Reactor with anti-spiral flow channel and method of use thereof

Abstract

Embodiments of the present disclosure relate to a reactor. The reactor includes a first helical channel having a plurality of first turns and a second helical channel having a plurality of second turns. The plurality of second turns of the second helical channel alternate with the plurality of first turns of the first helical channel. The reactor also includes a permeable membrane that divides the first helical channel into a first passage and a second passage along a length of the first helical channel. The permeable membrane is configured to control fluid flow between the first passage and the second passage.

Description

[0001] Cross-reference to related applications

[0002] This application claims priority to U.S. Provisional Application No. 63 / 471,330, filed June 6, 2023, pursuant to 35 USC § 119, the contents of which are incorporated herein by reference in their entirety. Background Technology

[0003] This disclosure relates to flow reactors, and more specifically, to flow reactors having a helical process and heat exchange channels.

[0004] Continuous flow reactors are more commonly used in industrial-scale chemical processes. Within these reactors, a continuous flow of reactants reacts to provide a continuous flow of products. Continuous flow reactors can handle high reactant concentrations and provide high mixing rates. Due to these advantages, continuous flow reactors have been adopted in the food, chemical, and pharmaceutical industries. Summary of the Invention

[0005] According to one aspect, embodiments of this disclosure relate to a reactor. The reactor includes a first helical channel having a plurality of first turns and a second helical channel having a plurality of second turns. The plurality of second turns of the second helical channel alternate with the plurality of first turns of the first helical channel. The reactor further includes a permeable membrane that divides the first helical channel into a first passage and a second passage along the length of the first helical channel. The permeable membrane is configured to control fluid flow between the first passage and the second passage.

[0006] According to another aspect, embodiments of this disclosure relate to a reactor. The reactor includes a first helical channel having a plurality of first turns and a second helical channel having a plurality of second turns. The plurality of second turns of the second helical channel alternate with the plurality of first turns of the first helical channel. A catalyst is disposed within the first helical channel, and the catalyst is configured to promote a reaction in a fluid flowing through the first helical channel.

[0007] According to another aspect, embodiments of this disclosure relate to a method. In this method, a first fluid flows through a first helical channel having a plurality of first turns wound around a longitudinal axis. A second fluid flows through a second helical channel having a plurality of second turns wound around the longitudinal axis. The plurality of second turns of the second helical channel alternate with the plurality of first turns of the first helical channel. A catalyst disposed in the first helical channel catalyzes a reaction in the first fluid.

[0008] According to another aspect, embodiments of this disclosure relate to a method. In this method, a first fluid flows through a first passage of a first helical channel. The first helical channel has a plurality of first turns wound around a longitudinal axis. Furthermore, in this method, a second fluid flows through a second passage of the first helical channel. A permeable membrane separates the first passage from the second passage along the length of the first helical channel. A third fluid flows through a second helical channel, which has a plurality of second turns wound around the longitudinal axis. The plurality of second turns of the second helical channel alternate with the plurality of first turns of the first helical channel. The permeable membrane is used to control the inflow of the second fluid into the first fluid.

[0009] Additional features and advantages will be set forth in the detailed description below, and to some extent, these additional features and advantages will be apparent from the description or will be recognized by practice of the embodiments described herein, which are included in the detailed description below, the claims, and the drawings.

[0010] It should be understood that the foregoing general description and the following detailed description are merely exemplary and intended to provide an overview or framework for understanding the nature and features of the claims. Drawings are included to provide further understanding and are incorporated in and form a part of this specification. Attached Figure Description

[0011] The accompanying drawings, which are incorporated in and form a part of this specification, illustrate several aspects of the invention and, together with the description, serve to explain the principles of the invention. In the drawings:

[0012] Figure 1-3 A reactor with a helical channel according to an exemplary embodiment is depicted, wherein the helical channel has various spacings between the turns of the channel;

[0013] Figure 4 A reactor with a helical channel according to an exemplary embodiment is depicted, the helical channel being connected to... Figure 1 Compared to having reverse flow;

[0014] Figure 5A and 5B A reactor with a helical channel, having a variable flow area, is depicted according to an exemplary embodiment;

[0015] Figure 6 and 7 The outline of a spiral channel designed to influence the magnitude of a velocity field, according to an exemplary embodiment, is depicted.

[0016] Figure 8A and 8BA cross-sectional view of adjacent spiral channels designed to facilitate heat transfer, according to an exemplary embodiment, is depicted.

[0017] Figure 9 A reactor having a central tube and an outer shell to provide additional thermal management is depicted according to an exemplary embodiment;

[0018] Figure 10A and 10B An example of a catalyst disposed in a first spiral channel of a reactor according to an exemplary embodiment is depicted;

[0019] Figure 11 A first helical channel containing a permeable membrane is depicted according to an exemplary embodiment, the permeable membrane dividing the first helical channel into a first passage and a second passage;

[0020] Figure 12 A reactor having a tap for removing gaseous byproducts from a first helical channel, according to an exemplary embodiment, is depicted;

[0021] Figure 13 Based on exemplary embodiments Figure 1 A graph showing the pressure drop modeling as a function of flow rate for a reactor design with a pressure of -5°C.

[0022] Figure 14 It is a graph of modeled pressure drop as a function of flow rate based on reactors of various diameters, according to an exemplary embodiment;

[0023] Figure 15 and 16 The following describes a method based on an exemplary embodiment. Figure 1 The flow field of reactor design for 5;

[0024] Figure 17 This is a graph of the volumetric heat transfer coefficient of a toluene / silicone oil system according to an exemplary embodiment;

[0025] Figure 18 A prototype of a reactor according to an exemplary embodiment is depicted;

[0026] Figure 19 It is a graph showing the volumetric mass transfer coefficient of a liquid-gas system as a function of residence time, according to an exemplary embodiment; and

[0027] Figure 20 This is a graph showing the volumetric mass transfer coefficient and pressure drop as a function of residence time, according to an exemplary embodiment. Detailed Implementation

[0028] Reference will now be made in detail to various embodiments of reactors with helical channels configured to provide improved thermal conductivity between the helical channels and enhanced mixing. Specifically, the reactor can be modified in various ways to alter the velocity field of the fluid flow in direction and magnitude, improve thermal management, catalyze reactions, and enhance contact between precursors. For example, the spacing, shape, and profile of the helical channels can be adjusted to increase / decrease residence time or accelerate / decelerate the flow rate. Furthermore, the helical channels can be coated or filled with catalyst or separated by a permeable membrane to modulate the kinetics of the reaction within the helical channels. These and other aspects and advantages of reactors with helical channels will be described with respect to the embodiments provided below and depicted in the figures. These embodiments are presented as illustrative but not as limiting.

