comprising the steps of: (a) initiating a gas flow in a reactor assembly further comprising an E/MEE, as described herein; (b) independently powering each RA coil to a first electromagnetic energy level; (c) powering the one or more RA frequency generators and applying a frequency to each RA coil; (d) independently powering each RA lamp; (e) independently powering each laser; (f) powering the x-ray source; and (g) subjecting the nanoporous carbon powder to harmonic electromagnetic resonance in ultramicropores of the nanoporous carbon powder to instantiate a fluid (preferably gaseous) or solid chemical reactant in a nanopore.

The invention also includes a process of instantiating a fluid (preferably gaseous) or solid chemical reactant within an ultramicropore of a nanoporous carbon powder comprising the steps of: (a) initiating a gas flow in a reactor assembly further comprising an E/MEE, as described herein; (b) independently powering each RA coil to a first electromagnetic energy level; (c) powering the one or more RA frequency generators and applying a frequency to each RA coil; (d) independently powering each RA lamp; (e) independently powering each laser; (f) powering the x-ray source; and (g) subjecting the nanoporous carbon powder to harmonic electromagnetic resonance in ultramicropores of the nanoporous carbon powder to instantiate the fluid (preferably gaseous) or solid chemical reactant in a nanopore. The invention further includes a fluid (preferably gaseous) or solid chemical reactant by the aforesaid process.

The invention can also include a process for producing a chemical reactant comprising the steps of:

(a) Adding a feed gas to an electromagnetic embedding apparatus comprising:

(i) a gas line containing the feed gas,

(ii) at least one E/MEE pencil lamp positioned below the gas line,

(iii) at least one E/MEE pencil lamp positioned above the gas line and

(iv) at least one E/MEE pencil lamp positioned to the side of the gas line, wherein each E/MEE pencil lamp is independently rotatably mounted, located along the length of the gas line;

(v) a power source operably connected to each pencil lamp, and

(vi) a central processing unit configured to independently control powering each E/MEE pencil lamp and a rotation position of each E/MEE pencil lamp;

(b) powering each pencil lamp, thereby subjecting the feed gas to electromagnetic radiation; optionally rotating one or more lamps;

(c) directing the feed gas from step (b) to a reactor assembly comprising:

(i) a gas inlet and one or more gas outlets,

(ii) a reactor chamber containing a nanoporous carbon disposed within a cup and, optionally, covered with a cap,

(iii) a first porous frit defining a floor of the reactor chamber disposed within the cup,

(iv) a second porous frit defining the ceiling of the reactor chamber and disposed below the cap; wherein each porous frit has a porosity that is sufficient to allow a gas to permeate into the reactor chamber and contain a nanoporous carbon,

(v) a reactor head space disposed above the reactor cap, and

(vi) at least one RA coil surrounding the reactor chamber and/or reactor head space operably connected to a power supply, wherein the computer processing unit is configured to control the power supply to the RA coil;

(d) powering each RA to a first electromagnetic energy level;

(e) subjecting the nanoporous carbon powder to harmonic patterning to instantiate product compositions; and

(f) collecting the chemical reactant from the product compositions.

The invention further includes a fluid (preferably gaseous) or solid chemical reactant produced by the aforesaid process. In embodiments, the chemical reactant is a fuel substance or a feedstock substance. In embodiments, the chemical reactant comprises a gas selected from the group consisting of hydrogen (H ₂ ), carbon (C), carbon monoxide (CO), ammonia (NH ₃ ), a substituted or unsubstituted hydrocarbon, a hydrocarbon derivative, and a carbohydrate. In embodiments, the chemical reactant comprises a substituted or unsubstituted hydrocarbon selected from the group consisting of alkanes, cycloalkanes alkenes, alkynes, and substituted or unsubstituted aromatic hydrocarbons, and can comprise a C1-C4 alkane, a Cs-C’x alkane, a C9-C16 alkane, or an alkane containing 17 or more carbon atoms. In embodiments, the chemical reactant comprises an alcohol or a nitroalkane.

The invention further includes thermal systems energized by combustion of a fuel to produce thermal energy thereby, comprising:

(a) a set of one or more fuel RAs that produces the fuel; a fuel intake system in fluid communication with the set of one or more fuel RAs, and further in fluid communication with a combustion chamber, wherein the fuel intake system delivers the fuel into a combustion chamber;

(b) a delivery system in fluid communication with the combustion chamber, wherein the delivery system delivers an oxidizing agent into the combustion chamber;

(c) a control system operatively coupled to the fuel intake system and the delivery system, wherein the control system regulates delivery of a preselected fuel amount and a preselected oxidizing agent amount to the combustion chamber, and wherein the control system triggers an ignition of the fuel and the oxidizing agent when the preselected fuel amount and the preselected oxidizing agent amount are present in the combustion chamber; and

(d) an ignition system within the combustion chamber, triggered by the control system, that ignites the fuel and the oxidizing agent to produce combustion of the fuel, wherein the combustion of the fuel produces the thermal energy.

In embodiments, the fuel comprises hydrogen. In embodiments, the set of one or more fuel RAs comprises a plurality of fuel RAs. In embodiments, the oxidizing agent enters the delivery system from a feedgas line or from ambient atmosphere. In embodiments, the thermal system comprises one or more auxiliary RAs that produce the oxidizing agent, which can comprise oxygen, wherein the one or more auxiliary RAs are in fluid communication with the delivery system, and wherein the one or more auxiliary RAs produce at least a portion of the preselected oxidizing agent amount in the combustion chamber.

The invention also includes methods of producing thermal energy, comprising the steps of :

(a) instantiating a fuel from a set of one or more RAs;

(b) supplying the fuel to a thermal apparatus; and

(c) reacting the fuel with an oxidizing agent in the thermal apparatus, wherein the step of reacting produces the thermal energy. In embodiments, the fuel comprises hydrogen. In embodiments, the oxidizing agent comprises oxygen, which can be produced by an auxiliary set of one or more RAs.

In embodiments, the invention pertains to thermal systems energized by oxidation of a fuel to produce thermal energy thereby, comprising a) a set of one or more fuel RAs that produces the fuel; b) a fuel intake system in fluid communication with the set of one or more fuel RAs, and further in fluid communication with a thermal apparatus, wherein the fuel intake system delivers the fuel into the thermal apparatus; c) a delivery system in fluid communication with the thermal apparatus, wherein the delivery system delivers an oxidizing agent into the thermal apparatus; d) a control system operatively coupled to the fuel intake system and the delivery system, wherein the control system regulates delivery of a preselected fuel amount and a preselected oxidizing agent amount to the thermal apparatus, and wherein the control system triggers an ignition of the fuel and the oxidizing agent when the preselected fuel amount and the preselected oxidizing agent amount are present in the thermal apparatus; and e) an ignition system within the thermal apparatus, triggered by the control system, that ignites the fuel and the oxidizing agent to produce the oxidation of the fuel, thereby producing the thermal energy.

In embodiments, the oxidation of the fuel is a combustion reaction, which can take place in a combustion chamber within the thermal apparatus, and/or which can create an open flame. In embodiments, the fuel comprises hydrogen. In embodiments, the set of one or more fuel RAs comprises more than one fuel RA. In embodiments, the oxidizing agent, which can comprise oxygen, enters the delivery system from a feedgas line or from ambient atmosphere, while in other embodiments, at least a portion of the oxidizing agent is produced by an auxiliary set of one or more RAs in fluid communication with the delivery system. In embodiments, the thermal system further comprises a heat recipient, which can be integrated into a furnace or boiler. Also disclosed herein are methods of producing thermal energy using such a thermal system, comprising the steps of providing the thermal system; instantiating the fuel by the set of one or more fuel RAs; providing an oxidizing agent; directing the fuel into the thermal apparatus; delivering the oxidizing agent into the thermal apparatus; mixing the fuel and the oxidizing agent to form a fuel-oxidant mixture; and igniting the fuel-oxidant mixture to produce a reaction that yields the thermal energy. In embodiments, the step of providing the oxidizing agent is performed by an auxiliary set of one or more RAs in fluid communication with the thermal apparatus; in embodiments, the step of providing the oxidizing agent comprises obtaining the oxidant from a conventional oxidant source. In embodiments, the step of mixing takes place before the step of directing, while in other embodiments, the step of directing and the step of delivering occur synchronously. In embodiments, the reaction is a combustion reaction which can create an open flame. In embodiments, the method further comprises a step of transferring the thermal energy to a heat recipient, wherein the step of transferring can comprise a heat transfer process selected from the group consisting of conduction, convection, or radiation.

In embodiments, the invention pertains to thermal systems, wherein the thermal system comprises a thermal device, and wherein the thermal system is integrated into one or more pieces of thermal equipment. In embodiments, at least one of the one or more pieces of thermal equipment is selected from the group consisting of furnaces, boilers, heaters, irons, warmers, ovens, stoves, dryers, annealers, kilns, bakers, cookers, sealers, smelters, solderers, torches, cutting torches, welders, melters, autoclaves, and sterilizers; at least one of the one or more pieces of thermal equipment can comprise a furnace or a boiler, or can comprise a cutting torch or a welder.

In embodiments, the invention pertains to methods of producing thermal energy, comprising: supplying a fuel to a thermal apparatus; delivering an oxidizing agent to the thermal apparatus; and reacting the fuel with the oxidizing agent in the thermal apparatus, wherein the step of reacting produces a radiant energy that includes thermal energy, and wherein at least one of the fuel and the oxidizing agent is instantiated by a set of one or more RAs. In embodiments, the fuel is instantiated by the set of one or more RAs, and the oxidizing agent is provided from a conventional source; in other embodiments, the oxidizing agent is instantiated by the set of one or more RAs. In embodiments, the step of supplying and the step of delivering produce a mixture within the thermal apparatus prior to the step of reacting the fuel with the oxidizing agent. In embodiments, the step of reacting comprises combusting the fuel with the oxidizing agent, which can take place within a combustion chamber within the thermal apparatus, and/or which can produce an open flame that produces the radiant energy, where the open flame can be deployed within a welding torch. In embodiments, the step of reacting takes place in a furnace, which can comprise a boiler. In embodiments, the method further comprises a step of transferring the thermal energy to a heat recipient by a heat transfer process selected from the group consisting of conduction, convection, and radiation.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 is a perspective view of an E/MEE of the invention.

FIG. 2A and 2C show reactor assembly components. FIG. 2B is an expanded view of the reactor assembly components of FIG. 2A.

FIG. 3A, FIG. 3B, FIG. 3C, FIG. 3D and FIG. 3E provides five views of coils which can be used in a reactor assembly.

FIG. 4A is a perspective view of an E/MEE of the invention used in carbon pretreatment. FIG. 4B shows reactor assembly components. FIG. 5A illustrates one conformation for a standard coil. FIG. 5B illustrates one conformation for a reverse field coil.

FIG. 6A and 6B are illustrations of two examples of two composite reactor assemblies. FIG. 6A illustrates a Composite Reactor with a copper body, carbon graphite cup and a carbon graphite cap and a metal foil boundary. FIG. 6B illustrates a Composite Reactor with a carbon graphite body and cap and metal foil boundary.

FIGs. 7A-7I illustrate various reactor assembly views according to the invention.

FIGs. 8A-8C are illustrations of reactor variations.

FIG. 9 is a diagram of an exemplary system comprising a reactor assembly.

FIG. 10 is a more detailed block diagram of the system illustrated in FIG. 9.

FIGs 11A-1 IB are block diagrams of an exemplary thermal system.

FIG. 12 is a block diagram of an exemplary thermal system.

DETAILED DESCRIPTION

The invention relates to methods of instantiating fuels in nanoporous carbon powders. As used herein, the term “fuel” refers to a chemical substance that reacts with other chemical substances (i.e., a chemical reactant) to release thermal energy. Chemical reactants produced by the methods and apparatuses disclosed herein can be formed as fluids (preferably gases) solids, or other states of matter.

The invention involves the production of a chemical reactant useful as a fuel substance using methods comprising the steps of contacting a bed comprising a nanoporous carbon powder with a feed gas composition, and optionally an electromagnetically activated gas, while applying electromagnetic radiation to the nanoporous carbon powder for a time sufficient to cause instantiation within and/or from carbon nanopores. The process results in a product composition comprising a chemical reactant substantially distinct from the feed gas composition. The processes of the invention have broad applicability in producing chemical reactants useful as fuels. Such fuels can be utilized for producing thermal energy, which in turn can be used for producing heat.

The invention relates to the discovery that carbon matrices can be used to instantiate, or fdter, or isolate, or extract, or nucleate, a variety of substances, for example producing nano-deposits, nanostructures, nanowires and nuggets comprising metals or non-metals, by employing processes that include the application of electromagnetic radiation, directly and/or indirectly, to gases, nano-porous carbon, or compositions and combinations thereof, thereby pre-treating these materials, and thereafter exposing a carbon matrix to pre-treated gas in an apparatus to cause metal or non-metal instantiation, nucleation, growth and/or deposition within the carbon matrix. In more detail, the invention relates to methods of instantiating chemical substances in any form, whether fluid (preferably gaseous), solid, or other. In embodiments, the invention produces metals and non-metals in nanoporous carbon matrices, through processes comprising the steps of contacting a bed comprising nanoporous carbon with an activated gas while applying electromagnetic radiation to the nanoporous carbon for a time sufficient to cause instantiation, including but not limited to nucleation, growth deposition and/or agglomeration, of elemental metal or non-metal nanoparticles within and/or from carbon nanopores and nano-pore networks and matrices. Such processes result in nanoporous carbon compositions or matrices characterized by elemental metals and/or non-metals deposited within carbon nanopores and agglomerated elemental nanoparticles, creating elemental metal nuggets, nanowires and other macrostructures that can be easily separated from the nanoporous carbon. In embodiments, these processes can produce elemental metal composition and macrostructures; in embodiments, the nanoporous carbon composition can also comprise non-metal nanostructures and/or macrostructures. In embodiments, the processes can instantiate, or filter, or isolate, or extract, or nucleate materials containing carbon, oxygen, nitrogen, sulfur, phosphorous, selenium, hydrogen, and/or halides (e.g., F, Cl, Br and I). Nanoporous carbon compositions further comprising metal oxides, nitrides, and sulfides such as copper oxide, molybdenum sulfide, aluminum nitride have been identified. Therefore, small inorganic molecules or compounds (e.g., molecules comprising 2, 3, 4, 5, 6, 7, 8, 9 or 10 or 25 atoms) can be instantiated, or filtered, or isolated, or extracted, or nucleated, using the processes disclosed herein. Examples of such small molecules include carbides, oxides, nitrides, sulfides, phosphides, halides, carbonyls, hydroxides, hydrates including water, clathrates, clathrate hydrates, and metal organic frameworks. In embodiments, the processes disclosed herein produce small molecules or other materials useful as fuels. In embodiments, such fuels comprise a fluid (preferably gaseous) selected from the group consisting of hydrogen (H ₂ ), carbon (C), carbon monoxide (CO), ammonia (NH ₃ ), a substituted or unsubstituted hydrocarbon, a hydrocarbon derivative, and a carbohydrate. In embodiments, the chemical reactant comprises a substituted or unsubstituted hydrocarbon selected from the group consisting of alkanes, cycloalkanes alkenes, alkynes, and substituted or unsubstituted aromatic hydrocarbons, and can comprise a C1-C4 alkane, a Cs-C’x alkane, a C9-C16 alkane, or an alkane containing 17 or more carbon atoms.

1. NANOPOROUS CARBON POWDERS AND COMPOSITIONS a. Nanoporous Carbon Powders

Nanoporous carbon powders or nanostructued porous carbons can be used in the processes and methods of the invention. Nanoporous carbon powders or nanostructued porous carbons are also refered to herein as “starting material” or “charge material”. The carbon powder preferably provides a surface and porosity (e.g., ultra-microporosity) that enhances metal deposition, including deposit, instantiation, and growth. Preferred carbon powders include activated carbon, engineered carbon, graphite, and graphene. For example, carbon materials that can be used herein include graphene foams, fibers, nanorods, nanotubes, fullerenes, flakes, carbon black, acetylene black, mesophase carbon particles, microbeads and, grains. The term “powder” is intended to define discrete fine, particles or grains. The powder can be dry and flowable or it can be humidified and caked, such as a cake that can be broken apart with agitation. Although powders are preferred, the invention contemplates substituting larger carbon materials, such as bricks and rods including larger porous carbon blocks and materials, for powders in the processes of the invention.

The examples used herein typically describe highly purified forms of carbon, such as >99.995%wt. pure carbon (metals basis). Highly purified forms of carbon are exemplified for proof of principle, quality control and to ensure that the results described herein are not the result of crosscontamination or diffusion within the carbon source. However, it is contemplated that carbon materials of less purity can also be used. Thus, the carbon powder can comprise at least about 95% wt. carbon, such as at least about 96%, 97%, 98% or 99% wt. carbon. In a preferred embodiment, the carbon powder can be at least 99.9%, 99.99% or 99.999% wt. carbon. In each instance, purity can be determined on either an ash basis or on a metal basis. In another preferred embodiment, the carbon powder is a blend of different carbon types and forms. In one embodiment, the carbon bed is comprised of a blend of different nano-engineered porous carbon forms. Carbon powders can comprise dopants.

The carbon powder preferably comprises microparticles. The volume median geometric particle size of preferred carbon powders can be between less than about 1 pm and 5 mm or more. Preferred carbon powders can be between about 1 pm and 500 pm, such as between about 5 pm and 200 pm. Preferred carbon powders used in the exemplification had median diameters between about 7 pm and 13 pm and about 30 pm and 150 pm.

The dispersity of the carbon particle size can improve the quality of the products. It is convenient to use a carbon material that is homogeneous in size or monodisperse. Thus, a preferred carbon is characterized by a poly dispersity index of between about 0.5 and 1.5, such as between about 0.6 and 1.4, about 0.7 and 1.3, about 0.8 and 1.2, or between about 0.9 and 1.1. The polydispersity index (or PDI) is the ratio of the mass mean diameter and number average diameter of a particle population. Carbon materials characterized by a bimodal particle size can offer improved gas flow in the reactor.

