Chemical Conversion Systems

Abstract

The device can include a plasma chamber fluidly connected to an auxiliary reaction chamber and an integrated reformer. The integrated reformer can be fluidly connected to the auxiliary reaction chamber. The auxiliary reaction chamber can be configured to utilize heat received from the plasma chamber from the heated first syngas stream to initiate an exothermic reaction with a second gas stream and output the heated second syngas stream to the integrated reformer.

Description

[Technical Field]

[0001] CROSS-REFERENCE TO RELATED APPLICATIONS This U.S. patent application claims priority to Provisional Patent Application No. 63 / 374,903, filed September 7, 2022. The disclosure of this prior application is considered part of the disclosure of the present application and is hereby incorporated by reference in its entirety.

[0002] The present disclosure generally relates to a plasma reaction system comprising a plasma chamber along with one or more additional chambers, including any combination of auxiliary reaction chambers and integrated reformers. [Background technology]

[0003] Unless otherwise noted herein, the materials described herein are not prior art to the claims of this application and are not admitted to be prior art by inclusion in this section.

[0004] Plasma-based dissociation reactions can be used to drive carbon-based chemical reactions, providing high temperatures and energy to drive the carbon-based chemical reactions to completion.

[0005] The subject matter claimed in this disclosure is not limited to implementations that solve any drawbacks or that operate only in environments such as those described above. Rather, this background is provided only to illustrate one example technology area in which some implementations described in this disclosure may be practiced. Summary of the Invention

[0006] The system may include a plasma chamber, an auxiliary reaction chamber, and an integrated reformer. The plasma chamber may be configured to receive a first gas stream from a plasma chamber inlet; add heat to the first gas stream to form a heated first syngas stream; and output the heated first syngas stream to the auxiliary reaction chamber. The auxiliary reaction chamber may be configured to receive the heated first syngas stream from the plasma chamber; receive a second gas stream from the auxiliary reaction chamber inlet; and output the heated second syngas stream to the integrated reformer. The heated second syngas stream may include a reaction product of the heated first syngas stream and the second gas stream. The integrated reformer may be configured to receive the heated second syngas stream from a first integrated reformer inlet; receive a third gas stream from a second integrated reformer inlet; and output syngas from the integrated reformer.

[0007] The device can include a plasma chamber in fluid communication with the auxiliary reaction chamber; and an integrated reformer in fluid communication with the auxiliary reaction chamber. The auxiliary reaction chamber can be configured to use heat from the heated first syngas stream received from the plasma chamber to initiate an exothermic reaction with a second syngas stream and output the heated second syngas stream to the integrated reformer.

[0008] A method for plasma carbon conversion may include passing a heated first syngas stream from a plasma chamber to an auxiliary reaction chamber; mixing the heated first syngas stream with a second gas stream in the auxiliary reaction chamber to initiate an exothermic reaction between the heated first syngas stream and the second gas stream; generating second thermal energy in the auxiliary reaction chamber using the exothermic reaction; passing the second thermal energy from the auxiliary reaction chamber to an integrated reformer; and generating syngas in the integrated reformer using the second thermal energy.

[0009] Example embodiments will be described and explained with additional specificity and detail through the accompanying drawings. [Brief explanation of the drawings]

[0010] [Figure 1] Block diagram of a plasma carbon conversion unit according to an example. [Figure 2] FIG. 1 illustrates the operation of a plasma reactor system according to an example. [Figure 3] 1 illustrates the operation of a plasma chamber, an auxiliary reaction chamber, and an integrated reformer, according to an example. [Figure 4] 1 is a block diagram of a plasma reaction system including a plasma chamber, an auxiliary reaction chamber, and an integrated reformer, according to an example; [Figure 5] 1 is a block diagram of a plasma reaction system including a plasma chamber, an auxiliary reaction chamber, and an integrated reformer, according to an example; [Figure 6] 1 is a block flow diagram of a plasma reaction system including a plasma chamber, an auxiliary reaction chamber, and an integrated reformer, according to an example; [Figure 7A] 1 is a block diagram of a plasma reaction system including one plasma reaction chamber and one auxiliary reaction chamber connected in parallel to multiple integrated reformers, according to an example. [Figure 7B] 1 is a block diagram of a plasma reaction system including multiple plasma reaction chambers connected in series with multiple auxiliary reaction chambers connected to an integrated reformer, according to an example. [Figure 7C] 1 is a block diagram of a plasma reaction system including multiple plasma reaction chambers connected in series with multiple auxiliary reaction chambers connected to an integrated reformer, according to an example. [Figure 7D] 1 is a block diagram of a plasma reaction system including multiple plasma reaction chambers connected to one auxiliary reaction chamber connected to one integrated reformer, according to an example; [Figure 7E] 1 is a block diagram of a plasma reaction including multiple plasma reaction chambers connected to one auxiliary reaction chamber connected to one integrated reformer connected to multiple auxiliary reaction chambers, according to an example. [Figure 7F]1 is a block diagram of a plasma reaction system including multiple plasma reaction chambers connected to one auxiliary reaction chamber connected to one integrated reformer connected to multiple auxiliary reaction chambers at different inlets, according to an example. [Figure 8] 1 is a diagram of a carbon dioxide utilization system using a plasma reaction system, according to an example. [Figure 9] FIG. 1 illustrates a system for synthesizing hydrogen gas and carbon monoxide using a plasma reaction system, according to an example. [Figure 10] FIG. 1 illustrates a system for converting biogas to hydrogen gas using a plasma reactor system, according to an example. [Figure 11] FIG. 1 illustrates an integrated reformer according to an example. [Figure 12] 1 illustrates a process flow for a plasma reactor system, according to an example. DETAILED DESCRIPTION OF THE INVENTION

[0011] Like reference numbers in the various drawings indicate like elements.

[0012] A gas reaction can occur in a reactor chamber of a gas reactor configured for an inlet flow and an outlet flow of gas. The inlet flow of gas can include one or more gas reactants, and the outlet flow can include one or more gas products produced based on the gas reactants included in the inlet flow. In some situations, the gas reaction can be an exothermic reaction that generates heat during the reaction process, while in other situations, the gas reaction can be an endothermic reaction that uses heat input to drive the reaction process. As such, the reactor chamber in which the gas reaction occurs can reach high temperatures during operation of the gas reactor.

[0013] A synthesis gas product can be produced with a H2:CO ratio (syngas ratio) of about 0.5:1 to 3:1. Various heat inputs can be used at different stages of the reaction process to produce the synthesis gas product. Maximizing the use of the thermal energy produced, recycling different gas streams, and preserving materials used in the high temperature reaction process can help increase synthesis gas production capacity, H2:CO ratios, and energy conversion efficiency.

[0014] Plasma reaction systems can enable the processing or reforming of gases (i.e., rearrangement of the molecular structure of hydrocarbons contained in the gas) by injecting unreacted gases after the plasma chamber contained in the plasma reaction system. The unreacted gases injected after the plasma chamber can react with "wasted" residual energy contained in the processed stream from the plasma chamber. This is achieved by one or more inlets designed to introduce an additional gas stream into the stream after the plasma chamber and to provide mixing between the two gas streams. If the reforming of the stream after the plasma is exothermic, the temperature of the mixed stream can be high enough for reforming to occur.

[0015] After mixing, the auxiliary reaction chamber can provide sufficient residence time for reformulation to occur in the mixed gas stream. Additionally or alternatively, the auxiliary reaction chamber can be or is externally cooled. The gas stream can leave the auxiliary reaction chamber and enter piping or tubing for further processing or storage of the gas.

[0016] Additionally, an integrated reformer can be present after the auxiliary reaction chamber. The integrated reformer can be a separate reaction unit connectable to the plasma reactor and / or the auxiliary reaction chamber. In systems including a plasma reactor, auxiliary reaction chamber, and integrated reformer, each of these units can be a separate unit or can be incorporated into a combined plasma reactor-auxiliary reaction chamber-integrated reformer unit, in which case the auxiliary reaction chamber and integrated reformer can be connected to the plasma reactor and to each other in any order and combination, including series, parallel, or combinations thereof. The auxiliary reaction chamber can provide the plasma reaction, and the integrated reformer can facilitate the non-plasma reaction.

[0017] The plasma chamber can be configured to facilitate the transfer of high heat energy from the plasma chamber to the auxiliary reaction chamber. The high heat energy can be used in the auxiliary reaction chamber to initiate a reforming reaction without using external heat input to the auxiliary reaction chamber. The reaction in the auxiliary reaction chamber can be an exothermic reaction, which can direct the output gas at a high temperature (high heat energy) to the integrated reformer. The reforming reaction in the integrated reformer can use the high heat energy of the product gas from the auxiliary reaction chamber without using external heat input. The reaction in the integrated reformer can be an endothermic reaction. The heat transferred from the plasma chamber and the auxiliary reaction chamber can be used to initiate an endothermic reaction in the integrated reformer. The remaining heat of the product gas from the integrated reformer can be used to preheat the feed gas (e.g., gas returning to the plasma chamber, the auxiliary reaction chamber, or the integrated reformer).

[0018] The plasma chamber, auxiliary reaction chamber, and integrated reformer can facilitate the following chemical reactions: (i) reforming natural gas (NG) with CO and / or O in the plasma chamber, (ii) reforming NG with CO and / or O in the auxiliary reaction chamber, and (iii) reforming NG with H O in the integrated reformer. That is, the net chemical reactions in one or more of the plasma chamber, auxiliary reaction chamber, and integrated reformer can include: (i) R: aCO + bCH + cO → dH + fCO + trace species (i.e., in the case of the plasma chamber), (ii) R: aCO + bCH + cO → dH + fCO + trace species (i.e., in the case of the auxiliary reaction chamber), and (iii) R: aH O + bCH → dH + fCO + trace species (i.e., in the case of the integrated reformer).

[0019] The use of an auxiliary reaction chamber in conjunction with a plasma chamber and an integrated reformer can facilitate syngas production amplification of up to 70 times the volume compared to syngas production without an auxiliary reaction chamber. Delivery capacity can also be increased (e.g., CO2 and CH4 delivery capacity can be increased 30 and 50 times compared to delivery capacity without an auxiliary reaction chamber). Syngas can be produced in the plasma chamber and auxiliary reaction chamber at a ratio of approximately H2:CO = 0.5:1 to 1:1. Syngas can be produced in the integrated reformer at a ratio of approximately H2:CO = 2:1 to 3:1. Consequently, the final syngas ratio (the ratio of syngas produced from the integrated reformer to the syngas received at the input to the plasma chamber) can have a ratio of H2:CO = 1.2:1 to 2:1.

[0020] The use of an auxiliary reaction chamber positioned between the plasma chamber and the integrated reformer (i) can facilitate improved energy efficiency by allowing the high thermal energy of the product gas from the plasma reactor to be used for further reforming reactions without additional power input, (ii) can facilitate reduced steam supply for reforming when using steam generated from the plasma reactor, and (iii) can facilitate improved syngas production capacity (e.g., up to 70 times more syngas product at H2:CO=2:1).

[0021] Reference will now be made to the drawings to illustrate various aspects of the examples, and it will be understood that the drawings are diagrammatic and schematic representations of such example embodiments and are not intended to be limiting of the disclosure, nor are they necessarily drawn to scale.

