Two-phase separator device incorporating inertial separation and porous media extraction

Abstract

To provide a phase separator device utilizing inertial separation and porous media extraction by a cyclone for the phase separation of a two-phase feed.SOLUTION: A phase separator device 10' comprises: a housing 16 extending from a first end to a second end, the housing having one or more first openings for first phase output 12 to exit and one or more second openings for second phase output to exit; and one or more guide vanes disposed in the housing. The housing includes an axial cyclone separation section 18 and a porous media section 22 through which an accumulated liquid flow is extracted through the liquid outlet and which prevents the flow of a gas flow to the liquid outlet. The axial cyclone separation section and the porous media section are configured and dimensioned to separate an input feed 11 introduced into the housing into first phase output and second phase output.SELECTED DRAWING: Figure 8

Description

[Technical field]

[0001] CROSS-REFERENCE TO RELATED APPLICATIONS This application claims the benefit of priority to (i) a provisional application having assigned Serial No. 62 / 928,912, filed on October 31, 2019, and (ii) a provisional application having assigned Serial No. 63 / 010,299, filed on April 15, 2020. The entire contents of both of the foregoing provisional applications are incorporated herein by reference.

[0002] The present disclosure relates to phase separator devices for phase separation of an input feed and systems / methods for utilizing and manufacturing phase separator devices, and more particularly, to phase separator devices that utilize inertial separation and porous media extraction for phase separation of a two-phase input feed (e.g., to separate the input feed of a two-phase mixture into a first phase output (e.g., into a liquid output stream) and a second phase output (e.g., into a gas output stream)). [Background technology]

[0003] In general, there are numerous applications for structures and assemblies for phase separation of an input feed.

[0004] There is an interest in improved systems and methods for phase separation of an input feed.

[0005] These and other inefficiencies and opportunities for improvement are addressed and / or overcome by the systems, methods and devices of the present disclosure. Summary of the Invention

[0006] The present disclosure provides advantageous phase separator devices for phase separation of an input feed, as well as improved systems / methods for utilizing and manufacturing the phase separator devices. More specifically, the present disclosure relates to phase separator devices utilizing inertial separation and porous media extraction for phase separation of a two-phase input feed (e.g., to separate the input feed of a two-phase mixture into a first phase output (e.g., into a liquid output stream) and a second phase output (e.g., into a gas output stream)). The phase separator devices can be utilized in standard gravity, microgravity, and zero gravity environments.

[0007] The present disclosure provides a phase separator device including a housing extending from a first end to a second end, the housing having one or more first openings through which a first phase output exits and one or more second openings through which a second phase output exits, and one or more guide vanes disposed in the housing, the housing including an axial cyclonic separation section and a porous media section, the axial cyclonic separation section and the porous media section configured and dimensioned to separate an input feed introduced into the housing into a first phase output and a second phase output.

[0008] The present disclosure provides a phase separator device, the phase separator device including one or more extractor elements disposed in a housing, the housing having an inlet for an input feed, a first outlet for a first phase output, and a second outlet for a second phase output, each extractor element including a threaded rod housed in a porous media tube, the one or more extractor elements configured and dimensioned to separate an input feed introduced at the inlet into a first phase output and a second phase output.

[0009] The present disclosure provides a phase separator device including a housing extending from a first end to a second end, the housing having one or more first openings through which a first phase output exits and one or more second openings through which a second phase output exits, and one or more guide vanes disposed in the housing, the housing including a countercurrent cyclone separation section and a porous media section, the countercurrent cyclone separation section and the porous media section configured and dimensioned to separate an input feed introduced into the housing into a first phase output and a second phase output.

[0010] The above described and other features are illustrated by the following drawings and detailed description.

[0011] Any combination or permutation of the embodiments is contemplated. Additional advantageous features, functions, and applications of the disclosed systems, methods, and devices of the present disclosure will become apparent from the following description, particularly when read in conjunction with the accompanying drawings. All references cited in this disclosure are incorporated herein by reference in their entirety.

[0012] The following figures are exemplary embodiments in which like elements are similarly numbered.

[0013] Features and aspects of the embodiments are described below with reference to the accompanying drawings, in which elements are not necessarily drawn to scale.

[0014] Exemplary embodiments of the present disclosure are further described with reference to the accompanying drawings. It should be noted that the various features, steps, and combinations of features / steps described below and illustrated in the drawings can be arranged and organized differently to result in embodiments that are still within the scope of the present disclosure. Reference is made to the accompanying drawings to assist those skilled in the art in making and using the disclosed systems, methods, and devices. [Brief description of the drawings]

[0015] [Figure 1] 1 illustrates inertial separation for cyclonic separation of a denser phase from a lighter gas phase. [Diagram 2] FIG. 1 is a diagram of an axial flow separator. [Diagram 3] FIG. 1 is a diagram of one stage of a five-stage cascade axial cyclone. [Figure 4] Component images for one stage of a five-stage cascade axial cyclone. [Diagram 5] Particle separation (collection efficiency) is shown as a function of particle size for each stage of a five-stage cascade axial cyclone. [Figure 6] FIG. 1 is a diagram of an exemplary phase separator device (e.g., a two-phase axial flow cyclone separator device with an axial inlet for the input feed) according to the present disclosure. [Figure 7] FIG. 7 is another view of the phase separator device of FIG. 6. [Figure 8] FIG. 2 is a diagram of another exemplary phase separator device (e.g., a two-phase axial flow cyclone separator device with a tangential inlet for the input feed) according to the present disclosure. [Figure 9] FIG. 2 is a diagram of another exemplary phase separator device (e.g., a two-phase counter-flow cyclone separator device with a tangential inlet for the input feed) according to the present disclosure. [Figure 10] FIG. 2 is a diagram of another exemplary phase separator device (e.g., a two-phase counter-flow cyclone separator device with an axial inlet for the input feed) according to the present disclosure. [Figure 11] FIG. 11 is another view of the phase separator device of FIG. [Figure 12] A radial / spiral flow path element designed to separate and extract one phase (eg, liquid) from a two-phase input feed (eg, a two-phase fluid input feed such as liquid and vapor). [Figure 13] FIG. 1 is another exemplary phase separator device of the present disclosure showing a cross-sectional view showing a two-phase inlet on the left, a first phase outlet (e.g., vapor phase outlet) on the right, and a second phase outlet (e.g., liquid phase outlet) at the top, where a central housing contains multiple (e.g., 31) parallel flow paths for fluid flow and separation. [Figure 14A] 14 is an additional drawing showing another view of the exemplary phase separator device of FIG. 13 utilizing multiple (e.g., 31) parallel flow separator elements within the separator main housing; FIG. 15 is a view of a phase separator device utilizing a radial / swirl liquid extractor. [Figure 14B] 14 is an additional drawing showing another view of the exemplary phase separator device of FIG. 13 utilizing multiple (e.g., 31) parallel flow separator elements within the separator main housing; FIG. 15 is a view of a phase separator device utilizing a radial / swirl liquid extractor. [Figure 14C] 14 is an additional drawing showing another view of the exemplary phase separator device of FIG. 13 utilizing multiple (e.g., 31) parallel flow separator elements within the separator main housing; FIG. 15 is a view of a phase separator device utilizing a radial / swirl liquid extractor. [Figure 14D] 14 is an additional drawing showing another view of the exemplary phase separator device of FIG. 13 utilizing multiple (e.g., 31) parallel flow separator elements within the separator main housing; FIG. 15 is a view of a phase separator device utilizing a radial / swirl liquid extractor. [Figure 14E] 14 is an additional drawing showing another view of the exemplary phase separator device of FIG. 13 utilizing multiple (e.g., 31) parallel flow separator elements within the separator main housing; FIG. 15 is a view of a phase separator device utilizing a radial / swirl liquid extractor. [Figure 15] FIG. 14 shows an isometric view of the phase separator device of FIG. 13. [Figure 16] 1 is another exemplary phase separator device according to the present disclosure. [Figure 17] 1 shows a porous medium within a spiral cavity of a phase separator device according to the present disclosure. [Figure 18] 1 illustrates a spiral passage of a phase separator device according to the present disclosure. [Figure 19] 1 illustrates the orientation of the inlet and outlet of a phase separator device according to the present disclosure. [Figure 20] 1 shows a schematic diagram of an exemplary custom test stand. [Figure 21]1 is a graph showing predicted gas phase pressure drop versus quality calculated using the analytical model and experimentally measured values ​​for Design A. [Figure 22] 1 is a graph showing predicted liquid phase pressure drop quality calculated using the analytical model and experimentally measured values ​​of Design A. [Figure 23] 13 is a graph showing predicted gas phase pressure drop versus quality calculated using the analytical model and experimentally measured values ​​of Design C. [Figure 24] 1 is a graph showing predicted liquid phase pressure drop versus quality calculated using an analytical model and experimentally measured values. DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS

[0016] The exemplary embodiments disclosed herein illustrate advantageous phase separator devices and systems of the present disclosure, as well as methods / techniques thereof. However, it should be understood that the disclosed embodiments are merely exemplary of the present disclosure, which may be embodied in various forms. Thus, the details disclosed herein with reference to the exemplary phase separator devices and associated processes / techniques of assembly and application should not be construed as limiting, but merely as a basis for teaching those skilled in the art how to make and use the advantageous phase separator devices of the present disclosure and / or alternative phase separator devices.

[0017] The present disclosure provides advantageous phase separator devices for phase separation of an input feed, as well as improved systems / methods for utilizing and manufacturing the phase separator devices.

[0018] More specifically, the present disclosure relates to a phase separator device that utilizes inertial separation and porous media extraction for phase separation of a two-phase input feed (e.g., to separate the input feed of a two-phase mixture into a first phase output (e.g., into a liquid output stream) and a second phase output (e.g., into a gas output stream)). The phase separator device can be utilized in standard gravity, microgravity, and zero gravity environments.

[0019] An exemplary phase separator device (e.g., a two-phase flow separator device) of the present disclosure incorporates inertial separation and porous media extraction. The device separates a two-phase input feed (e.g., a two-phase fluid stream) into a first phase output and a second phase output (e.g., a fluid output stream for each phase). In certain embodiments, the device can separate mixed fluid streams of both liquids and gases. The liquids and gases may include liquid and vapor phases of the same chemical / component (e.g., ammonia) or may include liquids and gases of two different components (e.g., liquid water and air).

[0020] The two-phase input feed (eg, the two-phase input stream) may be at room temperature (eg, about 20-25 degrees Celsius) or may be at other operating temperatures.

[0021] The two-phase input feed / stream can be at atmospheric pressure (e.g., nominally 1 atmosphere) or can be at higher or lower pressure. For example, the exemplary phase separator device may be utilized for separation of a two-phase input / stream / mixture that flows or is input as a compressed fluid in a partial or fully closed loop system.

[0022] The two-phase flow / input can be in standard gravity to microgravity to zero gravity environments. Note that separation, capture, and extraction of the liquid (or solid) phases can be much more complicated in microgravity to zero gravity environments since gravity (the force of Earth's gravitational force) typically cannot be used in such separation, capture, and extraction processes.

[0023] In an exemplary embodiment, the role of the phase separator device is to achieve separation of the first and second phases (e.g., liquid and gas phases) by utilizing the only difference between the properties of the first phase output (e.g., liquid output) and the second phase output (e.g., gas component) in a two-phase input / mixture, particularly by employing differences in density and / or capillary forces.

[0024] In certain embodiments, of interest is the separation and capture of the liquid phase. There are several approaches / techniques that can be employed to separate the liquid, including (i) cooling the two-phase mixture to condense the fluids, (ii) using de-misters, (iii) using inertial separators such as cyclones or impactors, and (iv) using wicks to extract the liquid phase.

[0025] With respect to inertial separation, it is noted that separation of a second phase (e.g., a gas phase) from a first phase (e.g., a liquid phase and / or a solid phase) can be achieved via inertial properties to separate a denser phase (e.g., a liquid phase and / or a solid phase) from a lighter phase (e.g., a gas phase) in an incoming input feed (e.g., an incoming two-phase fluid stream).

[0026] The effectiveness of inertial separation increases with increasing mass (density) of the denser phase (e.g., liquid droplets or solid particles) compared to the lighter phase (e.g., gas density). This effectiveness also increases with decreasing gas viscosity. Inertial separation techniques can be utilized in devices such as cyclones, centrifuges, impactors, and particle collectors.

[0027] Referring now to the drawings, in which like parts are respectively designated with the same reference numerals throughout the specification and drawings, the drawings are not necessarily to scale and in certain drawings parts may be exaggerated for purposes of clarity.

[0028] As shown in Figure 1, the effectiveness of separation is increased by increasing the inertia of the denser phase (e.g., liquid or solid particles) in the separation device by increasing its velocity. Furthermore, separation is also increased in cyclone separation by decreasing the radius of curvature in the fluid passages (e.g., decreasing the radius of the separator housing).

[0029] With regard to axial flow separators (e.g., axial flow cyclones), it is noted that an axial flow cyclone design is illustrated in FIG. 2. The function of an axial flow cyclone is to separate the denser phase (e.g., liquid or solid particles such as dust) present in the incoming input feed (e.g., incoming gas stream) from the feed, provide a cleaned lighter output phase (e.g., gas stream or clean gas), and provide a denser output (e.g., liquid or solid particle stream). In an axial flow cyclone, the incoming input feed (e.g., gas stream) and the cleaned lighter phase output (cleaned gas stream) can be on the same axis with the gas stream entering and exiting in the same traveling direction. Some of the main components of an axial flow cyclone are a cylindrical housing, one or more guide vanes, and an outlet passage (opening) for the cleaned gas and separated liquid or solid particles.

[0030] Axial cyclone technology is primarily employed in products for the separation of particles (solid or liquid) from gas streams in industrial applications, or air intakes for engines and buildings. Axial cyclones remove larger particles in the incoming gas stream for subsequent collection and application. In other applications, axial cyclones remove a portion of the particles in the gas stream and act as a pre-cleaner for further particle collection (e.g., filters), thereby extending the life of the filter.

[0031] Figures 3 and 4 show the design of one stage of a five-stage cascaded axial cyclone used to collect solid particles (e.g., dust) for subsequent use in size fractionation samples. Figure 5 shows particle separation (collection efficiency) as a function of particle size for each stage of a five-stage cascaded axial cyclone. In this example, the five stages were able to achieve separation and collection of particles as small as 1 micrometer. Collection efficiency for each stage was achieved by varying the guide vane pitch angle, the inner and outer diameters of the guide vanes and the cyclone housing.