The carbon powder is preferably porous. The pores, or cavities, residing within the carbon particles can be macropores, micropores, nanopores and/or ultra-micropores. A pore can include defects in electron distribution, compared to graphene, often caused by changes in morphology due to holes, fissures or crevices, corners, edges, swelling, or changes in surface chemistry, such as the addition of chemical moieties or surface groups, etc. For example, variation in the spaces that may arise between layers of carbon sheets, fullerenes or nanotubes are contemplated. It is believed that instantiation preferentially occurs at or within a pore or defect-containing pore and the nature of the surface characteristics can impact instantiation. For example, Micromeritics enhanced pore distribution analysis (e.g., ISO 15901-3) can be used to characterize the carbon. It is preferred that the carbon powder is nanoporous. A “nanoporous carbon powder” is defined herein as a carbon powder characterized by nanopores having a pore dimension (e.g., width or diameter) of less than 100 nm. For example, IUPAC subdivides nanoporous materials as microporous (having pore diameters between 0.2 and 2 nm), mesoporous materials (having pore diameters between 2 and 50 nm) and macroporous materials (having pore diameters greater than 50 nm). Ultramicropores are defined herein as having pore diameters of less than about 1 nm.

Uniformity in pore size and/or geometry is also desirable. For example, ultramicropores in preferred carbon materials (e.g., powders) account for at least about 10% of the total porosity, such as at least about 20%, at least about 30%, at least about 40%, at least about 50%, at least about 60%, at least about 70%, at least about 80%, or at least about 90%. Preferred carbon materials (e.g., powders) are characterized with a significant number, prevalence, or concentration of ultra-micropores having the same diameter, thereby providing predictable electromagnetic harmonic resonances and/or standing wave forms within the pores, cavities, and gaps. The word “diameter” in this context is not intended to require a spherical geometry of a pore but is intended to embrace a dimension(s) or other characteristic distances between surfaces. Accordingly, preferred carbon materials (e.g., powders) are characterized by a porosity (e.g., nanopores or ultramicropores) of the same diameter account for at least about 10% of the total porosity, such as at least about 20%, at least about 30%, at least about 40%, at least about 50%, at least about 60%, at least about 70%, at least about 80%, or at least about 90%.

Measuring adsorption isotherm of a material can be useful to characterize the surface area, porosity, e.g., external porosity, of the carbon material. Carbon powders having a surface area between about 1 m ² /g and 3000 m ² /g are particularly preferred. Carbon powders having an ultramicropore surface area of at least about 50 m ² /g, preferably at least about 300 m ² /g, at least about 400 m ² /g, at least about 500 m ² /g or higher are particularly preferred. Activated or engineered carbons, and other quality carbon sources, can be obtained with a surface area specification. Surface area can be independently measured by BET surface adsorption technique.

Surface area correlation with metal deposition was explored in a number of experiments. Classical pore surface area measurements, using Micromeritics BET surface area analytical technique with nitrogen gas at 77K (-196.15°C) did not reveal a substantial correlation in the deposition of metal elements at >5o confidence level, or probability of coincidence. However, a correlation with ultramicropores (pores having a dimension or diameter of less than 1 nm) was observed. Without being bound by theory, instantiation is believed to be correlated to resonating cavity features of the ultra-micropore and ultramicropore network such as the distance between surfaces or walls. Features of the ultramicropore, can be predicted from ultramicropore diameter as measured by BET, augmented by density function theory (DFT) models, for example. With the aid of machine learning, more precise relationships between ultramicropore size, distribution, turbostratic features, wall separation and diameter and elemental metal nucleation can be established.

Carbon materials and powders can be obtained from numerous commercial providers. MSP- 20X and MSC-30 are high surface area alkali activated carbon materials with nominal surface areas of 2,000-2,500 m ² /g and >3,000 m ² /g and median diameters of 7-13 pm and 60-150 pm respectively (Kansai Coke & Chemicals Co). Norit GSX is a steam -washed activated carbon obtained from Alfa Aesar. The purified carbon forms used in the experimental section all exceed >99.998wt% C (metals basis).

Modifying the surface chemistry of the carbon can also be desirable. For example, improved performance was observed when conditioning the carbon with an acid or base. Contacting the carbon with a dilute acid solution selected from the group consisting of HC1, HF, HBr, HI, sulfuric acid, phosphoric acid, carbonic acid, and nitric acid followed by washing with water (such as deionized water) can be beneficial. The acid is preferably in an amount less than about 30%, less than about 25%, less than about 20% less than about 15%, less than about 10%, or less than about 5%, preferably less than or equal to 1% vol. The preferred acid for an acid wash is an acid having a pKa of less than about 3, such as less than about 2. After washing, it can be beneficial to subject the carbon to a blanket of a gas, such as helium, hydrogen, or mixtures thereof. Alternative gases include, without limitation, carbon monoxide, carbon dioxide, nitrogen, argon, neon, krypton, helium, ammonia, and hydrogen. The carbon can also be exposed to a base, such as KOH before or after an acid treatment.

Controlling residual water content in the carbon which may include moisture can improve performance. For example, the carbon material can be placed in an oven at a temperature of at least about 100°C, preferably at least about 125°C, such as between 125°C and 300°C for at least 30 minutes such as about an hour. The oven can be at ambient or negative pressure, such as under a vacuum. Alternatively, the carbon material can be placed in an oven with high vacuum at a temperature of at least about 250°C, preferably at least about 350°C, for at least one hour, such as at least 2, 3, 4, 5, or 6 hours. Alternatively, the carbon material can be placed in an oven with high vacuum at a temperature of at least about 700°C, preferably at least about 850°C, for at least one hour, such as at least 2, 3, 4, 5, or 6 hours. Alternatively, the water or moisture can be removed by vacuum or lyophilization without the application of substantial heat. Preferably, the water, or moisture, level of the carbon is less than about 35%, 30%, 25%, 20%, 15%, 10%, 5%, such as less than about 2%, by weight carbon. In other embodiments, the carbon can be exposed to a specific relative humidity (RH) such as 0.5%, 1%, 2%, 5%, 12% RH or 40% RH or 70% RH or 80% RH or 90% RH, for example, at 22 °C.

Pre-treatment of the carbon material can be selected from one or more, including all, the steps of purification, humidification, activation, acidification, washing, hydrogenation, drying, chemistry modification (organic and inorganic), and blending. For example, the carbon material can be reduced, protonated, or oxidized. The order of the steps can be as described, or two or more steps can be conducted in a different order.

For example, MSP-20X was exposed to an alkali (C:KOH at a molar ratio of 1:0.8), activated at 700°C for 2 hours, washed with acid and then hydrogenated to form MSP-20X Lots 1000 when washed with HC1 and 105 when washed with HNO3. MSP-20X was washed with acid and then hydrogenated to form MSP-20X Lots 1012 when washed with HC1 and 1013 when washed with HNO3. Activated carbon powder developed for the storage of hydrogen was HC1 acid washed, then subjected to HNO3 washing and hydrogenation to form APKI lots 1001 and 1002, as substantially described in Yuan, J. Phys. Chem. 20081 124614345-14357. Poly(ether ether ketone) (PEEK, Victrex 450P) and poly(ether imide) (PEI, Ultem® 1000) was supplied by thermally oxidized in static air at 320°C for 15 h, and carbonized at the temperature range of 550 -1100°C in nitrogen atmosphere, at the carbon yield of 50 - 60 wt%. These carbons were then activated by the following procedures: (1) grind the carbonized polymer with KOH at KOH/carbon ~ 1/1 - 1/6 (w/w), in the presence of alcohol, to form a fine paste; (2) heat the paste to 600 - 850°C in nitrogen atmosphere for 2 h; (3) wash and rinse with DI water and dry in vacuum oven. PEEK/PEI (50/50 wt) blend was kindly supplied by PoroGen, Inc. Likewise, the acid washing sequence of Lots 1001 and 1002 was reversed to form APKI lots 1003 and 1004. Universal grade, natural graphite, ~200 mesh was purchased from Alfa Aesar, product number 40799. Graphite lots R and Z were HC1 washed and hydrogenated to form R lot 1006 and Z lot 1008, respectively. Alfa Aesar graphite R and Z were nitric acid washed and hydrogenated to form R lot 1007 and Z lot 1009, respectively. MSC-30 (Kansai Coke and Chemicals) was acid washed and then hydrogenated to form MSC30 lots 1010 when washed with HC1 and 1011 when washed with HNO3. MSC-30 was exposed to an alkali (C:KOH at a molar ratio of 1:0.8), activated at 700C for 2 hours, HC1 or nitric acid washed and then hydrogenated to form MSC- 30 lots 1014 (HC1 washed) and 1015 (HNO3 washed), respectively. MSP-20X, MSC-30, Norit GSX and Alfa Aesar R were subjected to purification by MWI, Inc. for MSP-20X Lots 2000 and 2004, MSC-30 Lots 2001, 2006 and 2008, Norit GSX Lots 2005 and 2007, and Alfa Aesar R Lot 2009 respectively. MSP-20X Lot 2000 and MSC-30 2001 were HC1 washed and hydrogenated to form MSP-20X Lot 2002 and MSC-30 Lot 2003, respectively. Alfa Aesar R was washed with 1%, 5%, 10%, 15%, 20%, 25%, and 30% HC1 (vol.) and then hydrogenated to for R Lot Graphite n% vol HC1, respectively. Purified MSP-20X (Lot 2006) was similarly washed by HC1, nitric acid, HF or H2SO4 to form MSP-20X 1% HC1, MSP-20X 1% HNO3, MSP-20X 0.4% HF, MSP-20X 0.55% H ₂ SO ₄ (Lot 1044), respectively. Purified Norit GSX (Lot 2007) was similarly washed by nitric acid, HF or H2SO4 to form Norit GSX 1% HNO ₃ (Lot 1045), Norit-GSX 0.4% HF, Norit-GSX 0.55% H ₂ SO ₄ , respectively. Purified MSC30 (Lot 2008) was similarly washed by HC1 and H2SO4 to form MSC30 1% HC1, and MSC30 5% H ₂ SO ₄ . Purified MSP20X (Lot 2006), Norit GSX (Lot 2007) and MSC30 (Lot 2008) were hydrogenated. Purified MSP-20X, Norit GSX and MSC30 were washed with 1% HC1 using methanol as a wetting agent. APKI-S-108 Lots 1021-1024 were recycled. The Ref-X Blend is a 40% Alfa Aesar R:60%MSP-20X (lot 2006) 850°C desorb then CO ₂ exposure at 138kPa (20 psi) for 5 days.

It is preferred to degas the nanoporous carbon powder can be degassed prior to initiating the process. For example, the nanoporous carbon powder can be degassed by subjecting the powder to a vacuum. A range of vacuums can be used, with or without elevated temperatures. It has been found that applying a vacuum of about 10' ² torr to 10' ⁶ torr was sufficient. The powder can be degassed prior to charging the powder into the reactor chamber. Preferably the powder can be degassed after the powder is charged into the reactor chamber. In the examples below, which are non-limiting, the carbon powder is charged into the reactor chamber, placed into the reactor assembly and the entire reactor assembly is subjected to a degassing step by maintaining the reactor assembly under vacuum. The degassing step can be performed at ambient temperature or an elevated temperature. For example, good results were achieved at a temperature of 400°C. Other temperatures can be at least 50°C, such as at least 100°C, at least 150°C, at least 200°C, or at least 300°C. The degassing step can be maintained for at least 30 minutes, such as at least 45 minutes, at least 60 minutes, at least 4 hours, at least 6 hours, at least 12 hours, or at least 24 hours. Degassing the carbon powder ensures that contaminant elements have been removed from the system.

The carbon can be recycled or reused. In recycling the carbon, the carbon can optionally be subjected to an acid wash and/or water removal one or more times. In this embodiment, the carbon can be reused one or more times, such as 2, 3, 4, 5, 10, 15, 20, or about 25 or more times. The carbon can also be replenished in whole or in part. It has been discovered that recycling or reusing the carbon can enhance metal nanostructure yields and adjust nucleation characteristics enabling change in element selectivity and resultant distributions. Thus, an aspect of the invention is to practice the method with recycled nanoporous carbon powder, e.g., a nanoporous carbon powder that has been previously subjected to a method of the invention one or more times. b. Nanoporous Carbon Compositions

The nanoporous carbon compositions produced by the processes described herein possess several surprising and unique qualities. The nanoporosity of the carbon powder is generally retained during processing and can be confirmed, for example, visually with a scanning electron microscope or modeled by BET analysis. Visual inspection of the powder can identify the presence of elemental nanostructures residing within and surrounding the nanopores. The nanostructures can be elemental metals or non-metals. Visual inspection of the powder can also identify the presence of elemental macrostructures residing within and surrounding the nanopores. The macrostructures can be elemental metals or nonmetals, and can contain interstitial and/or internal carbon, as generally described by Inventor Nagel in U.S. Patent 10,889,892 and U.S. Patent 10,844,483, each of which is incorporated herein by reference in its entirety. Methods for instantiating gases are described in USSN 63/241,697 by Inventor Nagel, which is incorporated herein by reference in its entirety.

Typically, the porosity of the nanoporous carbon compositions will be at least about 70% of the porosity attributed to ultramicropores of the nanoporous carbon powder starting, or charge, material and having a total void volume that is about 40% or more of the bulk material volume. The pores, or cavities, residing within the carbon particles can be macropores, micropores, nanopores and/or ultra-micropores. A pore can include defects in electron distribution, compared to graphene, often caused by changes in morphology due to holes, fissures or crevices, edges, comers, swelling, dative bonds, or other changes in surface chemistry, such as the addition of chemical moieties or surface groups, etc. For example, the spaces that may arise between layers of carbon sheets, fullerenes, nanotubes, or intercalated carbon are contemplated. It is believed that instantiation preferentially occurs at or within a pore and the nature of the surface characteristics can impact the deposit. For example, Micromeritics enhanced pore distribution analysis (e.g., ISO 15901-3) can be used to characterize the carbon. It is preferred that the carbon powder is nanoporous. Chemical reactant products or product compositions useful as fuels that are produced by the process can be isolated or harvested from nanoporous carbon compositions.

2. METHODS AND APPARATUS

Conceptually, the apparatus for baseline experimentation can be broken into two primary areas: Gas Processing and Reactor Assembly. a. Gas Processing:

The gas processing section controls gas composition and flow rate, with the optional embedding of electromagnetic (e.g., light) information or electromagnetic gas pre-treatment to the reactor.

The invention includes an electromagnetic embedding enclosure (E/MEE or EMEE), or apparatus, for processing a gas (feed gas or first gas composition, used interchangeably herein) comprising or consisting of: a central processing unit and power supply; one or more gas supplies; a housing having a housing inlet and housing outlet; an upstream gas line that is in fluid connection with each gas supply and the housing inlet; an internal gas line in fluid connection with the housing inlet and housing outlet; a downstream gas line in fluid connection with the housing outlet; at least one pencil lamp positioned below the internal gas line, at least one pencil lamp positioned above the internal gas line and/or at least one pencil lamp positioned to the side of the internal gas line; an optional short-wave lamp and/or a long wave lamp; and an optional coil wrapped around the internal gas line, operably connected to a frequency generator; wherein each lamp is independently rotatably mounted, located along the length of the internal gas line, and powered by the power supply; and wherein the central processing unit independently controls powering the frequency generator, if present, and each lamp and the rotation position of each lamp.

It will be understood that spatial terms, such as “above”, “below”, “floor” and “to the side” are relative to a particular specified object or other point of reference. Thus, a lamp, for example, that is positioned “above” a gas line takes its orientation from the gas line as reference point; if the gas line is positioned “above” the floor of the room in which the apparatus is housed, the lamp positioned “above” the gas line is also “above” the floor. A lamp that is positioned “above” the floor does not have a designated position with respect to a gas line that is also positioned “above” the floor unless the lamp’s position is also specified with reference to said gas line. In other words, if one were to draw X, Y and Z axes through a particular assembly or apparatus, the terms “above”, “below” and “to the side” is intended to only refer to positions relative to such axes and not as the axes would be drawn relative to the space or room in which the assembly resides.

Feed gases can preferably be research grade or high purity gases, for example, as delivered via one or more gas supplies, such as a compressed gas cylinder. Examples of gases that can be used include, for example and without limitation, air, oxygen, nitrogen, helium, neon, argon, krypton, xenon, ammonium, carbon monoxide, carbon dioxide and mixtures thereof. Preferred gases include nitrogen, helium, argon, carbon monoxide, carbon dioxide and mixtures thereof. Nitrogen, air and helium are preferred. In certain of the examples below, a highly purified nitrogen gas was used. The use of highly purified nitrogen gas facilitated product gas analysis. The feed gas can be added continuously or discontinuously, throughout the process. The gases can be free of metal salts and vaporized metals. One or more gases (e.g., 2, 3, 4, 5, or more gases) can optionally pass through a gas manifold comprising mass flow meters to produce a feed gas composition, also called the reactor feed gas. The reactor feed gas may then either by-pass an electromagnetic (EM) embedding enclosure (E/MEE) or pass through one or more E/MEEs. The E/MEE exposes the reactor feed gas to various electromagnetic field (EMF) sources. Flow rates, compositions, and residence times can be controlled. The rate of flow of the reactor feed gas can be between 0.01 standard liters per minute (SLPM) and 10 SLPM, or 100 SLPM or more. A constant flow of gas can maintain a purged environment within the reactor. The schematics shown in FIG. 1 depicts a flow path for the gases through a sample E/MEE. The sample E/MEE comprises a series of lights and coils that can optionally expose the reactor feed gas to EM radiation. EMF sources within the E/MEE can be energized simultaneously or in sequence or a combination thereof.