[0029] Figure 1 An embodiment of reactor 10 is depicted. Reactor 10 includes a first helical channel 12 through which at least one first fluid flows. In one or more embodiments, two or more first fluids flow in the first helical channel 12, and in the first helical channel 12, the two or more first fluids react or combine to form a product stream. The first helical channel 12 includes a plurality of first turns 14 wound around a longitudinal axis 16 of reactor 10. As used herein, a "turn" is a complete rotation (e.g., 360 degrees) around the longitudinal axis 16, wherein the starting point of the turn is axially displaced along the longitudinal axis 16 from the ending point of the turn. In one or more embodiments, the first turns 14 are wound around the longitudinal axis in a continuous curve such that, when reactor 10 is viewed from above, the first turns 14 define a circular, elliptical, oval, or other curved shape. In one or more other embodiments, the first turns 14 are wound around the longitudinal axis 16 in substantially linear segments (with rounded or pointed apexes) such that, when reactor 10 is viewed from above, the first turns 14 define a triangular, quadrilateral, or other polygonal shape. In one or more other embodiments, the first loop 14 is wound around the longitudinal axis 16 in both curved and linear segments, such that the first loop defines a shape having both curved and linear regions (e.g., a runway shape). Each first loop 14 has a first maximum cross-sectional dimension D1, and in one or more embodiments, the first maximum cross-sectional dimension D1 is centered on the longitudinal axis 16. In the depicted embodiment, the first loop 14 defines a circular helix with a first maximum cross-sectional dimension (diameter) D1 centered on the longitudinal axis 16.

[0030] Reactor 10 also includes a second helical channel 18 through which at least one second fluid flows. In the figures, opposite shaded lines are used to distinguish the first helical channel 12 and the second helical channel 18 (for non-cross-sectional views). In one or more embodiments, the at least one second fluid is a heat exchange fluid configured to heat or cool at least one first fluid in the first helical channel 12, for example, to promote mixing, reaction, etc., of the fluids in the first helical channel 12. Nevertheless, in one or more other embodiments, at least one second fluid may be selected to use the heat generated by the first fluid in the first helical channel 12 to perform a reaction or generate heat to promote a reaction in the first fluid in the first helical channel 12. Thus, for example, an exothermic reaction may take place in the first helical channel 12, and an endothermic reaction may take place in the second helical channel 18 (or vice versa).

[0031] The second helical channel 18 comprises a plurality of second coils 20. Similar to the first helical channel 12, the "coils" 20 of the second helical channel 18 are complete rotations (e.g., 360 degrees) about a longitudinal axis 16, wherein the starting point of the coil is axially displaced along the longitudinal axis 16 from the ending point of the coil. In one or more embodiments, the second coils 20 are wound around the longitudinal axis in a continuous curve such that, when viewed from above, the second coils 20 define a circular, elliptical, oval, or other curved shape. In one or more other embodiments, the second coils 20 are wound around the longitudinal axis 16 in substantially linear segments (with rounded or pointed apexes) such that, when viewed from above, the second coils 20 define a triangular, quadrilateral, or other polygonal shape. In yet another one or more other embodiments, the second coils 20 are wound around the longitudinal axis 16 in both curved and linear segments such that the second coils 20 define a shape having both curved and linear regions (e.g., a racetrack shape). Each second coil 20 has a second maximum cross-sectional dimension D2, and in one or more embodiments, the second maximum cross-sectional dimension D2 is centered on the longitudinal axis 16. In the depicted embodiment, the second ring 20 further defines a circular helix having a second maximum cross-sectional dimension (diameter) D2 centered on the longitudinal axis 16.

[0032] In one or more embodiments, the second maximum cross-sectional dimension D2 is equal to the first maximum cross-sectional dimension D1. However, in one or more other embodiments, the second maximum cross-sectional dimension D2 is different from (greater than or less than) the first maximum cross-sectional dimension D2.

[0033] like Figure 1 As shown, the second spiral channel 18 has a plurality of second turns 20 that alternate with the first spiral channel 12's plurality of first turns 14. In this way, the second turns 20 are positioned between subsequent first turns 14.

[0034] In one or more embodiments, at least one first fluid flowing through the first helical channel 12 includes a liquid, a gas, a slurry, or a combination thereof. In one or more embodiments, a second fluid flowing through the second helical channel 18 includes a liquid, a gas, a slurry, or a combination thereof.

[0035] In one or more embodiments, the first helical channel 12 is defined by a first wall 22 having a first outer surface 24. Furthermore, in one or more embodiments, the second helical channel 18 is defined by a second wall 26 having a second outer surface 28. In one or more embodiments, the first outer surface 24 contacts the second outer surface 28. Specifically, the first outer surface 24 contacts the second outer surface 28 at an interface 30 between the first turn 14 and the second turn 20 along the length of the first helical channel 12 and the second helical channel 18. In such embodiments, the contact between the surfaces 24, 28 of the helical channels 12, 18 improves the thermal conductivity between the helical channels 12, 18 (e.g., the second channel 18 more effectively heats or cools the first helical channel 12). Nevertheless, in one or more other embodiments, the first helical channel 12 and the second helical channel 18 share a common wall (e.g., as shown in the image). Figure 5B and 8B As shown in the image).

[0036] like Figure 1 As shown, reactor 10 has a length L along a longitudinal axis 16 between a first end 32 and a second end 34. The length L of reactor 10 is not particularly limited, and in one or more embodiments, the length L is from 1 mm to 10,000 mm, particularly from 100 mm to 5,000 mm. In one or more embodiments, the first helical channel 12 includes at least one first inlet 36 at the first end 32 and a first outlet 38 at the second end 34. In one or more embodiments, the first helical channel 12 includes two or more first inlets 36 to receive two fluid flows, and the fluids react within the first helical channel 12 and exit through the first outlet 38.

[0037] Furthermore, in one or more embodiments, the second helical channel 18 includes a second inlet 40 at a second end 34 and a second outlet 42 at a first end 32. As mentioned above, in one or more embodiments, heat exchange fluid flows from the second inlet 38 through the second helical channel 18 to the second outlet 40. Because the first inlet 36 of the first helical channel 12 is arranged at the end opposite to the second inlet 40 of the second helical channel 18, in one or more embodiments, the reactor 10 can be configured for counter-helical flow, which enhances heat transfer between the first helical channel 12 and the second helical channel 18. Nevertheless, the first inlet 36 of the first helical channel 12 and the second inlet 40 of the second helical channel 18 can be arranged at the same end, such that fluid flows simultaneously from the first end 32 to the second end 34 (or from the second end 34 to the first end 32) through both the first helical channel 12 and the second helical channel 18.

[0038] In different embodiments, the shapes of the helical channels 12 and 18 may vary. For example, the spacing or cross-sectional flow area of ​​the helical channels 12 and 18 may vary. Figure 1 As shown, the spacing P relates to the interval between the first turns 14 of the first helical channel 12 and between the second turns 20 of the second helical channel 18. In one or more embodiments, the spacing P is from 1 mm to 10,000 mm, particularly from 10 mm to 100 mm. For a given length L, the spacing P determines the number of first turns 14 of the first helical channel 12, and a larger spacing P corresponds to fewer first turns 14. In one or more embodiments, the spacing P between the second turns 20 of the second helical channel 18 is the same as the spacing P between the first turns 14. In one or more embodiments, the spacing P is constant along the length L of the reactor 10, and in one or more other embodiments, the spacing P varies along the length L of the reactor 10.

