Systems and methods for local distribution, local consumption, and / or local storage of hydrogen gas

Abstract

Systems and related devices and methods for producing hydrogen gas for on-site distribution, on-site consumption, and / or on-site storage are disclosed herein. An exemplary system includes a pyrolysis reactor that can be coupled to a source of reactants comprising hydrocarbons. The pyrolysis reactor has one or more flow channels positioned to transfer heat to the reactants to convert the hydrocarbons into an output comprising hydrogen gas and carbon particulates. The system further includes a carbon separation system operably coupled to the pyrolysis reactor to separate the hydrogen gas and carbon particulates from each other in the output. In various embodiments, the system further includes a component for on-site consumption of the filtered hydrogen gas.

Description

Technical Field

[0001] This technology generally relates to systems for generating hydrogen gas from hydrocarbon fuels in situ. In particular, this technology relates to small-scale (e.g., residential-scale) pyrolysis reactor systems for generating hydrogen gas from natural gas and methane and consuming the same.

[0002] [Reference to Related Applications] This application claims priority to U.S. Provisional Patent Application No. 63 / 034,385, filed Jun. 3, 2020, and U.S. Provisional Patent Application No. 63 / 113,931, filed Nov. 15, 2020, which are hereby incorporated by reference in their entireties and made a part of this specification.

Background Art

[0003] Hydrogen is typically produced by large-scale reactors operating at high temperatures in industrial facilities. The produced hydrogen is then transported for use in fuel cells and / or other industrial processes such as producing fertilizers with a particular ammonia as the main component and / or for final use in other applications. In recent years, the use of hydrogen gas as a heat energy source for heating and electricity has attracted interest as an attractive stepping stone between current fossil fuel-based power generation systems and fully renewable energy systems because no greenhouse gases and other harmful chemicals are emitted during the combustion of hydrogen gas. However, the amount of heat released per mole when hydrogen gas is burned is less than that of natural gas, and thus an efficient production system is required.

[0004] Several methods for producing hydrogen include steam methane reforming (SMR), gasification, plasma-driven dissociation, thermal dissociation, and the thermal decomposition of gases, such as methane, using catalytic molten metals or salts. Recent technological advances in catalytic methane thermal decomposition have led to the development of novel combinations of molten metals and salts, enabling high conversion rates (over 50%) of methane at moderate temperatures (below 1100°C) using bubble tower reactors, where the conversion occurs at the heterogeneous interface between the fluid in the molten tower and the rising methane bubbles. These systems represent a promising development toward technological trends that enable hydrogen production without the simultaneous release of greenhouse gases, because carbon is naturally separated in solid form during the thermal decomposition reaction. To date, these methods have only been used for industrial-scale applications, which typically require large, continuous-operation reactors for industrial hydrogen production at a lower cost and / or lower carbon footprint than conventional SMR processes. [Overview of the project]

[0005] According to a first aspect of the present invention, a system for producing hydrogen gas that can be distributed locally, consumed locally, and / or stored locally, wherein the system is The system includes a pyrolysis reactor that can be coupled to a source of reactants containing hydrocarbons, the pyrolysis reactor having one or more flow channels positioned to transfer heat to the reactants to convert the hydrocarbons into an output containing hydrogen gas, carbon particulates, and heat, and the pyrolysis reactor is sized to receive the reactants at a flow rate of 500 to 1,000,000 standard cubic centimeters per minute. Includes a carbon separation system operably coupled to the pyrolysis reactor to separate hydrogen gas and carbon particulate matter in the output, A system is provided that includes a power generation component that can be coupled in-situ to a pyrolysis reactor to accept at least a portion of the output and convert this output into electricity.

[0006] According to another aspect of the present invention, a method for producing hydrogen gas that can be distributed locally, consumed locally, and / or stored locally, the method comprising: The process includes a step in the pyrolysis reactor where a fuel gas containing hydrocarbons is received at a flow rate of 500 to 1,000,000 standard cubic centimeters per minute. The step includes heating the fuel gas in the pyrolysis reactor to the reaction temperature, at which point at least a portion of the hydrocarbons in the fuel gas are converted into hydrogen gas and carbon particulate matter. The step includes separating and capturing hydrogen gas and carbon particles, A method is provided which includes the step of converting at least a portion of captured hydrogen gas into electricity using a power generation component, wherein the power generation component is coupled in-situ to a pyrolysis reactor. [Brief explanation of the drawing]

[0007] [Figure 1] This is a block diagram of a system for producing hydrogen gas that can be locally distributed, consumed, and / or stored, according to some embodiments of the present technology. [Figure 2] This is a block diagram of a system for producing hydrogen gas that can be locally distributed, locally consumed, and / or locally stored, according to another embodiment of the present technology. [Figure 3] This is a block diagram of a reactor system for producing hydrogen gas according to several embodiments of this technology. [Figure 4] This is a schematic diagram of a reactor system coupled to a carbon separator according to some embodiments of this technology. [Figure 5] This is a schematic diagram of a reactor system equipped with features for facilitating the efflux of carbon particles from the reactor system according to several embodiments of this technology. [Figure 6] This is a schematic diagram of a reactor system equipped with an integrated carbon separator configured according to various embodiments of this technology. [Figure 7] This is a schematic diagram of a reactor system equipped with an integrated carbon separator configured according to various embodiments of this technology. [Figure 8]This is a schematic diagram of a reactor system equipped with an integrated carbon separator configured according to various embodiments of this technology. [Figure 9] This is a schematic diagram of a reactor system equipped with an integrated carbon separator configured according to various embodiments of this technology. [Figure 10] This is a schematic diagram of a reactor system equipped with an integrated carbon separator configured according to various embodiments of this technology. [Figure 11] This is a schematic diagram of a reactor system including integrated heating features according to various embodiments of this technology. [Figure 12] This is a schematic diagram of a reactor system including integrated heating features according to various embodiments of this technology. [Figure 13] This is a schematic diagram of a reactor system divided into numerous reaction chambers according to various embodiments of this technology. [Figure 14] This is a schematic diagram of a reactor system coupled to a power generation system according to some embodiments of this technology. [Figure 15] This is a schematic diagram of a reactor system coupled to a household heating system according to some embodiments of this technology. [Figure 16] This is a block diagram of another reactor system for producing hydrogen gas according to some embodiments of this technology. [Figure 17A] Figure 16 is a schematic diagram of a reaction chamber used in a reactor system according to several embodiments of this technology. [Figure 17B] Figure 16 is a schematic diagram of a reactor system including a number of reaction chambers according to several embodiments of this technology. [Figure 18] According to several embodiments of this technology, the graph shows the relationship between the length of the reaction chamber and the temperature of the reactants flowing through the reaction chamber for various flow rates. [Figure 19] This graph shows the effect of the relationship between surface area-to-volume ratio and flow chamber diameter on the reaction within the reaction chamber, according to several embodiments of this technology. [Figure 20]A diagram showing representative dimensions of a reaction chamber that meets uniform reaction conditions to obtain the maximum pressure drop before and after the reactor according to some embodiments of the present technology. [Figure 21] A schematic diagram of a cyclone separator for separating carbon from hydrogen gas according to some embodiments of the present technology. [Figure 22A-C] A partial schematic isometric view (A, B, C) of a carbon collection system according to various embodiments of the present technology. [Figure 23] A table showing power, heating, cooling, and natural gas demand and usage for various representative applications according to some embodiments of the present technology.

Embodiments for Carrying out the Invention

[0008] The figures are not necessarily drawn to scale. Similarly, some components and / or operations can be separated into different block states from each other, or they can be combined into a single block state, the purpose of which is for the description of some specific embodiments of the present technology. Furthermore, the present technology can be realized in various modified and deformed forms, and specific specific embodiments are illustratively shown in the drawings and will be described in detail below. However, the present invention is not limited to the specific specific embodiments that illustrate the present technology.

[0009] Overview To enable the use of hydrogen produced by industrial reactors for residential and commercial building use, all existing natural gas pipelines would need to be replaced with hydrogen-compatible materials. This large-scale replacement of gas pipelines can be prohibitively expensive for widespread adoption. However, residential heating using fossil fuels is one of the biggest contributors to global greenhouse gas emissions. Therefore, switching to hydrogen combustion in residential heating appliances would yield extraordinarily large environmental benefits. Furthermore, hydrogen can be converted directly into electricity using fuel cells or other devices, or indirectly into electricity via thermoelectric converters and heat engines at the building level. Using hydrogen for on-site power generation (e.g., within the same building, within the same area, within a single appliance and / or housing, with traditional appliances and / or within spaces conventionally designated for on-site combined heat and power generation) would reduce reliance on carbon-emitting power sources, thereby providing even greater environmental benefits.

[0010] Systems for producing hydrogen gas for local distribution, local consumption, and / or local storage, as well as related apparatus and methods, are disclosed herein. In some embodiments, a typical system includes an input line connectable to a source of reactants containing hydrocarbons, and a reactor in fluid communication with the input line. The reactor has one or more flow channels positioned to transfer heat to the reactants to convert the hydrocarbons into an output (e.g., an output product stream) containing hydrogen gas, carbon particulate matter, and heat (and other gases, e.g., residual reactants). The system includes a carbon separation system operably coupled to the pyrolysis reactor to separate the hydrogen gas and carbon particulate matter in the output from each other. In various embodiments, the system further includes components for local consumption of the filtered hydrogen gas. For example, the system may include one or more burners for burning hydrogen gas, and one or more heat pathways coupled between the burners and the reactor for transferring heat from the burners to the reactor. To transfer heat, in one embodiment, the heat pathways can direct hot flue gas from the burners along and / or into the reactor.

[0011] The system may further include one or more generators operably coupled to the reactor and / or burner. The generators receive hydrogen and / or heat to produce electricity. The electricity can be used to power various components of the system and / or directed to a power grid. The power grid can power single-family homes, multi-family homes, commercial buildings, and / or any other suitable space. In some embodiments, more power is produced than the power consumed toward nearby use locations (e.g., at the building level). In some such embodiments, the excess power is exported to an external power source or a power grid. In some such embodiments, the excess power is stored in a secondary fuel cell for later consumption at building scale. The overall system may also further include a circulating system operably coupled to the generators by the reactor, burner, and / or heat path. The circulating system receives excess heat from other components in the system and circulates this heat within a heating network and / or hot water network for single-family homes, multi-family homes, commercial buildings, and / or any other suitable space.

[0012] As disclosed herein, the system can be scaled down to the level of a house, residential area, or single commercial building, thereby generating hydrogen near the point of use and thus avoiding the need to overhaul infrastructure to enable the construction of a hydrogen or hydrogen / natural gas mixed grid or infrastructure network. In other words, the disclosed system design enables partial or complete decarbonization of residential heating and / or electricity demand without any changes to the natural gas infrastructure network, because hydrogen is generated on-site from natural gas and also consumed on-site. However, small-scale pyrolysis reactors also present many challenges. To address these challenges, the various embodiments disclosed herein include features that utilize the modification of the pyrolysis reactor for small-scale applications and / or integration with a residential heating system.

[0013] For ease of reference, the systems and components described herein may be described herein with reference to the top, bottom, top, bottom, upward, downward, and / or horizontal, x-y plane, vertical, or z direction with respect to the spatial orientation state of the illustrated embodiments. However, it should be understood that the systems and components described herein can be moved to and used in different spatial orientation states without changing the structure and / or function of the embodiments disclosed in this Art.

[0014] Furthermore, although this specification primarily describes a system for decomposing natural gas into hydrogen gas for local consumption, the scope of this technology is not limited thereto, as will be understood by those skilled in the art. For example, the pyrolysis reactor described herein can also be used to decompose any other suitable hydrocarbon. Therefore, the scope of this technology is not limited to any particular subset of embodiments.

[0015] Description of the drawing Figure 1 is a block diagram of a system 100 capable of producing and / or utilizing (e.g., distributing, consuming, and / or storing) hydrogen gas on a localized scale or size according to some embodiments of the present technology. In some embodiments, the production and utilization of hydrogen gas in system 100 occurs within a single room. For example, system 100 can be embodied as a single electrical appliance positioned in a space conventionally occupied by a conventional natural gas furnace or burner, and / or can serve as a direct replacement for these conventional electrical appliances. In another embodiment, system 100 can take the form of a number of devices and / or electrical appliances operably connected to one another. Furthermore, in some embodiments, system 100 produces and utilizes hydrogen gas on other localized scales. For example, as will be described in detail below, System 100 can produce and utilize hydrogen gas for one-room apartments, single-family homes, multi-unit dwellings, apartments, residential areas, public facilities (e.g., single shops, government buildings, hospitals, schools, or any other suitable space), commercial buildings (e.g., office buildings), data centers, or any other suitable space. Because System 100 produces and utilizes hydrogen gas on-site, it can be implemented to replace and / or complement existing uses of hydrocarbon fuels (e.g., natural gas, methane, and other hydrocarbons) and existing power sources, without requiring any infrastructure overhaul.

[0016] In the illustrated embodiment, the entire system 100 includes a reactor system 110, one or more blowers 118, a power generation system 120, a circulation system 130, and a cooling system 140 separate from the circulation system 130. The reactor system 110 includes a reactor 112 operably connected to a fuel source 10 and a carbon separator 114 operably connected to the reactor 112. The reactants from the fuel source include hydrocarbons that can be decomposed by the reactor system 110. Examples of suitable reactants include natural gas, methane, gasoline, jet fuel, propane, kerosene, diesel, and / or any other suitable hydrocarbon fuel. As will be described in detail below, the reactor 112 receives the reactants and decomposes the hydrocarbons into hydrogen gas and carbon particulate matter, which is then sent to the carbon separator 114. The carbon separator 114 removes the carbon particulate matter from the hydrogen gas, thereby producing hydrogen fuel. The carbon separator 114 can then collect carbon particles and direct them to a carbon disposal component 20 (e.g., an empty bin into which carbon can be disposed of or resold), while the hydrogen gas is available within the reactor system 110 and / or elsewhere in the entire system 100. For example, in the illustrated embodiment, the reactor system 110 further includes one or more burners 116 operably coupled to one or more blowers 118 to burn the hydrogen gas. A heat path between the burners 116 and the reactor 112 can transfer the heat generated by burning the hydrogen gas. For example, the heat path can direct hot flue gas around and into the reactor 112. The reactor 112 receives heat from the burning hydrogen gas and uses this heat to decompose further hydrocarbons.

[0017] Additionally or alternatively, the reactor system 110 can direct hydrogen gas to the power generation system 120 (where the hydrogen gas is consumed) and / or to the hydrogen storage component 30 for distribution and / or subsequent consumption. For example, the hydrogen storage component 30 can be used to reheat the reactor 112 after a period of non-use of the fuel for combustion. For a reactor 112 containing about 10 kilograms (kg) of KCl, the amount of energy required to heat the reactor 112 from room temperature to an operating temperature of about 1000°C is approximately 11,000 kilojoules (kJ). Assuming that the heat is utilized relatively completely, this energy can be generated by burning about 860 standard liters of hydrogen gas. In another embodiment, utilizing hydrogen storage can decouple hydrogen generation from hydrogen consumption. That is, stored hydrogen can complement and / or replace the flow of hydrogen produced during periods of high demand. In another embodiment, stored hydrogen can also be redistributed within the hydrogen infrastructure network. Using a hydrogen infrastructure network, fuel cells (e.g., fuel cells used later by System 100, fuel cells used in automobiles, and / or any other suitable fuel cells) can be charged and / or hydrogen can be redistributed to nearby apartments, houses, and / or buildings in response to high energy demand with minimal additional infrastructure.

[0018] Non-limiting examples of materials that can be used to store hydrogen include typical gas storage tanks and solid materials (or solid substances), such as zeolites, Pd, H3N:BH3, and / or any of the solid materials listed in Table 1 below. TIFF2023528472000002.tif147156 Table 1

[0019] As shown in Figure 1, the power generation system 120 further includes one or more burners 116 operably coupled to a blower 118 for burning hydrogen gas, and one or more generators 124 operably coupled to the output of the burners 116 and / or reactor 112 (e.g., hot gas, hydrogen gas, and / or heat via a physical heat transfer medium, e.g., heat via a heat transfer fluid). The generators 124 generate electricity using flue gas from the burners 116, heat from the burners 116, and / or output from the reactor 112. In various embodiments, the generators 124 include thermoelectric converters, thermophotovoltaic systems, alkali metal thermoelectric converters (AMTECs), fuel cells, internal combustion engines, turbines, microturbines, thermionic generators, steam turbines, and / or Stirling engines. The power generation system 120 can then direct the generated electricity to the power transmission network 40 for local consumption, local storage, and / or local distribution. For example, the power transmission network 40 may include a secondary battery for storing a portion of the generated electricity and various electronic devices in the home that consume a portion of the generated electricity. As described above, in some embodiments, more electricity is generated than is consumed near the point of use (e.g., on-site). In some such embodiments, the excess electricity is exported to the power transmission network 40 and / or stored in a secondary fuel for later consumption.

