Reactor assembly and method for carrying out the reaction

Abstract

This invention provides a reactor assembly and method for distributing energy throughout the entire reactor. [Solution] A reactor is provided, comprising a first set of fluid channels and a second set of fluid channels oriented to be in thermal contact with the first set of fluid channels, 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, and the channels of either the first or second set of fluid channels are nonlinear.

Description

Technical Field

[0001] This application claims priority to U.S. Patent Application Serial No. 16 / 359,909, filed on March 20, 2019, entitled "Reactor Assemblies and Methods of Performing Reactions", which is hereby incorporated by reference in its entirety.

[0002] Statement Regarding Rights to Inventions Made Under Federally Sponsored Research and Development This invention was made with government support under Contract No. DE-AC05-76RL01830 awarded by the U.S. Department of Energy (DOE). The government has certain rights in this invention.

[0003] This disclosure relates to reactor assemblies and methods for performing reactions. Embodiments of the disclosure are related to the performance of exothermic reactions. Embodiments of the disclosure can also utilize solar energy or other heat sources to drive exothermic reactions.

Background Art

[0004] In the case of hydrogen production, current commercial technologies include conventional steam methane reforming in systems that burn a portion of the product stream to promote an exothermic reaction, and electrolysis of water 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 have the advantage of higher overall energy efficiency and reduced carbon emissions compared to conventional steam methane reforming and electrolysis of water using grid electricity.

[0005] The reactor system is designed to steam reform methane and other hydrocarbons using concentrated solar photovoltaic power. Reactor assemblies and methods are provided, including U.S. Patent No. 9,950,305, entitled "Solar Thermochemical Processing System and Method," issued on April 24, 2018, and U.S. Patent Application Publication No. 15 / 950,068, entitled "Solar Thermochemical Processing System and Method," filed on April 10, 2018, each incorporated herein by reference in its entirety. [Overview of the project]

[0006] A reactor is provided which may include a first set of fluid channels and a second set of fluid channels oriented to be in thermal contact with the first set of fluid channels. The channels of one or both sets of fluid channels may be nonlinear.

[0007] Also provided is a stacked reactor assembly which may include first and second sets of fluid channels in a stacked configuration, wherein the fluid channels are oriented to be in thermal contact with each other, and at least one of the first set of fluid channels is in thermal contact with the other channels of the second set of multiple fluid channels.

[0008] A reactor assembly is also provided which may 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 of the nonlinear channels in the first set of fluid channels.

[0009] A process is provided for distributing energy throughout the reactor. The process may 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 promote or drive an endothermic reaction in at least one of a set of fluid channels. In certain embodiments, the heat in the channels can be supplied from a variety of sources, including electric heating, exothermic chemical processes, and / or solar energy. The reactor and / or method can provide high-temperature endothermic reactions such as methane steam reforming or reverse water-gas shift, where the reaction heat is supplied primarily by solar energy. The reactor and / or method of the present disclosure has applications in synthesis gas production, which can be a precursor to the production of many chemicals, including hydrogen, which may be useful in refineries, fuel cells including fuel cell vehicles, and other chemical processing applications.

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

[0012] The integration of nonlinear fluid channels and / or nonlinear counterflow or nonlinear countercrossflow channels can offer two advantages, leading to performance and economic benefits. Firstly, this combination can provide heat diffusion, which, as described below, reduces the severity of hot spots and thermal stress, warms cold spots, and improves reactor life. Secondly, this combination can provide additional heat to the reaction by enabling the recovery of thermal energy (sensible heat) from the product stream. This can reduce the amount of solar energy required for a given amount of reaction, thus making the reactor system more efficient, more productive, and less expensive.