[0032] 6 illustrates an exemplary design and configuration of an embodiment of a phase separator device 10 (e.g., a two-phase axial flow cyclone separator device 10) for an input feed 11 (e.g., for a liquid / gas mixture input feed 11). As shown in FIG. 6, the device 10 takes the form of a two-phase axial flow cyclone separator device 10 with an axial inlet 13 for the input feed 11. The phase separator device 10 is thus configured and dimensioned to be utilized for phase separation of the input feed 11 (two-phase mixture 11) into a first phase output 12 (e.g., to a liquid output stream 12) and to a second phase output 14 (e.g., to a gas output stream 14).

[0033] More specifically, the phase separator device 10, discussed further below, includes a housing 16 extending from a first end to a second end, the housing 16 having one or more first openings through which the first phase output 12 exits and one or more second openings through which the second phase output 14 exits. One or more guide vanes 24 are disposed within the housing 16 of the phase separator device 10. As noted above, the device 10 includes an axial inlet 13 for the input feed 11. FIG. 7 shows another depiction of the phase separator device 10 of FIG. 6 (e.g., a two-phase axial flow cyclone separator device 10 with an axial inlet 13 for the input feed 11).

[0034] In general, the phase separator device 10 is configured and dimensioned to separate a darker phase (e.g., liquid phase) present in the input feed 11 from the incoming input feed 11 and provide a cleaned lighter phase output 14 (e.g., second phase output 14) and a darker output 12 (e.g., liquid stream at first phase output 12). The incoming input feed 11 and the outgoing cleaned second phase output 14 may be on the same axis as the incoming and outgoing gas streams / input feed 11 in the same traveling direction.

[0035] The design of the exemplary phase separator device 10 can utilize two distinct sections, and may utilize a third section, to accomplish the separation, collection, and extraction of the first phase output 12 (liquid phase) from the second phase output 14 (gas phase). These sections may include an axial flow cyclone separation section 18, an optional liquid collection section 20 prior to a porous media section 22, and / or a porous media section 22 for liquid extraction.

[0036] The role of the porous media section 22 is to form a porous barrier that performs at least three important functions. First, section 22 acts as a barrier to allow liquid accumulation and physically supports the layer of liquid accumulation. Second, the pressure drop across this liquid layer and the porous membrane 22 prevents gas flow to the liquid outlet because the pressure drop is much lower in the gas (vapor) outlet passage. Third, the porous media section 22 allows the flow of accumulated liquid to be extracted through the liquid outlet. The liquid can be extracted via a suction pump located downstream of the liquid outlet and / or can utilize upstream pressure in a pressurized system.

[0037] The porous media section 22 may be located in one or more locations in the axial flow separator device 10. As illustrated in Figure 6, the porous media section 22 is located at the bottom, e.g., wall or bottom, of the annular collection section located downstream of the guide vanes 24. The porous media section 22 may also be located in the wall of the cylindrical housing 16 adjacent to or just downstream of the vanes.

[0038] The porous media section 22 can be made from several types of porous materials including, but not limited to, porous metals, polymeric membranes, foams, fibrous materials, polymers, ceramics, and / or glasses. The porous metals can be materials from several metal alloys including, but not limited to, nickel, cobalt, iron, copper, aluminum, palladium, titanium, tungsten, platinum, silver, gold, and stainless steels, as well as nickel-based steels such as Hastelloy® (Haynes Stellite Company, Kokomo, Indiana).

[0039] The average pore size of the porous media section 22 can be as low as 0.1 microns and as high as 100 microns (eg, depending on the fluid conditions, temperature, and / or fluid viscosity).

[0040] In some embodiments, the inside diameter of the cyclone housing 16 can range from about 0.5 to about 20 inches.

[0041] In certain embodiments, two or more parallel axial flow separator devices 10 may be employed in a parallel arrangement that may be required to split an incoming mixed two-phase flow 11 into two or more parallel flows.

[0042] 8, the device 10′ takes the form of a two-phase axial flow cyclone separator device 10′ with a tangential inlet 15 for the input feed 11. The phase separator device 10′ with the tangential inlet 15 is thus configured and dimensioned to be utilized for phase separation of the input feed 11 (two-phase mixture 11) into a first phase output 12 (e.g., into a liquid output stream 12) and into a second phase output 14 (e.g., into a gas output stream 14).

[0043] Similar to device 10, phase separator device 10' includes a housing 16 extending from a first end to a second end, the housing 16 having one or more first openings through which the first phase output 12 exits and one or more second openings through which the second phase output 14 exits. One or more guide vanes 24 may be disposed within the housing 16 of the phase separator device 10'. As noted above, device 10' includes a tangential inlet 15 for the input feed 11.

[0044] Similar to the operation of device 10, phase separator device 10' is configured and dimensioned to separate a darker phase (e.g., liquid phase) present in input feed 11 from the incoming input feed 11 and provide a cleaned lighter phase output 14 (e.g., second phase output 14) and a darker output 12 (e.g., liquid stream in first phase output 12). The incoming input feed 11 and the outgoing cleaned second phase output 14 may be on different axes, with the gas flow / input feed 11 entering via a tangential inlet 15 tangent to the axis exiting the cleaned second phase output 14. As similarly discussed with respect to device 10, device 10' with tangential inlet 15 may include an axial cyclone separation section 18, an optional liquid collection section 20 prior to the porous media section 22, and / or a porous media section 22 for liquid extraction. As also discussed, the porous media section 22 of the device 10' may be located in one or more locations in the device 10', and the porous media section 22 may be fabricated from several types of porous materials.

[0045] It should be noted that exemplary cyclone separator devices of the present disclosure (e.g., devices 10, 10', 300, 300') can be categorized based on their fluid inlet configurations (13, 15, 313, 315) and the overall flow path through the cyclone separator device. Figures 7-10 show four exemplary combinations of inlet designs (13, 15, 313, 315) and flow directions for the input (11, 311) and output (12, 14, 312, 314) fluid streams. Figures 9-10 are discussed in more detail below.

[0046] These four exemplary combinations of Figures 7-10 may be referred to as (i) axial inlet axial flow cyclone separator device 10 (Figure 7), (ii) tangential inlet axial flow cyclone separator device 10' (Figure 8), (iii) axial inlet counterflow cyclone separator device 300 (Figure 10), and (iv) tangential inlet counterflow cyclone separator device 300' (Figure 9).

[0047] It should be noted that there are numerous sub-variations of these four exemplary configurations, as depicted in Figures 7-10. For example, one potential set of sub-variations can address the location of the outlets (12, 14, 312, 314) for the separated materials. For example, but not limited to, these outlets can be axially located at the bottom or sidewalls near the bottom end of the cyclone separator device (e.g., 12, 14, 312).

[0048] With reference to the axial inlet 13, 313 and the tangential inlet 15, 315, it is noted that both of these two inlet configurations create the high speed swirling motion required to separate, via centripetal forces, the higher mass components contained in the incoming mixed fluid stream 11, 311. For example, these inlet configurations may be (i) a tangential inlet (15, 315 in Figs. 8 and 9) where the incoming fluid stream 11, 311 enters tangentially into the top of the cylindrical cyclone separator device 10', 300', and (ii) an axial inlet (13, 313 in Figs. 7 and 10) where the incoming fluid stream 11, 311 passes through a set of swirling (guide) vanes 24.

