CN108978308B

CN108978308B - Cyclone separator and pulping and drying system

Info

Publication number: CN108978308B
Application number: CN201810679640.8A
Authority: CN
Inventors: 何平
Original assignee: Guangxi App Paper Co ltd
Current assignee: Guangxi App Paper Co ltd
Priority date: 2018-06-27
Filing date: 2018-06-27
Publication date: 2021-10-15
Anticipated expiration: 2038-06-27
Also published as: CN108978308A

Abstract

The application discloses cyclone and slurrying drying system, wherein the cyclone includes first casing and second casing. First casing connect in the top of second casing, just first casing with second casing intercommunication, the feed inlet has been seted up on the first casing, treats the separation material process the feed inlet enters into in first casing and the second casing in order to form the whirlwind air current, the second casing is the obconical setting, wherein the second casing includes that the polylith is the curb plate of strip setting, the polylith curb plate connects gradually in order to form the lateral wall of second casing, wherein the extending direction of the connecting wire that the polylith curb plate connection formed with cyclone during operation the contained angle between the air current direction that is close to the inner wall in the second casing is less than 25. Through the mode, the good separation effect can be achieved.

Description

Cyclone separator and pulping and drying system

Technical Field

The application relates to the technical field of pulping and drying, in particular to a cyclone separator and a pulping and drying system.

Background

The Chinese has been changing over the land for three decades, and along with the rapid development of the industries such as news, printing and packaging, the Chinese pulping and papermaking industry has also opened a new chapter. With the increasing demand for some high-grade paper products such as liquid food packaging paper, low basis weight coated paper, etc., China has become the world's largest consumer of high-yield commercial pulp (chemi-mechanical pulp). However, the cyclone separator used in the pulping process at present has high manufacturing cost and poor separation efficiency, and becomes a great bottleneck of the technology in the papermaking field.

Disclosure of Invention

The technical problem that this application mainly solved provides cyclone and slurrying drying system, can realize the separation of thick liquid and humid air better.

In order to solve the technical problem, the application adopts a technical scheme that: a cyclonic separator is provided comprising a first housing and a second housing. First casing connect in the top of second casing, just first casing with second casing intercommunication, the feed inlet has been seted up on the first casing, treats the separation material process the feed inlet enters into in first casing and the second casing in order to form the whirlwind air current, the second casing is the obconical setting, wherein the second casing includes that the polylith is the curb plate of strip setting, the polylith curb plate connects gradually in order to form the lateral wall of second casing, wherein the extending direction of the connecting wire that the polylith curb plate connection formed with cyclone during operation be close to the inner wall in the second casing contained angle between the air current direction is less than 25.

In order to solve the above technical problem, another technical solution adopted by the present application is: a pulp drying system is provided that includes a pre-drying section and a flash drying section. And the pre-drying section is used for pre-drying the slurry to obtain a slurry block. The flash drying section includes a defibrator for defibering the pulp mass into a fluff pulp, a drying assembly for drying the fluff pulp to obtain a dried fluff pulp, and a cyclone for creating a cyclonic airflow to separate the dried fluff pulp from wet air.

The cyclone separator comprises a first shell and a second shell, the first shell is connected to the top of the second shell, a feed inlet is formed in the first shell to receive airflow carrying the dry flocculent pulp and form the cyclone airflow in the cyclone separator, the second shell is arranged in an inverted cone shape, the second shell comprises a plurality of side plates, the side plates are sequentially connected to form a side wall of the second shell, and an included angle formed between the extending direction of a connecting line formed by connecting the side plates and the airflow direction close to the inner wall in the second shell is smaller than 25 degrees when the cyclone separator works.

Compared with the prior art, the beneficial effects of this application are: this application connects gradually through the polylith curb plate in order to form the lateral wall of second casing, is different from the mode that adopts large tracts of land panel among the prior art, can reduce the cost, the extending direction of connecting wire with cyclone during operation contained angle between the airflow direction of being close to the lateral wall in the second casing is less than 25, so can make the extending direction of connecting wire unanimous or unanimous roughly with the airflow direction of lateral wall, can also reduce the interference to the air current under the more condition of connecting wire, realizes good separation effect on reduce cost's basis.

Drawings

FIG. 1 is a schematic structural view of an embodiment of a cyclone separator of the present application;

FIG. 2 is a schematic view of a cyclonic airflow in an embodiment of the cyclone separator of the present application;

FIG. 3 is a schematic view of a second housing in an embodiment of the cyclone separator of the present application in an expanded configuration;

FIG. 4 is a schematic view of another expanded configuration of the second housing in the cyclone embodiment of the present application;

FIG. 5 is a schematic block diagram of an embodiment of a pulp drying system of the present application;

FIG. 6 is a schematic diagram of a press in an embodiment of a pulp drying system of the present application;

FIG. 7 is a schematic structural diagram of an air duct in an embodiment of a pulp drying system of the present application.

Detailed Description

The technical solutions in the embodiments of the present application will be clearly and completely described below with reference to the drawings in the embodiments of the present application, and it is obvious that the described embodiments are only a part of the embodiments of the present application, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present application.

