A diffuser ejector, a carbon dioxide transcritical refrigeration system and a throttling loss recovery method thereof

Abstract

The present application belongs to the technical field of fluid machinery and throttling loss recovery in refrigeration and heat pump system, and discloses a diffuser ejector, a carbon dioxide transcritical refrigeration system and a throttling loss recovery method thereof, which solves the problems of early diffusion of jet flow at the nozzle outlet of the existing CO2 transcritical ejector, unstable secondary flow entrainment and large pressure recovery loss of single-stage diffuser. The diffuser ejector comprises a shell, a working nozzle, a straight pipe rectifying section, a suction chamber, a secondary flow inlet, a first mixing chamber, a first diffuser section, a second mixing chamber and a second diffuser section. The working nozzle is arranged in the shell, the straight pipe rectifying section is coaxially communicated with the outlet of the working nozzle, the suction chamber is arranged at the outer periphery of the outlet of the working nozzle and is communicated with the secondary flow inlet, and the first mixing chamber, the first diffuser section, the second mixing chamber and the second diffuser section are sequentially arranged along the flow direction of the mixed flow. The present application is beneficial to improving the stability of jet flow at the outlet of the working nozzle, the stability of secondary flow entrainment, the pressure recovery capacity and the operation stability.

Description

Technical Field

[0001] This invention belongs to the field of fluid mechanics and throttling loss recovery technology in refrigeration and heat pump systems, and particularly relates to a diffuser ejector, a transcritical carbon dioxide refrigeration system and a method for recovering throttling losses. Background Technology

[0002] Carbon dioxide (CO2), as a natural refrigerant, possesses advantages such as zero ozone depletion potential, low global warming potential, large volumetric refrigeration capacity, good heat transfer performance, and wide availability, making it suitable for applications in supermarket cold chain logistics, cold storage, heat pump water heating, automotive air conditioning, and low-temperature refrigeration. Due to its low critical temperature, CO2 typically operates in transcritical cycles at medium to high ambient temperatures. A typical transcritical CO2 refrigeration system mainly consists of a compressor, gas cooler, throttling device, evaporator, and gas-liquid separator.

[0003] In the transcritical CO2 cycle, the refrigerant on the high-pressure side remains at a relatively high pressure after releasing heat through the gas cooler. If a conventional throttling valve is used to reduce the pressure, the pressure energy in the high-pressure refrigerant will be dissipated as irreversible throttling losses, leading to a decrease in the system's coefficient of performance (COP). An ejector can utilize the high-speed jet formed by the expansion of the high-pressure primary flow to entrain the low-pressure secondary flow, and achieve a certain degree of pressure recovery through mixing and diffusion processes. Therefore, it is considered an important component for recovering throttling losses in the transcritical CO2 cycle, reducing the compressor pressure ratio, and improving system energy efficiency.

[0004] However, the internal flow of CO2 transcritical ejectors exhibits complex characteristics such as high-speed compressibility, two-phase phase transformation, strong shear mixing, local shock waves, and pressure recovery. Traditional fixed-geometry ejectors typically employ a single mixing chamber and a single diffuser chamber structure. When the jet diffusion at the nozzle exit is too rapid, the low-pressure region within the suction chamber is prone to instability, leading to a decrease in secondary flow entrainment capacity. When the length and diameter of the mixing chamber are mismatched, secondary flow blockage, insufficient mixing, or excessive wall friction losses may occur. When the diffuser section bears the main pressure recovery over a short distance, boundary layer separation, backflow, and reduced pressure recovery efficiency are likely to occur.

[0005] Existing nozzle structures with straight pipe sections can improve the local flow at the nozzle exit to some extent, but they mainly focus on jet stability near the nozzle tip, and do not adequately consider velocity stratification, remixing, and segmented pressure recovery in the subsequent mixing chamber and diffuser section. Therefore, it is necessary to propose a novel transcritical CO2 ejector structure that can both stabilize the nozzle exit jet and organize the mixing and diffuser processes into distinct zones. Summary of the Invention

[0006] One objective of this invention is to provide a diffuser ejector that effectively solves the problems of premature diffusion of the nozzle outlet jet, unstable secondary flow entrainment, and large single-stage diffusion pressure recovery loss in existing CO2 transcritical ejectors.