[0049] The overall flow paths through the exemplary separator devices may be classified as: (i) axial flow (devices 10, 10' of Figures 7 and 8); and (ii) counter-flow (devices 300, 300' of Figures 9 and 10).

[0050] In an axial flow separator configuration (device 10, 10' of Figures 7 and 8), the incoming fluid stream 11 and the outgoing cleaned / separated fluid stream 14 may be on the same axis as the outgoing gas / input stream 11 and cleaned / separated stream 14 in the same traveling direction. In a counter-flow separator configuration (device 300, 300' of Figures 9 and 10), the flow path of the cleaned / separated fluid 314 undergoes a 180 degree reversal in its axial flow direction as the fluid 314 enters the lower portion of the separator housing 316 and then exits in the opposite direction through an outlet tube located in the upper section of the separator device 300, 300'.

[0051] It should be noted that each of these four exemplary cyclone separator device configurations 10, 10', 300, 300' can be combined with a porous media 22, 322 to produce an advantageous two-phase separator device 10, 10', 300, 300' as provided by the present disclosure.

[0052] 6 and 10 / 11 illustrate two examples of two design embodiments of a two-phase flow cyclone separator device 10, 300 (e.g., for liquid / gas mixtures). Both designs 10, 300 utilize two different sections, and may utilize a third to achieve separation, collection, and extraction of the liquid phase from the gas phase. These sections may include a cyclone separation section 18 (axial flow), 318 (counterflow), an optional liquid collection section 20, 320 before the porous media section 22, 322, and / or a porous media section 22, 322 for liquid extraction with a liquid extraction section below the porous media section 22, 322.

[0053] In an embodiment, as shown in Figures 10 and 11, an exemplary phase separator device 300 (e.g., a two-phase counter-current cyclone separator device 300 with an axial inlet 313 for the input feed) utilizes radial flow turning (guiding) vanes 324 coupled with the design of the counter-current cyclone separator device 300. Figure 11 illustrates such a configuration. It should be noted that, as discussed further below, device 300 includes several similar components to device 10, and such similar components of device 300 can function in a similar manner as such similar components of device 10.

[0054] The main difference between device 300 versus device 10 is the location for the exit of the gas phase (314) and liquid phase (312). In a counter-flow design as depicted in Figures 10 and 11 (e.g., two-phase counter-flow cyclone separator device 300 with axial inlet 313 for the input feed), the gas undergoes a reversal of its flow direction (e.g., a 180 degree turn) and thereby exits in the opposite direction to the incoming fluid 311. The separated liquid stream 312 now passes through a porous media section 322 (e.g., a section 322 shaped as a disk rather than an annular shaped porous media 22), which can be located at the bottom or side of the housing 316. In either case, a porous media membrane 322 is utilized to form an imperious barrier to the vapor and to support the liquid layer 320.

[0055] As noted above, Figure 11 illustrates an exemplary design and configuration of an embodiment of a phase separator device 300 (e.g., a two-phase counter-current separator device 300) for an input feed (e.g., for an input feed of a liquid / gas mixture). As shown in Figure 11, the device 300 takes the form of a two-phase counter-current cyclone separator device 300 with an axial inlet 313 for the input feed 311. Thus, the phase separator device 300 is configured and dimensioned to be utilized for phase separation of the input feed 311 (two-phase mixture 311) into a first phase output 312 (e.g., to a liquid output stream 312) and a second phase output 314 (e.g., to a gas output stream 314).

[0056] More specifically, the phase separator device 300, discussed further below, includes a housing 316 extending from a first end to a second end, the housing 316 having one or more first openings through which the first phase output 312 exits and one or more second openings through which the second phase output 314 exits. One or more turning (guide) vanes 324 positioned in series are disposed within the housing 316 of the phase separator device 300.

[0057] In general, the phase separator device 300 is configured and dimensioned to separate a darker phase (e.g., liquid phase) present in the input feed 311 from the incoming input feed 311 and provide a cleaned lighter phase output 314 (e.g., second phase output 14) and a darker output 312 (e.g., liquid stream in first phase output 312). The incoming input feed 311 and the cleaned second phase output 314 can be on the same axis as the gas / input feed 311, however, the input feed 311 and output 314 exit in opposite directions.

[0058] The design of the exemplary phase separator device 300 can utilize two distinct sections, and may utilize a third section, to accomplish the separation, collection, and extraction of the first phase output 312 (liquid phase) from the second phase output 314 (gas phase). These sections can include a countercurrent cyclone separation section 318, an optional liquid collection section 320 prior to a previous media section 322, and / or a porous media section 322 for liquid extraction.

[0059] The exemplary device 300 may utilize an optional conical skirt 328, which is located on the outside of the gas outlet tube 326 and below the swirler 324. One or more skirts 328 may be incorporated into the design of the device 300. The function of the skirt is to improve liquid separation efficiency by directing the liquid against the outer wall of the separator housing 316 and away from the inlet to the gas outlet tube. Note that the devices 10, 10', 300' may also utilize an optional conical skirt similar to the conical skirt 328.

[0060] Similar to the device 10 discussed above, the design of the exemplary phase separator device 300 can utilize two distinct sections, and may utilize a third section, to achieve separation, collection, and extraction of the first phase output 312 (liquid phase) from the second phase output 314 (gas phase). These sections can include a countercurrent cyclone separation section 318, an optional liquid collection section 320 prior to a porous media section 322, and / or a porous media section 322 for liquid extraction.

[0061] Similar to section 22, the role of porous media section 322 is to form a porous barrier that performs at least three important functions. First, section 322 acts as a barrier to allow liquid accumulation, providing physical support to the layer of liquid accumulation. Second, the pressure drop across this liquid layer and porous membrane 322 prevents gas flow to the liquid outlet since the pressure drop is much lower in the gas (vapor) outlet passage. Third, porous media section 322 allows the flow of accumulated liquid to be extracted through the liquid outlet. Liquid can be extracted via a suction pump located downstream of the liquid outlet and / or can utilize upstream pressure in a pressurized system.

[0062] The porous media section 322 may be located in one or more locations in the axial flow separator device 300. As shown in FIG. 11, the porous media section 322 is located at the bottom, e.g., at the wall or bottom, and is located downstream of the guide vanes 324. It should be noted that the exemplary section 322 can be formed as a disk or the like, although the disclosure is not limited thereto. The porous media section 322 can also be located / located at and / or beyond the wall of the cylindrical housing 316 adjacent to or just downstream from the vanes.

[0063] The porous media section 322 can be made from several types of porous materials, including but not limited to porous metals, polymeric membranes, foams, fibrous materials, polymers, ceramics, and / or glasses. The porous metals may be materials from several metal alloys, including but not limited to nickel, cobalt, iron, copper, aluminum, palladium, titanium, tungsten, platinum, silver, gold, and stainless steels, as well as nickel-based steels such as Hastelloy® (Haynes Stellite Company, Kokomo, Indiana).

[0064] The average pore size of the porous media section 322 can be as low as 0.1 microns and as high as 100 microns (eg, depending on the fluid conditions, temperature, and / or fluid viscosity).

[0065] In some embodiments, the inner diameter of the cyclone housing 316 can range from about 0.5 to about 20 inches.

