CN219539840U - Separator for dust-containing process gas - Google Patents

Abstract

The present disclosure relates to a separator for a dusty process gas, comprising: a cylinder provided with a gas inlet and a gas outlet; and a cyclone centrifugal distributor, a packing type separation part and a vane type separation part which are arranged in the cylinder, wherein the cyclone centrifugal distributor is used for enabling the gas passing through the cyclone centrifugal distributor to form a cyclone therein, the packing type separation part comprises packing, and the vane type separation part comprises a plurality of vanes, wherein the cyclone centrifugal distributor, the packing type separation part and the vane type separation part are sequentially arranged from a gas inlet to a gas outlet, so that dust-containing process gas entering the cylinder from the gas inlet can be sequentially separated step by step through the cyclone centrifugal distributor, the packing type separation part and the vane type separation part. By means of the separator, the separation effect on the dust-containing process gas is enhanced.

Description

Separator for dust-containing process gas

Technical Field

The present disclosure relates to the field of separation purification technology, and more particularly, to separators for dusty process gases.

Background

In chemical production, process gases such as feed gases and exhaust gases often carry, in addition to gases, impurities comprising liquids, dust particles and viscous components between the liquids and the dust particles. For the dust-containing process gas, the impurities in the dust-containing process gas are easy to adhere to equipment and pipelines, and scaling or blocking and other phenomena are generated, so that the operation stability of the equipment is adversely affected.

Currently, gas-liquid separators are commonly used to remove these impurities from dusty process gases. The gas-liquid separator mainly separates and eliminates impurities by means of gravity sedimentation, centrifugal sedimentation and the like. However, the existing gas-liquid separators do not provide an ideal separation of such dusty process gases.

In addition, the dust-containing process gas can bring a large workload to the separation device of the gas-liquid separator, thereby shortening the service life of the separation device and reducing the stability of long-period operation of the equipment.

Disclosure of Invention

This section provides a general summary of the disclosure, and is not a comprehensive disclosure of its full scope or all of its features.

It is an object of the present disclosure to provide a separator capable of enhancing the separation effect on a dust-containing process gas.

It is another object of the present disclosure to provide a separator capable of reducing a separation workload to improve stability of long-period operation of a device.

To achieve one or more of the above objects, according to the present disclosure, there is provided a separator for a dust-containing process gas, comprising:

a cylinder provided with a gas inlet and a gas outlet; and

the cyclone centrifugal distributor is arranged in the cylinder body and is used for enabling the gas passing through the cyclone centrifugal distributor to form cyclone therein, the filler type separation part comprises filler, the vane type separation part comprises a plurality of vanes,

the cyclone centrifugal distributor, the packing type separation part and the vane type separation part are sequentially arranged from the gas inlet to the gas outlet, so that dust-containing process gas entering the cylinder from the gas inlet can be sequentially separated step by step through the cyclone centrifugal distributor, the packing type separation part and the vane type separation part.

In the separator for dust-laden process gas described above, the cyclone centrifugal distributor may comprise a rotating plate which is curved for swirling the gas passing through the cyclone centrifugal distributor via the rotating plate.

In the separator for dust-laden process gas described above, the cyclone centrifugal distributor may include two rows of rotating plate sets disposed opposite each other at a spacing, wherein each of the two rows of rotating plate sets includes a plurality of rotating plates.

In the separator for dust-containing process gas described above, the plurality of rotary blades of one of the two-row rotary blade groups may be staggered in the spaced longitudinal direction with respect to the plurality of rotary blades of the other-row rotary blade group.

In the separator for dust-laden process gas described above, the rotating blade may comprise a curved section and a straight section, the straight section being connected to the curved section tangentially to an end of the curved section.

In the separator for dust-laden process gas described above, the straight run section may comprise an inner straight run section and an outer straight run section, wherein the inner straight run section is connected to the inner end tangentially to the inner end of the curved section and the outer straight run section is connected to the outer end tangentially to the outer end of the curved section.

In the separator for dust-containing process gas described above, each of the plurality of blades may have a multi-fold structure including a plurality of fold portions, wherein the multi-fold structure is folded at each of the plurality of fold portions, and the multi-fold structure is provided with a bladder-shaped rotating structure at least one of the plurality of fold portions for reversing a flow direction of dust-containing process gas entering therein.

