CN218951340U

CN218951340U - Vertical low-temperature separator

Info

Publication number: CN218951340U
Application number: CN202320021593.4U
Authority: CN
Inventors: 刘丽; 请求不公布姓名
Original assignee: Sichuan Jujie Innovative Materials Technology Co ltd
Current assignee: Sichuan Jujie Innovative Materials Technology Co ltd
Priority date: 2023-01-05
Filing date: 2023-01-05
Publication date: 2023-05-02
Anticipated expiration: 2033-01-05

Abstract

The utility model relates to a vertical low-temperature separator, which comprises a tank body, wherein the tank body is provided with an inlet, a first outlet and a second outlet; the feeding distributor is communicated with the inlet, a liquid storage cavity is formed between the feeding distributor and the bottom of the tank body, and the first outlet is communicated with the liquid storage cavity; the gas-liquid separation device is positioned above the feeding distributor, and a first cavity is formed between the feeding distributor and the gas-liquid separation device; the cyclone device is positioned above the gas-liquid separation device, a second cavity is formed between the gas-liquid separation device and the cyclone device, the mist catcher is positioned above the cyclone device, a third cavity is formed between the cyclone device and the mist catcher, an air storage cavity is formed between the mist catcher and the top of the tank body, and the second outlet is communicated with the air storage cavity; the cyclone device comprises a plurality of cyclone tubes, the lower ends of the cyclone tubes are communicated with the second cavity, and the upper ends of the cyclone tubes are communicated with the third cavity; the separator not only can effectively treat natural gas with heavy hydrocarbon and wax, but also is not easy to cause blockage.

Description

Vertical low-temperature separator

Technical Field

The utility model relates to the technical field of natural gas treatment equipment, in particular to a vertical low-temperature separator.

Background

Natural gas is called green energy, which is clean, efficient and high-quality fuel, and most countries in the world use natural gas as the preferred fuel and increase the proportion of energy supply in each country. Natural gas is playing an increasingly important role and has become a world three-major energy prop in parallel with petroleum and coal. In the wellhead natural gas project, natural gas dehydration and hydrocarbon removal skid block devices are built and mainly used for removing easily-condensed liquid carried by raw gas, including water and multi-carbon hydrocarbon; the low-temperature separator is core equipment in a natural gas dehydration and dealkylation skid device, is mainly used for removing hydrocarbon, water drop liquid foam and the like in natural gas, and is commonly used at present: screen separators, vane separators, cyclone separators.

The prior art discloses cryogenic separators, such as a multi-separation natural gas cryogenic separator disclosed in chinese patent CN215288669U, a packing type natural gas cryogenic separator disclosed in chinese patent CN208878195U, and a cryogenic separator with a small amount of light hydrocarbon in treated natural gas disclosed in chinese patent CN217535932U, which are all cryogenic separators for treating natural gas, but because of the structure and internal layout, the existing cryogenic separators generally only can treat some conventional natural gas without heavy hydrocarbon and wax, and for natural gas with heavy hydrocarbon and wax, the existing cryogenic separators generally have problems that natural gas cannot be separated effectively and blockage is very easy to occur, so that development of a cryogenic separator suitable for treating natural gas with heavy hydrocarbon and wax is highly desired.

Disclosure of Invention

The utility model provides a vertical low-temperature separator, which aims to solve the problem that the existing low-temperature separator is not suitable for treating natural gas with heavy hydrocarbon and wax, has reasonable internal layout, can effectively treat the natural gas with heavy hydrocarbon and wax, is not easy to block, and has the main conception that:

a vertical low-temperature separator comprises a tank body which is a vertical tank body and is provided with an inlet, a first outlet and a second outlet,

the feeding distributor is fixed on the tank body and communicated with the inlet, a liquid storage cavity is formed between the feeding distributor and the bottom of the tank body, the first outlet is communicated with the liquid storage cavity,

the gas-liquid separation device is fixed on the tank body and is positioned above the feeding distributor, a first cavity is formed between the feeding distributor and the gas-liquid separation device,

the cyclone device is fixed on the tank body and is positioned above the gas-liquid separation device, a second cavity is formed between the gas-liquid separation device and the cyclone device, and

the mist catcher is fixed on the tank body and is positioned above the rotational flow device, a third cavity is formed between the rotational flow device and the mist catcher, a gas storage cavity is formed between the mist catcher and the top of the tank body, the second outlet is communicated with the gas storage cavity,