Referring to fig. 1 and 2, the cyclone separator 11 of the cyclone separator embodiment of the present application includes a first housing 111 and a second housing 112. The first housing 111 is attached to the top of the second housing 112. The first housing 111 has a cylindrical shape. The second housing 112 is disposed in an inverted conical shape. In the present embodiment, the top of the second housing 112 refers to the position of the circular surface in the shape of an inverted cone as the top, and the position in the shape of a cone as the bottom. One end of the first housing 111 is connected to the top of the second housing 112, for example, by welding. The inside of the first casing 111 and the inside of the second casing 112 are communicated to form a communicated inner chamber so as to form a cyclone airflow. The side wall of the first housing 111 is formed with a feed port 11 b. For example, the side wall of the first housing 111 is formed with a feed inlet 11b adjacent to the top of the first housing 111, the feed inlet 11b being adapted to receive an airflow carrying fluff pulp, i.e. the material to be separated comprises at least humid air and fluff pulp, and to form a cyclonic airflow within the interior of the cyclone separator 11. An air outlet 11a is formed at the top of the first casing 111, and when the cyclone separator 11 separates the flocculent pulp from the humid air, the humid air is discharged from the air outlet 11 a. A discharge port 11c is formed at the bottom of the second casing 112, and the separated flocculent pulp is discharged from the discharge port 11c to enter the next link. In the present embodiment, the wet air refers to an air component to be separated for the floc slurry, and there is no particular limitation on the humidity.

Referring to fig. 1 and fig. 3, in the present embodiment, the second housing 112 includes a plurality of side plates 1121 disposed in a strip shape. The side plates 1121 are steel plates, for example. The side plate 1121 is further a stainless steel plate. The side plates 1121 are sequentially connected to form a side wall of the second housing 112. For example, two adjacent side plates 1121 are welded at opposite sides along the length direction. Referring to fig. 3, fig. 3 shows an expanded structure of the second housing 112, for example, two adjacent side plates 1121 of the plurality of side plates 1121 are connected in sequence by side edges and side edges, so as to form side walls of the second housing 112. For example, in the manufacturing process, the side plates 1121 that are not subjected to the crimping step are sequentially connected side by side to form a fan-shaped structure as shown in fig. 3, and have a side B and a side a, and then the fan-shaped structure is subjected to the crimping step to connect the side a and the side B to form a side wall of the second housing 112 as shown in fig. 1, and it should be noted that if the side of the side plates 1121 is taken as a front view direction, the side may also be represented as a plane (for example, the side B is actually a plane when viewed from the side B direction), so that two adjacent side plates 1121 of the plurality of side plates 1121 are sequentially connected by the connection of the side surface and the side surface, and then the side plates are crimped and connected to form the second housing 112 in an inverted cone shape. Referring to fig. 3, in the unfolded state, an acute angle formed by a connecting line 1122 of the side plates 1121 with the central axis is less than 60 °, and optionally less than 45 °. In this embodiment, the central axis is perpendicular to a tangent line of the center point of the arc edge of the fan-shaped structure. By arranging the connection structure for the side plates 1121, it can be realized that an included angle β between an extending direction of a connection line 1122 formed by connecting a plurality of side plates 1121 and an airflow direction inside the second housing 112 close to the side wall when the cyclone separator 11 is in operation is less than 25 °, as shown in fig. 2.

With reference to fig. 2, specifically, the airflow carrying the flocculent slurry enters the first housing 111 from the feeding port 11b, for example, the airflow enters the first housing 111 along a tangential direction, and due to the high speed of the airflow, a spiral airflow is generated in the inner cavity of the cyclone separator 11 on the basis of gravity and centrifugal force, especially, the airflow near the inner wall of the cyclone separator 11 may rub against the sidewall, in this embodiment, it has been long researched and developed by the inventor that, when the cyclone separator 11 works, the sidewall of the second housing 112 is formed by the connection of the side plates 1121, and an included angle β between the extending direction of the connection line 1122 and the airflow direction near the sidewall in the second housing 112 is smaller than 25 °. Optionally, the angle β between the direction of extension of the connecting line 1122 and the direction of airflow within the second housing 112 adjacent the side wall is less than 20 ° when the cyclonic separator 11 is in operation. Optionally, the angle β between the direction of extension of the connecting line 1122 and the direction of airflow within the second housing 112 adjacent the side wall is less than 15 ° when the cyclonic separator 11 is in operation. Optionally, the angle β between the direction of extension of the connecting line 1122 and the direction of airflow within the second housing 112 adjacent the side wall is less than 10 ° when the cyclonic separator 11 is in operation. Optionally, when the cyclone separator 11 is in operation, the angle β between the extension direction of the connecting line 1122 and the airflow direction near the side wall in the second housing 112 is less than 5 °

Since the cyclone separator 11 plays an important role in separating the flocculent pulp from the wet air, the protrusions or depressions of the inner wall of the cyclone separator 11, such as weld seams, have a great influence on the flow of the airflow, so that the airflow cannot effectively flow, and the flocculent pulp may not be effectively discharged or directly escape from the air outlet 11 a. In the prior art, the most common technical means is to reduce the weld to ensure the smoothness of the inner wall, thereby reducing the disturbance caused by the impact of the air flow and the weld. In order to reduce welding seams, the most common method at home and abroad is to manufacture the cyclone separator by adopting plates with large areas, so that the welding seams can be reduced, but the plates with large volumes are expensive.