[0022] 1 shows a cross-sectional view of a plasma reaction system 100 including a plasma chamber 120 and an auxiliary reaction chamber 130. The plasma chamber 120 can include any number of inlets, including a first inlet 110, a second inlet 112, and a third inlet 114, through which one or more gases 102a, 102b, and 102c can enter the plasma chamber 120. By positioning two or more of the first inlet 110, the second inlet 112, or the third inlet on opposite or substantially opposite sides of the plasma chamber 120, the gas flow 102a corresponding to the first inlet 110 and the gas flow 102b corresponding to the second inlet 112 can create forward and reverse vortex configurations within the plasma chamber 120, promoting mixing and reaction of the gases 102a and 102b within the plasma chamber 120. The first inlet 110 and / or the second inlet 112 and / or the third inlet 114 can be positioned along any surface or other portion of the plasma chamber 120 and oriented in any direction to promote the flow of gases 102a, 102b, 102c into the plasma chamber 120 with different vortex configurations between the first inlet 110 and / or the second inlet 112 and / or the third inlet 114. For example, the first inlet 110 can be positioned at the top of the plasma chamber 120 such that the gas 102a enters from the top of the plasma chamber 120, while the second inlet 112 and / or the third inlet 114 can be positioned at the bottom of the plasma chamber 120 such that the gases 102b, 102c enter from the bottom of the plasma chamber 120. As another example, the second inlet 112 and the third inlet 114 may both be along a side of the plasma chamber 120, and the second inlet 112 and the third inlet 114 may be positioned opposite or substantially opposite one another. In some embodiments, the plasma chamber 120 may include one or more of the first inlet 110, or the second inlet 112, or the third inlet 114.

[0023] Multiple inlets can be oriented in a particular direction such that a forward vortex arrangement (i.e., corresponding to the first inlet 110) and / or a reverse vortex arrangement (i.e., corresponding to the second inlet 112) can include multiple inlet ports. As shown in FIG. 1 , for example, a reverse vortex arrangement can be formed by gases 102b and 102c flowing through the second inlet 112 and / or a third inlet 114, which can be oriented in the same or similar flow direction as the second inlet 112. Additionally or alternatively, the forward vortex arrangement can include more inlet ports than the first inlet 110, such as one or more inlet ports adjacent to the first inlet 110. Gases 102a, 102b, 102c entering the plasma chamber 120 through multiple inlet ports, which can contribute to a forward and / or reverse vortex arrangement, may or may not mix to form a single gas stream moving in the same direction. Gases 102b and 102c flowing through the second inlet 112 and the third inlet 114 can form gas flow streams 104 and 106, respectively, which are redirected by the top surface of the plasma chamber 120 and then enter the plasma chamber 120 as separate streams that mix within the plasma chamber 120.

[0024] One or more chamber walls 125 may surround the plasma chamber 120 and define an interior space of the plasma chamber 120 where chemical reactions between gases flowing into the plasma chamber 120 can occur. The chamber walls 125 may be one or more of: opaque to gases; inert to chemical reactions occurring within the plasma chamber 120; have a high melting point; or include a low thermal expansion coefficient. For example, the chamber walls 125 may include one or more of quartz, boron nitride, aluminum, ceramic, silicon carbide, tungsten, molybdenum, any other refractory material, or mixtures thereof. Additionally or alternatively, the chamber walls 125 may be made of a radio frequency transparent material that allows energy guided by one or more waveguides 140 to be delivered to the plasma 150 within the plasma chamber 120. In this manner, energy from microwave, electric, or other sources can be guided by the waveguides 140 through the chamber walls 125 to deliver energy to the plasma 150 and the plasma chamber 120.

[0025] In these and other embodiments, the average temperature of the plasma chamber 120 may generally range from about 1,000 Kelvin (K) to about 3,500 K, and the peak temperature of the plasma 150 may reach about 50,000 K or higher. The temperature at a particular location within the plasma chamber 120 (e.g., the center of the plasma chamber 120) may, in some cases, exceed the melting point of the chamber walls 125 and / or the waveguide 140. The forward and / or reverse vortex arrangement of the gases 102a, 102b, 102c may provide an insulating effect such that the chamber walls 125 and / or the waveguide 140 may not reach their respective melting points when the temperature at a particular location in the plasma chamber 120 exceeds their respective melting points.

[0026] The gases 102a, 102b, 102c in the plasma chamber 120 may include reactant gases that are involved in chemical reactions associated with reforming natural gas, producing hydrocarbons, combusting reactants, or any other chemical reaction that may be facilitated in the high temperature reactive environment provided by the plasma chamber 120 (where heat from the plasma 150 may provide sufficient energy to break molecular bonds and / or initiate certain chemical reactions). The outlet gas stream 160 may include chemical products produced by the chemical reactions occurring within the plasma chamber 120 and unreacted reactants contained in the gases 102a, 102b, 102c that entered the plasma chamber 120.

[0027] The outlet gas stream 160 can be mixed with one or more auxiliary reaction chamber gas flows 162, 164 to form the auxiliary reaction chamber inlet flow 170. The auxiliary reaction chamber gas flows 162, 164 can include gases that are the same as or similar to the gases 102a, 102b, 102c injected into the plasma chamber 120. Additionally or alternatively, the auxiliary reaction chamber gas flows 162, 164 can include reactants not present in the gases 102a, 102b, 102c and / or materials that facilitate the occurrence of one or more chemical reactions within the auxiliary reaction chamber 130. For example, waste gases and / or effluents from an associated chemical process or other plasma reactor can be included in the auxiliary reaction chamber gas flows 162, 164 to increase the waste-to-product conversion ratio of one or more waste gases or effluents. Additionally, including waste materials in the auxiliary reaction chamber gas flows 162, 164 can increase the waste-to-energy conversion relative to a threshold value.

[0028] Oxidant gases, such as air, oxygen, or nitric oxide, may be included in the auxiliary reaction-chamber gas flows 162, 164 to promote certain chemical reactions and enhance the production of certain chemical products. The inclusion of the auxiliary reaction chamber 130 from which the outlet gas stream 160 and various other gases are obtained may increase the reactivity of one or more chemical reactants, thereby enhancing the efficiency of the plasma reaction system 100. Additionally or alternatively, the inclusion of the auxiliary reaction chamber 130 in the plasma reaction system 100 may allow the plasma chamber 120 to be smaller, since the auxiliary reaction chamber 130 may increase the conversion rate of chemical reactants. In these and other embodiments, the auxiliary reaction-chamber gas flows 162, 164 may comprise a total flow rate ranging from about 50% to up to about 5000% of the flow rate of the outlet gas stream 160 exiting the plasma chamber 120 to provide gases and / or liquids for the chemical reactions occurring in the auxiliary reaction chamber 130.

[0029] The auxiliary reaction chamber gas flows 162, 164 may be directed through one or more auxiliary reaction chamber inlets 134, 136 to mix with the exit gas flow 160 of the plasma chamber 120. In some embodiments, the auxiliary reaction chamber inlets 134, 136 may be oriented at approximately 90° with respect to the exit gas flow 160, such that the auxiliary reaction chamber gas flows 162, 164 may be approximately perpendicular to the exit gas flow 160. Additionally or alternatively, the auxiliary reaction chamber inlets 134, 136 may be oriented at an angle ranging from approximately 30° to approximately 180° (i.e., counter-flow) with respect to the exit gas flow 160. Additionally or alternatively, the number of auxiliary reaction chamber inlets and / or the orientation of each auxiliary reaction chamber inlet may be different, with the two auxiliary reaction chamber inlets 134, 136 and the two auxiliary reaction chamber gas flows 162, 164 pointing in the same or similar direction relative to the exit gas flow 160. For example, a single auxiliary reaction chamber inlet can be used that is oriented 180° relative to the exit gas flow 160. As another example, three auxiliary reaction chamber inlets can be used that are oriented at various angles relative to the exit gas flow 160. The size and / or number of the auxiliary reaction chamber inlets (e.g., the two auxiliary reaction chamber inlets 136, 136) can be set based on the selected flow rates through the plasma chamber 120 and / or the auxiliary reaction chamber 130.

[0030] The auxiliary reaction chamber inlet flow 170 can be directed to the auxiliary reaction chamber 130 for further processing of one or more gases contained in the auxiliary reaction chamber inlet flow 170. One or more walls 132 of the auxiliary reaction chamber 130 can be made of a material with high heat resistance and / or a low coefficient of thermal expansion. For example, the walls 132 can include one or more of carbon steel or other carbon composites, nickel alloys, aerospace grade aluminum, titanium, quartz, ceramic, tungsten, molybdenum, or any other suitable material, including a refractory material.

[0031] The gases contained in the auxiliary reaction chamber inlet flow 170 can react in the auxiliary reaction chamber 130 to produce one or more chemical products. The chemical products produced by the chemical reactions in the auxiliary reaction chamber 130 can include the same chemical products produced by the chemical reactions occurring in the plasma chamber 120. Additionally or alternatively, the chemical products formed in the auxiliary reaction chamber 130 can include different chemicals that are not formed in the plasma chamber 120 based on different chemical reactions facilitated by materials contained in the auxiliary reaction chamber gas flows 162, 164 that were not present in the gases 102a, 102b, 102c that entered the plasma chamber 120.

[0032] In these and other embodiments, the chemical reaction occurring in the auxiliary reaction chamber 130 can be facilitated by heat carried over from the plasma chamber 120. As such, the auxiliary reaction chamber 130 may not include a plasma, and an energy source for heating the plasma 150 may not be directed to the auxiliary reaction chamber 130. Due to the absence of a plasma and / or a directed energy source, the auxiliary reaction chamber 130 may operate at a lower temperature than the plasma chamber 120, may include a larger volume than the plasma chamber 120, and / or may operate at the same or a different pressure (e.g., higher or lower) to facilitate the occurrence of the chemical reaction. Additionally or alternatively, because the auxiliary reaction chamber 130 can be operated at a lower temperature than the plasma chamber 120, the auxiliary reaction chamber 130 can be made of a material that is less heat-resistant than the plasma chamber 120. For example, the plasma chamber 120 can include aerospace-grade aluminum, while the auxiliary reaction chamber 130 can include molybdenum metal.

[0033] Chemical products formed during the chemical reactions occurring within the auxiliary reaction chamber 130, unreacted chemical reactants, and any other gases contained within the auxiliary reaction chamber 130 are directed out of the auxiliary reaction chamber 130 in an outlet gas stream 180. The outlet gas stream 180 may be sent to auxiliary devices of the plasma reaction system 100, such as a scrubber, a pressure swing adsorption unit, an amine unit, and / or a compressor. Additionally or alternatively, the outlet gas stream 180 may be sent to a second stage auxiliary reaction chamber for further processing of the products, unreacted chemicals, and / or any other gases contained within the outlet gas stream 180. Additionally or alternatively, the outlet gas stream 180 may be sent to an integrated reformer for further processing of the products, unreacted chemicals, and / or any other gases contained within the outlet gas stream 180.

[0034] 2, the plasma reaction system 200 can include (i) a plasma chamber 210, (ii) an auxiliary reaction chamber 230 fluidly coupled to the plasma chamber 210, and (iii) an integrated reformer 250 fluidly coupled to the auxiliary reaction chamber. The auxiliary reaction chamber 230 can be configured to absorb heat from the heated first syngas stream 214 received from the plasma chamber to initiate an exothermic reaction with one or more second gas streams 262, 264 and output the heated second syngas stream 234 to the integrated reformer 250. The "heated second syngas stream" can be a reaction product of the reaction between the heated first syngas stream and the second gas stream.

