A phase separator and a phase separation method for continuous phase separation of a phase change absorbent

Abstract

The application relates to the technical field of phase separation devices, and is a phase separator and a phase separation method for continuous phase separation of a phase change absorbent, which comprises a baffle, an upper baffle, a lower baffle and a shell, the front side, the back side and the right side of the upper baffle are in close connection with the front side, the back side and the right side of the inner wall of the shell respectively, the lower baffle is fixed in the shell of the upper baffle, and the front side, the back side and the right side of the lower baffle are in close connection with the front side, the back side and the right side of the inner wall of the shell respectively. The phase separator adopts the combined structure of the baffle, the hydrophobic membrane and the hydrophilic membrane, can efficiently perform continuous phase separation treatment on the phase change absorbent, significantly improves the phase separation efficiency, realizes rapid and complete upper and lower phase separation, greatly reduces the operation cost of the process, and realizes efficient and low-energy-consumption phase separation of the phase change absorbent.

Description

Technical Field

[0001] This invention relates to the field of phase separation device technology, and is a phase separator and phase separation method for continuous phase separation of phase change absorbents. Background Technology

[0002] Phase change absorbents (PCIs) are a relatively new carbon capture concept proposed in the last decade. Before absorbing CO2, PCIs are homogeneous; after CO2 absorption, they spontaneously form two immiscible liquid phases: a CO2-poor phase (upper phase) and a CO2-rich phase (lower phase). Only the rich phase enters the regeneration unit. The advantages of PCIs are: CO2 is enriched in one phase, increasing the CO2 loading capacity of the PCIe, which increases the CO2 recycling capacity and reduces regeneration energy consumption; on the other hand, it significantly reduces the amount of liquid entering the regeneration unit, thereby substantially reducing the ineffective latent heat of vaporization and the sensible heat of the absorbent. Experimental studies and process simulations demonstrate that PCIs have enormous potential for reducing energy consumption.

[0003] Compared to traditional absorbents, phase change absorbents spontaneously enrich and separate into two phases after absorption. However, due to the significant changes in viscosity and surface tension during the phase change process, the separation process between the organic and support phases in the enriched liquid phase varies with changes in physical properties, making it difficult to control and potentially increasing equipment investment and absorbent usage. Therefore, the practical application of phase change absorbents urgently requires the design and development of dedicated phase separation equipment to improve the phase separation rate, shorten the critical phase separation residence time, and reduce system material consumption.

[0004] Patent application CN118356771A discloses a phase change separator and a phase change separation control method. The separator has four overflow plates arranged longitudinally, dividing it into five chambers, with the absorbent overflowing between each chamber. However, the document does not mention the principle of phase separation, the separation effect is unclear, and key parameters such as equipment volume and critical phase separation residence time are not provided, making it indistinguishable from traditional liquid-liquid settling separators.

[0005] Patent application CN120189732A discloses a phase-separation device and its application in the phase-separation treatment of two-phase absorbents for carbon capture. The device's housing contains a top phase-separation chamber, a phase-separation chamber, and a separation chamber connected sequentially. The pre-phase-separation chamber includes a hydrocyclone and a rectifier plate. The phase-separation chamber includes a phase-separation reinforcement plate and a rotating fixing frame, the latter allowing adjustment of the phase-separation reinforcement plate's angle. The surface of the phase-separation reinforcement plate is coated with a hydrophilic material, a hydrophobic material, or a combination thereof. The hydrophilic and hydrophobic materials used in this application are both dense materials, preventing absorbent permeability. Furthermore, the hydrocyclone and the phase-separation reinforcement plate with angle adjustment function have complex structures and high costs.

[0006] Patent application CN217662456U discloses a carbon dioxide capture system with an embedded phase separator for phase change absorbents. The structure and phase separation principle of that phase separator are completely different from those in this application.

[0007] Patent application CN120459673A discloses a horizontal coalescing phase separator suitable for phase separation of lean and rich liquids in phase change absorbents. Its main innovation lies in the use of coalescing packing coupled with centrifugal phase separation technology within the separator. The coalescing packing is a fibrous material, including one or more combinations of stainless steel fiber, nylon fiber, polytetrafluoroethylene fiber, and glass fiber. However, the phase separator described in this document uses centrifugal equipment, resulting in high energy consumption and difficulty in control.

[0008] Patent application CN120695495A discloses a centrifugal-gravity coupled liquid-liquid phase separator, which cascades centrifugal phase separation with gravity sedimentation phase separation. The liquid is first centrifuged and then enters the gravity phase separator. However, its centrifugal separation has high energy consumption, and even slight changes in inlet flow rate and liquid properties can lead to re-emulsification, reducing its effectiveness.

