CN211753192U

CN211753192U - Gas-liquid coalescence filter core and contain its filter equipment

Info

Publication number: CN211753192U
Application number: CN202020002036.4U
Authority: CN
Inventors: 陈锋; 刘佳霖; 吴小林; 姬忠礼; 邢颜凝; 卢锦杰
Original assignee: China University of Petroleum Beijing
Current assignee: China University of Petroleum Beijing
Priority date: 2020-01-02
Filing date: 2020-01-02
Publication date: 2020-10-27
Anticipated expiration: 2030-01-02

Abstract

The utility model provides a gas-liquid coalescence filter core and contain its filter equipment. The filter element comprises a pre-separation layer, a coalescing layer and a drainage layer which are arranged in sequence along the airflow direction; the pre-separation layer is a porous structure layer with water and oil repellency formed by profiled fibers; the coalescence layer is a porous structure layer formed by profiled fibers and is divided into a hydrophobic and oleophobic area and a hydrophilic and lipophilic area which are arranged at intervals along the circumferential direction; the drainage layer is a porous structure layer formed by profiled fibers, the drainage layer is divided into a hydrophilic and hydrophilic oil-repellent area and a hydrophobic and oil-repellent area along the thickness direction, the air inlet side is the hydrophilic and hydrophilic oil-repellent area, the air outlet side is the hydrophobic and oil-repellent area, and the thickness of the hydrophobic and oil-repellent area accounts for 1/3-2/3 of the total thickness of the drainage layer. The filter device containing the filter element can remarkably reduce the filtration pressure drop while improving the filtration efficiency.

Description

Gas-liquid coalescence filter core and contain its filter equipment

Technical Field

The utility model relates to a filter core especially relates to a filter core of filtering gas-liquid mixture, belongs to heterogeneous flow separation technical field.

Background

Condensate droplets and particles are often carried in the transportation process of industrial gases such as natural gas, coal bed gas and the like and the use process of compressed air, and the impurities can cause serious problems such as corrosive wear of pipelines, measurement failure of metering equipment, failure of a dry gas sealing system of a compressor, shutdown of a large compressor unit and the like. To remove impurities, gas-liquid filtration is widely used in the above-mentioned industrial sites. Wherein, the tiny liquid drops are mainly removed by the coalescence-separation action of the gas-liquid coalescence-filter element.

The working principle of the gas-liquid coalescence filter element is as follows: the gas containing liquid passes through the aggregation layer and the liquid drainage layer from the inside of the filter element. The aperture of the coalescence layer is small, the fiber is fine, the liquid drop is easy to be caught and coalesced on the fiber to form large liquid drop, and the transmission between layers is carried out in the coalescence layer under the action of gas driving force and the capillary force of hydrophilic and oleophilic materials. When the liquid is transported to the last layer of exhaust side of the coalescing layer, the liquid drops are not easy to be discharged due to the capillary force action between the fibers and the liquid drops of the coalescing layer, so that the liquid can be accumulated on the surface and form a liquid film. The obstruction of the gas flow by this liquid film is the main cause of the too high pressure drop. The droplets are only discharged when the gravitational force of the droplets is greater than the capillary force between the droplets and the material. The effect of traditional drainage layer is then to prevent that gas from causing the secondary to smuggle when passing through the liquid film, and then improves filtration efficiency.

The aggregation layer and the drainage layer are the key points of the filtering performance of the gas-liquid coalescence filter element, the aggregation layer is a filter material with small aperture formed by glass fiber and polypropylene fiber, and the drainage layer is a filter material with large aperture formed by polyester fiber, polypropylene fiber, aramid fiber and the like. The main function of the coalescence layer is to intercept and coalesce small drops into large drops for discharge, and the main function of the drainage layer is to provide a drainage channel to prevent secondary entrainment. The gas passes through the filter element accumulation layer and the liquid drainage layer from inside to outside in sequence.

At pipeline conveying gas's in-process, the liquid drop constantly is intercepted by the filter core, and the filter core pressure drop constantly risees, and this not only makes gas handling capacity diminish, and the too high filter core that causes is buckled damage failure very easily simultaneously to the pressure drop, and then leads to a large amount of liquid drops to get into filter low reaches, causes the harm to pipeline, equipment, leads to shutting down the maintenance when serious. In order to ensure the normal operation of core equipment, a plurality of filtering separators and coalescing separators are generally arranged in a gas station along the way, although the treatment capacity is large, the more filter elements are, the higher the pressure drop is, the larger the energy consumption is, and the filter element cost and the energy consumption cost are increased.