In the separator for dust-containing process gas described above, the packing-type separation portion and the vane-type separation portion may be arranged in the longitudinal direction of the cylinder, and the packing-type separation portion and the vane-type separation portion may form an integral structure in such a manner as to meet in the lateral direction of the cylinder.

In the separator for dust-laden process gas described above, the monolithic structure may be fixed to the drum at its top and bottom by means of connection plates, wherein the connection plates comprise a top connection plate fixed to the drum on the packed separation side and a bottom connection plate fixed to the drum on the vaned separation side.

In the separator for dust-containing process gas described above, it may further include a differential pressure gauge provided on the cylinder for monitoring a differential pressure between an upstream of the packed separation section and a downstream of the vane separation section, and a flushing port for flushing the packed separation section and the vane separation section when the differential pressure reaches a set value.

According to the present disclosure, by first generating a swirling flow in a dust-containing process gas using a swirling flow centrifugal distributor, it is possible to enhance a separation and removal effect on dust particles and dust-containing droplets having relatively large mass, then directly intercepting and separating the remaining dust particles and viscous components using a filler type separation part and condensing liquid-phase mist into droplets by means of a coalescing action, and finally separating the previously condensed droplets using a vane type separation part, it is possible to enhance a separation and removal effect on impurities in the form of minute mist during separation, thereby achieving a complete purification treatment of the dust-containing process gas and obtaining a clean gas that no longer entrains impurities including liquid, dust particles and viscous components. Moreover, the arrangement sequence of the cyclone centrifugal distributor, the packing type separation part and the vane type separation part realizes the step-by-step separation filtration from coarse filtration to fine filtration, reduces the work load of each stage, prolongs the service life of each stage, and improves the stability of long-period operation of the equipment.

The above features and advantages and other features and advantages of the present disclosure will be more apparent from the following detailed description of exemplary embodiments thereof in connection with the accompanying drawings.

Drawings

FIG. 1 shows a separator in schematic diagram form, according to an embodiment of the present disclosure;

FIG. 2 illustrates, in cross-section, a cyclonic centrifugal distributor according to an embodiment of the present disclosure, taken along line A-A;

FIG. 3 illustrates in a schematic diagram a rotary blade according to an embodiment of the present disclosure;

FIG. 4 shows a rotary blade in a schematic diagram according to another embodiment of the present disclosure; and

fig. 5 shows in schematic diagram a multi-fold structure according to an embodiment of the present disclosure.

Detailed Description

The disclosure is described in detail below with the aid of exemplary embodiments with reference to the accompanying drawings. It is noted that the following detailed description of the present disclosure is for purposes of illustration only and is in no way limiting of the present disclosure. Furthermore, the same or similar reference numbers are used throughout the drawings to refer to the same parts.

As mentioned before, in chemical production, the process gas, in addition to containing gas, is entrained with impurities comprising liquid, dust particles and viscous components between the liquid and the dust particles. For example, in coal chemical industry production, process gases carry along impurities such as dust, coal tar, and the like. These impurities can clog the compressor, corrode the rotor of the compressor, and prevent the system from operating stably for long periods of time. For such dust-containing process gases, the separation effect of the existing gas-liquid separators is not ideal, mainly the removal effect of dust particles and dust-containing liquid droplets is not good, and the removal effect of impurities (including mist liquid and possibly dust particles and/or viscous components) in the form of fine mist during the separation is not good.

To solve the above problems, referring to fig. 1 to 5, according to an embodiment of the present disclosure, there is provided a separator 1 for dust-containing process gas, comprising:

a cylinder 10 provided with a gas inlet 101 and a gas outlet 102; and

a cyclone centrifugal distributor 11, a packing type separation part 12 and a vane type separation part 13 provided in the cylinder 10, the cyclone centrifugal distributor 11 for forming a cyclone therein of gas passing through the cyclone centrifugal distributor 11, the packing type separation part 12 including packing, the vane type separation part 13 including a plurality of vanes 131,

wherein the cyclone centrifugal distributor 11, the packing type separation part 12 and the vane type separation part 13 are sequentially arranged from the gas inlet 101 to the gas outlet 102, so that dust-containing process gas entering the cylinder 10 from the gas inlet 101 can be separated step by step sequentially through the cyclone centrifugal distributor 11, the packing type separation part 12 and the vane type separation part 13.