FIG. 1 is an illustration of an E/MEE of the invention for the production of gaseous chemical reactants. Gas enters the E/MEE via the inlet 101, or entrance, in line 102 and exits at the outlet, or exit, 110. The inlet 101 and outlet 110 may optionally have valves.

Line 102 can be made of a transparent or translucent material (glass is preferred) and/or an opaque or non-translucent material, such as stainless steel or non-translucent plastic (such as TYGON® manufactured by Saint-Gobain Performance Plastics) or a combination thereof. Using an opaque material can reduce or eliminate electromagnetic exposure to the gas as the gas resides within the line. The length of line 102 can be between 50 cm and 5 meters or longer. The inner diameter of line 102 can be between 2 mm and 25 cm or more. Line 102 can be supported on and/or enclosed within a housing or substrate 111, such as one or more plates, with one or more supports 112. For example, substrate 111 can be configured as a plane or floor, pipe, or box. Where the substrate is a box, the box can be characterized by a floor, a ceiling and side walls. The box can be closed to and/or insulated from ambient EM radiation, such as ambient light.

One or more lamps (such as 2, 3, 4, 5, 6, 7, 8, 9, 10 lamps or more) can be configured within the E/MEE. Lamps (numbered individually) are preferably pencil lamps characterized by an elongated tube with a longitudinal axis. The pencil lamps can independently be placed such that their longitudinal axes are (i) parallel to the line 102, (ii) disposed radially in a vertical plane to the line 102, or (iii) perpendicular to the plane created along the longitudinal axis of the line 102 or along the vertical axis of the line 102.

Each lamp can, independently, be fixed in its orientation by a support 112. Each lamp can, independently, be affixed to a pivot 113 to permit rotation from a first position. For example, the lamps can be rotated between about 0 and 360 degrees, such as about 45, 90, 135, 180, 225 or 270 degrees, preferably about 90 degrees relative to a first position. The rotation can be with respect to the x, y, and/or z axis wherein (i) the x-axis is defined as the axis parallel to the gas line and its vertical plane, (ii) the y-axis defining the axis perpendicular to the gas line and parallel to its horizontal plane, and (iii) the z-axis is defined as the axis perpendicular to the gas line and parallel to its vertical plane.

Referring to the specific pencil lamps within an E/MEE, line 102 is configmed along the E/MEE with gas flowing from the inlet 101 and exiting at the outlet 110. Lamp 103, a neon lamp, is first and is shown above line 102 oriented to be along the z-axis and perpendicular to line 102, with the tip of the lamp pointed towards line 102. Lamp 109, a krypton lamp, is shown below line 102 oriented to be parallel to the x-axis, with the tip pointing towards the outlet 110. Lamps 104 and 105, a long wave and short-wave lamp, respectively, are shown parallel to line 102 oriented to be along the x-axis with the tips pointing towards the inlet. Lamp 122, an argon lamp, is shown to be below line 102 oriented to be parallel to the x-axis, with the tip pointing towards the inlet 101 at approximately the same distance from the inlet as lamps 104 and 105. Lamp 106, a neon lamp, is downstream at about the midpoint of the E/MEE, is above line 102 with the tip pointing down. Lamp 107, a xenon lamp, is shown downstream of lamp 106 above line 102, parallel to the x axis of line 102 and points toward the outlet 110. Lamp 108, an argon lamp, is below line 102 and the tip is pointing toward line 102 along the z-axis. Optional coil 120 is wrapped around line 102. Each of these lamps can be independently rotated, for example, 90 degrees along any axis. Each lamp is connected to a power supply or power source to turn on or off the power. Each lamp can be independently rotated 1, 2, 3, 4 or more times during the process. For convenience, each lamp is held by a pivot that can be controlled by a central processing unit, such as a computer programmed to rotate the pivot and provide power to each lamp. For the ease of describing the experimental procedures, each orientation of each lamp is called “position n” wherein n is 0, 1, 2, 3, 4, or more. As the procedure is conducted, each lamp can be powered for specific periods of time at specific amperage(s) and positioned or repositioned.

In the exemplification described below, the initial bulb position for each lamp is described with a degree. A zero-degree (0°) reference point is taken as the 12 o’clock position on the glass pipe when looking down the gas pipe in the direction of intended gas flow (e.g., when looking at the E/MEE exit). The length of the glass pipe or line is taken as the optical length (e.g., in this instance 39 inches). For example, 6 inches from the end is defined as 6 inches from the optical end of pipe.

The lamps can be placed above, below, or to the side (for example, level with the longitudinal axis or a plane parallel to (above or below) the longitudinal axis), for example, of line 102. The lamps can be independently placed between 5 and 100 cm from the center of the line 102 in the vertical plane, as measured from the tip of the lamp to the center of line 102. One or more lamps can be placed in the same vertical plane along line 102, as illustrated by lamps 122, 104, and 105. Two lamps are in the same vertical plane if they (as defined by the tip or base of the lamp) are the same distance from the inlet 101. Preferably, lamp 105 can be placed in a plurality of (e.g., 2, 3, 4, 5 or more) vertical planes along the length of line 102 within the E/MEE. Further, one or more lamps can be placed in the same horizontal plane above, below or through line 102, as shown with lamps 104 and 105. Two lamps are in the same horizontal plane if they (as defined by the tip or base of the lamp) are the same distance from the center of line 102. Preferably, lamps can be placed in a plurality of (e.g., 2, 3, 4, 5 or more) horizontal planes along the length of line 102 within the E/MEE, as generally illustrated.

It is understood that “pencil lamps,” as used herein, are lamps filled with gases or vapor that emit specific, calibrated wavelengths upon excitation of the vapor. For example, pencil lamps include without limitation argon, neon, xenon, and mercury lamps. For example, without limitation, one or a plurality of lamps can be selected from argon, neon, xenon or mercury or a combination thereof. Preferably, at least one lamp from each of argon, neon, xenon, and mercury are selected. Wavelengths between 150 nm and 1000 nm can be selected. One example of a pencil lamp is a lamp characterized by an elongated tube having a tip and a base.

Long wave and/or short-wave ultraviolet lamps can also be used. Pencil lamps used in the E/MEE were purchased from VWR™ under the name UVP PEN RAY® rare gas lamps, or Analytik Jena in the case of the UV short wave lamps.

A power supply is operably connected to independently to each lamp, E/MEE coil, and frequency generator. The power supply can be AC and/or DC.

The E/MEE can be open or enclosed. Where the E/MEE is enclosed, the enclosure is typically opaque and protects the gas from ambient light. Without limitation, the enclosure can be made of a plastic or resin or metal. It can be rectangular or cylindrical. Preferably, the enclosure is characterized by a floor support.

In baseline experimentation the feed gas can by-pass the E/MEE section and are fed directly to the reactor assembly. The energy levels and frequencies provided by the EM sources can vary.

FIG. 4A provides a second illustration of an E/MEE of the invention. Gas enters the E/MEE at inlet 401 and exits at outlet 409 along line 410. Pencil lamp 402 and Pencil lamp 403 are shown parallel to and above line 410 along the vertical plane through line 410 axis. Pencil lamps 404 and 405 are parallel to and below line 410 in the same horizontal plane equidistant from the vertical plane through line 410. Pencil lamp 406 is shown above and perpendicular to line 410, positioned along the z axis. An optional coil 407 is a conductive coil wrapped around line 410. Pencil lamp 408 is shown below and perpendicular to line 410 along the y axis. Substrate 411 provides a base for supports 412. Pivots 413 control the position of each pencil lamp and permit rotation along axis x, y and z. An optional x-ray source 429 is also shown directed towards the coil 407. The coil 407 is preferably made of conducting material and is connected to a power supply and, optionally, a frequency generator. The coil can comprise copper, aluminum, platinum, silver, rhodium, palladium or other metals or alloys (including braidings, platings and coatings) and can optionally be covered with an insulating coating, such as glyptal. It can be advantageous to use a braid of 1, 2, 3 or more metal wires. The coil can be manufactured from wire typically used in an induction coil and can vary in size and the number of turns. For example, the coil can comprise, 3, 4, 5, 6, 7, 8, 9, 10 or more turns. The inner diameter of the coil can be between 2 cm and 6 cm or more and preferably snugly fits the line 410. An x-ray source 429 can included in the E/MEE. For example, the x-ray source can be directed at line 410 along the line between the inlet 401 and outlet 409. For example, it can be advantageous to direct the x-ray source at coil 407, where present. b. Reactor Assembly (RA):

The invention further relates to a reactor assembly comprising:

A gas inlet and one or more gas outlets;

A reactor chamber, preferably containing a nanoporous carbon material or powder;

A first porous frit defining a floor of the reactor chamber, A second porous frit defining the ceiling of the reactor chamber; wherein each porous frit has a porosity that is sufficient to allow a gas to permeate into the reactor chamber and contain a nanoporous carbon material;

An optional reactor cup defining side walls of the reactor chamber;

An optional reactor cap positioned above the second porous frit;

A reactor body disposed below the first porous frit;

A reactor head space disposed above the reactor cap;

An optional foil disposed between the reactor chamber and reactor cup;

One or more coils surrounding the reactor body and/or the reactor chamber operably connected to a power supply and/or frequency generator;

An optional x-ray source configured to expose the reactor head space to x-rays;

One or more optional lasers configured to direct a laser towards a frit and/or through the reactor chamber;

A computer processing unit configured to control the power supply, frequency generator, lamps, lasers, and x-ray source, when present.

The invention also includes a reactor assembly comprising:

A gas inlet and one or more gas outlets;

A reactor chamber, preferably containing a nanoporous carbon material;

A first porous frit defining a floor of the reactor chamber, A second porous frit defining the ceiling of the reactor chamber; wherein each porous frit has a porosity that is sufficient to allow a gas to permeate into the reactor chamber and contain a nanoporous carbon material;

A reactor head space disposed above the reactor cap;

2, 3, 4, 5 or more RA coils surrounding the reactor chamber and/or reactor head space operably connected to an RA frequency generator and power supply;

2, 3, 4, 5 or more pairs of lamps wherein the pairs of lamps are disposed circumferentially around the RA coils and define a space between the pairs of lamps and the RA coils;

An optional x-ray source configured to expose the reactor chamber to x-rays;

One or more optional lasers configured to direct a laser through the reactor chamber; and

A computer processing unit configured to control the power supply, frequency generator and the optional x-ray source and lasers.

As previously described, the terms “above,” “floor” and “ceiling” are intended to describe relational spatial features. “Floors” and “ceilings” are typically opposing sides of a space or volume where the head space is adjacent to the “ceiling” and distal to the “floor,” irrespective of the relational geometry to the room or space in which the apparatus resides. In other words, a “ceiling” represents a boundary wall or plane in an assembly confining a space or volume (generally understood as the “top” boundary of such space or volume), while the “floor” represents a boundary wall or plane opposite the ceiling in the same assembly confining the same space or volume (generally understood as the “bottom” boundary of such space or volume). Rotating the assembly on an axis by, for example, 45, 90 or 180 degrees, for example, does not change the relative position of the two planes or assemblies to each other, and such a rotated assembly can still include references to the ceiling or a floor structure thereof as these structures were identified in the assembly prior to such rotation.

The invention also includes a reactor assembly comprising:

A gas inlet and one or more gas outlets;

A reactor chamber, preferably containing a nanoporous carbon material;

A first porous frit defining a floor of the reactor chamber,

A second porous frit defining the ceiling of the reactor chamber; wherein each porous frit has a porosity that is sufficient to allow a gas to permeate into the reactor chamber and contain a nanoporous carbon material;

A reactor head space disposed above the reactor chamber;

An induction coil surrounding the reactor chamber and/or reactor head space operably connected to a power supply; and A computer processing unit configured to control the power supply. The reactor chamber can optionally contain a cap and/or cup to contain the carbon material.

As shown in FIGs 2A, 2B and 2C, the reactor assembly comprises a reactor body 202 and starting, or charge, material 204 (which is generally a nanoporous carbon powder) and is located downstream of the gas sources 221 and E/MEE 222, as shown in FIG. 2A. As described above, it is possible for reactor feed gas to bypass the E/MEE. The reactor body 202 can be a packed bed tubular micro-reactor surrounded by one or more conducting coils 208, as illustrated in FIG. 2A, FIG. 2B, and FIG. 2C. FIG. 2A and FIG. 2B show cross sections of the reactor assembly. The conducting coil 208 can be manufactured from electrically conducting material, such as, without limitation, copper, aluminum, platinum, silver, rhodium, palladium or other metals or alloys (including braidings, platings and coatings) and can optionally be covered with an insulating coating, such as glyptal. The coil can be manufactured from wire typically used in an induction coil and can vary in size and the number of turns. For example, the coil can comprise 3, 4, 5, 6, 7, 8, 9, 10 or more turns. The inner diameter of the coil can be between 2 cm and 6 cm or more and preferably snugly fits the reactor body containment 207. The wire used can have a diameter of between 5 mm and 2 cm.

Each conducting coil 208 (or coils) can generate inductive heat and, optionally, a magnetic field. Standard induction coils or reverse field induction coils (coils that have a lower and upper sections connected through an extended arm that allows the sections to be wound in opposite directions, thereby producing opposing magnetic fields) are preferred. The coil 208 can be water- cooled via a heat exchanger. The coil can be connected to a power flange 210, which can be water cooled as well and in turn can connect to a power supply, such as an Ambrell lOkW 150-400kHz power supply. In baseline experimentation a standard coil was used with simple copper windings. The windings can form a coil 208 such that the connection to the power supply is at opposite ends of the coil FIG. 5A or the coil can return such that the connection to the power supply is adjacent, as shown in FIG. 5B.

Referring to FIG. 2A, FIG. 2B, and FIG. 2C, the reactor assembly can optionally further comprise one or more coils 208, preferably surrounding the reactor body and its containment system. For example, the reactor assembly can comprise 1, 2, 3, 4, 5, 6, 7, 8, 9, or 10 or more coils, also called RA coils. As shown in FIG. 2B, one or more electromagnetic (E/M) coils can be used to provide magnetic fields. Preferably, 1, 2, 3, 4, or 5 or more E/M coils can be used, more preferably 3, 4, or 5 E/M coils. FIG. 3A-3E shows groupings of three coils, for example, which can generally be numbered 1, 2, or 3, from top to bottom. A grouping of coils, as shown in FIG. 3A-3E, can be called a boundary. Where a plurality of groupings is used, the number of coils used is independently selected. Further, the groupings can be equidistantly spaced along or irregularly spaced. Coils can be manufactured from electrically conducting materials, such as, without limitation, copper, platinum, silver, rhodium, palladium and, wire braids or coated wires of two or more materials. Each coil in a grouping may be made of the same material or different. For example, a grouping can be made such that each coil is made of a different material. For example, a braiding of copper wire and silver wire can be used. Silver plated copper wire can be used. A first RA coil can be made of a copper winding. A second RA coil can be a copper/silver braid. A third RA coil can be a platinum wire winding. An RA coil can be configured to create a magnetic field and wherein each power supply independently provides AC and/or DC current. Any one or all RA coils can be optionally lacquered.

The coils are preferably circular in geometry. However, other geometries, such as, without limitation, rounded shapes, ellipses and ovoids can be used. The wire diameter can be between about 0.05 mm (> about 40 gauge) and about 15 mm (about 0000 gauge) or more. For example, the wire diameter can be between about 0.08 mm (about 40 gauge) and about 0.8 mm (about 20 gauge) wire. Excellent results have been obtained using 0.13 mm (36 gauge) wire. Coils can be wire windings (e.g., the wire can be wound in 1, 2, 3, 4, 5, 6, 7, 8, 9, 20, or more turns or can be a single turn. In this context, a “wire” can also be considered a band where the width of the material is greater than the depth. FIGS. 3A-C provide illustrations or views of various coils and groupings of coils. A wire coil can be made of a single wire, a wire alloy or two or more wires. For example, two wires comprising different metals can be wound or braided together.

The inner diameter (or dimension(s) where the coil is not a circle) of each coil can be the same or different and can be between 2 and 200 cm.

Coils 208 can independently be connected to one or more power supplies, such as an AC or DC power supply or combination thereof. For example, an AC current can be supplied to alternating (1, 3, and 5, for example) or adjacent coils (1, 2 and/or 4, 5, for example) while DC current is supplied to the remaining coils. Current can be provided (independently) in a frequency, such as in a patterned frequency, e.g., triangle, square or sine pattern or combination thereof. The frequency supplied to each coil can be the same or different and between 0 to 50 MHz or higher. While the coils 208 can generate and transfer thermal energy, or heat, to the reactor feed gas they are predominantly used to create a magnetic field.

The power supply can be an AC and/or DC power supply or combination thereof. Current can be provided (independently) in a frequency, such as in a patterned frequency, e.g., triangle, square or sine pattern or combination thereof. The frequency supplied to each coil can be the same or different and between 0 to 50 MHz or higher, such as between 1 Hz to 50 Mhz.

As described above, the RA coils typically surround the reactor chamber and/or reactor head space. For example, a first RA coil can be aligned with the first (or bottom) frit. A second RA coil can be aligned with the reactor chamber or nanoporous carbon bed. A third RA coil can be aligned with the second (or top) frit. Where present, a fourth RA coil can be disposed between the first RA and the second RA coil. When present, a fifth RA coil can be disposed between the second RA coil and third RA coil. When two or more reactor chambers, or nanoporous carbon beds are present, it can be desirable to add additional RA coils, also aligned with a second or additional reactor chambers or nanoporous carbon beds. Additional RA coils can be added to align with additional frits when present.

The RA coils can typically be supported in a support or stator to maintain a fixed distance between each coil. The support, when present, can be transparent. In one embodiment, the RA coils can be configured in a cartridge that can be removed or moved.