Different from the conventional scheme in the prior art, the present embodiment is sequentially connected to form the side wall of the second casing 112 through the plurality of side plates 1121, and different from the manner of using a large-area plate in the prior art, the present embodiment can reduce the cost by manufacturing the cyclone separator through a plate having a small area, and meanwhile, the inventor has found through long-term research and development that by setting the included angle β between the extending direction of the connecting line 1122 and the airflow direction inside the second casing 112 close to the side wall when the cyclone separator 11 works to be smaller than 25 °, the extending direction of the connecting line 1122 and the airflow direction of the side wall can be consistent or substantially consistent, the interference to the airflow can be reduced even when there are many connecting lines 1122, and a good separation effect can be achieved on the basis of reducing the cost.

Optionally, the side plates 1121 are welded in sequence along the connecting line 1122. In other words, the side plates 1121 are connected together by welding, and an included angle β between the direction of the welding seam and the direction of the air flow is less than 25 °. The width D of at least a portion of the side panels 1121 is uniform and is between 1m-2 m. Optionally, the width D of at least a portion of the side panel 1121 is 1.5 m.

In this embodiment, the side plates 1121 are sequentially connected to form a side wall of the second housing 112, and due to different specific design and manufacturing conditions, it is not excluded that a leftover material and the side plates 1121 together form a complete side wall of the second housing 112 in the manufacturing process. The scrap can also be considered as a side panel 1121. As shown in fig. 3, if the leftmost leftover material in the drawing is regarded as a side plate 1121, if it cannot have the full width D, the widths D of other side plates 1121 with the full width are the same, that is, the widths D of at least part of the side plates 1121 are the same.

In this embodiment, the width D of the side plate 1121 is between 1m and 2m, so that the cost can be reduced by using a plate with a smaller area/size, and then the width D of the side plate 1121 is consistent, so that the position of the connecting wire 1122 can be uniformly arranged, and the influence on the airflow can be further reduced. In the prior art, steel plates with the width larger than 4m are often welded to manufacture the cyclone separator so as to reduce welding seams. In this embodiment, the second casing of the cyclone separator 11 is made of a steel plate having a width of 1m to 2m, and the connection lines 1122 are provided to effectively separate the second casing even if the number of welding lines is increased, thereby reducing the manufacturing cost.

Referring to fig. 4, fig. 4 shows another expanded structure of the second housing 112, the second housing 112 may further include an end plate 1123 connected to an end of the plurality of side plates 1121, which are in the same extending direction and are close to the bottom of the second housing 112, and a side edge of the side plate 1121, which is closest to the bottom of the second housing 112, of the plurality of side plates 1121 is connected to a side edge of the end plate 1123 to form a side wall of the second housing 112.

As shown in fig. 4, one side of the end plate 1123 is connected to one end of the side plates 1121, the end is an end of the side plates 1121 that extends in the same direction and is close to the bottom of the second housing 112, and the other side of the end plate 1123 is connected to the side of the side plate 1121 that is closest to the bottom of the second housing 112, and it should be noted that, in a side view, the side of the side plate 1121/end plate 1123 is presented in a face manner. As shown in fig. 4, for example, in the manufacturing process, the side plates 1121 that are not subjected to the curling process are sequentially connected side to side, then one side of the end plate 1123 is connected to the end of each side plate 1121 near the bottom of the second case 112 to form a fan-shaped structure as shown in fig. 4, which has an a side and a C side, and then the fan-shaped structure is subjected to the curling process to connect the a side and the C side, such as welding, to form the side wall of the second case 112 as shown in fig. 1.

Referring to fig. 5, the embodiment of the pulp drying system of the present application includes a pre-drying section 2a and a flash drying section 2 b. The pre-drying section 2a is used for pre-drying the slurry to obtain a slurry block. In this embodiment, the pre-drying process includes a dewatering process for dewatering the slurry to increase the consistency or dryness to form a cake, facilitating further drying in the flash drying section 2 b. The flash drying section 2b comprises a defiberizer 22, a drying assembly 23 and a cyclone 11, wherein the defiberizer 22 is used for defibering the pulp mass into a fluff pulp, the drying assembly 23 is used for drying the fluff pulp, and the cyclone 11 is used for forming a cyclone airflow to separate the dried fluff pulp from the wet air.

With continued reference to fig. 1-4, the cyclonic separator 11 includes a first housing 111 and a second housing 112. The first housing 111 is connected to the top of the second housing 112. The second housing 112 is disposed in an inverted conical shape. The second casing 112 is provided with a feed port 11 b. For example, the second housing 112 may have a side wall adjacent the top opening with a feed inlet 11b for receiving an airstream carrying dry fluff pulp (i.e., material to be separated including fluff pulp) and creating a cyclonic airflow within the cyclone separator 11. The feed port 11b communicates with the discharge port of the drying module 23. So that the dried fluff pulp enters the cyclone 11 with the air flow. Specifically, the airflow enters the first housing 111 in a tangential direction of the side wall. The second housing 112 includes a plurality of side plates 1121, the side plates 1121 are connected in sequence to form a side wall of the second housing 112, wherein an included angle β between an extending direction of the connecting line 1122 and an airflow direction inside the second housing 112 close to the side wall when the cyclone separator 11 is in operation is less than 25 °. Optionally, the angle β between the direction of extension of the connecting line 1122 and the direction of airflow within the second housing 112 adjacent the side wall is less than 20 ° when the cyclonic separator 11 is in operation. Optionally, the angle β between the direction of extension of the connecting line 1122 and the direction of airflow within the second housing 112 adjacent the side wall is less than 15 ° when the cyclonic separator 11 is in operation. Optionally, when the cyclone separator 11 is in operation, the angle β between the extension direction of the connecting line 1122 and the airflow direction near the side wall in the second housing 112 is less than 10 °