[0020] Furthermore, as shown in Figure 1, the power generation system 120 can direct excess high-temperature flue gas and / or heat to the reactor system 110 and / or circulation system 130. The reactor system 110 uses the unconverted heat and flue gas to help heat the reactor, thereby allowing further hydrocarbons to be decomposed into hydrogen gas. The reactor system 110 can then direct the excess and / or parasitic (as an undesirable incidental) heat lost to the circulation system 130 (for example, by the flow of high-temperature gas and / or high-temperature fluid and / or via a physical heat transfer medium, such as a heat transfer fluid or other suitable heat transfer medium).

[0021] In the illustrated embodiment, the circulation system 130 includes a condensing heat exchanger 132 operably coupled to the reactor system 110, a heat sink 134 operably coupled to the power generation system 120, and a circulation pump 136 operably coupled to the condensing heat exchanger 132 and the heat sink 134. The condensing heat exchanger 132 receives excess and / or parasitic heat lost from the reactor system 110. The condensing heat exchanger 132 then reuses the heat (e.g., in a boiler, furnace, and / or similar equipment) to circulate the heat into the heating system network 50. For example, the condensing heat exchanger 132 can use the excess heat from the reactor 112 to supply hot water for the apartment. The heat sink 134 receives excess and / or parasitic heat lost from the power generation system 120. The circulation pump 136 then circulates a fluid (e.g., water, air, or other suitable heat transfer fluid) along the heat sink 144 and the condensing heat exchanger 132, transferring heat from the heat sink 144 to the condensing heat exchanger 132, thereby further sending it into the heating network 50 for reuse.

[0022] Furthermore, as shown in Figure 1, after the components of system 100 have extracted heat from the flue gas for various uses, system 100 may direct the flue gas to the exhaust system 60. In some embodiments, system 100 replaces all hydrocarbons in the reactants with hydrogen gas products from reactor system 110. Thus, in these embodiments, the flue gas contains only water vapor, only oxygen gas, and / or any other molecules present in the air from blower 118 (e.g., nitrogen gas). In other words, the flue gas does not contain any new carbon dioxide molecules that would normally result from the combustion of hydrocarbons. In some embodiments, the exhaust system 60 utilizes an existing ventilation system in the space where system 100 is implemented (e.g., an existing exhaust system for directing carbon dioxide away from the furnace).

[0023] Furthermore, as shown in Figure 1, the power generation system 120 is preferably directed to the cooling system 140, which uses the heat and / or electricity to circulate cool air. In various embodiments, the cooling system 140 may include an absorption chiller, a compression air conditioner, and / or a heat pump. In some embodiments, the cooling system 140 is operably coupled directly to the reactor system 110 to receive hydrogen gas and / or heat (not shown). In such embodiments, the cooling system 140 uses the hydrogen gas and / or heat to drive a cooling system, e.g., any of the systems described above. Furthermore, in some embodiments, the cooling system 140 may be integrated with and / or incorporated into the circulation system 130.

[0024] In some embodiments, the reactor system 110 and / or power generation system 120 may direct heat and / or electricity to heating and / or cooling components without circulating energy. For example, a heating component (e.g., a condensing heat exchanger 132) receives heat from the reactor 112, transfers this heat to a fluid (e.g., water, air, or another suitable fluid), and directs the heated fluid into the heating system network 50, rather than returning and receiving the fluid back. In a particular embodiment, the heating component receives heat from the reactor 112, transfers this heat to water from an external source, and directs the hot water into the living space. The used hot water then flows out into the sewer and / or household wastewater treatment system, rather than circulating back into the circulation system 130. In another embodiment, a cooling component may receive heat and / or electricity from the power generation component 124, use the heat and / or electricity to drive a cool air generator, and direct the cool air into the living space. Next, the cool air dissipates within the living space, while the cooling components can draw in fresh cooling air from an external source.

[0025] In various embodiments, the reactor system 110, power generation system 120, circulation system 130, and / or cooling system 140 may include one and / or two or more sensors (not shown) to collect data related to the components of the system. For example, the sensors can measure the weight or optical properties of the solid carbon produced by the reactor system 110. The data from these sensors can then be used to create a report on the amount of carbon removed from the reactants, thereby allowing the user to access carbon credits or carbon credit or carbon reduction payments (e.g., from state, federal, and / or commercial carbon markets). The data can also be used to alert the user if the carbon disposal component 20 is full (or nearly full), thereby prompting the user to empty the carbon disposal component 20.

[0026] In some embodiments, the sensor can measure electrical properties (e.g., conductivity, frequency-dependent conductivity, electrical impedance spectroscopic properties, and / or any other suitable properties) at the reactor 112. In some embodiments, the sensor can perform ultrasonic measurements to calculate the flow rate of reactants through the reactor 112 and / or the amount of carbon deposits in the reactor 112. In some embodiments, the gas flow sensor can calculate the ratio of reactants (e.g., methane) to products (e.g., hydrogen) flowing out of the reactor 112. In such embodiments, this ratio can be said to indicate the degree of the pyrolysis reaction occurring in the reactor 112. In some embodiments, thermocouples or other temperature sensors measure the temperature of the reactor 112, flue gas from the burner 116, the generator 124, the condensing heat exchanger 132, and / or any other suitable components of the system 100. In some embodiments, a hydrogen gas sensor (e.g., a sensor that passes an electric current through a palladium wire) monitors the reactant conversion rate and / or the hydrogen production rate.

[0027] In some embodiments, system 100 includes a controller 150 operably coupled to the system's sensors and various components via an input / output (I / O) link. Based on any of the above-mentioned measurements, the controller 150 can adjust the operation of system 100. For example, the controller 150 can adjust the input flow rate of reactor 112 and / or the operating temperature of reactor 112 based on the measured ratio of reactant to hydrogen gas coming out of reactor 112 (e.g., to increase or decrease the amount of hydrogen in this ratio). In some embodiments, the controller 150 includes a memory storing past conditions and hydrogen consumption, as well as a predictive analytics component. Based on any of the above-mentioned measurements and data from memory, the predictive analytics component can determine the degree of adjustment regarding the operation of any of the components in system 100, and the controller 150 can complete this adjustment. For example, predictive analytics can determine periods of high and low hydrogen demand, and the controller 150 can toggle reactor 112 on and off according to the determined periods (e.g., by starting or stopping the reactant input).

[0028] As described above, system 100 is scaled to produce and utilize hydrogen gas for one-room apartments, single-family homes, multi-unit dwellings, apartments, residential areas, public facilities (e.g., single shops, government buildings, hospitals, schools, or any other suitable space), commercial buildings (e.g., office buildings), data centers, or any other suitable space. The scale is best quantified in terms of typical reactant consumption. For example, when methane is used as the reactant, typical scales include a natural gas flow rate range of approximately 500 standard cubic centimeters (sccm) per minute to approximately 37,500 sccm for a single-family home (e.g., a standalone house or a single unit in a multi-unit dwelling), a natural gas flow rate range of approximately 150,000 sccm to approximately 3,750,000 sccm for a multi-unit dwelling with a centralized system 100, and a natural gas flow rate range of approximately 150,000 sccm to approximately 3,750,000 sccm for a residential area with a centralized system 100. In another quantification example, when methane is used as the reactant, typical scales include natural gas consumption of approximately 10 million British pounds of thermal units (MMBtu / year) to approximately 164 MMBtu / year (or approximately 15,981 Btu / hour to approximately 18,721 Btu / hour) for a single-family home, natural gas consumption of approximately 4,875 MMBtu / year to approximately 6,300 MMBtu / year for a small apartment complex, and commercial buildings with centralized systems (e.g., industrial sites, offices, campuses, etc.). Examples of natural gas consumption include approximately 9,500 MMBtu / year to approximately 136,189 MMBtu / year for ports, hospitals, malls, and / or any other suitable commercial buildings; approximately 453,963 MMBtu / year to approximately 1,232,184 MMBtu / year for large residential complexes and / or residential areas; and approximately 2,468,421 MMBtu / year to approximately 3,350,000 MMBtu / year for data centers with high power and cooling demands.

[0029] Figure 23 is a table listing additional examples of scales for various applications and the power consumed by specific components of System 100 at different scales. As shown, the table shows the approximate scales for each embodiment in terms of power, heating, cooling, and natural gas required for different embodiments of System 100 (Figure 1), as well as demand and usage. Exemplary scales include the usage and related needs of residential, commercial, district, and data center facilities for power, heat, and cooling. Thus, the table in Figure 23 provides a technical background for distinguishing the needs and system requirements for these embodiments, in contrast to the extremely large scales used in the industrial production of hydrogen. However, as should be understood, the values ​​in the table in Figure 23 are shown exemplarily only, and the present invention is not limited to the specific embodiments shown.

[0030] Returning to Figure 1 and referring to it again, for any of the above-mentioned applications, system 100 is preferable to include multiple reactors 112 to meet the consumption demands of the space in which system 100 is deployed. For example, when methane is used as the reactant, a single reactor may exhibit a CH4 consumption of approximately 500 sccm to approximately 172,853,881 sccm, or approximately 10 MMBtu / year to approximately 3,350,000 MMBtu / year. This range is significantly lower than the typical output of an industrial pyrolysis reactor, even when multiple reactors 112 are used in cooperation. In order for reactors 112 to be able to operate efficiently at the scale required for localized consumption, particularly at the residential level, the reactors include features to address numerous shortcomings.

[0031] Firstly, in a typical embodiment, the carbon produced by the pyrolysis reaction is removed from the reactor 112 and separated from the production logistics, while balancing concerns regarding safety, efficiency, and convenience. For example, it is preferable to remove the carbon from the reactor 112 in a manner that results in the separation of the user from the relatively high-temperature components of the reactor 112. Furthermore, the carbon should be separated by a system that does not require maintenance too frequently (e.g., hourly, daily, weekly, etc.), otherwise the user may be reluctant to adopt the reactor. In another embodiment, it is preferable that the carbon be separated by a system that does not consume excessive power, otherwise the efficiency of system 100 may fall below a usable level. Therefore, in various embodiments, it is preferable that the reactor system 110 includes features that help to alleviate these concerns.

[0032] Secondly, due to the periodic and / or uneven demand for heat and electricity in residential and / or single-building environments, the output of reactor 112 may often need to be adjusted. In some embodiments, the target adjustment scale is on the order of minutes to hours. Furthermore, in some embodiments, the adjustment includes periods when hydrogen gas is not required (e.g., on a workday when no one is in the house) and periods when hydrogen gas is required at a rate higher than the rate at which hydrogen gas can be produced by the reactor (e.g., during peak power consumption times).

[0033] Thirdly, reactor 112 may be subject to space constraints, for example, when the reactor is retrofitted into existing equipment space (e.g., furnace space). Therefore, it is desirable that reactor 112 has features that allow a reactor 112 adapted to space constraints to operate efficiently despite those constraints. In connection with this, it is desirable that system 100 and / or reactor 112 have features that help reduce and / or minimize parasitic heat losses, thereby increasing (or maximizing) the energy efficiency from reactor 112. For example, as mentioned above, it is desirable that reactor 112 be coupled to circulation system 130 to regenerate parasitic heat losses within the circulation system 130. Concerns regarding the efficiency of system 100 and / or reactor 112 may be particularly important in residential-scale reactors, as such reactors may have a relatively high surface area-to-volume ratio compared to industrial-scale towers, and therefore may exhibit more parasitic heat losses. Furthermore, it is preferable that the reactor 112 has a monitoring and control system specific to residential scale and / or local consumption of hydrogen gas products.

[0034] Further details regarding the features that system 100 and / or reactor system 110 include in order to solve these problems will be described with reference to Figures 3 to 19 below.

[0035] Figure 2 is a block diagram of a system 100 for producing hydrogen gas that can be distributed, consumed, and / or stored locally, according to another embodiment of the present technology. The system 100 shown in Figure 2 is substantially the same as the system 100 described above with reference to Figure 1. For example, as shown, the system 100 includes a reactor system 110 operably coupled to a fuel source 10, a power generation system 120 operably coupled to the reactor system 110, and a circulation system 130 operably coupled to the reactor system 110 and the power generation system 120. However, in the illustrated embodiment, the output of the generator 124 has been modified. For example, as shown, electricity from the generator 124 can be sent to the reactor system 110 to power one or more components in the reactor system. For example, the electricity can power a heat generator (e.g., a resistive coil coupled to the reactor, input valve, output valve, carbon separator 114, and / or any other suitable component). In the illustrated embodiment, the high-temperature flue gas from the generator 124 is sent directly to the condensing heat exchanger 132 to deliver heat to the circulation system 130.

[0036] Figure 3 is a schematic diagram of the material flow through the reactor system 110 according to several embodiments of the present technology. As shown in the figure, the reactants enter the reactor along the input path 302. As mentioned above, the reactants are preferably natural gas and / or pure methane. Therefore, the input path 302 is preferably connected to an existing gas line to supply the reactants to the reactor 112. The reactor 112 controlsly heats the reactants above the enthalpy point, where the enthalpy point represents the minimum energy at which some amount of the pyrolysis reactants is produced (for example, the reactor 112 provides at least an initiation energy). As a result, the reactor 112 produces a pyrolysis reaction that decomposes the hydrocarbons in the reactants into hydrogen gas and carbon. For example, in the case of a methane reactor, the pyrolysis reaction is represented by the following equation: CH4 (gas) → C (solid) + 2H2 (gas) Furthermore, in the case of CH4, the enthalpy point is approximately 75 kJ per mole of CH4, thereby raising the temperature of CH4 to approximately 650°C. In some embodiments, the reactor 112 controlsly heats the reactants to a temperature above approximately 1300°C in order for the pyrolysis reaction to occur completely during a relatively short residence time (e.g., a few seconds). In some embodiments, the reactor 112 is or includes a heated column containing a molten material, e.g., molten metal, molten salt, and / or a combination thereof. The hot liquid may contain a pure substance or a mixture of many substances. In such embodiments, the reactants are fed below the surface of the liquid in the reactor 112, for example, by a subsurface feed tube or a porous spurger. The reactor includes components for separating the reactants into a buoyant state, which are carried to the top of the heated column by their buoyancy. As the bubbles rise, the hot liquid transfers heat to the reactants, causing the pyrolysis reaction described above. In some embodiments, the reactor 112 may have one or more heat storage devices, which may have reaction chambers according to some embodiments described below. Each reaction chamber may have one or more channels for a heat exchange material and reactants in the heat exchange material. The heat exchange material may be selected based on its relatively low thermal conductivity, relatively low coefficient of thermal expansion, and / or relatively high thermal stability. In various embodiments, the heat exchange material may include cordierite, mullite, alpha-alumina, and / or combinations thereof. As the reactants flow through the channels, the heat exchange material transfers heat to the reactants to produce the thermal decomposition reaction described above.

[0037] Furthermore, as shown in Figure 3, the output from reactor 112 is split into hydrogen pathway 310 and carbon pathway 320, corresponding to the two products from the pyrolysis reaction. Hydrogen gas is directed into hydrogen pathway 310, and carbon particles are directed into carbon pathway 320. As described above, the hydrogen in hydrogen pathway 310 can be directed back to somewhere else in reactor system 110 and / or system 100 (Figure 1). On the other hand, carbon pathway 320 is preferably directed to a disposal system (e.g., carbon disposal component 20 as described with reference to Figure 1). As shown, carbon pathway 320 is preferably in fluid communication with blower 118, thereby helping to ensure that carbon particles move completely to carbon disposal component 30 (Figure 1) without blocking the outlet from reactor 112. In some embodiments, the splitting is achieved by a carbon separator (not shown) that is separate from reactor 112 and in fluid communication with it. In some embodiments, the separation is carried out by a carbon separator (not shown) integrated into the reactor 112, as will be described in detail below with reference to, for example, Figures 6 to 8.

[0038] In the illustrated embodiment, the reactor system 110 further divides the hydrogen gas hydrogen pathway 310 into first and second hydrogen pathways 312 and 314. A portion of the hydrogen gas is directed toward the burner 116 in the first hydrogen pathway 312. The burner 116 mixes the hydrogen gas in the first hydrogen pathway 312 with air from the blower 118 in the air input pathway 304 and burns it, supplying heat to the reactor 112. This heat compensates for parasitic heat loss from the reactor 112 and supplies the energy necessary to heat the reactants above their enthalpy point, thereby causing a thermal decomposition reaction. On the other hand, a portion of the hydrogen gas is directed toward exiting the reactor system 110 along the second hydrogen pathway 314 for any purpose described above with reference to Figure 1. That is, the hydrogen gas directed out of the reactor system 110 along the second hydrogen pathway 314 may be used to generate heat and / or electricity within the system 100, stored for later use, and / or used for further distribution. For example, in neighborhood or multi-household scale systems, the hydrogen gas exiting the reactor system 110 along the second hydrogen pathway 314 may be distributed to individual homes or units through a piping system for local consumption.