[0009] The existing phase separators mentioned above mainly involve adding a large number of complex structures and special coalescing materials, which leads to complex manufacturing and control, and high equipment costs. Furthermore, they lack data on equipment volume, making it impossible to determine the critical phase separation residence time required for different phase change absorbers, thus hindering their integration with actual industrial absorption and desorption processes. Summary of the Invention

[0010] This invention provides a phase separator and a phase separation method for continuous phase separation of phase change absorbents, which can effectively shorten the critical phase separation residence time.

[0011] The technical solution of this invention is achieved through the following measures: A phase separator for continuous phase separation of a phase change absorbent includes a baffle plate, an upper baffle plate, a lower baffle plate, and a housing. The front, rear, and right sides of the upper baffle plate are respectively sealed to the front, rear, and right sides of the inner wall of the housing. The lower baffle plate is fixed inside the housing below the upper baffle plate, and its front, rear, and right sides are respectively sealed to the front, rear, and right sides of the inner wall of the housing. A feed inlet is provided on the right side of the housing between the upper and lower baffle plates. The vertical distance between the upper and lower baffle plates gradually decreases from right to left. The left sides of both the upper and lower baffle plates are spaced from the left side of the inner wall of the housing, forming a gap between the left sides of the upper and lower baffle plates. At the pre-phase flow outlet, several baffles perpendicular to the feed inlet are fixed at intervals between the upper and lower baffles, forming a baffle channel. An upper filter membrane parallel to the upper baffle is installed in the shell above the upper baffle, forming an upper auxiliary phase separation channel between the upper baffle and the upper filter membrane. An upper phase region is formed in the shell above the upper filter membrane, and an upper phase outlet is provided on the shell corresponding to the upper phase region. A lower filter membrane parallel to the lower baffle is installed in the shell below the lower baffle, forming a lower auxiliary phase separation channel between the lower baffle and the lower filter membrane. A lower phase region is formed in the shell below the lower filter membrane, and a lower phase outlet is provided on the shell corresponding to the lower phase region. The upper and lower filter membranes are hydrophilic or hydrophobic membranes.

[0012] The following are further optimizations and / or improvements to the above-mentioned technical solution:

[0013] Furthermore, the aforementioned baffles are in the form of three to five.

[0014] Furthermore, the angle between the upper partition and the horizontal direction, and the angle between the lower partition and the horizontal direction, are both 10 to 15 degrees.

[0015] Furthermore, the interval between the adjacent baffles is 50mm to 100mm.

[0016] Furthermore, the material of the above-mentioned hydrophobic membrane is one of polytetrafluoroethylene, polyvinylidene fluoride, and polypropylene, with a membrane pore diameter ranging from 0.1 μm to 10 μm and a membrane thickness of 0.1 mm.

[0017] Furthermore, the material of the above-mentioned hydrophilic membrane is one of hydrophilic modified polyethersulfone, cellulose acetate, and polyvinyl alcohol, with a membrane pore diameter ranging from 0.1 μm to 10 μm and a membrane thickness of 0.1 mm.

[0018] The second technical solution of the present invention is achieved through the following measures: a phase separation method for a phase separator used for continuous phase separation of phase change absorbents, comprising:

[0019] The phase change absorbent to be separated enters the shell through the feed inlet and then flows along the baffle channel between the baffles. During the flow in the baffle channel, the phase change absorbent continuously changes its flow velocity and direction, thereby performing pre-phase separation to form an upper phase and a lower phase. The pre-separated phase change absorbent then flows out from the pre-separated outlet. Because the upper phase formed by pre-separation has a lower density, the upper phase, carrying some of the lower phase, overflows upward to the upper auxiliary phase separation channel and comes into contact with the upper filter membrane. The upper phase passes through the upper filter membrane and enters the upper phase zone, while the lower phase is retained by the upper filter membrane. The lower phase, carrying some of the upper phase, flows downward to the lower auxiliary phase separation channel and comes into contact with the lower filter membrane. The lower phase passes through the lower filter membrane and enters the lower phase zone, while the upper phase is retained by the lower filter membrane. The upper phase in the upper phase zone is discharged through the upper phase outlet, and the lower phase in the lower phase zone is discharged through the lower phase outlet. In this way, the phase change absorbent is continuously separated into phases.