The drum 10 is a vessel in which the dust-laden process gas is separated and filtered. As shown in fig. 1, the cartridge 10 may include a cartridge body 10a, an upper head 10b, and a lower head 10c, wherein the upper head 10b and the lower head 10c are disposed at upper and lower ends of the cartridge body 10a, respectively. It is contemplated that the upper head 10b and the lower head 10c may be integrally formed with the barrel body 10a, such as by welding or integral casting. However, it is also contemplated that the upper head 10b and the lower head 10c may be separate pieces and connected to the cartridge body 10a.

A gas inlet 101 may be provided on the cartridge body 10a of the cartridge 10 for allowing the dusty process gas to enter the cartridge 10 therethrough, and a gas outlet 102 may be provided on the upper head 10b of the cartridge 10 for allowing the separately filtered dusty process gas to exit the cartridge 10 therethrough. It is contemplated that the gas inlet 101 and the gas outlet 102 may also be provided at other locations of the cartridge body 10, for example, the gas outlet 102 may also be provided on the cartridge body 10a.

In the embodiment according to the present disclosure, the separator 1 further comprises a cyclone centrifugal distributor 11, a packed separation section 12 and a vane separation section 13 provided within the cylinder 10, and these three are arranged such that the dust-laden process gas entering the cylinder 10 from the gas inlet 101 can be separated stepwise sequentially through the cyclone centrifugal distributor 11, the packed separation section 12 and the vane separation section 13.

Specifically, the cyclone centrifugal distributor 11 is arranged closer to the gas inlet 101 than the packed separation section 12 and the vane separation section 13 are, so that the dust-containing process gas entering the cylinder 10 from the gas inlet 101 will first be separated and filtered by the cyclone centrifugal distributor 11. As an example, as shown in fig. 1, the cyclone centrifugal distributor 11 may be directly connected to the gas inlet 101, so that the dust-laden process gas entering from the gas inlet 101 can directly enter the cyclone centrifugal distributor 11. However, it is also conceivable that the cyclone centrifugal distributor 11 is not directly connected to the gas inlet 101, as long as the arrangement of the cyclone centrifugal distributor 11 is such that the dust-laden process gas is able to pass the cyclone centrifugal distributor 11 first with respect to the packed separation section 12 and the vane separation section 13.

The cyclonic centrifugal distributor 11 is configured such that the gas passing through the cyclonic centrifugal distributor 11 forms a swirling flow therein. Thus, when the dust-laden process gas enters the cyclone centrifugal distributor 11, the dust-laden process gas forms a cyclone in the cyclone centrifugal distributor 11, thereby changing the flow direction of the gas flow and reducing the velocity of the gas flow, in which case large droplets, dust particles and dust-laden droplets are separated from the gas flow by relatively large gravity and centrifugal force and fall to the bottom of the cylinder 10 so as to be finally discharged from, for example, a drain port N1 and a purge port N2 provided at a lower head 10c of the cylinder 10 as shown in fig. 1, thereby achieving preliminary separation of the dust-laden process gas. The formation of a swirl in the swirling centrifugal distributor 11 enables effective separation of large droplets, dust particles and dust-containing droplets having a relatively large weight. Furthermore, it will be appreciated that the gas stream leaving the cyclonic centrifugal distributor 11 may also continue to rise around the wall of the drum 10 so that the initially separated dust-laden process gas may be further separated by centrifugation. The impurities in the primarily separated dust-laden process gas are substantially in the form of fine droplets comprising a mist of liquid and typically also dust particles and/or viscous components between the liquid and the dust particles that cannot be removed in the cyclone centrifugal distributor 11.