[0039] Furthermore, as shown in Figure 3, the flue gas from the burner 116, after heating the reactor 112, exits the reactor system through the flue path 334. In some embodiments, the flue path 334 is directed to other systems for consumption (e.g., to the power generation system 120 and / or circulation system 130 described above with reference to Figure 1). In some embodiments, the flue path 334 is directed to an outlet and discharged (e.g., into the exhaust system 60 described above with reference to Figure 1).

[0040] In the following description, Figures 4 to 15 illustrate the system features used in a molten material embodiment of reactor 112, and Figures 16 to 21 illustrate the system features used in a regeneration reaction chamber embodiment of reactor 112. However, as will be understood by those skilled in the art, such embodiments are not necessarily limited to those described in these embodiments. For example, arranging reactor 112 in parallel with generator 124, which will be described later with reference to Figure 14, is not limited to the molten material embodiment of reactor 112. Therefore, the scope of protection of this technology is not limited to any subset of the embodiments described below.

[0041] Figure 4 is a schematic diagram of a reactor system 110 configured according to several embodiments of the present technology. In the illustrated embodiment, the reactor 112 has a body 412 having a first end 414 and a second end 416. The portion of the reactor 112 near the first end 414 is in fluid communication with a reactant source (e.g., a fuel source 10 (Figure 1)) and sends the reactant in the input path 302 to the body 412. The body 412 has a molten material 418, which controlsly imparts heat to the reactant bubbles 419 flowing from the first end 414 toward the second end 416. The heat from the molten material 418 causes a thermal decomposition reaction to occur within the body 412. The resulting carbon particulate matter and hydrogen gas exit the body 412 toward the second end 416 along a first outlet path 420. In some embodiments, a portion of the total carbon particles is not carried out of the main body 412 by the flow of hydrogen gas along the first outlet path 420. Therefore, in some embodiments, for example, as described below in detail with reference to Figures 6 to 10, the main body 412 preferably has an integrated carbon separator that separates a portion (or all) of the carbon from the hydrogen gas and molten metal within the main body 412. For example, in some embodiments, as described below in detail with reference to Figure 5, the main body 412 preferably has the feature of increasing the amount of carbon carried out of the reactor 112 along the first outlet path 420.

[0042] The first outlet path 420 sends carbon particulate matter and hydrogen gas to one or more carbon separators 114 (two are shown, referred to as the first carbon separator 114a and the second carbon separator 114b, respectively). The carbon separators 114 can sequentially remove particles based on their particle size and / or composition. For example, the first carbon separator 114a removes relatively large-diameter carbon particulate matter and / or carbon particulate matter contaminated with molten metal (e.g., carrying some molten metal), and the second carbon separator 114b removes small-diameter particles to further remove impurities from the output stream of hydrogen gas. In the illustrated embodiment, the first carbon separator 114a removes contaminated particles from the first outlet path 420. The first carbon separator 114a then sends the contaminated particles back to the main body 412 along the reintroduction path 422, and directs the filtered output towards the second carbon separator 114b along the second outlet path 424. The second carbon separator 114b can remove uncontaminated carbon particles from the output of the second outlet path 424. The second carbon separator 114b can then direct the filtered hydrogen gas outward along the hydrogen path 310 and the solid carbon outward along the carbon path 320.

[0043] The main body 412 is preferably made from a material with a melting point higher than the operating temperature of the reactor 112. For example, in one embodiment, the main body 412 is preferably made from quartz. Furthermore, as described above, the molten material 418 may contain a suitable molten metal, a molten salt, and / or a combination thereof. The molten material 418 may consist of a pure material (e.g., a single molten metal) or a mixture of various materials (e.g., various molten metals).

[0044] As described above, one challenge in the efficient operation of reactor 112 is to efficiently and safely remove carbon from reactor 112 and / or from the hydrogen gas in the reactor's output flow. Figures 5 to 10 are schematic diagrams of reactor 112 of the type shown in Figure 4, such reactors are equipped with features for removing carbon from reactor 112 and / or output according to various embodiments of the present technology.

[0045] Figure 5 is a schematic diagram of a reactor system 110, characterized by features that facilitate the outflow of carbon particulate matter from reactor 112, according to several embodiments of the present technology. Similar to reactor 112 described above with reference to Figure 4, the illustrated reactor has a body 412 extending from a first end 414 to a second end 416. The first end 414 is in fluid communication with the reactant source, and the second end 416 is in fluid communication with the other components of the reactor system 110. In the illustrated embodiment, the body 412 of reactor 112 has a conical component 520 that helps to facilitate the outflow of fluid from the second end 416 of reactor 112 and carry away carbon particulate matter. For example, the diameter of the body 412 is relatively large. Thus, within the body 412, the reactants can have a low empty velocity that allows the thermal decomposition reaction to proceed completely. In the first region 522 of the conical component 520, the conical component 520 has a diameter that is overall fitted to the body to transfer the reactor output to the conical component 520. In the second region 524, the diameter gradually decreases, thereby increasing the gas emptying velocity of the output. In the third region 526 near the second end 416, the diameter is even smaller. As a result, in the third region 526, the gas emptying velocity of the output allows light carbon particles (e.g., carbon with little or no metal contamination) to be carried out of the reactor 112 and directed towards the carbon separator 114. In the illustrated embodiment, the reactor system 110 includes a single carbon separator 114 that directs filtered hydrogen gas from the output to the hydrogen path 310 and carbon particles from the output to the carbon path 320.

[0046] Figures 6 to 10 are schematic diagrams of reactors 112 of the type shown in Figure 4, having an integrated carbon separator 114 according to various embodiments of the present technology. For example, similar to the reactor 112 described above with reference to Figure 4, each of the reactors 112 shown in Figures 6 to 10 has a body 412 extending from a first end 414 to a second end 416. The first end 414 is in fluid communication with the reactant source, and the second end 416 is in fluid communication with other components of the reactor system 110. As described above, in some embodiments, the output flow does not carry all (or some) of the carbon particles out of the reactor 112. In such embodiments, the reactor 112 is preferably equipped with one or more of the integrated carbon separators 114 described below to avoid large carbon buildup within the reactor 112.

[0047] In some embodiments, as shown in Figures 6, 7, and 10, the carbon particles concentrate on the upper surface 418a of the molten material 418. For example, in some embodiments, the flow of reactants through the main body 412 is sufficient to propel the carbon particles into the molten material 418, but insufficient to carry them above the metallic material. Therefore, it is preferable for the reactor 112 to have a carbon separator 114 that scoops up the upper surface 418a of the molten material 418 to remove carbon from the reactor 112.

[0048] For example, as shown in Figure 6, the carbon separator 114 may have a mechanical scooping component 622 that scoops up the top surface 418a to push the carbon deposit 620 out of the reactor 112 and into the carbon pathway 320 toward the carbon disposal component 20. Alternatively or additionally, the carbon separator 114 may have a fluid scooping component 722, as described with reference to Figure 7. The fluid scooping component 722 can direct a fluid (e.g., air or any other suitable fluid) across the top surface 418a of the molten material 418 to push the carbon deposit 620 out of the reactor 112 and into the carbon pathway 320 toward the carbon disposal component 20. In some embodiments, the mechanical scooping component 622 and / or the fluid scooping component 722 periodically scoop up the top surface 418a. For example, the mechanical scooping component 622 and / or the fluid scooping component 722 are good at scooping the top surface 418a while the reactor 112 is inactive (e.g., during periods of hydrogen gas consumption). In some embodiments, the mechanical scooping component 622 and / or the fluid scooping component 722 continuously scoop the top surface 418a. In some embodiments, the mechanical scooping component 622 and / or the fluid scooping component 722 continuously scoop the top surface 418a only for a specific (e.g., rerun, ideal) period. For example, the mechanical scooping component 622 and / or the fluid scooping component 722 are better suited to continuously scooping the top surface 418a while the reactor 112 is operating to keep the top surface 418a clear, and to reducing the scooping of the top surface 418a while the reactor 112 is inactive to improve the efficiency of the reactor system 110 (Figure 1).

[0049] Additionally or alternatively, as shown in Figure 10, for example, the reactor 112 may have a passive carbon separator 114 through which carbon from the upper surface 418a of the molten material 418 can fall out of the reactor 112 and / or fall into the carbon disposal component 20. In some such embodiments, for example, in the embodiment shown in Figure 10, the body 412 of the reactor 112 preferably has a passive carbon separator 114. In the illustrated embodiment, the carbon separator 114 has an opening in the body 412 of the reactor through which carbon accumulated on the upper surface 418a of the molten material 418 can fall out of the reactor 112 and fall into the carbon pathway 320 toward the carbon disposal component 20. One advantage of the passive carbon separator 114 is that the efficiency of the system 100 (Figure 1) is improved because less (or no) energy is required to remove the carbon from the reactor 112. However, the passive carbon separator 114 may also reduce the efficiency of the reactor 112 if too much heat escapes through it.

[0050] In some embodiments, as shown in Figure 8, carbon particles concentrate around carbon accumulation zones 820 within the molten material 418. For example, in some embodiments, carbon accumulation zones 820 occur around the point where the reactants reach their enthalpy and a thermal decomposition reaction takes place. That is, after the thermal decomposition reaction, some of the carbon particles cease to flow, while hydrogen gas and / or other carbon particles continue to pass through the molten material 418. Therefore, in some embodiments, the reactor 112 has a carbon separator 114 that collects carbon at a precipitate component 822 within the molten material 418 for periodic and / or continuous removal. In such embodiments, the precipitate component 822 collects carbon in the molten material 418 while also helping to control the precipitation of carbon from the output.

[0051] In some embodiments, as shown in Figure 9, the carbon particles are concentrated around the bottom surface 418b of the molten material 418 and near the first end 414 of the reactor 112. For example, in some embodiments, some of the carbon resulting from the pyrolysis reactor is denser than the high-temperature molten material 418, and therefore such carbon settles toward the first end 414 of the body 412. Therefore, in some embodiments, the first end 414 of the body 412 preferably has a surface 415 that slopes toward a portion 922 of the carbon separator 114 located at the lowest part of the body 412. At the lowest part, the portion 922 of the carbon separator 114 can collect carbon deposits 920 from the body 412 and direct the carbon particles into the carbon pathway 320 toward the carbon disposal component 20. In some embodiments, the density of the molten material 418 is adjusted relative to the carbon density by selectively adding one or more catalytically inert components to the molten material 418 and / or by adjusting the temperature of the molten material 418. In such embodiments, the density of the molten material 418 is reduced, thereby causing the carbon in the molten material 418 to settle toward the component 922 of the carbon separator 114 for collection and removal.

[0052] As mentioned above, another challenge regarding the efficient operation of reactor 112 is adapting the reactor to periodic and / or non-uniform demand curves for hydrogen and / or electricity. Therefore, in some embodiments, reactor 112 is preferable to have features that address the non-uniform demand curves typical of residential-scale reactors. For example, in the case of a periodic demand curve that includes periods when no (or little) hydrogen or energy is needed, reactor 112 is preferable to have features that allow reactor 112 to cool or rapidly reheat in response to demand. Alternatively or additionally, reactor 112 is preferable to have features that generate a small amount of heat to offset regulated heat losses during periods when no (or little) hydrogen or energy is produced, resulting in shorter reheat periods when demand increases. Additional details of typical solutions are described below with reference to Figures 11-13.

[0053] Figures 11 and 12 are schematic diagrams of a reactor system 110 including rapid heating features integrated into the reactor 112 according to various embodiments of the present technology. As described with reference to Figure 11, the body 412 of the reactor 112 is preferably surrounded by a chamber 1140. The chamber 1140 has a space 1142 and one or more electric heaters 1144 (two are shown). During periods of low demand, the space 1142 is preferably evacuated to reduce parasitic heat loss (e.g., by creating at least a partial vacuum). In some embodiments, the inner surface of the chamber 1140 has a reflective effect to further reduce parasitic heat loss. When demand begins to increase, the space 1142 is preferably filled (e.g., with air), and the electric heaters 1144 are preferably pumping heat around the body 412, while a burner 116 pumps heat into the body 412 to rapidly reheat the reactor 112. In some embodiments, the electric heater 1144 transfers heat around the main body 412 during periods of low demand to further reduce parasitic heat loss. Furthermore, in some embodiments, the chamber 1140 has a generator (e.g., a thermoelectric generator) that captures a portion of the parasitic heat loss. In some such embodiments, the captured parasitic heat loss is then used to power the electric heater 1144 to reheat the reactor.

[0054] As shown in Figure 12, the reactor preferably has a reheat system 1240 integrated into the body 412 of the reactor 112. In the illustrated embodiment, the reheat system 1240 has a heating coil 1242 embedded in the molten material 418 and connected to a supply line 1244 located outside the body 412. The heating coil 1242 may be an electric coil (resistive or inductive) and / or a fluid coil (e.g., a hot gas, including flue gas from a burner). By integrating the reheat system 1240 with the body 412 of the reactor 112, the reheat system 1240 can rapidly deliver heat to the center of the reactor, which may reheat slowly if not configured in this way. For example, if the temperature of the body 412 falls below the melting point of the molten material 418, some of the material may solidify, obstructing the flow of gas and / or material through the body 412 during reheating. Therefore, heating the center of the body 412 requires heat conduction from the outer surface of the body 412. By simultaneously supplying heat to the center of the body 412, the reheat system 1240 can accelerate the rate at which the reactor 112 is reheated. Furthermore, in some embodiments, the heating coil 1242 can supply heat to the body 412 during periods of low demand, thereby counteracting the effects of parasitic heat loss.

[0055] As can be understood, in some embodiments, the reactor system 110 may have both the chamber 1140 described above with reference to Figure 11 and the reheat system 1240 described above with reference to Figure 12 in order to accelerate the reheat process. Furthermore, in various embodiments, the reactor system 110 may include a large burner to deliver a large amount of heating power to the reactor 112 during the reheat process, a porous medium burner embedded in the body 412, such as a sparger, to circulate the hot gas into the body 412 during the reheat process, a system for inducing an exothermic reaction within the reactor 112, and / or various other suitable features for accelerating the reheat process. In embodiments with a large burner, such a large burner may use a typical fuel gas (e.g., natural gas), hydrogen gas from a hydrogen storage component 30 (Figure 1), and / or a mixture of these two types of gases. In embodiments equipped with a porous medium burner, such a porous medium burner can burn a fuel gas (e.g., natural gas, hydrogen, and / or a mixture of these two gases) during the reheat process, and then deliver the reactants to the main body 412 after the reactor 112 has reached its operating temperature.

[0056] In some embodiments, the reactor 112 may optionally utilize a cascade configuration to adapt the reheating process to enable rapid partial start-up. For example, the reactor 112 may have a number of reaction chambers arranged in series or parallel. Each chamber may be sized to reheat rapidly and have a net positive output after taking parasitic effects into account during operation. It may also be possible to adjust the burner output considerably, and the burner may use a mixture of CH4 and H2 flow. Figure 13 is a schematic diagram of an example of a reactor 112 divided into a number of reaction chambers 1312a to 1312d according to some embodiments of the art.

[0057] In the illustrated embodiment, the reactor 112 has four reaction chambers (referred to as the first to fourth reaction chambers 1312a to 1312d, respectively) that are in fluid communication with the input path 302. A series of first valves 1322 control the flow of reactants to each of the reaction chambers 1312, and a series of second valves 1324 control the flow of reactants and / or output from the reactor 112 to a series of burners 116 (referred to as the first to fourth burners 116a to 116d, respectively). Each of the burners 116a to 116d corresponds to each of the reaction chambers 1312a to 1312d, respectively. When demand increases initially, it is preferable to reheat the first reaction chamber 1312a with the first burner 116a. During this initial period, it is preferable that the first burner 116a reheats the first reaction chamber 1312a by burning reactants (e.g., natural gas) and / or stored hydrogen from the earlier operation of reactor 112. Once the first reaction chamber 1312a reaches operating temperature, it is preferable to pass the reactants through the first reaction chamber 1312a to initiate the generation of hydrogen gas.

[0058] Next, it is preferable to direct a portion of the hydrogen gas along the second hydrogen pathway 314 to meet the increasing demand, while sending a portion of the hydrogen gas along the first hydrogen pathway 312 to initiate reheating of the second reaction chamber 1312b and / or maintain the temperature of the first reaction chamber 1312a. In some embodiments, the first burner 116b is preferable to reheat the second reaction chamber 1312b by burning the combination of hydrogen gas and reactants from the first reaction chamber 1312a. Once the second reaction chamber 1312b reaches operating temperature, it is preferable to pass the reactants through the second reaction chamber 1312b to increase the amount of hydrogen gas produced by reactor 112. Next, the reheating process is preferable to continue for the third and fourth reaction chambers 1312c, 1312d.

[0059] When many of the reaction chambers 1312 reach their operating temperature and reactor 112 generates more hydrogen gas, burners 116a-116d alter the composition of these gases that are burned. In some embodiments, burners 116a-116d stop burning the entire reaction together before or when the fourth reaction chamber 1312d reaches its operating temperature. Similarly, when many of the reaction chambers 1312 reach their operating temperature and reactor 112 generates more hydrogen gas, it is preferable to increase the amount of hydrogen gas diverted to the second hydrogen pathway 314 to be sent outside reactor 112.