[0039] Figure 1-3 An example of a reactor 10 with different spacing P between turns 14 and 20 of spiral channels 12 and 18 is depicted. Figure 1 A basic case with a spacing P of X (e.g., 60 mm) is depicted. Figure 2 A case of reduced spacing with a spacing P of 0.5X (e.g., 30 mm) is depicted, and it can be seen that the number of loops 14 and 20 on length L increases compared to the basic case. Figure 3 A case of increased spacing P with a spacing of 2X (e.g., 120 mm) is depicted, and it can be seen that the number of loops 14 and 20 on length L is reduced compared to the basic case. Although Figure 1-3Each of these describes a constant spacing P along the length of reactor 10, but as mentioned above, the spacing P along the length of reactor 10 can be variable. For example, the spacing P can be shorter near the first inlet 36 and longer toward the first outlet 38, such that the increased residence time compensates for the reduction in the driving force of the chemical process. Additionally, a longer spacing P can be used when reactor 10 is part of a multi-step process or during (chemical) quenching to compensate for the increased flow rate and limit the increase in pressure drop. Furthermore, a longer spacing P can be used when the heat transfer rate becomes less important (lower chemical driving force), thus the reduction in pressure drop is beneficial from an energy perspective.

[0040] Figure 4 An embodiment is described, wherein with Figure 1-3 Compared to the embodiment shown, the flow through reactor 10 is reversed. Figure 4 In this reactor 10, at least one first inlet 36 of the first helical channel 12 is located at the second end 34, and a first outlet 38 of the first helical channel 12 is located at the first end 32. Correspondingly, a second inlet 40 of the second helical channel 18 is located at the first end 32, and a second outlet 42 of the second helical channel 18 is located at the second end 34. In the depicted embodiment, the flow in the respective helical channels 12, 18 remains opposite, but... Figure 1-3 Compared to the embodiments shown, Figure 4 The direction of each flow in the process is reversed.

[0041] Besides the spacing P, the cross-sectional flow areas of the helical channels 12 and 18 can vary along their lengths, such as... Figure 5A and 5B As shown. In Figure 5A In this configuration, the cross-sectional flow area of ​​the first helical channel 12 changes in opposite directions to the cross-sectional flow area of ​​the second helical channel 18. For example, at the first position 44, the first helical channel 12 has a first inner surface 46 defining a first flow area 48. At the first position 44, the second helical channel 18 has a second inner surface 50 defining a second flow area 52. It can be seen that the second flow area 52 is smaller than the first flow area 48. At the second position 54, the first flow area 48 defined by the first inner surface 46 is smaller than the second flow area 52 defined by the second inner surface 50.

[0042] By increasing and decreasing the first flow area 48 in the first helical channel 12, the flow rate within the first helical channel 12 is accelerated and decelerated to promote the mixing of one or more fluids within the first helical channel 12. This can help to make the temperature within one or more fluids more uniform and / or enhance the contact between different fluids and their reactants.

[0043] like Figure 5A As shown, the first helical channel 12 is defined by a first wall 22, and the second helical channel 18 is defined by a second wall 26. It can be seen that the first outer surface 24 of the first wall 22 contacts the second outer surface 28 of the second wall 26, which, as discussed above, improves the thermal conductivity between the first helical channel 12 and the second helical channel 18. Figure 5B As shown, the first helical channel 12 and the second helical channel 18 have a common wall 55. In this way, the common wall 55 partially defines a first inner surface 46 of the first helical channel 12 and partially defines a second inner surface 50 of the second helical channel 18. The common wall 55 also provides enhanced thermal conductivity between the first helical channel 12 and the second helical channel 18.

[0044] Figure 6 and 7 An example depicting the profile of the first inner surface 46. In Figure 6 In this embodiment, the first inner surface 46 includes a first region 56 having a constant flow area and a necking region 58 disposed between the first regions 56. In one or more embodiments, the flow area of ​​the necking region 58 gradually decreases from a maximum flow area in one of the first regions 56 to a minimum flow area, for example, at the midpoint of the necking region 58, and then expands back to a maximum flow area in another of the first regions 56. Figure 7 In the process, the flow area continuously varies between the first region 56, which has the largest flow area, and the necking region 58, which has the smallest flow area.

[0045] Typically, the shape and profile of the first helical channel 12 are designed to alter the velocity field of the fluid flowing through it. The helical flow introduces a directional change in the velocity field through the centrifugal force exerted on the fluid as it flows around the longitudinal axis 16. Furthermore, the shape of the flow area (including any profile) can alter the magnitude of the velocity field, for example, by accelerating or decelerating the flow.

[0046] In addition, the design of reactor 10 enhances the heat transfer to / from the heat exchange fluid carried in the second spiral channel 18. Figure 8A and 8B Each depicts a cross-section of the spiral channels 12 and 18, taken from adjacent turns 14 and 20 passing through the spiral channels 12 and 18. For example... Figure 8A As shown, the first outer surface 24 of the first helical channel 12 contacts the second outer surface 28 of the second helical channel 18. The contact between the outer surfaces 24 and 28 of the helical channels 12 and 18 provides good thermal conductivity, especially when the walls 22 and 26 of the helical channels 12 and 18 are made of a material with high thermal conductivity (e.g., metal).

[0047] Figure 8ASpiral channels 12, 18 with walls 22, 26 of uneven thickness are also depicted. Specifically, inner surfaces 46, 50 define polygonal shapes (e.g., trapezoids) that create sections of walls 22, 26 that are thicker than other sections. While trapezoids are depicted, inner surfaces 46, 50 may define other polygonal or circular shapes. Furthermore, while the embodiments depicted so far contemplate spiral channels 12, 18 in which the volume and channel shape / profile are identical, the first spiral channel 12 may differ from the second spiral channel 12 in at least one aspect of volume, channel shape, or profile design.

[0048] exist Figure 8B In reactor 10, a common wall 55 is shared between spiral channels 12 and 18. For example... Figure 8B As can be seen, the common wall 55 has a non-uniform thickness to provide a stable heat conduction path between the spiral channels 12 and 18, regardless of the shape of the spiral channels 12 and 18.

[0049] While thermal management of the spiral channels 12 and 18 can be enhanced by improving thermal conductivity, further configurations can be made to heat or cool the first spiral channel 12, such as... Figure 9 As shown in the diagram. As discussed above, the first helical channel 12 and the second helical channel 18 are wound around the longitudinal axis 16 of the reactor 10. The central aperture defined by the helical channels 12, 18 may be hollow, such that nothing is disposed inside the reactor 10. However, in one or more other embodiments, the reactor 10 includes a central tube 60 through which additional heat exchange fluid can flow to heat or cool the fluid in the first helical channel 12. Furthermore, in one or more embodiments, the reactor 10 is provided with a housing 62 that defines a cavity 64 surrounding the helical channels 12, 18. This cavity 64 may also be filled with heat exchange fluid to heat or cool the fluid in the first helical channel 12. Thus, one or both of the central tube 60 and the housing 62 can be used to provide additional thermal management for the reactor.