the cyclone device comprises a plurality of cyclone pipes, the lower ends of the cyclone pipes are communicated with the second cavity, and the upper ends of the cyclone pipes are communicated with the third cavity. In the scheme, the feeding distributor is configured so as to perform preliminary gas-liquid separation on the mixed gas and liquid entering the tank body, and meanwhile, more uniform gas phase distribution can be realized, and the free liquid phase enters a liquid storage cavity below through the feeding distributor; by arranging the gas-liquid separation device above the feeding distributor, heavy hydrocarbon, wax and liquid (water and dehydrating agent) in the mixed gas-liquid can be effectively intercepted and separated, secondary separation is realized, and particularly, heavy hydrocarbon and wax can be effectively removed, and a cyclone tube in a subsequent cyclone device is prevented from being blocked; the cyclone device is arranged above the gas-liquid separation device so as to effectively remove liquid drops carried in the gas, including light hydrocarbons, residual heavy hydrocarbons and wax, and realize three-time separation; and through the configuration of the top at cyclone, can further intercept the liquid drop that entrained in the gas, including light hydrocarbon etc. the clean gas that does not carry liquid drop is discharged from the second export of mist catcher top, accomplishes the purification to taking natural gas of heavy hydrocarbon and wax, for current cryogenic separator, this cryogenic separator not only is applicable to the processing and takes natural gas of heavy hydrocarbon and wax, and inside rationally distributed is difficult to appear the problem of jam moreover.

Preferably, the gas-liquid separation device adopts a vane type gas-liquid separation device. Is beneficial to better intercept and separate heavy hydrocarbon, wax, liquid (water and dehydrating agent) and the like in the natural gas.

In order to solve the problem of improving separation effect and efficiency, further, the cyclone device is matched with the inner wall of the tank body and separates the second cavity and the third cavity in the tank body, the cyclone device is further provided with a first liquid discharging hole which is communicated with the third cavity, the upper end of the cyclone tube is higher than the first liquid discharging hole, the upper end of the first downcomer is communicated with the first liquid discharging hole, and the lower end of the first downcomer at least extends to the lower part of the gas-liquid separation device and is sealed in a liquid way. In the scheme, the second cavity and the third cavity are separated by the cyclone device, so that liquid drops separated from the upper mist catcher can be gathered in the third cavity above the cyclone device; by configuring the first drain hole to be in communication with the third chamber and lower than the upper end of the cyclone tube, liquid collected in the third chamber can flow downward through the first drain hole without overflowing into the cyclone tube; the first downcomer is communicated with the first liquid discharge hole, and the lower end of the first downcomer extends at least to the lower part of the gas-liquid separation device, so that the liquid collected in the third cavity is independently downwards drained by the first downcomer, the separated liquid can be effectively prevented from contacting with the ascending airflow, and the separation effect and efficiency are improved.

In order to solve the problem of improving the separation effect and efficiency, the device further comprises a second downcomer, wherein the upper end of the second downcomer is communicated with the cyclone device, and the lower end of the second downcomer at least extends to the lower part of the gas-liquid separation device and is in liquid seal. The lower end of the second downcomer is arranged to extend to at least the lower part of the gas-liquid separation device, so that the liquid separated from the cyclone device is independently downwards guided by the second downcomer, the separated liquid can be effectively prevented from contacting with the ascending airflow again, the separation effect and efficiency are improved, and in addition, the gas can be effectively prevented from ascending along the downcomer by liquid sealing the lower end of the second downcomer, so that the gas can only ascend through the cyclone tube of the cyclone device after passing through the gas-liquid separation device.

Further, the cyclone device also comprises a separation plate, a cylinder body and a bottom plate, wherein the separation plate is horizontally fixed in the tank body and separates the second cavity and the third cavity in the tank body,

the two ends of the cylinder body are respectively connected with the partition plate and the bottom plate, the partition plate, the cylinder body and the bottom plate jointly enclose a closed liquid discharge cavity, the bottom plate is provided with a plurality of first through holes for adapting the cyclone tubes, the partition plate is provided with a plurality of second through holes for adapting the cyclone tubes, the lower ends of the cyclone tubes are respectively communicated with the second cavity through the first through holes, the upper ends of the cyclone tubes are respectively extended into the third cavity through the second through holes,

the first drain hole is formed in the partition plate,

the bottom plate is also provided with a second liquid discharge hole which is communicated with the liquid discharge cavity, and the upper end of the second downcomer is fixed on the bottom plate and communicated with the second liquid discharge hole. By adopting the cyclone device, liquid drops carried in the gas can be further separated, which is favorable for further separating residual heavy hydrocarbon, wax and liquid (water and dehydrating agent), thereby realizing better separation effect.

Preferably, the cyclone tube is vertically arranged. Is beneficial to reducing the pressure loss.

In order to facilitate the installation of the cyclone device, preferably, a support is installed on the inner wall of the tank body, the partition plate is fixed on the support, and the first liquid discharge hole is formed on the outer side of the cylinder body. The first downcomer can extend downwards from the outer side of the cylinder without passing through the cylinder, which is beneficial to simplifying the structure, facilitating assembly and reducing cost.

Preferably, the mist catcher is a wire mesh filler mist catcher.