[0035] The plasma reaction system 200 can include a plasma chamber 210 connected in series to one or more auxiliary reaction chambers (e.g., auxiliary reaction chamber 230) and one or more integrated reformers (e.g., integrated reformer 250). The plasma chamber 210 can be the same as or similar to the plasma chamber 120 described in connection with FIG. 1. As such, the plasma chamber 210 can be configured to have one or more inlet flows, each of which can include one or more gases and / or a particular vortex configuration. Additionally or alternatively, the plasma chamber 210 can include a plasma heated by an energy source, such as a microwave source or a power source. In these and other embodiments, the first auxiliary reaction chamber 230 can be the same as or similar to the auxiliary reaction chamber 130 described in connection with FIG. 1. As such, the auxiliary reaction chamber 230 can have a size or volume larger than the size or volume of the plasma chamber 210 and / or can operate at the same or a different pressure than the pressure of the plasma chamber 210.

[0036] The integrated reformer 250 can be connected to the auxiliary reaction chamber 230 by mixing the outlet flow of the heated second syngas stream 234 of the first auxiliary reaction chamber 230 with one or more third gas streams 256a, 256b (e.g., input flows to the integrated reformer 250) and supplying it to the integrated reformer 250 as the integrated reformer inlet flow 252.

[0037] The integrated reformer 250 does not have to be connected to a heat source, such as the plasma 212 used to heat the plasma chamber 210. The integrated reformer can use heat from the heated second syngas stream 234 to initiate endothermic reactions to generate an outlet flow 254 (e.g., a gas product such as syngas). In this manner, chemical reactions that may occur within the integrated reformer 250 between gases contained in the integrated reformer stream 252 can be facilitated by heat from the auxiliary reaction chamber 230, which can be received by the integrated reformer 250 along with gases in the outlet flow of the heated second syngas stream 234 from the auxiliary reaction chamber 230.

[0038] The temperature of the integrated reformer 250 may be lower than the temperature of the auxiliary reaction chamber 230. As such, the integrated reformer 250 may be made of a material that has a lower thermal resistance and / or a higher coefficient of thermal expansion than the materials used in the auxiliary reaction chamber 230 and / or the plasma chamber 210. Additionally or alternatively, the integrated reformer 250 may include a larger volume than the auxiliary reaction chamber 230 and / or may be operated at the same or a different pressure than the auxiliary reaction chamber 230 to facilitate chemical reactions occurring within the integrated reformer 250.

[0039] The outlet flow 254 of the integrated reformer 250 can be sent to auxiliary devices of the plasma reaction system 100, such as a scrubber, a pressure swing adsorption unit, an amine unit, and / or a compressor, for further processing of the gas contained in the outlet flow 254. The outlet flow 254 can be directed to one or more additional auxiliary reaction chambers and / or integrated reformers (e.g., a second auxiliary reaction chamber in series, a second and third auxiliary reaction chambers in series, etc.), or any combination. In these and other embodiments, the operating temperature of each subsequent auxiliary reaction chamber in the series of auxiliary reaction chambers and / or integrated reformers can be lower than the operating temperature of the previous chamber in the series. As such, each subsequent chamber can have a larger size and / or volume than the previous chamber in the series and / or the same or a different pressure than the previous chamber in the series.

[0040] The outlet flow 254 of the integrated reformer 250, the outlet flow of the heated second syngas stream 234 of the auxiliary reaction chamber 230, and / or the outlet flow of the heated first syngas stream 214 of the plasma chamber 210 may be directed to one or more chambers (e.g., auxiliary reaction chambers, integrated reformers) that may be configured in parallel with each other.

[0041] 3, the plasma reaction system 300 can include a plasma carbon conversion unit 302. The plasma carbon conversion unit 302 can include one or more of a plasma chamber 310, an auxiliary reaction chamber 330, or an integrated reformer 350. The plasma chamber 310 can be configured to receive a first gas stream 306, which can include one or more of CO, CH (e.g., methane, natural gas, or renewable natural gas), O, etc., from one or more plasma chamber inlets.

[0042] The first gas flow can be directed to the plasma chamber 310 at a reference input flow rate of 1. The first gas flow can include any suitable ratio of gases to generate heat. The first gas flow can include a CO2:CH4 ratio of about 1:10 to about 10:1. Alternatively or additionally, the first gas flow can include a CO2:CH4 ratio of about 3:7 to about 5:5. The first gas flow can include a (CO2 + CH4):O2 ratio of about 1:10 to about 10:1. Alternatively or additionally, the first gas flow can include a (CO2 + CH4):O2 ratio of about 3:2 to about 4:1.

[0043] The plasma chamber 310 can be configured to apply power to the first gas stream to form a heated first syngas stream 315. The plasma chamber 310 can be configured to add heat to the first gas stream 306 using an external power source (e.g., microwave power 305). The external power source (e.g., microwave power 305) can be configured to promote an exothermic reaction within the plasma chamber 310 to add heat to the first gas stream 306. Alternatively or additionally, the plasma chamber 310 can be configured to add heat to the first gas stream 306 using an endothermic reaction. The plasma chamber 310 can be configured to output the heated first syngas stream 315 to the auxiliary reaction chamber 330 at a reference output flow rate of about 1 to 2 times the reference input flow rate. The heated first syngas stream 315 can be output to the auxiliary reaction chamber 330 at a syngas ratio of about 1:10 to about 10:1. Alternatively or additionally, the heated first syngas stream 315 may be output to the auxiliary reaction chamber 330 at a syngas ratio of about 1:2 to about 1:1. The syngas ratio may be the volume ratio of H to CO in the syngas (i.e., H:CO).

[0044] The auxiliary reaction chamber 330 can be configured to receive the heated first syngas flow 315 from the plasma chamber 310 at a flow rate (1x the reference output flow rate) that can be substantially the same as or higher than the flow rate supplied to the plasma chamber 310 (1x the reference input flow rate). The flow rates between two different flow rates can be substantially the same if the percentage difference between the lower flow rate and the higher flow rate is less than one or more of the following: 10%, 5%, 3%, 2%, or 1% (i.e., calculated as (1-(lower flow rate / higher flow rate) x 100)). The auxiliary reaction chamber 330 can be configured to receive a second gas flow 336 (which can include one or more of CO, CH, O, etc.) from the auxiliary reaction chamber inlet at a flow rate that can be from about 1 to about 29 times the flow rate of the reference input flow rate (i.e., the flow rate supplied to the plasma chamber 310 at 1x the flow rate). The second gas stream 336 may include a ratio that may be similar to the ratio provided in the first gas stream 306. That is, the second gas stream 336 may include a CO2:CH4 ratio of about 1:10 to about 10:1. Alternatively or in addition, the second gas stream 336 may include a CO2:CH4 ratio of about 3:7 to about 5:5. The second gas stream 336 may include a (CO2 + CH4):O2 ratio of about 1:10 to about 10:1. Alternatively or in addition, the second gas stream 336 may include a (CO2 + CH4):O2 ratio of about 3:2 to about 4:1.

[0045] The auxiliary reaction chamber 330 can be configured to initiate an exothermic reaction using thermal energy from the heated first syngas stream 315 received from the plasma chamber 310. The auxiliary reaction chamber 330 can be configured to initiate an exothermic reaction using thermal energy from the heated first syngas stream 315 without using additional external heat input.

[0046] The auxiliary reaction chamber 330 can be configured to output a heated second syngas stream 335 to the integrated reformer 350. The heated second syngas stream 335 can include the reaction products of the heated first syngas stream 315 and the second gas stream 336. The flow rate of the heated second syngas stream 335 directed from the auxiliary reaction chamber 330 to the integrated reformer 350 can be about 2 to about 30 times the nominal output flow rate (e.g., provided at 1.0 times the flow rate from the plasma chamber 310). The heated second syngas stream 335 can be output to the integrated reformer 350 at a syngas ratio (e.g., H:CO) of about 1:10 to about 10:1. Alternatively or additionally, the heated second syngas stream can be output to the integrated reformer 350 at a syngas ratio of about 1:2 to about 1:1.

[0047] The integrated reformer 350 may be configured to receive the heated second syngas stream 335 from a first integrated reformer inlet and a third gas stream 356 (which may include, for example, CH, HO, etc.) from a second integrated reformer inlet at a flow rate that may be about 2 to about 20 times the nominal input flow rate (i.e., provided to the plasma chamber 310 at 1.0 times the flow rate). The third gas stream 356 may include an HO:CH ratio of about 1:10 to about 10:1. Alternatively or additionally, the third gas stream 356 may include an HO:CH ratio of about 1:2 to about 3:1.

[0048] The integrated reformer 350 can be configured to use thermal energy from the heated second syngas stream 335 received from the auxiliary reaction chamber 330 to initiate endothermic reactions. The integrated reformer 350 can be configured to use thermal energy from the heated second syngas stream 335 to initiate endothermic reactions without using additional external heat input to the integrated reformer. Alternatively, or in addition, remaining thermal energy from the heated second syngas stream 335 that can be output from the integrated reformer 350 can be used to preheat various feed gases (e.g., the first gas stream 306, the second gas stream 336, the third gas stream 356, etc.).

[0049] The integrated reformer 350 can be configured to output a synthesis gas stream 355 (e.g., synthesis gas) from the integrated reformer 350 at a flow rate that is about 4 times to about 70 times greater than the reference output flow rate (i.e., supplied from the plasma chamber 310 at 1.0 times the flow rate).

[0050] The syngas stream 355 may be produced from the integrated reformer 350 with a syngas ratio of about 1:10 to about 10:1 (which may differ from the incoming syngas ratio received at the integrated reformer 350). Alternatively or additionally, the syngas stream 355 may be produced from the integrated reformer 350 with a syngas ratio of about 2:1 to about 3:1 (which may differ from the incoming syngas ratio received at the integrated reformer 350). Alternatively or additionally, the syngas stream 355 may be output from the integrated reformer 350 with a final syngas ratio of about 1:10 to about 10:1 (which may be a combination of the syngas ratio produced from the integrated reformer 350 and the incoming syngas ratio received at the auxiliary reaction chamber 330). Alternatively or additionally, the syngas stream 355 may be output from the integrated reformer 350 with a final syngas ratio (which may be a combination of the syngas ratio produced from the integrated reformer 350 and the incoming syngas ratio received at the auxiliary reaction chamber 330) of about 6:5 to about 2:1.

[0051] One or more of the plasma chamber 310, auxiliary reaction chamber 330, or integrated reformer 350 can be configured to carry out various chemical reactions, such as partial oxidation reactions, dry methane reforming reactions, steam methane reforming reactions, hydrocarbon cracking reactions, water-gas shift reactions, and methanol synthesis reactions. The partial oxidation reaction can include, for example, CH4 + 1 / 2 O2 → 2H2 + CO. The dry methane reforming reaction can include, for example, CH4 + CO2 → 2H2 + 2CO. The steam methane reforming reaction can include, for example, CH4 + H2O → 3H2 + CO. The hydrocarbon cracking reaction can include, for example, CxHy → CH4 + H2 + C + trace species. The water-gas shift reaction can include, for example, CO + H2O → H2 + CO2. The methanol synthesis reaction can include, for example, 2H2 + CO → CH3OH.