In the practical operation of the pulp drying system of this embodiment, the pre-drying stage 2a receives the low-consistency pulp, for example, the pulp with the consistency of about 5.5%, and performs the dewatering treatment to obtain the pulp with the high dryness, for example, the pulp with the consistency of 45% or more, for example, the pulp in the form of particles. The defiberizer 22 decomposes the pulp to be fiberized or flocculent to obtain flocculent pulp, the fiberized flocculent pulp can flow into the drying assembly 23 along with the airflow, and the water content of the flocculent pulp is evaporated under the drying of the drying assembly 23, thereby improving the dryness of the flocculent pulp. After the airflow passes through the drying assembly 23, the discharge port of the drying assembly 23 enters the feed port 11b of the cyclone separator 11, the airflow enters the cyclone separator 11 at a high speed, a spiral is formed in the first casing 111 and the second casing 112, under the action of centrifugal force and gravity, the wet air with a low density is discharged from the air outlet 11a at the top of the second casing 112, and the flocculent pulp with a high density is discharged from the discharge port 11c at the bottom of the second casing 112, in this embodiment, the side walls of the second casing 112 are sequentially connected through the side plates 1121, and an included angle between the extending direction of the connecting line 1122 and the airflow direction close to the side wall in the second casing 112 when the cyclone separator 11 works is smaller than 25 °, so that the manufacturing cost of the cyclone separator 11 can be reduced, and meanwhile, the interference to the airflow can be reduced, thereby improving the separation efficiency.

Referring to fig. 3 and fig. 4, optionally, a plurality of side plates 1121 are welded in sequence along a connecting line 1122, and the width D of at least a portion of the side plates 1121 is uniform and is between 1m and 2 m.

Optionally, the second shell 112 further includes an end plate 1123 connected to an end of the plurality of side plates 1121, which is in the same extending direction and is close to the bottom of the second shell 112, and a side edge of the side plate 1121, which is closest to the bottom of the second shell 112, of the plurality of side plates 1121 is connected to a side edge of the end plate 1123 to form a side wall of the second shell 112.

The cyclone separator 11 in this embodiment can specifically refer to the explanation of the cyclone separator implementation in this application, and will not be described herein again.

Optionally, the predrying section 2a comprises a pulp distributor 201 and a press 202, the pulp distributor 201 being arranged at the feed inlet of the press 202 for distributing the pulp such that the pulp enters the press 202. The press 202 is used to pre-dry the pulp to form a pulp mass. Further, the pulp distributor 201 can uniformly distribute the pulp to uniformly enter the press 202, and the dryness of the pulp is improved to obtain pulp blocks under the pre-drying treatment of the press 202.

Referring to fig. 6, the press master 202 is specifically a multi-press zone twin-wire press master 202, which is a press master that performs a press dewatering process under multiple pressures. The press 202 comprises a first wire 2021 and a second wire 2022. For example, the first net 2021 and the second net 2022 are mesh fabrics on which the slurry can be laid, and the first net 2021 and the second net 2022 allow moisture to permeate therethrough, so that the slurry can be dewatered. The first and

second nets

2021 and 2022 are supported by first and second tensioning mechanisms 2023 and 2024, respectively, and in this embodiment, the first tensioning mechanism 2023 may include a plurality of tensioning devices, and the second tensioning mechanism 2024 may include a plurality of tensioning devices, of which only the first and second tensioning mechanisms 2023 and 2024 are labeled above two, respectively, in fig. 6. The first net 2021 and the second net 2022 can be rotated so that the slurry can be continuously transported for drying. The first web 2021 and the second web 2022 are in partial contact, e.g., in partial continuous contact, forming a nip. At the feed inlet of the press 202, a gap, for example in the shape of a wedge, is formed between the first wire 2021 and the second wire 2022 to receive the slurry, forming a wedge-shaped press zone. In this embodiment, the first wire 2021 and the second wire 2022 form a gap at the inlet of the press 202, the height of the gap gradually decreases from the inlet to the outlet until the first wire 2021 and the second wire 2022 come into contact, gradually transitioning from the wedge-shaped press section to the press section. Further, the gap formed by the first net 2021 and the second net 2022 in the wedge-shaped filter press zone is adjustable in height, for example, by adjusting the position of the corresponding component between the first tensioning mechanism 2023 and the second tensioning mechanism 2024. The press 202 further comprises a plurality of pairs of press rolls 2025, which pairs of press rolls 2025 are arranged in sequence in the direction from the inlet to the outlet of the press 202 in the press zone. Wherein one of each pair of press rolls 2025 is disposed on the side of the first web 2021 and the other is disposed on the side of the second web 2022, and each pair of press rolls 2025 is used to press the slurry between the first web 2021 and the second web 2022.