In order to solve the problem of achieving a better mist capturing effect, the mist capturing device further comprises a second filler part and a first filler part, wherein the second filler part is configured to be matched with the inner diameter of the tank body so as to eliminate a gap between the second filler part and the inner wall of the tank body,

the first filler portion is smaller than the inner diameter of the tank body, the first filler portion is arranged below the second filler portion, and a gap is reserved between the first filler portion and the inner wall of the tank body. The second filler part and the first filler part can form a convex-shaped structure, so that the thickness of the filler in the mist catcher can be increased, liquid drops carried in gas can be better intercepted, the intercepted liquid drops are more favorably separated from the filler, a better mist catching effect can be realized, and the method is particularly favorable for intercepting residual heavy hydrocarbon, wax and liquid (water and dehydrating agent) in the gas.

In order to facilitate assembly, further, the mist catcher also comprises a supporting frame, the supporting frame comprises an annular bottom plate, the center of the annular bottom plate is connected with a first grating plate, the inner ring of the annular bottom plate is connected with a supporting cylinder,

the supporting frame also comprises a second grating plate arranged above the annular bottom plate, a first filling cavity is formed between the supporting cylinder and the first grating plate, the first filling part is arranged in the first filling cavity, a second filling cavity is formed between the supporting cylinder and the second grating plate, the second filling part is arranged in the second filling cavity,

the annular bottom plate is provided with a third liquid drain hole. By adopting the structure, the first packing part and the second packing part are convenient to install and replace, liquid drops intercepted by the second packing part fall down more easily through the space between the supporting cylinder and the side wall of the tank body and flow downwards through the third liquid discharging hole, separation with ascending air flow is realized, and better separation effect is realized.

In order to solve the problem of improving the separation effect and efficiency, the device further comprises a third downcomer, wherein the upper end of the third downcomer is connected with the annular bottom plate and communicated with the third liquid discharge hole, and the lower end of the third downcomer is in liquid seal in the third cavity. By arranging the third downcomer and sealing the lower end of the third downcomer in the third cavity, droplets separated from the mist catcher are independently downwards guided by the third downcomer, and the separated droplets can be effectively prevented from contacting with ascending air flow, thereby being beneficial to improving separation effect and efficiency.

In order to solve the problem of preventing the gas-liquid separation device from being blocked, further, a plurality of flushing nozzles are further arranged in the second cavity, and the flushing nozzles face the gas-liquid separation device and are used for flushing the gas-liquid separation device. Through configuration washing nozzle, can wash gas-liquid separation device from gas-liquid separation device's top, can wash away heavy hydrocarbon and wax etc. that are attached to gas-liquid separation device to can effectively prevent gas-liquid separation device and block up.

Compared with the prior art, the vertical low-temperature separator provided by the utility model has reasonable internal layout, can effectively treat natural gas with heavy hydrocarbon and wax, and is not easy to cause blockage.

Drawings

In order to more clearly illustrate the technical solutions of the embodiments of the present utility model, the drawings that are needed in the embodiments will be briefly described below, it being understood that the following drawings only illustrate some embodiments of the present utility model and therefore should not be considered as limiting the scope, and other related drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.

Fig. 1 is a schematic structural diagram of a vertical cryogenic separator according to embodiment 1 of the present utility model, and dotted lines with arrows in the drawing indicate air flow directions.

Fig. 2 is a partial cross-sectional view of a cyclone device in a vertical cryogenic separator according to embodiment 1 of the present utility model.

Fig. 3 is a cross-sectional view at A-A in fig. 1.

Fig. 4 is a cross-sectional view at B-B in fig. 1.

Fig. 5 is a schematic structural diagram of a vertical cryogenic separator according to embodiment 2 of the present utility model.

Fig. 6 is a schematic structural diagram of a vertical cryogenic separator according to embodiment 3 of the present utility model, and dotted lines with arrows in the drawing indicate air flow directions.

Fig. 7 is a partial sectional view of a mist catcher in a vertical cryogenic separator according to embodiment 3 of the present utility model.

Description of the drawings

Tank 100, inlet 101, first outlet 102, second outlet 103, liquid storage chamber 104, first chamber 105, second chamber 106, third chamber 107, gas storage chamber 108, support 109, flushing nozzle 110, liquid seal 111

Feed distributor 200

Gas-liquid separation device 300 and blade 301

Swirl device 400, swirl tube 401, bottom plate 402, first through hole 403, cylinder 404, partition plate 405, second through hole 406, liquid discharge chamber 407, first liquid discharge hole 408, first downcomer 409, second liquid discharge hole 410, and second downcomer 411

Mist catcher 500, first packing portion 501, second packing portion 502, annular bottom plate 503, first grid plate 504, support cylinder 505, second grid plate 506, support frame 507, third drain hole 508, third downcomer 509

Bolt pair 600.

