Reactor assembly and method for carrying out a reaction

Abstract

A reactor is provided that can include a first set of fluid channels and a second set of fluid channels oriented in thermal contact with the first set of fluid channels. Also provided is a reactor assembly in which one or both channels of the first set of fluid channels are nonlinear. Another embodiment provides at least one of the first set of fluid channels in thermal contact with a plurality of other channels of the second set of fluid channels. A reactor assembly is also provided that can include a first set of fluid channels defining at least one nonlinear channel having a positive function and a second set of fluid channels defining at least another nonlinear channel having a negative function related to the positive function of one nonlinear channel of the first set of fluid channels. A process for distributing energy throughout a reactor is provided. The process can include transporting reactants through the first set of fluid channels to the second set of fluid channels and thermally engaging at least one of the first set of fluid channels with at least two of the second set of fluid channels.

Description

[Technical Field]

[0001] This application claims priority to U.S. Patent Application Serial No. 16 / 359,909, filed March 20, 2019, entitled "Reactor Assemblies and Methods of Performing Reactions," the entire contents of which are incorporated herein by reference.

[0002] STATEMENT AS TO RIGHTS TO INVENTIONS MADE UNDER FEDERALLY SPONSORED RESEARCH AND DEVELOPMENT This invention was made with Government support under Contract DE-AC05-76RL01830 awarded by the U.S. Department of Energy. The Government has certain rights in this invention.

[0003] The present disclosure relates to a reactor assembly and a method for carrying out a reaction. Embodiments of the present disclosure have been related to carrying out an endothermic reaction. Embodiments of the present disclosure can also utilize solar energy or other heat sources to drive the endothermic reaction. [Background technology]

[0004] For hydrogen production, current commercial technologies include conventional steam methane reforming in systems that combust a portion of the product stream to drive the endothermic reaction, and water electrolysis, where the energy for the electrochemical reaction typically comes from the electrical grid. Solar thermochemical production of hydrogen from natural gas or other methane sources can offer the advantage of higher overall energy efficiency and reduced carbon emissions compared to conventional steam methane reforming and water electrolysis using grid electricity.

[0005] Reactor systems are designed for steam reforming of methane and other hydrocarbons using concentrated solar power. Reactor assemblies and methods are provided, including U.S. Patent No. 9,950,305, entitled "Solar Thermochemical Processing System and Method," issued April 24, 2018, and U.S. Patent Application Publication No. 15 / 950,068, entitled "Solar Thermochemical Processing System and Method," filed April 10, 2018, each of which is incorporated herein by reference in its entirety. Summary of the Invention

[0006] A reactor is provided that can include a first set of fluid channels and a second set of fluid channels oriented in thermal contact with the first set of fluid channels, wherein the channels of one or both sets of fluid channels can be nonlinear.

[0007] Also provided is a stacked reactor assembly that can include first and second sets of fluid channels in a stacked configuration, where the fluid channels are oriented in thermal contact with each other and at least one of the first set of fluid channels is in thermal contact with another channel of the second set of fluid channels.

[0008] Also provided is a reactor assembly that can include a first set of fluid channels defining at least one nonlinear channel having a shape defined by a positive mathematical function, and a second set of fluid channels defining at least another nonlinear channel having a shape defined by a negative mathematical function related to the positive mathematical function of one nonlinear channel of the first set of fluid channels.

[0009] A process for distributing energy throughout a reactor is provided, which can include transporting reactants through a first set of fluid channels to a second set of fluid channels, and thermally engaging at least one of the first set of fluid channels with at least two of the second set of fluid channels.

[0010] Embodiments of the present disclosure can utilize thermal energy to facilitate or drive endothermic reactions in at least one of the set of fluid channels. In certain embodiments, channel heat can be provided from a variety of sources, including electrical heating, exothermic chemical processes, and / or solar energy. The reactor and / or method can accommodate high-temperature endothermic reactions such as methane steam reforming or reverse water gas shift where the heat of reaction is provided primarily by solar energy. The reactor and / or method of the present disclosure finds application in syngas generation, which can be a precursor to the production of many chemicals, including hydrogen, which can be useful in refineries, fuel cells, including fuel cell vehicles, and other chemical processing applications.

