WO2023202421A1

WO2023202421A1 - Continuous reactor

Info

Publication number: WO2023202421A1
Application number: PCT/CN2023/087500
Authority: WO
Inventors: 邱志成; 贾振宇; 李鑫; 武术方; 李志勇; 金剑
Original assignee: 中国纺织科学研究院有限公司
Priority date: 2022-04-20
Filing date: 2023-04-11
Publication date: 2023-10-26
Also published as: CN114733469A; CN114733469B

Abstract

A continuous reactor for preparing polyester fibers, comprising: a reactor body (10) having at least two reaction chambers (11) disposed therein; a reaction slurry inlet (17), provided at a lower part of the reactor body (10) and in communication with a reaction chamber (11); a high-pressure injection apparatus, communicated with the slurry inlet (17) and used for spraying slurry into the reaction chamber (11), the slurry being sprayed into the reactor body (10) via the slurry inlet (17) by means of the high-pressure injection apparatus, and being quickly and uniformly mixed with material located inside the reactor body (10), thus avoiding agglomeration of particulate matter in the slurry.

Description

A continuous reaction kettle

Technical field

The invention belongs to the technical field of chemical equipment, and specifically relates to a continuous reaction kettle.

Background technique

At present, functional polyester fibers are generally prepared using the masterbatch method. The masterbatch method is to first melt and mix functional powder and carrier resin to obtain a functional masterbatch with high functional powder content, and then uniformly mix the functional masterbatch melt and the polyester melt for spinning in a continuous reaction kettle. The spinning process yields functional polyester fibers. Since in the process of preparing functional polyester fiber by masterbatch method, the dispersion of functional powder in high-viscosity polyester melt mainly relies on the mechanical shear force provided by the continuous reaction kettle, it is difficult to achieve the dispersion of functional powder in polyester. The high uniform dispersion in the melt makes the prepared functional polyester melt have poor spinning performance, making it difficult to spin fine or ultra-fine denier functional polyester fibers.

In order to solve the above technical problems, the existing technology has been improved and the functional powder is made into a slurry and then added to the continuous reaction kettle through online addition or other methods to mix with the polyester oligomer to improve the functional powder in the finished functional polyester. Related technologies for bulk dispersion performance. However, because functional powder slurries often use glycol monomers as solvents, when mixed with polyester oligomers, there is often a problem that excessive glycol monomers evaporate instantaneously at high temperatures, causing the functional powder to re-agglomerate. .

In view of this, the present invention is proposed.

Contents of the invention

The technical problem to be solved by the present invention is to overcome the shortcomings of the existing technology and provide a continuous reaction kettle. The slurry is injected into the kettle body through the slurry inlet by a high-pressure injection device, and is quickly and uniformly mixed with the materials located in the kettle body. During the mixing process, agglomeration between particulate matter in the slurry is effectively avoided.

In order to solve the above technical problems, the basic concept of the technical solution adopted by the present invention is:

A continuous reaction kettle, including:

The kettle body has at least two reaction chambers inside;

A slurry inlet is provided at the lower part of the kettle body and communicates with the reaction chamber;

A high-pressure injection device is connected to the slurry inlet and is used to inject slurry into the reaction chamber.

In the above solution, the slurry is injected into the kettle through the slurry inlet from the high-pressure injection device, and is quickly and evenly mixed with the materials located in the kettle. During the mixing process, agglomeration between particulate matter in the slurry is effectively avoided. By using the above-mentioned continuous reactor to produce polyester fiber, functional polyester oligomers with small dispersed particle sizes of functional powder can be obtained, which improves the spinning performance of functional polyester and is suitable for the production of high-quality fibers, films and other products.