The RA coils can, additionally or alternatively, be aligned with the reactor headspace. The reactor headspace can typically be a volume above the second, or top, frit. It is understood that where the reactor assembly is positioned horizontally (or at some other angle than vertical), the geometry of the spaces is maintained, albeit rotated. The reactor headspace can typically be an enclosed volume. For example, the reactor assembly can be inserted into a closed ended transparent (e.g., glass) tube, vial, or bottle. The reactor assembly can be movably engaged with the RA coils (or boundary), thereby permitting each RA coil to align to a different element within the reactor assembly. For example, the first RA coil can be realigned with the reactor chamber.

Referring to FIG. 2A, FIG. 2B, and FIG. 2C, a reactor body 202 can also be a packed, moving, or fluidized bed or other configuration characterized by one or more chambers that receive the charge material 204 and facilitates transfer of a reactor feed gas through the charge material 204 and can transfer thermal and/or electromagnetic energy to the charge material 204. The reactor chamber is sized to contain the desired amount of charge material 204. For the experiments described herein, the chamber is designed to contain between 20 mg to 100 grams of nanoporous carbon powder. Larger reactors can be scaled up.

The reactor body 202 is generally contained within a housing, e.g., closed end tube, 207 and frits 203, which function to contain the charge material 204. It can be advantageous to use a reactor within a translucent or transparent housing, such as quartz or other materials characterized by a high melting point. The volume of the reactor bed can be fixed or adjustable. For example, the reactor bed can contain about 1 gram, or less of starting material, between about 1 g to 1 kg of starting material or more. Where the reactor assembly comprises two or more reactor chambers, the reactor chambers are preferably directly or indirectly stacked, preferably having a common central axis, and can be separated by one or two frits.

The reactor body 202 can, for example and without limitation, be made of a thermally conductive material, such as graphite, copper, aluminum, nickel, molybdenum, platinum, iridium, cobalt, or niobium, or non-thermally conducting material, such as quartz, plastic (e.g., acrylic), or combinations thereof. An optional cup 206 capped with cap 205 can be advantageous. The cup and cap material can be independently selected. For example, a graphite cup can be combined with a graphite cap, which is the selection for the examples below. A copper cup can be combined with a graphite cap. A graphite cup can be combined with a copper cap. A copper cup can be combined with a copper cap and so on.

The reactor assembly can also receive the gas line through the entrance, or inlet, 201 and to provide an exhaust through an exit, or outlet, 209, optionally controlled by valves. A head space defined by a closed end tube 207 can be configured above the reactor body. The reactor body is preferably made of graphite, copper, or other inorganic rigid material. The gas line is preferably made of an inert tubing, such as glass, acrylic, polyurethane, plexiglass, silicone, stainless steel, and the like can also be used. Tubing can, optionally, be flexible or rigid, translucent or opaque. The inlet is generally below the charge material. The outlet can be below, above, or both.

Frits 203 used to define the chamber containing the charge material are also shown. The frits can be made of a porous material which permits gas flow. The frits will preferably have a maximum pore size that is smaller than the particle size of the starting material. Pore sizes of between 2 and 50 microns, preferably between 4 and 15 microns can be used. The thickness of the frits can range satisfactorily between approximately 1 and 10 mm or more. The frits are preferably made of an inert material, such as silica or quartz. Porous frits from Technical Glass Products (Painesville Tp., Ohio) are satisfactory. On the examples below, fused quartz #3 porous frits (QPD10-3) with a pore size between 4 and 15 microns and a thickness of 2-3 microns and fused quartz frits with a pore size between 14 and 40 microns (QPD10-3) were used. The purity of the frits exemplified herein was very high, 99.99%wt, to ensure that the results obtained cannot be dismissed as the result of contamination. Frits of lower purity and quality can also be used. The diameter of the porous frit is preferably selected to permit a snug fit within the reactor interior, or cup. That is, the diameter of the porous frit is approximately the same as the inner diameter of the reactor or cup, if present.

FIG. 6A and 6B are illustrations of two examples of two composite reactor assemblies. FIG. 6A illustrates a Composite Reactor with a copper reactor body 606, carbon graphite cup 605, and a carbon graphite cap 601 and a metal foil boundary 607. FIG. 6B illustrates a Composite Reactor with a carbon graphite reactor body 606 and cap 601 and metal foil boundary 607. The embodiments depicted in FIG. 6A and FIG. 6B show a top frit 602 and a bottom frit 604, with a graphite bed 603 therebetween. Referring to FIG. 6A and 6B, a foil 607 can optionally encase the chamber containing the charge material on the inside and/or outside of the frits 602, 604 and/or cup 605, thereby creating a metal boundary surrounding the starting material. The foil 607 can be a metal, such as copper, platinum, niobium, cobalt, gold, silver, or alloys thereof. The foil 607 can also be graphite or the like. The foil 607 can be between 0 and 0.5 cm thick, preferably 1-10 mm. The profile of the reactor can be linear, or it can be configured to contain a constriction below the lower frit, providing the general appearance of a lollipop.

The reactor assembly may be augmented with additional forms of electromagnetic radiation, such as light. FIG. 4B exemplifies light sources 426 and 427 that generate light directed through the reactor housing 415 and starting material contained therein. Preferred light sources 426 and 427 can be lasers and/or can emit light in a wavelength between 10 nm and 1 mm. The light is optionally subjected to one or more filters 428, as shown in the use of light sources (beams) in FIG. 4B. Preferably, the reactor assembly comprises 2, 3, 4, 5 or more pairs of lamps disposed circumferentially around the RA coils. Pencil lamps, such as the lamps used within the E/MEE, which is incorporated herein by reference from above, are preferred. The pairs of lamps preferably define a boundary surrounding the coil and are not touching or otherwise adjacent to the coils. Two lamps are considered paired where they are proximal to each other, such as within the same plane with the center axis of an RA coil. Paired lamps can be parallel or orthogonal to each other and the RA coil center axis. Lamps can be considered proximal to each other if the space between any two points between the lamp tip and base is within 10 cm, preferably within 5 cm. Lamps that are positioned orthogonally to the RA coil center axis are generally positioned along the line defined by the radius of one or more RA coils.

The RA lamps, e.g., the pencil lamps proximal to the reactor body, can be matched, or paired, to one or more E/MEE lamps, e.g., the pencil lamps residing within the E/MEE housing and proximal to the gas line. For example, where an E/MEE pencil lamp is a neon lamp, a pair of RA lamps can be neon pencil lamps. Additionally, where an E/MEE pencil lamp is a neon lamp, a pair of RA lamps can be neon pencil lamps. Such matched lamps can emit light characterized by substantially the same wavelength. This can be conveniently achieved by using lamps from the same manufacturer with the same specifications.

The reactor can be in a closed or open housing 415 and can be supported therein by reactor supports. The reactor feed gas is directed to the reactor inlet frit, or bottom frit, directed through the starting material contained within the housing 415 and exits the reactor at the reactor exit frit, or top frit. The reactor feed gas can then be exhausted or recycled, optionally returning to the E/MEE for further treatment.

The reactor can further comprise an x-ray source 211 (FIG. 2C) or 424 (FIG. 4B) and/or one or more lasers 212 (FIG. 2C) or 426 and 427 (FIG. 4B). Preferred x-ray sources include a mini-x. The x-ray is preferably directed through the reactor towards a gas headspace, or target holder 213 (FIG. 2C), above the charge material. The x-ray can be directly or indirectly provided from the source, such as by reflecting the x-ray from a foil disposed above or below a frit. FIG. 7A illustrates a top view of a preferred reactor assembly. Pencil lamp 1501, pencil lamp 1502 and pencil lamp 1503 are shown with the tip directed towards a center axis of the reactor assembly along a radius of the reactor assembly. Pencil lamp 1504, pencil lamp 1505 and pencil lamp 1506 are shown directed parallel to a center axis of the reactor assembly and are disposed in a plane along a radius of the reactor assembly. Pencil lamp 1501, together with pencil lamp 1504, form a first RA lamp pair. Pencil lamp 1502, together with pencil lamp 1505, form a second RA lamp pair. Pencil lamp 1503, together with pencil lamp 1506, form a third RA lamp pair. As with the E/MEE pencil lamps, each RA lamp can be rotated along its x, y or z axis. Each pair can optionally reside within the same radial plane, as shown. Outer support 15109 provides support for the pencil lamps 1501, 1502 and 1503. Inner support 15110 provides support for the pencil lamps 1504, 1505 and 1506. The outer and inner supports are preferably made of non-conductive materials (such as polymers or resins) and are preferably transparent. An optional x-ray source 1507 is shown directing x-rays towards the center axis of the reaction chamber 1508. Reactor connector 15111 is also shown.

FIG. 7B is a perspective view of this reactor assembly. Pencil lamp 1509, pencil lamp 1510 and pencil lamp 1511 are shown directed with the tip towards a center axis of the reactor assembly along a radius of the reactor assembly. The tip of each lamp aligns with the center, or third, RA coil 1517 and is in the same horizontal plane. Pencil lamp 1512, pencil lamp 1513 and pencil lamp 1514 are shown directed parallel to a center axis of the reactor assembly, disposed in a plane along a radius of the reactor assembly and is charaterized by a tip pointing towards top of the reactor, away from the gas inlet 1520. These lamps are illustrated above the horizontal pencil lamps. The length of each pencil lamp align with RA coils 1516, 1517 and 1518. Outer support 15109 and inner support 15110 support the pencil lamps. An optional x-ray source 1515 is shown directing x-rays towards the center axis of the reactor assembly above the third RA coil 1516. Disposed within the reactor assembly can be a reflecting plate to direct the x-ray towards the reaction chamber. Reactor connector 15111 is also shown, as well as other non-material connectors and spacers. Gas inlet 1520 and gas outlet 1519 are also shown.

FIG. 7C is a second perspective view of a reactor assembly. Pencil lamp 1521, pencil lamp 1522 and pencil lamp 1523 are shown directed with the tip towards a center axis of the reactor assembly along a radius of the reactor assembly. Pencil lamp 1524, pencil lamp 1525 and pencil lamp 1526 are shown directed parallel to a center axis of the reactor assembly, disposed in a plane along a radius of the reactor assembly and is charaterized by a tip pointing towards the bottom of the reactor, towards the gas inlet 1532. These vertical lamps are shown above the horizontal lamps and, again, each pair of lamps can optionally lie in the same radial plane. The tip of each pencil lamp aligns with the third RA coil 1528. Outer support 15109 and inner support 15110 support the pencil lamps. Three RA coils 1528, 1529 and 1530 are shown. An optional x-ray source 1527 is shown directing x- rays towards the center axis of the reactor assembly. Disposed within the reactor assembly can be a reflecting plate to direct the x-ray towards the reaction chamber. Reactor connector 15111 is also shown, as well as other non-material connectors and spacers. Gas inlet 1532 and gas outlet 1531 are also shown.

FIG. 7D is a cross sectional side view of the reactor assembly, stripped of the pencil lamps and x-ray source. Gas enters at the inlet 1541 and exits at the outlet 1540. RA coils 1537, 1538 and 1539 are shown. The first, or bottom, frit 1535 and the second, or top, frit 1533 contain the reaction chamber 1534, which can be charged with nanoporous carbon powder. The reactor body 1536 is also shown. Other non-material spacers and connectors remain unlabeled.

FIG. 7E is a second cross sectional side view of a reactor assembly, stripped of the pencil lamps and x-ray source. Gas enters at the inlet 1551. RA coils 1545, 1546 and 1547 are shown. The first, or bottom, frit 1544 and the second, or top, frit 1542 contain the reaction chamber 1543, which can be charged with nanoporous carbon powder. The reactor body 1548 is also shown. X-ray source 1549 directs x-rays towards the center axis of the reactor assembly which is then deflected towards the reactor chamber with element 1550. Other non-material spacers and connectors remain unlabeled.

FIG. 7F is a second cross sectional side view of a reactor assembly with the pencil lamps and x-ray source. Gas enters at the inlet 1564. RA coils 1555, 1556 and 1557 are shown. The first, or bottom, frit 1554 and the second, or top, frit 1552 contain the reaction chamber 1553, which can be charged with nanoporous carbon powder. The reactor body 1558 is also shown. Vertical pencil lamps 1560 and 1561 are shown as are horizontal pencil lamps 1560 and 1559. X-ray source 1562 directs x-rays towards the center axis of the reactor assembly which is then deflected towards the reactor chamber with element 1563. Other non-material spacers and connectors remain unlabeled.

FIG. 7G is a perspective view of a reactor assembly with the pencil lamps and x-ray source. Gas enters at the inlet 1577 and exits at outlet 1578. A first laser 1575 and a second laser 1576 directing radiation towards the reaction chamber along the axis of the reactor assembly is shown. RA coils 1571, 1572 and 1573 are shown. In this embodiment, pencil lamps 1565, 1566, 1567, 1568, 1569, and 1570 are all shown horizontally disposed in pairs along the radius towards the reactor assembly central axis. Tips are proximal to RA coils 1571, 1572 and 1573. X-ray source 1574 directs x-rays towards the center axis of the reactor assembly. Support 15109 (FIG. 7A) supports all of the horizontal pencil lamps. Other non-material spacers and connectors remain unlabeled.

FIG. 7H is a perspective view of a reactor assembly with the pencil lamps and x-ray source. Gas enters at the inlet 1591 and exits at outlet 1592. A first laser 1589 and a second laser 1590 directing radiation towards the reaction chamber along the axis of the reactor assembly is shown. RA coils 1585, 1586 and 1587 are shown. In this embodiment pencil lamps 1579, 1580, 1581, 1582, 1583, and 1584 are all shown vertically disposed in pairs in radial planes aligned with the RA coils. Tips are proximal to RA coils 1585, 1586 and 1587. X-ray source 1588 directs x-rays towards the center axis of the reactor assembly. Supports 15109 and 15110 support the pencil lamps. Other nonmaterial spacers and connectors remain unlabeled.

FIG. 71 is a perspective view of a reactor assembly illustrating 5 RA coils, horizontal pencil lamps and an x-ray source. Gas enters at the inlet 15107 and exits at outlet 15108. A first laser 15105 and a second laser 15106 directing radiation towards the reaction chamber along the axis of the reactor assembly is shown. RA coils 1599, 15100, 15101, 15102 and 15103, defining a cyndrical boundary, are shown. In this embodiment pencil lamps 1593, 1594, 1595, 1596, 1597, and 1598 are all shown horizontally disposed in pairs in radial planes aligned with the RA coils. Tips are proximal to RA coils 1599 and 15103. X-ray source 15104 directs x-rays towards the center axis of the reactor assembly. Support 15109 supports the pencil lamps. Other non-material spacers and connectors remain unlabeled. i. Ni-1 Reactor:

Referring to FIG. 8A, the reactor body (1702) is based on a high purity nickel (Ni) rod. The Ni rod, with an outside diameter of 15.873 mm (OD) is bored through then machined with a female thread on one end. The inside diameter allows for the installation of upper and lower frit and carbon bed. The carbon reaction medium is housed inside the reactor body (1702). To load the reactor, the reactor body (1702) is positioned with the gas discharge opening (1706) facing down on a flat surface. A quartz frit (1705) is placed inside the reactor body (1702) to form the upper containment. 100 mg of carbon is then loaded into the reactor body (1702). After loading of the graphite bed inside the reactor body (1702), a second quartz frit (1703) is installed. A reactor pole (1701), machined out of a high purity graphite rod with matched male threads for the reactor body (1702), is then screwed onto the reactor body (1702).

The reactor pole (1701) is designed to allow and provide for graphite bed compression (1704) equivalent to that provided by the cup design (1710 in FIG. 8B and 1717 in FIG. 8C). ii. NiPtG Reactor:

Referring to FIG. 8B, in the NiPtG Reactor embodiment, the reactor body (1707) is based on a high purity nickel (Ni) rod. The Ni rod, with an outside diameter of 15.873 mm (OD) is bored through then machined on one end to have an inside diameter of 11.68 mm (ID). The inside diameter allows for the installation of a graphite cup (1708) and an optional 0.025 mm platinum (Pt) foil (1713). The graphite cup provides for reactor wall and foil isolation from the carbon bed. The carbon reaction medium is housed inside a 99.9999 _wt % pure graphite cup (1708). To load the reactor, a quartz frit (1709) is placed inside the graphite cup (1708) to form the bottom containment. 100 mg of carbon (1710) is then loaded into the cup (1708). After loading of the graphite bed inside the cup, a second quartz frit (1711) is installed; this system is defined as the cup assembly. Prior to installing the cup assembly, the foil (1713) is used to line the inside surface of the reactor wall. The cup assembly is then placed within the nickel reactor body (1707) and foil (1713). After the cup assembly is installed, a 99.9999 _wt % pure graphite cap (1712) is screwed onto the reactor body. The cap secures the cup from movement after assembly. iii. PtlrGG Reactor:

Referring to FIG. 8C, the reactor body (1714) is based on a high purity graphite rod. The graphite rod, with an outside diameter of 15.873 mm (OD) is bored through then machined on one end to have an inside diameter of 11.68 mm (ID). The inside diameter allows for the installation of a graphite cup (1715) for reactor wall isolation from the carbon bed. The carbon reaction medium is housed inside a 99.9999 _wt % pure graphite cup (1715). To load the reactor, a quartz frit (1716) is placed inside the graphite cup to form the bottom containment. 100 mg of carbon (1717) is then packed into the cup. After loading of the graphite bed inside the cup, a second quartz frit (1718) is installed; this system is defined as the cup assembly. The cup assembly is then placed within the graphite reactor body (1714). After the cup assembly is installed, a cap (1719) composed of platinum and 10%wt iridium is screwed onto the reactor body. The cap secures the cup from movement after assembly.

The residence time of the starting material within the reactor is effective to instantiate, or filter, or isolate, or extract, or nucleate, product into the starting material and can be between 0 and 15 minutes or more.

Preferred reactors used in the methods of the invention are shown in the table below.