[0011] The disclosed reactor assembly and / or method can have two sets of spiral-shaped fluid channels separated by a thin member and arranged in opposite spiral directions to form a cross-flow pattern, a counter-flow pattern, or a counter-cross-flow pattern. Each set can be an array of repeating nonlinear units defining one or more channels of a spiral flow path. The axes of symmetry of the two channel groups can coincide at a hub. The repeating units of each fluid channel can be the same or different, although according to exemplary embodiments, the repeating units can be different. The nonlinear fluid channels forming the repeating units of the array can be derived from a general curve of helical nature, which can be either planar or three-dimensional. Many types of helical curves can be used, but Archimedean spirals and logarithmic spirals and their three-dimensional derivatives are particularly relevant.

[0012] The integration of nonlinear fluid channels and / or nonlinear counterflow or countercrossflow channels can provide two advantages that lead to performance and economic benefits. First, this combination can provide heat diffusion, which, as explained below, reduces the severity of hot spots and thermal stresses, warms cold spots, and improves reactor life. Second, this combination can enable the recovery of thermal energy (sensible heat) from the product stream to provide additional heat for the reaction. This can lower the amount of solar energy required for a given amount of reaction, thus making the reactor system more efficient, more productive, and less costly.

[0013] Embodiments of the present disclosure are described below with reference to the accompanying drawings, in which: [Brief explanation of the drawings]

[0014] [Figure 1] FIG. 1 is a cross-sectional view of a reactor assembly according to an embodiment of the present disclosure. [Figure 2] FIG. 1 is a diagram of a set of channels of a reactor assembly according to an embodiment of the present disclosure. [Figure 3] 1 shows two sets of reactor channels in a stacked configuration according to an embodiment of the present disclosure. [Figure 4] 1 shows two sets of reactor channels in a stacked configuration according to an embodiment of the present disclosure. [Figure 5A] 1A and 1B are partial and overall configurations of a reactor assembly according to an embodiment of the present disclosure. [Figure 5B] 1A and 1B are partial and overall configurations of a reactor assembly according to an embodiment of the present disclosure. [Figure 5C] 1A and 1B are partial and overall configurations of a reactor assembly according to an embodiment of the present disclosure. [Figure 5D] 1A and 1B are partial and overall configurations of a reactor assembly according to an embodiment of the present disclosure. [Figure 6]FIG. 1 is a diagram of the overall configuration and reactor within the (r, θ) coordinate range, according to an embodiment of the present disclosure. [Figure 7A] 1 is a depiction of a reactor shown with portions cut away according to an embodiment of the present disclosure. [Figure 7B] 1 is a depiction of a reactor in which one fluid channel in a first set of fluid channels is shown in thermal contact with multiple fluid channels in a second set of fluid channels. [Figure 8] FIG. 1 is a schematic diagram of a reaction according to an embodiment of the present disclosure. [Figure 9] 1 is a depiction of heat flux distribution data according to an embodiment of the present disclosure. [Figure 10A] 1 is a depiction of thermal and stress distribution data according to an embodiment of the present disclosure. [Figure 10B] 1 is a depiction of thermal and stress distribution data according to an embodiment of the present disclosure. [Figure 10C] 1 is a depiction of thermal and stress distribution data according to an embodiment of the present disclosure. [Figure 11A] 1 is a depiction of thermal and stress distribution data according to an embodiment of the present disclosure. [Figure 11B] 1 is a depiction of thermal and stress distribution data according to an embodiment of the present disclosure. [Figure 11C] 1 is a depiction of thermal and stress distribution data according to an embodiment of the present disclosure. [Figure 12] 1 is reaction data according to an embodiment of the present disclosure. [Figure 13] 1 is reaction data according to an embodiment of the present disclosure. DETAILED DESCRIPTION OF THE INVENTION

[0015] In the case of actual solar concentrators, it is recognized that hot spots can exist on the surface of the reactor due to imperfections in the solar concentrator's optics. Hot spots, or localized areas of high solar flux, can limit the maximum total operating flux due to metallurgical limitations of the reactor. Hot spots or other temperature gradients can also induce significant thermal stresses in the reactor, potentially shortening its overall thermal cycle life due to low cycle fatigue. Therefore, temperature differences associated with temperature gradients can lead to high operating and / or capital costs and failures of the reactor system, causing a shortened lifespan.