It is worth noting that: in the field of gas-liquid coalescing filtration, pressure drop and efficiency are two of the most significant indicators of concern. Low resistance and high efficiency filter elements have been the ultimate goal of development. The liquid drop absorption and interception of the fibers are promoted, the efficiency is improved, the liquid discharge of the reinforcing material after the liquid absorption and interception is well performed, the phenomenon that the efficiency is improved, excessive liquid is accumulated while the material is prevented, more liquid drops are carried by subsequent air flow, the efficiency is reduced, and meanwhile, the pressure drop is further increased due to the excessive liquid in the material. This loses the original significance of improving efficiency and reducing pressure drop.

The existing gas-liquid coalescence filter can improve the efficiency by increasing the number of filter element layers, the pore size gradient arrangement of a filter layer, the drainage layer and the like, but has no good performance in the aspect of pressure drop.

SUMMERY OF THE UTILITY MODEL

An object of the utility model is to provide a filter core of filtering gas-liquid, this filter core can show the filtration pressure drop that reduces the filter core when improving filtration efficiency.

Another object of the present invention is to provide a filter device, which comprises the above filter element of the present invention.

In order to achieve the technical purpose, the utility model provides a gas-liquid coalescence filter element, which comprises a pre-separation layer, a coalescence layer and a drainage layer which are arranged in sequence along the direction of gas flow;

wherein the pre-separation layer is a hydrophobic and oleophobic porous structure layer formed by profiled fibers, the aperture is 8-12 μm, and the thickness of the pre-separation layer is 1-2 mm;

the coalescence layer is a porous structure layer formed by profiled fibers, the aperture is 3-8 mu m, the thickness of the coalescence layer is 0.4-0.6 mm, and the coalescence layer is divided into a hydrophobic and oleophobic area and a hydrophilic and hydrophilic area which are arranged at intervals along the circumferential direction;

the drainage layer is a porous structure layer formed by profiled fibers, the pore diameter is 10-20 microns, the thickness of the drainage layer is 2-3 mm, the drainage layer is divided into a hydrophilic and hydrophilic oil-repellent area and a hydrophobic and oil-repellent area along the thickness direction, the air inlet side is the hydrophilic and hydrophilic area, the air outlet side is the hydrophobic and oil-repellent area, and the thickness of the hydrophobic and oil-repellent area is 1/3-2/3 of the total thickness of the drainage layer.

The utility model discloses a gas-liquid coalescence filter core adopts the dysmorphism fibre, the better interception liquid drop ability of great specific surface area through the dysmorphism fibre performance, the ability of absorption and transmission liquid is strengthened through the stronger liquid wicking ability of dysmorphism fibre, the specific hydrophobic oleophobic district of hydrophobic and hydrophilic oily district's setting of cooperation simultaneously prevents that liquid from accumulating in a large number in the filter core, make the filter core can better raise the efficiency, absorb liquid can discharge liquid again, promptly when improving filtration efficiency, can show the filtration pressure drop that reduces the filter core.

The utility model discloses a gas-liquid coalescence filter core contains profiled fiber pre-separation layer, profiled fiber coalescence layer, profiled fiber drainage layer.

Wherein, the utility model discloses a hydrophobic oleophobic profiled fiber pre-separation layer can carry out effectual interception to the large granule. A preseparation layer of a certain thickness may reduce the preseparation effect or add additional resistance. After the whole body is subjected to hydrophobic and oleophobic modification treatment, liquid drops can be quickly discharged and are not easy to accumulate in the liquid drops.

In one embodiment of the present invention, in the pre-separation layer, the raw material of the profiled fiber may be polyester fiber, polypropylene fiber or oleophilic fiber with approximate thickness (including oleophilic fiber obtained by modification). The shape of the fibers of the profiled fibers used is non-circular, such as cross, triangular or trilobal (shown in fig. 1); preferably a cross-shape. The diameter (circumscribed circle diameter) of the shaped fibers used for the pre-separation layer is 12 μm to 18 μm, preferably 15 μm to 16 μm.

In a specific embodiment of the present invention, the pre-separation layer is a single-layer structure. For example, the preseparation layer may consist of one or more sub-separation layers. Preferably, the pre-separation layer consists of 1 sub-separation layer.