[0013] Embodiments of this disclosure are described below with reference to the following attached drawings. [Brief explanation of the drawing]

[0014] [Figure 1] This is a cross-sectional view of a reactor assembly according to an embodiment of the present disclosure. [Figure 2] This is a diagram of the set of channels in a reactor assembly according to an embodiment of the present disclosure. [Figure 3] This embodiment of the disclosure shows two sets of reactor channels in a stacked configuration. [Figure 4] This embodiment of the disclosure shows two sets of reactor channels in a stacked configuration. [Figure 5A] This shows some and all of the configuration of a reactor assembly according to embodiments of the present disclosure. [Figure 5B] This shows some and all of the configuration of a reactor assembly according to embodiments of the present disclosure. [Figure 5C] This shows some and all of the configuration of a reactor assembly according to embodiments of the present disclosure. [Figure 5D] This shows some and all of the configuration of a reactor assembly according to embodiments of the present disclosure. [Figure 6]It is a diagram of the configuration within the range of (r,θ) coordinates and the entire reactor according to an embodiment of the present disclosure. [Figure 7A] It is a depiction of a reactor shown in a state where some parts are cut away according to an embodiment of the present disclosure. [Figure 7B] It is a depiction of a reactor shown in a state where one fluid channel in the first set of fluid channels is in thermal contact with a plurality of fluid channels in the second set of fluid channels. [Figure 8] It is a schematic diagram of a reaction according to an embodiment of the present disclosure. [Figure 9] It is a depiction of heat flux distribution data according to an embodiment of the present disclosure. [Figure 10A] It is a depiction of heat and stress distribution data according to an embodiment of the present disclosure. [Figure 10B] It is a depiction of heat and stress distribution data according to an embodiment of the present disclosure. [Figure 10C] It is a depiction of heat and stress distribution data according to an embodiment of the present disclosure. [Figure 11A] It is a depiction of heat and stress distribution data according to an embodiment of the present disclosure. [Figure 11B] It is a depiction of heat and stress distribution data according to an embodiment of the present disclosure. [Figure 11C] It is a depiction of heat and stress distribution data according to an embodiment of the present disclosure. [Figure 12] It is reaction data according to an embodiment of the present disclosure. [Figure 13] It is reaction data according to an embodiment of the present disclosure.

Mode for Carrying Out the Invention

[0015] In actual solar concentrators, it is recognized that defects in the solar concentrator's optics can lead to the presence of hot spots on the reactor surface. Hot spots, or localized areas of high solar flux, can limit the maximum total operating flux due to the reactor's metallurgical limitations. Hot spots or other temperature gradients can also induce significant thermal stress in the reactor, potentially shortening the 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 in the reactor system, resulting in a reduced lifespan.

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

[0017] Referring next to Figure 2, an example of a nonlinear channel 20 is shown. The nonlinear channel 20 can diverge from the hub 22 of the reactor to the edge 24, and the nonlinear channel 20 may have a dividing member 28 within it. The nonlinear channel 20 combined 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 in the general direction of bulk flow, is one-dimensional, for example, has a width, is typically in the direction of heat and / or mass transfer, and is between 1 micron and 1 millimeter. A mesochannel can be of any length in the general direction of bulk flow, is one-dimensional, for example, has a width, is typically in the direction of heat and / or mass transfer, is greater than 1 millimeter and less than 1 centimeter.

[0018] Referring next to Figure 3, according to one exemplary embodiment of the present disclosure, one set of nonlinear channels 20 of fluid channels can be associated with another set of linear fluid channels 26, and these channels may be stacked on top of each other according to the exemplary embodiment.

[0019] Next, referring to Figure 4, a pair of nonlinear channels 20 and 40 are shown according to one configuration, with fluid communication at 42 of the fluid channels 20 and 40. As shown, both channels 20 and 40 are nonlinear. As shown in Figures 5A to 5D, the nonlinear channels 20 and 40 can be associated to form at least a portion of a reactor assembly 50 having these channels that diverge from the hub 22 and extend to the edge 24 of the assembly 50. Within each of these channels, there may be a split member 58. The split member 58 can extend toward the edge 24 to form a pair of fluid conduits. According to an exemplary embodiment, there may be a plurality of nonlinear channels 52, as well as a plurality of nonlinear channels 54, which can form a portion, or all, of the reactor 50 in the case of Figure 5D. According to an exemplary embodiment, this can be considered a helical channel design.