In some embodiments, the high pressure injection device includes

An injection part is connected with the slurry inlet and is used to inject slurry into the reaction chamber;

A stirrer is provided in the reaction chamber, and the stirrer extends from the top to the bottom of the kettle body. There is an included angle A between the injection direction of the injection part and the extension direction of the stirrer, which satisfies 15 °≤A≤75°;

Preferably, the included angle A satisfies 30°≤A≤60°; more preferably, the included angle A satisfies 30°≤A≤45°.

In the above scheme, by setting the injection direction of the injection part to be inclined to the extension direction of the agitator, so that there is a certain angle between the two, the slurry is sprayed into this area, which is conducive to the continuous flow of the slurry. The materials in the reactor are dispersed to avoid agglomeration between particulate matter in the slurry.

In some embodiments, the agitator includes a stirring shaft and a stirring blade arranged on the stirring shaft, the spraying part is provided with a nozzle hole, and the distance between the nozzle hole and the edge of the stirring blade is d. The radius of the kettle body in the horizontal direction is r, satisfying r/2≤d≤r.

In the above scheme, the distance between the nozzle hole and the edge of the stirring blade is an area formed when the above conditions are met. The shear force of the stirring flow field is strong. Therefore, spraying the slurry into this area is conducive to the continuous flow of the slurry. The materials in the reactor are dispersed to avoid agglomeration between particulate matter in the slurry.

In some embodiments, the high pressure injection device further includes

A three-phase mixer, the three-phase mixer includes a cylinder with a high-pressure gas inlet, a solid-liquid slurry inlet and a slurry outlet;

The injection part is connected with the slurry inlet and the slurry outlet, and is used to inject the slurry in the three-phase mixer into the reaction chamber;

Preferably, the solid-liquid slurry inlet and the slurry outlet are located at both ends of the barrel, and the high-pressure gas inlet is located on the side wall of the barrel.

In the above scheme, the gas-liquid-solid three-phase slurry composed of solid-liquid slurry and high-pressure gas is sprayed into the reaction kettle by the injection part in the form of a high-pressure jet. During this process, the high-speed flowing slurry flows through the central area The lower pressure will force other materials in the reactor to flow to the central area to achieve rapid and even mixing; in addition, the high-pressure gas can also act as a turbulent flow during the injection process, thereby further dispersing the slurry efficiently and evenly. , greatly shortening the mixing time of materials. When producing polyester fiber products, it can solve the problem of functional powder re-agglomeration caused by the evaporation of excess glycol monomer in the functional powder slurry due to too long mixing time.

In some embodiments, the high-pressure gas inlet, solid-liquid slurry inlet and slurry outlet are respectively connected to a high-pressure gas supply pipe, a solid-liquid slurry supply pipe and a slurry discharge pipe;

The high-pressure gas supply pipe is provided with a pressure reducing valve, the three-phase mixer is provided with a pressure sensor, the pressure reducing valve and the The pressure sensors are all connected to a controller, and the controller controls the opening of the pressure reducing valve according to the pressure in the three-phase mixer detected by the pressure sensor.

Further, the injection part is a nozzle, the nozzle includes a nozzle head and a tubular structure, the nozzle head is provided with the nozzle hole;

The nozzle hole is connected to the slurry inlet; one end of the tubular structure is connected to the nozzle, and a flow channel communicated with the nozzle hole is formed inside. The side of the tubular structure close to the nozzle is connected to the nozzle. The slurry discharge pipe is connected;

Preferably, an adjustment valve is provided inside the tubular structure for adjusting the diameter of the nozzle hole.

In some embodiments, it also includes

The shell is set on the outside of the kettle body and is formed by at least two vertical cylindrical shells connected in parallel in the horizontal direction. The connection between two adjacent shells is in the direction toward the outside of the continuous reaction kettle. It has an included angle α, satisfying 30°≤α≤90°.

In the above scheme, at least two vertical cylindrical structure shells are connected side by side in the horizontal direction, so that the inside of the shell can accommodate a kettle body with multiple reaction chambers, and two adjacent vertical cylindrical shells can be accommodated. The angle between the shell connections of the cylindrical structure is controlled within the above range, which can minimize the stirring flow field velocity stagnation zone formed in each reaction chamber.