In actual operation, the pulp distributor 201 distributes the pulp more uniformly to the wedge-shaped press filtration zone at the feed inlet of the press 202, the pulp is dewatered by gravity and the pressure of the wedge-shaped zone, and as the first wire 2021 and the second wire 2022 rotate, the pulp enters the press zone from the wedge-shaped press filtration zone and is pressed by the multiple pairs of press rolls 2025, so that the free water in the pulp is continuously dragged out, and the dryness of the pulp is continuously improved.

Specifically, the press master 202 includes 6 pairs of press rolls 2025. The first press roller group 2025a to the sixth press roller group 2025f are provided in this order from the inlet port to the outlet port of the press roll 202. The extrusion zone is further divided into an S-shaped extrusion zone and a linear extrusion zone. The first pressure roller set 2025a and the second pressure roller set 2025b are sequentially disposed in the S-shaped pressing section. Two press rollers in the first press roller set 2025a are arranged in parallel, the center of a press roller on one side of the first net 2021 is higher than the center of another press roller on one side of the second net 2022, and the other press roller on one side of the second net 2022 is closer to the feed inlet of the pulp extruder 202 than the press roller on one side of the first net 2021, so that the first net 2021 and the second net 2022 are S-shaped when they are wound around the two press rollers of the first press roller set 2025 a. As the slurry passes through the first press roll set 2025a, the first wire 2021 and the second wire 2022 are subjected to a tension force from the two press rolls of the first press roll set 2025a, so that the slurry between the first wire 2021 and the second wire 2022 is dewatered. The same applies to the second press roller set 2025 b.

The third press roll group 2025c to the sixth press roll group 2025f are sequentially disposed in a linear extrusion zone, taking the third press roll group 2025c as an example, two press rolls of the third press roll group 2025c are disposed opposite to each other up and down, and axes passing through centers of circles of the two press rolls in the up-down direction are parallel to each other, and the axes are not coincident, and the two press rolls of the third press roll group 2025c are respectively disposed on one side of the first net 2021 and the second side of the first net 2021 to extrude the slurry between the first net 2021 and the second net 2022. The same applies to the fourth to sixth roller groups 2025 f. For example, the third and sixth

pressure roller groups

2025c and 2025f are driven by a driving motor, and the fourth and fifth

pressure roller groups

2025d and 2025e are driven rollers.

Optionally, the temperature of the slurry is 60 ° to 70 °. The inventors have long found that higher temperatures decrease the viscosity of the pulp, increase the flow and permeability, and facilitate dewatering, but that too high a temperature has an effect on the life of the soft material in the press 202 and thus also on the life of the entire press 202. Through multiple research and tests, the inventor finds that the slurry temperature of more than 60 ℃ is relatively proper, the dehydration effect of the slurry of 60 ℃ can be improved by 3 percent compared with that of 40 ℃, the improvement effect of the continuous increase of the temperature on the dryness is not obvious, and the limit temperature of a common colloid material is 90 ℃, so that the temperature control range of 60-70 ℃ is relatively reasonable. In this embodiment, the pulp temperature can be controlled by arranging a heating pipe in the white water tank, and introducing steam into the heating pipe to realize heating.

Alternatively, the line pressure between the pairs of press rolls 2025 is gradually increased in a direction from the inlet to the outlet of the press 202. The line pressure represents the pressure per unit length of the contact surface between a pair of press rolls.

Higher line pressure is more beneficial for dewatering but is detrimental to the life of the wire and the drive load and is directly related to the stiffness of the press rolls and cannot be simply pursued for high line pressure, but the determination of line pressure is very important for dewatering in the press 202. In this embodiment, the linear pressure between the pairs of press rollers 2025 is gradually increased, and the slurry can be sequentially and effectively dewatered, so that the dewatering effect is better.

For example, the design linear pressure of the S-shaped extrusion area is 60-80N/mm, the third press roll set 2025c is 80-100N/mm, the fourth press roll set 2025d is 100-.

In this embodiment, the pre-drying section 2a further comprises a crushing screw (not shown) for crushing the pulp mass after the pre-drying process of the press 202 to form a granular pulp mass.

Referring to fig. 5, in the present embodiment, the eucalyptus pulp with a pulp temperature of 60-70 ° and a concentration of about 5.5% is processed by the press 202 of the present embodiment through the twin-wire multi-extrusion pre-drying process to form pulp lumps with a dryness of more than 45%, the pulp lumps are granulated by the crushing screw to form granular pulp lumps, and then the granular pulp lumps are conveyed to the defiberizer 22 for fiberization, and the fiberized flocculent pulp enters the corresponding air duct 235 under the suction effect of the conveying fan to enter the multiple sets of drying towers 232 for drying.

With continued reference to fig. 5, the drying assembly 23 may optionally include a plurality of sets of heat exchanger banks 231 and a plurality of sets of drying towers 232. Wherein each set of drying towers 232 corresponds to a set of heat exchanger sets 231. The air to be heated flows through the heat exchanger group 231 to become dry air, and the dry air is led to the corresponding drying tower 232. In other words, each drying tower 232 has a corresponding heat exchanger group 231 for providing the drying air after heat exchange.