Table 1:

The invention further relates to methods of instantiating materials in nanoporous carbon powders. It has been surprisingly found that light elements, such as hydrogen, oxygen, helium, and the like are instantiated, or fdtered, or isolated, or extracted, or nucleated. Instantiating is defined herein to include the nucleation and assembly of atoms within carbon structures, particularly, ultramicropores, and it includes without limitation processes such as filtering, or isolating, or extracting, or nucleating such atoms. Without being bound by theory, it is believed instantiation is related to, inter alia, degrees of freedom of the electromagnetic field as expressed by quantum field theory. By exposing a gas to harmonic resonances, or harmonics, of electromagnetic radiation within one or more ultramicropores, vacuum energy density is accessed and allows for the nucleation and assembly of atoms. Electromagnetic energy that is within the frequencies of light, x-rays, and magnetic fields subjected to frequency generators can enhance the formation and maintenance of such harmonics. Modifying the boundaries of the system, by selecting the reactor materials and adding a foil layer can also enhance the harmonics.

In particular, the invention includes processes of producing, or instantiating, nanoporous carbon compositions comprising the steps of: adding a nanoporous carbon powder into a reactor assembly as described herein; adding a feed gas to the reactor assembly; powering the one or more RA coils to a first electromagnetic energy level; heating the nanoporous carbon powder; harmonic paterning the nanoporous carbon powder between a first electromagnetic energy level and a second electromagnetic energy level for a time sufficient to instantiate, or filter, or isolate, or extract, or nucleate, a chemical reactant in a nanopore and, optionally, collecting the chemical reactant.

The invention includes a process for producing a chemical reactant comprising the steps of:

(a) adding a feed gas to an electromagnetic embedding apparatus:

(b) exposing the feed gas to at least one E/MEE light source;

(c) directing the feed gas from step (b) to a reactor assembly comprising:

A gas inlet and one or more gas outlets;

A reactor chamber containing a nanoporous carbon disposed within a cup and, optionally, covered with a cap;

A first porous frit defining a floor of the reactor chamber disposed within the cup, A second porous frit defining the ceiling of the reactor chamber; wherein each porous frit has a porosity that is sufficient to allow a gas to permeate into the reactor chamber;

A reactor head space disposed above the reactor chamber;

At least one RA coil surrounding the reactor chamber and/or reactor head space operably connected to a power supply, wherein the computer processing unit is configured to control the power supply to the RA coil;

(d) subjecting the nanoporous carbon powder to harmonic paterning to instantiate, or filter, or isolate, or extract, or nucleate, the chemical reactant integrated within a product composition;

(e) collecting the product composition comprising the chemical reactant; and

(f) isolating the chemical reactant from the product composition.

The term “harmonic paterning” is defined herein as oscillating between two or more energy levels (or states) a plurality of times. The energy states can be characterized as a first, or high, energy level and a second, or lower, energy level. The rates of initiating the first energy level, obtaining the second energy level and re-establishing the first energy level can be the same or different. Each rate can be defined in terms of time, such as over 1, 2, 3, 4, 5, 6, 7, 8, 9, 10 or more seconds. Each energy level can be held for a period of time, such as 1, 2, 3, 4, 5, 6, 7, 8, 9, 10 or more seconds. Harmonic paterning is continued until instantiation is achieved.

Where two more electromagnetic radiation sources are present (e.g., coils, x-ray source, lasers, and/or lamps), each can be subjected to harmonic paterning and the paterning can occur independently, simultaneously or sequentially.

The process further comprises independently powering any additional electromagnetic radiation source, as described above in the E/MEE apparatus or reactor assembly. For example, the process further comprises the step(s) of powering RA frequency generator(s) connected to one or more RA coils, one or more lamps or lasers, x-ray sources, induction coils, E/MEE coils, and the like substantially as described above. c. Use Cases for Chemical Reactants

Methods and and apparatus for producing chemical reactants in accordance with these inventions can be appreciated in more detail by reference to the following description and Figures. i. General Use Cases

In general terms, a reactor assembly (RA) as disclosed herein can interface with a system within which a chemical reaction can take place, which chemical reaction utilizes the chemical reactant(s) produced by the RA. Such a system for utilizing chemical reactants to support chemical reactions can be termed a “reaction system,” (RS) and it can comprise an apparatus or enclosure within which a chemical reaction takes place. The term “reaction system” is not limited to closed vessels for reactions, since it is understood that certain chemical reactions such as flame combustion do not require a closed system, but can occur in “the open.” As described previously, a RA produces a chemical reactant that can be supplied to a RS; one or more RAs can produce one or more chemical reactants, to be used by one or more RSs.

In the exemplary embodiment, shown schematically in FIG. 9, a plurality of RAs, (RA-1, 12 and RA-2, 14) can produce the same or different substances, to be supplied to RS 10. As an example, one RA can produce a chemical reactant useful as a fuel (e.g., H ₂ ), while the other RA can produce a chemical reactant useful as an oxidizing agent (e.g., O ₂ ). The RAs producing the fuel are also termed “fuel RAs.” These chemical reactants can be conveyed into the RS 10, where the designated reaction takes place, advantageously producing energy or other reaction products that can be beneficially employed. RAs such as RA-1 (12) and RA-2 (14) are capable of instantiating a desired chemical substance(s) or mixture of chemical substances, including but not limited to simple mono-elemental atoms and molecules (e.g., alkali metals such as Na, alkaline earth metals such as Ca, H ₂ , O ₂ , halogen molecules such as Cl ₂ , etc.), simple multi-elemental molecules comprising at least two elements (e.g., CO, NH ₃ or H ₂ O ₂ , etc.), or complex multi-elemental molecules comprising at least two elements in various distinguished configurations (e.g., hydrocarbons, carbohydrates, alcohols, etc.). As depicted in FIG. 9, the RAs 12 and 14 can be coupled to any RS apparatus 10 that can immediately, or almost immediately, or at other timing, consume the chemical substance(s) (such as fuel(s)) through combustion or other chemical reaction.

Depending on the particular embodiment, the RS 10 acting as a “fuel-sink” can be, without limitation: (i) any fuel-consuming apparatus, such as a thermal apparatus that converts fuel to heat, alone or in combination with (ii) an engine that converts fuel to mechanical energy; (iii) a fuel-cell that converts fuel to electricity; (iv) any other apparatus that consumes a chemical substance; (v) any fuel-storage facility such as a tank or other container that stores the fuel; (vi) any reactant- transformation process that uses a chemical reactant as a feedstock or precursor in the production of other chemicals or materials, or any combination of the foregoing.

As depicted in FIG. 9, the RAs 12 and 14 can be coupled to any RS apparatus 10 that can immediately, or almost immediately, or at other timing, consume the chemical substance(s) such as fuel(s) through combustion or other chemical reaction. These various dispositions of chemical substances such as fuels/reductants or oxidants can be generalized by the concept of "fuel/reductant sink" and "oxidizer sink". Accordingly, the output(s) of such RA(s) 12, 14 in some embodiments is/are directed through a "conduit" to a "fuel sink" or an "oxidizer sink" which receives the fuel/reductant or oxidizer and processes it. Depending on the particular embodiment, the RS 10 acting as a “fuel-sink” can be any fuel-consuming apparatus such as for an example an engine that converts fuel to mechanical energy; or a furnace that converts fuel to heat; or other apparatus that consumes a chemical substance.

Systems incorporating one or more RAs in communication with one or more RSs can include one or more fuel consumers, one or more fuel retainers and one or more fuel transformers. For example, RAs 12 and/or 14 can be coupled to a storage facility apparatus whereby the chemical substance(s) (e.g., a fuel) can be retained for use elsewhere or later; or can be moved through a conduit for other processing such as being used as a feedstock or precursor to the production of other chemicals.

In embodiments, a plurality of RAs can be harnessed to form an integrated system delivering appropriate quantities of chemical reactants to a RS in order to achieve a desired reaction. Such a system is illustrated in FIG. 10. FIG. 10 depicts a series of RAs 500(l-n) that supplies a chemical substance such as a fuel to a RS 10 via a conduit 600. In the example shown, "N" RA(s) 500(1), 500(2), ... , 500(N) (where N is any positive integer) can be configured to assemble the fuel or fuel mixture in sufficient quantities appropriate for the fuel sink and deliver the fuel to the fuel sink, i.e., RS 10.

In the depicted example, "M" RAs(s) 900 (where M is zero or any positive integer) can be configured to assemble a second chemical substance, such as a chemical reactant (e.g., an oxidant) appropriate for the fuel sink and deliver the chemical substance to the fuel sink, i.e., RS 10. It is understood that the RA bank or set 900(1) -900(M) is optional, to be used in systems where a second chemical substance is to be provided to the RS in addition to the chemical substance produced by the RA bank or set 500(1) - 500(n). Any number of additional RAs or banks or sets of RAs can be provided to supply any number of and quantity of chemical substances individually, alternately, simultaneously or in any desired mixtures or ratios, to RS 10.

The chemical substances produced by RAs 500, 900 are supplied to RS 10 via one or more conduits 600, 600’. Thus, as material moves between points it is said to move through a “conduit”. Examples of such materials include without limitation: hydrogen, ammonia (NH ₃ ), hydrocarbons, alcohols (as fuels); oxygen, ozone, hydrogen peroxide (H2O2), (as oxidants); helium, xenon, argon, krypton, (as elements to moderate or buffer the reaction); nitrogen, other gases, fuels, oxidizing agents, boron, calcium, aluminum, and any other elements or compounds used within the system. Depending on an implementation’s design and engineering constraints, a “conduit” may vary from being a trivial, almost abstract, connection to a complicated path in which a number of operations are performed, sometimes conditionally, on the subject material. Such operations may include, for example and without limitation, being: pumped, collected, combined, e.g., combined with the output of other conduits or sources, pressurized, compressed, liquefied, solidified, stored, packaged, transported, hauled, unpackaged, repackaged, gasified, uncompressed, depressurized, filtered, mixed, agitated, centrifuged, shaken, oscillated, stirred, vibrated, gated, shunted, injected, diverted, merged, blown, aerated, propelled, spun, blended, dissolved, extracted, sensed, tested, humidified, dehumidified, monitored, measured, regulated, accumulated, cooled, heated, or otherwise processed. Such operations may involve the use of components including for example and without limitation: pumps, sensors, gates, shunts, injectors, valves, baffles, pipes, splitters, plumbing, relays, filters, controls, accumulators, tanks, containers, reservoirs, fans, blowers, propellers, impellers, aerators, agitators, oscillators, vibrators, shakers, stirrers, centrifuges, pressurizers, humidifiers, dehumidifiers, compressors, refrigerators, blenders, mixers, vats, dissolvers, extractors, coolers, heaters, gasifiers, liquefiers, and sensors and controls for flow, humidity, concentration, density, purity, particle size, particle diameter, particle surface area, particle weight, viscosity, temperature, volume, and pressure, as well as other sensors and controls and processing equipment. Each operation may be performed zero or more times, sometimes simultaneously, and the order in which they are performed (and whether they are appropriate or necessary) depends on a particular implementation's design, tradeoffs, and constraints. Conduits may also be used to route power and signal cables. A conduit 600, 600’ may thus without limitation comprise a single pipe or other structure capable of conducting fluids (preferably gases), a conveyor for conducting powders or solids, a blower system for moving powders or gas. a manifold that couples the outputs of multiple RAs 500 together as a bank or set of RAs, a mixer that mixes the outputs of multiple RAs together, or any other suitable structure for conveying outputs of RAs 500 to RS 10. As shown in FIG. 10, a conduit can act as a fuel intake manifold for delivering the instantiated chemical reactants to the RS 10. The conduit(s) 600, 600’ may also convey fuel supplied by another fuel source(s), for example, a storage tank or other production process such as e.g., electrolysis. Such additional source(s) could be used in some embodiments and/or under some operating conditions in addition to RA(s) 500, 900 to provide sufficient fuel quantities and/or flow rates and/or combinations to meet demands of the RS 10. For example, RA(s) 500, 900 may operate for an extended period of time to develop substances for storage in storage tanks, and RS 10 may later consume the substances stored in the storage tanks. Delivery of chemical reactants from RAs to the one or more RSs can be coordinated by control systems that monitor aspects of the overall system, and that regulate the flow of materials through the different components of the overall system. In the embodiment depicted in FIG. 10, aspects of each RA 500, 900 are monitored and regulated by processor 100 through bus 300/300’, which may comprise a digital data bus in one embodiment. The various monitored aspects may include, without limitation, power, temperature, humidity, configuration, pressure, flow, concentration, viscosity, density, purity, particle dimension, and any other relevant state or parameter; together with the operation of fans, blowers, oscillators, pumps, valves, reservoirs, accumulators, pressurizers, compressors and/or other devices used to support the processes shown.

The processor 100 may also send signals over bus 300/300’ to control aspects of the state and operation of each RA 500, 900 such as flow control, output rate, and any other relevant state, parameter or characteristic. As shown in FIG. 10, computer processor 100 provides an electronic controller that senses, monitors, coordinates, regulates, and controls the various aspects of chemical substance production and usage. Processor 100 is connected as needed (120, 140, 180, 300, 300’, 400, 400’, etc.) to other various components (200, 500, 900, 670, 670’, 10) to receive sensor input signals and send control signals. Computer processor 100 may be operatively coupled to a non-transitory storage device(s) (not shown) that stores executable instructions. The computer processor 100 may include a CPU(s) and/or a GPU(s) that reads instructions from the storage device and executes the instructions to perform functions and operations the instructions specify. In some embodiments, the computer processor 100 can comprise or consist of hardware such as a programmable or nonprogrammable gate array, an ASIC or any other suitable implementation comprising hardware and/or software. In some embodiments, processor 100 can be implemented as multiple processors which may, although not necessarily, be mutually connected or communicating and including an absence or any plurality of connection or communication means. Computer processor 100 receives operating power 120 from the battery 200, from which it can also receive sensory signals 140 and to which it can send control signals. Implementations can have connections beyond those specifically illustrated here, from computer processor 100 to other components. For example, computer processor 100 can be operatively coupled to numerous input sensors; numerous output devices such as actuators, displays and/or audio transducers; and digital communication devices such as buses, networks, a wireless or wired data transceivers, etc.

In some embodiments, battery 200 provides ancillary power to various components in addition to processor 100. Battery 200 is shown external to the reactor, although in many embodiments it can be internal to the reactor, such as if the RS is implemented as or includes a fuel cell, an alternator/generator, or possesses other electrical power generation capabilities, if present, to receive and maintain charge. In some embodiments, battery 200 can be supplemented or replaced by other power sources such as solar panels, fuel cells, generators, alternators, or any external power sources, etc. In embodiments, the system depicted in FIG. 10 can have connections from battery 200 and processor 100 to other components not shown in the Figure. In embodiments, a battery 200 can be included as an initial power source. A battery 200 can also be useful in remote locations; in situations where battery acquisition, maintenance, or replacement may be difficult; or in emergency and special situations. In embodiments, the system and/or its battery 200 can provide for being jump-started with manually operated, or other kinetic current sources, or with solar panels.

In an embodiment, an operator (and/or the computer processor 100) activates the system by setting an ignition switch (not shown) to "on". Referring to FIG. 10, this action by the operator or computer processor 100 gates power from battery 200 to the other components as appropriate, which can include RAs 500, 900 (if present), the processor 100, and optionally the RS, for example in systems where the RS requires preparation in anticipation of fuel flow. Once started, processor 100 senses, monitors, coordinates, regulates, and controls, as necessary, the activity and interaction of all components. The RAs 500, 900 (if present) can be started under control of processor 100, with the appropriate environment being established for producing the desired chemical reactants, including as examples and without limitation: power, temperature, humidity, pressure, charge, and electromagnetic fields. If sensors and controls in the RAs 500, 900 (if present) are required, such signals can be transmitted through bus 300/300’ to and from the processor 100. Once ready, the RAs 500, 900 (if present) are operationally activated under control of processor 100, which thereafter senses, monitors, coordinates, regulates, and controls RAs 500, 900 to ensure proper operation.

In an embodiment, the RAs 500 are activated to instantiate, or filter, or isolate, or extract, or nucleate, a chemical reactant useful as a fuel material, which can be atoms or molecules, such as hydrogen (H ₂ ). The chemical reactant produced by the RAs 500 is/are collected by the conduit 600, optionally purified or separated, which can further process it in various ways (denoted by the chemical processor 670) as appropriate before it is delivered to the RS 10 through an intake port 750. The chemical processor 670 can include various aspects of conduit(s) 600 that may exist and be attached to processor 100 and battery 200. Similarly, RAs 900 in one embodiment can instantiate, or fdter, or isolate, or extract, or nucleate, a chemical reactant useful as an oxidizing agent which can be atoms or molecules, such as oxygen (O ₂ ). The chemical reactant emitted by the RAs 900 (1-M) (if present) is/are collected by the conduit 600’ which can process it in various ways (denoted by the chemical processor 670’) as appropriate before it is delivered to the RS 10 through its reactant intake 750’.

After an operation reacting the different chemical reactants takes place in the RS 10 with satisfactory completion, the computer 100 can conduct a proper close-down for the RAs 500, 900, conduits 600, 600’, processors 670, 670’, RS 10, battery 200, any other integrated equipment, and for itself 100. The satisfactory completion of the intended chemical reaction in the RS 10 can be determined in various ways depending on the particular specific embodiment. In certain embodiments, the completion can be signaled by the operator setting an ignition switch (not shown) to "off," or can be signaled via some computer interaction or artificial intelligence decision, or can be signaled by any sensor, detector, monitor, or probe interior to, or exterior to RS which may be available to the processor, or can be signaled by parameters pertaining to the RS itself, such as the passage of time or the generation of heat or other energy, or can be signaled by the status of a storage unit or other non-reactive fuel sink, such as a storage tank reaching a full state.