The packed separation section 12 is arranged downstream of the cyclone centrifugal distributor 11 and upstream of the vane separation section 13, depending on the flow direction of the dust-laden process gas. The packing type separation part 11 is composed of a packing, and the material of the packing may be a wire mesh, a fiber felt, or the like, which has small pores so as to realize separation and filtration of gas. When the dust-containing process gas filtered by the cyclone centrifugal distributor 11 passes through the packing type separation part 12, the fine mist is intercepted by the packing and attached to the packing due to the smaller pores and higher density of the packing, and particularly dust particles and sticky components in the fine mist are directly intercepted by the packing to realize separation and removal. In addition, the liquid phase component in the fine mist gradually coalesces into larger droplets by the coalescing action of the filler. It will be appreciated that some of these droplets may fall to the bottom of the bowl 10 by coalescing more and more so that their own weight exceeds the combined force of the gas lifting force and the liquid surface tension. On the other hand, the remaining coalesced larger droplets leave the packed separation section 12 with the gas flow through the packed separation section 12 and enter the downstream vane separation section 13. The packing type separation section 12 aggregates mist into droplets by coalescence for removal in the downstream vane type separation section 13, so that impurities in the form of mist which are not originally easily separated and removed can be removed more easily. The impurities in the dusty process gas separated by the packed separation section 12 are now substantially in the form of droplets.

The vane separator 13 is disposed downstream of the packed separator 12. The vane type separating part 13 includes a plurality of vanes through which the air flow passes when passing through the vane type separating part 13, and the separation and filtration of the impurities in the air flow are realized by the air flow colliding with the vanes when passing through the vanes. Therefore, when the dust-containing process gas, which has been separated and filtered by the packing separation section 12, passes through the vane type separation section 13, the dust-containing process gas collides with the vanes, causing impurities in the form of liquid droplets at this time to adhere to the surfaces of the vanes and form a liquid film by the coalescing effect between the liquid droplets. These liquid films are stranded and flow down into the bottom of the cylinder 10 by the combined action of their own weight, the surface tension of the liquid and the kinetic energy of the gas flow passing through the blades, for example, in a sump provided in the bottom of the cylinder 10.

Thus, by first separating impurities having a relatively large weight such as large droplets, dust particles and dust-containing droplets by swirling the gas therein using a swirling centrifugal distributor, then directly intercepting and separating the remaining dust particles and viscous components using a filler type separation section and agglomerating the liquid phase mist into droplets by means of agglomerating action, and finally separating the previously agglomerated droplets using a vane type separation section, the removal effect of the dust particles and dust-containing droplets and the impurities in the form of minute mist during separation is enhanced, the complete purification treatment of the dust-containing process gas is achieved and a clean gas is obtained without sandwiching the above impurities. Moreover, the arrangement sequence of the cyclone centrifugal distributor, the packing type separation part and the vane type separation part realizes the step-by-step separation filtration from coarse filtration to fine filtration, reduces the work load of each stage, prolongs the service life of each stage, and improves the stability of long-period operation of the equipment.

In an embodiment according to the present disclosure, as shown in fig. 2, the cyclone centrifugal distributor 11 may include a rotating sheet 111, the rotating sheet 111 being curved for swirling the gas passing through the cyclone centrifugal distributor 11 via the rotating sheet 111.

The curved shape of the rotary blade 111 imparts centrifugal force to the dusty process gas as it passes through the rotary blade 111, thereby changing the gas flow direction and gas flow velocity of the dusty process gas, thereby creating a swirling flow. It will be appreciated that other ways and structures of generating a swirling flow are also contemplated, such as other shapes and types of components having curved contours on the surface.

In an embodiment of the present disclosure, referring to fig. 2, the rotational flow centrifugal distributor 11 may include two rows of rotating blade groups 11a, 11b arranged opposite to each other at a space, wherein each of the two rows of rotating blade groups includes a plurality of rotating blades 111.

By providing two rows of rotating blade sets 11a, 11b arranged opposite to each other with a space, the dust-laden process gas entering the cyclone centrifugal distributor 11 can pass through the two rows of rotating blade sets 11a, 11b at the same time by passing through the space, whereby the dust-laden process gas can flow to the two rows of rotating blade sets respectively and form a cyclone by the plurality of rotating blades 111 of each row, thereby realizing a double-rotation centrifugal flow of the dust-laden process gas, which increases the brownian motion collision opportunity of the gas as a whole, and further enhances the separation effect.