[0020] Referring next to Figure 6, a set of nonlinear channels originating from the reactor hub 22 to the edge 24 is shown. These channels are shown aligned along an exemplary polar coordinate system 110, and the shape of the nonlinear channel 60 can be considered to have a positive mathematical function with respect to the coordinate system, while the shape of the nonlinear channel 80 can be considered to have a negative mathematical function with respect to the coordinate system.

[0021] The mathematical function defining the shape and direction of the channel can be expressed by the general formula θ = f(r), referring to the polar coordinate system 110 with coordinates (r,θ) in Figure 6, where f is an arbitrary function defining a particular curvature. For example, the Archimedean spiral and similar curves are given by θ = ((rb) / a) c The logarithmic spiral curve is obtained by θ=(1nr-1na) / b. A straight 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) in polar coordinate system 110, a corresponding set of channels 80 may 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=f1(r), and another set of nonlinear channels can be defined by a negative function θ=-f2(r), where the mathematical functions f1 and f2 may be identical or not. Furthermore, the mathematical function describing the shape of a nonlinear channel may be essentially a three-dimensional spatial curve, in which case the general function θ=f(r,z) referring to cylindrical coordinate system (r,θ,z) can be substituted for θ=f(r) in the ongoing considerations without loss of generality.

[0022] According to an exemplary embodiment, the nonlinear mathematical functions of the shapes of fluid channels 60 and 80, when obtained as absolute values, may be equal to each other, thereby having a mirror image of each other. According to another embodiment, the fluid channels may not be mirror images of each other, but may still be configured as inverse helices. According to an exemplary embodiment, the reactor may include multiple nonlinear fluid channels having the same positive function, as well as multiple nonlinear channels having the same negative function. The reactor may include the whole of one set of nonlinear channels having a positive function and another set of nonlinear channels having a negative function. Referring to Figure 7A according to an exemplary embodiment, a reactor 200 is shown including an inlet 202 and an outlet 204. The 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 the passage 230, there may be a member 216 between the sets of fluid channels 214 and 212. This can be a thermally conductive member that can also form the ceiling of a first set of fluid members 212 and the floor of a second set of fluid channels 214. According to an exemplary embodiment, at least a portion of the channels 212 may be equipped with a catalyst, for example, to facilitate a desired reaction. The catalyst can be packed into one or both sets of channels, for example, in the form of foam, felt, grid, or particles. The catalyst can also be coated onto the channel walls, including portions of member 216 that form the floor of one set of channels and the ceiling of the other set.

[0023] According to an exemplary embodiment, the catalyst supported by the foam 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 the reactor 200 may have the same number of thermal connections as 2, if not 14, as shown as multiple contacts in 206 of the other set of channels 214.

[0024] This process transports reactants through a first set of fluid channels and extracts products from a second set of fluid channels, and at least one of the first set of fluid channels can be thermally engaged with at least two of the second set of fluid channels, for example, as shown in Figure 7A. According to an exemplary embodiment, an endothermic reaction may be provided in one of these sets of fluid channels, for example, as shown in Figure 8, fluid channel 212 may be provided and may have reactants that can be endothermic, which may be necessary to facilitate an endothermic reaction with solar energy. According to an exemplary embodiment, the reactor in Figure 7A has an unshown portion (below a portion or surface) that can be exposed to solar energy to supply energy to facilitate or drive this endothermic reaction. According to another embodiment, as the reaction proceeds through the reactor and the heated products return through a set of fluid channels 214, the heat of these products is transferred to an endothermic reaction in channel 212 via member 216.

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

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

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

[0028] Next, referring to Figure 8, a schematic diagram is shown for generating the reactants of this disclosure and receiving the product from the reactor. Thus, a process for distributing energy throughout a reactor, such as the reactor of this specification, is provided.

[0029] In certain embodiments, and also referring to Figure 7A, a methane-vapor feed gas mixture enters the reactor 200 at a hub inlet 202 and is distributed into 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 start to finish. Each channel contains a catalyst. This catalyst medium can take the form of a foam conforming to the shape of the channel, but can also include a substrate maintained within the channel, such as particles. Since each reaction channel can branch at a short distance from the center, the catalyst medium insert is sufficiently wide near the hub.