[0050] In addition to controlling the reaction and / or mixing in the first helical channel 12 through thermal management, reactor 10 also allows for control of the reaction and mixing by other means. In one or more embodiments, reactor 10 contains a catalyst located in the first helical channel 12, such as... Figure 10A and 10B As shown. In Figure 10A In this embodiment, the solid catalyst is a coating 66 deposited on the first inner surface 46. In one or more embodiments, any of a variety of vapor deposition techniques known in the art can be used to deposit the solid catalyst. Figure 10BIn this embodiment, the solid catalyst is provided in the form of beads or pellets 68 filling the first helical channel 12. It can be seen that the beads or pellets 68 do not completely block the flow area of ​​the first helical channel 12, and the flow through the beads or pellets 68 can be tailored based on the selection of the size or shape of the beads or pellets 68. In one or more embodiments, the catalyst can be used to catalyze reactions such as hydrogenation, halogenation, oxidation, polymerization, nitration, esterification, or fermentation.

[0051] According to one or more other embodiments, a permeable membrane 70 may be used to control the reaction / mixing of fluid in the first helical channel 12, the permeable membrane dividing the first helical channel 12 along its length from a first end 32 to a second end 34, such as... Figure 11 As shown in the diagram. In one or more embodiments, the permeable membrane 70 divides the first helical channel 12 into a first passage 72 and a second passage 74. In such embodiments, the first passage 72 may be in fluid communication with a first inlet 36, and the second passage 74 may be in fluid communication with another first inlet 36. In this way, the first passage 72 may receive a first fluid precursor, and the second passage 74 may receive a second fluid precursor. The permeable membrane 70 may be configured to control how the second fluid precursor interacts with the first fluid precursor. For example, the permeable membrane 70 may have pores that affect the amount of the second precursor that passes through the permeable membrane 70 along the length of the first helical channel 12 to reach the first passage 72. Furthermore, the pore size may allow only droplets or bubbles of a certain size to pass through the permeable membrane 70.

[0052] In these ways, the permeable membrane 70 can control reaction kinetics by increasing or decreasing the surface area of ​​one precursor in another. That is, the permeable membrane 70 can limit the passage of the second precursor to bubbles or droplets below a certain size to increase the surface area of ​​the second precursor in the first precursor. Furthermore, the permeable membrane 70 can control the amount of the second precursor passing through at one time. If too much of the second precursor passes through at once, it may coalesce and drift to the outer edge of the first helical channel 12 due to centrifugal force.

[0053] Furthermore, in one or more embodiments, the permeable membrane 70 tapers along the length of the first helical channel 12. In this way, the ratio of the flow area in the first passage 72 to the flow area in the second passage 74 varies along the length of the first helical channel 12. For example, the ratio of the flow area in the first passage to the flow area in the second passage may vary from 50:50 at the first end 32 to 100:0 at the second end 34. In such embodiments, the first passage 70 may be in fluid communication with the first outlet 38.

[0054] Furthermore, in one or more embodiments, the outer wall 75 or a portion thereof is also a membrane 70. In this way, fluid in the first helical channel 12 can be continuously fed into another component. For example, the membrane 70 can selectively feed desired products or undesired byproducts into another component, such as for further reaction or storage / removal.

[0055] In another embodiment, the reaction kinetics in the first helical channel 12 can be controlled by removing gaseous byproducts, such as... Figure 12 As shown in the diagram. In certain chemical reactions, gases can be generated along with desired chemical products, and the presence of gases within the fluid flow can shorten the residence time of the liquid phase in the first helical channel 12 and affect the intensity of heat transfer. Therefore, as... Figure 12 As shown, reactor 10 may be provided with one or more taps 76 through which gas can escape from the liquid phase in the first spiral channel 12.

[0056] Experimental examples of modeling

[0057] Various embodiments of the disclosed reactor 10 are modeled to determine flow characteristics.

[0058] Figure 13 It is a graph of pressure drop as a function of flow rate. For according to... Figure 1 The reactor example of -5 uses modeling data that considers reactor 10 with a diameter of 75 mm and a length of 400 mm. Specifically, Figure 1 The foundation spacing P shown is 60 mm (volume is 0.6 L). Figure 2 The small pitch P shown is 30 mm (volume 0.5 L), and Figure 3 The large spacing P shown is 120 mm (volume 0.67 L). The basic spacing of the counterflow reactor 10 is 60 mm (volume 0.61 L), and the volume of the variable flow area reactor 10 shown in Figure 5 is 0.61 L. The fluid considered in the model is water. Figure 13 As can be seen, reactor 10 with the largest spacing has the lowest pressure drop. Reactors with both base spacing and reverse base spacing have the same pressure drop for the modeled flow rate, which is slightly higher than the pressure drop of the largest spacing. The variable cross-section reactor 10 has a slightly larger base spacing and reverse base spacing, and the small-spacing reactor has the highest pressure drop. Nevertheless, all modeled reactors exhibit a pressure drop of less than 0.25 bar.

[0059] Figure 14This is a graph showing the pressure drop as a function of flow rate for reactors with different diameters but maintaining the same spacing P. Specifically, diameters of 225 mm, 350 mm, and 503 mm are considered, corresponding to volumes of 7.8 L, 18.78 L, and 44.3 L, respectively. All considered reactors have a length of 730 mm, and the data were modeled based on water as the fluid in the reactor. It can be seen that the pressure drop increases as the diameter decreases.

[0060] Figure 15 and 16 Velocity field diagrams of two reactors 10 according to this disclosure are depicted. Figure 15 The velocity field diagram corresponds to Figure 1 The embodiment depicted in the figure shows that the spiral channel 12 changes the direction and magnitude of the velocity vector, indicating effective mixing of the fluid within the spiral channel 12. Figure 16 The velocity field diagram corresponds to the embodiment with variable flow area depicted in Figure 5. It can be seen that increasing and decreasing the flow area produces even greater changes in the magnitude of the velocity vector, and the helical winding also changes the direction of the velocity vector, which again demonstrates the effective mixing within the helical channel 12.

[0061] Furthermore, the heat transfer intensity of the ethanol / silicone oil system (the latter designated as the utility) was adiabatically simulated for a SiC reactor with a volume of 600 mL in each of the first spiral channel 12 and the second spiral channel 18. Each spiral channel 12, 18 has walls 22, 26 with a thickness of 5 mm. A heat transfer intensity as high as 2.2 × 10⁻⁶ was found for 5 L / min ethanol and 15 L / min utility (50% in the central tube). 5 W / m 3 K. For the same residence time, a reactor with approximately 65% ​​less internal volume operating with 20 L / min of auxiliary material will have approximately 50% greater heat transfer.

[0062] Figure 17 The figure illustrates the effect of process fluid and total heat exchange fluid flow rates on the thermal performance of a 0.6 L SiC reactor for a toluene-silicone oil system at different total (second spiral channel and central tube) heat exchange fluid flow rates (2 + 2 L / min; 5 + 2 L / min; 5 + 5 L / min) and two flow rates in the first spiral channel (5 L / min and 1 L / min). As expected, higher flow rates provide better reactor thermal performance.