[0007] To solve the above-mentioned technical problems, the technical solution adopted by the present invention is: a diffuser ejector, comprising a housing, a working nozzle, a straight tube rectifier section, an intake chamber, a secondary flow inlet, a first mixing chamber, a first diffuser section, a second mixing chamber, and a second diffuser section.

[0008] The working nozzle is located inside the housing, and the inlet of the working nozzle is the primary flow inlet. The straight pipe rectifying section is coaxially connected to the outlet of the working nozzle. The suction chamber is located on the outer periphery of the outlet of the working nozzle and is connected to the secondary flow inlet. The first mixing chamber, the first diffuser section, the second mixing chamber, and the second diffuser section are arranged sequentially along the mixed flow direction. The outlet of the second diffuser section constitutes the ejector outlet.

[0009] The working nozzle is used to expand and accelerate the high-pressure CO2 primary flow to form a low-pressure, high-speed jet; the suction chamber is used to introduce a low-pressure CO2 secondary flow; the straight pipe rectification section is used to limit the radial diffusion of the high-speed jet flowing out of the working nozzle outlet to maintain the low-pressure zone at the inlet of the suction chamber and the first mixing chamber; the first mixing chamber, the first diffusion section, the second mixing chamber, and the second diffusion section sequentially form a segmented mixing and diffusion channel for premixing, preliminary diffusion and pressurization, remixing, and final diffusion pressure recovery.

[0010] Furthermore, the working nozzle is a Laval nozzle structure, including a tapering section, a nozzle throat, and a diverging section, with the straight pipe rectifying section located between the downstream end of the diverging section of the working nozzle and the upstream end of the first mixing chamber.

[0011] Furthermore, the primary inlet, working nozzle, straight pipe rectifier section, first mixing chamber, first diffuser section, second mixing chamber, and second diffuser section are arranged coaxially.

[0012] Furthermore, the diameter of the nozzle throat is 1.5 mm to 2.3 mm, and the diameter of the inlet of the working nozzle is 12 mm to 20 mm.

[0013] Furthermore, the length of the straight rectifier section is 5 mm to 15 mm, and the diameter of the outlet of the straight rectifier section is 4.0 mm to 5.5 mm.

[0014] Furthermore, the first mixing chamber is a straight pipe section of equal diameter, with a diameter of 8 mm to 12 mm and a length of 35 mm to 60 mm; the diffusion angle of the first diffuser section is 2° to 4°, and the first diffuser section is used to initially decelerate and restore the pressure of the mixed flow after premixing in the first mixing chamber.

[0015] Furthermore, the second mixing chamber is a straight pipe section of equal diameter, with a diameter of 11 mm to 14 mm and a length of 20 mm to 45 mm. The second mixing chamber is used to remix the velocity-stratified fluid after passing through the first diffuser section. The diffusion angle of the second diffuser section is 3° to 8°, and the diameter of the outlet of the second diffuser section is 12 mm to 20 mm.

[0016] Furthermore, the first and second diffusion sections are expanded using linear conical expansion, circular arc transition expansion, or multi-segment broken line approximation expansion.

[0017] Another object of the present invention is to provide a transcritical carbon dioxide refrigeration system, comprising a compressor, a gas cooler, an evaporator, a gas-liquid separator, and a diffuser ejector as described in the above embodiments; the inlet of the compressor is connected to the gas phase outlet of the gas-liquid separator, the outlet of the compressor is connected to the inlet of the gas cooler, the outlet of the gas cooler is connected to the primary flow inlet of the diffuser ejector, the outlet of the evaporator is connected to the secondary flow inlet of the diffuser ejector, and the ejector outlet of the diffuser ejector is connected to the gas-liquid separator.

[0018] Another objective of this invention is to provide a method for recovering throttling losses in a transcritical carbon dioxide refrigeration system, comprising the following steps: First, high-pressure CO2 from the outlet of the gas cooler enters the working nozzle through the primary flow inlet and expands and accelerates to form a low-pressure, high-speed jet; second, a low-pressure CO2 secondary flow enters the suction chamber through the secondary flow inlet and is entrained by the low-pressure, high-speed jet; subsequently, the low-pressure, high-speed jet is first constrained and rectified through a straight pipe rectification section, and then enters the first mixing chamber, the first diffuser section, the second mixing chamber, and the second diffuser section sequentially together with the CO2 secondary flow; finally, the mixed flow from the ejector outlet of the diffuser ejector is sent to a gas-liquid separator.