[0016] The present disclosure will be described with reference to Figures 1-13. Referring initially to Figure 1, a reactor 10 is shown according to one cross-section including a first set of fluid channels 12 in a stacked configuration atop a second set of fluid channels 14. These fluid channels can be in thermal contact with one another via a member 16. According to an exemplary embodiment, one or both of these sets of channels can include nonlinear fluid channels. According to other embodiments, one of the channels in the first set of fluid channels can be in thermal contact with multiple other channels in the second set of fluid channels. As shown in Figure 1, the reactor 10 can include a flow of reactants into the first set of fluid channels, across the length of the member 16, then through a fluid passage to the second set of fluid channels 14, and then exiting the reactor after traversing the member 16.

[0017] Referring now to FIG. 2, an example of a nonlinear channel 20 is shown. The nonlinear channel 20 can diverge from the hub 22 to the edge 24 of the reactor, and the nonlinear channel 20 can have a dividing member 28 therein. The nonlinear channel 20 in combination with the dividing member 28 can form, for example, a pair of fluid passages 30. The channel can be a microchannel or a mesochannel. A microchannel can be of any length and have one dimension, e.g., a width, in the general direction of bulk flow, typically in the direction of heat and / or mass transfer, greater than one micron and less than one millimeter. A mesochannel can be of any length and have one dimension, e.g., a width, in the general direction of bulk flow, typically in the direction of heat and / or mass transfer, greater than one millimeter and less than one centimeter.

[0018] Referring now to FIG. 3, according to one exemplary embodiment of the present disclosure, one set of fluid channels, nonlinear channels 20, can be associated with another set of linear fluid channels 26, which may be stacked on top of each other according to an exemplary implementation.

[0019] Referring now to FIG. 4, a pair of nonlinear channels 20 and 40 are shown according to one configuration, with fluid channels 20 and 40 in fluid communication at 42. As shown, both channels 20 and 40 are nonlinear. As shown in FIGS. 5A-5D, nonlinear channels 20 and 40 can be associated to form at least a portion of a reactor assembly 50, with these channels diverging from hub 22 and extending to edge 24 of assembly 50. Within each of these channels, there can be a dividing member 58. Dividing member 58 can extend toward edge 24 to form a pair of fluid conduits. According to an exemplary embodiment, there can be multiple nonlinear channels 52, as well as multiple nonlinear channels 54, which can form part of, or in the case of FIG. 5D, all of, reactor 50. According to an exemplary embodiment, this can be considered a spiral channel design.

[0020] 6, there is shown a set of nonlinear channels emanating from the reactor hub 22 to the edge 24. These channels are shown aligned along an exemplary polar coordinate system 110, where the shape of nonlinear channel 60 can be viewed as having a positive mathematical function with respect to the coordinate system, while the shape of nonlinear channel 80 can be viewed as having a negative mathematical function with respect to the coordinate system.

[0021] The mathematical function defining the shape and direction of a channel can be expressed by the general formula θ=f(r), where f is any function defining a particular curvature, with reference to a polar coordinate system 110 having coordinates (r, θ) in FIG. 6. For example, the Archimedes spiral and similar curves are expressed by θ=((rb) / a) c The logarithmic spiral curve is given by θ = (1nr - 1na) / b. The line is given by θ = d, where a, b, c, and d are arbitrary constant parameters. For a set of nonlinear channels 60 described by a positive function θ = f(r) with respect to a polar coordinate system 110, the corresponding set of channels 80 can be described by an associated negative function defined by θ = -f(r). More generally, one set of nonlinear channels can be defined by a positive function θ = f(r) and another set of nonlinear channels can be defined by a negative function θ = -f(r), where the mathematical functions f and f may or may not be identical. Furthermore, the mathematical function describing the shape of the nonlinear channels may essentially be a three-dimensional space curve; in this case, a general function θ = f(r,z) referenced to a cylindrical coordinate system (r,θ,z) can replace θ = f(r) in the ongoing discussion without loss of generality.