It is contemplated that the spacing between the two rows of rotating blades may be uniform throughout from the inlet end to the tail end of the air flow (as shown in fig. 2), or may taper from the inlet end to the tail end of the air flow, or may take other variations depending on the desired flow rate and velocity of the split air flow.

Furthermore, it is also conceivable that the plurality of rotary blades in each column of rotary blade groups are equally spaced in the longitudinal direction of the column and the orientation of the rotary blades is also the same, or that the spacing and orientation can be adjusted to obtain a desired swirl and reduce the possibility of clogging. For example, the spacing between the rotary pieces can be set large so that scaling and clogging are less likely, whereby continuous operation can be achieved without replacement of spare parts, thereby enabling cost reduction.

It should be noted that the fact that the two rows of the rotary blade groups each include a plurality of rotary blades means that each of the two rows of the rotary blade groups includes a plurality of rotary blades, and the number of rotary blades of each row of the rotary blade groups may be the same or different. That is, the number of rotary pieces of one of the two columns of rotary piece groups may be the same as or different from the number of rotary pieces of the other column.

In the embodiment according to the present disclosure, as shown in fig. 2, the plurality of rotary pieces 111 of one column of rotary piece groups 11a or 11b of the two columns of rotary piece groups 11a, 11b are staggered with respect to the plurality of rotary pieces 111 of the other column of rotary piece groups 11b or 11a in the longitudinal direction of the above-described interval.

The dusty process gas contains not only gas but also liquid, in particular solid components such as dust particles, and therefore, when the dusty process gas enters the cyclone centrifugal distributor 11, the distribution of impurities in the gas stream may not be uniform, not only in the transverse direction of the separation, but also in the longitudinal direction of the separation. By this staggered arrangement of the rotating blades, the probability of capturing impurities in the air flow can be increased, especially in case of uneven distribution of impurities in the longitudinal direction of the gap.

In an embodiment according to the present disclosure, as shown in fig. 3 and 4, the rotary blade 111 may include a curved section 111a and a straight section 111b, the straight section 111b being connected to the curved section 111a in a tangential manner to an end of the curved section 111a.

Similar to the previous description of the effect of the curved shape, the curved section of the rotating blade imparts centrifugal force to the dusty process gas as it passes through the curved section, thereby changing the gas flow direction and gas flow velocity of the dusty process gas, thereby creating a swirling flow. In addition, the straight section tangential to the end of the curved section allows the gas to enter and leave the curved section smoothly, thereby maintaining the stability of the cyclone centrifugal distributor and the whole separator and reducing the damage of the cyclone centrifugal distributor and the whole separator due to the turbulence of the gas flow.

As an example, as shown in fig. 3, straight run section 111b may be located outside of curved section 111a, i.e., on the side of curved section 111a that is located near the outside of the cyclonic centrifugal distributor, to enable the swirling gas to smoothly exit curved section 111a and exit cyclonic centrifugal distributor 11, thereby maintaining the stability of the cyclonic centrifugal distributor and the overall separator, reducing the damage to the cyclonic centrifugal distributor and the overall separator from airflow turbulence.

It is contemplated that straight segment 111b may include an inner straight segment 111b 'and an outer straight segment 111b″ as shown in fig. 4, wherein inner straight segment 111b' is connected to the inner end tangentially to the inner end of curved segment 111a and outer straight segment 111b″ is connected to the outer end tangentially to the outer end of curved segment 111a.

It is clearly understood that the inner end of the curved section 111a is the end of the curved section 111a that is adjacent to the inner side of the centrifugal cyclone distributor, and the outer end of the curved section 111a is the end of the curved section 111a that is adjacent to the outer side of the centrifugal cyclone distributor. By providing the inner straight section and the outer straight section which are respectively tangentially connected to both ends of the curved section, it is possible to smoothly enter the curved section 111a and to smoothly leave the curved section 111a and thus the cyclone centrifugal distributor 11 with the gas after swirling via the curved section 111a, respectively, whereby the stability of the cyclone centrifugal distributor and the whole separator can be maintained during the whole process of the dust-laden process gas passing through the cyclone sheet, thereby reducing the damage of the cyclone centrifugal distributor and the whole separator due to the turbulence of the gas flow more effectively.