[0019] Compared with the prior art, the beneficial technical effects of the present invention are: (1) High stability of the jet at the outlet of the working nozzle: The high-speed core at the outlet of the working nozzle is constrained and rectified by the straight pipe rectification section, which suppresses the excessive diffusion of the CO2 primary flow immediately after passing through the outlet of the working nozzle and maintains a continuous low-pressure zone near the suction chamber.

[0020] (2) Improved CO2 secondary flow entrainment capability: The first mixing chamber extends the shear contact distance between the low-pressure high-speed jet and the CO2 secondary flow, which is beneficial to improving the CO2 secondary flow entrainment stability and initial momentum exchange effect.

[0021] (3) The pressure recovery process is smoother: By designing the first diffusion section to adopt a small-angle micro-diffusion structure, part of the pressure recovery in the traditional single-stage diffusion is shared in advance, reducing the reverse pressure gradient of the end diffusion section.

[0022] (4) Better remixing effect: The second mixing chamber provides a remixing space for the fluid after micro-expansion in the first diffuser section, which can weaken the peak axial velocity, radial velocity stratification and local backflow tendency.

[0023] (5) Reduced risk of diffuser separation: By enabling the second diffuser section to complete the final pressure recovery under relatively uniform inlet flow field conditions, it is beneficial to improve the stability of outlet pressure.

[0024] (6) Strong feasibility for engineering applications: The diffuser ejector of the present invention has no complex active moving parts, can be prepared by conventional machining, integral molding or additive manufacturing, and can be used in conjunction with gas coolers, evaporators, gas-liquid separators and compressors in existing CO2 transcritical refrigeration systems.

[0025] In summary, this invention designs the straight pipe rectification section downstream of the working nozzle outlet, along with the first mixing chamber, the first diffuser section, the second mixing chamber, and the second diffuser section, as a single integrated structure. This structure, through a continuous process of "rectification and entrainment—premixing—micro-diffraction and pressurization—remixing—final diffusion," ensures that the entrainment, mixing, deceleration, and pressurization within the ejector no longer occur concentrated in a single mixing chamber or a single diffuser section, but are completed step-by-step in multiple functional areas. This improves the stability of the jet at the working nozzle outlet, the stability of the secondary flow entrainment, the pressure recovery capability, and the operational stability. Attached Figure Description

[0026] Figure 1 This is a schematic diagram of the structure of the diffuser ejector of the present invention.

[0027] Figure 2 This is a schematic diagram of the connection structure of the carbon dioxide transcritical refrigeration system in Embodiment 2 of the present invention.

[0028] Explanation of reference numerals in the attached diagram: Straight pipe rectifier section -1; First mixing chamber -2; First diffuser section -3; Second mixing chamber -4; Second diffuser section -5; Secondary flow inlet -6; Primary flow inlet -7; Ejector outlet -8; Converging section -9; Nozzle throat -10; Diverging section -11; Compressor -12; Gas cooler -13; Evaporator -14; Gas-liquid separator -15; Diffuser ejector -16. Detailed Implementation

[0029] Example 1: This example provides a diffuser ejector with an axisymmetric circular channel structure. The diffuser ejector stabilizes the jet at the nozzle outlet through the straight tube rectifier section 1 and improves the entrainment, mixing and pressure recovery process of the CO2 two-phase flow through the segmented mixing diffuser channel.

[0030] like Figure 1As shown, the diffuser ejector provided in this embodiment includes a housing, a secondary flow inlet 6, an ejector outlet 8, and a working nozzle, a straight pipe rectifying section 1, a first mixing chamber 2, a first diffuser section 3, a second mixing chamber 4, and a second diffuser section 5 arranged sequentially along the axial direction. The first mixing chamber 2, the first diffuser section 3, the second mixing chamber 4, and the second diffuser section 5 are arranged sequentially along the mixed flow direction. The working nozzle is located inside the housing, and the inlet of the working nozzle is the primary flow inlet 7. A suction chamber is provided on the outer periphery of the working nozzle, and the suction chamber communicates with the secondary flow inlet 6. The primary flow inlet 7 is located at the upstream end of the working nozzle, and the outlet of the second diffuser section 5 constitutes the ejector outlet 8. The working nozzle is used to expand and accelerate the high-pressure CO2 primary flow to form a low-pressure high-speed jet. The suction chamber is used to introduce the low-pressure CO2 secondary flow. The straight pipe rectification section 1 is used to constrain the low-pressure area near the inlet of the suction chamber and the first mixing chamber 2. The first mixing chamber 2, the first diffuser section 3, the second mixing chamber 4 and the second diffuser section 5 sequentially form a segmented mixing and diffuser channel for premixing, preliminary diffuser pressurization, remixing and final diffuser pressure recovery.