[0020] The following are further optimizations and / or improvements to the above-mentioned technical solution:

[0021] Furthermore, when the lower phase is water, the upper filter membrane is a hydrophobic membrane and the lower filter membrane is a hydrophilic membrane. The phase change absorbent to be separated enters the shell through the feed inlet and then flows along the baffle channel between the baffles. During the flow in the baffle channel, the phase change absorbent continuously changes its flow speed and direction, thereby performing pre-phase separation to form an upper phase and a lower phase. The phase change absorbent after pre-phase separation then flows out from the pre-phase separation outlet. Because the upper phase formed by pre-phase separation has a lower density, the upper phase carrying part of the lower phase overflows upward to the upper auxiliary phase separation channel and comes into contact with the hydrophobic membrane. The upper phase passes through the hydrophobic membrane and enters the upper phase zone, while the lower phase is trapped by the hydrophobic membrane. The lower phase carrying part of the upper phase flows downward to the lower auxiliary phase separation channel and comes into contact with the hydrophilic membrane. The lower phase passes through the hydrophilic membrane and enters the lower phase zone, while the upper phase is trapped by the hydrophilic membrane. The upper phase in the upper phase zone is discharged through the upper phase outlet, and the lower phase in the lower phase zone is discharged through the lower phase outlet. In this way, the phase change absorbent is continuously separated.

[0022] The beneficial effects of this invention are as follows:

[0023] (1) The phase separator designed in this invention adopts a combination structure of baffle, hydrophobic membrane and hydrophilic membrane, which can efficiently perform continuous phase separation treatment of phase change absorbent. When the volume of the phase separator is the same, the critical phase separation residence time can be significantly shortened, thereby significantly improving the phase separation efficiency, realizing rapid and complete separation of upper and lower phases, thereby greatly reducing the operating cost of the process and realizing efficient and low-energy phase separation of phase change absorbent.

[0024] (2) By optimizing structural parameters, such as the number of baffles and the tilt angle of the upper and lower baffles, this invention significantly reduces the critical phase separation residence time and equipment volume required for phase separation, thereby reducing the manufacturing and operating costs of the equipment and improving energy utilization efficiency.

[0025] (3) The phase splitter of the present invention adopts a continuous operation design, which reduces heat loss and equipment wear, improves the stability and reliability of the system, and realizes effective heat recovery and utilization.

[0026] (4) The phase separator described in this invention can be flexibly adapted to various industrial scenarios by adjusting design parameters (such as the number of baffles, the tilt angle of the upper and lower baffles) according to the composition and load conditions of different phase change absorbents, and meets the needs of carbon capture systems of different scales and types, and has wide applicability.

[0027] (5) The phase separator described in this invention has made significant progress in reducing energy consumption, reducing equipment size, and improving phase separation efficiency. It provides an efficient, energy-saving, and economical solution for the application of phase change absorbents in the field of carbon capture, which helps to promote the large-scale commercial application of carbon capture technology. Attached Figure Description

[0028] Appendix Figure 1 This is a schematic diagram of the main structure of a phase separator used for continuous phase separation of phase change absorbents.

[0029] The codes in the attached diagram are as follows: 1 is the feed pipe, 2 is the upper phase discharge pipe, 3 is the lower phase discharge pipe, 4 is the baffle, 5 is the upper partition, 6 is the lower partition, 7 is the shell, 8 is the pre-phase separation outlet, 9 is the baffle channel, 10 is the upper filter membrane, 11 is the upper auxiliary phase separation channel, 12 is the upper phase zone, 13 is the lower filter membrane, 14 is the lower auxiliary phase separation channel, 15 is the lower phase zone, and α is the included angle. Detailed Implementation

[0030] The present invention is not limited to the following embodiments, and the specific implementation can be determined according to the technical solution of the present invention and the actual situation.

[0031] For ease of description, the relative positions of the components are described based on the appendix to the instruction manual. Figure 1 The layout is described using a diagrammatic method, such as the positional relationships of front, back, top, bottom, left, and right, which are based on the instructions attached. Figure 1 The orientation of the layout is determined by the direction of the map.

[0032] Unless otherwise specified, all chemical reagents and chemical products mentioned in this invention are known and commonly used chemical reagents and chemical products in the prior art; unless otherwise specified, all percentages in this invention are mass percentages.