The Figures that follow depict other use cases that exemplify the principles for the RAs and RSs as disclosed herein. ii. Use Cases Involving Gaseous Reaction Products

In embodiments, the chemical reactant produced by the methods disclosed herein can be in gaseous form, which can be entrained within gaseous product compositions, or “product gas.” The invention particularly relates to the identification and collection of a product gas produced by the methods. The product gas can be collected from the process in a continuous, semi-continuous or batch manner. The product gas typically comprises the feed gas or feed gas composition, as discussed above, and the chemical reactant in gaseous form. The chemical reactant in gaseous form is distinct from the feed gas, and preferably contains one or more gases not present in the feed gas. For example, where the feed gas is pure nitrogen (e.g., a gas comprising at least 99%vol nitrogen, such as at least 99.9%vol nitrogen), the product gas will contain one or more other materials (e.g., elements or molecules that exist in gas form under ambient conditions). The feed gas can also include air. In embodiments, the product gas comprises hydrogen and an additional gas such as helium, water, neon, nitrogen, carbon monoxide, oxygen, argon, carbon dioxide, fluorocarbons, ammonia, krypton, xenon, methane and other hydrocarbons or organics and mixtures thereof. For avoidance of doubt, the term “product gas,” as used herein, is understood to be compositionally distinct different from the term “feed gas,” and the term “product gas” explicitly excludes air.

In embodiments, the product gas comprises one or more chemical reactants in gaseous form, and can include, without limitation chemical reactants or additional gases including helium, water, neon, nitrogen, carbon monoxide, oxygen, argon, carbon dioxide, fluorocarbons, ammonia, krypton, xenon, methane and other hydrocarbons or organics and mixtures thereof, provided that such chemical reactants or additional gases are not components of the feed gas or feed gas composition. The invention permits the manufacture of green gas, such as product gas that has less than 0.5%vol CO2, such as less than 100 ppm CO2. Preferred product gases comprise at least about l%vol (preferably at least about 4%vol) of a chemical reactant. Product gases can further comprise neon, helium, argon, and combinations thereof. Typically, the product gas will further comprise the components found in the feed gas (e.g., nitrogen or air), however, in concentrations distinct therefrom.

The invention permits the manufacture of green gas, such as product gas that has less than 0.5%vol CO2, such as less than 100 ppm CO2. In an embodiment, hydrogen can be isolated from, or purified, the product gas, thereby producing a high concentration hydrogen gas. An example of a purification system utilizing a hydrogen-selective membrane. Examples of suitable materials for membranes include palladium and palladium alloys, and especially thin films of such metals and metal alloys. Palladium alloys are particularly effective, especially palladium with 35 weight % to 45 weight % copper. Another effective alloy is palladium with 2 weight % to 10 weight % gold, such as palladium with 5 weight % gold. Hydrogen-selective membranes can be configured to be a foil. Alternatively or additionally, a pressure swing adsorption system can be used to concentrate hydrogen and remove unwanted gases. Such processes use activated carbon, silica, or zeolites. iii. Use Cases Involving Fuels Generally

In embodiments, the invention particularly relates to the identification and collection of chemical reactants useful as fuels produced by the disclosed methods. In embodiments, the methods and apparatus disclosed above can produce chemical reactants such as fuel substances and/or reductants including, but not limited to, the many and varied substances containing hydrogen, carbon, nitrogen, oxygen, calcium, sodium, potassium, phosphorus, sulfur, or other materials, such as other oxidizable materials, such as, by way of example but not limited to: hydrogen (H ₂ ), carbon (C), carbon monoxide (CO); ammonia (NH ₃ ); unsaturated aliphatic hydrocarbons, such as alkynes and alkenes (including olefins); saturated hydrocarbons (e.g., alkanes, paraffins); cyclic and polycyclic hydrocarbons including aromatic compounds; heterocyclic compounds; and a vast collection of other organic compounds, of which a small sample includes: alcohols, such as alkanols (such as monohydric (CJUn+iOH), diols or polyols, unsaturated aliphatic, alicyclic, and other alcohols having various hydroxyl attachments); nitroalkanes such as nitromethane (CH3NO2); carbohydrates; and the like. In embodiments, these fuel substances can include substituted or unsubstituted alkanes or paraffins of various sizes and structures, for example methane (CH ₄ ), ethane (C2H6, CH3CH3), propane tCTHx). butane (C4H10); pentane (C5H12), hexane (CSHH), heptane (C?HI ₆ ), octane (C ₈ H i ₈ ), C9-C16 alkanes, or heavier molecules can also be used as fuel or for other purposes, such as lubricating oil, wax, or asphalt. In many cases, the methods and apparatuses disclosed herein can directly instantiate, or filter, or isolate, or extract, or nucleate, the chemical substance, the production of which might otherwise require transformation by a chemical reaction or a different source.

While the use of these methods and apparatuses for producing conventional chemical reactants useful as fuels (including but not limited to those disclosed herein) is especially advantageous, these methods and apparatuses also are capable of producing materials not usually considered to be fuels, but which can be economically harnessed in appropriate situations for the energy of their exothermic fuel-like reactions with other chemical substances, such as oxygen and other oxidizing agents described herein. Such atypical fuels produced by these methods and apparatuses include those elements such as calcium, sodium, lithium, and the like, that are so reactive in the natural environment that they are not encountered in their unbound, elemental state. Examples of such atypical fuels include, without limitation, alkali metals: Li (which can react, e.g., with O2, H ₂ O, CO2, N ₂ ), Na, K, and the like; alkaline earth metals (Be, Mg, Ca, and the like); and those other elements and compounds that can be involved in exothermic reactions, such as Al, Fe, CaO, and the like, including for example but without limitation, those that can be made to undergo exothermic reactions, such as Al, Fe, CaO. While the reactions involving conventional fuels tend to take place via a redox mechanism using an oxidizing agent such as oxygen, the chemical substances available as fuels are not limited to those that undergo redox reactions. Atypical fuels can produce energy through non-redox mechanisms, for example, a reaction between metal oxide such as CaO, and H ₂ O, and similar reactions.

Chemical reactants produced by the methods and apparatuses disclosed herein can also include oxidants (i.e., oxidizing agents), which can be used to react with reductants or fuels produced by the methods and apparatuses disclosed herein, or which can be isolated to be used for other purposes. The oxidants that can be instantiated, or fdtered, or isolated, or extracted, or nucleated, by these methods and apparatuses include without limitation, atomic oxygen and oxygen species, hydrogen peroxide, water (which can exothermically oxidize alkali metals, alkaline earth metals, and the like, and can exothermically react with alkali metal oxides or alkaline earth metal oxides such as CaO), halogen molecules such as F ₂ , CL, Br ₂ , and the like, and other reactive metals (e.g., metal oxides) or non-metals.

In embodiments, the invention particularly relates to the identification and collection of chemical reactants useful as fuels produced by the foregoing methods. Fuels or oxidants that react with such fuels can be produced by the methods and apparatuses disclosed herein and can be stored in various containers or other retaining mechanisms for use elsewhere. Such containers or retaining mechanisms (collectively, “retainers”) allow the chemical reactants thus produced to be stored for use elsewhere or at a later time. Retainers can include, without limitation, bags or tanks or bottles (for fluids (preferably gases), caves (for gases), bags, envelopes or boxes (for solids), conduits, or any other vessel or other structure that at least for a discernible period of time (whether short or long), either while in transit or statically, stores a quantity of the chemical reactant. iv. Use Cases Involving Fuels: Thermal Systems

A number of use cases can be envisioned that employ one or more RAs, as described above, for the production of fuels and/or oxidants to be used in one or more RSs in systems that function to produce heat. As used herein, a RS that effects the reaction between the fuel-reactant produced by the RAs and an oxidant-reactant produced by the RAs; or between the fuel reactant produced by the RAs and an oxidant derived from a conventional oxidant source, for example ambient air, or an oxygen tank, or a pipeline, or a similar conventional source; or between an oxidant produced by the RAs and a fuel reactant derived from a conventional fuel source, such as a tank, a pipeline, or a similar conventional source, is termed a “thermal apparatus.” A thermal device comprises the thermal apparatus and the sets of one or more RAs that produce the fuel or oxidant reactants (or both), and further comprise any sources of fuel or oxidant that do not involve their production by a set of one or more RAs. A thermal system comprises one or more thermal devices, with each thermal device comprising at least one thermal apparatus, as described herein. Such a system, comprising one or more RAs and one or more RSs to produce thermal energy and to transfer it to an external body or environment, is termed a “thermal system.” A thermal system comprises mechanisms or subsystems for heat transfer: the process of transferring the thermal energy to the external body or environment is termed “heat transfer”; the external body or environment to which the thermal energy is transferred is termed the “heat recipient.”

As used herein, the term “thermal system” includes, without limitation, those devices, apparatuses, appliances, or equipment employing a thermal apparatus for which the production of thermal energy is a goal or by-product. In other words, the primary goal for a thermal system is the production of heat (i.e., the transfer of thermal energy from one body to another) as distinguished from having a primary goal of producing mechanical energy. This distinguishes a thermal system in accordance with the principles of the invention from an engine or other mechanism that leverages the principles of the invention to produce thermal energy, but uses such thermal energy for the purposes of performing work. For example, while a locomotive can include a boiler that burns coal to heat water, the primary objective of the locomotive boiler is not the production of the thermal energy per se, but rather the transfer of heat into the water to turn it into steam, so that the expansion of the steam performs useful work by driving a piston or otherwise producing mechanical energy. A boiler in this context, even if it uses thermal energy produced by certain of the systems and methods disclosed herein, is not acting as a thermal device, but is acting as part of an engine. By contrast, a boiler is operated to achieve a primary goal of heating a substance like water or steam is acting as a thermal device. A thermal device can produce heat by the same thermodynamic mechanism as an engine uses (for example, combustion), but the thermal device uses the thermal energy in an unmediated manner simply to produce heat: it lacks a prime mover to convert the thermal energy into useful work that can, in turn, produce mechanical or electrical energy.

The difference between a thermal device (i.e., a device used primarily for the production of heat) and a heat-driven engine is well demonstrated by cogeneration or combined-heat-and-power facilities, which can use the thermal energy produced by combustion not only to perform work such as driving a gas or steam-powered generator but also to heat water that can be used for process heating, building heating, and the like. The systems and methods for instantiating fuels and optionally oxidants as disclosed herein can be employed to produce thermal energy for both end-uses, the production of work and the unmediated production of heat. However, only those devices involved in the unmediated production of heat are thermal devices, although they can be combined with other systems using the production of heat to perform work.

Exemplary thermal devices and systems can include equipment for the production of thermal energy and the transfer of heat (termed “thermal equipment” herein) including, without limitation, furnaces, boilers, heaters, irons, warmers, ovens, stoves, dryers, annealers, kilns, bakers, cookers, sealers, smelters, solderers, torches, cutting torches, welders, melters, autoclaves, sterilizers, and the like and combinations thereof. Thermal equipment might be of any size, scale, scope, or use, including, without limitation, small, medium, large, personal, hobby, home, domestic, household, commercial, laboratory, hospital, factory, manufacturing, industrial, etc., and pieces of thermal equipment can be used separately or can be combined. As examples, a thermal system can be used as a home hot water heater or boiler heated by combustion of instantiated H ₂ and instantiated O _2; an industrial furnace or boiler heated by the combustion of instantiated H ₂ as fuel and instantiated O ₂ as oxidant, or a welding/cutting device using instantiated gaseous acetylene as reactant (fuel) and ambient or instantiated gaseous O ₂ as oxidant.

In embodiments, a thermal device can include any flame, heater, or burner that performs the combustion of an instantiated reactant (such as a fuel or an oxidant) with another instantiated or noninstantiated reactant (such as, respectively, an oxidant or a fuel), with the production of heat that is transferred to a heat recipient to energize a chemical reaction therein. This operation of a thermal device for the initiation or propagation of chemical reactions in a heat recipient is seen, for example, in metal cutting operations (as opposed to metal welding), in which the heat from the metal cutting torch heats the metal to its kindling temperature, at which point the heat of the torch overcomes the activation energy for the metal’s combustion, allowing it to become oxidized. Innumerable chemical reactions take place on the same principle: heat from a flame, burner, or the like raises the temperature of the heat recipient sufficiently to energize or to initiate a chemical reaction.

A thermal apparatus suitable for implementation in a thermal device and thermal system is capable of using any fuel that can be produced by a RA, or by a combination of multiple RAs. In other embodiments, the term “thermal apparatus” pertains to a RS in a thermal system that effects the reaction between the fuel reactant and an oxidant, wherein either the fuel or the oxidant or both is produced by a set of one or more RAs. In many thermal apparatus embodiments, hydrogen is the preferred fuel, although any material that can be produced by a RA (including without limitation lithium, sodium, potassium, ammonia, or hydrocarbons), or by a combination of various materials produced by RAs, is subject to consideration provided such fuel is compatible with (e.g., can be burned by) the apparatus. Any oxidizing agent that reacts appropriately with the fuel in the context of the apparatus can be employed (including without limitation: oxygen, fluorine, chlorine, bromine, hydrogen peroxide). While the oxidizing agent is advantageously oxygen in preferred embodiments, any chemical that reacts appropriately with the fuel and satisfies an implementation's constraints can be used as an oxidizing agent. The oxidizing agent can be instantiated (or filtered, or isolated, or extracted, or nucleated), collected, and managed by a system more or less similar to that assembling the fuel, but it is generally separated therefrom in order to prevent premature reaction between fuel and agent, until the fuel and agent are combined, combusted, or otherwise chemically reacted in the thermal apparatus with the agent being introduced into the thermal apparatus in the conventional way.

In preferred embodiments, the thermal apparatus will use hydrogen as the fuel and oxygen as the oxidant, and will produce the combustion of hydrogen in the presence of oxygen, i.e., sustain the ongoing exothermic chemical reaction as shown in EQ 1 :

EQ 1: 2H ₂ (g) + O ₂ (g) 2H ₂ O (g) AH = - 483.6 kJ which produces a flame in the range of 3073K (2800°C, 5072°F). An even hotter flame of 3773K (3500°C, 6,332°F) can be attained in oxyacetylene embodiments wherein instantiated acetylene is burned in the presence of instantiated pure oxygen). In certain embodiments, the hydrogen fuel is instantiated or fdtered, or isolated, or extracted, or nucleated by one or more RAs, and the oxygen is drawn from the atmosphere or from another oxygen source. In other embodiments, at least one auxiliary RA can be used to produce oxygen or the oxidizing agent of choice. Implementations can also use additional RAs configured to produce a supply of oxidizing agent to react with the fuel. Producing the oxidizing agent within the system can advantageously allow the thermal device to produce very hot flames, for example an oxyhydrogen flame for metal-cutting applications. In embodiments, the ability to produce the oxidizing agent within the system permits it to be used in environments where ambient oxygen is scarce or unavailable, such as underwater (e.g., submarines), or in confined or unvented places (e.g., vaults, tunnels, and mines).

In certain embodiments, it can be advantageous to moderate the heat produced by the system: for example, the very hot adiabatic flame temperature of the stoichiometric reaction of hydrogen and oxygen (2800°C) may be too extreme and therefore undesirable for food preparation. The reaction temperature can be reduced by including other materials as secondary streams that do not participate in, or contribute much heat to, the exothermic reaction but that rather absorb heat and thereby lower the effective temperature produced by the primary reaction. Such moderating (“buffering”) materials might include for example, without limitation: excess fuel, excess oxidizer, or other gases such as nitrogen, helium, argon, krypton, etc. Effective temperature of the thermal apparatus can also be moderated, without limitation, by buffering a hot flame with stone, ceramic, brick, or other intermediating material which re-emits the heat in a milder, less intense form, or by other techniques familiar to those of ordinary skill in the art.

FIG. 11 A depicts an embodiment of a thermal system 1000A using at least one RA or plurality of RAs 1002 (1 -N, where N a positive integer) producing a fuel such as hydrogen, which RAs 1002 can be identical or non-identical, and can be the sole source of fuel used alone as a fuel source for the thermal apparatus 1004 or producing fuel to be stored in a receptacle or retainer such as a storage tank (not shown) which is then used to supply the thermal apparatus 1004 with fuel. As has been previously described, the RAs instantiating the fuel can be configured to catalytically instantiate, or filter, or isolate, or extract, or nucleate an oxidizable fuel, such fuel being suitably reactive with the oxidizing agent selected for use in the thermal apparatus 1004 to produce the desired thermal energy. In addition, a secondary RA or plurality of RAs (not shown) can produce a moderating gas such as helium, nitrogen, argon, or the like, that can mix with or be introduced with the fuel to lower the effective combustion temperature of the fuel when it is combusted in the thermal apparatus 1004. Such a moderating gas can also be introduced from an external source. The set(s) of RAs and the thermal apparatus 1004 receive power from the battery 1008 in the depicted embodiment, although it is understood that other sources of power can be employed. The illustrative system 1000 A uses a set of conduits 1010, shown here as conveying hydrogen and oxygen, to direct the fuel and the oxidant to the thermal apparatus 1004. It is understood that the conduits 1010 can convey any reactant produced by the set of RAs 1002 for reaction with the oxidizing agent (e.g., oxygen), here depicted as being provided by an air/oxygen intake subsystem 1012. The reactants (here hydrogen as fuel and oxygen as oxidizing agent) that are conveyed through the conduits 1010 enter the thermal apparatus 1004 through a set of ports 1020 and 1022, with the fuel entering through a fuel intake port 1020 and the oxidizing agent entering through an oxidizer port 1022. While the depicted embodiment illustrates the two reactants entering the thermal apparatus 1004 through separate ports and conduits, it is understood that they can be premixed prior to entering the thermal apparatus, using techniques familiar to artisans of ordinary skill. It should also be understood that moderating substances, such as without limitation, noble gases, may also be delivered from various sources to the combustion chamber though these, or other (not shown), conduits. Within the thermal apparatus 1004 the reaction between the fuel and the oxidizing agent takes place, for example using conventional techniques known in the field, such as using an ignition system (not shown) to initiate the reaction between the fuel and the oxidizing agent (e.g., combustion) that results in the production of thermal energy 1030. Delivery of the oxidizing agent can take place at the same time as the delivery of the fuel, or before or after, so long as the fuel and the oxidizing agent are present at the same time in adequate quantities to permit the desired exothermic reaction to take place, i.e., synchronous delivery. During operation the combustion chamber may receive additional fuel, oxidant, and possible moderating material on a continuous or sporadic basis, as applicable to the design and constraints of the embodiment.