[0030] Near the edge of the reactor where the channels terminate, a slot-shaped opening connects the channels to a second set of channels that curve in the opposite direction to the first set of channels. The second set of channels 214 may be called the thermal recovery channels, while the first set of channels may be called the reaction channels. The reaction channels and thermal 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 a stream of reaction products from the reaction channels to enter the thermal recovery channels. The stream of products, returned to the center by the thermal recovery channels, flows out of the reactor through an annular space 204 between the inlet and outlet connecting pipes. Like the reaction channels, the thermal recovery channels may also be bifurcated.

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

[0032] By simulating the reaction flow and heterogeneous solar flux distribution under steam methane reforming conditions in embodiments of this reactor assembly and method, it is possible to understand the influence of the reactor geometry and channel configuration on the 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 perfect circle. In one embodiment incorporating countercross flow, two sets of channels can occupy a significant area of ​​the reactor, and thus the fluid can be used to provide substantial heat diffusion from the high-temperature zone to the low-temperature zone.

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

[0035] The counter-crossflow arrangement of reaction and recovery channels enables efficient heat diffusion from uneven solar irradiation to a substantially greater extent than that achieved by direct heat conduction through the metal layer. The reduction of hot spots leads to reduced operating 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 a mapping practice in which a parabolic dish was pointed towards the full moon. The results are shown in Figure 9 in W / m 2 As shown, multiple hotspots are clearly present. This flux distribution was specified as the boundary condition for the reactor front in the simulation model. For comparison, a reactor with the nonlinear channel of this disclosure and a preceding design of a radial-counterflowlinear channel with otherwise similar reactor and channel dimensions were simulated. The linear and nonlinear reactor models are shown in Figures 10A-10C and 11A-11C, respectively.

[0037] Figures 10B and 11B show the reactor surface temperature distribution under typical high solar flux conditions (total incident photovoltaic power of 9.6 kW, >80% methane conversion, methane flow rate of 0.032 mol / s, and a ratio of vapor to carbon of 3) for linear and nonlinear reactors, respectively. For the nonlinear helical countercross-flow reactor, the maximum surface temperature was found to be 988°C, more than 100°C lower than 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 that of the linear reactor. The superior heat diffusion in the nonlinear reactor is due to the intersection of any reaction channels below the hotspot by multiple recovery channels downstream of the hotspot, resulting in a larger amount of heat being received, which 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 ​​a single wedge-shaped reaction channel, or about 5% of the total surface area. Heat diffusion within the nonlinear reactor extends to at least the region enclosed by the reaction channels and the connected thermal recovery channels, or up to approximately 18% of the total surface area.

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

[0039] One embodiment of the present disclosure was tested in a solar thermochemical reaction system comprising a parabolic dish-type solar concentrator, an on-sun reactor unit positioned at the focal point of the dish, and a ground-based plant balance. The configuration of the reaction system is shown in Figure 8. The on-sun reactor unit included a steam methane reforming reactor, a regenerative heat exchanger, a vaporizer, and an onboard process controller. A supply gas system, water pump, process analyzer, and tail gas flare were located on the ground. The supply gas was controlled using a mass flow controller. The methane stream was preheated by a network of regenerative heat exchangers using the product stream. The concentrated solar energy was absorbed by the reforming reactor to catalytically convert methane into synthesis gas. The synthesis gas product stream was cooled by the supply gas stream and additional air cooling. The composition of the product gas was analyzed by process gas chromatography. After the separation of condensate, the product stream was discharged through a flare.

[0040] The nonlinear reactor, referred to as TRL6, was manufactured according to the design described in the previous section. In this particular embodiment of the present disclosure, the reactor was manufactured by machining individual plates and diffusing-coupling stacks of plates. The reactor is 14.85 m 2 It was tested paired with an Infinia PowerDish III parabolic dish concentrator with a nominal mirror area under moderate to high solar flux conditions. A linear reactor with otherwise similar reactor and channel dimensions, called TRL5, was also manufactured and tested on-sun with a dish concentrator of the same specifications.