[0063] Experimental Example

[0064] In addition to the modeling data, a prototype reactor 10 was also constructed, such as Figure 18As shown in the diagram, reactor 10 has a first helical channel 12 with a volume of 28 mL. Two fluids are pumped into corresponding first inlets 36 of the first helical channel 12. One fluid is yellow, and the other is blue. The fluid observed in the first helical channel 12 is green, indicating that the fluids are effectively mixed.

[0065] use Figure 18 The gas-liquid system was studied in a reactor. Specifically, the absorption of CO2 in a 0.5 M NaHCO3 / Na2CO3 buffer solution was measured to determine the mass transfer intensity. Figure 19 A graph depicts the volumetric mass transfer coefficient as a function of residence time. For a residence time of 4 seconds, the volumetric mass transfer coefficient is approximately 15.5 × 10⁻⁶. -2 s -1 Furthermore, for a residence time of approximately 12 seconds, the volumetric mass transfer coefficient is approximately 6.10. -2 s -1 These values ​​fall within the range reported in the literature for various types of contactor technologies. Furthermore, it is believed that using the values ​​described above... Figure 11 The membrane described above can further enhance the intensity of the mass transfer process.

[0066] in this regard, Figure 20 The graph shows the volumetric mass transfer coefficient and pressure drop as a residence time of approximately 4 seconds to approximately 40 seconds. The volumetric mass transfer coefficient of a device having a first helical channel 12 with a volume of 463 mL is measured. This first helical channel is divided by a permeable membrane 70 into a first liquid passage 70 with a volume of 393 mL and a second gas passage 72 with a volume of 70 mL. The permeable membrane 70 has pores up to a size of 7.86 mm. Figure 20 As shown, even at low residence times (high flow rates), the pressure drop is relatively low (only about 0.25 bar).

[0067] Unless otherwise expressly stated, it is not intended to interpret any method described herein as requiring its steps to be performed in a particular order. Therefore, no particular order is intended to be inferred where the method claims do not actually enumerate the order in which the steps are followed, or where the claims or description do not specifically state that the steps should be limited to a particular order. Furthermore, as used herein, the article “a(a)” is intended to include one or more parts or elements, and is not intended to be construed as referring to only one.

[0068] The subject matter of this disclosure may also particularly relate to the following aspects:

[0069] According to aspect (1), a reactor is provided. The reactor includes: a first helical channel including a plurality of first turns; a second helical channel including a plurality of second turns, the plurality of second turns of the second helical channel alternating with the plurality of first turns of the first helical channel; and a permeable membrane dividing the first helical channel into a first passage and a second passage along the length of the first helical channel; wherein the permeable membrane is configured to control fluid flow between the first passage and the second passage.

[0070] According to aspect (2), a reactor as described in aspect (1) is provided, wherein the first passage has a first cross-sectional flow area and the second passage has a second cross-sectional flow area, and wherein the first cross-sectional flow area and the second cross-sectional flow area vary along the length of the first helical passage.

[0071] According to aspect (3), a reactor as described in aspect (2) is provided, wherein the first cross-sectional flow area increases along the length of the first helical channel, and the second cross-sectional flow area decreases along the length of the first helical channel.

[0072] According to aspect (4), a reactor according to any one of aspects (1) to (3) is provided, the reactor further comprising a first inlet in fluid communication with the first passage and a second inlet in fluid communication with the second passage, wherein the first inlet is configured to receive a first fluid and the second inlet is configured to receive a second fluid, and wherein the permeable membrane is configured to control the mixing of the second fluid in the first fluid.

[0073] According to aspect (5), a reactor as described in aspect (4) is provided, wherein the second spiral channel includes a third inlet configured to receive heat exchange fluid.

[0074] According to aspect (6), a reactor as described in aspect (5) is provided, wherein the first inlet and the second inlet are disposed at a first end of the reactor and the third inlet is disposed at a second end of the reactor, the first end being opposite to the second end, such that the flow of the first fluid and the second fluid through the first helical channel is countercurrent to the flow of the heat exchange fluid through the second helical channel.

[0075] According to aspect (7), a reactor according to any one of aspects (1) to (6) is provided, wherein the first helical channel is configured to change the velocity field of the fluid flowing through the first helical channel, wherein the velocity field varies in direction and magnitude.

[0076] According to aspect (8), a reactor according to any one of aspects (1) to (7) is provided, wherein the first helical channel is defined by a first wall having a first outer surface, wherein the second helical channel is defined by a second wall having a second outer surface, and wherein the first outer surface contacts the second outer surface along the length of the first helical channel.

[0077] According to aspect (9), a reactor according to any one of aspects (1) to (7) is provided, wherein the first helical channel includes a first inner surface, wherein the second helical channel includes a second inner surface, and wherein the first inner surface and the second inner surface share a common wall.

[0078] According to aspect (10), a reactor according to any one of aspects (1) to (9) is provided, the reactor further comprising a central tube extending along the longitudinal axis of the reactor, wherein the first helical channel and the second helical channel are wound around the central tube, and wherein the central tube is configured to carry a heat exchange fluid.

[0079] According to aspect (11), a reactor according to any one of aspects (1) to (10) is provided, the reactor further comprising a shell disposed around the first helical channel and the second helical channel to form a cavity between the shell and the first helical channel and the second helical channel, wherein the cavity is configured to carry a heat exchange fluid.

[0080] According to aspect (12), a reactor according to any one of aspects (1) to (11) is provided, the reactor further comprising at least one tap in fluid communication with the first helical channel, wherein the tap is configured to remove gas released during fluid flow through the first helical channel.

[0081] According to aspect (13), a reactor as described in any one of aspects (1) to (12) is provided, the reactor further comprising a catalyst disposed within the first passage.

[0082] According to aspect (14), a reactor as described in aspect (13) is provided, wherein the catalyst is coated on the inner surface of the first passage.

[0083] According to aspect (15), a reactor as described in aspect (13) is provided, wherein the catalyst comprises a plurality of beads or pellets.

[0084] According to aspect (16), a reactor is provided. The reactor includes: a first helical channel including a plurality of first turns; a second helical channel including a plurality of second turns, the plurality of second turns of the second helical channel alternating with the plurality of first turns of the first helical channel; and a catalyst disposed within the first helical channel; wherein the catalyst is configured to promote a reaction in a fluid flowing through the first helical channel.

[0085] According to aspect (17), a reactor as described in aspect (16) is provided, wherein the catalyst is coated on the inner surface of the first helical channel.

[0086] According to aspect (18), a reactor as described in aspect (16) is provided, wherein the catalyst comprises a plurality of beads or pellets.

[0087] According to aspect (19), a reactor is provided according to any one of aspects (16) to (18), wherein the first helical channel is configured to change the velocity field of the fluid flowing through the first helical channel, wherein the velocity field varies in direction and magnitude.

[0088] According to aspect (20), a reactor is provided according to any one of aspects (16) to (19), wherein the first helical channel includes a first cross-sectional flow area that varies along the length of the first helical channel.

[0089] According to aspect (21), a reactor as described in aspect (20) is provided, wherein the second helical channel includes a second cross-sectional flow area that varies along the length of the second helical channel, and wherein the second cross-sectional area varies in opposite directions to the first cross-sectional area.