[0031] The working nozzle adopts a Laval nozzle design, including a converging section 9, a nozzle throat 10, and a diverging section 11. The high-pressure CO2 primary flow is accelerated in the converging section 9, reaches a critical or near-critical flow state near the nozzle throat 10, and further expands in the diverging section 11. The inlet diameter of the working nozzle is 12 mm to 20 mm; in this embodiment, the inlet diameter is 16 mm to ensure a stable supply of the primary flow inlet 7. The diameter of the nozzle throat 10 is 1.5 mm to 2.3 mm; in this embodiment, the diameter is 1.9 mm. The nozzle throat 10 determines the critical mass flow rate of the primary flow and the nozzle expansion capacity.

[0032] The straight-tube rectifier section 1 is coaxially connected to the outlet of the working nozzle, and is located between the downstream end of the diffuser section 11 of the working nozzle and the upstream end of the first mixing chamber 2. The length of the straight-tube rectifier section 1 is 5 mm to 15 mm. In this embodiment, the length of the straight-tube rectifier section 1 is 10 mm, which is used to stabilize the high-speed core of the working nozzle outlet and maintain the low-pressure entrainment zone. If the straight-tube rectifier section 1 is too short, the rectification effect will be insufficient; if it is too long, it will increase the wall friction loss. Therefore, it can be selected within the range of 5 mm to 15 mm according to the refrigeration system capacity and working pressure. The diameter of the outlet of the straight-tube rectifier section 1 is 4.0 mm to 5.5 mm. In this embodiment, the diameter of the outlet of the straight-tube rectifier section 1 is 4.6 mm, which is used to control the jet size before the low-pressure high-speed jet enters the mixing zone.

[0033] The first mixing chamber 2 is used to complete the initial shear contact and premixing of the low-pressure high-speed jet and the low-pressure CO2 secondary flow. The first diffuser section 3, as a micro-diffuser, preferably has a diffusion angle smaller than that of the second diffuser section 5, so that the mixed flow undergoes gentle deceleration and initial pressure recovery. The mixed flow after passing through the first diffuser section 3 enters the second mixing chamber 4, further weakening the velocity stratification and local backflow tendency, and achieving remixing. The second diffuser section 5, as the terminal diffuser section, converts part of the kinetic energy of the mixed flow into pressure energy, making the outlet pressure of the diffuser ejector higher than the inlet pressure of the secondary flow 6.

[0034] The first mixing chamber 2 is a straight pipe section of equal diameter, with a diameter of 8 mm to 12 mm. In this embodiment, the diameter of the first mixing chamber 2 is 10 mm, which is used to provide space for premixing of primary and secondary flows and initial momentum exchange. The length of the first mixing chamber 2 is 35 mm to 60 mm. In this embodiment, the length of the first mixing chamber 2 is 45 mm, which is used to extend the shear contact distance and avoid excessive friction loss.

[0035] The first diffusion section 3 is a small-angle micro-diffusion section with a diffusion angle of 2° to 4°. In this embodiment, the diffusion angle of the first diffusion section 3 is 3°, which is used for small-angle initial pressure recovery.

[0036] The second mixing chamber 4 is a straight pipe section of equal diameter, with a diameter of 11 mm to 14 mm. In this embodiment, the diameter of the second mixing chamber 4 is 13 mm, which is used to reduce the risk of CO2 secondary flow blockage and improve remixing. The length of the second mixing chamber 4 is 20 mm to 45 mm. In this embodiment, the length of the second mixing chamber 4 is 25 mm, which is used to weaken the velocity stratification of the fluid after passing through the first diffuser section 3 and stabilize the flow field entering the terminal diffuser section.