Detailed Description

The following description of the embodiments of the present utility model will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present utility model, but not all embodiments. The components of the embodiments of the present utility model generally described and illustrated in the figures herein may be arranged and designed in a wide variety of different configurations. Thus, the following detailed description of the embodiments of the utility model, as presented in the figures, is not intended to limit the scope of the utility model, as claimed, but is merely representative of selected embodiments of the utility model. All other embodiments, which can be made by a person skilled in the art without making any inventive effort, are intended to be within the scope of the present utility model.

Example 1

In this embodiment, as shown in fig. 1, a vertical low-temperature separator is provided, and the tank 100 is a vertical tank 100, that is, the length of the tank 100 is substantially consistent with the vertical direction; the tank 100 is configured with an inlet 101, a first outlet 102 and a second outlet 103, wherein the inlet 101 is mainly used for inputting natural gas to be treated, and the inlet 101 can be preferentially configured on the side wall of the tank 100, as shown in fig. 1; the first outlet 102 is mainly used for draining liquid, and may be preferably configured at the bottom of the tank 100, or may be configured at a side wall of the tank 100, as shown in fig. 1; the second outlet 103 is mainly used for discharging purified gas (i.e., natural gas), and may be preferably formed at the top of the tank 100, as shown in fig. 1, or may be formed at a side wall of the tank 100.

A closed cavity is formed in the tank 100 for processing mixed gas and liquid, such as processing natural gas with heavy hydrocarbons and waxes, and in practice, a feed distributor 200, a gas-liquid separation device 300, a cyclone device 400, and a mist catcher 500 are also provided in the tank 100, wherein,

as shown in fig. 1, the feed distributor 200 may be fixed in the tank 100 by the support 109 and is in communication with the inlet 101, so that the natural gas input from the inlet 101 passes through the feed distributor 200, and the feed distributor 200 is utilized to perform gas-liquid preliminary separation on the incoming mixed gas-liquid, and meanwhile, more uniform gas phase distribution may be realized, so as to facilitate subsequent continuous processing. As shown in fig. 1, in this embodiment, a space is provided between the feed distributor 200 and the bottom of the tank 100, so that a liquid storage chamber 104 for storing a liquid phase can be formed between the feed distributor 200 and the bottom of the tank 100, and a free liquid phase can enter the liquid storage chamber 104 below through the feed distributor 200; the first outlet 102 communicates with the liquid storage chamber 104, as shown in fig. 1, to discharge the separated liquid phase (including heavy hydrocarbons, waxes, liquids (water and dewatering agent), etc.). In practice, the feed distributor 200 may be of conventional construction, for example, a gas flow distributor as disclosed in chinese patent CN 214715464U.

As shown in fig. 1 and 3, the gas-liquid separation device 300 may be fixed to the tank 100 and located at a position above the feed distributor 200 by a certain distance, so that a first cavity 105 may be formed between the feed distributor 200 and the gas-liquid separation device 300, so that the gas flow leaving the feed distributor 200 may rise from the first cavity 105 and all enter the gas-liquid separation device 300, and the gas-liquid separation device 300 may effectively intercept and separate heavy hydrocarbons, wax and liquid (water and dehydrating agent) in the mixed gas-liquid, so as to realize secondary separation, and particularly may effectively remove heavy hydrocarbons and wax, and prevent the cyclone 401 in the subsequent cyclone device 400 from being blocked. In implementation, the gas-liquid separation device 300 can preferably adopt the blade 301 type gas-liquid separation device 300, which is beneficial to better intercept and separate heavy hydrocarbon, wax, liquid (water and dehydrating agent) and the like in natural gas. In practice, the vane 301 type gas-liquid separation device 300 includes a supporting frame and a plurality of vanes 301 disposed on the supporting frame, where the supporting frame can be fixed on an inner wall of the tank body 100, as shown in fig. 1 and 3, each vane 301 can be disposed obliquely, and each vane 301 is parallel to each other, a gap is formed between two adjacent vanes 301, and the gap forms a flow channel for passing gas, in an actual operation process, mixed gas and liquid enters the flow channel from below the gas-liquid separation device 300 and flows in a laminar flow state in the flow channel, heavy hydrocarbons and wax in the mixed gas and liquid (natural gas) are continuously collected on the back (i.e., the lower surface) of the upper vane 301, and are adhered to the vanes 301, and gradually collected into large droplets, so that the heavy hydrocarbons and wax in the mixed gas can be removed from the liquid storage cavity 104 at the bottom of the tank body 100 (a small amount of heavy hydrocarbons and wax still adhered to the vanes 301) under the action of gravity, thereby avoiding blocking the subsequent cyclone 401, and increasing the service time of the cyclone 401 and increasing the repair time. In this embodiment, by arranging the vane 301 type gas-liquid separation device 300 below the cyclone device 400, when the gas flow rate is high in the actual use process, the vane 301 type gas-liquid separation device 300 can effectively increase the diameter of the liquid drops to be separated, and plays a role of coalescing the liquid drops, so that the separation efficiency of the subsequent cyclone tube 401 can be significantly increased; during operation, large droplets are separated from the gas stream during successive impingement on the surface of the blade 301. When the gas flow rate is low, the vane 301 type gas-liquid separation device 300 mainly plays a role of separating liquid, thereby increasing the operation flexibility of the whole cryogenic separator.