[0090] According to aspect (22), a reactor according to any one of aspects (16) to (21) is provided, wherein the first helical channel is defined by a first wall having a first outer surface, wherein the second helical channel is defined by a second wall having a second outer surface, and wherein the first outer surface contacts the second outer surface along the length of the first helical channel.

[0091] According to aspect (23), a reactor according to any one of aspects (16) to (21) is provided, wherein the first helical channel includes a first inner surface, wherein the second helical channel includes a second inner surface, and wherein the first inner surface and the second inner surface share a common wall.

[0092] According to aspect (24), a reactor according to any one of aspects (16) to (23) is provided, the reactor further comprising a first inlet at a first end of the reactor in fluid communication with the first helical channel, wherein the second helical channel comprises a second inlet configured to receive heat exchange fluid, the second inlet being disposed at a second end of the reactor opposite to the first end, such that the fluid flow through the first helical channel is countercurrent to the flow of the heat exchange fluid through the second helical channel.

[0093] According to aspect (25), a reactor according to any one of aspects (16) to (24) is provided, the reactor further comprising at least one tap in fluid communication with the first helical channel, wherein the tap is configured to remove reaction-emitted gases from the fluid flowing through the first helical channel.

[0094] According to aspect (26), a reactor according to any one of aspects (16) to (25) is provided, the reactor further comprising a central tube extending along the longitudinal axis of the reactor, wherein the first helical channel and the second helical channel are wound around the central tube, and wherein the central tube is configured to carry a heat exchange fluid.

[0095] According to aspect (27), a reactor according to any one of aspects (16) to (26) is provided, the reactor further comprising a shell disposed around the first helical channel and the second helical channel to form a cavity between the shell and the first helical channel and the second helical channel, wherein the cavity is configured to carry a heat exchange fluid.

[0096] According to aspect (28), a reactor according to any one of aspects (16) to (27) is provided, the reactor further comprising a permeable membrane that divides the first helical channel into a first passage and a second passage along the length of the first helical channel, wherein the permeable membrane is configured to control fluid flow between the first passage and the second passage.

[0097] According to aspect (29), a system is provided. The system comprises two or more reactors connected in series according to any one of aspects (1) to (15) or (16) to (28).

[0098] According to aspect (30), a system of aspect (29) is provided, wherein the two or more reactors include a first reactor and a second reactor, wherein the first reactor includes a first spacing between a plurality of first rings, wherein the second reactor includes a second spacing between the plurality of first rings, and wherein the first spacing is different from the second spacing.

[0099] According to aspect (31), a system as described in aspect (29) is provided, wherein the two or more reactors include a first reactor and a second reactor, wherein either or both of the first reactor and the second reactor include a spacing that varies across the plurality of first rings.

[0100] According to aspect (32), a system is provided according to any one of aspects (29) to (31), wherein the plurality of first rings of the first reactor includes a first maximum cross-sectional size, wherein the plurality of first rings of the second reactor includes a second maximum cross-sectional size, and wherein the first maximum cross-sectional size is different from the second maximum cross-sectional size.

[0101] According to aspect (33), a method is provided. The method includes: flowing a first fluid through a first helical channel, the first helical channel including a plurality of first turns wound around a longitudinal axis; flowing a second fluid through a second helical channel, the second helical channel including a plurality of second turns wound around the longitudinal axis, the plurality of second turns of the second helical channel alternating with the plurality of first turns of the first helical channel; and catalyzing a reaction in the first fluid using a catalyst disposed in the first helical channel.

[0102] According to aspect (34), the method of aspect (33) is provided, wherein the catalyst is coated on the inner surface of the first helical channel.

[0103] According to aspect (35), the method of aspect (33) is provided, wherein the catalyst comprises a plurality of beads or pellets.

[0104] According to aspect (36), a method is provided in any one of aspects (33) to (35), wherein causing the first fluid to flow further includes changing the velocity field of the first fluid flowing through the first helical channel, wherein the velocity field varies in direction and magnitude.

[0105] According to aspect (37), a method is provided in any one of aspects (33) to (36), wherein the first spiral channel includes a first cross-sectional flow area that varies along the length of the first spiral channel.

[0106] According to aspect (38), the method of aspect (37) is provided, wherein the second spiral channel includes a second cross-sectional flow area that varies along the length of the second spiral channel, and wherein the second cross-sectional area varies in opposite directions to the first cross-sectional area.

[0107] According to aspect (39), a method is provided in any one of aspects (33) to (38), wherein the first spiral channel is defined by a first wall having a first outer surface, wherein the second spiral channel is defined by a second wall having a second outer surface, and wherein the first outer surface contacts the second outer surface along the length of the first spiral channel.

[0108] According to aspect (40), a method is provided in any one of aspects (33) to (38), wherein the first spiral channel includes a first inner surface, wherein the second spiral channel includes a second inner surface, and wherein the first inner surface and the second inner surface share a common wall.

[0109] According to aspect (41), a method of any one of aspects (33) to (40) is provided, wherein causing the second fluid to flow further includes causing the second fluid to flow in a flow direction opposite to that of the first fluid.

[0110] According to aspect (42), a method is provided in any one of aspects (33) to (41), the method further comprising removing gas released from the first fluid during the flow of the first fluid.

[0111] According to aspect (43), a method is provided in any one of aspects (33) to (42), wherein causing the second fluid to flow further includes using the second fluid to control the temperature of the first fluid.

[0112] According to aspect (44), a method is provided in any one of aspects (33) to (43), the method further comprising flowing a heat exchange fluid through a central tube extending along a longitudinal axis, the first helical channel and the second helical channel being wound around the longitudinal axis.

[0113] According to aspect (45), a method is provided in any one of aspects (33) to (44), the method further comprising controlling the temperature of the first fluid by causing a heat exchange fluid to flow in a cavity defined by a housing disposed around the first helical channel and the second helical channel.

[0114] According to aspect (46), a method according to any one of aspects (33) to (45) is provided, wherein the first spiral channel includes a permeable membrane that divides the first spiral channel into a first passage and a second passage along the length of the first spiral channel, wherein the method further includes controlling a third fluid from the second passage to flow into the first fluid from the first passage.

[0115] According to aspect (47), a method is provided. The method includes: allowing a first fluid to flow through a first passage of a first helical channel, the first helical channel including a plurality of first turns wound around a longitudinal axis; allowing a second fluid to flow through a second passage of the first helical channel, wherein a permeable membrane separates the first passage from the second passage along the length of the first helical channel; allowing a third fluid to flow through a second helical channel, the second helical channel including a plurality of second turns wound around the longitudinal axis, the plurality of second turns of the second helical channel alternating with the plurality of first turns of the first helical channel; and using the permeable membrane to control the inflow of the second fluid into the first fluid.

[0116] According to aspect (48), the method of aspect (47) is provided, wherein the first passage has a first cross-sectional flow area and the second passage has a second cross-sectional flow area, and wherein the first cross-sectional flow area and the second cross-sectional flow area vary along the length of the first spiral passage.

[0117] According to aspect (49), the method of aspect (48) is provided, wherein the first cross-sectional flow area increases along the length of the first helical channel, and the second cross-sectional flow area decreases along the length of the first helical channel.