[0060] In some embodiments, the reactor 112 may have one or more insulating materials (e.g., the chambers 1140 described above with reference to Figure 11) and / or a mechanical actuator (not shown). The mechanical actuator may move the insulating material from one reaction chamber 1312 to the next during the reheating process. Once applied to one reaction chamber 1312, the insulating material can accelerate the reheating process by reducing parasitic heat loss from the reaction chamber 1312. Once the individual reaction chambers 1312a to 1312d reach their operating temperature, the insulating material may be removed and the parasitic heat loss may be captured somewhere in the system 100 (Figure 1). In some embodiments, the insulating material may remain on the reaction chambers 1312 even after these reaction chambers 1312 have reached their operating temperature.

[0061] In some embodiments, reactor 112 turns off the operation of one or more of the reaction chambers 1312 when the demand for hydrogen gas and / or electricity decreases. For example, during periods of low demand, reactor 112 can operate the first and second reaction chambers 1312a,1312b and cool the third and fourth reaction chambers 1312c,1312d. In some embodiments, each of the reaction chambers 1312a-1312d is thermally coupled to one another to utilize parasitic heat loss from one reaction chamber 1312, thereby heating another reaction chamber 1312. For example, after the first reaction chamber 1312a reaches its operating temperature, it is preferable to redirect the parasitic heat loss from the first reaction chamber 1312a to the second-to-fourth reaction chambers 1312b-to-d to partially reheat the second-to-fourth reaction chambers 1312b-to-d.

[0062] In some embodiments, the reactor system 110 (Figure 1) can avoid the reheat process by maintaining the reactor 112 near its operating temperature, even during periods of low demand (or no demand). In various embodiments, the reactor 112 can operate continuously to generate hydrogen gas by maintaining the temperature of the reactor 112, while continuously adjusting the input flow of reactants according to demand. In continuous operation embodiments, the reactor 112 maintains heat according to normal operation using hydrogen gas. Excess hydrogen gas and / or electricity is better stored or distributed within local facilities when demand is low. For example, the controller 150 (Figure 1) may direct electricity to the energy grid to offset and / or address the cost of continuously operating the reactor 112. In another embodiment, excess energy may be stored in a secondary battery to supplement the output from the reactor 112 when demand exceeds the reactor's output capacity.

[0063] In embodiments that regulate the input flow of the reactants, a controller 150 (Figure 1) can be used to measure and respond to, and / or predict, the demand, and then control the input flow to meet the demand. For example, the controller 150 may determine that the demand increases around 5 p.m. each day, and then increase the input flow at or around 5 p.m. to meet the demand. During periods of low (or non)operation, the temperature of the reactor 112 may be maintained by the chamber 1140 described above with reference to Figure 11, the reheat system 1240 described above with reference to Figure 12, and / or any other suitable components. For example, the reactor 112 may have a pilot light or another electric heater running at all times to compensate for the heat loss from the reactor 112. In some embodiments that regulate the input flow of the reactants, the heat loss from the reactor 112 may be at least partially recovered using a heat storage tank that is in thermal contact with the reactor 112.

[0064] As described above with reference to Figure 1, another potential challenge for reactor 112 is, given size constraints, modifying the reactor to meet the size constraints imposed on certain residential and commercial building applications, and efficiently integrating reactor 112 with other components of system 100. Thus, in some embodiments, reactor 112 can be integrated with one or more other components of system 100 to achieve improved operational efficiency of system 100. That is, the efficiency and / or operating costs of system 100 can be improved by locating the components of system 100 within a shared space.

[0065] For example, the reactor 112 is preferably integrated with the generator 124 and / or the circulation system 130. The integrated component can share one or more heat inputs (e.g., share a single burner system) and / or can directly use parasitic heat losses from one component to heat the other. Furthermore, the integrated component can easily fit into the aforementioned space constraints. For example, the integrated component can more easily fit into the space conventionally designated for other equipment, such as a traditional boiler or furnace.

[0066] The general uses of compact thermoelectric converters in residential heating equipment, such as furnaces, boilers, and hot water heaters, are already described in U.S. Patent Application No. 16 / 794,142, filed March 12, 2019, by Ashton et al., and are incorporated herein by reference. However, when reactor 112 is integrated in situ with other components of system 100, several unique thermodynamic synergies are possible within system 100. For example, to increase the overall exergy of system 100, it is desirable to add a high-temperature component, such as reactor 112, immediately upstream, immediately downstream, and / or in parallel with generator 124. Heat not utilized by generator 124 can be utilized by reactor 112, or vice versa, thereby capturing a large portion of the free energy content in the input reactant (e.g., methane input) before heat is lost (e.g., at the heat exchanger downstream of the equipment). As a result, the efficiency of the integrated system 100 can be said to be superior to the efficiency of a system in which the components operate separately.

[0067] In another embodiment, using hydrogen instead of natural gas in the equipment may help improve the efficiency of the heat transfer process from the flame to the generator 124. Furthermore, hydrogen has a higher flame temperature, and this higher flame temperature also helps increase the efficiency of the generator 124 under constant heating demand. In addition, the availability of on-demand electricity from other components in the system 100 and on-site electricity storage helps enable the various disclosed embodiments to solve the operational challenges of the reactor 112 at a residential scale. For example, the on-site generator 124 can provide an electrically heated action to the reactor 112 (for example, according to the embodiments described above with reference to Figures 11 and 12) and / or actuate electrically driven valves or actuators in the reactor 112.

[0068] Figure 14 is a schematic diagram of a reactor system 110 coupled to a power generation system 120 according to several embodiments of the present technology. In the illustrated embodiment, the system includes two reactors 112 and two generators 124 arranged in parallel. In the illustrated embodiment, each reactor 112 is positioned adjacent to a burner 116, next to the hot end 1426 of the generator 124. In the parallel configuration, heat from the burner 116 is directly transferred into each of the reactors 112 and also directly to the hot end 1426 of each of the generators 124. The heat transferred to the reactors 112 maintains the operating temperature of the reactors 112, causing a thermal decomposition reaction to occur, thereby generating hydrogen gas. In some embodiments, at least a portion of the hydrogen gas is separated from carbon particles in a carbon separator and then sent to the burner 116 along a first hydrogen pathway 312. In the illustrated embodiment, the supply hydrogen fuel for burner 116 comes as a whole from the first hydrogen path 312, where it is mixed with air to regulate the combustion temperature of the hydrogen flame. In various other embodiments, the supply hydrogen fuel can be replenished with hydrogen from a storage tank and / or other fuels (e.g., natural gas).

[0069] On the other hand, the heat transferred to the generator 124 creates a temperature difference between the high-temperature end 1426 and the low-temperature end 1426 of the generator 124. In the illustrated embodiment, the low-temperature end of the generator 124 is positioned within the chamber 1440, separated from the high-temperature end 1426 by a space 1427. The chamber 1440 insulates the low-temperature end 1428 of the generator 124 from the reactor 112, while the space 1427 helps maintain the temperature difference between the high-temperature end 1426 and the low-temperature end 1428 of the generator 124. The generator 124 then uses this temperature difference to generate electricity according to an arbitrary appropriate mechanism. For example, in some embodiments, the generator 124 is a thermionic transducer with the high-temperature end 1426 separated from the low-temperature end 1428 by a vacuum (or partial vacuum) or a suitable material within the space 1428. In such embodiments, the high-temperature and low-temperature ends 1426 and 1428 are preferably metal plates separated by the space 1427. When the high-temperature end 1426 is heated to a high temperature, the heated metal surface releases electrons through space 1427 to the low-temperature end 1428, resulting in usable electrical energy. The thermoelectron converter can generate electricity from the heat of the burner without any moving parts in the generator 124, thereby easing the maintenance and / or space requirements of the system 100. Heat not used by either the reactor 112 or the generator 124 flows outward along path 1434, and such heat is preferably directed to a sink and / or heat exchanger in the circulation system 130 (Figure 1).

[0070] Figure 15 is a schematic diagram of a reactor system 110 coupled to a circulation system 130 according to several embodiments of the present technology. In the reactor system 110, the reactor 112 receives heat from one or more burners 116 located on each side of the reactor 112. One or more insulated walls 1540 are positioned around the burners 116. The insulated walls 1540 restrict or prevent heat from flowing in any direction other than the direction toward the reactor 112 in order to maintain the operating temperature of the reactor 112. The circulation system 130 is positioned around the insulated walls 1540 to capture heat not absorbed by the reactor 112 and / or parasitic heat loss from the reactor 112. Thus, the heat not absorbed by the reactor 112 flows directly into the circulation system 130. In the illustrated forms of the reactor system 110 and the circulation system 130, system 100 (Figure 1) can utilize all or almost all of the heat generated by the burners 116.

[0071] In various other embodiments, the system 100 in Figure 1 may include various other series configurations between the components of the system 100. For example, in some embodiments, the reactor 112 and the generator 124 are arranged in series, with the generator 124 positioned close to the burner 116 so that it directly receives heat. In some such embodiments, the reactor system 110 is positioned between the generator 124 and the heat dissipation loop for the generator 124. This series configuration is suitable for embodiments where the operating temperature of the generator 124 is higher than the operating temperature of the reactor 112, so that the generator 124 can meet the high demand for heat from the burner 116, while still having enough excess heat to maintain the operating temperature of the reactor 112. As just one example, several thermoelectron energy converters, thermophotovoltaic converters, and other high-temperature heat engines are suitable for this configuration. To give another example, in some embodiments, the reactor 112 and the generator 124 are arranged in series, and the reactor system 110 is positioned close to the burner 116 so that it directly receives heat. In some such embodiments, the generator 124 is positioned immediately downstream to directly utilize the heat released from the reactor system 110. This series configuration is suitable for embodiments in which a cryogenic generator 124 is utilized. As an example, several alkali metal thermoelectric converters or Stirling engines in which the heat engine is a bottoming cycle on the reactor 112 are suitable for this configuration.

[0072] In other embodiments where the thermodynamic synergies described above are not required, each component of system 100 may be isolated from the other components. Positioning the components separately can help address the spatial requirements described above, so that the components of system 100 can fit within the available space. That is, rather than requiring a large enough space for all the components of system 100, system 100 can fit into corresponding individual spaces, which can then be interconnected.

[0073] Figure 16 is a block diagram of the material flow through a regenerative pyrolysis reactor 112 according to another embodiment of the present technology. In the illustrated embodiment, the reactor 112 has an input valve 1602 operably coupled to a fuel source 10, two reaction chambers 1612 (referred to as the first reaction chamber 1612a and the second reaction chamber 1612b, respectively) operably coupled to the input valve 1602, and one or more output valves 1604 operably coupled to the reaction chambers 1612. Each of the reaction chambers 1612 may have a heat exchange material and one or more channels through which the heat exchange material flows. In various embodiments, the heat exchange material may be cordierite, mullite, alpha alumina, and / or combinations thereof. Furthermore, in some embodiments, each of the reaction chambers 1612 has a single and / or integrated structure composed of the heat exchange material. As the reactants flow through one of the reaction chambers 1612, the heat exchanger heats the reactants above the enthalpy point of the thermal decomposition reaction, thereby causing the hydrocarbons in the reactants to decompose into hydrogen gas and carbon particles. The hydrogen gas is then preferably used to generate heat and / or electricity. In some embodiments, for example, the hydrogen gas is burned to preheat and / or maintain the heat in the reaction chamber 1612. In some embodiments, the reactor 112 operates in a circulating manner, as will be described in detail below.

[0074] For example, during the first period, the input valve 1602 may direct the reactants into the first reaction chamber 1612a. The first reaction chamber 1612a can undergo a thermal decomposition reaction, thereby breaking down the reactants into carbon particles and hydrogen gas. Next, the output valve 1604 may direct at least a portion of the output from the first reaction chamber 1612a towards the carbon separator 114, the blower 118, and the burner 116. As described above, the carbon separator 114 can remove the carbon particles from the hydrogen gas flow, the blower 118 can mix the hydrogen gas with oxygen, and the burner 116 can burn the hydrogen with oxygen. Next, the flue valve 1606 may direct the resulting high-temperature flue gas into and / or around the second reaction chamber 1612b to heat the second reaction chamber 1612b. In some embodiments, the high-temperature flue gas burns carbon in the second reaction chamber 1612b, sending heat further to the second reaction chamber 1612b. The output valve 1604 can direct the high-temperature flue gas flowing out of the second reaction chamber 1612b toward the generator 124 and / or the circulation system 130. The generator 124 uses the high-temperature flue gas to generate electricity, which is output to the electrical equipment network 40, while the circulation system 130 uses the high-temperature flue gas to output heat into the heating equipment network 50. Any remaining flue gas is then released through the exhaust system 60.

[0075] During the second period, it is preferable to reverse the flow through valves 1602, 1604, and 1606, thereby utilizing the heat transferred into the second reaction chamber 1612b to cause a pyrolysis reaction and to reheat the reaction chamber 1612a. Specifically, the input valve 1602 directs the reactants into the second reaction chamber 1612b, the output valve 1604 directs at least a portion of the hydrogen gas from the second reaction chamber 1612b toward the burner 116, the flue valve 1606 directs the hot flue gas into and / or around the first reaction chamber 1612a, and the output valve 1604 directs the hot flue gas from the first reaction chamber 1612a toward the generator 124 and / or the circulation system 130.

[0076] In some embodiments, reactor 112 cycles reaction chambers 1612 between an operating phase and a preheating phase after a suitable length of time (for example, by switching the direction of the reactants between the first reaction chamber 1612a and the second reaction chamber 1612b). For example, in various embodiments, reactor 112 may cycle reaction chambers 1612 around each other every minute, every two minutes, every ten minutes, every thirty minutes, or after any other suitable period. In some embodiments, reactor 112 cycles reaction chambers 1612 around each other when the temperature in the operating reaction chamber (e.g., the reaction chamber producing the pyrolysis reaction) falls below a predetermined temperature. The predetermined temperature may be selected to help ensure that the reactants react sufficiently while in the operating reaction chamber. Below the predetermined temperature, the reactants may not react sufficiently rapidly and / or may not react at all in the operating reaction chamber. In various embodiments, reactor 112 is preferably configured to cycle reaction chambers 1612 together when the temperature inside the operating reaction chamber falls below approximately 1200°C.

[0077] In some embodiments, the inputs and outputs of the reaction chamber 1612 are preferably connected by a piping system to valves 1602, 1604, and 1606, which are preferably coupled to actuators to switch the valves 1602, 1604, and 1606 to direct the fluid flow into the pipes. Thus, the reactor 112 can cycle the reaction chambers 1612 with each other by issuing commands to switches 1602, 1604, and 1606 to switch the valves. As a result, the reactor 112 can cycle the reaction chambers 1612 with each other in a rapid and efficient manner, depending on the time the reactor operates the valves. In various embodiments, the reactor 112 can cycle the reaction chambers 1612 with each other in less than 1 minute, less than 30 seconds, less than 10 seconds, or almost instantaneously. In some embodiments, each of the valves 1602, 1604, and 1606 can switch the corresponding valve simultaneously. In some embodiments, one or more of the valves 1602, 1604, and 1606 can sequentially switch the corresponding valves. For example, output valve 1604 can switch the corresponding valve after all of the hydrogen gas from the operating reaction chamber has been directed to the appropriate destination.

[0078] In some embodiments, the output valve 1604 directs a portion of the hydrogen gas from the operating reaction chamber away from the reactor 112. For example, the hydrogen gas can be directed to a generator 124 to generate electricity and / or to a hydrogen storage. In some embodiments, the stored hydrogen gas can later be used to heat one or more of the reaction chambers 1612. In some such embodiments, the use of stored hydrogen allows the reactor 112 to cool between its most frequent use periods without requiring another energy source (e.g., heat and / or electricity) to restart the reactor 112.

[0079] In some embodiments, the reactor 112 may include one or more additional components and / or alternative arrangements of one or more of the components described above. In some embodiments, for example, the carbon separator 114 is preferably positioned between the reaction chamber and the output valve 1604. In some embodiments, the reactor 112 may have a number of output valves 1604, a number of carbon separators 114, and / or a number of burners 116. Furthermore, in some embodiments, one or more of the components of the reactor 112 are combined. For example, the burner 116 can be integrated with the blower 118 in a single component state. In another embodiment, one or more of the valves 1602, 1604, and 1606 can be combined in a single component state. In some embodiments, the reactor 112 may have three or more reaction chambers 1612, for example, three, four, five, ten, and / or any other appropriate number of reaction chambers 1612. In some such embodiments, two or more reaction chambers 1612 are operational during the operation of the reactor 112 (for example, used to heat the reactants). In some such embodiments, two or more reaction chambers 1612 are preheated during the operation of the reactor 112.