In a specific embodiment of the present invention, the pre-separation layer can be obtained by needle punching or water needling of profiled fibers.

Wherein, the utility model discloses a profiled fiber coalescence layer with hydrophilic and hydrophilic oil-repellent district and hydrophobic and oil-repellent district adopts the profiled fiber in specific diameter and aperture, filtration, coalescence between performance fibre and the liquid drop that can be fine, and the filtering capability who realizes filtration efficiency and the common influence of filtration pressure drop is the highest. The larger specific surface area of the profiled fiber can effectively increase the liquid drop interception efficiency, and meanwhile, the stronger liquid wicking capability of the profiled fiber can accelerate the absorption and the migration of liquid.

In one embodiment of the present invention, in the aggregation layer, the foreign fiber is made of glass fiber or oleophilic fiber (including oleophilic fiber obtained by modification treatment) having a thickness similar to that of the glass fiber. The shape of the fibers of the profiled fibers used is non-circular, such as cross, triangular or trilobal (shown in fig. 1); preferably a cross-shape. The diameter (circumscribed circle diameter) of the profiled fiber adopted by the aggregation layer is 3-5 μm.

In one embodiment of the present invention, the coalescing layer is a multi-layer structure including a plurality of sub-coalescing layers. For example, the coalescing layer is formed from one or more coalescing layers. Preferably, the coalescing layer is comprised of 3-5 (4) subcondensing layers.

In a specific embodiment of the present invention, the coalescence layer can be obtained by dispersing and defibering the shaped fiber, and beating the shaped fiber.

In a specific embodiment of the present invention, the vertical cross section of the hydrophobic and oleophobic area of the coalescing layer of the present invention is an upright trapezoid, the trapezoidal structure fully utilizes the characteristics of the possible longitudinal distribution of liquid, the hydrophobic and oleophobic area with a larger bottom is more beneficial to the accumulation and discharge of liquid, and if under the working condition with smaller liquid content, the hydrophobic and oleophobic area is designed to be rectangular; a plurality of hydrophobic and oleophobic areas are arranged at equal intervals; preferably, the perimeter of the coalescence layer is 5 pi cm-12 pi cm, the coalescence layer comprises 4-8 hydrophobic and oleophobic areas, and when the perimeter diameter of the filter element is designed to be smaller or larger than the range, the hydrophobic and oleophobic areas are correspondingly reduced or increased; more preferably, the ratio of the length of the upper bottom to the length of the lower bottom of the upright trapezoid with the vertical section of the hydrophobic and oleophobic area is greater than or equal to 1/3 and less than 1, preferably 1/3-3/4.

The utility model discloses a conglomerate layer can make liquid distribution change, promotes the liquid drop from hydrophobic oleophobic district to hydrophilic oleophilic district, from last discharge extremely down, and hydrophobic oleophobic part has reduced the liquid that accumulates in the filter core inside simultaneously, has overcome and can cause the problem that is difficult to the flowing back when the profiled fiber absorbed liquid ability is stronger, and then has reduced the pressure drop.

Wherein, the utility model discloses a profiled fiber drainage layer have hydrophobic oleophobic district of water and hydrophilic oily district, and hydrophobic oily district prevents that the liquid drop secondary from smuggleing secretly. The drainage layer with a specific pore size can better absorb the liquid discharged by the aggregation layer and does not cause the increase of the pressure drop of the drainage layer. A drainage layer of a certain thickness simultaneously has a certain capacity to store liquid.

In one embodiment of the present invention, in the drainage layer, the raw material of the profiled fiber is polyester fiber, polypropylene fiber, or oleophilic fiber (including oleophilic fiber obtained by modification treatment) with approximate thickness. The shape of the fibers of the profiled fibers used is non-circular, such as cross, triangular or trilobal (shown in fig. 1); preferably a cross-shape. The diameter (circumscribed circle diameter) of the shaped fiber used in the liquid discharge layer is 12 μm to 18 μm, preferably 15 μm to 16 μm.

In a specific embodiment of the present invention, the drainage layer is a single-layer structure. For example, the drainage layer is composed of one or more than two sub-drainage layers; preferably, the drainage layer consists of 1 sub-drainage layer.

In a specific embodiment of the present invention, the drainage layer can be obtained by needle punching, water needling, etc. of the profiled fiber.