[0037] The diffusion angle of the second diffuser section 5 is 3° to 8°. In this embodiment, the diffusion angle of the second diffuser section 5 is 4°, which is used to complete the final pressure recovery and reduce the risk of separation. The diameter of the outlet of the second diffuser section 5 is 12 mm to 20 mm. In this embodiment, the diameter of the outlet of the second diffuser section 5 is 16 mm, which is used to output the intermediate pressure mixed flow.

[0038] Example 2: This example provides a transcritical carbon dioxide refrigeration system, including a compressor 12, a gas cooler 13, an evaporator 14, a gas-liquid separator 15, and the diffuser ejector 16 described in Example 1.

[0039] like Figure 1 and Figure 2As shown, the inlet of compressor 12 is connected to the gas phase outlet of gas-liquid separator 15, the outlet of compressor 12 is connected to the inlet of gas cooler 13, the outlet of gas cooler 13 is connected to the primary flow inlet 7 of diffuser ejector 16, the outlet of evaporator 14 is connected to the secondary flow inlet 6 of diffuser ejector 16, and the ejector outlet 8 of diffuser ejector 16 is connected to gas-liquid separator 15.

[0040] like Figure 2 As shown, in a transcritical carbon dioxide refrigeration system, the high-temperature, high-pressure CO2 discharged from compressor 12 enters gas cooler 13 to release heat and then enters the primary inlet 7 of diffuser ejector 16. CO2 from evaporator 14 enters the suction chamber as a secondary CO2 stream. The primary CO2 stream expands and accelerates through the working nozzle, forming a low-pressure, high-speed jet, while the secondary CO2 stream is drawn in under pressure differential and shear action. The high-speed primary CO2 stream, rectified by straight pipe rectifier section 1, is premixed with the secondary CO2 stream in the first mixing chamber 2, resulting in initial momentum exchange. The premixed stream in the first mixing chamber 2 enters the first diffuser section 3, where it is gently decelerated and undergoes initial pressure recovery in a small-angle expansion channel. Subsequently, the mixed stream enters the second mixing chamber 4 for remixing, further weakening the velocity gradient and local pressure inhomogeneity, making the velocity and pressure distribution more uniform, thus making the flow more stable before entering the second diffuser section 5. Finally, the mixed flow is further decelerated and pressurized in the second diffuser section 5, so that the ejector outlet pressure of the diffuser ejector 16 is higher than the secondary flow inlet 6, thereby realizing the pressurization of the low-pressure CO2 secondary flow and the partial recovery of the expansion energy of the high-pressure CO2 primary flow.

[0041] Example 3: This example provides a method for recovering throttling losses in the transcritical carbon dioxide refrigeration system described in Example 2, comprising the following steps: First, high-pressure CO2 from the outlet of the gas cooler 13 enters the working nozzle through the primary flow inlet 7 and expands and accelerates to form a low-pressure, high-speed jet. Second, the low-pressure CO2 secondary flow enters the suction chamber through the secondary flow inlet 6 and is entrained by the low-pressure, high-speed jet. Subsequently, the low-pressure, high-speed jet first passes through the straight pipe rectifying section 1 for constrained rectification, and then enters the first mixing chamber 2, the first diffuser section 3, the second mixing chamber 4, and the second diffuser section 5 together with the CO2 secondary flow, completing jet stabilization, premixing, initial pressurization, remixing, and final pressure recovery. Finally, the mixed flow from the ejector outlet 8 of the diffuser ejector 16 is sent to the gas-liquid separator 15.

[0042] Of course, the above description is not intended to limit the invention, and the invention is not limited to the examples given above. The diffuser ejector 16 of the invention can be scaled up or down proportionally according to different cooling capacity levels and operating conditions. The first diffuser section 3 and the second diffuser section 5 can adopt a straight conical expansion, a circular arc transition expansion, or a multi-segment broken line approximate expansion form; the first mixing chamber 2 and the second mixing chamber 4 can be straight pipe sections of equal diameter, or conventional equivalent adjustments can be made without changing the "premixing-micro-diffusion-remixing-final diffusion" functional zoning. Changes, modifications, additions, or substitutions made by those skilled in the art within the scope of the invention should also fall within the protection scope of the invention.