[0080] Figure 17A is a schematic partial view of a reaction chamber 1712 used in reactor 112 of Figure 16 according to several embodiments of the present technology. In the illustrated embodiments, the reaction chamber 1712 has a number of flow channels 1780 extending from a first end 1714 of the reaction chamber 1712 to a second end 1716 of the reaction chamber 1712 located opposite the first end 1714. Together, the flow channels 1780 form a passage 1772 through which the heat exchange material of the reaction chamber 1712 passes. Thus, during operation, the reactants can flow into the flow channels 1780 at the first end 1714, travel down along the passage 1772, and exit from the flow channels 1780 at the second end 1716. The reaction chamber 1712 can transfer heat to the reactants moving along the passage 1772, thereby causing a thermal decomposition reaction.

[0081] In the illustrated embodiment, the reaction chamber 1712 has a circular tubular shape. In various other embodiments, the reaction chamber 1712 can take other shapes, e.g., square, rectangular, hexagonal, and / or other tubular shapes, coils, or other non-axial shapes, and / or any other suitable shapes. Similarly, in the illustrated embodiment, each of the flow channels 1780 has a circular tubular shape. In various other embodiments, the flow channels 1780 of the reaction chamber 1712 can take other shapes, e.g., square, rectangular, hexagonal, and / or other tubular shapes, coils, and / or any other suitable shapes. The reaction chamber 1712 can be manufactured by various known manufacturing techniques applicable to the desired structure. For example, the reaction chamber 1712 can be manufactured by additive manufacturing processes (e.g., 3D printing), die processes, molding processes, extrusion processes, and / or any combination of manufacturing techniques.

[0082] As shown in Figure 17A, the reaction chamber 1712 has a length L and diameter D1 that match the length of the passage 1772. As further shown, each of the flow channels 1780 has a diameter D2. The length L, diameter D1, and diameter D2 may vary depending on the desired power capacity of the reaction chamber 1712, the size requirements regarding the space in which the reactor 112 (Figure 16) is incorporated, and / or the preferred operating conditions for the reaction chamber 1712. Furthermore, the dimensions may be interdependent. For example, the diameter D1 may be set according to the diameter D2 and the desired channel density. In another embodiment, the length L may depend in part on the diameter D2 to help the reactants flowing through the flow channels 1780 reach the enthalpy point in the reaction chamber 1712. In various exemplary embodiments, the length L of the reaction chamber 1712 is preferably in the range of about 0.5 meters (m) to about 10 meters, the diameter D1 of the reaction chamber 1712 is preferably in the range of about 0.1 meters to about 1 meter, the diameter D2 of the flow channel is preferably in the range of about 0.01 centimeters (cm) to about 1 meter, and / or the channel density is preferably in the range of about 1 channel per square inch (CPI) to about 500 CPI. In one embodiment, for example, the length L of the reaction chamber 1712 is approximately 1 m, the diameter D1 of the reaction chamber 1712 is approximately 1.3 cm, the diameter D2 of the flow channel is approximately 0.635 cm, and the channel density is approximately 4 CPI.

[0083] Further details on how operational considerations may affect each dimension are provided below. As those skilled in the art will understand, the exemplary operating conditions described below are illustrative only, and various other appropriate operational considerations may be added to the reactor to meet the output requirements described above. For example, although reaction chamber 1712 is described below with reactant input flow rates of 1 standard liter per minute (SLPM) and 5 SLPM, reaction chamber 1712 may have any other appropriate reactant input flow rates.

[0084] One consideration regarding the dimensions of the reaction chamber is whether the reaction chamber 1712 can heat the incoming reactants to a temperature higher than the desired reaction temperature (e.g., a temperature higher than or well above the enthalpy point). For example, given a heat transfer material, a temperature of the reaction chamber, and a ratio of the surface area to volume (S / V) of the flow channel 1780 (determined by the diameter D2 of the flow channel 1780), the reaction chamber 1712 transfers heat to the incoming reactants at a rate R1. At a heat transfer rate R1, a specific induction time (e.g., the time to heat the reactants to a temperature higher than the desired temperature) and residence time (e.g., the reaction time) are required to convert the hydrocarbons in the incoming reactants to hydrogen and carbon by thermal decomposition. Therefore, at a heat transfer rate R1, it is desirable that the reactants have a total time requirement to reach the desired degree of conversion in the thermal decomposition reaction (e.g., a desired percentage of decomposed hydrocarbons). The overall time requirement can be met by varying the length L of the reaction chamber 1712 and / or the input flow rate of the reactants. Additionally or alternatively, the S / V ratio is preferably selected for the length L set to meet the overall time requirement. In some embodiments, the desired operating temperature is preferably about 1200°C to about 1600°C. In some such embodiments, the residence time required to convert all or almost all of the hydrocarbons to hydrogen gas and carbon is in seconds, but includes less than 1 second. In one embodiment, the operating temperature may vary from about 1200°C to about 1400°C in a reactor having an inlet flow rate of about 5 SLPM and a flow channel diameter D2 of about 1.3 cm, resulting in an induction time of about 0.27 seconds and a residence time of about 0.38 seconds. With respect to a reaction chamber with a length L of about 1 m, about 90% of the reactants are converted within the reaction chamber.

[0085] Figure 18 shows an example of the relationship between the length of the reaction chamber 1712 and the temperature of the reactants flowing through the reaction chamber 1712 for various input flow rates and various heat transfer rates. As shown in the figure, 20 watts (W / m²) per square meter-Kelvin. 2At the first heat transfer rate of K) and an input flow rate of 1 SLPM for the reactant, the reactant's temperature rises by 1200°C over a length L of approximately 40 cm. In contrast, at this first heat transfer rate and an input flow rate of 5 SLPM for the reactant, the reactant's temperature rises by 1200°C over a length L of approximately 100 cm. Further in contrast, at an input flow rate of 5 SLPM for the reactant and 100 W / m 2 At the second heat transfer rate K, the reactant's temperature increases by 1200°C over a length L of approximately 40 cm. With respect to various embodiments, the inventors have confirmed that, with respect to an input flow rate varying from approximately 1 SLPM to approximately 5 SLPM, a diameter D2 of the flow channel 1780 ranging from approximately 0.5 cm to approximately 5 cm, and a desired operating temperature increase of approximately 1000°C, the required length L may vary from approximately 0.05 m to approximately 1.3 m.

[0086] In some embodiments, to further reduce the size of the reaction chamber 1712, the reactants may be preheated before entering the reaction chamber 1712. For example, in some embodiments, the reactants are preheated to a temperature of about 500°C before entering the reaction chamber 1712. In some embodiments, the reactants are preheated using a high-temperature output flowing out of the operating reaction chamber and / or by preheating the reaction chamber. For example, the reactant input line may include a coil that wraps around the output section from the operating reaction chamber to cool the output section and preheat the reactants at the same time. In another example, as described above with reference to Figure 16B, the reactant input line may include a coil that wraps around the output section from the preheated reaction chamber to cool the flue gas and preheat the reactants at the same time.

[0087] Another consideration regarding the dimensions of the reaction chamber is whether the reaction chamber 1712 can withstand continuous and / or extended operation. One constraint on such operation is that the heat exchange material in the reaction chamber 1712 cannot withstand the relatively high pressure drop between the flow channels 1780 when they are at high temperatures (e.g., above 1000°C). Therefore, the dimensions of the reaction chamber 1712 and the given operating conditions should be selected, at least in part, based on the expected pressure drop across the flow channels 1780 during operation.

[0088] For example, the pressure drop around the flow channel 1780 is determined by the gas or fluid flow rate of the reactants, the channel diameter D2, and the channel length (e.g., the length L of the reaction chamber 1712). Therefore, in some embodiments, the diameter D2 of the flow channel 1780 and / or the length L of the reaction chamber 1712 are preferably selected to take into account the pressure drop around the flow channel 1780. For example, as confirmed by the inventors, for a reaction chamber 1712 having a length L of about 5 m, a flow channel diameter D2 of about 0.5 cm to about 1.5 cm, a reactant input flow rate of about 1 SLPM to about 5 SLPM, and an operating temperature of about 1500°C, the pressure drop is less than about 1 pound (psi) per square inch, which is within acceptable limits.

[0089] Furthermore, in some embodiments, carbon material adhering to the surface walls of the flow channel 1780 (also known as “fouling”) may partially (or completely) block the flow channel 1780 during operation. A reduction in the flow channel diameter D2 due to fouling may adversely affect the dimensions of the reaction chamber 1712 selected to meet pressure drop requirements. For example, carbon particles may be generated in the reaction chamber 1712 as a result of heterogeneous and / or homogeneous pyrolysis reactions. Heterogeneous reactions occur based on the interaction between the reactants and the high-temperature surface or walls of the reaction chamber 1712. In contrast, homogeneous reactions occur in the gas phase of the reactants, resulting in the nucleation and growth of carbon particles in the gaseous reactants. Carbon particles generated by homogeneous reactions are carried by the gas flow to the second end 1716 of the reaction chamber 1712. Once the carbon particles have left the reaction chamber 1712, it is preferable that they be collected by a carbon separator, such as a series of cyclones and / or carbon filters. Carbon particles generated by heterogeneous reactions often remain in the flow chamber of reaction chamber 1712, causing fouling of the flow channel 1780 over time. The ratio of heterogeneous to homogeneous reactions is influenced by the S / V ratio in the flow channel 1780 (determined by the diameter D2 of the flow channel 1780) and the contact time between the walls of reaction chamber 1712 and the reactants. Therefore, in some embodiments, the diameter D2 of the flow channel 1780 is selected to maximize the amount of thermal decomposition reaction that occurs as a homogeneous reaction.

[0090] Figure 19 shows the effect of the relationship between the S / V ratio and the diameter D2 of the flow channel 1780 on the type of reaction in the reaction chamber 1712 in Figure 17, given a given input flow rate. In the illustrated relationship, the first region 1902 corresponds to an S / V ratio of approximately 10,000 / cm to approximately 1,000 / cm. In the first region 1902, the pyrolysis reaction is entirely (or almost entirely) heterogeneous. The second region 1904 corresponds to an S / V ratio between approximately 1,000 / cm and approximately 100 / cm. In the second region 1904, the pyrolysis reaction is mainly heterogeneous, with some homogeneity beginning to occur. The third region 1906 corresponds to an S / V ratio of approximately 100 / cm to approximately 20 / cm. In the third region 1906, the pyrolysis reaction is mainly homogeneous, with some heterogeneity remaining. The fourth region 1908 corresponds to an S / V ratio of less than approximately 20 / cm. In the fourth region 1908, the pyrolysis reaction is entirely (or nearly entirely) homogeneous. Therefore, in some embodiments, the flow channel diameter D2 is preferably selected within the fourth region 1908 and thus preferably has a diameter D2 of approximately 0.2 cm or more. In such embodiments, fouling can play only a minimal role in the pressure drop between flow channels.

[0091] Furthermore, as confirmed by the inventors, the pressure drop across the flow channel within region 1908 satisfies all the above-mentioned requirements regarding pressure drop (e.g., exhibiting a pressure drop of less than 1 psig / m). For example, Figure 20 shows the relationship between diameter D2 and pressure drop across the flow channel for various input flow rates. In Figure 20, the minimum diameter required to maintain a pressure drop of less than 1 psig / m is indicated by line 2002. For example, when the input flow rate is 1 SLPM, the minimum diameter indicated by line 2002 is approximately 0.3 cm. In another embodiment, when the input flow rate is 50 SLPM, the minimum diameter indicated by line 2002 is approximately 1.1 cm. As indicated by each of the lines 2002, the minimum diameter for each input flow rate is greater than 0.2 cm with respect to region 1908 as described above, with reference to Figure 19. Thus, the diameter that satisfies the requirement of a pressure drop of 1 psig / m also results in a nearly uniform response overall, thereby avoiding concerns regarding pressure drop due to fouling.

[0092] Figure 17B is a schematic partial view of a reactor 112 of the form shown in Figure 16A, according to some embodiments of the present technology. For example, in the illustrated embodiment, the reactor 112 has an input valve 1702, two reaction chambers 1712, two output valves 1704 (referred to as the first output valve 1704a and the second output valve 1704b, respectively), a carbon separator 114, and a burner 116. In Figure 17B, the flow of material through the reactor 112 is indicated by arrows over a first period in the same manner as described above with reference to Figure 16 as a whole. However, in the illustrated embodiment, the output valves 1704 are combined with flue valves 1606 (Figure 16) to operate in conjunction. For example, the first output valve 1704a directs the output from the first reaction chamber 1712a into the carbon separator 114 and burner 116, while the second output valve 1704b directs the flue gas from the burner 116 into the second reaction chamber 1712b. During the second period, the fluid flow through reactor 112 is reversed. During the second period, the second output valve 1704b directs the output from the second reaction chamber 1712b into the carbon separator 114 and burner 116, while the first output valve 1704a directs the flue gas from the burner 116 into the first reaction chamber 1612a.

[0093] Furthermore, as shown in Figure 17B, the reaction chamber 1712 of reactor 112 is preferably oriented vertically (for example, along the z-axis). Vertical orientation can help avoid effects caused by fouling by utilizing gravity to help carry carbon particles out of the reaction chamber 1712. Gravity-based assistance for removing carbon particles can be important because carbon particles can change the effective fluid density and / or velocity, and therefore can change the ability of the fluid to carry the carbon out of the reactor, even if the carbon as a whole is produced by a homogeneous reaction. The inventors have confirmed that, with respect to a reaction chamber 1712 having a gas emptying velocity of about 1 m / s to about 30 m / s, an operating temperature of about 1400°C, and nearly 100% thermal decomposition activity with respect to CH4 molecules, the reaction chamber 1712 has a capacity of about 268 grams per cubic meter (g / m³).3 It is necessary to remove the carbon particles and completely avoid the effects of fouling. Furthermore, the inventors have confirmed that, in the case of a reaction chamber 1712 having a vertical orientation and a flow channel 1708 (Figure 17A) with a diameter D2 of approximately 1 cm to approximately 5 cm, the carbon particles stabilize the gas flow through the reaction chamber 1712 and are removed from the reaction chamber 1712 by the flow of material through the reaction chamber 1712. Moreover, when the diameter D2 of the flow channel 1708 (Figure 17A) is approximately 1 cm to approximately 5 cm, the carbon is completely removed from the reaction chamber 1712, even in the case of horizontal reactant flow and / or vertical upward reactant flow. Furthermore, the inventors have confirmed that in the case of a flow channel 1708 with a larger diameter D2, the pressure drop is lower. Therefore, in the case of such a flow channel 1708, the inventors have confirmed that a larger flow rate is possible while avoiding concerns regarding pressure drop.

[0094] Furthermore, as shown in Figure 17B, the input valve 1702 can act as an output valve for a preheating reaction chamber (e.g., the second reaction chamber 1712b in the illustrated flow) to direct the hot flue gas out of the reactor 112. Thus, in some embodiments, the input valve 1702 may have an input coil wound around an output channel from the reaction chamber 1712 to preheat the reactants flowing into the reactor 112 using the heat from the hot flue gas. Furthermore, in some embodiments, the output line from the reactor may be positioned adjacent to the input line leading to the reactor, thereby also allowing the hot flue gas to preheat the reactants flowing into the reactor 112.

[0095] Figure 21 is a schematic diagram of a cyclone separator 2100 that can be used in a carbon separator 114 according to several embodiments of the present technology. As shown in Figure 21, the cyclone separator 2100 has a main barrel 2102 in fluid communication with an inlet pipe 2110 (referred to separately as a first inlet pipe 2110a and a second inlet pipe 2110b), a conical section 2104 in fluid communication with the main barrel 2102, a collection section 2106 in fluid communication with the conical section 2104, and a dipleg 2108 in fluid communication with the collection section 2106.

[0096] The first inlet pipe 2110a is preferably in fluid communication with the outlet of any of the reactors described above in order to receive the mixture containing carbon particles and hydrogen gas along the reactor output path 2112. The second inlet pipe 2110b is preferably connected to the catalyst vapor source in order to receive the catalyst vapor along the catalyst input path 2114. As shown in Figure 21, the catalyst input path 2114 collides with the reactor output path 2112 in the main barrel 2102, creating a cyclone that moves downward into the cyclone separator 2100. The cyclone then exerts a centrifugal force on the mixture of carbon particles and hydrogen gas flowing through it. Based on the impact caused by this force and the density difference between the hydrogen gas and the carbon particles, the mixture separates as it moves through the cyclone separator 2100. The tapered wall of the conical section 2104 maintains the cyclone velocity and collects and flows the mixture toward the collection section 2106 and the dip leg 2108. Some or all of the carbon particulate matter is captured in the collection section 2106 and sent to the carbon disposal component 20 (Figure 1), after which the dip leg 2108 sends the resulting hydrogen gas elsewhere. In some embodiments, the cyclone separator 2100 captures carbon particulate matter with a diameter of about 10 micrometers (μm) or larger. Carbon particulate matter with a diameter of less than about 10 μm may escape from the cyclone separator 2100 during output. Therefore, in various embodiments, the carbon separator 114 may have a series of cyclone separators and / or other particulate matter capture units, e.g., wet scrubbing components, baghouse filters, and / or electrostatic precipitators, and / or other suitable components.