[0066] In certain embodiments, two or more parallel axial flow separator devices 300 may be employed in a parallel arrangement that may be required to split the incoming mixed two-phase flow 311 into two or more parallel flows.

[0067] 9, the device 300′ takes the form of a two-phase counter-flow cyclone separator device 300′ with a tangential inlet 315 for the input feed 311. The phase separator device 300′ with the tangential inlet 315 is thus configured and dimensioned to be utilized for phase separation of the input feed 311 (two-phase mixture 311) into a first phase output 312 (e.g., into a liquid output stream 312) and into a second phase output 314 (e.g., into a gas output stream 314).

[0068] Similar to device 300, phase separator device 300' includes a housing 316 extending from a first end to a second end, the housing 316 having one or more first openings through which a first phase output 312 exits and one or more second openings through which a second phase output 314 exits. One or more guide vanes 324 may be disposed within the housing 316 of phase separator device 300'. As above, device 300' includes a tangential inlet 315 for input feed 311.

[0069] Similar to the operation of device 300, phase separator device 300' is configured and dimensioned to separate a darker phase (e.g., liquid phase) present in input feed 311 from the incoming input feed 311 and provide a cleaned lighter phase output 314 (e.g., second phase output 314) and a darker output 312 (e.g., liquid stream in first phase output 312). The incoming input feed 311 and the outgoing cleaned second phase output 314 may be on different axes, with the gas flow / input feed 311 entering via a tangential inlet 315 tangent to the axis exiting the cleaned second phase output 314. As similarly discussed for device 300, device 300' with tangential inlet 315 may include a countercurrent cyclone separation section 318, an optional liquid collection section 320 prior to porous media section 322, and / or a porous media section 322 for liquid extraction. As also discussed, the porous media section 322 of the device 300' may be disposed in one or more locations in the device 300', and the porous media section 322 may be fabricated from several types of porous materials.

[0070] FIG. 12 shows a radial / swirl liquid phase extractor element 128. FIG. 12 shows the element 128 used to separate the liquid phase from the flowing two-phase fluid 111 (liquid and vapor input 111 - FIG. 13). In an exemplary embodiment, one can take a threaded rod 124 and enclose it in a porous media tube 126. The two-phase fluid 111 follows the spiral flow path shown in FIG. 12, and the inertial energy due to the circular flow path causes the denser fluid (e.g., liquid) to move radially outward and the less dense fluid (e.g., vapor) to move inward. This separation places the liquid phase in intimate contact with the porous tube 126, etc. A pressure difference is then applied between the inner flow path and the outer volume of the porous tube 126, causing liquid flow through the porous tube 126. The magnitude of this pressure differential, the diameter and length of element 128, the thread pitch and groove dimensions, wetted surface area, thickness and density, and the average pore size of tube 126 can all be adjusted to provide nearly 100% efficiency in capturing the liquid phase and extracting it from element 128.

[0071] In an exemplary embodiment, the diameter of the threaded component 124 can be very small (on the order of 1 / 16 inch) to very large (several feet) depending on the flow rate of the two-phase fluid and the allowable pressure drop. The thickness of the porous tube 126 can range from 0.10 inch to several inches depending on the application. The average pore size in the tube 126 can be as low as 0.1 microns and as high as 100 microns depending on the flow conditions, temperature, and / or fluid viscosity.

[0072] For the embodiments disclosed herein, the dimensions of the spiral channel and the porous media may remain constant along the length of the channel. It is recognized that improved separation performance can be obtained by varying the dimensions of the spiral channel, including the cross section and pitch along the fluid flow path. Furthermore, the thickness of the porous media can also be adjusted along the length of the channel to improve phase separation. For the embodiments disclosed herein, the porous media may have a constant average pore size and density, and further optimization of performance can be achieved using a gradient pore size distribution within the porous media.

[0073] As shown in FIG. 13, to utilize a liquid extraction element 128 (or multiple elements 128), the element 128 can be inserted into a housing 116 that provides one inlet for the input feed 111 (liquid-vapor mixture feed 111) and two outlets, one for the first phase output 112 (e.g., liquid output) and one for the second phase output 114 (e.g., vapor). Each element 128 of the phase separator device 100 induces the two-phase fluid 111 entering the inlet for the feed 111 to direct flow into a spiral flow path at one end (the input 111 end) of each element 128. A gas outlet for the second phase output 114 of the device 100 can be connected to the opposite end of each element 128. A second outlet for the first phase output 112 (e.g., liquid) can be attached to the housing 116 surrounding each element 128, and the second outlet for the first phase output 112 (e.g., liquid) can receive the liquid phase flowing through the various porous media 126.

[0074] The porous media 126 can be made from several types of porous materials, including but not limited to, porous metals, polymeric membranes, foams, fibrous materials, polymers, ceramics, and / or glasses. The porous metals can be materials from several metal alloys, including but not limited to, nickel, cobalt, iron, copper, aluminum, palladium, titanium, tungsten, platinum, silver, gold, and stainless steels, as well as nickel-based steels such as Hastelloy® (Haynes Stellite Company, Kokomo, Indiana).

[0075] The device 100 may include a single element 128 as described above, or the device 100 may include multiple elements 128 in either a series and / or parallel flow path configuration. Depicted in Figure 13 is such an exemplary device 100 that includes 31 liquid phase separator elements 128, the elements 128 being in a parallel flow path configuration.

[0076] FIG. 16 shows a phase separator device 200 used to separate phases from a flowing two-phase fluid 211 (liquid and vapor). The design is a spiral passage, possibly with a non-constant surface area, one surface of the passage is a porous medium as shown in FIG. 17. The mixed phase fluid 211 enters the spiral passage tangentially as shown in FIG. 16 and FIG. 19. The two-phase fluid 211 follows the spiral flow path shown in FIG. 18, and only the liquid phase exits the spiral passage tangentially via the output 212. The centripetal force due to the circular flow path causes the denser fluid with more inertia (liquid) to move radially outwards, and therefore the less dense fluid with more inertia (vapor) to move inwards. This separation puts the gas phase in intimate contact with the porous medium. The other side of the porous medium provides a pressure differential that causes the gas to flow through the porous medium at a lower pressure. The gas phase exits at both ends via output 214, spiraling along the central axis and is collected via additional piping (not shown).

[0077] The diameter, length, convolution pitch, convolution dimensions, thickness, density, and average pore size of the porous medium of device 200 can be varied based on the application of device 200 and the requirements of the input / fluid 211 to be separated.

[0078] The porous media of device 200 can be made from several types of porous materials, including but not limited to porous metals, polymeric membranes, foams, fibrous materials, polymers, ceramics, and / or glasses. The porous metals may be materials from several metal alloys, including but not limited to nickel, cobalt, iron, copper, aluminum, palladium, titanium, tungsten, platinum, silver, gold, and stainless steels, as well as nickel-based steels such as Hastelloy® (Haynes Stellite Company, Kokomo, Indiana). EXAMPLES

[0079] The following examples are merely illustrative of the phase separator devices disclosed herein and are not intended to limit the scope thereof. Note that surrogate fluid testing of the exemplary proposed designs utilizing inertial separation with a porous media vapor barrier verified the feasibility of liquid / vapor phase separation. This was the primary objective of this project phase, and thus the exemplary project was successful. The performance of both Designs A and C (discussed below) exceeded the minimum performance specifications for this exemplary project phase, which were greater than 75% liquid capture efficiency and less than 5 PSID pressure drop for each fluid path.