[0041] Referring to Figures 12 and 13, the reactor's performance was evaluated by the 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 with respect to solar chemistry was defined as the ratio of the difference in higher heat output between the reactor product stream and the supply stream to the direct solar radiation (DNI) that becomes the incident energy to the dish concentrator reflector, and therefore includes effects resulting from reflectance, receiver intercept, heat loss around the reactor receiver, and the approach to equilibrium chemical conversion within the reactor. Data on the system's energy efficiency with respect to solar chemistry from on-sun tests are 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 superior thermal diffusion capability of the nonlinear reactor design allowed the reaction channels to reach higher temperatures when the reactor was operated under the same surface temperature constraints. The higher thermodynamic efficiency of the endothermic reaction at high temperatures is thought to compensate for the additional radiant heat lost, and therefore the overall high conversion efficiency of the TRL6 reactor for solar chemistry could extend into the high-flux region.

[0043] For comparison, the TRL5 reactor system did not operate at the same high solar flux as the linear reactor system due to its surface temperature exceeding the design point, as heat diffusion was not enhanced. In the low to medium solar flux range, the linear reactor system also outperformed the linear reactor in terms of energy efficiency relative to solar chemistry.

[0044] The performance advantages of nonlinear reactors become even more apparent when examining the reactor's energy efficiency. The reactor's thermal-chemical efficiency is defined as the ratio of the difference in higher heat generation between the reactor product stream and the supply stream to the amount of concentrated solar thermal energy the reactor receives, and therefore includes the effects of heat loss around the reactor and receiver, as well as the degree of chemical transformation within the reactor. Data on the reactor's thermal-chemical efficiency obtained from on-sun tests are shown in Figure 13.

[0045] The TRL5 reactor achieved an energy efficiency of 60%–70% for thermal chemistry, but was limited to low to medium flux operations due to hot spot issues and temperature limitations of the reactor material. Using the TRL6 reactor, an energy conversion efficiency of as high as 85% for thermal chemistry was achieved in the high flux region. Some data points even suggest that performance levels close to 90% may be possible. The superior performance of the nonlinear reactor in terms of energy efficiency is attributed to its greater thermal diffusion capability.

[0046] Exergy analysis was performed based on on-sun performance data of the TRL6 reactor. The objective was to evaluate the efficiency of the reactor and heat exchanger's second law and to identify the cause and scale of exergy breakdown. In the exergy analysis, exergy breakdown at the reactor front was estimated by approximating the surface temperature using the mean value based on IR thermographic measurements. The reference environment was selected as 25°C and 1 atm, with the chemical composition proposed by Szargut et al. The exergy efficiency of the TRL6 reactor was determined to be over 90%. For example, when tested under conditions of a methane feed flow rate of 0.048 mol / s, a vapor-to-carbon ratio of 2.2, a concentrated photovoltaic input of 10.88 kW, and an average reactor surface temperature of 820°C, the reactor rate of exergy breakdown was estimated at 5.34 kW, and the reactor's exergy efficiency was 90.2%.

Claims

1. It is a reactor, The first set of fluid channels, A second set of fluid channels oriented to be in thermal contact with the first set of fluid channels. Includes, The reactor wherein one of the first or second set of fluid channels is nonlinear.

2. The reactor according to claim 1, wherein the first set of channels defines a microchannel.

3. The reactor according to claim 1, wherein the first set of channels defines a mesochannel.

4. The reactor according to claim 1, wherein the first and second sets of channels define a microchannel.

5. The reactor according to claim 1, wherein the first and second sets of channels define a mesochannel.

6. The reactor according to claim 1, wherein both the first and second sets of fluid channels are nonlinear.

7. The reactor according to claim 1, wherein each of the set of fluid channels diverges from the hub of the reactor and extends to the edge of the reactor.

8. The reactor according to claim 7, wherein each channel of the first set of fluid channels is in fluid communication with each channel of the second set of fluid channels located at the edge of the reactor.

9. The reactor according to claim 1, wherein each channel of the first or second set of channels includes a dividing member.