[0052] The plasma chamber 310 can be configured to carry out any suitable reaction, including one or more of a partial oxidation reaction, a dry methane reforming reaction, a steam methane reforming reaction, or a hydrocarbon decomposition reaction. In one example, the plasma chamber 310 can be configured to carry out one or more of: (i) a partial oxidation reaction + dry methane reforming reaction, (ii) a dry methane reforming reaction, (iii) a steam methane reforming reaction, or (iv) a hydrocarbon decomposition reaction. In one example, the plasma chamber 310 can be configured to promote the net chemical reaction: R0: a0CO2 + b0CH4 + c0O2 → d0H2 + f0CO + trace species.

[0053] The auxiliary reaction chamber 330 can be configured to conduct any suitable exothermic reaction using the thermal energy received from the plasma chamber 310 to initiate the exothermic reaction. The auxiliary reaction chamber 330 can be configured to conduct one or more of a partial oxidation reaction, a dry methane reforming reaction, or a steam methane reforming reaction. In one example, the auxiliary reaction chamber 330 can be configured to conduct one or more of the following: (i) a partial oxidation reaction + a dry methane reforming reaction, or (ii) a partial oxidation + a steam methane reforming reaction. In one example, the auxiliary reaction chamber 330 can be configured to promote the following net chemical reaction: R1: a1CO2 + b1CH4 + c1O2 → d1H2 + f1CO + trace species.

[0054] The integrated reformer 350 can be configured to perform any suitable endothermic reaction using the thermal energy received from the auxiliary reaction chamber 330 to perform the endothermic reaction. The integrated reformer 350 can be configured to perform one or more of the following reactions (e.g., to produce methanol, liquid fuels, chemicals, plastics, etc.): (i) a steam methane reforming reaction, (ii) a dry methane reforming reaction, (iii) a water-gas shift reaction, (iv) a catalytic reaction, or (v) a non-catalytic reaction. In one example, the integrated reformer 350 can be configured to promote the following net chemical reaction: R2: a2H2O + b2CH4 → d2H2 + f2CO + trace species.

[0055] As shown in FIG. 4 , the plasma reaction system 400 can include a plasma carbon conversion unit 402 (PCCU), which can promote a high-temperature reaction environment to drive chemical reactions to completion. The PCCU 402 can be used to perform chemical reactions that dissociate carbon dioxide 406 and / or produce various product gases, such as hydrogen gas and carbon monoxide. Chemical reactions performed using the PCCU 402 can result in increased product gas yields compared to baseline amounts (which may not involve the use of the PCCU 402) because the PCCU 402 can promote energy to drive the formation of the product gases. Additionally or alternatively, the PCCU 402 can convert biogas 406a to syngas (syngas 456a) and, in addition, contain unreacted (or residual) carbon dioxide gas 456b. The energy generated by the PCCU 402 can promote further operation of other processing units and / or chemical reactions. For example, excess heat from a plasma reactor (e.g., plasma chamber 310 shown in FIG. 3) can be used to drive the operation of an integrated reformer 350, a heat utilization unit, a compressor, or any other process for the formation, recycling, and / or separation of various product gases.

[0056] The PCCU 402 can use various inputs, including one or more of biogas 406a, carbon dioxide 406b, methane gas 406c (or any other hydrocarbon gas), and input energy to produce various outputs, including one or more of carbon dioxide gas 456b, energy 455, heat 456h, syngas 456a, steam, etc. The amount of carbon dioxide 406b included in the input stream to the PCCU 402 can be greater than the amount of carbon dioxide 456b included in the output stream of the PCCU 402. Furthermore, because the chemical reactions occurring in the PCCU 402 can be exothermic reactions that can generate heat 456h, the input energy 405 can be less than the output energy 455 produced by the PCCU 402. The energy 455 produced by the chemical reactions occurring in the PCCU 402 and / or unreacted carbon dioxide 456b from the chemical reactions can be recycled and included in the input to the PCCU 402 to drive further chemical reactions or dissociation of carbon dioxide.

[0057] 5, the plasma reaction system 500 may include a PCCU (e.g., including one or more of a plasma chamber 510, an auxiliary reaction chamber 530, or an integrated reformer 550) and a carbon dioxide separator 590. The plasma chamber 510 may be configured to receive a first gas stream (e.g., natural gas 506a, carbon dioxide 506b, and oxygen gas 506d) and use energy 505 to facilitate the production of a heated first syngas stream (e.g., syngas).

[0058] The auxiliary reaction chamber 530 can be configured to receive (i) a heated first syngas stream 515 (e.g., syngas) from the plasma chamber 510 and (ii) a second gas stream (e.g., natural gas 516a, carbon dioxide 516b, and / or oxygen gas 516d) from one or more auxiliary reaction chamber inlets. The auxiliary reaction chamber 530 can be configured to use thermal energy generated by exothermic chemical reactions occurring within the plasma chamber 510 to facilitate the production of the heated second syngas stream 535 (e.g., syngas). The production of the heated second syngas stream 535 (e.g., syngas) occurring within the auxiliary reaction chamber 530 can occur without additional external heat input to the auxiliary reaction chamber 530.

[0059] The integrated reformer 550 can be configured to receive (i) the heated second synthesis gas stream 535 (e.g., synthesis gas) from the auxiliary reaction chamber 530, and (ii) a third gas stream (e.g., natural gas 546a steam 546e) from one or more integrated reformer inlets. The integrated reformer 550 can be configured to use heat energy generated by exothermic chemical reactions occurring in the auxiliary reaction chamber 530 to facilitate the production of the synthesis gas stream 555 (e.g., synthesis gas). The integrated reformer 550 can use heat energy generated by exothermic reactions occurring in the auxiliary reaction chamber 530 to perform endothermic reactions to facilitate the production of the synthesis gas stream 555 (e.g., synthesis gas). The production of the synthesis gas stream 555 (e.g., synthesis gas) occurring in the integrated reformer 550 can occur without additional external heat input to the integrated reformer.

[0060] Carbon dioxide separator 590 may be configured to receive syngas stream 555 (e.g., syngas) from integrated reformer 550. Carbon dioxide separator 590 may be configured to separate carbon dioxide 596b from input syngas (e.g., syngas stream 555 (e.g., syngas)) to produce output syngas 595.

[0061] 6, the gas flow and energy flow diagram of the plasma reaction system 600 can include one or more of a plasma chamber 610, an auxiliary reaction chamber 630, or an integrated reformer 650. The plasma chamber 610 can be configured to initiate an exothermic reaction upon receiving energy 605. The plasma chamber 610 can be configured to receive one or more chemicals suitable for initiating an exothermic reaction that produces heat, which is directed to the auxiliary reaction chamber 630. The one or more chemicals can include CO2 606b, CH4 606c, O2 606d, combinations thereof, etc.

[0062] The flow rates of the one or more chemicals may include any rate suitable for achieving exothermic and / or endothermic reactions. The base input flow rate of CO to the plasma chamber 610 may be from about 0.1 kg / hour to about 50 kg / hour. In one example, the base input flow rate of CO to the plasma chamber 610 may be from about 2 kg / hour to about 10 kg / hour. The base input flow rate of CH to the plasma chamber 610 may be from about 0.1 kg / hour to about 50 kg / hour. In one example, the base input flow rate of CH to the plasma chamber 610 may be from about 1 kg / hour to about 10 kg / hour. The base input flow rate of O to the plasma chamber 610 may be from about 0.1 kg / hour to about 50 kg / hour. In one example, the base input flow rate of O to the plasma chamber 610 may be from about 1 kg / hour to about 10 kg / hour.

[0063] The energy in the plasma chamber 610 can be increased using the energy 605 and / or input chemicals (e.g., CH4). The input power to the plasma chamber 610 can include an amount suitable to initiate an exothermic reaction and can include about 0.1 kW to about 100 kW. In one example, the input power can be about 1.0 kW to about 10 kW. The input chemicals can facilitate any amount of energy production suitable to initiate an exothermic reaction. For example, the energy production facilitated by a base input flow rate of CO2 to the plasma chamber 610 can be about 1 kW to about 500 kW. In one example, the energy production facilitated by a base input flow rate of CO2 to the plasma chamber 610 can be about 1 kW to about 100 kW.

[0064] The auxiliary reaction chamber 630 can be configured to receive the heated first syngas stream 615 from the plasma chamber 610. The heated first syngas stream 615 can be combined with one or more additional chemicals in the auxiliary reaction chamber 630. The one or more additional chemicals can include the same chemicals input to the plasma chamber 610. The flow rates of the one or more chemicals introduced into the auxiliary reaction chamber 630 can be selected to initiate an exothermic reaction in the auxiliary reaction chamber 630. The flow rate of CO2 into the auxiliary reaction chamber 630 can be from about 1 kg / hour to about 1000 kg / hour. In one example, the flow rate of CO2 into the auxiliary reaction chamber 630 can be from about 10 kg / hour to about 250 kg / hour. The flow rate of CH4 into the auxiliary reaction chamber 630 can be from about 1 kg / hour to about 1000 kg / hour. In one example, the flow rate of CH4 into the auxiliary reaction chamber 630 can be from about 1 kg / hour to about 100 kg / hour. The flow rate of O2 into the auxiliary reaction chamber 630 can be from about 1 kg / hour to about 500 kg / hour. In one example, the flow rate of O2 into the auxiliary reaction chamber 630 can be from about 1 kg / hour to about 100 kg / hour.

[0065] The energy in the auxiliary reaction chamber 630 can be increased using energy 605 and / or input chemicals (e.g., CH4). The input chemicals can facilitate any suitable amount of energy production to initiate an exothermic reaction without additional power input to the auxiliary reaction chamber 630. For example, the energy production facilitated by the flow rate of CH4 into the auxiliary reaction chamber 630 can be from about 1 kW to about 5000 kW. In one example, the energy production facilitated by the flow rate of CH4 into the auxiliary reaction chamber 630 can be from about 100 kW to about 1000 kW. Alternatively or additionally, the energy production facilitated by the flow rate of the heated first syngas stream 615 into the auxiliary reaction chamber 630 can be from about 1 kW to about 1000 kW. In one example, the energy production facilitated by the flow rate of the heated first syngas stream 615 into the auxiliary reaction chamber 630 can be from about 10 kW to about 100 kW. The flow rates of one or more of the heated first syngas stream 615 or input chemicals (e.g., CO2, CH4, O2, etc.) to the auxiliary reaction chamber 630 can be selected to maximize the production of the heated second syngas stream 635 for input to the integrated reformer 650.

[0066] The integrated reformer 650 may be configured to receive the heated second syngas stream 635 and one or more additional chemicals (e.g., CH 606c, HO 646w) and perform an endothermic reaction to produce a syngas 655. The flow rates for the one or more chemicals sent to the integrated reformer 650 may be selected to perform an endothermic reaction within the integrated reformer 650. The flow rate of CH to the integrated reformer 650 may be from about 1 kg / hour to about 500 kg / hour. In one example, the flow rate of CH to the integrated reformer 650 may be from about 1 kg / hour to about 100 kg / hour. The flow rate of HO to the integrated reformer 650 may be from about 1 kg / hour to about 500 kg / hour. In one example, the flow rate of HO to the integrated reformer 650 may be from about 1 kg / hour to about 100 kg / hour.

[0067] The energy in the integrated reformer 650 can be increased using the heated second syngas stream 635 and / or an input chemical (e.g., CH). The input chemical can facilitate any suitable amount of energy production to initiate endothermic reactions without additional power input to the integrated reformer 650. For example, the energy production facilitated by the flow rate of CH to the integrated reformer 650 can be from about 1 kW to about 10,000 kW. In one example, the energy production facilitated by the flow rate of CH to the integrated reformer 650 can be from about 100 kW to about 5,000 kW. Alternatively or additionally, the energy production facilitated by the flow rate of the heated second syngas stream 635 to the integrated reformer 650 can be from about 1 kW to about 10,000 kW. In one example, the energy production facilitated by the flow rate of the heated first syngas stream 615 to the integrated reformer 650 can be from about 100 kW to about 1,000 kW.