In a specific embodiment of the present invention, the thickness of the hydrophobic and oleophobic area of the drainage layer is 1/2 of the total thickness of the drainage layer.

The utility model discloses a flowing back layer has guaranteed that profiled fiber self absorbed liquid ability is stronger, promotes the discharge of liquid after the coalescence of coalescence layer, simultaneously, has guaranteed that liquid can not be in the inside accumulation of flowing back layer, causes the secondary of pressure drop to rise and the secondary of liquid drop to smuggly secretly, and effectual raising the efficiency reduces the pressure drop.

The utility model discloses an among the embodiment, this gas-liquid coalescence filter core still includes the support chassis, and the outer parcel of support chassis is separating layer, coalescence layer and drainage layer in advance.

In a specific embodiment of the present invention, the supporting framework can be made of non-metallic materials such as metal or polypropylene, and is used for supporting the outer filtering material, and the air flow flows out from the inner side of the framework along the radial direction.

The utility model discloses a gas-liquid coalescence filter core can show the filtration pressure drop that reduces the filter core when improving filtration efficiency. The filter element can be used for gas-liquid separation. The filter element has the accumulation efficiency of 99.48 to 99.78 percent for particles with the diameter of about 0.1 mu m, the number of penetrating particles is reduced by 30 percent, the accumulation efficiency of more than 0.3 mu m large particles is 99.83 to 99.99 percent, and the filtration pressure drop is reduced by about 2 KPa.

The utility model also provides a filter equipment, wherein, this filter equipment contains the utility model discloses an above-mentioned gas-liquid coalescence filter core. The device includes, but is not limited to, a gas-liquid coalescing filter.

Specifically, the three-layer structure of the filter element is respectively and sequentially and tightly wound on the filter framework, and the special-shaped fiber gas-liquid coalescence filter is formed by adhesive sealing with the upper metal sealing end cover and the lower metal sealing end cover.

The utility model discloses an each component part (preseparation layer, coalescence layer, drainage layer) of gas-liquid coalescence filter core all adopts the fibre that has special-shaped cross section, and the more traditional circular fibre of dysmorphism fibre compares, possess great specific surface area to change the flow field around the fibre to a certain extent, increase interception efficiency, to the dysmorphism fibre that has the slot, more impurity that get off by the filtration can be saved to the existence of slot, and prevent that the secondary from smuggleing secretly. Meanwhile, the capillary action is increased by the grooves, so that the absorption and transfer of liquid are facilitated, more liquid is discharged, and the pressure drop and the operation cost are effectively reduced.

The profiled fiber pre-separation layer enhances the interception effect on large particles and liquid drops, improves the efficiency, and ensures that the inside of the pre-separation layer is not blocked by the particles and the liquid due to the larger aperture; the profiled fiber aggregation layer improves the aggregation capability of small liquid drops and fibers, improves the efficiency, and simultaneously, the liquid is transported and transferred more quickly in the aggregation layer; the special-shaped fiber liquid drainage layer has a specific aperture, improves the absorption capacity of discharged liquid of the coalescence layer, effectively reduces pressure drop, solves the problem of overhigh pressure drop caused by accumulation of the liquid in the coalescence layer, and simultaneously ensures that liquid drops are not secondarily entrained.

The gas-liquid coalescence filter element of the utility model is provided with a specific hydrophobic and oleophobic area and a hydrophilic and lipophilic area for the pre-separation layer, the coalescence layer and the drainage layer respectively, so that large liquid drops are easier to fall off from the pre-separation layer, and the pressure drop and the subsequent coalescence layer are not easy to accumulate in the layer; for the coalescence layer, the hydrophilic and lipophilic regions and the hydrophobic and oleophobic regions are in patterned distribution, the hydrophilic and oleophobic parts guide liquid to move, the liquid distribution is changed, meanwhile, the trapezoidal stripes at the intervals of affinity and hydrophobicity are more beneficial to the accumulation of the liquid in the lipophilic region and the discharge of the liquid from top to bottom, and the accumulation of the liquid in the coalescence layer is effectively reduced; for the drainage layer, when guaranteeing stronger absorbed liquid ability, the gas discharge side is the interior liquid content that can effectual reduction accumulation in the drainage layer of hydrophobic oleophobic district, prevents that the liquid drop secondary from smuggleing secretly, improves filtration efficiency.