[0022] According to an exemplary embodiment, the nonlinear mathematical functions of the geometry of fluid channels 60 and 80, when taken as absolute values, may be equal to each other, thereby having mirror images of each other. According to other embodiments, the fluid channels may not be mirror images of each other, but may still be configured as inverse spirals. According to an exemplary embodiment, a reactor may include multiple nonlinear fluid channels with the same positive function and multiple nonlinear channels with the same negative function. A reactor may include an entire set of nonlinear channels with positive functions and another set of nonlinear channels with negative functions. According to an exemplary embodiment, and referring to FIG. 7A , a reactor 200 is shown including an inlet 202 and an outlet 204. Reactor 200 may include, for example, a first set of fluid channels 212 and a second set of fluid channels 214, connected by a fluid passage 230. Apart from passage 230, there may be a member 216 between the sets of fluid channels 214 and 212. This may be a thermally conductive member that may also form the ceiling of the first set of fluid members 212 and the floor of the second set of fluid channels 214. According to an exemplary embodiment, at least a portion of channels 212 may be provided with a catalyst, for example, to facilitate a desired reaction. The catalyst may be packed into either or both sets of channels, for example, in the form of a foam, felt, grid, or particles. The catalyst may also be coated on the channel walls, including the portion of member 216 that forms the floor of one set of channels and the ceiling of the other set.

[0023] According to an exemplary embodiment, a foam-supported catalyst may be provided in one set of channels 212. According to an exemplary embodiment, and with respect to the individual fluid channels 212 of one set, the individual fluid channels of reactor 200 may have as many thermal connections, as shown as multiple contacts at 206, as two, if not fourteen, individual channels 214 of the other set.

[0024] This process transports reactants through a first set of fluid channels and extracts products from a second set of fluid channels, e.g., as shown in FIG. 7A, at least one of the first set of fluid channels can be thermally coupled with at least two of the second set of fluid channels. According to an exemplary embodiment, an endothermic reaction can be provided in one of these sets of fluid channels; for example, as shown in FIG. 8, fluid channel 212 can be provided and can have potentially endothermic reactants necessary to promote an endothermic reaction with solar energy. According to an exemplary embodiment, the reactor of FIG. 7A has a portion (below a surface or portion) not shown that can be exposed to solar energy to provide energy to promote or drive this endothermic reaction. According to another embodiment, as the reaction proceeds through the reactor and heated products return through set of fluid channels 214, the heat of these products is transferred to the endothermic reaction in channel 212 via member 216.

[0025] Embodiments of the present disclosure can utilize most metals as materials of construction, including Ni, Cu, stainless steel alloys, Ti, Ti alloys, superalloys such as Inconel, Hastelloy and Haynes alloys, and combinations thereof. Ceramics may also be useful.

[0026] The dividing members 216 between sets of channels can have flat, concave, or convex profiles. The dividing members can be of any thickness necessary to support the structure of the channels and provide a thermal conduction path. According to an exemplary embodiment, the dividing members can have a thickness between 0.1 and 3.2 mm. The dividing members can be impermeable solids.

[0027] The height of the individual channels within each set can be less than 100 microns (0.1 millimeters) or greater than 1 centimeter, however, in embodiments in which a solid catalyst is used, the channel height is preferably greater than 1 mm, and even more preferably greater than 5 mm, to provide sufficient catalyst material to support the reaction.

[0028] 8, a schematic diagram for producing reactants and receiving products from a reactor of the present disclosure is shown. Thus, a process for distributing energy throughout a reactor, such as the reactors herein, is provided.

[0029] In a specific embodiment, and referring to FIG. 7A , a feed gas mixture of methane and steam enters the reactor 200 at a hub inlet 202 and is distributed to a set of identical channels 212 with nonlinear sidewalls. The channels traverse approximately one reactor radius and can change direction by more than 90 degrees from beginning to end. Within each channel resides a catalyst. This catalytic media can take the form of a foam that conforms to the shape of the channel, but can also include a substrate, such as particles, maintained within the channel. Each reaction channel can branch a short distance from the center, allowing the catalytic media insert to be sufficiently wide near the hub.