It is contemplated that the inner straight section 111b 'may be angled with respect to the above-described spaced centerlines as shown in fig. 2 and 4 so that the spaced airflows entering the cyclonic centrifugal distributor 11 can smoothly enter the inner straight section 111b', thereby reducing the damage to the cyclonic centrifugal distributor and the overall separator from airflow turbulence.

It is also contemplated that the curved section 111a may have multiple curved sections to enable multiple changes in the direction and speed of the airflow through the curved section 111a, thereby enhancing the cyclonic centrifugal effect. Alternatively, the curved section 111a may have an S shape having two curved sections.

In the embodiment of the present disclosure, as shown in fig. 2, the cyclone centrifugal distributor 11 is further provided with a baffle 112, the baffle 112 including an upper baffle and a lower baffle respectively located at the upper side and the lower side of the rotating sheet 111. Alternatively, the rotation piece 111 may be fixedly connected to the upper and lower baffles.

By providing the upper and lower baffles, the gas flow entering the cyclone centrifugal distributor 11 can be prevented from flowing upward and downward, so that the dust-containing process gas entering the cyclone centrifugal distributor 11 can be substantially completely split through the rotating plate, thereby enhancing the separation efficiency of the cyclone centrifugal distributor 11 for the gas entering therein.

In embodiments of the present disclosure, the packing of the packed separation section 12 may be stacked from multiple layers of coalescing wire mesh.

As the dusty process gas passes through the coalescing screen, the mist collides with the filaments of the screen and adheres to the surfaces of the filaments. As the air flow continues through the coalescing screen, mist on the surface of the filaments continues to spread and settle, so that larger droplets are formed which will flow along the filaments and become increasingly more wettable through the screen, the surface tension of the liquid and the capillary action of the filaments.

It is contemplated that the coalescing screen may be a discounted coalescing screen to facilitate the formation of larger droplets by more filament intersections. It is also contemplated that the coalescing screen may be other types of coalescing screens, such as, for example, a wave-type coalescing screen.

In the embodiment of the present disclosure, each of the plurality of blades 131 of the blade-type separating part 13 has a multi-fold structure. Only two blades are shown in fig. 5, and only 2 folds are shown per blade. It will be appreciated that the number of blades and folds is not limited to 2.

It is clearly understood that a multi-fold structure refers to a structure in which the direction of extension is changed multiple times. By providing the vanes with a multi-fold structure, when the air flow passes between the vanes, the air flow collides with the vanes due to the fold and thereby removes the liquid droplets, and the liquid droplets not removed undergo the same collision action at the next fold, thereby repeatedly acting, and the separation efficiency of the vane type separation portion 13 is improved.

It is contemplated that the plurality of blades of the blade-type separating portion 13 may also take other forms to obtain a better impact separation effect. For example, adjacent vanes are disposed at an angle such that the air flow passing therebetween collides with the vanes, thereby effecting gas-liquid separation.

In an embodiment of the present disclosure, as shown in fig. 5, the multi-fold structure may include a plurality of fold portions 131a, wherein the multi-fold structure folds at each of the plurality of fold portions 131a, and the multi-fold structure is provided with a bladder-shaped rotating structure 141 at least one of the plurality of fold portions 131a, the bladder-shaped rotating structure 141 for reversing a flow direction of dust-containing process gas entering therein.

By providing a capsule-like rotating structure where the folding of the multi-fold structure occurs, gas can further enter the capsule-like rotating structure and collide therein and the direction of flow is changed, whereby capturing droplets in the gas can be facilitated. In addition, by arranging the capsule rotating structures at the plurality of folding positions, the gas can continuously enter the next capsule rotating structure at the downstream under the driving of the gas flow after the gas flows reversely in the capsule rotating structure at the upstream and leaves the capsule rotating structure, so that the repeated operation can prevent the trapped liquid drops from being carried away by the gas flowing at high speed to form secondary entrainment, thereby improving the separation efficiency of the vane type separation part 13.

In the embodiment of the present disclosure, as shown in fig. 1, the packing type separation portion 12 and the vane type separation portion 13 are arranged in the longitudinal direction of the cylinder 10.