10. The reactor according to claim 9, wherein the divided member extends to form a pair of fluid passages.

11. The reactor according to claim 10, wherein each individual channel in both the first and second sets of channels includes a dividing member.

12. The reactor according to claim 1, wherein the other of the first or second set of fluid channels is linear.

13. The reactor according to claim 1, further comprising a member for separating the first set of fluid channels from the second set of fluid channels.

14. The reactor according to claim 13, wherein the aforementioned member is thermally conductive.

15. The reactor according to claim 13, wherein the member defines the floor of one of the sets of fluid channels and the ceiling of the other set of fluid channels in at least one cross-section.

16. It is a stackable reactor, The first set of fluid channels, The system includes a second set of fluid channels stacked on top of the first set of fluid channels and oriented to be in thermal contact with the first set of fluid channels, The reactor wherein at least one channel of the first set of fluid channels is in thermal contact with a plurality of other channels of the second set of fluid channels.

17. The reactor according to claim 16, wherein the first set of channels defines a microchannel.

18. The reactor according to claim 16, wherein the first set of channels defines a mesochannel.

19. The reactor according to claim 16, wherein the first and second sets of channels define a microchannel.

20. The reactor according to claim 16, wherein the first and second sets of channels define a mesochannel.

21. The reactor according to claim 16, wherein one channel of the first set of fluid channels is in thermal contact with at least two of the other channels of the second set of fluid channels.

22. The reactor according to claim 16, wherein one channel of the first set of fluid channels is in thermal contact with 2 to 14 of the other channels of the second set of fluid channels.

23. The reactor according to claim 16, wherein at least one of the first set of fluid channels is in fluid communication with at least one of the other fluid channels of the second set of fluid channels.

24. The reactor according to claim 23, wherein each channel of the first set of fluid channels is in fluid communication with each channel of the second set of fluid channels.

25. The reactor according to claim 16, wherein one of the sets of fluid channels is stacked on top of the other set of fluid channels in at least one cross-section.

26. It is a reactor, A first set of fluid channels defining at least one nonlinear channel having a shape defined by a positive mathematical function, A second set of fluid channels defines at least another nonlinear channel having a shape defined by a negative mathematical function related to the positive mathematical function of one of the first set of fluid channels, and The reactor, including the reactor.

27. The reactor according to claim 26, wherein the first set of channels defines a microchannel.

28. The reactor according to claim 26, wherein the first set of channels defines a mesochannel.

29. The reactor according to claim 26, wherein the first and second sets of channels define a microchannel.

30. The reactor according to claim 26, wherein the first and second sets of channels define a mesochannel.

31. The reactor according to claim 26, wherein the absolute value of the mathematical function of one channel is equivalent to the absolute value of the mathematical function of the other channel.

32. The reactor according to claim 26, wherein the first set of fluid channels defines a plurality of nonlinear channels having the same positive mathematical function; and the second set of fluid channels defines a plurality of nonlinear channels having the same negative mathematical function related to the plurality of nonlinear channels of the first set of fluid channels.

33. The reactor according to claim 32, wherein the absolute value of the mathematical function of the plurality of nonlinear channels of the first set of fluid channels is equivalent to the absolute value of the mathematical function of the plurality of nonlinear channels of the second set of fluid channels.

34. The reactor according to claim 26, wherein each of the individual fluid channels of the first set defines a nonlinear channel having the positive mathematical function; and each of the individual fluid channels of the second set defines a nonlinear channel having the negative mathematical function related to the positive mathematical function of the individual nonlinear channel of the first set of fluid channels.

35. The reactor according to claim 34, wherein the absolute value of the mathematical function of the individual nonlinear channels of the first set of fluid channels is equivalent to the absolute value of the mathematical function of the individual nonlinear channels of the second set of fluid channels.

36. This is a process for distributing energy throughout the entire reactor. Transporting reactants from 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 The process including the process described above.

37. The process according to claim 36, further comprising carrying out an endothermic reaction within one of the set of fluid channels.

38. The process according to claim 37, further comprising accelerating the endothermic reaction by solar energy.

39. The process according to claim 37, further comprising promoting the endothermic reaction with the catalyst.

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