[0030] Near the edge of the reactor where the channels terminate, slot-shaped openings connect the channels to a second set of channels that curve in the opposite direction from the first set of channels. The second set of channels 214 may be referred to as heat recovery channels, while the first set of channels may be referred to as reaction channels. The reaction and heat recovery channels are separated by a solid intermediate member 216 that allows heat transfer by conduction. A slot-shaped opening 230 penetrates the intermediate member, allowing the reaction product stream from the reaction channel to enter the heat recovery channel. Once the product stream is returned to the center by the heat recovery channel, it exits the reactor through the annular space 204 between the inlet and outlet connecting pipes. Like the reaction channels, the heat recovery channels may also be bifurcated.

[0031] The spiral counter-crossflow pattern of this reactor is clearly shown in Figures 5D and 7A, where a three-dimensional model of the reactor is rendered in wireframe style. The reactor structure can alternatively be described by a repeating sequence of a single flow channel in a circular pattern, as shown in isometric views in Figures 4-5D. 1. Start with one spiral heat recovery channel, i.e., half of the flow path. 2. Add one reaction channel of the opposite helical direction. 3. The reaction channel and the heat recovery channel are connected by a slot opening between them near the periphery of the reactor. The reaction channel is shown without catalyst and with a portion of its top wall removed for clarity. 4. Repeat the heat recovery channels in a circular pattern. 5. Repeat the reaction recovery channel in a circular pattern. 6. Complete the pattern into a full circle, creating one group of spiral reaction channels and one group of heat recovery channels in the opposite spiral, arranged in counterflow.

[0032] The reaction flow and non-uniform solar flux distribution under steam methane reforming conditions of embodiments of the present reactor assembly and method can be simulated to understand the impact of reactor geometry and channel configuration on temperature and thermomechanical stress distribution.

[0033] In one embodiment, the reactor provides heat diffusion across a large reactor area and multiple channels. The nonlinear rotation can be more than a quarter of a full circle. In one embodiment incorporating counter-cross flow, the two sets of channels can occupy a significant area of ​​the reactor, thus providing substantial heat diffusion from the hot zone to the cold zone using fluid.

[0034] Each feed stream flowing through channel 212 is in thermal contact with multiple product streams in counterflow channel 214 via dividing member 216, with the flow paths of the latter group of streams occupying approximately one-fifth of the total area between the two sets of flow channels. Referring to FIG. 7B, the red area is occupied by the feed stream in one channel. The yellow area is the portion of the flow paths of all product streams flowing across said feed stream. The yellow area therefore represents the degree of heat diffusion imparted to each single channel. This area is 18% of the total area between the hub and edge.

[0035] The counter-crossflow arrangement of the reaction and recovery channels can efficiently spread the heat of non-uniform solar irradiation to a substantially greater extent than is achieved by direct heat conduction through the metal layer. The reduction of hot spots leads to reduced operational and capital costs due to improved reactor operability under high flux conditions, and extended reactor life due to reduced thermal stress.

[0036] The solar flux distribution on the reactor surface can be estimated from the lunar flux distribution obtained in previous experiments through mapping exercises in which a parabolic dish was pointed at the full moon. The results are shown in Figure 9 in W / m 2 The flux distribution is shown in Figure 10A-10C and Figures 11A-11C, respectively. The flux distribution was specified as a boundary condition at the front of the reactor in the simulation model. A reactor with a nonlinear channel according to the present disclosure and a previous design of a radial countercurrent linear channel with otherwise similar reactor and channel dimensions were simulated for comparison. The linear and nonlinear reactor models are shown in Figures 10A-10C and 11A-11C, respectively.