The utility model discloses a gas-liquid coalescence filter core with every layer structure twine in succession can, processing is simple and convenient, the appearance is compact, easy to assemble. Meanwhile, the special-shaped fiber and the reasonably arranged hydrophilic and lipophilic regions have the synergistic effect, so that the filter element has the excellent characteristics of large specific surface area, strong interception capability, strong liquid absorption and transfer capability and the like of the special-shaped fiber, and meanwhile, the problems of accumulation of liquid in the filter element, secondary rise of pressure drop, entrainment of liquid drops and the like caused by the special-shaped fiber are solved through reasonable modification. The two interact, so that the efficiency of the filter element is improved, and the pressure drop is reduced.

The utility model discloses a gas-liquid coalescence filter core can be under the current condition of filtering separation device in station, directly adopts the utility model discloses a profiled fiber filter core makes the filter core under the operating mode (the undulant operating mode of liquid content promptly) of the gaseous liquid content of different entries, and pressure drop, energy consumption are showing and are reducing, under the same operating mode, can prolong filter core life more than 3 times, save the running cost more than 30%.

Drawings

FIG. 1 is a schematic view of the fiber shape of a shaped fiber.

Fig. 2A is a schematic front view of the gas-liquid coalescing filter according to example 1.

Fig. 2B is a schematic top view of the gas-liquid coalescing filter according to embodiment 1.

Fig. 3 is a schematic view of the patterning process of the profiled fiber coalescing layer of example 1.

Fig. 4 is a schematic view of the modified depth of the profiled fiber drainage layer of example 1.

Fig. 5 is a plot of pressure drop versus conventional filter element for the shaped fiber filter element of example 1.

Fig. 6 is a graph comparing the filtration efficiency of the profiled fiber filter element of example 1 to that of a conventional filter element.

Description of the main figures:

1. a support framework; 2. a profiled fiber pre-separation layer; 3. a profiled fiber coalescing layer; 4. and (4) draining the liquid layer by the profiled fibers.

Detailed Description

In order to clearly understand the technical features, objects and advantages of the present invention, the following detailed description is given to the technical solution of the present invention, but the technical solution of the present invention is not limited to the limit of the implementable range of the present invention.

Interpretation of related terms

Gas-liquid coalescence filter element: the filter is generally composed of an inner metal supporting framework and an outer fiber filtering material (including an inner coalescence layer and an outer drainage layer), when gas containing liquid drops passes through the filter, the liquid drops are captured by the fibers, small liquid drops are converged to gradually become larger liquid drops, and finally the larger liquid drops are discharged downwards along the outer surface of the filter under the action of gravity, so that the purpose of gas-liquid separation is achieved. The functions of each part are as follows:

sealing the end cover: the filter element is sealed and fixed to prevent gas leakage.

Support frame (filter frame): the rigidity and the strength of the filter element are increased, and the filter element is stable under the conditions of filter paper softening caused by high pressure and liquid wetting, gas impact and the like.

Pre-separation layer: for the early removal of solid particles and large liquid droplets entrained in the gas.

Coalescing layer (filter material): a core element of a coalescing filter element. Small droplets in the gas coalesce into large droplets on the fibers of the coalescing layer.

Draining a liquid layer: this component has a significant impact on filtration efficiency. The drainage layer facilitates the drainage of large coalesced droplets while reducing re-entrainment of the droplets.

Concentration of gas-containing liquid: the number of droplets contained in each cubic meter of gas.

Secondary entrainment: the droplets that have been captured by the coalescing filter reenter the downstream gas stream due to the action of the gas stream, causing an increase in the concentration of droplets in the downstream gas stream, resulting in a decrease in filtration efficiency, a phenomenon that is very likely to occur in micron-sized droplets.

Surface modification treatment: the surface property of the material is changed by a chemical reagent, such as changing the hydrophilic and oleophilic surface into a hydrophobic and oleophobic surface.

Example 1

The present embodiment provides a gas-liquid coalescing filter, which is structured as shown in fig. 2A and 2B, and comprises a filter frame 1 and a filter element wound on the surface of the support frame 1. The profiled fiber pre-separation layer 2 is wound on the surface of the filter framework 1, and the number of winding turns is 1 turn; the profiled fiber aggregation layer 3 is continuously wound along the profiled fiber pre-separation layer 2 for 4 circles; the profiled fiber drainage layer 4 is continuously wound along the profiled fiber aggregation layer 3, and the number of winding turns is 1 turn.