[0097] For example, the carbon separator 114 may be a baghouse filter operably coupled to a cyclone separator 2100 to capture additional carbon particulate matter from the mixture. A baghouse filter is a type of fabric filter air-matter separator employed for particulate matter removal from manufacturing and other industrial operations to prevent dust and solid particulate matter from escaping into the open environment. The baghouse utilizes fabric filter bags and / or pleated filters arranged in rows and mounted vertically within a sheet metal housing. A gas flow containing dust is driven by a blower through a duct system into the baghouse. The gas in the flow then passes through the filter, while the particulate matter remains on the surface of the filter material, thus separating the particulate matter from the gas. Over time, dust accumulates on the filter surface and begins to form a filter cake. Therefore, it is good to remove the dust from the filter using various cleaning systems and / or to manually empty the filter periodically. When used in the carbon separator 114, the baghouse filter can accept a flow of hydrogen gas and carbon particulate matter. Hydrogen gas can pass through the fabric filter, but the filter can capture carbon particles.

[0098] Figures 22A to 22C are partial schematic isometric views of carbon collection systems 2220A to 2220C according to various embodiments of the present technology. As shown, each of the carbon collection systems 2220A to 2220C has an inlet and a large storage area for collecting carbon from system 100 (Figure 1). As shown in Figure 22A, carbon collection system 2220A preferably includes a removable storage bin which is preferably emptied and / or replaced periodically. As shown in Figure 22B, carbon collection system 2220B preferably has a funnel section leading to a lower opening through which carbon can be continuously and / or periodically removed from carbon collection system 2220B. For example, the user may empty carbon collection system 2220B through the opening once a week. As shown in Figure 22C, carbon collection system 2220C preferably includes a disposable storage tank. For example, it would be good for the user to periodically remove one (or both) of the storage tanks and replace them with empty storage tanks. Then, it would be good for the full storage tanks to be taken to another location and / or disposed of in exchange for empty storage tanks.

[0099] Embodiment For convenience, several embodiments of this technology are described below as numbered embodiments (1, 2, 3, etc.). These are provided as examples and do not limit the technology. It should be noted that any of the dependent embodiments can be combined in any appropriate manner, and each can be made into an independent embodiment. Other embodiments can be provided in a similar manner. [Embodiment 1] A system for producing hydrogen from natural gas, methane, or other available fuel gas on a scale consistent with the local distribution, consumption, or storage of hydrogen, the system comprising a compact reactor for the conversion of the gas to hydrogen and carbon, and a separation system for the recovery or disposal of the carbon or other solid matter from the reactor. [Embodiment Clause 2] The system according to Embodiment Clause 1, wherein the reactor has a columnar molten metal, and the metal comprises a single chemical element or a mixture of chemical elements. [Embodiment 3] The system according to Embodiment 1 or 2, characterized in that the conversion of the gas to hydrogen and carbon is carried out by passing the gas through a columnar molten salt, the columnar molten salt comprising a single salt or a mixture of different salts. [Embodiment Clause 4] The system according to any one of Embodiments 1 to 3, characterized in that the use or storage of hydrogen described above is incorporated into the system. [Embodiment Claim 5] The system according to any one of Embodiment Claims 1 to 4, characterized in that the hydrogen is transported to a location other than the place where the hydrogen is generated in a usable or storable manner. [Embodiment Claim 6] The system according to any one of Embodiment Claims 1 to 5, characterized in that the generated hydrogen is used to heat a reaction vessel that converts methane, natural gas, or other fuel gas into hydrogen and carbon. [Embodiment Claim 7] The system according to any one of Embodiment Claims 1 to 6, wherein the hydrogen and the solid substance in the production logistics are separated from each other using a cyclone-type separator. [Embodiment Clause 8] The system according to any one of Embodiment Clauses 1 to 7, characterized in that the hydrogen and solid material in the production logistics are separated using a number of cyclone-type separators, thereby dividing the solid material according to its particle size and / or density. [Embodiment Claim 9] The system according to any one of Embodiment Claims 1 to 8, characterized in that the solid substance in the production logistics is carried out from the reaction vessel by the flow of the gas product. [Embodiment Claim 10] The system according to any one of Embodiment Claims 1 to 9, characterized in that the flow velocity of the production logistics is increased by reducing the cross-sectional area of ​​the reaction vessel near the outlet, thereby enabling the solid material in the production logistics to be carried out by the gas product. [Embodiment Claim 11] The system according to any one of Embodiment Claims 1 to 10, characterized in that the hydrogen and solid matter in the production logistics are separated from each other using a combination of a cyclone-type separator and membrane separation. [Embodiment 12] The system according to any one of Embodiments 1 to 11, characterized in that the hydrogen and the solid substance are separated from each other by controlled precipitation of carbon in the reaction vessel. [Embodiment Claim 13] The system according to any one of Embodiment Claims 1 to 12, characterized in that the solid substance is separated from the reaction vessel using a mechanical skimming device. [Embodiment Claim 14] The system according to any one of Embodiment Claims 1 to 13, characterized in that the solid substance is separated from the reaction vessel using a lateral flow of gas. [Embodiment Claim 15] The system according to any one of Embodiment Claims 1 to 14, characterized in that the hydrogen and the solid substance in the production logistics are separated from each other using an electrostatic separator. [Embodiment Claim 16] The system according to any one of Embodiment Claims 1 to 15, characterized in that the hydrogen and the solid substance in the production logistics are separated from each other by filtration. [Embodiment Claim 17] The system according to any one of Embodiment Claims 1 to 16, characterized in that the reaction vessel is periodically replaced to remove solid matter. [Embodiment Claim 18] The system according to any one of Embodiment Claims 1 to 17, characterized in that only a small portion of the above gas is converted into hydrogen and carbon. [Embodiment Claim 19] The system according to any one of Embodiment Claims 1 to 18, characterized in that the carbon or other solid material is disposed of on-site. [Embodiment Claim 20] The system according to any one of Embodiment Claims 1 to 19, characterized in that the carbon or other solid material is removed from the system and transported away from the site. [Embodiment Clause 21] A system for producing hydrogen from natural gas, methane, or other available fuel gas on a scale consistent with residential use, the system including a compact reactor for the conversion of the gas to hydrogen and carbon, a separation system for the recovery or disposal of carbon or other solid matter from the reactor, and an electrical appliance for utilizing the produced hydrogen for water or space heating. [Embodiment Clause 22] The system according to Embodiment Clause 21, characterized in that the heating electrical appliance is selected from a furnace, a boiler, or a water heater. [Embodiment Clause 23] The system according to Embodiment Clause 22, characterized in that the combustion chamber of the heating electrical appliance is used to provide reaction heat for the reactor. [Embodiment Claim 24] The system according to any one of Embodiment Claims 21 to 23, wherein the reactor has a columnar molten metal, and the metal comprises a single chemical element or a mixture of chemical elements. [Embodiment Claim 25] The system according to any one of Embodiment Claims 21 to 24, characterized in that the conversion of the gas to hydrogen and carbon is carried out by passing the gas through a columnar molten salt, the columnar molten salt comprising a single salt or a mixture of different salts. [Embodiment Clause 26] The system according to any one of Embodiments 21 to 25, characterized in that the use or storage of hydrogen described above is incorporated into the system. [Embodiment Claim 27] ​​The system according to any one of Embodiment Claims 21 to 26, characterized in that the hydrogen is transported to a location other than the place where the hydrogen is generated in a usable or storable manner. [Embodiment Claim 28] The system according to any one of Embodiment Claims 21 to 27, characterized in that the generated hydrogen is used to heat a reaction vessel that converts methane, natural gas, or other fuel gas into hydrogen and carbon. [Embodiment Clause 29] The system according to any one of Embodiment Clauses 21 to 28, wherein the hydrogen and the solid substance in the production logistics are separated from each other using a cyclone-type separator. [Embodiment Claim 30] The system according to any one of Embodiment Claims 21 to 29, characterized in that the hydrogen and solid material in the production logistics are separated using a number of cyclone-type separators, thereby dividing the solid material according to its particle size and / or density. [Embodiment Claim 31] The system according to any one of Embodiment Claims 21 to 30, characterized in that the solid substance in the production logistics is carried out from the reaction vessel by the flow of the gas product. [Embodiment Claim 32] The system according to any one of Embodiment Claims 21 to 31, characterized in that the flow velocity of the production logistics is increased by reducing the cross-sectional area of ​​the reaction vessel near the outlet, thereby enabling the solid material in the production logistics to be carried out by the gas product. [Embodiment Claim 33] The system according to any one of Embodiment Claims 21 to 32, characterized in that the hydrogen and solid matter in the production logistics are separated from each other using a combination of a cyclone-type separator and membrane separation. [Embodiment Claim 34] The system according to any one of Embodiment Claims 21 to 33, characterized in that the hydrogen and the solid substance are separated from each other by controlled precipitation of carbon in the reaction vessel. [Embodiment Claim 35] The system according to any one of Embodiment Claims 21 to 34, characterized in that the solid substance is separated from the reaction vessel using a mechanical skimming device. [Embodiment Claim 36] The system according to any one of Embodiment Claims 21 to 35, characterized in that the solid substance is separated from the reaction vessel using a lateral flow of gas. [Embodiment Claim 37] The system according to any one of Embodiment Claims 21 to 36, characterized in that the hydrogen and the solid substance in the production logistics are separated from each other using an electrostatic separator. [Embodiment Claim 38] The system according to any one of Embodiment Claims 21 to 37, characterized in that the hydrogen and the solid substance in the production logistics are separated from each other by filtration. [Embodiment Claim 39] The system according to any one of Embodiment Claims 21 to 38, characterized in that the reaction vessel is periodically replaced to remove solid matter. [Embodiment Claim 40] The system according to any one of Embodiment Claims 21 to 39, characterized in that only a small portion of the above gas is converted into hydrogen and carbon. [Embodiment Claim 41] The system according to any one of Embodiment Claims 21 to 40, characterized in that the carbon or other solid material is disposed of on-site. [Embodiment Claim 42] The system according to any one of Embodiment Claims 21 to 41, characterized in that the carbon or other solid material is removed from the system and transported away from the site. [Embodiment 43] A system for producing hydrogen from natural gas, methane, or other available fuel gas on a scale consistent with residential use, the system comprising a compact reactor for the conversion of the gas to hydrogen and carbon, a separation system for the recovery or disposal of carbon or other solid matter from the reactor, and a device for generating electricity using the produced hydrogen. [Embodiment Clause 44] The system according to Embodiment Clause 43, characterized in that the hydrogen is converted into electricity using a thermoelectric converter, an alkali metal thermoelectric converter (AMTEC), a fuel cell, an internal combustion engine, a thermoelectric generator, or a Stirling engine. [Embodiment Clause 45] The system according to Embodiment Clause 43 or 44, wherein the reactor has a columnar molten metal, and the metal comprises a single chemical element or a mixture of chemical elements. [Embodiment Claim 46] The system according to any one of Embodiment Claims 43 to 45, characterized in that the conversion of the gas to hydrogen and carbon is carried out by passing the gas through a columnar molten salt, the columnar molten salt comprising a single salt or a mixture of different salts. [Embodiment Clause 47] The system according to any one of embodiments 43 to 46, characterized in that the use or storage of hydrogen described above is incorporated into the system. [Embodiment Claim 48] The system according to any one of Embodiment Claims 43 to 47, characterized in that the hydrogen is transported to a location other than the place where the hydrogen is generated in a usable or storable manner. [Embodiment Claim 49] The system according to any one of Embodiment Claims 43 to 48, characterized in that the generated hydrogen is used to heat a reaction vessel that converts methane, natural gas, or other fuel gas into hydrogen and carbon. [Embodiment Claim 50] The system according to any one of Embodiment Claims 43 to 49, wherein the hydrogen and the solid substance in the production logistics are separated from each other using a cyclone-type separator. [Embodiment Claim 51] The system according to any one of Embodiment Claims 43 to 50, characterized in that the hydrogen and solid material in the production logistics are separated using a number of cyclone-type separators, thereby dividing the solid material according to its particle size and / or density. [Embodiment Claim 52] The system according to any one of Embodiment Claims 43 to 51, characterized in that the solid substance in the production logistics is carried out from the reaction vessel by the flow of the gas product. [Embodiment Claim 53] The system according to any one of Embodiment Claims 43 to 52, characterized in that the flow velocity of the production logistics is increased by reducing the cross-sectional area of ​​the reaction vessel near the outlet, thereby enabling the solid material in the production logistics to be carried out by the gas product. [Embodiment Claim 54] The system according to any one of Embodiment Claims 43 to 53, characterized in that the hydrogen and solid matter in the production logistics are separated from each other using a combination of a cyclone-type separator and membrane separation. [Embodiment Claim 55] The system according to any one of Embodiment Claims 43 to 54, characterized in that the hydrogen and the solid substance are separated by controlled precipitation of carbon in the reaction vessel. [Embodiment Claim 56] The system according to any one of Embodiment Claims 43 to 55, characterized in that the solid substance is separated from the reaction vessel using a mechanical skimming device. [Embodiment Claim 57] The system according to any one of Embodiment Claims 43 to 56, characterized in that the solid substance is separated from the reaction vessel using a lateral flow of gas. [Embodiment Clause 58] The system according to any one of Embodiment Clauses 43 to 57, characterized in that the hydrogen and the solid substance in the production logistics are separated using an electrostatic separator. [Embodiment Clause 59] The system according to any one of Embodiment Clauses 43 to 58, characterized in that the hydrogen and solid matter in the production logistics are separated by filtration. [Embodiment Claim 60] The system according to any one of Embodiment Claims 43 to 59, characterized in that the reaction vessel is periodically replaced to remove solid matter. [Embodiment Claim 61] The system according to any one of Embodiment Claims 43 to 60, characterized in that only a small portion of the above gas is converted into hydrogen and carbon. [Embodiment Claim 62] The system according to any one of Embodiment Claims 43 to 61, characterized in that the carbon or other solid material is disposed of on-site. [Embodiment Claim 63] The system according to any one of Embodiment Claims 43 to 62, characterized in that the carbon or other solid material is removed from the system and transported away from the site. [Embodiment Clause 64] A system for producing hydrogen from natural gas, methane, or other available fuel gas on a scale consistent with residential use, the system comprising: a compact reactor for the conversion of the gas to hydrogen and carbon; a separation system for the recovery or disposal of carbon or other solid matter from the reactor; and an electrical appliance for using the produced hydrogen for heating water or space and generating electricity on-site. [Embodiment Claim 65] The system according to Embodiment Claim 64, characterized in that the hydrogen is converted into electricity using a thermoelectric converter, fuel cell, internal combustion engine, thermoelectric generator, or Stirling engine. [Embodiment Clause 66] The system according to Embodiment Clause 65, characterized in that the heating electrical appliance is selected from a furnace, a boiler, or a water heater. [Embodiment Claim 67] The system according to any one of Embodiment Claims 64 to 66, wherein the reactor has a columnar molten metal, and the metal comprises a single chemical element or a mixture of chemical elements. [Embodiment Claim 68] The system according to any one of Embodiment Claims 64 to 67, characterized in that the conversion of the gas to hydrogen and carbon is carried out by passing the gas through a columnar molten salt, the columnar molten salt comprising a single salt or a mixture of different salts. [Embodiment Clause 69] The system according to any one of embodiments 64 to 68, characterized in that the use or storage of hydrogen described above is incorporated into the system. [Embodiment Claim 70] The system according to any one of Embodiment Claims 64 to 69, characterized in that the hydrogen is transported to a location other than the place where the hydrogen is generated in a usable or storable manner. [Embodiment Claim 71] The system according to any one of Embodiment Claims 64 to 70, characterized in that the generated hydrogen is used to heat a reaction vessel that converts methane, natural gas, or other fuel gas into hydrogen and carbon. [Embodiment Claim 72] The system according to any one of Embodiment Claims 64 to 71, wherein the hydrogen and the solid substance in the production logistics are separated from each other using a cyclone-type separator. [Embodiment Claim 73] The system according to any one of Embodiment Claims 64 to 72, characterized in that the hydrogen and solid material in the production logistics are separated using a number of cyclone-type separators, thereby dividing the solid material according to its particle size and / or density. [Embodiment Claim 74] The system according to any one of Embodiment Claims 64 to 73, characterized in that the solid substance in the production logistics is carried out from the reaction vessel by the flow of the gas product. [Embodiment Claim 75] The system according to any one of Embodiment Claims 64 to 74, characterized in that the flow velocity of the production logistics is increased by reducing the cross-sectional area of ​​the reaction vessel near the outlet, thereby enabling the solid material in the production logistics to be carried out by the gas product. [Embodiment Claim 76] The system according to any one of Embodiment Claims 64 to 75, characterized in that the hydrogen and solid matter in the production logistics are separated from each other using a combination of a cyclone separator and membrane separation. [Embodiment Claim 77] The system according to any one of Embodiment Claims 64 to 76, characterized in that the hydrogen and the solid substance are separated by controlled precipitation of carbon in the reaction vessel. [Embodiment Claim 78] The system according to any one of Embodiment Claims 64 to 77, characterized in that the solid substance is separated from the reaction vessel using a mechanical skimming device. [Embodiment Claim 79] The system according to any one of Embodiment Claims 64 to 78, characterized in that the solid substance is separated from the reaction vessel using a lateral flow of gas. [Embodiment Claim 80] The system according to any one of Embodiment Claims 64 to 79, characterized in that the hydrogen and the solid substance in the production logistics are separated using an electrostatic separator. [Embodiment Claim 81] The system according to any one of Embodiment Claims 64 to 80, characterized in that the hydrogen and solid matter in the production logistics are separated by filtration. [Embodiment Claim 82] The system according to any one of Embodiment Claims 64 to 81, characterized in that the reaction vessel is periodically replaced to remove solid matter. [Embodiment Claim 83] The system according to any one of Embodiment Claims 64 to 82, characterized in that only a small portion of the above gas is converted into hydrogen and carbon. [Embodiment Claim 84] The system according to any one of Embodiment Claims 64 to 83, characterized in that the carbon or other solid material is disposed of on-site. [Embodiment Claim 85] The system according to any one of Embodiment Claims 64 to 84, characterized in that the carbon or other solid material is removed from the system and transported away from the site. [Embodiment 86] A system for producing hydrogen from natural gas, methane, or other available fuel gas on a scale consistent with residential use, the system comprising: a compact reactor for the conversion of the gas to hydrogen and carbon; a separation system for the recovery or disposal of solid carbon or other solid matter from the reactor; and a system for storing the produced hydrogen for later use. [Embodiment Claim 87] The system according to Embodiment Claim 86, wherein the reactor has a columnar molten metal, and the metal comprises a single chemical element or a mixture of chemical elements. [Embodiment Clause 88] The system according to Embodiment Clause 86 or 87, characterized in that the conversion of the gas to hydrogen and carbon is carried out by passing the gas through a columnar molten salt, the columnar molten salt comprising a single salt or a mixture of different salts. [Embodiment Clause 89] The system according to any one of embodiments 86 to 88, characterized in that the use or storage of hydrogen described above is incorporated into the system. [Embodiment Claim 90] The system according to any one of Embodiment Claims 86 to 89, characterized in that the hydrogen is transported to a location other than the place where the hydrogen is generated. [Embodiment Claim 91] The system according to any one of Embodiment Claims 86 to 90, characterized in that the generated hydrogen is used to heat a reaction vessel that converts methane, natural gas, or other fuel gas into hydrogen and carbon. [Embodiment Claim 92] The system according to any one of Embodiment Claims 86 to 91, wherein the hydrogen and the solid substance in the production logistics are separated from each other using a cyclone-type separator. [Embodiment Claim 93] The system according to any one of Embodiment Claims 86 to 92, characterized in that the hydrogen and solid material in the production logistics are separated using a number of cyclone-type separators, thereby dividing the solid material according to its particle size and / or density. [Embodiment Claim 94] The system according to any one of Embodiment Claims 86 to 93, characterized in that the solid substance in the production logistics is carried out from the reaction vessel by the flow of the gas product. [Embodiment Claim 95] The system according to any one of Embodiment Claims 86 to 94, characterized in that the flow velocity of the production logistics is increased by reducing the cross-sectional area of ​​the reaction vessel near the outlet, thereby enabling the solid material in the production logistics to be carried out by the gas product. [Embodiment Claim 96] The system according to any one of Embodiment Claims 86 to 95, characterized in that the hydrogen and solid matter in the production logistics are separated from each other using a combination of a cyclone separator and membrane separation. [Embodiment Claim 97] The system according to any one of Embodiment Claims 86 to 96, characterized in that the hydrogen and the solid substance are separated by controlled precipitation of carbon in the reaction vessel. [Embodiment Claim 98] The system according to any one of Embodiment Claims 86 to 97, characterized in that the solid substance is separated from the reaction vessel using a mechanical skimming device. [Embodiment Claim 99] The system according to any one of Embodiment Claims 86 to 98, characterized in that the solid substance is separated from the reaction vessel using a lateral flow of gas. [Embodiment Claim 100] The system according to any one of Embodiment Claims 86 to 99, characterized in that the hydrogen and the solid substance in the production logistics are separated using an electrostatic separator. [Embodiment Claim 101] The system according to any one of Embodiment Claims 86 to 100, characterized in that the hydrogen and solid matter in the production logistics are separated by filtration. [Embodiment Claim 102] The system according to any one of Embodiment Claims 86 to 101, characterized in that the reaction vessel is periodically replaced to remove solid matter. [Embodiment Claim 103] The system according to any one of Embodiment Claims 86 to 101, characterized in that only a small portion of the above gas is converted into hydrogen and carbon. [Embodiment Claim 104] The system according to any one of Embodiment Claims 86 to 103, characterized in that the carbon or other solid material is disposed of on-site. [Embodiment Claim 105] The system according to any one of Embodiment Claims 86 to 104, characterized in that the carbon or other solid material is removed from the system and transported away from the site. [Embodiment Item 106] A system for producing hydrogen gas that can be distributed locally, consumed locally, and / or stored locally, wherein the system is The invention includes a pyrolysis reactor that can be coupled to a source of reactants containing hydrocarbons, the pyrolysis reactor having one or more flow channels positioned to transfer heat to the reactants to convert the hydrocarbons into an output containing hydrogen gas, carbon particles, and heat, and the pyrolysis reactor being sized to receive the reactants at a flow rate of 1,000 to 40,000 standard cubic centimeters per minute. The output includes a carbon separation system operably coupled to the pyrolysis reactor to separate the hydrogen gas and carbon particles from each other. A system comprising a power generation component that can be coupled in-situ to the pyrolysis reactor to accept at least a portion of the above output and convert said output into electricity. [Embodiment Item 107] The system according to Embodiment 106, further comprising a heating component and / or a cooling component, wherein the heating component and / or the cooling component are operably coupled to the pyrolysis reactor and / or the power generation component to receive a portion of the heat and / or power. [Embodiment 108] The power generation component of the system according to embodiment 106 or 107 includes at least one of a thermoelectric converter, alkali metal thermoelectric converter, thermophotovoltaic converter, thermoelectric converter, gas turbine, fuel cell, microturbine, internal combustion engine, steam turbine, or Stirling engine. [Embodiment Item 109] A system according to any one of embodiments 106 to 108, further comprising a burner operably coupled to the pyrolysis reactor through one or more channels to receive and burn at least a portion of the above output, and a heat communication path coupled between the burner and the pyrolysis reactor and positioned to direct heat from the burner to the pyrolysis reactor. [Initiation clause 110] The system according to any one of embodiments 106 to 109, further comprising a heating component in thermal contact with the pyrolysis reactor, wherein the heating component includes at least one of a furnace, a forced air distribution system, a boiler, a radiator distribution system, a heat pump, a hybrid heating system, or a hot water heating system. [Mention Section 111] The system according to any one of embodiments 106 to 110, further comprising a cooling component operably coupled to the pyrolysis reactor and / or the power generation component, wherein the cooling component comprises at least one of an absorption chiller, a compression air conditioner, or a heat pump. [Initiation Clause 112] The above reactants include hydrocarbon gases, and the above pyrolysis reactor is At least one vertical column made of molten salt, having a lower end and an upper end, An input valve positioned toward the lower end and in fluid communication with the input supply source, The system according to any one of embodiments 106 to 111, having an output valve positioned toward the upper end. [Embodiment Item 113] The pyrolysis reactor further comprises an electric heating coil thermally coupled to at least one vertical column, according to embodiment 112. [Embodiment Clause 114] The system according to embodiment 112 or 113, wherein at least a portion of the carbon separation system is integrated with the at least one vertical column of the pyrolysis reactor. [Implementation clause 115] The system according to any one of embodiments 112 to 114, wherein at least one vertical column made of the molten salt comprises two or more vertical columns made of the molten salt, and the pyrolysis reactor has one or more valves positioned to separately and independently control the amount of the reactant supplied to each of the vertical columns according to a target output from the pyrolysis reactor. [Implementation clause 116] The above output is a first output, and the pyrolysis reactor has a first reaction chamber, a second reaction chamber, one or more burners, and one or more valves operably coupled to the above input supply source, the first reaction chamber, the second reaction chamber, and the one or more burners. In the first embodiment, the one or more valves described above are Fluid communication is established between the above input source and the above first reaction chamber, and the above first reaction chamber converts at least a first portion of the above hydrocarbon in the reactant into the above first output. Fluid communication is established between the first reaction chamber and the one or more burners, and the one or more burners burn at least a portion of the hydrogen gas in the first output to produce a second output containing high-temperature flue gas. Fluid communication is established between one or more of the above-mentioned burners and the second reaction chamber, and the second reaction chamber receives at least a portion of the second output to absorb heat from the high-temperature flue gas of the second output, and the absorbed heat is at least partially stored within the second reaction chamber. In the second embodiment, one or more of the above valves are Fluid communication is established between the above input source and the above second reaction chamber, and the above second reaction chamber converts at least a second portion of the hydrocarbon in the reactant into a third output including hydrogen gas, carbon particles, and heat. Fluid communication is established between the second reaction chamber and the one or more burners, and the one or more burners burn at least a portion of the hydrogen gas in the third output to produce a fourth output containing high-temperature flue gas. A system according to any one of embodiments 106 to 111, wherein fluid communication is established between one or more burners and the first reaction chamber, the first reaction chamber receives at least a portion of the fourth output and absorbs heat from the high-temperature flue gas of the fourth output, and the absorbed heat is at least partially stored in the first reaction chamber. [Embodiment Clause 117] The above valve is further connected to a controller that stores instructions, and in response to the above instructions, the controller, At the first point in time, position one or more of the valves in the first configuration. At the second point in time, position one or more of the valves in the second configuration. The system according to Embodiment 116, wherein at a third point in time, one or more valves are repositioned to the first embodiment. [Embodiment 118] The system according to Embodiment 117, further comprising one or more temperature sensors operably coupled to the controller and positioned to measure a first temperature of the first reaction chamber and a second temperature of the second reaction chamber, wherein, in response to the command, the controller further positions one or more valves to the second configuration when the first temperature of the first reaction chamber falls below a predetermined threshold. [Implementation clause 119] The system according to Embodiment 117, further comprising one or more pressure sensors operably coupled to the controller and positioned to measure a first pressure drop before and after the first reaction chamber and a first pressure drop before and after the second reaction chamber, wherein, in response to the command, the controller further positions one or more valves to the second configuration when the first pressure drop before and after the first reaction chamber reaches a predetermined threshold. [Embodiment Item 120] Each of the first and second reaction chambers has a plurality of flow channels extending along the corresponding longitudinal axis, and the cross-section of the first and second reaction chambers lateral to the corresponding axis is 1 square inch (6.45 cm). 2 The system according to any one of embodiments 116 to 119, having a channel density of 1 to 10 channels per unit. [Initiation Clause 121] The system according to any one of embodiments 116 to 120, wherein at least a portion of the carbon separation system is integrated with the pyrolysis reactor between the first reaction chamber and the second reaction chamber. [Embodiment Section 122] The system according to any one of embodiments 116 to 121, wherein one or more valves divert at least a portion of the hydrogen gas in the first output away from the pyrolysis reactor along the flow path before the first output is combusted. [Embodiment Item 123] The system according to any one of embodiments 116 to 122, further comprising at least a third reaction chamber operably coupled to one or more valves to receive at least one of the above-mentioned reactants and the second output. [Embodiment Clause 124] The system according to any one of embodiments 106 to 123, wherein the above-mentioned pyrolysis reactor is a first pyrolysis reactor, and the system further comprises a second pyrolysis reactor that can be coupled to a source of the reactants containing the hydrocarbons. [Embodiment Item 125] A method for producing hydrogen gas that can be distributed locally, consumed locally, and / or stored locally, wherein the method is The process includes a step in the pyrolysis reactor where a fuel gas containing hydrocarbons is received at a flow rate of 500 to 1,000,000 standard cubic centimeters per minute. The step includes heating the fuel gas in the pyrolysis reactor to the reaction temperature, wherein at the reaction temperature, at least a portion of the hydrocarbons in the fuel gas is converted into hydrogen gas and carbon particles. The step includes separating and capturing the above-mentioned hydrogen gas and the above-mentioned carbon particles, A method comprising the step of converting at least a portion of the captured hydrogen gas into electricity using a power generation component, wherein the power generation component is coupled in-situ to the pyrolysis reactor. [Embodiment Clause 126] The method according to embodiment 125, further comprising the step of burning at least a portion of the captured hydrogen gas to heat the pyrolysis reactor. [Embodiment Clause 127] The method according to embodiment 125 or 126, wherein the power generation component includes at least one of a thermoelectric converter, an alkali metal thermoelectric converter, a thermophotovoltaic converter, a thermoelectric converter, a turbine, a fuel cell, a microturbine, an internal combustion engine, a steam turbine, or a Stirling engine. [Embodiment 128] The method according to any one of embodiments 125 to 127, wherein the step of heating the fuel gas in the pyrolysis reactor includes passing the reactant through a chamber of molten fluid. [Embodiment Section 129] The method according to any one of embodiments 125 to 127, wherein the step of heating the fuel gas in the pyrolysis reactor includes passing the fuel gas through a preheated first reaction chamber, and the method further includes the step of burning at least a portion of the captured hydrogen gas to heat a second reaction chamber. [Embodiment Item 130] The method according to Embodiment 129, further comprising passing the fuel gas through the preheated first reaction chamber for a period of time, then passing the fuel gas through the second reaction chamber, and heating the first reaction chamber by burning the at least portion of the captured hydrogen gas. [Embodiment Item 131] The method according to any one of embodiments 125 to 130, further comprising the steps of (a) using at least a portion of the captured hydrogen gas and / or (b) using the generated electricity at (i) a heating component and / or (ii) a cooling component. [Embodiment Item 132] The method according to any one of embodiments 125 to 131, further comprising the step of burning at least a portion of the captured hydrogen gas at a heating component, wherein the heating component includes at least one of a furnace, a forced air distribution system, a boiler, a radiator distribution system, a heat pump, a hybrid heating system, or a hot water heating system. [Embodiment Item 133] The method according to any one of embodiments 125 to 132, further comprising the step of using at least a portion of the electricity generated above within a cooling component, wherein the cooling component includes at least one of an absorption chiller, a compression air conditioner, or a heat pump.