[0080] The counterflow cyclone (Design A) provided the highest liquid capture efficiency of the three designs evaluated. Measured liquid capture efficiencies ranged from 93% to 100%, depending on quality factors. This design also provided the lowest pressure drop across the separator with less than 1 PSID pressure drop for both the liquid and gas flow paths.

[0081] The liquid extractor (design C) performed similarly to design A with the same low pressure drop across the gas flow path. This design showed slightly lower liquid capture efficiency at 40% and 50% quality and had a higher liquid pressure drop.

[0082] The gas extractor (design B) did not perform well in initial testing, with superior performance achieved with designs A and C, so no record runs were performed using this configuration.

[0083] Mathematical models have been developed to predict the pressure drop across both the gas and liquid flow paths. These models consider the liquid and gas properties and the effects of operating pressure, temperature and flow rate. The models are designed to be suitable for subsequent scale-up of the separator and operation with the working fluid.

[0084] A Proof of Principle (PoP) was performed to determine whether inertial separation techniques combined with exemplary porous media techniques could be used to create a vapor / liquid phase separator for use in cooled lasers in directed energy weapon systems. For this current phase, the target liquid separation efficiency was greater than 75%, with 50% quality and less than 15 psid fluid pressure drop. Surrogate fluids including water and air have been used to test the functionality of three different exemplary phase separator designs scaled down to approximately 1% mass flow rate of the full-scale final device. Experimental results from this study were evaluated against the aforementioned targets. Additionally, the data was used to validate analytical models. These models can be scaled to scale and further developed to optimize designs for future phases of this multi-phase project.

[0085] Test Procedures / Equipment A custom test stand was constructed to evaluate an exemplary phase separator design for operational performance under near-ambient conditions utilizing surrogate fluids, water, and air. These surrogate fluids were used to simulate a two-phase mixture of a refrigerant at its critical temperature of its operating pressure (R717 at 20° C. and 124 PSIG). FIG. 20 shows a schematic diagram of this custom test stand. Pressurized water and air were fed through a flow meter (left side) that entered a water atomizer, in this case a conventional paint spray gun modified for this purpose. The resulting two-phase mixture was then fed into the inlet port of the PoP phase separator. The device separates the gas and liquid that exit through their respective outlets. A valve located at the outlet was used to regulate the pressure in the system. The output stream flow then passed through a trap to separate the two phases, and the gas flow rate was measured with a flow meter. Pressure sensors located at the inlet and outlet ports were used to monitor the system pressure and pressure drop. Gas temperature and relative humidity (RH) were monitored in a liquid trap on the gas outlet flow path.

[0086] A brief description of the test procedure is as follows: (i) place the phase separator on the test bench and ensure all connections are leak-free; (ii) set the water and air input flow rates to the desired quality; (iii) adjust the gas outlet backpressure valve to reach the desired system input pressure and the liquid outlet backpressure valve for optimal liquid capture efficiency; (iv) wait for the system to stabilize and record all pressures, flows, temperatures, and RH; and (v) repeat for each quality level to be tested.

[0087] A maximum flow rate of 80 standard liters per minute (SLPM) was used during testing assuming 0% relative humidity (RH) input, and a maximum RH output of 80% was observed during testing with air temperatures between 15 and 20°C. Note that the maximum amount of water that air can hold is 12.8g / m3 at 15°C and 17.3g / m3 at 20°C.

[0088] Design A - Reverse flow cyclone FIG. 10 is a schematic diagram showing the main components of the proposed design (Design A version). With respect to the operation of FIG. 10 (Design A version), note that (i) the flow through the counter-flow cyclone vanes creates a centripetal force to separate the liquid from the gas, (ii) the liquid flows to the outside and bottom of the housing, (iii) the porous membrane and liquid layer provide an impermeable barrier to the gas flow, (iv) liquid extraction occurs via a controlled differential pressure across the membrane, and (v) the vapor phase exits through a vertical outlet. Note that such an exemplary cyclone separator is robust in design and highly reliable. Note that the use of a porous medium to support the liquid layer advantageously provides a barrier to vapor transmission while allowing the liquid to pass through.

[0089] FIG. 9 shows another version of the Design A phase separator and its key components that were constructed for evaluation. The vane assembly imparts cyclonic motion to separate the liquid and gas phases, and the conical skirt 328 reduces the amount of liquid exiting the separator through the steam exhaust port. The upper housing was constructed using PVC tee fittings, the liquid outlet housing was constructed using PVD caps, and the body housing and steam exhaust tubes were constructed using clear polycarbonate tubing. Note that the version of the Design A phase separator shown in FIG. 9 was assembled and tested utilizing the custom test stand of FIG. 20.

[0090] Numerous experiments were performed utilizing the Design A phase separator version shown in Figure 9, adjusting the length of the main housing body, the relative placement of the impeller and the connection of the internal vapor extraction tube and media grade (average pore size), as well as the thickness of the porous media before performing a run for recording. It was found that application of media grade 2 porous media with an inlet pressure of 4.0 psi resulted in efficient separation of over 90% of the liquid at all mixture quality levels tested for this scale size phase separator (Design A phase separator version shown in Figure 9).

[0091] Table 1 shows some key summary results based on record test runs on the Design A phase separator version shown in Figure 9. Note that at all quality levels, no gas was observed exiting the device through the liquid port.

[0092] [Table 1]

[0093] The results shown in Table 1 indicate that Design A (FIG. 9) met the performance requirements with liquid and gas pressure drops across the separator all less than 1 PSID and was close to the goal with a liquid capture efficiency of greater than 93%.

[0094] Design B - Gas Extractor Figure 16 is a schematic diagram showing the main components of this proposed design. Regarding the operation of Figure 16 (Design B), note that (i) the flow through the spiral passage creates a centripetal force to separate the liquid from the gas, (ii) the liquid moves outward and travels the entire length of the spiral channel, and (iii) the gas flows inward and passes through an inner porous membrane via a controlled pressure differential and exits the device axially.

[0095] This proposed design (Design B) is unique and significantly different from Design A. The two-phase mixture is intended to follow the spiral flow path and move all of the gas phase through the porous medium toward the center. The liquid continues to flow through the spiral path and exits the device.

[0096] Figure 16 shows a constant cross section through the spiral flow channel. It was recognized early on that there was a significant pressure drop associated with the gas exiting along the spiral flow channel, and to modify the spiral flow channel into a variable pitch, variable cross section helix. Thus, a first generation prototype was created. For the first generation prototype, the two-phase inlet channel starts at a 1 inch diameter and continuously decreases to approximately 1 / 8 inch diameter at the liquid exit port. The spacing between the channels remains constant, resulting in a variable pitch along the flow channel length. The purpose of this modification was to create a more uniform pressure drop across the length of the porous media that would produce a constant gas extraction. It is noted that initial testing of this prototype had poor separation efficiency. Nearly all of the liquid phase exited through the porous media along with the gas phase. It was speculated that this design did not have enough centripetal force to separate the two fluids, and creating a modified design with a much smaller diameter would have a greater inertial separation and therefore better performance.