[0033] like Figure 1As shown, this invention provides a phase separator for continuous phase separation of a phase change absorbent, including a baffle 4, an upper baffle 5, a lower baffle 6, and a housing 7. The front, rear, and right sides of the upper baffle 5 are respectively sealed to the front, rear, and right sides of the inner wall of the housing 7. The lower baffle 6 is fixed inside the housing 7 below the upper baffle 5, and its front, rear, and right sides are respectively sealed to the front, rear, and right sides of the inner wall of the housing 7. A feed inlet is provided on the right side of the housing 7 between the upper baffle 5 and the lower baffle 6. The vertical distance between the upper baffle 5 and the lower baffle 6 gradually decreases from right to left. The left sides of both the upper baffle 5 and the lower baffle 6 are spaced from the left side of the inner wall of the housing 7. A pre-phase separation outlet 8 is formed between the left sides of the upper baffle 5 and the lower baffle 6. Several baffles 4 perpendicular to the feed inlet are fixed at intervals on the left and right, forming a baffle channel 9 between the baffles 4; an upper filter membrane 10 parallel to the upper baffle 5 is provided in the shell 7 above the upper baffle 5, and an upper auxiliary phase separation channel 11 is formed between the upper baffle 5 and the upper filter membrane 10; an upper phase region 12 is formed in the shell 7 above the upper filter membrane 10, and an upper phase outlet is provided on the shell 7 corresponding to the upper phase region 12; a lower filter membrane 13 parallel to the lower baffle 6 is provided in the shell 7 below the lower baffle 6, and a lower auxiliary phase separation channel 14 is formed between the lower baffle 6 and the lower filter membrane 13; a lower phase region 15 is formed in the shell 7 below the lower filter membrane 13, and a lower phase outlet is provided on the shell 7 corresponding to the lower phase region 15; the upper filter membrane 10 and the lower filter membrane 13 are hydrophilic or hydrophobic membranes.

[0034] Whether the upper filter membrane 10 and the lower filter membrane 13 are hydrophilic or hydrophobic depends on the composition of the phase change absorbent. For example, when the phase change absorbent is composed of monoethanolamine and water, since the density of monoethanolamine is greater than that of water, and it is necessary to separate the two, then the upper filter membrane 10 is a hydrophilic membrane and the lower filter membrane 13 is a hydrophobic membrane.

[0035] Due to the action of the baffle 4 and the inclined upper and lower baffles 5 and 6, the phase change absorbent continuously changes its flow velocity and direction within the baffle channel 9, thereby increasing the collision probability between phase change absorbent droplets, promoting droplet coalescence and phase separation, and achieving a pre-phase separation effect. The pre-separated phase change absorbent flows out from the pre-separated outlet 8. The upper phase formed by pre-separation has a lower density (when the lower phase is water, the upper filter membrane 10 is a hydrophobic membrane, and the lower filter membrane 13 is a hydrophilic membrane), and overflows upward to the upper auxiliary phase separation channel 11, where it contacts the hydrophobic membrane. Due to its hydrophobicity, the hydrophobic membrane allows the upper phase to pass through while retaining the lower phase. The lower phase formed by pre-separation has a higher density, and flows downward to the auxiliary phase separation channel, where it contacts the hydrophilic membrane. Due to its hydrophilicity, the hydrophilic membrane allows the lower phase to pass through while retaining the upper phase.

[0036] The design of the gradually decreasing vertical distance between the upper partition 5 and the lower partition 6 from right to left, along with the hydrophilic and hydrophobic membranes parallel to the upper partition 5 and the lower partition 6 respectively, not only makes the phase separator compact and small in size, but also allows for continuous phase separation of the phase change absorbent. Simultaneously, the gradually decreasing vertical distance between the upper partition 5 and the lower partition 6 from right to left causes the flow cross-sectional area of ​​the phase change absorbent to continuously decrease as it flows from left to right. After exiting the pre-phase separation outlet 8, the flow cross-sectional area increases again. Combined with the baffle 4, this forces the flow direction and velocity of the phase change absorbent to change significantly multiple times within the phase separator, increasing the droplet contact probability, improving droplet coalescence speed, and promoting the phase separation effect.

[0037] To improve phase separation efficiency and shorten the critical phase separation residence time, the baffles 4 are three to five in number; and the angles α between the upper baffle 5 and the horizontal direction and the lower baffle 6 and the horizontal direction are both 10 to 15 degrees. Under the premise of the same phase separator volume, if there are fewer than three baffles 4, it is difficult to meet the pre-phase separation requirements, the phase separation effect between the upper and lower phases is poor, and the critical phase separation residence time is longer; if there are more than five baffles 4, the formed baffle channel 9 becomes narrower, and the resistance increases when the phase change absorbent passes through the baffle channel 9, reducing the collision probability between phase change absorbent droplets, thereby reducing the pre-phase separation effect.

[0038] As required, the interval between adjacent baffles 4 is 50mm to 100mm.