[0068] The flow rate of one or more of the heated second syngas stream 635 or the input chemicals (e.g., CH4, etc.) to the integrated reformer 650 can be selected to maximize the production of syngas 655 for output from the integrated reformer 650. For example, the flow rate of the syngas 655 from the integrated reformer 650 can be from about 10 kg / hour to about 10,000 kg / hour. Alternatively, or in addition, the flow rate of the syngas 655 from the integrated reformer 650 can be from about 10 kg / hour to about 100 kg / hour. The energy produced by the integrated reformer 650 can be from 1 kW to about 100,000 kW. In one example, the energy produced by the integrated reformer 650 can be from 100 kW to about 10,000 kW.

[0069] The energy of syngas 655 may include any suitable ratio compared to one or more of: (i) the energy produced by heated first syngas stream 615 as output from plasma chamber 610, or (ii) the energy produced by heated second syngas stream 635 as output from auxiliary reaction chamber 630. In one example, the energy of syngas 655 may include a ratio of 1 to 100 times the energy produced by heated first syngas stream 615. In another example, the energy of syngas 655 may include a ratio of 1 to 10 times the energy of heated second syngas stream 635.

[0070] 7A is a diagram of an example plasma reaction system 700a including a plasma chamber 710 connectable to a first reaction chamber (e.g., auxiliary reaction chamber 730), which can be connected to a second reaction chamber (e.g., integrated reformer 750), a third reaction chamber 752, and a fourth reaction chamber 754, which can be connected in parallel to each other. Although plasma reaction system 700a is illustrated with the first reaction chamber arranged in series first, followed by the second reaction chamber (e.g., integrated reformer 750), the third reaction chamber 752, and the fourth reaction chamber 754 in parallel, the outlet flow of plasma chamber 710 can be achieved by first arranging the first reaction chamber, the second reaction chamber (e.g., integrated reformer 750), the third reaction chamber 752, and / or the fourth reaction chamber 754 in parallel in a single serial stage. Additionally or alternatively, one or more reaction chambers may be configured in parallel with one another in a first series stage, and one or more reaction chambers may be configured in parallel in a second series stage after the first series stage, and any number of series stages with any number of reaction chambers configured in parallel in each series stage are contemplated. Additionally or alternatively, each reaction chamber configured in parallel in a particular series stage may be simultaneously connected to one or more reaction chambers in a subsequent series stage and isolated from one or more other reaction chambers in the same subsequent series stage.

[0071] Various reactor units can be inserted between one or more reaction chambers involved in a chemical process involving the plasma reaction system 700a. For example, a non-plasma heat source can be inserted between two serial stages to provide supplemental thermal energy to one or more reaction chambers. As another example, an integrated reformer, a pressure swing adsorption unit, an air separation unit, and / or any other reactor unit can be implemented to facilitate the addition and / or removal of materials from a chemical process. The reaction chambers described herein can include any type of reaction chamber, including an auxiliary reaction chamber or an integrated reformer. Furthermore, the first reaction chamber need not be present, and the plasma chamber 710 can be fluidly connected to a second reaction chamber (e.g., the integrated reformer 750), a third reaction chamber 752, and / or a fourth reaction chamber 754.

[0072] Reaction chambers configured in parallel can receive gases of the same or similar composition flowing at the same or similar flow rates. As a result, reaction chambers configured in parallel can be operated at the same or similar temperatures and can include the same or similar volumes and / or operating pressures. Additionally or alternatively, one or more reaction chambers configured in parallel in a particular serial stage can receive gases at a different flow rate and / or composition than the gases received by other reaction chambers in the same particular serial stage. For example, a first pipe directing gas to a first reaction chamber in a particular serial stage can include a larger diameter than a second pipe directing gas to a second reaction chamber in the particular serial stage, such that the first reaction chamber receives a greater gas flow rate than the second reaction chamber.

[0073] As shown in Figures 7A to 7F, plasma reaction systems 700a, 700b, 700c, 700d, 700e, and 700f can be configured to include (i) one or more plasma chambers (e.g., plasma chamber 710), (ii) one or more auxiliary reaction chambers (e.g., auxiliary reaction chamber 730), or (iii) one or more integrated reformers (e.g., integrated reformer 750).

[0074] The one or more plasma chambers may include a single plasma chamber 710 that can feed in series into a single auxiliary reaction chamber 730, as shown in Figure 7A. The one or more plasma chambers may include multiple plasma chambers 710a, 710b, 710c that can separately feed multiple auxiliary reaction chambers 730a, 730b, 730c, as shown in Figures 7B and 7C. The one or more plasma chambers may also include multiple plasma chambers 710a, 710b, 710c that can feed in series into a single auxiliary reaction chamber 730, as shown in Figures 7D-7F.

[0075] The one or more auxiliary reaction chambers may include a single auxiliary reaction chamber 730 that can be configured to feed multiple integrated reformers 750, as shown in Figure 7A. The one or more auxiliary reaction chambers may include multiple auxiliary reaction chambers 730a, 730b, 730c that can be configured to feed a single integrated reformer 750, as shown in Figures 7B, 7C, 7E, and 7F. The one or more auxiliary reaction chambers may include multiple auxiliary reaction chambers 730a, 730b, 730c that can be configured to feed a single integrated reformer 750 at separate feed positions (e.g., first feed position 759a, second feed position 759b, third feed position 759c, etc.) to produce syngas 755, as shown in Figures 7C and 7F. The one or more auxiliary reaction chambers may include a single auxiliary reaction chamber 730 (e.g., configured to receive the second gas stream 736) that may be configured to feed a single integrated reformer 750 (e.g., configured to receive the third gas stream 756), as shown in Figure 7D. The one or more auxiliary reaction chambers may include multiple auxiliary reaction chambers 730a, 730b, 730c that may be configured to feed the single integrated reformer 750 at feed locations, as shown in Figure 7E.

[0076] Various configurations of the one or more plasma chambers, one or more auxiliary reaction chambers, and one or more integrated reformers can be selected to maximize energy conversion efficiency (ECE) (i.e., ECE = product energy / input energy). The one or more auxiliary reaction chambers can be configured to receive one or more additional heated first syngas streams from one or more additional plasma chambers (e.g., plasma chambers 710a, 710b, 710c). The one or more integrated reformers can be configured to receive one or more additional heated second syngas streams from one or more additional auxiliary reaction chambers (e.g., auxiliary reaction chambers 730a, 730b, 730c). The one or more additional heated second syngas streams can be received at one or more additional integrated reformer inlets (e.g., first feed position 759a, second feed position 759b, third feed position 759c, etc., as shown in Figures 7C and 7F).

[0077] FIG. 8 is a diagram of a plasma reaction system 800 for carbon dioxide utilization using a PCCU. The carbon dioxide utilization system can include a precompressor unit 802 that can input biogas to increase the pressure of input biogas 801, which can include methane and carbon dioxide. The increase in pressure of the input biogas 801 can be facilitated by directing electrical power 881 from a heat utilization unit 880 to the precompressor unit 802. For example, the input biogas 801 can be obtained by the precompressor unit 802 at a pressure of 0.5 atm, 1 atm, 1.5 atm, 2 atm, or other pressure, and the biogas 803 exiting the precompressor unit 802 can be at a pressure of 2 atm, 3 atm, 5 atm, 10 atm, 20 atm, 100 atm, or other pressure. The pressurized biogas 803 can be sent to a scrubber 804 that can remove impurities, pollutants, or other harmful components of the biogas. For example, scrubber 804 may include a dry scrubbing process in which harmful substances (e.g., sulfur oxides, particulate matter, acid gases, etc.) are adsorbed onto a dry reagent contained in scrubber 804. As another example, scrubber 804 may include a wet scrubbing process in which biogas 803 is sprayed with a wet substance (e.g., water) to separate one or more components from biogas 803.

[0078] The air separator 806 may receive an input air stream 805 and separate the input air stream 805 into its constituent components, which may primarily include nitrogen gas and oxygen gas. The air separator 806 may facilitate separation of the components contained in the input air stream 805 via one or more of fractional distillation, pressure swing adsorption, vacuum pressure swing adsorption, membrane separation, or any other separation method. The separated air components 807a, 807b may be sent to the plasma chamber 810 of the PCCU, which may include one or more of the plasma chamber 810, the auxiliary reaction chamber 830, or the integrated reformer 850.

[0079] The cleaned biogas 849 can be sent to the plasma chamber 810 and auxiliary reaction chamber 830 of the PCCU. The plasma reactor can include a plasma chamber 810 made of quartz or ceramic material, with one or more waveguides configured to facilitate chemical reactions occurring within the plasma chamber 810. Fuel (e.g., natural gas or a hydrocarbon such as methane) and other input compounds heated by electricity or microwaves can react to provide additional heat to the input compounds in the plasma chamber 810. The plasma chamber 810 can be configured to receive inlet streams of cleaned biogas 849a, separated air components 807a, 807b, and carbon dioxide 887b from the amine unit 886 to affect chemical reactions between the inlet gas streams. For example, the incoming cleaned biogas 849a can react with the incoming carbon dioxide 887b and oxygen 807b at the high temperature provided by the electrically heated plasma to form syngas 811 and excess heat, which can then be sent to the auxiliary reaction chamber 830.

[0080] The auxiliary reaction chamber 830 can be configured to receive the syngas 811 from the plasma chamber 810, the cleaned biogas 849b, and the carbon dioxide 887c from the amine unit 886 to affect a chemical reaction between the inlet gas streams. For example, in the auxiliary reaction chamber 830, the incoming cleaned biogas 849b can react with the incoming carbon dioxide 887c at an elevated temperature provided by heat generated by the plasma chamber 810 (e.g., via an exothermic reaction) to form the syngas 831 and excess heat, which can then be sent to the integrated reformer 850. In this and other examples, oxygen gas obtained from the air separator 806 can facilitate the reaction between the cleaned biogas and the carbon dioxide.

[0081] Integrated reformer 850 may include a steam methane reforming reactor (SMR) or any other reactor vessel that may be configured to convert hydrocarbons contained in natural gas 809 into hydrogen and carbon monoxide using electrically or microwave-generated heat (e.g., heat provided by plasma chamber 810) and chemical reaction heat (e.g., heat provided by the plasma chamber and auxiliary reaction chambers) rather than combusted natural gas or other fuel. Additionally or alternatively, integrated reformer 850 may be configured to generate additional synthesis gas using natural gas 809. Integrated reformer 850 may be configured to obtain a recycled stream of steam 851b from heat utilization unit 880, which provides additional reactants and facilitates higher conversion of hydrocarbons and biogas to one or more product gases.