Reaction products can be directed out of the thermal apparatus 1004 as exhaust 1028. The thermal energy 1030 produced by the thermal apparatus 1004 can be directed to any appropriate heat recipient 1032 and transferred thereto using any form of heat transfer, including radiation, conduction, convection, or a combination thereof. As would be understood by skilled artisans, the particular configuration of the intake ports 1020, 1022, the reaction/combustion chamber or other structure, and the manner of emitting or otherwise using and handling the resulting thermal energy 1030 together with the byproduct exhaust 1028, if any, will depend on the particular type of thermal apparatus 1004. The chemical reaction between the fuel instantiated or filtered, or isolated, or extracted, or nucleated, by the set of RAs 1002 and the oxidant provided by the air/oxygen/oxidant intake 1012 as performed by the thermal apparatus 1004 is the source of the thermal energy 1030 that provides the heat transfer to the heat recipient 1032. A computer system 1040 receives data from the components of the system and controls their activity and interaction, including without limitation the sensing, direction, and regulation of heat transfer 1030 from the thermal apparatus 1004 to the heat recipient 1032. Illustrative pathways for receiving/transmitting data are shown schematically as dotted lines W, X, Y, and Z in the Figure, although it is understood that other appropriate pathways for sensing, directing, and regulating aspects and components of the system can exist in addition to those depicted by the dotted lines.

FIG. 1 IB depicts an embodiment of a thermal system 1000B having similar components to those shown in 11 A with the same numbering, except that the oxygen/air intake is replaced by a second set of one or more RAs 1050 for assembling an oxidizing agent such as oxygen. This second bank of RAs 1050 (having 1-M RAs, where M is a positive integer) produces an oxidizing agent such as oxygen; the RAs in this second bank of RAs can be identical or non-identical, and can be used to supply the thermal apparatus with the oxidizing agent, either directly as shown, or by producing the oxidizing agent which is then stored in a receptacle or retainer such as a storage tank (not shown), from which the oxidizing agent can be drawn to react with the fuel in the thermal apparatus 1004. As was previously described, a moderating gas such as helium, nitrogen, argon, and the like, can be mixed with the instantiated oxidant to lower the effective combustion agent. Such moderating gas can be produced by a separate set of RAs (not shown) or can be introduced from an external source. As has been previously described, the RAs instantiating the oxidizing agent can be configured to catalytically instantiate, or filter, or isolate, or extract, or nucleate an oxidant, such oxidant being suitably reactive with the fuel selected for use in the thermal apparatus 1004 to produce the desired thermal energy. In the depicted embodiment, both sets of RAs 1002 and 1050, along with the thermal apparatus 1004 receive power from the battery 1008, although it is understood that other sources of power can be employed and other arrangements for supplying the two sets of RAs 1002 and 1050.

FIG. 12 depicts an embodiment of a thermal system 2301 comprising a first plurality of RAs 2500 (1 - N, where N a positive integer) producing hydrogen, and a second optional plurality of RAs 2550 (1-M, where M is zero or a positive integer) producing oxygen, both in fluid communication with a thermal apparatus 2700. The thermal apparatus 2700 has a fuel intake port 2750 and an oxidizing agent intake port 2780. The thermal apparatus 2700 has a reaction chamber (not shown) such as a combustion chamber or other structure of known conventional design. Fuel (such as hydrogen) is introduced into the chamber through the fuel intake port 2750 and the oxidizing agent (such as oxygen) are introduced into the chamber through the oxidizing agent intake port 2780. In the depicted embodiment, the fuel and the oxidizing agent form a fuel-oxidant within the chamber. In other embodiments, not depicted in this Figure, the fuel and the oxidant are pre-mixed and enter the chamber as a fuel-oxidant mixture, instead of the depicted arrangement in which the fuel and the oxidizing agent each enter the chamber through its own intake port. Once the fuel-oxidant mixture has formed adequately, a source of ignition or other reaction initiator (not shown) starts a reaction within the thermal apparatus 2700 that causes the fuel and oxidizing agent to react. The fuel and oxidizing agent are thus ignited and combine exothermically to produce thermal energy 2800. Delivery of the oxidizing agent can take place at the same time as the delivery of the fuel, or before or after, so long as the fuel and the oxidizing agent are present at the same time in adequate quantities to permit the desired exothermic reaction to take place, i.e., synchronous delivery. During operation the combustion chamber may receive additional fuel, oxidant, and possible moderating material on a continuous or sporadic basis, as applicable to the design and constraints of the embodiment. The thermal apparatus 2700 may further include an exhaust 2950 for removing byproduct(s) of the reaction/combustion. Exhaust 2950 can include an exhaust pipe, a chimney, drain, flue, or any other conventional exhaust structure. Such exhausted byproduct(s) of the reaction may comprise or include water in the case of using hydrogen and oxygen as fuel and oxidizing agent respectively. As is well known, other types of combustion or incomplete combustion could produce other byproducts such as carbon dioxide, carbon monoxide, nitrogen oxides or other gases. For example, if atmospheric air is used as the source of oxygen, other materials in the air (e.g., nitrogen) can react as well to produce various reaction byproducts as is well known. The particular configuration of the intake ports 2750, 2780, the reaction/combustion chamber or other structure, and the manner of emitting or otherwise using and handling the resulting heat and radiant energy 2800 together with the byproduct exhaust 2950, if any, will depend on the particular type of thermal apparatus 2700. It should be noted that in some thermal apparatus the reaction (such as combustion) may not occur in any clearly bounded chamber; a household lighter, a candle or a torch are non-limiting examples in which combustion occurs in the open and is not confined in a chamber. In embodiments, the fuel and the oxidant may be delivered synchronously to produce a fuel-oxidant mixture which can be reacted (e.g., combusted) as an open flame, which then produces the thermal energy.

In certain embodiments, hydrogen is a preferred fuel to be produced by the RAs 2500 (1-N), although it is understood that any material that can be produced by a RA either in isolation or in combination with other materials that can be produced by another RA can be used as a fuel to be introduced into the thermal apparatus 2700. Ultimately, the fuel instantiated by the RAs 2500 (1-N) is delivered to fuel intake port 2750 of the thermal apparatus 2700, where it is used in a reaction with the oxidizing agent from the RAs 2550 (1-M) introduced through the oxidizing agent intake port 2780, to produce heat in a conventional and well-understood manner. Any oxidizing agent that reacts appropriately with the fuel can be considered, including but not limited to oxygen. In embodiments, the thermal system 2301 can draw some or all oxygen from the atmosphere or from other oxygen sources such as tanks or gas lines, in which case the RAs 2550 that produce oxygen, as shown in this Figure, are replaced by conduits to permit the ingress of oxygen from these other sources, allowing the oxygen to enter the thermal apparatus 2700 for example through a conduit 2600’ and the intake port 2780, replacing the oxygen that is produced by RAs such as are shown in the depicted embodiment. As shown in this Figure, the thermal system 2301 uses a conduit 2600/2600’ to convey fuel/oxidant to the appropriate intake port 2750/2780 of the thermal apparatus 2700. In embodiments, at least one auxiliary RA2550 can be used to produce some or all of the oxygen needed. In yet other embodiments, not shown in this Figure, certain RAs from the fuel-producing bank or set of RAs 2500 or from the oxidizing agent bank or set of RAs 2550 can be designated to produce a moderating material (such as, without limitation, helium, nitrogen, argon, water vapor, etc.) that can be mixed with, and/or introduced with, the fuel (and/or oxidizing agent) to lower the effective combustion temperature. It is also possible for there to be additional RAs (not shown) and conduits (also not shown) to separately produce and deliver a moderating material to thermal apparatus 2700 to dilute and cool the reaction heat. In embodiments, the system can include a temperature regulating subsystem (not shown), which can be automatic, semi-automatic, and/or manual, that can affect the temperature by methods including controlling the production, flow and/or delivery of at least one of the fuel, oxidizing agent, or moderating material.

As the fuel/oxidant is assembled and emitted by the at least RAs 2500/2550, it can be collected and introduced into the thermal apparatus 2700 directly, (e.g., at the fuel/oxidant intake port 2750/2780). However, it is understood that the fuel and oxidant can also each undergo additional processing steps (not shown) during their passage to the thermal apparatus 2700. Such processing steps can include, without limitation, being: pumped, collected, combined, e.g., combined with the output of other conduits or sources, pressurized, compressed, liquefied, solidified, stored, packaged, transported, hauled, unpackaged, repackaged, gasified, uncompressed, depressurized, filtered, mixed, agitated, centrifuged, shaken, oscillated, stirred, vibrated, gated, shunted, injected, diverted, merged, blown, aerated, propelled, spun, blended, dissolved, extracted, sensed, tested, humidified, dehumidified, monitored, measured, regulated, accumulated, cooled, heated, or otherwise processed. Such operations may involve the use of components including for example and without limitation: pumps, sensors, gates, shunts, injectors, valves, baffles, pipes, splitters, plumbing, relays, filters, controls, accumulators, tanks, containers, reservoirs, fans, blowers, propellers, impellers, aerators, agitators, oscillators, vibrators, shakers, stirrers, centrifuges, pressurizers, humidifiers, dehumidifiers, compressors, refrigerators, blenders, mixers, vats, dissolvers, extractors, coolers, heaters, gasifiers, liquefiers, and sensors and controls for flow, humidity, concentration, density, purity, particle size, particle diameter, particle surface area, particle weight, viscosity, temperature, volume, and pressure, as well as other sensors and controls and processing equipment. In situations where additional processing steps are carried out, each step may be performed zero or more times, and the order in which they are performed (and whether they are necessary) depends on the requirements of the particular thermal system 2301.

In the depicted embodiment, the RAs 2500/2550 receive power as needed, from battery 2200 or other electrical storage cell (e.g., a capacitor) or electrical power source (such power may be governed by a start switch in some implementations). Aspects of the operation of each RA 2500/2550 are sensed, monitored, coordinated, regulated and controlled by a processor 2100 through sensor/control line(s) 2300/2300’. Regulation can include parameters such as, without limitation, power, temperature, humidity, configuration, pressure, flow, concentration, viscosity, density, purity, particle dimension, and any other relevant state or parameter; together with the operation of fans, blowers, oscillators, pumps, valves, reservoirs, accumulators, pressurizers, compressors and/or other devices used to support the processes shown.

As depicted in 12, a computer processor 2100 senses, monitors, coordinates, regulates, and controls the various other aspects of the thermal system 2301, and is connected as needed to the other various components to receive sensor input signals and send control signals. Processor 2100 receives operating power 2120 from the battery 2200, from which it may also receive sensory signals 2140 and to which it may send control signals 2160. In embodiments, the thermal system 2301 can have connections beyond those specifically illustrated here, from processor 2100 to other components; in other embodiments, certain connections illustrated in FIG. 12 can be optional. In the depicted embodiment, the processor 2100, and optionally the battery 2200, may also be connected to the On- Off Switch, which activates the various components.

An operator activates the thermal system 2301 by turning the On-Off Switch to "on". This gates power from battery 2200 to the other components as appropriate, including processor 2100, and the banks or sets of RAs 2500, 2550. The banks or sets of RAs 2500, 2550 are started under command and control of processor 2100 as the appropriate environment is established, including for example and without limitation: temperature, humidity, pressure, charge, electromagnetic fields. This involves sensors and controls in the banks or sets of RAs 2500, 2550, the signals of which are transmitted through sensor/control lines 2300/2300’ to and from the processor 2100. Power as appropriate is delivered to the RAs in the banks or sets of RAs 2500, 2550 through power conductors 2400/2400’. Once the RAs 2500, 2550 and their environment are suitably prepared, the banks or sets of RAs 2500, 2550 are operationally activated under command and control of processor 2100, which thereafter senses, monitors, coordinates, regulates, and controls the banks or sets of RAs 2500, 2550 to ensure proper operation.

In their active state, RAs 2500 instantiate, or filter, or isolate, or extract, or nucleate, the fuel, which in an exemplary embodiment comprises hydrogen atoms and molecules. The instantiated fuel emitted by the fuel-producing RAs 2500 is collected by the conduit 2600, and is further processed by optional processing steps (denoted by 2670) as appropriate before the fuel is delivered to the thermal apparatus 2700 through its fuel intake 2750. If necessary, 2670 can represent various additional steps and/or structures, as described above.

For embodiments in which the oxidizing agent is oxygen drawn from the atmosphere, it is extracted and processed in a conventional fashion and introduced into the thermal apparatus 2700 at its oxidizing agent intake port 2780. In some embodiments, the oxidizing agent is assembled by the bank or set of RAs 2550, and delivered through conduit 2600’ to the oxidizing agent intake port 2780 of the thermal apparatus 2700, where it is used in the reaction with the fuel to produce heat and other radiant energy via conventional reactions. Conduit 2600’ may deliver the oxidizing agent for optional processing steps (denoted by 2670’) as appropriate before the oxidizing agent is introduced into the thermal apparatus 2700 through its oxidizing agent intake 2780. If necessary, 2670’ may involve various additional steps and/or structures, as described above.

As shown in FIG. 12, the fuel is delivered to the fuel intake port 2750 of the thermal apparatus 2700, where it is used in an exothermic reaction with the oxidizing agent that is delivered to the oxidizing agent intake port 2780 of the thermal apparatus 2700, thereby producing thermal energy 2800. The thermal energy 2800 produced by the thermal apparatus can be transferred to a heat recipient 2900 by a heat transfer process including conduction, convection, radiation, or some combination thereof. In an exemplary embodiment, a thermal system in accordance with the invention can be integrated into a residential or industrial furnace or boiler (where a boiler is understood to be a furnace that specifically heats water to convert it to steam), so that such a device receives a transfer of thermal energy produced by combustion of one or both of an instantiated fuel and an instantiated oxidant, for example, instantiated H ₂ and instantiated O ₂ . In another exemplary embodiment, a thermal system in accordance with the invention can be used for welding applications. Other thermal systems incorporating the principles of the invention can be readily envisioned by practitioners of ordinary skill in the art.

In more detail, exothermic reactions produced by reacting (a) a first reactant (e.g., a fuel instantiated, or filtered, or isolated, or extracted, or nucleated by the thermal apparatus according to the present invention or obtained elsewhere provided that the reaction involves a second reactant is instantiated, or filtered, or isolated, or extracted, or nucleated by a RA system as disclosed herein) with (b) a second reactant (e.g., an oxidizing agent that can be instantiated, or filtered, or isolated, or extracted, or nucleated by a RA system as disclosed herein, or obtained elsewhere provided that the first reactant is instantiated, or filtered, or isolated, or extracted, or nucleated by a RA system as disclosed herein) yield thermal energy that can be transferred as heat to a body or an environment external to the source of the thermal energy. Such transfers result in a change in temperature from the source of the thermal energy to the external recipient via heat transfer. As an example, the exothermic reaction mentioned in EQI above combines hydrogen fuel and oxygen to produce water, yielding 241 kJ/mole of heat that can be transferred to other bodies or environments. By producing a fuel that can support an exothermic chemical reaction, the systems and methods disclosed herein can energize a thermal apparatus for the production of thermal energy. Transferring this thermal energy from the source (the thermal apparatus) to the external body or environment entails heat transfer.

As mentioned previously, heat transfer takes place by conduction, convection, radiation, or some combination thereof. In thermal conduction, the thermal energy is transferred as heat due to the migration of free electrons or the excitation of lattice vibrational waves (phonons) between the higher- temperature heat source and the lower-temperature heat recipient. Conduction most commonly involves the contact of one object or fluid with another, but without any significant movement of mass in the direction of the energy flow, such as takes place when a solid body comes into contact with another solid body, with a transfer of thermal energy from one to another. Conduction is involved in everyday activities such as cooking food in a skillet or pressing clothes with an iron. By contrast, thermal convection transfers thermal energy as heat due to the bulk movement of molecules within fluids, whether liquid or gas. Convection takes place, for example, when water is heated in a pan or when clothes are dried in a dryer. Conduction and convection involve objects or materials as both heat source and heat recipient, but convection involves the presence of fluid motion as the heat is transferred from heat source to heat recipient, while conduction does not. Thermal energy can also be transferred by emanation from a heat source without involving any transfer medium, with the heat being transferred in the form of electromagnetic radiation particularly in the infrared region of the electromagnetic spectrum. This type of heat transfer, termed thermal radiation, conveys heat from a heat donor to a non-contiguous heat recipient without involving a fluid transfer medium. Thermal energy travels by radiation when the sun warms the Earth’s surface or when an open flame warms the space around it.

As previously described, the thermal systems according to the principles of the invention comprise a thermal apparatus and further comprise those mechanisms or subsystems for the transfer of the thermal energy from the thermal apparatus to the heat recipient, i.e., heat transfer. Thermal systems as disclosed herein can transfer heat by any of the known forms of heat transfer processes, whether conduction, convection, radiation, or some combination thereof. Conduction as performed by a thermal system is a heat transfer process that occurs within a heat recipient due to the energy of the molecules, atoms, or other component of that substance, related to its intrinsic properties, without macroscopic movement of any of its parts. Convection as performed by a thermal system is a combined type of heat transfer occurring in a heat recipient fluid that includes both heat conduction within the fluid and macroscopic motion in the fluid. The thermal energy produced by the thermal apparatus excites the molecules in the heat recipient fluid, producing motion therein due to diffusive and bulk current flows, including motion due to thermal expansion, density /buoyancy forces, and phase changes. Thermal radiation as performed by a thermal system is energy transfer in the form of electromagnetic waves. Energy transport takes place by photons released by molecules and atoms involved in the reaction that produces the thermal energy, with that energy being conveyed in electromagnetic waves: the wavelengths of electromagnetic waves generated by heated bodies are in the range of 0.3 - 10 pm. Radiation with a longer wavelength than the visible spectrum of electromagnetic radiation is termed infrared, and radiation with a shorter wavelength than the visible spectrum is termed ultraviolet. Thermal radiation, because it involves no intervening medium between heat source and heat recipient, can transfer heat in a vacuum. Thermal systems in accordance with the principles of the invention can use any of the aforesaid mechanisms alone or in combination to produce the desired transfer of heat produced by the thermal apparatus to the heat recipient. In embodiments, the combustion in the thermal apparatus transfers the thermal energy by radiation and does not involve any intermediation between heat source and heat recipient. In other embodiments, the thermal apparatus transfers the thermal energy (i.e., produces heat) in the heat recipient by conduction or convection. In yet other embodiments, there is some combination of the various forms of heat transfer in the thermal device.