[0037] The reactor surface temperature distribution under a typical set of high solar flux conditions (9.6 kW total incident solar power, >80% methane conversion, 0.032 mol / s methane flow rate, and a steam-to-carbon ratio of 3) is shown in Figures 10B and 11B for the linear and nonlinear reactors, respectively. For the nonlinear spiral counter-crossflow reactor, the maximum surface temperature was found to be 988 °C, a decrease of more than 100 °C from the maximum surface temperature of 1114 °C for the linear reactor. Visually, the high-temperature region on the surface of the nonlinear reactor is more uniformly spread than in the linear reactor. The superior heat diffusion by the nonlinear reactor is attributed to the intersection of any reaction channel under the hot spot with multiple recovery channels downstream of the hot spot, resulting in a larger amount of received heat that then diffuses to other channels rather than returning to the same channel. Conceptually, heat diffusion in a linear reactor can be limited to the area of ​​one wedge-shaped reaction channel, or approximately 5% of the total surface area. The heat diffusion in the nonlinear reactor covers at least the area enclosed by the reaction channel and the connected heat recovery channel, or up to about 18% of the total surface area.

[0038] The von Mises stress in psi is shown for the linear and nonlinear reactors, respectively, in Figures 10C and 11C. The nonlinear reactor exhibits a lower maximum stress than the linear reactor. This difference may be due to heat diffusion and the resulting reduction in thermomechanical stress.

[0039] One embodiment of the present disclosure was tested in a solar thermochemical reaction system consisting of a parabolic dish-type solar concentrator, an Onsun reactor unit located at the focus of the dish, and a balance of the plant located on the ground. The reactor system configuration is shown in Figure 8. The Onsun reactor unit included a steam methane reforming reactor, a regenerative heat exchanger, a water vaporizer, and an onboard process controller. The feed gas system, water pump, process analyzer, and tail gas flare were located on the ground. The feed gas was controlled using a mass flow controller. The methane stream was preheated using a network of recuperative heat exchangers using the product stream. Concentrated solar energy was absorbed by the reforming reactor to catalytically convert methane to syngas. The syngas product stream was cooled using the feed gas stream and additional air cooling. The product gas composition was analyzed using a process gas chromatograph. After condensed water was separated, the product stream was discharged through a flare.

[0040] A nonlinear reactor, designated TRL6, was fabricated according to the design described in the previous section. In this particular embodiment of the present disclosure, the reactor was fabricated by machining individual plates and diffusion bonding a stack of plates. The reactor was 14.85 m 2 It was paired with an Infinia PowerDish III parabolic dish concentrator with a nominal mirror area of ​​1.0 and tested under moderate to high solar flux conditions. A linear reactor with otherwise similar reactor and channel dimensions, called TRL5, was also fabricated and tested at Onsun using a dish concentrator with the same specifications.

[0041] Referring to Figures 12 and 13, reactor performance was evaluated by energy conversion efficiency at both the reaction system level, i.e., the reactor and its heat exchanger network and dish concentrator, and the reactor component level, i.e., the reactor itself. The system's energy efficiency for solar chemistry is defined as the ratio of the difference in the higher heating value between the reactor product stream and the feed stream to the direct solar radiation (DNI), which is the incident energy on the dish concentrator reflector, and therefore includes effects due to reflectance, receiver intercept, heat losses around the reactor receiver, and approach to equilibrium chemical conversion within the reactor. System energy efficiency for solar chemistry data from the on-sun test is shown in Figure 12.

[0042] In the TRL6 reactor system, the system's energy efficiency for solar chemistry reached 60% to 70%. This reactor system was able to consistently achieve high efficiency under moderate to very high flux conditions. The excellent heat diffusion capability of the nonlinear reactor design allowed the reaction channel to reach higher temperatures when the reactor was operated at the same surface temperature limit. The higher thermodynamic efficiency of endothermic reactions at high temperatures is thought to be able to compensate for the additional lost radiative heat, and therefore the overall high solar chemistry conversion efficiency of the TRL6 reactor could extend into the high flux region.

[0043] In comparison, without enhanced heat dissipation, the TRL5 reactor system did not operate at the same high solar flux as the nonlinear reactor system due to surface temperatures exceeding the design point. In the low to moderate solar flux range, the nonlinear reactor system also outperformed the linear reactor in terms of energy efficiency for solar chemistry.