As shown in fig. 1 to 4, the cyclone device 400 is fixed to the tank 100 and is located at a position above the gas-liquid separation device 300 by a certain distance, so that a second cavity 106 can be formed between the gas-liquid separation device 300 and the cyclone device 400, as shown in fig. 1, and simultaneously, the cyclone device 400 is matched with the inner wall of the tank 100, so that the second cavity 106 and the third cavity 107 can be separated in the tank 100,

as shown in fig. 1, the mist catcher 500 is also fixed to the tank 100 and is located at a position above the cyclone device 400 by a certain distance, so that the third cavity 107 may be formed between the cyclone device 400 and the mist catcher 500, meanwhile, a certain distance is further formed between the mist catcher 500 and the top of the tank 100, so that the gas storage cavity 108 may be formed between the mist catcher 500 and the top of the tank 100, and the second outlet 103 is communicated with the gas storage cavity 108, so as to discharge the purified gas, and in implementation, the second outlet 103 is preferably configured at the top of the tank 100, as shown in fig. 1, of course, the second outlet 103 may also be configured at a side surface of the tank 100, which is not repeated herein.

In implementation, the cyclone device 400 may be an existing cyclone device 400, for example, the cyclone device 400 includes a plurality of cyclone tubes 401, the lower ends of the cyclone tubes 401 are communicated with the second cavity 106, and the upper ends of the cyclone tubes 401 are communicated with the third cavity 107, so that the gas in the second cavity 106 can only rise to the third cavity 107 through the cyclone tubes 401, so as to continuously separate the entrained light hydrocarbon, heavy hydrocarbon, wax, liquid (water and dehydrating agent) and the like in the rising process. In a more complete solution, the cyclone device 400 further includes a partition plate 405, a cylinder 404, and a bottom plate 402, as shown in fig. 1 and 2, where the partition plate 405 may be horizontally fixed in the tank 100 and separate the second cavity 106 and the third cavity 107 in the tank 100, it may be understood that, in implementation, an outer edge of the partition plate 405 may be directly fixed to a side wall of the tank 100, or the partition plate 405 may be fixed to a support 109, for example, as shown in fig. 1 and 2, the partition plate 405 is fixed to the support 109 by a bolt pair 600, the support 109 is fixed to an inner wall of the tank 100, and upper and lower ends of the cylinder 404 are respectively connected to the partition plate 405 and the bottom plate 402, so that the partition plate 405, the cylinder 404, and the bottom plate 402 may jointly enclose a closed drain cavity 407, as shown in fig. 1 and 2. To facilitate the arrangement of the swirl tubes 401, in this embodiment, as shown in fig. 1 and 4, the bottom plate 402 is configured with a plurality of first through holes 403 for adapting the swirl tubes 401, the partition plate 405 is configured with a plurality of second through holes 406 for adapting the swirl tubes 401, so that the lower ends of the swirl tubes 401 can be respectively communicated with the second cavity 106 through the first through holes 403, for example, the lower ends of the swirl tubes 401 can be butted with the first through holes 403, can be inserted into the first through holes 403, can also extend into the second cavity 106 through the first through holes 403, and can be communicated with the second cavity 106 as shown in fig. 1 and 2; meanwhile, the upper ends of the swirl tubes 401 extend into the third cavity 107 through the second through holes 406, and the extending height is determined according to practical requirements, as shown in fig. 1 and 2, only by preventing the liquid above from flowing into the swirl tubes 401.

In practice, to facilitate draining the liquid collected above the partition plate 405, in practice, the partition plate 405 is further configured with a first drain hole 408, and the upper end of the cyclone 401 is higher than the first drain hole 408, as shown in fig. 1 and 2, the first drain hole 408 may be in communication with the second cavity 106 and the third cavity 107, so that the liquid collected above the partition plate 405 may flow downward through the first drain hole 408. In a more sophisticated version, sealing rings are provided between the partition 405 and the support 109 and/or between the partition 405 and the side walls of the tank 100 to prevent leakage so that liquid can only fall through the first drain hole 408.