The flocculent pulp is dried in a plurality of groups of drying towers 232 in sequence. Specifically, the flocculent pulp enters the air pipe 235 corresponding to the drying tower 232 which dries the flocculent pulp first, enters the drying tower 232 along with the air flow, and then sequentially enters the remaining drying towers 232.

For example, in the present embodiment, the drying assembly 23 includes three sets of heat exchanger sets 231 and three sets of drying towers 232. The three groups of heat exchanger groups 231 are first to third heat exchanger groups 2311 to 2313. The three groups of drying towers 232 are first to third drying towers 2321 to 2323. The first heat exchanger group 2311 provides the drying air to the first drying tower 2321, the second heat exchanger group 2312 provides the drying air to the second drying tower 2322, and the third heat exchanger group 2313 provides the drying air to the third drying tower 2323.

The first drying tower 2321 includes a first drying tower feed inlet disposed near the top of the first drying tower 2321, an air outlet disposed at the top of the first drying tower 2321, and a discharge outlet disposed at the bottom of the first drying tower 2321. The second drying tower 2322 includes a feed inlet disposed near the top of the second drying tower 2322, an air outlet disposed at the top of the second drying tower 2322, and a discharge outlet disposed at the bottom of the second drying tower 2322. The third drying tower 2323 includes a feed inlet disposed near the top of the third drying tower 2323, an air outlet disposed at the top of the third drying tower 2323, and a discharge outlet disposed at the bottom of the third drying tower 2323.

The feed inlet of the first drying tower 2321 is communicated with the corresponding air duct 235, the discharge outlet of the first drying tower is communicated with the feed inlet of the second drying tower 2322, and the discharge outlet of the second drying tower 2322 is communicated with the feed inlet of the third drying tower 2323, so that the flocculent pulp sequentially passes through the first to

third drying towers

2321 and 2323 for drying treatment.

Further, two ends of the air duct 235 of the drying assembly 23 are respectively used for communicating the multiple sets of heat exchanger sets 231 and the drying towers 232 corresponding thereto. And the air pipe 235 corresponding to the drying tower 232 for drying the flocculent pulp first is communicated with the discharge hole of the defiberizing machine 22, so that the flocculent pulp enters the air pipe 235.

For example, drying assembly 23 includes a first ductwork 235a, a second ductwork 235b, and a third ductwork 235c, wherein the first ductwork 235a communicates with the feed inlets of the first heat exchanger 2311 and the first drying tower 2321. And the middle part of the first air pipe 235a is communicated with the discharge hole of the defiberizer 22. The second air duct 235b is communicated with the feed inlets of the second heat exchanger group 2312 and the second drying tower 2322, and the middle part of the second air duct 235b is communicated with the discharge outlet of the first drying tower 2321. The third air duct 235c communicates the feed inlets of the third heat exchanger 2313 and the third drying tower 2323.

With continued reference to fig. 5, the drying assembly 23 further includes a first condensate tank 233 and a second condensate tank 234. Each set 231 of heat exchanger sets includes at least a first heat exchanger, a second heat exchanger, and a third heat exchanger arranged in sequence along the direction of the airflow. The airflow direction is the flowing direction of the air to be heated, and the air with heating flows through the first heat exchanger, the second heat exchanger and the third heat exchanger in sequence. Among them, the first heat exchanger group 2311 includes a first heat exchanger 2311a, a second heat exchanger 2311b and a third heat exchanger 2311 c. The second heat exchanger group 2312 includes a first heat exchanger 2312a, a second heat exchanger 2312b and a third heat exchanger 2312 c. The third heat exchanger group 2313 includes a first heat exchanger 2313a, a second heat exchanger 2313b and a third heat exchanger 2313 c. The first steam is passed to the

third heat exchangers

2311c, 2312c, 2313c of the multi-bank heat exchanger bank 231. The condensed water generated by the

third heat exchangers

2311c, 2312c, 2313c of the plurality of sets of heat exchangers enters the first condensed water tank 233. Specifically, the first steam is introduced into the air inlets of the

third heat exchangers

2311c, 2312c and 2313c in the multiple heat exchanger sets 231, respectively, and the water outlets of the

third heat exchangers

2311c, 2312c and 2313c are communicated with the water inlet of the first condensed water tank 233. The condensed water generated after the heat exchange enters the first condensed water tank 233 from the water outlets of the

third heat exchangers

2311c, 2312c, and 2313c and the water inlet of the first condensed water tank 233.

The second steam is introduced into the

second heat exchangers

2311b, 2312b, 2313b of the plurality of heat exchanger groups 231 together with the steam generated from the first condensate tank 233, and the condensate water generated from the

second heat exchangers

2311b, 2312b, 2313b of the plurality of heat exchanger groups 231 is introduced into the second condensate tank 234. Specifically, the outlet port of the first condensed water tank 233 communicates with the inlet ports of the

second heat exchangers

2311b, 2312b, 2313b, and the second steam enters the

second heat exchangers

2311b, 2312b, 2313b together with the steam generated from the first condensed water tank 233 through the inlet ports of the

second heat exchangers

2311b, 2312b, 2313b so that the

second heat exchangers

2311b, 2312b, 2313b generate heat. The water outlets of the

second heat exchangers

2311b, 2312b and 2313b are communicated with the water inlet of the second condensate tank 234, and after heat exchange, the condensate water generated by the

second heat exchangers

2311b, 2312b and 2313b of the plurality of heat exchanger groups 231 enters the second condensate tank 234 through the water outlets of the

second heat exchangers

2311b, 2312b and 2313b and the water inlet of the second condensate tank 234.