[0118] According to aspect (50), a method is provided in any one of aspects (47) to (49), wherein causing the first fluid to flow further comprises changing the velocity field of the first fluid flowing through the first passage of the first spiral channel, wherein the velocity field varies in direction and magnitude.

[0119] According to aspect (51), a method is provided in any one of aspects (47) to (50), wherein the first spiral channel is defined by a first wall having a first outer surface, wherein the second spiral channel is defined by a second wall having a second outer surface, and wherein the first outer surface contacts the second outer surface along the length of the first spiral channel.

[0120] According to aspect (52), a method is provided in any one of aspects (47) to (50), wherein the first spiral channel includes a first inner surface, wherein the second spiral channel includes a second inner surface, and wherein the first inner surface and the second inner surface share a common wall.

[0121] According to aspect (53), a method is provided in any one of aspects (47) to (52), wherein causing the third fluid to flow further includes causing the second fluid to flow in a flow direction opposite to that of the first fluid.

[0122] According to aspect (54), a method is provided in any one of aspects (47) to (53), the method further comprising removing gas released from the first fluid during the flow of the first fluid.

[0123] According to aspect (55), a method is provided in any one of aspects (47) to (54), wherein causing the third fluid to flow further includes using the third fluid to control the temperature of the first fluid.

[0124] According to aspect (56), a method is provided in any one of aspects (47) to (55), the method further comprising flowing a heat exchange fluid through a central tube extending along a longitudinal axis, the first helical channel and the second helical channel being wound around the longitudinal axis.

[0125] According to aspect (57), a method is provided in any one of aspects (47) to (56), the method further comprising controlling the temperature of the first fluid by causing a heat exchange fluid to flow in a cavity defined by a housing disposed around the first helical channel and the second helical channel.

[0126] According to aspect (58), a method is provided in any one of aspects (47) to (57), wherein the first helical channel includes a catalyst disposed in the first passage, and wherein the method further includes catalyzing a reaction in the first fluid using the catalyst.

[0127] It will be apparent to those skilled in the art that various modifications and variations can be made without departing from the scope or spirit of the disclosed embodiments. Since modifications, combinations, sub-combinations, and variations in the spirit and substance of the disclosed embodiments will be apparent to those skilled in the art, the disclosed embodiments should be understood to encompass all contents within the scope of the appended claims and their equivalents.

Claims

1. A reactor comprising: a first spiral channel comprising a plurality of first turns; a second spiral channel comprising a plurality of second turns, the plurality of second turns of the second spiral channel alternating with the plurality of first turns of the first spiral channel; and a permeable membrane dividing the first spiral channel into a first passageway and a second passageway along a length of the first spiral channel; wherein the permeable membrane is configured to control fluid flow between the first passageway and the second passageway.

2. The reactor of claim 1, wherein the first passageway has a first cross-sectional flow area and the second passageway has a second cross-sectional flow area, and wherein the first cross-sectional flow area and the second cross-sectional flow area vary along the length of the first spiral channel.

3. The reactor of claim 2, wherein the first cross-sectional flow area increases along the length of the first spiral channel and the second cross-sectional flow area decreases along the length of the first spiral channel.

4. The reactor of any one of claims 1 to 3, further comprising a first inlet in fluid communication with the first passageway and a second inlet in fluid communication with the second passageway, wherein the first inlet is configured to receive a first fluid and the second inlet is configured to receive a second fluid, and wherein the permeable membrane is configured to control mixing of the second fluid in the first fluid.

5. The reactor of claim 4, wherein the second spiral channel comprises a third inlet configured to receive a heat exchange fluid.

6. The reactor of claim 5, wherein the first inlet and the second inlet are disposed at a first end of the reactor and the third inlet is disposed at a second end of the reactor, the first end opposite the second end, such that flow of the first fluid and the second fluid through the first spiral channel is counter-current to flow of the heat exchange fluid through the second spiral channel.

7. The reactor of any one of claims 1 to 6, wherein the first spiral channel is configured to vary a velocity field of a fluid flowing through the first spiral channel, wherein the velocity field varies in direction and magnitude.

8. The reactor of any one of claims 1 to 7, wherein the first spiral channel is defined by a first wall having a first outer surface, wherein the second spiral channel is defined by a second wall having a second outer surface, and wherein the first outer surface is in contact with the second outer surface along the length of the first spiral channel.

9. The reactor of any one of claims 1 to 7, wherein the first spiral channel comprises a first inner surface, wherein the second spiral channel comprises a second inner surface, and wherein the first inner surface and the second inner surface share a common wall. ​ 10. The reactor of any one of claims 1-9, further comprising a center tube extending along a longitudinal axis of the reactor, wherein the first spiral passage and the second spiral passage are wrapped around the center tube, and wherein the center tube is configured to carry a heat exchange fluid.

11. The reactor of any one of claims 1-10, further comprising a shell disposed around the first spiral passage and the second spiral passage so as to form a cavity between the shell and the first spiral passage and the second spiral passage, wherein the cavity is configured to carry a heat exchange fluid.

12. The reactor of any one of claims 1-11, further comprising at least one tap in fluid communication with the first spiral passage, wherein the tap is configured to remove gas evolved during fluid flow through the first spiral passage.

13. The reactor of any one of claims 1-12, further comprising a catalyst disposed within the first passage.

14. The reactor of claim 13, wherein the catalyst is coated on an inner surface of the first passage.

15. The reactor of claim 13, wherein the catalyst comprises a plurality of beads or pellets.

16. A reactor, comprising: a first spiral passage comprising a plurality of first turns; a second spiral passage comprising a plurality of second turns, the plurality of second turns of the second spiral passage alternating with the plurality of first turns of the first spiral passage; and a catalyst disposed within the first spiral passage; wherein the catalyst is configured to promote a reaction in a fluid flowing through the first spiral passage.

17. The reactor of claim 16, wherein the catalyst is coated on an inner surface of the first spiral passage.

18. The reactor of claim 16, wherein the catalyst comprises a plurality of beads or pellets.

19. The reactor of any one of claims 16-18, wherein the first spiral passage is configured to vary a velocity field of a fluid flowing through the first spiral passage, wherein the velocity field varies in direction and magnitude.

20. The reactor of any one of claims 16-19, wherein the first spiral passage comprises a first cross-sectional flow area that varies along a length of the first spiral passage.

21. The reactor of claim 20, wherein the second spiral passage comprises a second cross-sectional flow area that varies along a length of the second spiral passage, and wherein the second cross-sectional area varies inversely to the first cross-sectional area.

22. The reactor of any one of claims 16-21, wherein the first spiral passage is defined by a first wall having a first outer surface, wherein the second spiral passage is defined by a second wall having a second outer surface, and wherein the first outer surface contacts the second outer surface along a length of the first spiral passage.

23. The reactor of any one of claims 16-21, wherein the first spiral passage comprises a first interior surface, wherein the second spiral passage comprises a second interior surface, and wherein the first interior surface and the second interior surface share a common wall.