In addition, the bottom plate 402 is further provided with a second liquid drain hole 410, as shown in fig. 1 and 2, the second liquid drain hole 410 is communicated with the liquid drain cavity 407, and in the actual operation process, the mixed gas passing through the blade 301 type gas-liquid separation device 300 continuously ascends in the second cavity 106 and enters the cyclone tube 401, the gas forced to flow into the spiral end face of the inlet 101 of the cyclone tube 401 rapidly rotates, and liquid drops entrained in the gas are thrown to the inner wall of the cyclone tube 401 under the forced action of centrifugal force, so that a liquid film is formed by coalescence; under the action of airflow pushing force, the liquid film is thrown out from the side seam at the tail end of the cyclone tube 401 and enters the liquid discharging cavity 407; during this process, a small portion of the gas is simultaneously thrown out of the side seam at the end of cyclone tube 401 and this portion of the gas is redirected to the low pressure region of inlet 101 of cyclone tube 401 to repeat the separation process described above. The gas passes through the cyclone tube 401 and enters the third cavity 107 above, and the thrown liquid is discharged downwards through the second liquid discharge hole 410. In implementation, the number of the cyclone tubes 401 may be generally calculated according to the gas flow, and the number may be increased or decreased in the later stage, so as to ensure the separation effect, and in this embodiment, six cyclone tubes 401 are disposed in the cyclone device 400, and the cyclone tubes 401 are vertically disposed, so that pressure loss is reduced.

In this embodiment, the mist catcher 500 may be an existing mist catcher 500, for example, a wire mesh filler mist catcher 500 may be preferably used; in this embodiment, by disposing the mist catcher 500 above the cyclone device 400, droplets entrained in the gas, including light hydrocarbons, can be further intercepted by the mist catcher 500, and clean gas without entrained droplets is discharged from the second outlet 103 above the mist catcher 500, so as to complete the purification of natural gas with heavy hydrocarbons and waxes.

To further enhance the separation effect and efficiency, in a more sophisticated version, a first downcomer 409 and a second downcomer 411 are also included, wherein,

as shown in fig. 1 and 2, the upper end of the first downcomer 409 may be fixed to the partition plate 405 and is communicated with the first drain hole 408, and since the first drain hole 408 is communicated with the third cavity 107, the first downcomer 409 may be communicated with the third cavity 107 above, and at the same time, the lower end of the first downcomer 409 extends at least to the lower side of the gas-liquid separation device 300 and is sealed with liquid, as shown in fig. 1, for example, the lower end of the first downcomer 409 passes through the second cavity 106, the gas-liquid separation device 300, the first cavity 105 and the feed distributor 200 in sequence, and then directly extends into the liquid storage cavity 104, and liquid sealing is achieved in the liquid storage cavity 104, so that the first downcomer 409 may be utilized to separately drain the liquid collected in the third cavity 107 downwards, and the separated liquid may be effectively prevented from contacting with the upward air flow, and preventing part of the liquid from being taken away again by the air flow, thereby being beneficial to improving the separation effect and efficiency. In addition, in implementation, the first drain hole 408 may be preferentially configured on the outer side of the barrel 404, as shown in fig. 1 and 2, so that the first downcomer 409 may extend downward through the outer side of the barrel 404 without passing through the barrel 404, which is beneficial to simplifying the structure and facilitating assembly.

As shown in fig. 1-4, the upper end of the second downcomer 411 may be fixed to the bottom plate 402 and in communication with the second liquid discharge holes 410 in the cyclone device 400, while the lower end of the second downcomer 411 extends at least below the gas-liquid separation device 300 and is liquid-tight; as an example, as shown in fig. 1, the lower end of the second downcomer 411, after passing through the first cavity 105 and the feed distributor 200, also extends into the liquid storage cavity 104, and forms a liquid seal in the liquid storage cavity 104, so that the liquid separated from the cyclone device 400 is separately drained downwards by using the second downcomer 411, and the separated liquid is effectively prevented from contacting with the ascending airflow, which is also beneficial to improving the separation effect and efficiency.

In implementation, a conventional structure may be used to implement the liquid seal, for example, in this embodiment, a liquid seal structure 111 adapted to each downcomer may be disposed at the lower end of each downcomer, and the liquid seal structure 111 may be a container enclosed by the side wall of the tank body 100 and having an opening at the upper end, as shown in fig. 1, and the lower ends of the first downcomer 409 and the second downcomer 411 may be respectively inserted into the corresponding liquid seal structure 111 to implement the liquid seal.

For natural gas with heavy hydrocarbon and wax, when the vertical low-temperature separator is actually used, mixed gas and liquid enter the feed distributor 200 through the inlet 101, the mixed gas and liquid realize preliminary separation of gas and liquid in the feed distributor 200, meanwhile, the gas phase distribution is more uniform, the separated liquid (comprising heavy hydrocarbon, wax, liquid (water and dehydrating agent) and the like) drops into the liquid storage cavity 104 below, and the mixed gas and liquid rises to the first cavity 105 and passes through the gas-liquid separation device 300; the heavy hydrocarbon, wax and liquid (water and dehydrating agent) in the mixed gas-liquid are effectively intercepted and separated by the gas-liquid separation device 300 after passing through the gas-liquid separation device 300, so that secondary separation is realized, and particularly, the heavy hydrocarbon and wax can be effectively removed, and the separated liquid drops into the liquid storage cavity 104 below; the mixed gas-liquid passes through the gas-liquid separation device 300, then enters the second cavity 106, continuously rises in the second cavity 106, and passes through the cyclone device 400 through the cyclone tube 401, in the process, liquid drops carried in the gas, including light hydrocarbons, residual heavy hydrocarbons, wax and the like, can be effectively removed by the cyclone tube 401, three-time separation is realized, and the separated liquid directly falls into the liquid storage cavity 104 through the first downcomer 409; the mixed gas and liquid enter the third cavity 107 after passing through the cyclone device 400, continuously ascend in the third cavity 107 and pass through the mist catcher 500, in the process of passing through the mist catcher 500, droplets entrained in the gas are further intercepted by the mist catcher 500, including light hydrocarbons and the like, the gas enters the gas storage cavity 108 above, the separated liquid drops on the partition plate 405 and directly falls into the liquid storage cavity 104 through the second downcomer 411, finally, clean gas in the gas storage cavity 108 after complete purification treatment is discharged through the second outlet 103, and the liquid separated by the whole equipment is collected in the liquid storage cavity 104 and discharged through the first outlet 102.