The steam generated by the at least second condensate tank 234 is directed to the first heat exchangers 2311a, 2312a, 2313a of the multi-bank heat exchanger bank 231. Further, the second steam may be selectively directed to the first heat exchangers 2311a, 2312a, 2313a,. The second steam is passed to the first heat exchangers 2311a, 2312a, 2313a in the plurality of heat exchanger groups 231 together with the steam generated from the second condensate tank 234, if necessary.

In this embodiment, the pressure of the first vapor is greater than the pressure of the second vapor. For example, the first steam has a pressure of 16bar and the second steam has a pressure of 7.5 bar.

In the present embodiment, the temperature inside the first drying tower 2321 is higher than the temperature inside the second drying tower 2322 and the third drying tower 2323. The temperature in the first to third drying towers 2311-2323 can be adjusted by controlling the introduction amount of the drying air or controlling the temperature of the drying air in the first to third heat exchanger groups 2311-2313.

Referring to fig. 7, in the present embodiment, sensing devices 2351 are respectively inserted into the side walls of the multiple groups of air pipes 235, the sensing devices 2351 are partially inserted into the multiple groups of air pipes 235, and an included angle α between an insertion direction of the sensing device 2351 and an axial direction of the air pipe 235 is 30 ° to 60 ° in an air flow direction in the multiple groups of air pipes 235. By setting the angle range, the problem of slurry blockage and the like caused by the fact that flocculent slurry is hung on the sensing device 2351 in the process of flowing along with the air flow can be prevented, and meanwhile, the disturbance to the air flow can also be reduced. Optionally, sensor device 2351 is inserted at an angle α of 40-50 with respect to the axial direction of air conduit 235. Optionally, the insertion direction of sensing device 2351 is at an angle α of 45 ° to the axial direction of air conduit 235. Sensing device 2351 includes at least one of a thermometer, a manometer, and a hygrometer. In this embodiment, sensing devices 2351 are respectively inserted on the side walls of the multiple groups of air pipes 235, that is, the sensing devices 2351 are respectively inserted on the first air pipe 235a, the second air pipe 235b and the third air pipe 235 c. Of course, in other embodiments, a sensing device 2351 may be inserted into a portion of the air conduit 235.

With continued reference to fig. 5, optionally, the drying system further includes a cooling tower 236 and a scrubbing tower 237, wherein the cooling tower 236 is used for cooling the flocculent slurry separated by the cyclone 11, and the scrubbing tower 237 is used for scrubbing at least the gas exhausted from the plurality of sets of drying towers 232 and the cooling tower 236. In this embodiment, the inlet 11b of the cyclone 11 is connected to the outlet of the drying tower 232 which finally dries the flocculent pulp, for example, to the outlet of the third drying tower 2323. The flocculated slurry is separated from the wet air in the cyclone 11 and discharged from the outlet of the cyclone 11 to the cooling tower 236, and the wet air is discharged from the outlet 11a at the top of the cyclone 11 to the scrubbing tower 237. The air outlet of the first drying tower 2321, the air outlet of the second drying tower 2322 and the air outlet of the third drying tower 2323 are respectively communicated with the air inlet of the scrubbing tower 237, so that the exhausted gas is introduced into the scrubbing tower 237 for scrubbing and then is exhausted from the scrubbing tower 237, thereby reducing pollution. The flocculent pulp after passing through the cyclone separator 11 enters a plate press 30 to be pressed to form pulp blocks with uniform size, thickness and weight.

In this embodiment, the fluff pulp may be re-dried in the drying assembly 23 after exiting the cyclone 11, and then the cyclone 11 may again separate the wet air. The above process may be repeated for a plurality of times, for example, 3 times, and may be specifically performed according to actual production conditions.

In summary, in the embodiment of the cyclone separator and the embodiment of the pulp drying system of the present application, the plurality of side plates 1121 are sequentially connected to form the side wall of the second casing 112, which is different from a manner of using a large-area plate material in the prior art, so that the material cost can be reduced, an included angle β between the extending direction of the connecting line 1122 and the airflow direction inside the second casing 112 close to the side wall when the cyclone separator 11 is in operation is smaller than 25 °, so that the extending direction of the connecting line 1122 and the airflow direction of the side wall are consistent or substantially consistent, the interference to the airflow can be reduced even when there are many connecting lines 1122, and a good separation effect can be achieved on the basis of reducing the cost.

The above description is only for the purpose of illustrating embodiments of the present application and is not intended to limit the scope of the present application, and all modifications of equivalent structures and equivalent processes, which are made by the contents of the specification and the drawings of the present application or are directly or indirectly applied to other related technical fields, are also included in the scope of the present application.