In exemplary embodiments, a thermal system in accordance with the principles of the invention can be used for residential or industrial furnaces, which can include hot water heaters, boilers, and the like. In such as system, whether a furnace or a hot water heater or boiler, combustion provides a source of thermal energy, which is then transferred to a heat recipient, for example a metal being heated directly by a furnace, or a fluid that is employed to transfer the heat to a secondary recipient or environment. In a conventional industrial furnace, hot water heater or boiler, combustion takes place in a burner or firebox, which often involves burning fossil fuels (e.g., coal, coke, oil, wood, etc.) in the presence of atmospheric oxygen to produce thermal energy. The thermal energy so produced is then transferred to a closed set of fluid-containing tubes or coils residing in the firebox. This section of the furnace is termed the “radiant section” of the furnace because the thermal energy produced by the combustion in that area is transmitted by radiation into the tubes containing the fluid. The fluidcontaining tubes are arranged so that they extend into an adjacent “convection” section of the furnace that is separate from and walled off from the radiant section. In the convection section, the heated fluid within the tubes transfers heat by convection to other, secondary, fluids that surround them. These secondary fluids, for example heat transfer liquids, can then transfer heat to other locations in the form of heated liquids or heated gases (such as is seen, for example, in a boiler, which produces steam from heating water). Alternatively, the heat carried by the tubes into the convection section can be used to heat the local environment within the convection section without involving secondary fluids for heat transfer. In this case, the heated tubes transfer heat to the ambient gases in the convection section, providing an oven-like atmosphere within the convection section in which a product or a material can be heated directly.

Thermal systems in accordance with the principles of the invention can be used in furnaces, heaters, boilers, and the like to instantiate, or fdter, or isolate, or extract, or nucleate, the reactants for combustion and to effect their combustion, thereby precluding or supplementing the need for conventional, hydrocarbon-based fuels and/or conventionally derived oxidizing agents in such devices. In embodiments, a combination of a fuel (such as hydrogen) produced by a set of one or more RAs and an oxidant (such as oxygen) produced by a second set of one or more RAs can be combusted in the radiant section of the furnace, heater, or boiler to produce the thermal energy for the system’s overall function. In other embodiments, only one of a fuel and an oxidant is produced by the set of one or more RAs, while the other reactant is provided by conventional sources. In either case, the systems and methods disclosed herein offer convenient and scalable alternatives to the fossil-fuel- derived sources of thermal energy used for conventional industrial and residential furnaces, heaters, and boilers. Advantageously, hydrogen thus produced can be used as a fuel source and oxygen can be used as the oxidant, thereby avoiding the CO2 associated with conventional hydrocarbon-powered furnaces, heaters, and boilers; in this embodiment, one or both of the reactants can be produced using a set of one or more RAs as disclosed herein. In a particularly advantageous embodiment, both the fuel and the oxidant for the combustion process (here hydrogen and oxygen) are produced by sets of one or more RAs.

In another exemplary embodiment, a thermal system can be used for metalworking such as welding, for example as a substitute for conventional oxyfuel welding. Oxy -fuel welding is a process that uses the combustion of a fuel gas and oxygen to generate a flame in a delivery device (a “torch”) having sufficient heat to melt metal so that two metal surfaces can be joined. The flame temperature produced by the welding system is sufficient to allow localized melting of the workpieces to which it is applied. The torch applies the flame to the workpieces, creating localized areas of molten metal on each; as the areas of localized melting merge and resolidify, the two metal workpieces become bonded to each other. Hydrocarbon-oxygen flames and hydrogen-oxygen flames can be used for welding, with the former having a range of temperatures depending on the fuel substance used (e.g., acetylene at 3500 °C), and with the latter producing an adiabatic temperature of about 2800 °C. Heat produced by the combustion of the reactants within the welding torch is transmitted to the workpieces (the heat recipients) by radiation at a sufficient temperature to ultimately melt the targeted portions thereof. Heat from the flame reaching the surface of each heat recipient (each, a workpiece) is then conducted throughout the targeted portion of the metals being welded, heating those areas of the metals sufficiently to change their states from solid to liquid, thereby creating a localized pool of melted metal. An additional metal, called a “filler,” is generally provided, which also melts into the localized pool and solidifies with the target metal(s), offering enhancements to the solidification process and the resulting bond between the workpieces. Equipment for conventional welding comprises a fuel source and an oxidant source (generally contained in cylinder tanks), each of which deliver the specific reactant under pressure through a conduit (a hose) to the torch, which applies the flame to the workpieces.

A thermal device according to the principles of the invention can provide instantiated fuel and/or oxidant that can be combusted to produce the flame for a welding torch. In more detail, in a thermal system according to the principles of the invention, the fuel and/or oxidant instantiated by their respective sets of one or more RAs can be directed through appropriate conduits into the welding torch for ignition and combustion, with the flame being directed towards the workpieces to perform the welding operation in accordance with practices familiar in the art. In an embodiment of a thermal system for welding, either the fuel source or the oxidant source or both is provided by the appropriate sets of one or more RAs, while the combustion process and further use of the thermal energy is performed in accordance with conventional welding practices.

While hydrogen is a preferred fuel for many applications, and oxygen a preferred oxidizing agent, the selection of the fuel is based on the needs of the welding procedure, as certain metals require higher temperatures for welding than others, and certain metals respond adversely to certain fuels used in the combustion process. For example, hydrogen is not used for welding ferrous materials because the introduction of non-combusted hydrogen (i.e., the presence of hydrogen atoms or ions) into the ferrous material causes a form of embrittlement known as hydrogen-induced cracking. Also, the combustion of hydrogen, producing a flame temperature of about 2800 °C, may not produce enough thermal energy for welding certain metals, in contrast to the combustion of acetylene and oxygen, which produces a flame temperature between about 3200 °C and 3500 °C, making this latter fuel more suitable for welding certain metals with higher melting points. In embodiments, fuel sources (whether provided conventionally or produced by a set of one or more RAs as disclosed herein) can be selected by the ordinarily skilled artisan to meet the needs of the particular welding operation, with the oxidant being generated by a set of one or more RAs as disclosed herein. In embodiments, a combination of a fuel (such as hydrogen) produced by a set of one or more RAs and an oxidant (such as oxygen) produced by a second set of one or more RAs can offer an advantageous alternative to conventional welding technologies. For example, a thermal system using the principles of the invention disclosed herein can be used in a thermal device suitable for underwater use; such a thermal device can provide a useful substitute for conventional oxyacetylene welding for use in submerged environments, because acetylene is unstable when stored in pressurized bottles/tanks; and explosive at pressures such as are found more than 10 meters underwater.

EXAMPLES

Example 1: Energy/Light Combed Activation (E/LC)

One hundred milligrams (100 mg) of powdered carbon was placed in a GG-EL graphite tubular reactor (15.875 mm) OD, with ID machined to ~9 mm). This reactor was inserted into a reactor assembly FIG 2A and then placed into a high vacuum oven for degassing according to the Degassing Procedure (See Profile 1 or Profile 2). After degassing, the reactor assembly is transferred to a test cell for processing. Research-grade Nitrogen (N2) was delivered at 2 SLPM to purge the system for a minimum of 25 seconds or more. The gases were fed through the E/MEE in a horizontal and level gas line, as described above. During purging, gas sampling lines are also purged. TEDLAR® sealed bags, when used, are connected to the sampling lines during the purge cycle.

Referring to FIG. 1, the argon “KC” light 108 located in position 0 (vertical lamp orientation; 7.62 cm from inlet or entrance flange; at 180°; bulb tip pointing up 2.54 cm from the outer diameter of the gas line) was turned on at the onset while simultaneously energizing the power supply to 5 amps. This light was kept on for a minimum hold time of 9 sec. Next light 109 in position 1 (109; horizontal lamp orientation; 7.62 cm from inlet or entrance flange; at 180°; bulb tip facing exit plate; bulb glass base at the optical entrance; 5.08 cm, from the outer diameter of the gas line), a krypton light, was turned on and the power is increased to 10 amps on the power supply. This was held for 3 seconds, light 107, in position 1 (107; horizontal lamp orientation; at 0°; bulb tip at the optical exit facing the exit plate; 5.04 cm from the outer diameter of the gas line), a xenon light was turned on and held for 9 seconds and the power was increased to 15 amps. After these 3 lights have been sequentially turned on, the sealed TEDLAR® bags are opened for gas collection, and the amperage delivered to reactor was adjusted to 100 amps and held for a minimum of 30 seconds. Immediately after the power was increased light 103 in position 1 (103; vertical lamp orientation; 7.62 cm from inlet or entrance flange; at 0°; bulb tip pointing down 2.54 cm from the outer diameter of the gas line), a neon light, was turned on.

Amperage harmonic patterning was then initiated on the reactor. With each amperage pattern (oscillation), the gases fed to the reactor can treated by the same or different light sequence. In one embodiment of the experimental protocol, the amperage of the reactor was increased to 78.5 amps over 1 second, the high-end harmonic pattern point. The amperage of the reactor was then decreased to 38.5 amps over 9 seconds and held at 38.5 amps for 3 seconds. Immediately at the start of the 3 second hold, an argon light 122 in position 1 (122; horizontal lamp orientation; at 180°; bulb tip pointing towards entrance plate at the optical entrance; 5.04 cm from the outer diameter of the gas line) was turned on. After the 3 second hold, amperage to the reactor was then ramped up to 78.5 amps over 9 seconds with a 3 second hold upon reaching 78.5 amps before a downward ramp was initiated. The reactor amperage was decreased to 38.5 amps, over 9 seconds and then held for 3 seconds. Immediately at the start of the 3 second hold, light 103 (103), a neon light in position 1, was turned on. The reactor amperage was again ramped up to 78.5 amps over 9 seconds, held there for 3 seconds, and then again ramped down to 38.5 amps over 9 seconds. A long-wave ultraviolet lamp (104; horizontal lamp orientation; at 90°; bulb tip facing entrance plate at the optical entrance; 5.04 cm from the outer diameter of the gas line) in position 1 was turned on.

The reactor was again ramped up to 78.5 amps over 9 seconds, held for 3 seconds, then decreased to 38.5 amps over another 9 seconds. Next a short-wave ultraviolet lamp (105 horizontal lamp orientation; 7.62 cm from inlet or entrance flange; at 270°; bulb tip at the optical entrance and facing the entrance plate; 5.04 cm from the outer diameter of the gas line) in the E/MEE (position 1) E/MEE section light was turned on and held for 3 seconds. The reactor was again ramped up to 78.5 amps over 9 seconds and held for 3 seconds. After the 3 second hold, the reactor amperage was decreased to 38.5 amps over another 9 seconds. The reactor was then held at 38.5 amps for 3 seconds, before another ramp up to 78.5 amps over 9 seconds was initiated. At 3 seconds into this ramp, lamp 107, in position 1 (107) was turned on and held there for the remaining 6 seconds of the 9 second total ramp. The reactor was held for 3 seconds in this condition.

The lights were turned off simultaneously in the E/MEE section as follows: (103), (108), (106), (105) and (104) and the reactor was deenergized. The reactor was held at this state, with continuous gas flow for 27 seconds during which the TEDLAR® bags are closed and removed. All remaining lights were turned off and gas flow continues for 240 seconds. Example 2: Degassing Profile 1

One hundred milligrams (100 mg) of powdered carbon was placed in a graphite tubular reactor (15.875 mm) OD, with ID machined to ~9 mm), as described above and loaded into a closed end system. After ten closed end set-ups have been completed, each individual unit was loaded into the degassing oven openings and all incoming and outgoing lines were connected to the closed end systems. Isolated each incoming line to each reactor while maintaining the outgoing lines in an open position. Started the vacuum system until the vacuum gauge reads at least 750 mmHg. Upon reaching 750 MmHg, closed all outgoing line valves from the closed end systems and secured the vacuum pump. Performed a 30-minute leak test of the system. After successfully passing the leak check, opened each incoming line to the closed end system one at a time at 0.4 slpm N ₂ . Once all incoming lines were open and the vacuum gauge reached a slight positive pressure, opened the outgoing gas line on the degassing oven. Started the degassing oven profde ramping from T _am b to 400°C over 1 hour while maintaining N ₂ flow. After the 1-hour ramp, maintained flow for an additional hour for temperature stabilization while maintaining gas flow. After the temperature stabilization was complete, secured all incoming gas flows and isolated the degassing oven vent line. Immediately started the vacuum pump and begin the degassing protocol. Maintained the temperature and vacuum for 12 hours. After the 12 hours, allowed the oven to cool prior to closed end unit removal.

Example 3: Degassing Profile 2

One hundred milligrams (100 mg) of powdered carbon was placed in a graphite tubular reactor (15.875 mm) OD, with ID machined to ~9 mm), as described above and loaded into a closed end system. After ten closed end set-ups have been completed, each individual unit was loaded into the degassing oven openings and connected all incoming and outgoing lines to the closed end systems. Isolated each incoming line to each reactor while maintaining the outgoing lines in an open position. Started the vacuum system until the vacuum gauge reads at least 750 mmHg. Upon reaching 750 MmHg, closed all outgoing line valves from the closed end systems and secured the vacuum pump. Performed a 30-minute leak test of the system. After successfully passing the leak check, opened each incoming line to the closed end system one at a time at 0.4 SLPM N ₂ . Once all incoming lines were open and the vacuum gauge reached a slight positive pressure, opened the gas outgoing gas line on the degassing oven. Started the degassing oven profde ramping from 200°C±50°C to 400°C over 1 hour while maintaining N ₂ flow. After the 1-hour ramp, maintained flow for an additional hour for temperature stabilization while maintaining gas flow. After the temperature stabilization was complete, secured all incoming gas flows and isolated the degassing oven vent line. Immediately started the vacuum pump and began the degassing protocol. Maintained the temperature and vacuum for 12 hours. After the 12 hours, allowed the oven to cool prior to closed end unit removal. Example 4: Gas analysis

For the chemical analysis of gas samples in TEDLAR® bags, a test protocol was developed based on the standard test method established for internal gas analysis of hermetically sealed devices. Prior to sample measurement, system background was determined by following exact measurement protocol that is used for sample gas. For system background and sample, a fixed volume of gas was introduced to the Pfeiffer QMA 200M quadrupole mass spectrometer (QMS) system through a capillary. Through a capillary, a fixed volume of gas was introduced to the Pfeiffer QMA 200M quadrupole mass spectrometer (QMS) system. After sample gas introduction, the ion current for specific masses (same as masses analyzed for system background) were measured. During background and sample gas analyses total pressure of the QMS system was also recorded, allowing for correction of the measured ion current.

Table 2: Gases analyzed for the test method and measured masses used in deconvolution.

Data analysis:

Measurements of the ion current for each mass were corrected to the average of measured background contributions corrected for pressure difference. Subsequent to the background correction, individual corrected mass signals were averaged and corrected to a known gas standard to determine the percent volume of 17 gas species. All corrections were determined using nitrogen and nitrogenhydrogen mixture reference gases analyzed to match selected process gas for test samples using the developed protocol based on the standard test method, in accordance with Military Standard (MIL- STD-883) Test Method 1018, Microcircuits, Revision L, FSC/Area: 5962 (DLA, 16 September 2019). Results below: l%=10,000 ppm, Volume values for gas blanks and samples were produced using the developed gas analysis test method and validated using a gas mixture standard of 99.98% nitrogen and 0.02% hydrogen. All analytical performed by EAG Laboratories, Liverpool, NY using standard TEDLAR® bag gas sampling protocols and specified mass spectrometry methods.

Mass Analyzer: Quadrupole mass spectrometer (Pfeiffer QMA 200M) Measurement mode: Analog scan for selected masses No. of channels used: 64

Mass resolution: Unit resolution Maximum detectable concentration: 100%

Minimum detectable concentration: 1 ppb Background vacuum: <2 x 10' ⁶ Torr

Results: Protocol 1:

Protocol 1 (cont.)

Protocol 2:

Standard (Nitrogen):

The patent and scientific literature referred to herein establishes the knowledge that is available to those with skill in the art. All United States patents and published or unpublished United States patent applications cited herein are incorporated by reference. All published foreign patents and patent applications cited herein are hereby incorporated by reference. All other published references, documents, manuscripts and scientific literature cited herein are hereby incorporated by reference.

While this invention has been particularly shown and described with references to preferred embodiments thereof, it will be understood by those skilled in the art that various changes in form and details may be made therein without departing from the scope of the invention encompassed by the appended claims. Additionally, while the invention has been described in connection with what is presently considered to be the most practical and preferred embodiment, it is to be understood that the invention is not to be limited to the disclosed embodiment, but on the contrary, is intended to cover various modifications and equivalent arrangements included within the spirit and scope of the appended claims. Numerical values where presented in the specification and claims are understood to be approximate values (e.g., approximately or about) as would be determined by the person of ordinary skill in the art in the context of the value. For example, a stated value can be understood to mean within 10% of the stated value, unless the person of ordinary skill in the art would understand otherwise, such as a value that must be an integer.