That is, the packing separation section 12 and the vane separation section 13 are arranged vertically in the cylinder 10, whereby the dust-containing process gas can be filtered through the packing separation section 12 and the vane separation section 13 in the lateral direction of the cylinder 10. In general, the cyclone centrifugal distributor 11 through which the gas first passes is disposed at the middle or lower portion of the cylinder 10, and when the packing type separation portion 12 and the vane type separation portion 13 are disposed in a vertical manner, it is possible to allow a large settling space to be left between both of the packing type separation portion 12 and the vane type separation portion 13 and the cyclone centrifugal distributor 11, facilitating gas-liquid separation. In addition, the vertical arrangement causes the impurities separated by the packing type separation portion 12 and the vane type separation portion 13 to be directly lowered to the bottom of the cylinder 10, and the problem that the impurities separated by the vane type separation portion 13 first fall into the packing type separation portion 12 to adversely affect the filtering effect of the packing type separation portion 12 does not occur. It is conceivable that the packing separator 12 and the vane separator 13 may also be arranged in the lateral direction of the cylinder 10, i.e. in a horizontal arrangement.

It is contemplated that the packing type separating portion 12 and the vane type separating portion 13 may be provided as a unitary structure in such a manner as to meet in the lateral direction of the cylinder 10, as shown in fig. 1.

The packing separation 12 and the vane separation 13 may be arranged next to each other in the transverse direction, that is to say substantially without any gaps between them. In this way, droplets agglomerated by mist in the packed separation section 12 by coalescence can be directly carried into the vane-type separation section 13 by means of the gas flow to be separated, without going a short distance to the vane-type separation section 13, so that the droplets may be redispersed and may become less likely to be separated by the vane-type separation section 13.

In the embodiment of the present disclosure, the integral structure is fixed to the cylinder 10 at the top and bottom thereof by the connection plates 14, wherein the connection plates 14 include a top connection plate 14a fixed to the cylinder 10 on the filler-separating portion 12 side and a bottom connection plate 14b fixed to the cylinder 10 on the vane-type separating portion 13 side.

As shown in fig. 1, the top connection plate 14a, the overall structure and the bottom connection plate 14b together form a zigzag shape such that the dust-containing process gas filtered through the cyclone centrifugal distributor 11 can pass through the packed-type separation section 12 and then the vane-type separation section 13 only. Further, with this configuration, the packing type separation portion 12 and the vane type separation portion 13 can be easily cleaned from the packing type separation portion 12 side and the vane type separation portion 13 side, respectively.

It is conceivable that the vane-type separation portion 13 may be provided thereunder with a drain pipe 132 for introducing the liquid separated by filtration thereof to the bottom of the separator 1.

As mentioned before, the dust-laden process gas separated and filtered via the cyclone centrifugal distributor 11 and the packed separation section 12 mainly entrains impurities in the form of droplets. Therefore, when separated by the vane separator 13, the droplets are coalesced into strands and form a large amount of liquid. By providing a drain below the vane separator 13, a large amount of liquid can be directed to the bottom of the cylinder 10 along a desired path, avoiding the adverse effect that a large area drop of liquid may cause separation of the rising gas below.

In the embodiment of the present disclosure, the separator 1 may further include a differential pressure gauge provided on the cylinder 10 for monitoring a differential pressure between an upstream of the packing type separation portion 12 and a downstream of the vane type separation portion 13, and a flushing port N3 for flushing the packing type separation portion 12 and the vane type separation portion 13 when the differential pressure reaches a set value.

The differential pressure gauge can reflect the cleaning condition of the packing type separating portion 12 and the vane type separating portion 13 as a whole. When, for example, fouling or clogging occurs in the packed separation section 12 and/or the vane separation section 13, the pressure difference between the upstream of the packed separation section 12 and the downstream of the vane separation section 13 changes. By providing a differential pressure gauge and a flushing port coupled thereto, automatic cleaning of the packing type and vane type separating portions can be achieved, whereby the stability of the packing type and vane type separating portions and thus the long-term operation of the entire apparatus can be improved.