Claims

1. A cyclone separator, comprising:

the cyclone separator comprises a first shell and a second shell, wherein the first shell is connected to the top of the second shell and is communicated with the second shell, a feed inlet is formed in the first shell, materials to be separated enter the first shell and the second shell through the feed inlet to form cyclone airflow, the second shell is arranged in an inverted cone shape, the second shell comprises a plurality of side plates arranged in a strip shape, the side plates are sequentially connected to form the side wall of the second shell, and an included angle formed between the extending direction of a connecting line formed by connecting the side plates and the airflow direction close to the inner wall in the second shell is smaller than 25 degrees when the cyclone separator works;

an air outlet is formed at the top of the first shell, and a discharge hole is formed at the bottom of the second shell; the cyclone separator is used for separating flocculent pulp from wet air, the separated wet air is discharged from the air outlet, and the separated flocculent pulp is discharged from the discharge hole.

2. The cyclone separator of claim 1, wherein: the side plates are welded in sequence along the connecting lines to form the side wall of the second shell, and at least part of the side plates are consistent in width and between 1m and 2 m.

3. The cyclone separator of claim 1, wherein: the second casing includes the end plate, connect in the same extending direction of polylith curb plate and be close to the tip of second casing bottom, just be closest in the polylith curb plate the side of the curb plate of second casing bottom with the side of end plate is connected, in order to form the lateral wall of second casing.

4. A pulp drying system, comprising:

the pre-drying section is used for pre-drying the slurry to obtain slurry blocks;

a flash drying section comprising a defibrator for defibering the pulp mass into a fluff pulp, a drying assembly for drying the fluff pulp to obtain a dried fluff pulp, and a cyclone for creating a cyclonic airflow to separate the dried fluff pulp from wet air;

5. The system of claim 4, wherein: the side plates are welded in sequence along the connecting lines to form the side wall of the second shell, and at least part of the side plates are consistent in width and between 1m and 2 m.

6. The system of claim 4, wherein: the second casing includes the end plate, connect in the same extending direction of polylith curb plate and be close to the tip of second casing bottom, just be closest to in the polylith curb plate the side of the curb plate of the bottom of second casing with the side of end plate is connected, in order to form the lateral wall of second casing.

7. The system of claim 4, wherein: the drying assembly comprises a plurality of groups of heat exchanger groups and a plurality of groups of drying towers, wherein each group of drying towers corresponds to one group of heat exchanger groups, air to be heated flows through the plurality of groups of heat exchanger groups respectively to become drying air, the drying air is led to the corresponding drying towers respectively, the flocculent pulp is dried by the plurality of groups of drying towers in sequence, the drying assembly comprises a first condensate water tank and a second condensate water tank, each group of heat exchanger groups at least comprises a first heat exchanger, a second heat exchanger and a third heat exchanger which are sequentially arranged along the flowing direction of the air to be heated, first steam is led to the third heat exchanger of the plurality of groups of heat exchanger groups, condensate water generated by the third heat exchanger of the plurality of groups of heat exchanger groups enters the first condensate water tank, and second steam and steam generated by the first condensate water tank are led to the second heat exchanger of the plurality of groups of heat exchanger groups together, condensed water generated by the second heat exchangers of the plurality of groups of heat exchanger groups enters the second condensed water tank, and steam generated by at least the second condensed water tank is led to the first heat exchangers of the plurality of groups of heat exchanger groups, wherein the pressure of the first steam is greater than that of the second steam.

8. The system of claim 7, wherein: the flash drying section comprises a plurality of groups of air pipes, the air pipes are respectively used for correspondingly communicating the heat exchangers and the drying towers corresponding to the heat exchangers, the middle part of the air pipe corresponding to the drying tower for drying the flocculent pulp firstly is communicated with a discharge hole of the defibrator so as to enable the flocculent pulp to enter the air pipes, sensing devices are respectively inserted on the side walls of the air pipes, the sensing devices are partially inserted into the air pipes, and the insertion direction of the sensing devices and the axial direction of the air pipes form 30-60 degrees in the air flow direction in the air pipes.

9. The system of claim 4, wherein: the pre-drying section comprises a pulp distributor and a pulp extruder, the pulp distributor is arranged at a feed inlet of the pulp extruder and is used for distributing the pulp to enter the pulp extruder, the pulp extruder is used for pre-drying the pulp to form pulp blocks, and the pulp blocks are discharged from a discharge outlet of the pulp extruder, wherein the pulp extruder comprises a first net, a second net, a first tensioning mechanism and a second tensioning mechanism, the first net and the second net are respectively supported by the first tensioning mechanism and the second tensioning mechanism, the first net and the second net are partially contacted to form a squeezing area, and a gap is formed between the first net and the second net at the feed inlet of the pulp extruder to receive the pulp and convey the pulp through rotation; the press roll comprises a plurality of pairs of press rolls, which are arranged in sequence from a feed inlet to a discharge outlet of the press roll, wherein one of the press rolls of each pair is arranged on one side of the first wire and the other press roll of each pair is arranged on one side of the second wire, so as to press the pulp between the first wire and the second wire to form the pulp cake.

10. The system of claim 9, wherein: the temperature of the slurry is 60-70 degrees, and/or the linear pressure between the pairs of press rolls is gradually increased from the feed inlet of the press master to the discharge outlet of the press master.