Wherein the average pore diameter of the profiled fiber pre-separating layer 2 is 10 μm, the thickness is 1.5mm, and the shape of the profiled fiber is cross-shaped. The diameter of the profiled fiber used (circumscribed circle diameter) was 15 μm. The pre-separation layer takes polyester fiber as raw material of profiled fiber. The pre-separation layer is obtained by integrally modifying the profiled fibers in modes of needling and the like.

The specific surface area (total area per unit length and unit mass) of the shaped fibers is higher than that of conventional round fibers. Great specific surface area is favorable to increasing the interception of fibre and granule, liquid drop to raise the efficiency, simultaneously, to oleophilic fibre, great specific surface area and fibre surface slot have accelerated the capillary action, and liquid can be faster by the absorption transfer, through carrying out partial modification treatment to filter media, fibre, guide liquid migration promotes liquid discharge, prevents that liquid from being absorbed the back at the inside a large amount of accumulations of filter core.

Wherein, the average aperture of the profiled fiber aggregation layer 3 is 5 μm, the thickness is 0.5mm, the shape of the adopted profiled fiber is cross-shaped, and the diameter (circumscribed circle diameter) of the profiled fiber is 4 μm. The aggregation layer takes glass fiber as raw material of the profiled fiber. The aggregation layer is the special-shaped fiber which is partially hydrophobic and oleophobic and is obtained by carrying out patterning modification on the special-shaped fiber in a series of modes such as dispersion and defibering, pulping and the like.

The specific mode is that the perimeter of the coalescence layer is 5cm along the perimeter direction of the coalescence layer and the perimeter direction of the coalescence layer, and the coalescence layer comprises 4 hydrophobic and oleophobic areas; the total length of the aggregation layer in the winding direction is 50mm, the length of the upper bottom of the upright trapezoid is 13mm, and the length of the lower bottom of the upright trapezoid is 26mm, as shown in fig. 3.

Wherein, the average pore diameter of the profiled fiber drainage layer 4 is 15 μm, the thickness is 2mm, the shape of the profiled fiber is cross, and the diameter (circumscribed circle diameter) of the profiled fiber is 15 μm. The drainage layer takes polyester fiber as raw material of profiled fiber. The drainage layer is a part of hydrophobic and oleophobic profiled fiber obtained by partially modifying the profiled fiber through needling and other modes.

Specifically, the exhaust side surface of the profiled fiber drainage layer is subjected to hydrophobic and oleophobic modification treatment, wherein the thickness of the drainage layer is 2mm in the thickness direction, and the hydrophobic and oleophobic modification thickness of the drainage layer is 2/3mm, as shown in fig. 4.

The comparison experiment is carried out to the shaped fiber gas-liquid coalescence filter of selecting for use this embodiment and traditional gas-liquid coalescence filter, and the filtering quality of this embodiment has obvious promotion than traditional gas-liquid coalescence filter.

The experimental parameters were as follows: the apparent air flow velocity on the inner surface of the filter element is 0.1m/s, aerosol is generated by adopting oil liquid (dioctyl sebacate, DEHS) specified in international test standard EN779, the particle size range of liquid drops in the aerosol at the inlet is 0.3-20 mu m, and the concentration is 480-520 mg/m-³。

The experimental results are as follows: compared with the traditional filter, the pressure drop rises more smoothly, the steady-state pressure drop is obviously reduced, the pressure drop is reduced by about 25 percent (see figure 5), more liquid is discharged from the bottom of the filter in the filtering process, the trapped liquid cannot block an airflow channel, and the service life is prolonged; meanwhile (see fig. 6), in terms of efficiency, the cumulative efficiency near the most penetrable particle size (0.1 μm) is improved from 99.68% to 99.78%, the number of penetrable particles is reduced by 30%, and meanwhile, the cumulative efficiency for large particles above 0.3 μm is 99.95% -99.99%, which shows that the secondary entrainment of liquid drops is effectively reduced.

Example 2

The profiled fibers of the pre-separation layer, the coalescing layer and the drainage layer in example 1 were shaped as trilobes, with the remaining parameters unchanged. The experiment result shows that the pressure drop reduction amplitude is 10%, and the cumulative efficiency near the most penetrable particle size in the aspect of efficiency is improved from 99.48% to 99.82%.