Specifically, the set value may be, for example, a value representing a pressure difference between an upstream of the packing type separation portion 12 and a downstream of the vane type separation portion 13, which correspond to the packing type separation portion 12 and the vane type separation portion 13 capable of operating normally. Further, as shown in fig. 1, the differential pressure gauge may include two pressure gauges P1, P2 provided upstream of the packing type separation portion 12 and downstream of the vane type separation portion 13, respectively, and the flushing port N3 may be provided on the side of the cylinder 10 opposite to the packing type separation portion 12, the side of the cylinder 10 opposite to the vane type separation portion 13, or both sides of the cylinder 10. In addition, the flushing port may clean the packed separation section 12 and the vane separation section 13 by supplying water, steam, nitrogen, or an inert gas.

The foregoing is merely specific embodiments of the disclosure, but the protection scope of the disclosure is not limited thereto, and any changes or substitutions that can be easily conceived by those skilled in the art within the technical scope of the disclosure are intended to be covered by the protection scope of the disclosure. Therefore, the protection scope of the present disclosure shall be subject to the protection scope of the claims.

Claims (10)

1. A separator for a dusty process gas, comprising:

a cylinder provided with a gas inlet and a gas outlet; and

a cyclone centrifugal distributor arranged in the cylinder body, a filler type separation part and a vane type separation part, wherein the cyclone centrifugal distributor is used for enabling the gas passing through the cyclone centrifugal distributor to form a cyclone therein, the filler type separation part comprises filler, the vane type separation part comprises a plurality of vanes,

the cyclone centrifugal distributor, the packing type separation part and the vane type separation part are sequentially arranged from the gas inlet to the gas outlet, so that dust-containing process gas entering the cylinder from the gas inlet can be sequentially separated step by step through the cyclone centrifugal distributor, the packing type separation part and the vane type separation part.

2. The separator for a dusty process gas of claim 1 wherein the cyclonic centrifugal distributor includes a rotating sheet that is curved for imparting the cyclonic flow to the gas passing through the cyclonic centrifugal distributor via the rotating sheet.

3. The separator for a dusty process gas of claim 2 wherein the cyclone centrifugal distributor includes two rows of rotating plate sets arranged opposite each other at a spacing, wherein each of the two rows of rotating plate sets includes a plurality of the rotating plates.

4. A separator for a dust-laden process gas as claimed in claim 3, wherein the plurality of said rotary blades of one of said two columns of rotary blade sets are staggered in the longitudinal direction of the space relative to the plurality of said rotary blades of the other column of rotary blade sets.

5. The separator for a dust-laden process gas of any one of claims 2 to 4, wherein the rotating sheet comprises a curved section and a straight section, the straight section being connected to the curved section tangentially to an end of the curved section.

6. The separator for a dusty process gas of claim 5 wherein the straight run section includes an inner straight run section and an outer straight run section, wherein the inner straight run section is connected to the inner end tangentially to the inner end of the curved section and the outer straight run section is connected to the outer end tangentially to the outer end of the curved section.

7. The separator for a dust-laden process gas of any one of claims 1 to 4, wherein each of the plurality of blades has a multi-fold structure comprising a plurality of folds, wherein the multi-fold structure folds at each of the plurality of folds, and wherein the multi-fold structure is provided with a bladder-like rotating structure at least one of the plurality of folds for reversing the flow direction of the dust-laden process gas entering therein.

8. The separator for dust-containing process gas according to any one of claims 1 to 4, wherein the packed separation portion and the vane separation portion are arranged in the longitudinal direction of the cylinder, and the packed separation portion and the vane separation portion form an integral structure in such a manner as to meet in the lateral direction of the cylinder.

9. The separator for dusty process gas of claim 8 wherein the monolithic structure is secured to the cylinder at its top and bottom by webs, wherein the webs include a top web secured to the cylinder on the packed separation side and a bottom web secured to the cylinder on the vaned separation side.

10. The separator for a dusty process gas of any of claims 1-4, further comprising a differential pressure gauge provided on the cylinder for monitoring a pressure differential between an upstream of the packed separation section and a downstream of the vane separation section, and a flushing port for flushing the packed separation section and the vane separation section when the pressure differential reaches a set point.