[0039] As required, the hydrophobic membrane is an organic polymer porous membrane, and the material of the hydrophobic membrane is one of polytetrafluoroethylene, polyvinylidene fluoride, and polypropylene. The membrane pore diameter ranges from 0.1 μm to 10 μm, and the membrane thickness is 0.1 mm.

[0040] As required, the hydrophilic membrane is an organic polymer porous membrane, and the material of the hydrophilic membrane is one of hydrophilic modified polyethersulfone, cellulose acetate, and polyvinyl alcohol. The membrane pore diameter ranges from 0.1 μm to 10 μm, and the membrane thickness is 0.1 mm.

[0041] like Figure 1 As shown, the present invention also provides a phase separation method for a phase separator used for continuous phase separation of phase change absorbents, comprising:

[0042] The feed inlet is connected to feed pipe 1, the upper phase outlet is connected to upper phase outlet pipe 2, and the lower phase outlet is connected to lower phase outlet pipe 3. The phase change absorbent to be separated enters the shell 7 through the feed inlet and then flows along the baffle channel 9 between the baffles 4. During the flow in the baffle channel 9, the phase change absorbent continuously changes its flow velocity and direction, thereby performing pre-phase separation to form an upper phase and a lower phase. The pre-separated phase change absorbent then flows out from the pre-separated outlet 8. Because the upper phase formed by pre-phase separation has a lower density, it carries some of the lower phase. After overflowing upwards to the upper auxiliary phase separation channel 11, the upper phase comes into contact with the upper filter membrane 10. The upper phase passes through the upper filter membrane 10 and enters the upper phase zone 12. The lower phase is trapped by the upper filter membrane 10. The lower phase, carrying part of the upper phase, flows downwards to the lower auxiliary phase separation channel 14 and comes into contact with the lower filter membrane 13. The lower phase passes through the lower filter membrane 13 and enters the lower phase zone 15. The upper phase is trapped by the lower filter membrane 13. The upper phase in the upper phase zone 12 is discharged through the upper phase outlet, and the lower phase in the lower phase zone 15 is discharged through the lower phase outlet. In this way, the phase change absorbent is continuously phase separated.

[0043] When the lower phase is water, the upper filter membrane 10 is a hydrophobic membrane and the lower filter membrane 13 is a hydrophilic membrane. The phase change absorbent to be separated enters the shell 7 through the feed inlet and then flows along the baffle channel 9 between the baffles 4. During the flow in the baffle channel 9, the phase change absorbent continuously changes its flow velocity and direction, thereby performing pre-phase separation to form an upper phase and a lower phase. The pre-separated phase change absorbent then flows out from the pre-separated outlet 8. Because the upper phase formed by pre-phase separation has a lower density, it carries some... The upper phase of the lower phase overflows upward to the upper auxiliary phase separation channel 11 and comes into contact with the hydrophobic membrane. The upper phase passes through the hydrophobic membrane and enters the upper phase region 12. The lower phase is trapped by the hydrophobic membrane. The lower phase, carrying part of the upper phase, flows downward to the lower auxiliary phase separation channel 14 and comes into contact with the hydrophilic membrane. The lower phase passes through the hydrophilic membrane and enters the lower phase region 15. The upper phase is trapped by the hydrophilic membrane. The upper phase in the upper phase region 12 is discharged through the upper phase outlet, and the lower phase in the lower phase region 15 is discharged through the lower phase outlet. In this way, the phase change absorbent is continuously phase separated.

[0044] The phase change absorbent used in the phase separation efficiency experiment of the phase separator below has the following composition: 30 wt.% MEA (monoethanolamine), 40 wt.% NHD (polyethylene glycol dimethyl ether), and 30 wt.% H2O. The phase change absorbent loading is 3.0 mol / kg, and the volume ratio of the upper and lower phases is approximately 1:1. The density of the upper phase of the phase change absorbent is approximately 1.01 g / mL, and the density of the lower phase is approximately 1.14 g / mL, with a density difference of approximately 0.13 g / mL. The viscosity of the upper phase of the phase change absorbent is approximately 4 mPa·s, and the viscosity of the lower phase is approximately 20 mPa·s, with a viscosity difference of approximately 16 mPa·s. Therefore, the upper phase of this phase separator is water, the upper filter membrane 10 is a hydrophilic membrane, and the lower filter membrane 13 is a hydrophobic membrane.