Example 3

In example 1, a coalescing layer having an average pore size of 3 μm was selected, with the remaining parameters being unchanged. The experimental results show that the pressure drop reduction is 15% and the cumulative efficiency in the vicinity of the most permeable particle size in terms of efficiency varies from 99.48% to 99.85%.

Comparative example 1

In example 1, the agglomerate layer was not modified, and the remaining parameters were unchanged. The experimental results showed a pressure drop reduction of 10% and a cumulative efficiency of 99.60% around the most permeable particle size in terms of efficiency.

Comparative example 2

In example 1, a drainage layer with an average pore size of 7 μm was selected, and the remaining parameters were unchanged. The experimental results showed a 5% increase in pressure drop with a cumulative efficiency of 99.58% near the most permeable particle size in terms of efficiency.

Comparative example 3

In example 1, a drainage layer with an average pore size of 25 μm was selected, and the remaining parameters were unchanged. The experiment result shows that the pressure drop is reduced by 5 percent, and the cumulative efficiency of the most penetrable grain diameter in the aspect of efficiency is 99.60 percent.

Comparative example 4

In example 1, the drainage layer was not modified, and the remaining parameters were not changed. The experimental result shows that the pressure drop is reduced by 20 percent, the cumulative efficiency near the most penetrable particle size in the aspect of efficiency is reduced to 99.50 percent, and the phenomenon of secondary entrainment is caused when large liquid drops with the diameter of more than 0.3 mu m appear.

Claims

1. A gas-liquid coalescence filter element is characterized by comprising a pre-separation layer, a coalescence layer and a liquid discharge layer which are sequentially arranged along the direction of gas flow;

the pre-separation layer is a hydrophobic and oleophobic porous structure layer formed by profiled fibers, the aperture is 8-12 μm, and the thickness of the pre-separation layer is 1-2 mm;

the aggregation layer is a porous structure layer formed by profiled fibers, the aperture is 3-8 mu m, the thickness of the aggregation layer is 1.6-2.4 mm, and the aggregation layer is divided into a hydrophobic and oleophobic area and a hydrophilic and hydrophilic area which are arranged at intervals along the circumferential direction;

the drainage layer is a porous structure layer formed by profiled fibers, the pore diameter is 10-20 microns, the thickness of the drainage layer is 2-3 mm, the drainage layer is divided into a hydrophilic and hydrophilic oil-repellent area and a hydrophobic and oil-repellent area along the thickness direction, the air inlet side is the hydrophilic and hydrophilic area, the air outlet side is the hydrophobic and oil-repellent area, and the thickness of the hydrophobic and oil-repellent area accounts for 1/3-2/3 of the total thickness of the drainage layer.

2. The gas-liquid coalescing filter element according to claim 1, wherein the shaped fibers of the pre-separation layer have a diameter of 12 μ ι η to 18 μ ι η.

3. The gas-liquid coalescing filter element according to claim 1 wherein the shaped fibers of the coalescing layer have a diameter of 3 μ ι η to 5 μ ι η.

4. The gas-liquid coalescing filter element according to claim 1, wherein the shaped fibers of the drainage layer have a diameter of 12 μ ι η to 18 μ ι η.

5. The gas-liquid coalescing filter element according to claim 1 wherein the pre-separation layer is of a single layer construction.

6. The gas-liquid coalescing filter element according to claim 1 wherein the coalescing layer is a multi-layer structure comprising a plurality of sub-coalescing layers; the aggregation layer is composed of 3-5 sub-aggregation layers.

7. The gas-liquid coalescing filter element according to claim 1 wherein the drainage layer is of a single layer construction.

8. The gas-liquid coalescing filter element according to claim 1 wherein the vertical cross-section of the hydrophobic and oleophobic area of the coalescing layer is an upright trapezoid; the plurality of hydrophobic and oleophobic areas are arranged at equal intervals.

9. The gas-liquid coalescing filter element according to claim 8, wherein the coalescing layer has a perimeter of 5 pi cm to 12 pi cm, the coalescing layer including 4 to 8 hydrophobic and oleophobic zones; wherein, the ratio of the length of the upper bottom to the length of the lower bottom of the trapezoid with the vertical section of the hydrophobic and oleophobic area is greater than or equal to 1/3 and less than 1.

10. A filter device comprising a gas-liquid coalescing filter element according to any one of claims 1 to 9.