[0100] conclusion Embodiments of the present invention can be embodied as computer-executable instructions, for example, routines executed by a general-purpose computer, personal computer, server, or other computing system. The technology can also be embodied in a dedicated computer or data processor that is specifically programmed, configured, or set up to execute one or more of the computer-executable instructions described in detail herein. The terms “computer” and “computing device” as used herein generally mean a device having a processor and non-temporary memory, and a device that can communicate with any data processor or network. Examples of data processors include programmable general-purpose or dedicated microprocessors, programmable controllers, ASICs, programming logic devices (PLDs), etc., or combinations of such devices. Computer-executable instructions are preferably stored in memory, for example, RAM, ROM, flash memory, etc., or combinations of such components. Computer-executable instructions may also be stored in one or more storage devices, for example, magnetic or optical disks, flash memory devices, or any other form of non-volatile or non-temporary storage medium for data. A computer executable instruction preferably contains one or more program modules, which may include routines, programs, objects, components, data structures, etc., and may also perform a specific task or implement an abstract data type.

[0101] As stated above, while specific embodiments of the Art have been described herein for illustrative purposes, well-known structures and functions have not been shown or described in detail so as not to unnecessarily obscure the description of the embodiments of the Art. The contents of this disclosure are valid to the extent that any reference cited herein is inconsistent with the contents of this disclosure. Where the context permits, singular or plural terms may also include plural or singular terms, respectively. Furthermore, unless the term “or” is expressly limited to referring to a list of two or more items and meaning only a single item excluded from other items, the use of the term “or” in such a list should be understood to include (a) any single item in the list, (b) all items in the list, or (c) any combination of items in the list. Furthermore, as used herein, the phrases “and / or,” for example, “A and / or B,” mean A only, B only, and both A and B. Furthermore, the terms “comprising,” “including,” “having,” and “with” are used throughout the specification to mean that any many identical features and / or other features in additional forms are included, at least the listed features.

[0102] From the foregoing, it will be clear that various modifications can be carried out without departing from the disclosure of this technology. For example, as will be understood by those skilled in the art, various components of this technology can be further divided into subcomponents, or various components and functions of this technology can be combined and integrated. In addition, certain aspects of this technology described in relation to certain embodiments can also be combined with or omitted in other embodiments. Furthermore, while advantages associated with certain embodiments of this technology have been described in relation to those embodiments, other embodiments can also achieve such advantages, and it is not necessarily required that all embodiments demonstrate such advantages that are within the scope of this technology. Accordingly, this disclosure and related technologies may include other embodiments that are not expressly shown or described herein.