[0097] It should be noted that a second generation Design B phase separator was fabricated. This design had a significantly smaller and deeper aspect ratio of the internal spiral channels. Continued testing with this design resulted in better separation performance levels than the first generation design with various flow rates and media grades of the porous element. In testing, liquid capture efficiency levels of up to 50% were observed at the 20% quality level, with much lower liquid capture efficiencies observed above 20% quality. No run tests for record were performed with this design due to the low phase separation efficiency.

[0098] Design C-Liquid Extractor Figure 12 is a schematic showing the proposed structure of the individual liquid extractor elements, and Figure 13 shows how they can be arranged in a bundle and operated in parallel to scale up. Regarding the operation of Figure 13 (Design C), note that (i) the flow through the spiral passage creates a centripetal force to separate the liquid from the gas, (ii) the gas flows inward and travels the entire length of the spiral channel, (iii) the porous membrane and liquid layer provide an impermeable barrier to the gas flow, (iv) the liquid flows outward and passes through the outer porous membrane using a controlled pressure differential, and (v) the liquid exits through a side port of the separator.

[0099] This design is similar to design A in that it uses inertial energy to separate the liquid and vapor phases, with the separated liquid passing through a porous medium. It differs from design A in that during separation, the liquid is in immediate contact with the porous medium for separation.

[0100] A single spiral element (e.g., Figure 12) was used for this PoP test. The two-phase fluid enters from the right through an ABS plastic housing with internal wings to initiate cyclonic motion. The fluid then passes through the spiral cavity, pushing the liquid outwards and maintaining the vapor phase towards the center. The liquid passes through the porous media and the vapor phase exits to the left through the spiral channels. The center housing was made using clear polycarbonate plastic so that it could be observed if the vapor phase passes through the porous media. Note that the Design C phase separator was assembled and tested utilizing a custom-made test stand in Figure 20.

[0101] Numerous experiments were performed adjusting the length of the main housing body (1 or 2 inches), media grade (average pore sizes of 0.2, 0.5, and 2), and porous thickness (0.062 and 0.125 inches). It was found that using media grade 2 porous media with an inlet pressure of 5.0 psig resulted in liquid separation efficiencies of approximately 80% or greater at all mixture quality levels tested.

[0102] Table 2 shows some key summary results of the run for record (R4R) testing for Design C. Note that in all cases, no gas was observed exiting the device through the liquid port.

[0103] [Table 2]

[0104] Discussion-Test Analysis-Design Comparison: Table 3 below shows the combined summary results for both Designs A and C. The liquid and gas phase pressures drop across each design along with their quality relative to their liquid capture efficiency. The results clearly show that Design A, a counterflow cyclone, is superior in terms of liquid capture efficiency to Design C, a liquid extractor. Design A started out at 50% quality with an efficiency of 93% and quickly rose to 99% at a lower quality. At this time, the low efficiency of 30% can be attributed to implementation / setup error. Design C started out at a low liquid capture efficiency of 79% and rose to a very high efficiency at a lower quality, but at a slightly slower rate.

[0105] Designs A and C both started out with approximately 1 PSID pressure drop at the gas outlet and both steadily decreased to 0 PSID as the quality decreased from 50% to 0%. This steady decrease in gas phase pressure drop with quality is expected and the trend is consistent with the engineering design model.

[0106] [Table 3]

[0107] Comparison of model predictions with experimental data – Design A Table 4 and FIG. 21 are a table and graph showing the quality versus predicted gas phase pressure drop calculated using the analytical model and experimentally measured values ​​for Design A. In FIG. 21, the modeled pressure drop is shown as a diamond and the experimental results are shown as a rectangle on the graph. Except for the 10% quality data points, the model predicted pressure drop is on average within 20% of the experimentally measured data and follows a similar non-linear upward tread. The data, when plotted as a function of gas flow rate, shows that the pressure increases primarily with the square of the gas flow rate plus some secondary factors, which is expected from a fundamental standpoint. The model accounts for fluid density, viscosity, and actual gas velocity in the separator, which are dependent on temperature and pressure.

[0108] [Table 4]

[0109] Table 5 and Figure 22 are a table and graph showing the predicted liquid phase pressure drop quality calculated using the analytical model and experimentally measured values ​​for Design A. In Figure 22, the modeled pressure drop is shown as diamonds and the experimental results are shown as rectangles on the graph. The model accounts for fluid density, viscosity, and actual gas velocity in the separator which are dependent on temperature and pressure.

[0110] With the exception of the 0% quality data point, the model predicted pressure drop is, on average, within 10% of the experimentally measured data. Interestingly, the pressure drop data is relatively constant when plotted as a function of quality or liquid flow rate. Thus, the pressure drop is relatively independent of the liquid flow rate. At first glance, this result seems to contradict the basic belief that pressure drop normally increases with increasing flow rate. However, the data is indeed correct, and this unusual finding results from two aspects that combine to produce an overall pressure drop in the liquid flow path. The first part of the pressure occurs across the inlet region and swirler of the cyclone. In this region, the pressure drop of the mixed fluid stream is primarily a result of the gas flow rate. Furthermore, this pressure drop dependence varies as the square of the gas flow rate plus some secondary factors. The pressure drop decreases with decreasing gas flow rate and mixture quality. The second main region for liquid pressure drop occurs across the exemplary porous metal media. Here, the pressure drop increases linearly with liquid flow rate, thus decreasing mixture quality. These two tendencies, one increasing while the other decreases, result in a pressure that is relatively independent of the quality of the mixture.

[0111] [Table 5]

[0112] Comparison of model predictions and experimental data – Design C Table 6 and Figure 23 are a table and graph showing the predicted gas phase pressure drop quality calculated using the analytical model and experimentally measured values ​​for Design C. In Figure 23, the modeled pressure drop is shown as a diamond and the experimental results are shown as a rectangle on the graph. The modeled data is slightly over 1 / 2 the value of the experimental data, but shows the same overall trend. As mentioned in the results section, a set of swirling vanes were installed on the inlet housing to initiate cyclonic motion before the fluid reaches the separator element, but this was not taken into account in our modeling and may explain the higher than expected pressure drop. The black circles shown in Figure 23 are the predicted pressure drop with adjustments to account for these additional vanes and other limitations in the device. The adjusted model results follow the same trends as the experimentally measured results, which follow the theoretically expected quadratic curvature.

[0113] [Table 6]

[0114] Looking at the modeled liquid pressure drop and measured experimental results for Design C, there does not appear to be a direct correlation. Table 7 and Figure 24 are a table and graph showing the quality versus predicted liquid phase pressure drop calculated using the analytical model and experimentally measured values. In Figure 24, a linear change in quality versus liquid pressure drop in the triangle predicted for laminar flow is predicted by the model. The experimentally measured values ​​are reasonably close to the predicted values ​​at 0% quality, but at all higher qualities, the measured values ​​are stable at approximately 2 PSID, which does not match the analytical model. The measured liquid pressure drop should decrease with increasing quality as the liquid flow rate through the media decreases. This could be an implementation issue, or a Venturi effect where high velocity gas passes through the separator, creating a lower pressure and affecting the liquid pressure drop measurements. Another issue is that water generally does not wet stainless steel well, and trapped air in the porous media could be restricting the flow and causing a higher than predicted pressure drop.

[0115] [Table 7]

[0116] Conclusions and Recommendations The PoP prototype studies indicate that using inertial energy in an exemplary porous medium is a viable option for achieving liquid / gas phase separation. It should also be recognized that limited work has been done to optimize the separation performance of these two designs, and additional work can be performed to improve their performance before moving to evaluation using refrigerant fluids. Continued testing with alternative fluids to optimize these designs can be performed at significantly less cost and in much less time than attempting to optimize performance levels using ammonia or other refrigerants.