Of course, it will be appreciated that the present vertical cryogenic separator may be used not only to treat natural gas with heavy hydrocarbons and waxes, but also to treat existing conventional natural gas, and will not be described in detail herein.

Example 2

In order to solve the problem of preventing the gas-liquid separation device 300 from being blocked, the main difference between the embodiment 2 and the above embodiment is that, in the vertical low-temperature separator provided in the present embodiment, a plurality of rinse nozzles 110 are further disposed in the second cavity 106, as shown in fig. 5, the rinse nozzles 110 may be fixed on the sidewall of the tank 100, and in implementation, the rinse nozzles 110 with adjustable directions may be selected, so that after the installation is completed, the rinse nozzles 110 face the gas-liquid separation device 300, so as to rinse the gas-liquid separation device 300. Specifically, by arranging the flushing nozzle 110, the gas-liquid separation device 300 can be periodically flushed from above the gas-liquid separation device 300 by the flushing nozzle 110, and for example, during the annual maintenance period, the gas-liquid separation device 300 can be flushed by the flushing nozzle 110, and heavy hydrocarbons, wax, and the like adhering to the gas-liquid separation device 300 can be flushed, so that the gas-liquid separation device 300 can be effectively prevented from clogging, and the separation effect of the gas-liquid separation device 300 can be improved.

Example 3

To solve the problem of achieving a better mist capturing effect, the main difference between the present embodiment 3 and the above-described embodiment is that the vertical cryogenic separator provided in the present embodiment, the mist capturing device 500 includes a first filler portion 501 and a second filler portion 502, wherein,

the second packing 502 is configured to be adapted to the inner diameter of the can 100, for example, the outer diameter of the second packing 502 is the same as the inner diameter of the can 100, so that the second packing 502 can transversely fill the entire can 100, as shown in fig. 6 and 7, thereby eliminating a gap between the second packing 502 and the inner wall of the can 100, allowing gas to enter the upper gas storage chamber 108 only after passing through the second packing 502,

the first packing portion 501 is smaller than the inner diameter of the tank body 100, and the first packing portion 501 is arranged below the second packing portion 502, so that a gap is formed between the first packing portion 501 and the inner wall of the tank body 100, and as shown in fig. 6 and 7, the second packing portion 502 and the first packing portion 501 can form a convex-shaped structure, so that the thickness of packing in the mist catcher 500 can be increased, liquid drops entrained in gas can be better intercepted, the intercepted liquid drops are more favorably separated from the packing, a better mist catching effect can be achieved, and the blocking of residual heavy hydrocarbons, wax, liquid (water and dehydrating agent) and the like in the gas is particularly favorable.

To facilitate assembly of the mist catcher 500, in a more sophisticated version, the mist catcher 500 further comprises a support frame, as shown in fig. 6 and 7, the support frame comprises an annular bottom plate 503402, a first grid plate 504 is connected to the center of the annular bottom plate 503402, and a support cylinder 505 is connected to the inner ring of the annular bottom plate 503402, and the support cylinder 505 is perpendicular to the annular bottom plate 503402, as shown in fig. 6 and 7.

Meanwhile, the support frame further includes a second grid plate 506 disposed above the annular bottom plate 503402 by a certain distance, as shown in fig. 6 and 7, so that a first packing cavity can be formed between the support cylinder 505 and the first grid plate 504, the first packing portion 501 is disposed in the first packing cavity, meanwhile, a second packing cavity can be formed between the support cylinder 505 and the second grid plate 506, and the second packing portion 502 is disposed in the second packing cavity, as shown in fig. 6 and 7. In addition, the annular bottom plate 503402 is further configured with a third drain hole 508, and the third drain hole 508 communicates with the third chamber 107 below so as to drain down. The mist catcher 500 adopting the structure not only facilitates the installation and replacement of the first packing part 501 and the second packing part 502, but also allows the liquid drops intercepted by the second packing part 502 to fall down more easily through the space between the supporting cylinder 505 and the side wall of the tank body 100 and flow downwards through the third liquid discharge hole 508, thereby realizing the separation from the ascending air flow and being beneficial to realizing better separation effect.