[0044] The performance advantages of nonlinear reactors become even more apparent when examining the reactor's energy efficiency. The reactor's thermal-to-chemical efficiency is defined as the ratio of the difference in the higher heating value between the reactor product stream and the feed stream to the amount of concentrated solar thermal energy received by the reactor, and therefore includes the effects of ambient heat losses to the reactor and receiver, as well as the extent of chemical conversion within the reactor. Reactor thermal-to-chemical efficiency data from the OnSun test are shown in Figure 13.

[0045] The TRL5 reactor achieved a heat-to-chemistry energy efficiency of 60%-70%, but was limited to low-to-moderate flux operation due to hot spot issues and temperature limitations of the reactor materials. With the TRL6 reactor, a heat-to-chemistry energy conversion efficiency of as much as 85% was achieved in the high flux regime. Some data points even suggest that performance levels approaching 90% may be possible. The nonlinear reactor's superior energy efficiency performance is attributed to its greater heat spreading capacity.

[0046] An exergy analysis was conducted based on the TRL6 reactor's on-site performance data. The objectives were to evaluate the second-law efficiency of the reactor and heat exchanger and to identify the cause and magnitude of exergy destruction. The exergy analysis estimated exergy destruction at the reactor front by estimating the surface temperature at an average value based on IR thermography measurements. The reference environment was selected as 25°C and 1 atm pressure with the chemical composition proposed by Szargut et al. The exergy efficiency of the TRL6 reactor was determined to be greater than 90%. For example, when tested under conditions of a methane feed rate of 0.048 mol / s, a steam-to-carbon ratio of 2.2, a concentrated solar power input of 10.88 kW, and an average reactor surface temperature of 820°C, the reactor rate of exergy destruction was estimated to be 5.34 kW, and the reactor's exergy efficiency was 90.2%.

Claims

1. 1. A reactor assembly comprising: a fluid inlet, a fluid outlet, and an edge; a first set of fluid channels in fluid communication with the fluid inlet; a second set of fluid channels in fluid communication with the first set of fluid channels and the fluid outlet, the second set of fluid channels oriented in thermal contact with the first set of fluid channels; Including, the fluid channels of either the first or second set of fluid channels have a curved shape; the fluid inlet and the fluid outlet are provided on a hub, and each of the sets of fluid channels diverges from the hub and extends to an edge of the reactor assembly; The reactor assembly, wherein each fluid channel of the first set of fluid channels is in fluid communication with each fluid channel of the second set of fluid channels at the edge of the reactor assembly.

2. 10. The reactor assembly of claim 1, wherein said first set of fluid channels are fluid channels having at least one dimension in the range of 1 μm to 1 mm.

3. 10. The reactor assembly of claim 1, wherein both the first and second sets of fluid channels are curved in shape.

4. A reactor assembly as described in claim 1, wherein the set of fluid channels have a coincident axis of symmetry at the hub.

5. 10. The reactor assembly of claim 1, wherein said curved shape means a spiral shape.

6. each fluid channel of the first or second set of fluid channels includes a dividing member; The reactor assembly of claim 1 , wherein the dividing member extends to form a pair of fluid passageways.

7. 7. The reactor assembly of claim 6, wherein individual fluid channels of both said first and second sets of fluid channels include dividing members.

8. 10. The reactor assembly of claim 1, wherein the other of said first or second sets of fluid channels is linear, wherein said linear means that said fluid channel does not include non-linear sidewalls.

9. 10. The reactor assembly of claim 1, The reactor assembly, wherein the first set of fluid channels and the second set of fluid channels curve in opposite directions.

10. 10. A process for distributing energy throughout a reactor assembly as recited in claim 1, comprising: transporting a reactant through the first set of fluidic channels to the second set of fluidic channels; and thermally engaging at least one of the first set of fluid channels with at least two of the second set of fluid channels; Including, The process further comprising carrying out an endothermic reaction within one of the sets of fluid channels, and further comprising facilitating the endothermic reaction with solar energy.

11. A reactor assembly as described in claim 1, wherein the curved shape is two-dimensional or three-dimensional.

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