[0082] The syngas 851a produced by the integrated reformer 850 can be sent to a heat utilization unit 880, which can produce a cooled product gas 851c and a stream of steam 851b and 851d. The heat utilization unit 880 can include a steam or power generation unit, which can be configured to receive an input stream of water 879 and the syngas 851a produced from the integrated reformer 850. The heat utilization unit 880 can use excess heat generated by the PCCU and input to the heat utilization unit 880 by the incoming syngas 851a stream from the integrated reformer 850 to vaporize the input water 879, and the produced steam 851d can be sent to a water gas shifter (WGS) 882. A portion of the syngas 851a sent from the integrated reformer 850 to the heat utilization unit 880 can be sent to the WGS 882 (851c). The WGS 882 can facilitate the formation of hydrogen gas via the water gas shift reaction, in which carbon monoxide and water react reversibly to form carbon dioxide and hydrogen (851e) that is sent back to the heat utilization unit 880. Additionally or alternatively, excess steam 851b from the heat utilization unit 880 can be sent to the integrated reformer 850 to reclaim excess heat and facilitate the formation of syngas 851a in the integrated reformer 850.

[0083] The hydrogen gas and unreacted or partially reacted materials can be sent from heat utilization unit 880 to compressor 884, which pressurizes input material 883 and sends output gas 885 to amine unit 886. The increase in pressure of input material 883 can be facilitated by excess power available from heat utilization unit 880. For example, input material 883 can be obtained by the compressor at a pressure of 0.5 atm, 1 atm, 1.5 atm, 2 atm, or other pressure, and the hydrogen gas and / or any other gases exiting compressor 884 can be at a pressure of 2 atm, 3 atm, 5 atm, 10 atm, 20 atm, 100 atm, or other pressure.

[0084] Amine unit 886 can contain various aqueous amine solutions that can react with gas 885 exiting compressor 884 to remove residual impurities (e.g., hydrogen sulfide, sulfur oxides, or any other harmful substances). Additionally or alternatively, the amines contained in amine unit 886 can facilitate the removal of acid gases such as carbon dioxide. Carbon dioxide 887b, 887c removed by amine unit 886 can be recycled and sent back to plasma chamber 810 and / or auxiliary reaction chamber 830 to further promote syngas reactions. Partially reacted or unreacted gases that may have entered amine unit 886 with the hydrogen gas product can be diverted with the recycled stream of biogas 849 to integrated reformer 850 to further promote the chemical reactions associated with the formation of syngas 851a and / or hydrogen gas product.

[0085] The remaining hydrogen gas and residue gas from amine unit 886 can be sent to a pressure swing adsorption unit 888 (PSA) to further separate the resulting gas 887a and produce high-purity H2 889a. For example, pressure swing adsorption unit 888 can include a membrane of adsorbent material that can separate hydrogen gas from any other gases that enter pressure swing adsorption unit 888 by capturing compounds that pass through the membrane other than hydrogen gas. The gas captured by the membrane can be desorbed from the adsorbent material by reducing the pressure in pressure swing adsorption unit 888, and this desorbed gas 889b can be recycled to the PCCU (e.g., integrated reformer 850) for further reaction.

[0086] Modifications, additions, or omissions can be made to the carbon dioxide utilization system without departing from the scope of the present disclosure. For example, the designations of different elements in the described manner are intended to help explain the concepts described herein and are not intended to be limiting. For example, in some embodiments, the precompressor unit 802, scrubber 804, air separator 806, PCCU (including plasma chamber 810, auxiliary reaction chamber 830, and integrated reformer 850), heat utilization unit 880, WGS 882, compressor 884, amine unit 886, and pressure swing adsorption unit 888 are depicted in the particular manner described to help explain the concepts described herein, but such depictions are not intended to be limiting. Furthermore, the carbon dioxide utilization system can include any number of other elements or be implemented in systems or contexts other than those described.

[0087] FIG. 9 is a diagram of a plasma reaction system 900 that synthesizes hydrogen gas and carbon monoxide using a PCCU. The carbon dioxide utilization system can include a precompressor unit 902 that can input biogas to increase the pressure of input biogas 901, which can include methane and carbon dioxide. The increase in pressure of the input biogas 901 can be facilitated by directing power 981 from a heat utilization unit 980 to the precompressor unit 902. For example, the input biogas 901 can be obtained by the precompressor unit 902 at a pressure of 0.5 atm, 1 atm, 1.5 atm, 2 atm, or other pressure, and the biogas 903 exiting the precompressor unit 902 can be at a pressure of 2 atm, 3 atm, 5 atm, 10 atm, 20 atm, 100 atm, or other pressure. The pressurized biogas 903 can be sent to a scrubber 904 that can remove impurities, pollutants, or other harmful components of the biogas. For example, the scrubber 904 may include a dry scrubbing process in which harmful substances (e.g., sulfur oxides, particulate matter, acid gases, etc.) are adsorbed onto a dry reagent contained in the scrubber 904. As another example, the scrubber 904 may include a wet scrubbing process in which the biogas is sprayed with a wet substance (e.g., water) to separate one or more components from the biogas 903. The cleaned biogas 949 may be sent to the plasma chamber 910, auxiliary reaction chamber 930, and / or integrated reformer 950 of the PCCU.

[0088] The air separator 906 can receive an input air stream 905 and separate the input air stream 905 into its constituent components, which may primarily include nitrogen and oxygen gases. The air separator 906 can facilitate separation of the components contained in the input air stream 905 via fractional distillation, pressure swing adsorption, vacuum pressure swing adsorption, membrane separation, or any other separation method. The separated air components 907a, 907b can be sent to a PCCU, which may include a plasma chamber 910, an auxiliary reaction chamber 930, and / or an integrated reformer 950.

[0089] The plasma chamber 910 may be made of quartz or a ceramic material, and one or more waveguides may be configured to facilitate chemical reactions that may occur within the plasma chamber 910. Fuel (e.g., hydrocarbons) and other input compounds heated by electricity or microwaves may react to provide additional heat to the input compounds of the plasma reactor. The plasma chamber 910 may be configured to receive an inlet stream of separated air components 907a, 907b and cleaned biogas 949a from a scrubber. Oxygen gas obtained from the air separator 906 and energy provided within the plasma reactor may facilitate the conversion of the cleaned biogas 949a to syngas 911.

[0090] The auxiliary reaction chamber 930 can be configured to obtain syngas 911 from the plasma chamber 910 and cleaned biogas 949b and affect a chemical reaction between the inlet gas streams. For example, in the auxiliary reaction chamber 930, the incoming biogas 949b can react at an elevated temperature supplied by the heat generated by the plasma chamber 910 (e.g., by an exothermic reaction) to form syngas 931 and excess heat, which can be sent to the integrated reformer 950.

[0091] The integrated reformer 950 may include a steam methane reforming reactor (SMR) or any other reactor vessel configured to obtain the scrubbed biogas 949c and / or natural gas 909 from the scrubber 904 and convert them into syngas 951a using electrically or microwave-generated heat and chemical reaction heat (e.g., heat provided by one or more of the plasma chamber 910 or auxiliary reaction chamber 930). Additionally or alternatively, the integrated reformer 950 may be configured to obtain a recycled stream of waste gas from the separator unit 988 and / or a recycled stream of steam 951b from the heat utilization unit 980, which provide additional reactants to facilitate a higher conversion rate of biogas to syngas 951a. The syngas 951a produced by the chemical reactions occurring within the PCCU may be produced more efficiently than syngas produced by other existing chemical processes. Additionally or alternatively, heat generated by reactions occurring in the plasma chamber 910 and / or auxiliary reaction chamber 930 may be input to the integrated reformer 950, so that additional heat may not be used to drive the synthesis gas reactions occurring in the integrated reformer 950.

[0092] The syngas 951a produced by the integrated reformer 950 can be sent to a heat utilization unit 980, which can generate one or more product gases 983 derived from the syngas 951a. The heat utilization unit 980 can include a steam or power generation unit, which can be configured to receive an input stream of water 979 and the syngas 951a produced from the integrated reformer 950. The heat utilization unit 980 can use excess heat generated by the PCCU and input to the heat utilization unit 980 by the incoming syngas 951a stream from the integrated reformer 950 to vaporize the input water 979, and the generated steam 951b can power the production of the syngas product gas 951a in the integrated reformer 950.

[0093] Excess steam 951b from the heat utilization unit 980 can be sent to the integrated reformer 950 to reclaim excess heat and drive the formation of syngas 951a in the integrated reformer 950. The product gas produced from the syngas 951a can include hydrogen gas and carbon monoxide in a ratio ranging from 0.5:1 to 2.9:1. The ratio of the product gas from the heat utilization unit 980 can depend on the volume and composition of the input biogas 901 entering the precompressor unit 902, the volume of the input air stream 905 entering the air separator 906, the amount of energy provided to the plasma chamber 910 of the PCCU, the amount of steam 951b sent from the heat utilization unit 980 to the integrated reformer 950, or a combination thereof. For example, if there is no recycle stream from the heat utilization unit 980 to the integrated reformer 950, the ratio of hydrogen gas to carbon monoxide ranges from about 0.5:1 to about 1.5:1, while the ratio of hydrogen gas to carbon monoxide can increase from about 1.3:1 to about 2.9:1 depending on the amount of steam 951b recycled to the integrated reformer 950.

[0094] Product gas 983 and unreacted or partially reacted materials may be sent from heat utilization unit 980 to compressor 984, which compresses product gas 983 (and any other input materials) and outputs pressurized product gas 985 to amine unit 986. The increase in pressure of product gas 983 may be facilitated by excess heat obtained from heat utilization unit 980. For example, product gas 983 may be obtained by compressor 984 at a pressure of 0.5 atm, 1 atm, 1.5 atm, 2 atm, or other pressure, and hydrogen gas and / or any other gases exiting compressor 984 may be at a pressure of 2 atm, 3 atm, 5 atm, 10 atm, 20 atm, 100 atm, or other pressure.

[0095] Amine unit 986 can include various aqueous amine solutions that can react with the pressurized product gas 985 exiting compressor 984 to remove residual impurities (e.g., hydrogen sulfide, sulfur oxides, or any other harmful substances). Additionally or alternatively, the amines included in amine unit 986 can facilitate the removal of acid gases such as carbon dioxide. Carbon dioxide 991 removed by amine unit 986 can be sent to another reactor unit or to a treatment system such as a carbon dioxide utilization system.

[0096] The pressurized product gas 985 processed in the amine unit 986 can be sent to a separator unit 988, which separates the various components of the product gas 987a. As such, partially reacted or unreacted gases that entered the separator unit 988 with the product gas can be diverted in a recycle stream 989b to the integrated reformer 950 to further complete the chemical reactions involved in forming the syngas 951a. Additionally or alternatively, the separator unit 988 can include a fractionation system, a vacuum pressure swing adsorption system, or any other separation process that can be designed to separate the product gas 989a (e.g., H and CO) from the unreacted or partially reacted component gases. The separated product gases 989a can also be split from one another so that the different product gases can be directed to different locations (e.g., different storage vessels).

[0097] Modifications, additions, or omissions can be made to the system for synthesizing hydrogen gas and carbon monoxide without departing from the scope of the present disclosure. For example, the designations of different elements in the described manner are intended to help explain the concepts described herein and are not intended to be limiting. For example, in some embodiments, the precompressor unit 902, scrubber 904, air separator 906, PCCU (including plasma chamber 910, auxiliary reaction chamber 930, and / or integrated reformer 950), heat utilization unit 980, compressor 984, amine unit 986, and separator unit 988 may be depicted in a particular manner described to help explain the concepts described herein, but such depictions are not intended to be limiting. Furthermore, the system for synthesizing hydrogen gas and carbon monoxide can include any number of other elements or be implemented in systems or contexts other than those described.