In practice, the annular bottom plate 503402 and the second grid plate 506 may be fixed to the inner wall of the can body 100, respectively, and in another embodiment, the support frame further includes a support bracket 507 connecting the annular bottom plate 503402 and the second grid plate 506, as shown in fig. 6 and 7, where the support bracket 507 is configured to be adapted to the inner wall of the can body 100, so that the entire support frame may be formed as a whole, and the whole may be fixed to the can body 100 through the support 109, or may be directly fixed to the can body 100 through welding, etc.

In practice, the first filler part 501 and the second filler part 502 may be respectively wire mesh fillers.

In a more complete embodiment, as shown in fig. 6 and 7, a third downcomer 509 is further included, where an upper end of the third downcomer 509 is connected to the annular bottom plate 503402 and is in communication with the third drain 508, and a lower end of the third downcomer 509 is in fluid sealing in the third cavity 107. By arranging the third downcomer 509 and sealing the lower end of the third downcomer 509 in the third cavity 107, droplets separated from the mist catcher 500 can be independently drained downwards by the third downcomer 509, and the separated droplets can be effectively prevented from contacting with the ascending air current, which is beneficial to improving the separation effect and efficiency.

In the present embodiment, the liquid seal structure 111 is disposed in the third chamber 107, and the lower end of the third downcomer 509 is inserted into the liquid seal structure 111 to realize liquid seal, as shown in fig. 6 and 7.

The foregoing is merely illustrative of the present utility model, and the present utility model is not limited thereto, and any person skilled in the art will readily recognize that variations or substitutions are within the scope of the present utility model.

Claims

1. The vertical low-temperature separator comprises a tank body which is a vertical tank body and is provided with an inlet, a first outlet and a second outlet, and is characterized by also comprising a feeding distributor which is fixed on the tank body and communicated with the inlet, a liquid storage cavity is formed between the feeding distributor and the bottom of the tank body, the first outlet is communicated with the liquid storage cavity,

the cyclone device comprises a plurality of cyclone pipes, the lower ends of the cyclone pipes are communicated with the second cavity, and the upper ends of the cyclone pipes are communicated with the third cavity.

2. The vertical cryogenic separator according to claim 1, wherein the gas-liquid separation device is a vane type gas-liquid separation device.

3. The vertical cryogenic separator of claim 1, further comprising a first downcomer, wherein the swirling device cooperates with an inner wall of the tank and separates the second and third chambers within the tank,

the cyclone device is also provided with a first liquid discharge hole which is communicated with the third cavity, the upper end of the cyclone tube is higher than the first liquid discharge hole, the upper end of the first downcomer is communicated with the first liquid discharge hole, and the lower end of the first downcomer at least extends to the lower part of the gas-liquid separation device and is sealed by liquid.

4. A vertical cryogenic separator according to claim 3, further comprising a second downcomer, the upper end of which communicates with the cyclone means, the lower end of which extends at least below the gas-liquid separation means and is liquid-tight.

5. The vertical cryogenic separator of claim 4, wherein the cyclone assembly further comprises a divider plate, a cylinder, and a bottom plate, wherein the divider plate is horizontally secured within the tank and separates the second and third chambers within the tank,

the first drain hole is formed in the partition plate,

the bottom plate is also provided with a second liquid discharge hole which is communicated with the liquid discharge cavity, and the upper end of the second downcomer is fixed on the bottom plate and communicated with the second liquid discharge hole.

6. The vertical cryogenic separator according to claim 5, wherein a support is mounted to an inner wall of the tank, the partition plate is fixed to the support, and the first drain hole is constructed at an outer side of the cylinder.

7. The vertical cryogenic separator according to any one of claims 1-6, wherein the mist catcher comprises a first filler portion and a second filler portion, wherein the second filler portion is configured to fit the inner diameter of the tank to eliminate a gap with the inner wall of the tank,

the first filler portion is smaller than the inner diameter of the tank body, the first filler portion is arranged below the second filler portion, and a gap is reserved between the first filler portion and the inner wall of the tank body.

8. The vertical cryogenic separator of claim 7, further comprising a support frame, the support frame comprising an annular base plate, a first grid plate being connected to a center of the annular base plate, and a support cylinder being connected to an inner ring of the annular base plate,

the annular bottom plate is provided with a third liquid drain hole.

9. The vertical cryogenic separator of claim 8, further comprising a third downcomer, an upper end of the third downcomer being connected to the annular bottom plate and in communication with the third drain hole, a lower end of the third downcomer effecting a liquid seal in the third chamber.

10. The vertical cryogenic separator according to any one of claims 1-6, characterized in that a number of flushing nozzles are also arranged in the second chamber, the flushing nozzles being directed towards the gas-liquid separation means for flushing the gas-liquid separation means.