[0045] By comparing the critical phase separation residence time of the phase separators in the comparative examples and the phase separation test, the phase separation effect of the phase separators is quantitatively compared. The smaller the critical phase separation residence time, the better the phase separation effect and the higher the phase separation efficiency; the larger the critical phase separation residence time, the worse the phase separation effect and the lower the phase separation efficiency. The critical phase separation flow rate is determined as follows: During the phase separation experiment, the flow rate of the phase change absorbent at the inlet is continuously increased from small to large until the area occupied by the emulsion formed in the phase separator reaches its maximum. At this point, the phase change absorbent that is not completely separated flows out from the upper and lower phase outlets of the phase separator (i.e., the phase separation at the upper and lower phase outlets is incomplete). The flow rate of the phase change absorbent at the inlet at this time is the critical phase separation flow rate of the phase separator. The critical phase separation residence time is calculated as follows: The ratio of the phase separator volume to the critical phase separation flow rate is the critical phase separation residence time.

[0046] The phase separators described in the following embodiments all refer to the phase separators for continuous phase separation of phase change absorbents as described in this invention.

[0047] The present invention will be further described below with reference to embodiments:

[0048] Example 1

[0049] The phase separator has the following characteristics: a volume of 12 L, five baffles 4, with the upper baffle 5 and the horizontal direction forming an angle α with the horizontal direction, and the lower baffle 6 and the horizontal direction both forming an angle α of 15 degrees. The hydrophobic membrane material is polytetrafluoroethylene with a pore diameter of 1 μm. The hydrophilic membrane material is cellulose acetate with a pore diameter of 1 μm. The membrane thickness of both the hydrophobic and hydrophilic membrane materials is 0.1 mm. The spacing between adjacent baffles 4 is 50 mm. In experiments using this phase separator, with a phase change absorbent feed flow rate of 100 L / h, the upper and lower phase outlets were completely separated. When the flow rate was greater than 100 L / h, the separation was incomplete. This indicates that the critical phase separation flow rate of the phase separator is 100 L / h, i.e., the critical phase separation residence time is 7.2 min.

[0050] Example 2

[0051] The phase separator has the following characteristics: a volume of 12 L, three baffles 4, an angle α between the upper baffle 5 and the horizontal direction, and an angle α between the lower baffle 6 and the horizontal direction, both of which are 15 degrees. The hydrophobic membrane material is polytetrafluoroethylene with a pore diameter of 1 μm. The hydrophilic membrane material is cellulose acetate with a pore diameter of 1 μm. The membrane thickness of both the hydrophobic and hydrophilic membrane materials is 0.1 mm. The spacing between adjacent baffles 4 is 50 mm. In experiments using this phase separator, when the phase change absorbent feed flow rate is 90 L / h, the upper and lower phase outlets are completely separated. When the flow rate is greater than 90 L / h, the separation is incomplete. This indicates that the critical phase separation flow rate of the phase separator is 90 L / h, i.e., the critical phase separation residence time is 8 min.

[0052] Comparative Example 1

[0053] The phase separator features the following characteristics: a volume of 12 L, no baffles, and angles α between the upper baffle 5 and the horizontal direction and between the lower baffle 6 and the horizontal direction are both 15 degrees. The hydrophobic membrane material is polytetrafluoroethylene with a pore diameter of 1 μm, and the hydrophilic membrane material is cellulose acetate with a pore diameter of 1 μm. The membrane thickness of both materials is 0.1 mm, and the spacing between adjacent baffles 4 is 50 mm. In experiments using this phase separator, with a phase change absorbent feed flow rate of 50 L / h, the upper and lower phase outlets were completely separated. When the flow rate exceeded 50 L / h, the phase separation was incomplete. This indicates that the critical phase separation flow rate of the phase separator is 50 L / h, i.e., the critical phase separation residence time is 14.4 min.

[0054] Example 3

[0055] The phase separator has the following characteristics: a volume of 12 L, three baffles 4, with the upper baffle 5 and the horizontal direction forming an angle α with the horizontal direction, and the lower baffle 6 and the horizontal direction both forming an angle α of 10 degrees. The hydrophobic membrane material is polytetrafluoroethylene with a pore diameter of 1 μm. The hydrophilic membrane material is cellulose acetate with a pore diameter of 1 μm. The membrane thickness of both the hydrophobic and hydrophilic membrane materials is 0.1 mm. The spacing between adjacent baffles 4 is 70 mm. In experiments using this phase separator, with a phase change absorbent feed flow rate of 75 L / h, the upper and lower phase outlets were completely separated. When the flow rate was greater than 75 L / h, the separation was incomplete. This indicates that the critical phase separation flow rate of the phase separator is 75 L / h, i.e., the critical phase separation residence time is 9.6 min.