[0103] This disclosure remains valid to the extent that any reference cited by this disclosure contradicts the disclosure.

Claims

1. A system for producing hydrogen gas that can be locally distributed, locally consumed, and / or locally stored, the system comprising: a pyrolysis reactor coupled to a source of reactants containing hydrocarbons, the pyrolysis reactor having one or more flow channels positioned to transfer heat to the reactants to convert the hydrocarbons into an output containing hydrogen gas, carbon particles, and heat; a carbon separation system operably coupled to the pyrolysis reactor to separate the hydrogen gas and the carbon particles in the output from each other; a power generation component that can be coupled on-site to the pyrolysis reactor to receive at least a portion of the output and convert the output into electricity.

2. The system according to claim 1, further comprising a heating component and / or a cooling component, the heating component and / or the cooling component being operably coupled to the pyrolysis reactor and / or the power generation component to receive a portion of the heat and / or electricity.

3. The system according to claim 1, wherein the power generation component includes at least one of a thermionic converter, an alkali metal thermoelectric converter, a thermophotovoltaic converter, a thermoelectric converter, a turbine, a fuel cell, a microturbine, an internal combustion engine, a steam turbine, or a Stirling engine.

4. The system according to claim 1, further comprising a burner operably coupled to the pyrolysis reactor through one or more flow paths to receive at least a portion of the output and burn the at least a portion, and a heat transfer path coupled between the burner and the pyrolysis reactor and positioned to direct heat from the burner to the pyrolysis reactor.

5. The system according to claim 1, further comprising a heating component in thermal communication with the pyrolysis reactor, the heating component including at least one of a furnace, a forced air distribution system, a boiler, a radiator distribution system, a heat pump, a hybrid heating system, or a hot water heating system.

6. The system according to claim 1, further comprising a cooling component operably coupled to the pyrolysis reactor and / or the power generation component, the cooling component including at least one of an absorption chiller, a compression air conditioner, or a heat pump.

7. The reactant includes a hydrocarbon gas, and the pyrolysis reactor has at least one vertical column made of molten salt with a lower end and an upper end, an input valve positioned towards the lower end and in fluid communication with an input source, and an output valve positioned towards the upper end, the system according to claim 1.

8. The pyrolysis reactor further has an electric heating coil thermally coupled to the at least one vertical column, the system according to claim 7.

9. At least a part of the carbon separation system is integrated with the at least one vertical column of the pyrolysis reactor, the system according to claim 7.

10. The at least one vertical column made of molten salt includes two or more vertical columns made of molten salt, and the pyrolysis reactor has one or more valves positioned to independently control the supply amount of the reactant to each of the vertical columns according to a target output from the pyrolysis reactor, the system according to claim 7.

11. The output is a first output, and the pyrolysis reactor has a first reaction chamber, a second reaction chamber, one or more burners, and one or more valves operably coupled to the input source, the first reaction chamber, the second reaction chamber, and the one or more burners, In a first configuration, the one or more valves establish fluid communication between the input source and the first reaction chamber, and the first reaction chamber converts at least a first portion of the hydrocarbon in the reactant to the first output, establish fluid communication between the first reaction chamber and the one or more burners, and the one or more burners burn at least a portion of the hydrogen gas in the first output to produce a second output including high-temperature flue gas, establish fluid communication between the one or more burners and the second reaction chamber, and the second reaction chamber receives at least a portion of the second output to absorb heat from the high-temperature flue gas of the second output, and the absorbed heat is at least partially stored in the second reaction chamber, In a second configuration, the one or more valves establish fluid communication between the input source and the second reaction chamber, and the second reaction chamber converts at least a second portion of the hydrocarbon in the reactant to a third output including hydrogen gas, carbon fine particles, and heat, Establish fluid communication between the second reaction chamber and the one or more burners, wherein the one or more burners combust at least a portion of the hydrogen gas in the third output to produce a fourth output comprising hot flue gas. Establish fluid communication between the one or more burners and the first reaction chamber, wherein the first reaction chamber receives at least a portion of the fourth output, absorbs heat from the hot flue gas of the fourth output, and the absorbed heat is at least partially stored within the first reaction chamber. The system according to claim 1.

12. Further comprising a controller communicatively coupled to the valve and storing instructions, which, when executed, cause the controller to Position the one or more valves in the first configuration at a first time point. Position the one or more valves in the second configuration at a second time point. Reposition the one or more valves in the first configuration at a third time point. The system according to claim 11.

13. Further comprising one or more temperature sensors operably coupled to the controller and positioned to measure a first temperature of the first reaction chamber and a second temperature of the second reaction chamber, which, when executed, further cause the controller to position the one or more valves in the second configuration when the first temperature of the first reaction chamber falls below a predetermined threshold. The system according to claim 12.

14. Further comprising one or more pressure sensors operably coupled to the controller and positioned to measure a first pressure drop across the first reaction chamber and a first pressure drop across the second reaction chamber, which, when executed, further cause the controller to position the one or more valves in the second configuration when the first pressure drop across the first reaction chamber reaches a predetermined threshold. The system according to claim 12.

15. Each of the first and second reaction chambers has a plurality of flow channels extending along a corresponding longitudinal axis, and the cross-sections of the first and second reaction chambers transverse to the corresponding axis have a channel density of 1 to 10 channels per square inch (6.45 cm 2 )), the system according to claim 11.

16. At least a portion of the carbon separation system is integrated with the pyrolysis reactor between the first reaction chamber and the second reaction chamber. The system according to claim 11.

17. The system of claim 11, wherein the one or more valves divert at least a portion of the hydrogen gas in the first output away from the pyrolysis reactor along a flow path before burning the first output.

18. The system of claim 11, further comprising at least a third reaction chamber operably coupled to the one or more valves to receive at least one of the reactants and the second output.

19. The pyrolysis reactor is a first pyrolysis reactor, and the system of claim 1 further comprises a second pyrolysis reactor connectable to a source of the reactants containing hydrocarbons.

20. A method of producing hydrogen gas for local distribution, local consumption, and / or local storage, the method comprising: receiving a fuel gas containing hydrocarbons at a pyrolysis reactor; heating the fuel gas in the pyrolysis reactor to a reaction temperature at which at least a portion of the hydrocarbons in the fuel gas are converted to hydrogen gas and carbon particulate; separating and capturing the hydrogen gas and the carbon particulate; converting at least a portion of the captured hydrogen gas to electricity using a power generation component, the power generation component being locally coupled to the pyrolysis reactor.

21. The method of claim 20, further comprising burning at least a portion of the captured hydrogen gas to heat the pyrolysis reactor.

22. The power generation component of claim 20 includes at least one of a thermionic converter, an alkali metal thermoelectric converter, a thermophotovoltaic converter, a thermoelectric converter, a turbine, a fuel cell, a microturbine, an internal combustion engine, a steam turbine, or a Stirling engine.

23. The step of heating the fuel gas in the pyrolysis reactor of claim 20 includes passing the reactants through a molten fluid chamber.

24. The step of heating the fuel gas in the pyrolysis reactor of claim 20 includes passing the fuel gas through a preheated first reaction chamber, and the method further includes burning at least a portion of the captured hydrogen gas to heat a second reaction chamber.

25. After passing the fuel gas through the preheated first reaction chamber over a period of time, the method further includes passing the fuel gas through the second reaction chamber, and heating the first reaction chamber by combusting at least a portion of the captured hydrogen gas, according to the method of claim 23.

26. The method of claim 20 further comprising using at least a portion of the captured hydrogen gas and / or (b) the generated electricity at (i) a heating component and / or (ii) a cooling component.

27. The method of claim 20 further comprising combusting at least a portion of the captured hydrogen gas at a heating component, the heating component including at least one of a furnace, a forced air distribution system, a boiler, a radiator distribution system, a heat pump, a hybrid heating system, or a hot water heating system.

28. The method of claim 20 further comprising using at least a portion of the generated electricity within a cooling component, the cooling component including at least one of an absorption chiller, a compression air conditioner, or a heat pump.

29. The system of claim 1, wherein the pyrolysis reactor is sized to produce hydrogen for consumption in a residential building and / or a commercial building.

30. The flow channels of the reactor are positioned in a core region of the reactor, and the system further includes a burner positioned to direct flue gas through at least a portion of the core region, according to the system of claim 1.

31. The reactor is configured to be retrofitted to a heating unit and sized to fit within the footprint of the heating unit, according to the system of claim 1.

32. The reactor of claim 31, wherein the reactor is thermally coupled to the heating unit to capture parasitic heat loss from the reactor in the heating unit.

33. A system for producing hydrogen gas that can be locally distributed, locally consumed, and / or locally stored, the system comprising A pyrolysis reactor that can be coupled to a source of reactants containing hydrocarbons, the pyrolysis reactor having one or more flow channels positioned to transfer heat to the reactants to convert the hydrocarbons into an output containing hydrogen gas, carbon particles, and heat, including a carbon separation system operably coupled to the pyrolysis reactor to separate the hydrogen gas from the carbon particles in the output, A system including a burner that can be coupled in situ to the pyrolysis reactor to receive at least a portion of the output and burn the at least a portion.

34. The one or more flow channels are positioned in a body of the pyrolysis reactor, the pyrolysis reactor further including a chamber at least partially surrounding the body and one or more electrical heaters positioned in the chamber to send heat around the body, the chamber and the one or more electrical heaters being configured to reduce parasitic heat loss from the body, the system of claim 33.

35. The hydrocarbon is a gas, and the pyrolysis reactor is At least one vertical column consisting of molten salt with a lower end and an upper end, An input valve positioned towards the lower end and in fluid communication with an input source, and An output valve positioned towards the upper end, the system of claim 33.

36. The output is a first output, the pyrolysis reactor having a first reaction chamber, a second reaction chamber, one or more pyrolysis burners, and one or more valves operably coupled to (1) the source, (2) the first reaction chamber, (3) the second reaction chamber, and (4) the one or more pyrolysis burners, In a first configuration, the one or more valves Direct the reactants from the source to the first reaction chamber, the first reaction chamber converting at least a first portion of the hydrocarbons in the reactants to the first output, Direct at least a portion of the hydrogen gas in the first output towards the one or more burners, the one or more burners burning the hydrogen gas to produce a second output containing hot flue gas, Direct the second output towards the second reaction chamber, the second reaction chamber absorbing heat from the hot flue gas of the second output and storing at least a portion of the heat, In a second configuration, the one or more valves Direct the reactants from the source to the second reaction chamber, which converts at least a second portion of the hydrocarbons in the reactants to a third output comprising hydrogen gas. Direct at least a portion of the hydrogen gas in the third output to the one or more burners, which burn the hydrogen gas to produce a fourth output comprising hot flue gas. Direct the second output to the first reaction chamber, which receives and absorbs heat from the hot flue gas of the fourth output. The system according to claim 33.

37. A system for producing hydrogen gas that can be locally distributed, locally consumed, and / or locally stored, the system comprising: A pyrolysis reactor, the pyrolysis reactor comprising: An input connectable to a source of reactants comprising hydrocarbons. One or more reaction channels coupled to the input, the one or more reaction channels positioned to transfer heat to the reactants to convert the hydrocarbons to an output stream comprising hydrogen gas and carbon particulate matter. An output thermally coupled to the input, the output positioned to transfer heat from the output stream to the reactants in the input to preheat the reactants in the input during operation. The system further comprises: A carbon separation system operably coupled to the output of the pyrolysis reactor to separate the hydrogen gas from the carbon particulate matter in the output stream. A burner coupled to the output of the pyrolysis reactor, the burner positioned to receive and burn at least a portion of the output stream. A system.

38. The burner is thermally coupled to one or more reaction channels and is positioned to supply heat transferred to the reactants in the one or more reaction channels. The system according to claim 37.

39. The pyrolysis reactor is sized to consume the reactants at a rate of 18 to 135,000 British thermal units per minute. The system according to claim 37.

40. The pyrolysis reactor is sized to consume the reactants at a rate of 10 million to 335 billion British thermal units per year. The system according to claim 37.

41. Further comprising a heating component, wherein the output part is operably coupled to the heating component downstream of the carbon separation system, and the heating component comprises at least one of a furnace, a forced air distribution system, a boiler, a radiator distribution system, a heat pump, a hybrid heating system, or a hot water heating system. The system according to claim 37.

42. The burner is a first burner, the output part is operably coupled to a second burner downstream of the carbon separation system, and the second burner is part of a heating component comprising at least one of a furnace, a forced air distribution system, a boiler, a radiator distribution system, a heat pump, a hybrid heating system, or a hot water heating system. The system according to claim 37.

43. The input part comprises one or more coils around the output part. The system according to claim 37.

44. The pyrolysis reactor further comprises a carbon removal component positioned to remove carbon from the one or more reaction channels. The system according to claim 37.

45. The carbon removal component is a mechanical scrap component, a fluid scrap component the inclined surface of one or more reaction channels, or a precipitation component, The system according to claim 44, comprising one or more of the above.

46. The pyrolysis reactor further comprises a chamber at least partially surrounding the one or more reaction channels, and the chamber is configured to maintain a vacuum. The system according to claim 37.

47. A pyrolysis reactor for producing hydrogen gas that can be locally distributed, locally consumed, and / or locally stored, the pyrolysis reactor comprising an input part connectable to a source of reactants containing hydrocarbons, a reaction chamber coupled to the input part, the reaction chamber having one or more flow channels positioned to provide input heat to the reactants to convert the hydrocarbons into an output stream containing hydrogen gas and carbon particles, An output part thermally coupled to the input part for transferring at least a portion of the heat in the output stream to the reactants in the input part. A pyrolysis reactor.

48. The pyrolysis reactor according to claim 47, further comprising a burner positioned to direct hot flue gas through the one or more flow channels of the reaction chamber.

49. The pyrolysis reactor according to claim 47, wherein the burner is coupled to the output portion of the pyrolysis reactor to receive at least a portion of the output stream and combust the at least a portion to generate the hot flue gas.

50. The pyrolysis reactor according to claim 47, wherein the one or more flow channels are oriented vertically to reduce fouling of the one or more flow channels from the output portion.

51. A chamber at least partially surrounding the one or more flow channels, and one or more heating components positioned within the chamber, wherein in a first state, the chamber is configured to contain gas and conduct heat from the one or more heating components to the one or more flow channels, and in a second state, the chamber is configured to maintain a vacuum, the pyrolysis reactor according to claim 47.

52. The pyrolysis reactor according to claim 47, wherein the one or more flow channels are sized to consume the reactant at a rate of 10 million to 7080000 million British thermal units per year.

53. The pyrolysis reactor according to claim 47, wherein the one or more flow channels are sized to consume the reactant at a rate of 0.018 to 6105 standard legislative feet per minute.

54. The pyrolysis reactor according to claim 47, wherein the one or more flow channels are sized to consume the reactant at a rate of 10 million to 335000000 million British thermal units per year.

55. The pyrolysis reactor according to claim 47, further comprising a carbon separation system fluidly coupled to the output portion to separate the hydrogen gas from the carbon particles in the output stream.

56. further comprising a carbon removal component at least partially within the reaction chamber, wherein the carbon removal component is a mechanical scrap component, a fluid scrap component an inclined surface of the one or more flow channels, or a precipitation component, and includes one or more of the foregoing, the pyrolysis reactor according to claim 47.

57. A method for producing hydrogen gas that can be locally distributed, locally consumed, and / or locally stored, the method comprising: receiving a fuel gas containing hydrocarbons at an input section of a pyrolysis reactor; at the input section, using residual heat in an output stream from the pyrolysis reactor to preheat the fuel gas; heating the fuel gas to a reaction temperature within one or more flow channels of the pyrolysis reactor, at which reaction temperature at least a portion of the hydrocarbons in the fuel gas are converted to hydrogen gas and carbon particulate; separating the hydrogen gas from the carbon particulate. **Claim 58** The method according to claim 57, further comprising burning at least a portion of the hydrogen gas in a burner of the pyrolysis reactor to heat the one or more flow channels. **Claim 59** The method according to claim 57, wherein the step of preheating the fuel gas comprises preheating the fuel gas to a temperature of at least 500 °C. **Claim 60** The method according to claim 57, wherein the fuel gas is received in an amount of from 0.018 to 6,105 standard cubic feet per minute. **Claim 61** The method according to claim 57, wherein the fuel gas is received in an amount of from 10 million to 335,000,000 million British thermal units per year. **Claim 62** The system according to claim 1, wherein the pyrolysis reactor is sized to receive the reactants at a flow rate of from 500 to 1,000,000 standard cubic centimeters per minute. **Claim 63** The method according to claim 20, wherein the fuel gas is received at the pyrolysis reactor at a flow rate of from 500 to 1,000,000 standard cubic centimeters per minute.

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