Claims

1. A diffuser ejector, characterized in that, It includes a housing, a working nozzle, a straight pipe rectifier section, a suction chamber, a secondary flow inlet, a first mixing chamber, a first diffuser section, a second mixing chamber, and a second diffuser section; The working nozzle is located inside the housing, and the inlet of the working nozzle is the primary flow inlet. The straight pipe rectifier section is coaxially connected to the outlet of the working nozzle. The suction chamber is located on the outer periphery of the outlet of the working nozzle and is connected to the secondary flow inlet. The first mixing chamber, the first diffuser section, the second mixing chamber, and the second diffuser section are arranged sequentially along the mixed flow direction. The outlet of the second diffuser section constitutes the ejector outlet. The working nozzle is used to accelerate the expansion of the high-pressure CO2 primary flow to form a low-pressure, high-speed jet. The inhalation chamber is used to introduce a low-pressure CO2 secondary flow; The straight tube rectifying section is used to limit the radial diffusion of the high-speed jet flowing out of the working nozzle outlet in order to maintain the low-pressure zone at the inlet of the suction chamber and the first mixing chamber. The first mixing chamber, the first diffusion section, the second mixing chamber, and the second diffusion section sequentially form a segmented mixing and diffusion channel for premixing, initial diffusion and pressurization, remixing, and final diffusion pressure recovery.

2. The diffuser ejector according to claim 1, characterized in that, The working nozzle is a Laval nozzle structure, including a converging section, a nozzle throat, and a diverging section. The straight pipe rectifying section is located between the downstream end of the diverging section of the working nozzle and the upstream end of the first mixing chamber.

3. A diffuser ejector according to claim 1, characterized in that, The primary inlet, working nozzle, straight pipe rectifier section, first mixing chamber, first diffuser section, second mixing chamber and second diffuser section are arranged coaxially.

4. A diffuser ejector according to claim 2, characterized in that, The diameter of the nozzle throat is 1.5 mm to 2.3 mm, and the diameter of the inlet of the working nozzle is 12 mm to 20 mm.

5. A diffuser ejector according to claim 1, characterized in that, The length of the straight rectifier section is 5 mm to 15 mm, and the diameter of the outlet of the straight rectifier section is 4.0 mm to 5.5 mm.

6. A diffuser ejector according to claim 1, characterized in that, The first mixing chamber is a straight pipe section of equal diameter, with a diameter of 8 mm to 12 mm and a length of 35 mm to 60 mm. The diffusion angle of the first diffusion section is 2° to 4°. The first diffusion section is used to initially decelerate and restore the pressure of the mixed flow after premixing in the first mixing chamber.

7. A diffuser ejector according to claim 6, characterized in that, The second mixing chamber is a straight pipe section of equal diameter, with a diameter of 11 mm to 14 mm and a length of 20 mm to 45 mm. The second mixing chamber is used to remix the velocity-stratified fluid after passing through the first diffuser section. The diffusion angle of the second diffuser section is 3° to 8°, and the diameter of the outlet of the second diffuser section is 12 mm to 20 mm.

8. A diffuser ejector according to claim 1, characterized in that, The first and second diffusion sections expand using linear conical expansion, circular arc transition expansion, or multi-segment broken line approximation expansion.

9. A transcritical carbon dioxide refrigeration system, characterized in that, Includes a compressor, a gas cooler, an evaporator, a gas-liquid separator, and a diffuser ejector as described in any one of claims 1-8; The compressor inlet is connected to the gas phase outlet of the gas-liquid separator, the compressor outlet is connected to the gas cooler inlet, the gas cooler outlet is connected to the primary flow inlet of the diffuser ejector, the evaporator outlet is connected to the secondary flow inlet of the diffuser ejector, and the diffuser ejector outlet is connected to the gas-liquid separator.

10. The method for recovering throttling losses in a transcritical carbon dioxide refrigeration system according to claim 9, characterized in that, Includes the following steps: First, the high-pressure CO2 from the outlet of the gas cooler enters the working nozzle through the primary inlet and expands and accelerates to form a low-pressure, high-speed jet. Secondly, the low-pressure CO2 secondary flow is made to enter the suction chamber through the secondary flow inlet and be entrained by the low-pressure high-speed jet. Subsequently, the low-pressure high-speed jet is first constrained and rectified through the straight pipe rectification section, and then enters the first mixing chamber, the first diffuser section, the second mixing chamber and the second diffuser section together with the CO2 secondary flow in sequence. Finally, the mixed flow from the ejector outlet of the diffuser is fed into the gas-liquid separator.

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