[0056] Comparative Example 2

[0057] The phase separator has the following characteristics: a volume of 12 L, 5 baffles, with both the upper baffle 5 and the horizontal direction forming an angle α with the horizontal direction, and the lower baffle 6 and the horizontal direction forming an angle α with the horizontal direction, both being 0 degrees. The hydrophobic membrane material is polytetrafluoroethylene (PTFE) with a pore diameter of 1 μm. The hydrophilic membrane material is cellulose acetate with a pore diameter of 1 μm. The membrane thickness of both the hydrophobic and hydrophilic membrane materials is 0.1 mm. The spacing between adjacent baffles 4 is 50 mm. In experiments using this phase separator, with a phase change absorbent feed flow rate of 60 L / h, the upper and lower phase outlets were completely separated. When the flow rate exceeded 60 L / h, the phase separation at the upper and lower phase outlets was incomplete. This indicates that the critical phase separation flow rate of the phase separator is 60 L / h, i.e., the critical phase separation residence time is 12 min.

[0058] Example 4

[0059] The phase separator features the following characteristics: a volume of 4 L, five baffles 4, with the upper baffle 5 and the horizontal direction forming an angle α with the horizontal direction, and the lower baffle 6 and the horizontal direction both forming an angle α of 15 degrees. The hydrophobic membrane material is polypropylene with a pore diameter of 1 μm. The hydrophilic membrane material is cellulose acetate with a pore diameter of 1 μm. The membrane thickness of both the hydrophobic and hydrophilic membrane materials is 0.1 mm. The spacing between adjacent baffles 4 is 50 mm. In experiments using this phase separator, with a phase change absorbent feed flow rate of 42 L / h, complete phase separation occurred at the upper and lower phase outlets. When the flow rate exceeded 42 L / h, phase separation at the upper and lower phase outlets was incomplete. This indicates that the critical phase separation flow rate of the phase separator is 42 L / h, i.e., the critical phase separation residence time is 5.7 min.

[0060] Example 5

[0061] The phase separator has the following characteristics: a volume of 12 L, three baffles 4, with the upper baffle 5 and the horizontal direction forming an angle α with the horizontal direction, and the lower baffle 6 and the horizontal direction both forming an angle α of 15 degrees. The hydrophobic membrane material is polyvinylidene fluoride with a pore diameter of 0.2 μm. The hydrophilic membrane material is hydrophilic modified polyethersulfone with a pore diameter of 0.2 μm. The membrane thickness of both the hydrophobic and hydrophilic membrane materials is 0.1 mm, and the interval between adjacent baffles 4 is 50 mm. In experiments using this phase separator, with a phase change absorbent feed flow rate of 80 L / h, the upper and lower phase outlets were completely separated. When the flow rate was greater than 80 L / h, the separation at the upper and lower phase outlets was incomplete. This indicates that the critical phase separation flow rate of the phase separator is 80 L / h, i.e., the critical phase separation residence time is 9 min.

[0062] Comparative Example 3

[0063] The phase separator has the following characteristics: a volume of 12 L, 5 baffles, and angles α between the upper baffle 5 and the horizontal direction, and between the lower baffle 6 and the horizontal direction, are both 15 degrees. No hydrophobic or hydrophilic membranes are installed in the phase separator; the thickness of both hydrophobic and hydrophilic membrane materials is 0.1 mm, and the spacing between adjacent baffles 4 is 50 mm. In experiments using this phase separator, with a phase change absorbent feed flow rate of 55 L / h, the upper and lower phase outlets were completely separated. When the flow rate exceeded 55 L / h, the phase separation at the upper and lower phase outlets was incomplete. This indicates that the critical phase separation flow rate of the phase separator is 55 L / h, i.e., the critical phase separation residence time is 13 min.

[0064] As can be seen from the above embodiments and comparative examples, in phase splitters of the same volume, the critical phase splitting dwell time of the phase splitter in the embodiments is less than that of the phase splitter in the comparative examples. This shows that the control of the number of baffles, the upper baffle, and the tilt angle of the lower baffle in the present invention can significantly shorten the critical phase splitting dwell time.

[0065] The above technical features constitute various embodiments of the present invention, which have strong adaptability and implementation effect. Unnecessary technical features can be added or removed according to actual needs to meet the needs of different situations.