[0098] FIG. 10 is a diagram of a plasma reaction system 1000 that converts biogas to hydrogen gas using a PCCU. The carbon dioxide utilization system can include a precompressor unit 1002 into which an input biogas 1001 can be input. The pressure increase of the input biogas 1001 can be facilitated by directing electrical power 881 from a heat utilization unit 1080 to the precompressor unit 1002. For example, the input biogas 1001 can be obtained by the precompressor unit 1002 at a pressure of 0.5 atm, 1 atm, 1.5 atm, 2 atm, or other pressure, and the biogas 1003 exiting the precompressor unit 1002 can be at a pressure of 2 atm, 3 atm, 5 atm, 10 atm, 20 atm, 100 atm, or other pressure. The pressurized biogas 1003 can be sent to a scrubber 1004 that can remove impurities, pollutants, or other harmful components of the biogas. For example, the scrubber 1004 may include a dry scrubbing process in which harmful substances (e.g., sulfur oxides, particulate matter, acid gases, etc.) are adsorbed onto a dry reagent contained in the scrubber 1004. As another example, the scrubber 1004 may include a wet scrubbing process in which the biogas is sprayed with a wet substance (e.g., water) to separate one or more components from the biogas 1003.

[0099] The air separator 1006 can receive an input air stream 1005 and separate the input air stream 1005 into its constituent components 1007a, 1007b, which may primarily include nitrogen gas 1007a and oxygen gas 1007b. The air separator 1006 can facilitate separation of the components contained in the input air stream 1005 via fractional distillation, pressure swing adsorption, vacuum pressure swing adsorption, membrane separation, or any other separation method. The separated air components 1007a, 1007b can be sent to a PCCU, which may include a plasma chamber 1010, an auxiliary reaction chamber 1030, and an integrated reformer 1050.

[0100] The plasma chamber 1010 may be made of quartz or a ceramic material, with one or more waveguides configured to facilitate chemical reactions occurring within the plasma chamber 1010. Fuel (e.g., hydrocarbons) and other input compounds heated by electricity or microwaves can react to provide additional heat to the input compounds in the plasma chamber 1010. The plasma chamber 1010 may be configured to obtain an inlet stream of separated air components 1007a, 1007b and cleaned biogas 1049a from the scrubber 1004. Oxygen gas obtained from the air separator 1006 and energy provided within the plasma chamber 1010 can facilitate the conversion of the cleaned biogas 1049a to syngas 1011.

[0101] The auxiliary reaction chamber 1030 can be configured to obtain the syngas 1011 from the plasma chamber 1010 and affect a chemical reaction between the inlet gas streams. For example, in the auxiliary reaction chamber 1030, the incoming cleaned biogas 1049b can react at an elevated temperature supplied by the heat generated by the plasma chamber 1010 (e.g., by an exothermic reaction) to form the syngas 1031 and excess heat, which can be sent to the integrated reformer 1050.

[0102] The integrated reformer 1050 can be a separate reaction unit connectable to the auxiliary reaction chamber 1030. The integrated reformer 1050 can include a steam methane reforming reactor (SMR) or any other reactor vessel configured to receive the scrubbed biogas 1049c from the scrubber 1004 and convert it to syngas 1051a using electrically or microwave-generated heat and chemical reaction heat (e.g., heat provided by the plasma chamber 1010 and / or the auxiliary reaction chamber 1030). Additionally or alternatively, the integrated reformer 1050 can be configured to receive a recycle stream of syngas 1089b from the PSA unit 1088 and / or a recycle stream of steam 1051b from the heat utilization unit 1080, where the recycle streams from the PSA unit 1088 and the heat utilization unit 1080 provide additional reactants to facilitate higher conversion of the biogas to syngas 1051a.

[0103] The syngas 1051a produced by the integrated reformer 1050 can be sent to a heat utilization unit 1080, which produces one or more cooled product gases 1051c derived from the syngas 1051a and 1083 derived from the syngas 1051e. The heat utilization unit 1080 can include a steam or power generation unit that can be configured to receive input streams of water 1079, the syngas 1051a produced by the integrated reformer 1050, and the syngas 1051e from a water-gas shifter (WGS). The heat utilization unit 1080 can use excess heat generated by the PCCU and input to the heat utilization unit 1080 by the incoming syngas 1051a stream from the integrated reformer 1050 to vaporize the input water 1079, and the produced steam 1051b can facilitate the conversion of biogas 1049c to a product gas (e.g., syngas 1051a). Additionally or alternatively, excess steam 1051b from the heat utilization unit 1080 can be sent to the integrated reformer 1050 to reclaim heat and promote further formation of syngas 1051a in the integrated reformer 1050.

[0104] The heat utilization unit 1080 can use excess heat generated by the PCCU and input to the heat utilization unit 1080 by the incoming syngas 1051a stream from the integrated reformer 1050 to vaporize water 1079, and the generated steam 1051d and syngas 1051c can be sent to a water gas shifter (WGS) 1082. Additionally or alternatively, excess steam 1051b from the heat utilization unit 1080 can be sent to the integrated reformer 1050 to reclaim the excess heat and drive the formation of syngas 1051a in the integrated reformer 1050.

[0105] A portion of the syngas 1051a sent from the integrated reformer 1050 to the heat utilization unit 1080 may be sent 1051c to the WGS 1082. The WGS 1082 may promote the formation of hydrogen gas via the water-gas shift reaction, in which carbon monoxide and water react reversibly to form carbon dioxide and hydrogen gas that is sent back to the heat utilization unit 1080 (1051e).

[0106] In these and other embodiments, the product gas 1083 (e.g., hydrogen gas produced in the WGS 1082) and unreacted or partially reacted materials can be sent from the heat utilization unit 1080 to a compressor 1084 that compresses the product gas (and any other input materials) and sends the pressurized product gas 1085 to the amine unit 1086. The increase in pressure of the product gas 1083 can be facilitated by power 1081 obtained from the heat utilization unit 1080. For example, the product gas 1083 can be obtained by the compressor at a pressure of 0.5 atm, 1 atm, 1.5 atm, 2 atm, or other pressure, and the compressed product gas 1085 (e.g., hydrogen gas and / or any other gas) exiting the compressor 1084 can be at a pressure of 2 atm, 3 atm, 5 atm, 10 atm, 20 atm, 100 atm, or other pressure.

[0107] The amine unit 1086 may contain various aqueous amine solutions that react with the pressurized product gas 1085 exiting the compressor 1084 to remove residual impurities (e.g., hydrogen sulfide, sulfur oxides, or any other harmful substances). Additionally or alternatively, the amines contained in the amine unit 1086 may facilitate the removal of acid gases such as carbon dioxide. The carbon dioxide 1091 removed by the amine unit 1086 may be sent to another reactor unit or treatment system, such as a carbon dioxide utilization system.

[0108] The product gas 1087a processed in the amine unit 1086 can be sent to a PSA unit 1088, which separates the various components of the product gas 1087a. For example, the PSA unit 1088 can separate the components contained in the product gas, and the PSA unit 1088 can include a membrane of adsorbent material that separates the gas components entering the PSA unit 1088 by filtering the compounds that pass through the membrane. Gases captured by the membrane can be desorbed from the adsorbent material by reducing the pressure within the PSA unit 1088, and the desorbed gases can be recycled to the PCCU (e.g., the integrated reformer 1050) for further reaction. Thus, partially reacted or unreacted gases that entered the separator unit with the product gas can be diverted in recycle stream 1089b to the integrated reformer 1050 to drive the chemical reactions associated with forming the syngas 1051a to further completion. Additionally or alternatively, the separated product gases may be split from one another so that different product gases 1089a may be directed to different locations (eg, different storage vessels).

[0109] Modifications, additions, or omissions can be made to the system for converting biogas to hydrogen gas without departing from the scope of the present disclosure. For example, the designations of different elements in the described manner are intended to help explain the concepts described herein and are not intended to be limiting. For example, in some embodiments, the precompressor unit 1002, scrubber 1004, air separator 1006, PCCU (including plasma chamber 1010, auxiliary reaction chamber 1030, and / or integrated reformer 1050), heat utilization unit 1080, WGS 1082, compressor 1084, amine unit 1086, and PSA unit 1088 are depicted in the particular manner described to help explain the concepts described herein, but such depictions are not intended to be limiting. Furthermore, the system for converting biogas to hydrogen gas can include any number of other elements or be implemented in systems or contexts other than those described.

[0110] FIG. 11 shows an example of an integrated reformer 1100. The integrated reformer 1100 can obtain one or more gaseous compounds from a plasma chamber. The gaseous compounds obtained from the plasma chamber can be heated to high temperatures due to exothermic reactions in the plasma chamber. As a result, excess heat from the plasma chamber can be transferred to the integrated reformer 1100 by the gaseous compounds output from the plasma chamber. In some embodiments, the integrated reformer 1100 can include an outer chamber and an inner reaction chamber, with the gaseous compounds flowing from the outer chamber into the inner reaction chamber. Additionally or alternatively, water and / or steam can be supplied to the integrated reformer 1100 so that the water and / or steam flows from the outer chamber into the inner reaction chamber or is supplied directly to the inner reaction chamber. The integrated reformer 1100 can output syngas or other gaseous products using an outlet 1124, which can be sent to one or more processing units for further processing of the gaseous products.

[0111] FIG. 11 shows a cross-sectional view of an example integrated reformer 1100. The integrated reformer 1100 can include an outer chamber 1102 and a reaction chamber 1104. The outer chamber 1102 can include a first inlet 1106 configured to receive a first gas stream (e.g., a gas stream including the heated second syngas stream from the auxiliary reaction chamber) and a second inlet 1108 configured to receive a second gas stream (e.g., a gas stream including a hydrocarbon fuel such as biogas, CH4, natural gas, or any combination thereof). The second gas stream can be from a heat utilization unit 1140 (e.g., a heat utilization unit similar to heat utilization units 880, 980, and 1080 of FIGS. 8, 9, and 10, respectively). The second gas stream can be heated or cooled to a predetermined temperature by the heat utilization unit 1140 before being directed to the outer chamber 1102.

[0112] The integrated reformer 1100 may provide a mixing and cooling zone 1110 within the outer chamber 1102 where the first and second gas streams can be mixed and cooled. To mix the first and second gas streams in the mixing and cooling zone 1110, a first end 1112 of a second inlet 1108 may extend through a wall of the outer chamber 1102 into the mixing and cooling zone 1110. The first end 1112 of the second inlet 1108 of the outer chamber 1102 may be bent so that the first end 1112 of the second inlet 1108 can be directed toward the first inlet 1106. The first and second gas streams may directly impinge on each other in the mixing and cooling zone 1110 for better mixing.

[0113] The first gas flow can be from the plasma chamber and / or the auxiliary reaction chamber, resulting in a first output flow (including the heated second syngas flow 635 from the auxiliary reaction chamber described in connection with FIG. 6). The first output flow from the plasma chamber (e.g., the first gas flow in FIG. 11) can have a high temperature (e.g., a temperature range between 1500° C. and 2500° C.) due to operation within the plasma chamber.

[0114] By mixing the first gas stream (hot) with a second gas stream (biogas in this example) that is at a relatively lower temperature than the first gas stream, the temperature of the mixture of the first and second gas streams can be lower than the temperature of the first gas stream. A cooling unit 1114 can be coupled to the outer chamber 1102 to efficiently cool the mixture of the first and second gas streams to a predetermined temperature or temperature range so that the temperature of the mixture of the first and second gas streams is within a range suitable for steam reforming (in the reaction chamber 1104 with steam) (e.g., between 700°C and 1000°C).