24. The reactor of any one of claims 16-23, further comprising a first inlet in fluid communication with the first spiral passage at a first end of the reactor, wherein the second spiral passage comprises a second inlet configured to receive a heat exchange fluid, the second inlet disposed at a second end of the reactor opposite the first end, such that fluid flow through the first spiral passage is counter-current to flow of the heat exchange fluid through the second spiral passage.

25. The reactor of any one of claims 16-24, further comprising at least one tap in fluid communication with the first spiral passage, wherein the tap is configured to remove reaction evolved gas from the fluid flowing through the first spiral passage.

26. The reactor of any one of claims 16-25, further comprising a center tube extending along a longitudinal axis of the reactor, wherein the first spiral passage and the second spiral passage are wrapped around the center tube, and wherein the center tube is configured to carry a heat exchange fluid.

27. The reactor of any one of claims 16-26, further comprising an outer shell disposed around the first spiral passage and the second spiral passage so as to form a cavity between the outer shell and the first spiral passage and the second spiral passage, wherein the cavity is configured to carry a heat exchange fluid.

28. The reactor of any one of claims 16-27, further comprising a permeable membrane dividing the first spiral passage into a first passageway and a second passageway along a length of the first spiral passage, wherein the permeable membrane is configured to control fluid flow between the first passageway and the second passageway.

29. A system comprising two or more reactors connected in series according to any one of claims 1-15 or 16-28.

30. The system of claim 29, wherein the two or more reactors comprise a first reactor and a second reactor, wherein the first reactor comprises a first spacing between a plurality of first turns, wherein the second reactor comprises a second spacing between the plurality of first turns, and wherein the first spacing is different than the second spacing.

31. The system of claim 29, wherein the two or more reactors comprise a first reactor and a second reactor, wherein either or both of the first reactor and the second reactor comprise a spacing that varies across the plurality of first turns.

32. The system of any one of claims 29-31, wherein the plurality of first turns of the first reactor comprises a first maximum cross-sectional dimension, wherein the plurality of first turns of the second reactor comprises a second maximum cross-sectional dimension, and wherein the first maximum cross-sectional dimension is different than the second maximum cross-sectional dimension.

33. A method comprising: flowing a first fluid through a first spiral channel, the first spiral channel comprising a plurality of first turns wound about a longitudinal axis; flowing a second fluid through a second spiral channel, the second spiral channel comprising a plurality of second turns wound about the longitudinal axis, the plurality of second turns of the second spiral channel alternating with the plurality of first turns of the first spiral channel; catalyzing a reaction in the first fluid using a catalyst disposed in the first spiral channel.

34. The method of claim 33, wherein the catalyst is coated on an inner surface of the first spiral channel.

35. The method of claim 33, wherein the catalyst comprises a plurality of beads or pellets.

36. The method of any one of claims 33-35, wherein flowing the first fluid further comprises varying a velocity field of the first fluid flowing through the first spiral channel, wherein the velocity field varies in direction and magnitude.

37. The method of any one of claims 33-36, wherein the first spiral channel comprises a first cross-sectional flow area that varies along a length of the first spiral channel.

38. The method of claim 37, wherein the second spiral channel comprises a second cross-sectional flow area that varies along a length of the second spiral channel, and wherein the second cross-sectional area varies inversely to the first cross-sectional area.

39. The method of any one of claims 33-38, wherein the first spiral channel is defined by a first wall having a first outer surface, wherein the second spiral channel is defined by a second wall having a second outer surface, and wherein the first outer surface contacts the second outer surface along a length of the first spiral channel.

40. The method of any one of claims 33-38, wherein the first spiral channel comprises a first inner surface, wherein the second spiral channel comprises a second inner surface, and wherein the first inner surface and the second inner surface share a common wall.

41. The method of any one of claims 33-40, wherein flowing the second fluid further comprises flowing the second fluid in a flow direction opposite the first fluid.

42. The method of any one of claims 33-41, further comprising removing a gas evolved from the first fluid during flow of the first fluid.

43. The method of any one of claims 33-42, wherein flowing the second fluid further comprises using the second fluid to control a temperature of the first fluid.

44. The method of any one of claims 33-43, further comprising flowing a heat exchange fluid through a central tube extending along a longitudinal axis, the first spiral channel and the second spiral channel being wrapped around the longitudinal axis.

45. The method of any one of claims 33-44, further comprising controlling a temperature of the first fluid by flowing a heat exchange fluid in a cavity defined by an outer shell disposed around the first spiral channel and the second spiral channel.

46. The method of any one of claims 33-45, wherein the first spiral channel comprises a permeable membrane dividing the first spiral channel into a first passageway and a second passageway along a length of the first spiral channel, wherein the method further comprises controlling a flow of a third fluid from the second passageway into the first fluid from the first passageway.

47. A method comprising: flowing a first fluid through a first passageway of a first spiral channel, the first spiral channel comprising a plurality of first turns wrapped around a longitudinal axis; flowing a second fluid through a second passageway of the first spiral channel, wherein a permeable membrane separates the first passageway from the second passageway along a length of the first spiral channel; flowing a third fluid through a second spiral channel, the second spiral channel comprising a plurality of second turns wrapped around the longitudinal axis, the plurality of second turns of the second spiral channel alternating with the plurality of first turns of the first spiral channel; and controlling a flow of the second fluid into the first fluid using the permeable membrane.

48. The method of claim 47, wherein the first passageway has a first cross-sectional flow area and the second passageway has a second cross-sectional flow area, and wherein the first cross-sectional flow area and the second cross-sectional flow area vary along the length of the first spiral channel.

49. The method of claim 48, wherein the first cross-sectional flow area increases along the length of the first spiral channel and the second cross-sectional flow area decreases along the length of the first spiral channel.

50. The method of any one of claims 47-49, wherein flowing the first fluid further comprises varying a velocity field of the first fluid flowing through the first passageway of the first spiral channel, wherein the velocity field varies in direction and magnitude.

51. The method of any one of claims 47-50, wherein the first spiral channel is defined by a first wall having a first outer surface, wherein the second spiral channel is defined by a second wall having a second outer surface, and wherein the first outer surface contacts the second outer surface along a length of the first spiral channel.

52. The method of any one of claims 47-50, wherein the first spiral channel comprises a first inner surface, wherein the second spiral channel comprises a second inner surface, and wherein the first inner surface and the second inner surface share a common wall.

53. The method of any one of claims 47-52, wherein flowing the third fluid further comprises flowing the second fluid in a flow direction opposite the first fluid.

54. The method of any one of claims 47-53, further comprising removing gas evolved from the first fluid during flow of the first fluid.

55. The method of any one of claims 47-54, wherein flowing the third fluid further comprises using the third fluid to control a temperature of the first fluid.

56. The method of any one of claims 47-55, further comprising flowing a heat exchange fluid through a central tube extending along a longitudinal axis about which the first and second spiral channels are wrapped.

57. The method of any one of claims 47-56, further comprising controlling a temperature of the first fluid by flowing a heat exchange fluid in a cavity defined by an outer shell disposed about the first and second spiral channels.

58. The method of any one of claims 47-57, wherein the first spiral channel comprises a catalyst disposed in the first passageway, and wherein the method further comprises catalyzing a reaction in the first fluid using the catalyst.

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