Claims

1. A phase separator for continuous phase separation of a phase change absorbent, characterized in that The baffles, the upper baffle, the lower baffle and the shell are connected tightly, the front side, the back side and the right side of the upper baffle are connected tightly with the inner wall of the shell, the lower baffle is fixed in the shell below the upper baffle, the front side, the back side and the right side of the lower baffle are connected tightly with the inner wall of the shell, the right side of the shell between the upper baffle and the lower baffle is provided with a feeding port, the vertical distance between the upper baffle and the lower baffle gradually decreases from right to left, the left side of the upper baffle and the left side of the lower baffle are provided with a space with the left side of the inner wall of the shell, the pre-phase separation outlet is formed between the left side of the upper baffle and the left side of the lower baffle, a plurality of baffles perpendicular to the feeding port are fixed between the upper baffle and the lower baffle, the flow channel is formed between the baffles; the upper filter membrane parallel to the upper baffle is arranged in the shell above the upper baffle, the upper auxiliary phase separation channel is formed between the upper baffle and the upper filter membrane, the upper phase area is formed in the shell above the upper filter membrane, the upper phase outlet is arranged on the shell corresponding to the upper phase area, the lower filter membrane parallel to the lower baffle is arranged in the shell below the lower baffle, the lower auxiliary phase separation channel is formed between the lower baffle and the lower filter membrane, the lower phase area is formed in the shell below the lower filter membrane, the lower phase outlet is arranged on the shell corresponding to the lower phase area, the upper filter membrane and the lower filter membrane are hydrophilic membranes or hydrophobic membranes; The baffles are three to five, the angle between the upper baffle and the horizontal direction and the angle between the lower baffle and the horizontal direction are 10 to 15 degrees.

2. The phase separator for continuous phase separation of phase change absorbent according to claim 1, characterized in that, The interval between adjacent baffles is 50 to 100 mm.

3. The phase separator for continuous phase separation of phase change adsorbent according to claim 1 or 2, characterized in that, The material of the hydrophobic membrane is one of polytetrafluoroethylene, polyvinylidene fluoride and polypropylene, the pore diameter of the membrane is 0.1 to 10 μm, and the thickness of the membrane is 0.1 mm. Or / and, the material of the hydrophilic membrane is one of hydrophilic modified polyether sulfone, cellulose acetate and polyvinyl alcohol, the pore diameter of the membrane is 0.1 to 10 μm, and the thickness of the membrane is 0.1 mm.

4. A phase separation method for a phase separator for continuously separating a phase change absorbent according to any one of claims 1 to 3, characterized by, The phase change absorbent to be phase separated enters the shell from the feeding port, then flows along the flow channel between the baffles, the phase change absorbent changes the flow speed and direction during the flow in the flow channel, thereby pre-phase separation is carried out, the upper phase and the lower phase are formed, the phase change absorbent after pre-phase separation then flows out from the pre-phase separation outlet, the upper phase formed by pre-phase separation is overflowed to the upper auxiliary phase separation channel due to the lower density, and the upper phase contacts the upper filter membrane, the upper phase passes through the upper filter membrane to enter the upper phase area, the lower phase is intercepted by the upper filter membrane, the lower phase with part of the upper phase flows to the lower auxiliary phase separation channel, and the lower phase contacts the lower filter membrane, the lower phase passes through the lower filter membrane to enter the lower phase area, the upper phase is intercepted by the lower filter membrane, the upper phase in the upper phase area is discharged from the upper phase outlet, the lower phase in the lower phase area is discharged from the lower phase outlet, thereby continuous phase separation of the phase change absorbent is carried out. ​ 5. The phase-splitting method of claim 4, wherein, When the lower phase is water, the upper filter membrane is a hydrophobic membrane and the lower filter membrane is a hydrophilic membrane, the phase change absorbent to be separated enters the shell from the feed port, then flows along the baffle channel between the baffles, and in the process of flowing along the baffle channel, the phase change absorbent continuously changes the flow speed and direction, thereby pre-separating to form an upper phase and a lower phase, the phase change absorbent after pre-separation then flows out from the pre-separation flow outlet, and because the upper phase formed by pre-separation is low in density, the upper phase with part of the lower phase entrained flows upward to the upper auxiliary separation channel, then contacts the hydrophobic membrane, the upper phase passes through the hydrophobic membrane to enter the upper phase area, the lower phase is intercepted by the hydrophobic membrane, the lower phase with part of the upper phase entrained flows downward to the lower auxiliary separation channel, then contacts the hydrophilic membrane, the lower phase passes through the hydrophilic membrane to enter the lower phase area, the upper phase is intercepted by the hydrophilic membrane, the upper phase in the upper phase area is discharged through the upper phase discharge port, and the lower phase in the lower phase area is discharged through the lower phase discharge port, thereby continuously separating the phase change absorbent in this way.

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