[0115] The integrated reformer 1100 may include a cooling unit 1114 disposed adjacent to the mixing and cooling zone 1110. The cooling unit 1114 may surround the mixing and cooling zone 1110. The cooling unit 1114 may include a tube 1116 (or pipe) disposed or wrapped around the outer chamber 1102 adjacent to the mixing and cooling zone 1110. The mixing and cooling zone 1110 may be located between the first inlet 1106 and the reaction chamber 1104.

[0116] The cooling unit 1114 may use water as a coolant to cool the mixture of the first gas stream and / or the second gas stream. For example, water may be supplied to a first end 1118 of a tube 1116 disposed around the outer chamber 1102. As the water flows through the tube 1116, it may absorb thermal energy (heat) from the mixture of the first gas stream and / or the second gas stream and become steam (e.g., water in a gaseous state).

[0117] The cooling unit 1114 can be configured to provide a flow to the reaction chamber 1104. A second end 1120 of the tube 1116 can be disposed within the reaction chamber 1104 adjacent to a mixed gas inlet 1122 of the reaction chamber 1104. The second end 1120 of the tube 1116 can be connected (or fluidly coupled) to the reaction chamber 1104 via the mixed gas inlet 1122 of the reaction chamber 1104.

[0118] The second end 1120 of the tube 1116 may be oriented opposite the mixed gas inlet 1122. A mixture of the first and second gas streams can be supplied to the reaction chamber 1104 through the mixed gas inlet 1122. Consequently, the mixture of the first and second gas streams can be mixed with steam in the reaction chamber 1104. Consequently, the reaction chamber 1104 can generate a third gas stream based on the first and second gas streams and steam using steam reforming. The reaction chamber 1104 may include an outlet 1124 for outputting the third gas stream (including syngas) generated by the integrated reformer 1100. The reaction chamber 1104 may include a catalyst 1126 to promote more reactions (e.g., catalytic processes) for syngas production. The catalyst may include a porous material or structure (e.g., a mesh, multiple tubes or pipes, a membrane). A catalyst 1126 can be positioned between the outlet 1124 and the mixed gas inlet 1122 so that the mixture of the first gas stream, the second gas stream, and steam from the cooling unit 1114 can efficiently pass through the catalyst 1126 for the catalytic process.

[0119] Modifications, additions, or omissions may be made to the integrated reformer 1100 without departing from the scope of the present disclosure. For example, the coolant in the cooling unit 1114 may be used to cool the mixture of the first gas stream and / or the second gas stream and steam from the heat utilization unit used in the steam reforming process. After cooling the mixture of the first gas stream and / or the second stream, the coolant may be condensed and reused in the cooling unit 1114.

[0120] FIG. 12 shows a flowchart of an example method 1200 of plasma carbon conversion. Method 1200 may be performed by any component, including one or more of a plasma chamber, an auxiliary reaction chamber, or an integrated reformer, or any other component or subcomponent. For ease of explanation, the methods described herein are shown and described as a series of operations. However, operations in accordance with the present disclosure may occur in various orders and / or simultaneously, and with other operations not shown and described herein. Furthermore, not all operations shown may be used to perform a method in accordance with the disclosed subject matter. Additionally, those skilled in the art will understand and appreciate that these methods may be represented as a series of interrelated states via state diagrams or events. While shown as individual blocks, various blocks may be divided into additional blocks, combined into fewer blocks, or eliminated depending on the implementation selected.

[0121] Method 1200 includes, in Operation 1205, sending a heated first syngas stream from the plasma chamber to an auxiliary reaction chamber. In Operation 1210, the method includes mixing the heated first syngas stream with a second gas stream in the auxiliary reaction chamber to initiate an exothermic reaction between the heated first syngas stream and the second gas stream (e.g., using first thermal energy from the heated first syngas stream). In Operation 1215, the method includes generating second thermal energy using the exothermic reaction in the auxiliary reaction chamber. In Operation 1220, the method includes sending the second thermal energy from the auxiliary reaction chamber to an integrated reformer. In Operation 1225, the method includes generating syngas in the integrated reformer using the second thermal energy. One or more of the second thermal energy or the syngas can be purified without external heat input. The method may include passing the third gas stream to an integrated reformer to produce synthesis gas.

[0122] The method 1200 may further include one or more of: (i) conducting one or more of a partial oxidation reaction, a dry methane reforming reaction, a steam methane reforming reaction, or a hydrocarbon cracking reaction in the plasma chamber; or (ii) conducting one or more of a partial oxidation reaction, a dry methane reforming reaction, or a steam methane reforming reaction in an auxiliary reaction chamber; or (iii) conducting one or more of a steam methane reforming reaction, a dry methane reforming reaction, a water gas shift reaction, a catalytic reaction, or a non-catalytic reaction in the integrated reformer.

[0123] The terms used in this disclosure, and particularly in the appended claims (e.g., the body of the appended claims), are generally intended as "open language" (e.g., the term "comprises" should be interpreted as "including, but not limited to").

[0124] Additionally, where a specific number of introduced claim recitations is intended, such intention will be explicitly stated in the claim; absent such recitation, no such intention exists. For example, to aid in understanding, the following appended claims may include the use of the introductory phrases "at least one" and "one or more" to introduce claim recitations. However, the use of such phrases should not be construed to mean that the introduction of a claim recitation with the indefinite article "a" or "an" limits a particular claim containing the introduced claim recitation to embodiments containing only one such recitation, even if the same claim includes the introductory phrases "one or more" or "at least one" and an indefinite article such as "a" or "an" (e.g., "a" and / or "an" should be construed to mean "at least one" or "one or more"); the same applies to the use of definite articles used to introduce claim recitations.

[0125] Additionally, even when a specific number of introduced claims is explicitly recited, those skilled in the art will recognize that such recitation should be interpreted to mean at least the recited number (e.g., the mere recitation of "two recitations" without other modifiers means at least two recitations, or more than two recitations). Furthermore, when conventions similar to "at least one of A, B, and C, etc." or "one or more of A, B, and C, etc." are used, it is generally intended that such configurations include A only, B only, C only, both A and B, both A and C, both B and C, or all of A, B, and C, etc.

[0126] Furthermore, a disjunctive word or phrase preceding two or more alternative terms, whether in the specification, claims, or drawings, should be understood to contemplate the possibility of including one of the terms, either of the terms, or both of the terms. For example, the phrase "A or B" should be understood to include the possibilities of "A" or "B" or "A and B."

[0127] All examples and conditional language set forth in this disclosure are intended for educational purposes to help the reader understand the disclosure and the concepts that the inventors have contributed to the development of the technology, and should not be construed as being limited to such specifically set forth examples and conditions. Although embodiments of the present disclosure have been described in detail, various changes, substitutions, and alterations can be made to the present disclosure without departing from the spirit and scope of the present disclosure.

Claims

1. 1. A plasma chamber comprising: receiving a first gas flow from a plasma chamber inlet; adding heat to the first gas stream to form a heated first synthesis gas stream; outputting the heated first synthesis gas stream to an auxiliary reaction chamber; a plasma chamber configured to A system comprising: The auxiliary reaction chamber comprises: receiving the heated first syngas stream from the plasma chamber; receiving a second gas flow from the auxiliary reaction chamber inlet; outputting the heated second syngas stream to an integrated reformer; It is structured as follows: the heated second syngas stream comprises the reaction product of the heated first syngas stream and the second syngas stream; The integrated reformer comprises: receiving the heated second synthesis gas stream from a first integrated reformer inlet; receiving a third gas stream from the second integrated reformer inlet; Outputting synthesis gas from the integrated reformer It is configured as follows: system.

2. The system of claim 1 , wherein the plasma chamber is further configured to add heat to the first gas flow using an exothermic reaction.

3. The system of claim 1 , wherein the plasma chamber is further configured to use heat to drive an endothermic reaction in the first gas stream.

4. The system of claim 1 , wherein the plasma chamber is configured to perform one or more of a partial oxidation reaction, a dry methane reforming reaction, a steam methane reforming reaction, or a hydrocarbon cracking reaction.

5. 10. The system of claim 1, wherein the auxiliary reaction chamber is further configured to use heat from the heated first syngas stream to initiate an exothermic reaction to produce the heated second syngas stream.

6. The system of claim 1 , wherein the auxiliary reaction chamber is further configured to perform one or more of a partial oxidation reaction, a dry methane reforming reaction, or a steam methane reforming reaction.

7. The system of claim 1 , wherein the integrated reformer is further configured to use heat from the heated second syngas stream to perform an endothermic reaction to produce the syngas.

8. 10. The system of claim 1, wherein the integrated reformer is further configured to perform one or more of a steam methane reforming reaction, a dry methane reforming reaction, a water gas shift reaction, a catalytic reaction, or a non-catalytic reaction.

9. The system of claim 1 , wherein the auxiliary reaction chamber is configured to receive one or more additional heated first syngas streams from one or more additional plasma chambers.

10. The system of claim 1 , wherein the integrated reformer is configured to receive one or more additional heated second syngas streams from one or more additional auxiliary reaction chambers.

11. The system of claim 10 , wherein the one or more additional heated second syngas streams are received at one or more additional integrated reformer inlets.

12. A device, a plasma chamber in fluid communication with the auxiliary reaction chamber; an integrated reformer in fluid communication with the auxiliary reaction chamber; It is equipped with the auxiliary reaction chamber is configured to use heat from the heated first syngas stream received from the plasma chamber to initiate an exothermic reaction with a second gas stream and output a heated second syngas stream to the integrated reformer; device.

13. 13. The device of claim 12, wherein the auxiliary reaction chamber is further configured to perform one or more of a partial oxidation reaction, a dry methane reforming reaction, or a steam methane reforming reaction.

14. 13. The device of claim 12, wherein the integrated reformer is further configured to use heat from the heated second syngas stream to perform an endothermic reaction to produce syngas.

15. The device of claim 12 , wherein the auxiliary reaction chamber is further configured to receive one or more additional heated first syngas streams from one or more additional plasma chambers.

16. 13. The device of claim 12, wherein the integrated reformer is further configured to receive one or more additional heated second syngas streams from one or more additional auxiliary reaction chambers.

17. 1. A method for plasma carbon conversion comprising: directing the heated first synthesis gas stream from the plasma chamber to an auxiliary reaction chamber; mixing the heated first synthesis gas stream with a second gas stream in the auxiliary reaction chamber to initiate an exothermic reaction between the heated first synthesis gas stream and the second gas stream; generating a second thermal energy in the auxiliary reaction chamber using the exothermic reaction; delivering the second thermal energy from the auxiliary reaction chamber to the integrated reformer; and generating synthesis gas in the integrated reformer using the second thermal energy; A method comprising:

18. the second thermal energy is generated without external heat input; or The synthesis gas is produced without external heat input.

18. The method of claim 17, wherein the first and second electrodes are one or more of:

19. directing a third gas stream to said integrated reformer to produce said synthesis gas; 20. The method of claim 17, further comprising:

20. conducting one or more of a partial oxidation reaction, a dry methane reforming reaction, a steam methane reforming reaction, or a hydrocarbon cracking reaction in the plasma chamber; or conducting one or more of a partial oxidation reaction, a dry methane reforming reaction, or a steam methane reforming reaction in the auxiliary reaction chamber; or In the integrated reformer, one or more of a steam methane reforming reaction, a dry methane reforming reaction, a water gas shift reaction, a catalytic reaction, or a non-catalytic reaction is performed.

20. The method of claim 17, further comprising one or more of:

Images