[0117] It should be noted that although Design A is superior to Design C in terms of liquid capture efficiency, Design A has some limitations related to its orientation. When operating in an environment where gravity is prevalent, Design A should generally face the liquid outlet downwards for correct operation. This means that for stationary ground-based applications, Design A should work well. In certain embodiments, for flying platform applications, Design A may not perform as designed. Furthermore, Design A should work in microgravity situations, since these types of designs have been shown to work in other applications before. When looking at Design C, this design has no known limitations in its orientation and is expected to work in orientations where gravity is present, including microgravity environments. For this reason, further optimization work should be performed to improve the liquid capture efficiency before making a final design selection.

[0118] Record run on a proof-of-principle phase separator. The following is a Record for Run (R4R) test procedure for a Phase 1 Proof of Principle (POP) design for a liquid / vapor phase separator (e.g., as employed in laser cooling applications). During R4R testing, all adjustable parameters (hardware dimensions, device orientation, etc.) are not altered for the duration of testing and data collection for each of the three designs.

[0119] Table 8 below are the volumetric water and air flow rates calculated to achieve the quality levels shown. These values ​​represent 1.25% and 2.5% by volume and 0.25% and 0.5% of the full-scale total mass flow rate for a system running R717. The choice of operation at low or high flow range was selected based on laboratory-scale prototype sizes and preliminary testing of each design prior to the actual recording run. Efforts were made to target one of these two flow ranges in case any of the designs required a different flow rate to operate properly. The water and flow rates for each quality level can be recalculated for these cases.

[0120] [Table 8]

[0121] Measurements: The following ports were installed to monitor pressure, temperature, and relative humidity where applicable for each design: pressure at the two-phase inlet, pressure at the gas outlet (before the back pressure regulator if employed to optimize performance), pressure at the liquid outlet (before the back pressure regulator if employed to optimize performance), liquid pressure drop across the porous media (design A only), pressure of the gas at the time of test, temperature of the gas at the outlet, relative humidity of the air at the outlet, liquid outflow, flow rate at the gas outlet, a capped container at the liquid outlet, a rotameter at the vent to measure air flow rate, and a water droplet trap at the gas outlet were employed to measure air and water flow rates separately.

[0122] [Table 9]

[0123] While particular embodiments have been described, presently unforeseen or unforeseen alternatives, modifications, variations, improvements, and substantial equivalents may occur to the applicant or those skilled in the art. It is therefore intended that the appended claims as filed, and as they may be amended, cover all such alternatives, modifications, variations, improvements, and substantial equivalents.

[0124] All ranges disclosed herein are inclusive of the endpoints, and the endpoints are combinable independently of one another (e.g., the range "up to 25 wt.%, or more specifically, 5 wt.% to 20 wt.%" includes the endpoints of the range "5 wt.% to 25 wt.%" and all intermediate values). "Combination" includes blends, mixtures, alloys, reaction products, and the like. The terms "first", "second", and the like do not denote any order, amount, or importance, but rather are used to distinguish one element from another. The terms "a" and "an" and "the" do not denote any quantitative limitations, unless otherwise indicated herein or clearly contradicted by context, and should be construed to cover both the singular and plural forms. "Or" means "and / or" unless otherwise indicated. Throughout this specification, references to "some embodiments", "embodiments", and the like mean that the particular element described in connection with an embodiment is included in at least one embodiment described herein and may or may not be present in other embodiments. In addition, it is to be understood that the described elements may be combined in any suitable manner in the various embodiments. "Combinations thereof" is open and includes any combination including at least one of the recited components or features, optionally including similar or equivalent components or features not recited.

[0125] Unless otherwise defined, technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this application belongs. All cited patents, patent applications, and other references are incorporated herein by reference in their entirety. However, if a term in this application contradicts or conflicts with a term in an incorporated reference, the term from this application shall take precedence over the conflicting term from the incorporated reference.

[0126] Although the system and method of the present disclosure have been described with reference to exemplary embodiments thereof, the present disclosure is not limited to such exemplary embodiments and / or implementations. Rather, the system and method of the present disclosure are susceptible to many implementations and applications, as will be readily apparent to those skilled in the art from the present disclosure. The present disclosure expressly encompasses such modifications, improvements, and / or variations of the disclosed embodiments. Since many changes can be made in the above structures, and many widely different embodiments of the present disclosure can be made without departing from its scope, it is intended that all matters contained in the drawings and this specification be interpreted as illustrative and not in a limiting sense. Additional modifications, changes, and substitutions are contemplated in the foregoing disclosure. It is therefore appropriate that the appended claims be interpreted broadly and in a manner consistent with the scope of the present disclosure.

Claims

1. 1. A phase separator device comprising: a housing extending from a first end to a second end, said housing having one or more first openings through which a first phase output exits and one or more second openings through which a second phase output exits; one or more guide vanes disposed on the housing; the housing includes an axial flow cyclone separating section and a porous media section; the axial flow cyclone separation section and the porous media section are configured and dimensioned to separate an input feed introduced into the housing into the first phase output and the second phase output.

2. 10. The phase separator device of claim 1, wherein the first phase output comprises a liquid and the second phase output comprises a gas.

3. 10. The phase separator device of claim 1, wherein the input feed is a fluid mixture.

4. 10. The phase separator device of claim 1, wherein the input feed comprises two different constituent liquids and gases.

5. 10. The phase separator device of claim 1, wherein the input feed comprises liquid and vapor phases of the same composition.

6. 10. The phase separator device of claim 1, wherein the input feed introduced into the housing comprises ammonia.

7. 10. The phase separator device of claim 1, wherein the input feed introduced into the housing comprises water and air.

8. The phase separator device of claim 1 further comprising a liquid collection section in the housing.

9. 1. A phase separator device comprising: one or more extractor elements disposed in a housing, the housing having an inlet for an input feed, and a first outlet for a first phase output and a second outlet for a second phase output; Each extractor element includes a threaded rod housed in a porous media tube; the one or more extractor elements are configured and dimensioned to separate the input feed introduced at the inlet into the first phase output and the second phase output.

10. 1. A phase separator device comprising: a housing extending from a first end to a second end, said housing having one or more first openings through which a first phase output exits and one or more second openings through which a second phase output exits; one or more guide vanes disposed on the housing; the housing includes a reverse flow cyclone separation section and a porous media section; the reverse flow cyclone separation section and the porous media section are configured and dimensioned to separate an input feed introduced into the housing into the first phase output and the second phase output.

11. 11. The phase separator device of claim 10, wherein the first phase output comprises a liquid and the second phase output comprises a gas.

12. 11. The phase separator device of claim 10, wherein the input feed is a fluid mixture.

13. 11. The phase separator device of claim 10, wherein the input feed comprises two different component liquids and gases.

14. 11. The phase separator device of claim 10, wherein the input feed comprises liquid and vapor phases of the same composition.

15. 11. The phase separator device of claim 10, wherein the input feed introduced into the housing comprises ammonia.

16. 11. The phase separator device of claim 10, wherein the input feed introduced into the housing comprises water and air.

17. The phase separator device of claim 10 further comprising a liquid collection section in the housing.

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