In some embodiments, the housing includes an upper head and a lower head, which are located at the top and bottom of the kettle body respectively. The slurry inlet is provided on the bottom wall of the kettle body, and the injection part is provided with The lower head is connected to the slurry inlet at a position opposite to the slurry inlet;

Preferably, the upper head and the lower head are at least one of an elliptical head, a spherical head, and a butterfly head respectively.

In some embodiments, the kettle body is provided with partitions extending upward from the bottom wall of the kettle body, and the partition walls separate the kettle body into multiple units arranged side by side and connected to each other. The reaction chamber has a gap between the partition plate and the top wall of the kettle body, and the gap gradually increases toward the direction of the material outlet of the kettle body;

Preferably, the height of the partition is 1/4 to 3/5 of the height of the kettle body.

In the above scheme, by controlling the height of the partition to 1/4 to 3/5 of the height of the kettle, enough gas phase space can be left for each reaction chamber in the kettle to avoid steam generated in the kettle causing The phenomenon of gas phase entrainment in materials. At the same time, it also avoids that when the height of the partition is designed to be too high, the material cannot flow smoothly into the next adjacent reaction chamber. When the height of the partition is designed to be too low, it is easy for the material to fail to occur in the reaction chamber at a specific temperature. After the reaction is complete, it immediately flows into the next adjacent reaction chamber, resulting in a reduction in the accuracy of the reaction.

In addition, the above solution sets the gap to gradually increase in the direction closer to the discharge port, that is, the height of the partition is limited to gradually decrease in the direction closer to the discharge port, so that the materials entering the kettle can smoothly Through the top of the partition between each reaction chamber, it flows sequentially from the reaction chamber connected to the second feed port to the reaction chamber connected to the discharge port, effectively reducing short circuit and back-mixing of materials in the kettle, and enabling precise control of the reaction. Degree.

In some embodiments, each of the reaction chambers is provided with a heating device, and the heating device is provided with a temperature adjustment component for adjusting the temperature in each of the reaction chambers;

Preferably, the heating device is a heat medium coil, and the temperature adjustment component is a heat medium flow regulating valve provided at the outlet of the heat medium coil.

In the above scheme, by adjusting the opening of the heat medium flow regulating valve, the temperature of each reaction chamber in the kettle can be accurately controlled. When producing polyester fiber, the low temperature of the slurry and the materials in the continuous reaction kettle can be accurately and independently controlled. Efficient mixing process and high-temperature evaporation removal process of excess glycol monomer as slurry carrier.

In some embodiments, the continuous reaction kettle further includes a material inlet and a material outlet, which are provided on the kettle body and are respectively connected to the reaction chambers located at both ends of the kettle body.

When the continuous reactor is producing polyester fiber, the material inlet is a polyester oligomer inlet, the solid-liquid slurry inlet is a functional powder slurry inlet, and the high-pressure gas inlet is a high-pressure nitrogen inlet.

After adopting the above technical solution, the present invention has the following beneficial effects compared with the existing technology:

In the continuous reaction kettle provided by the present invention, the slurry is sprayed into the kettle body through the slurry inlet by a high-pressure injection device, and is quickly and evenly mixed with the materials located in the kettle body. During the mixing process, the particles in the slurry are effectively avoided. of reunion. By using the above-mentioned continuous reactor to produce polyester fiber, functional polyester oligomers with small dispersed particle sizes of functional powder can be obtained, which improves the spinning performance of functional polyester and is suitable for the production of high-quality fibers, films and other products.

The continuous reaction kettle provided by the present invention can leave a large enough gas phase space for each reaction chamber in the kettle body by controlling the height of the partition to 1/4 to 3/5 of the height of the kettle body, thereby avoiding the gas phase generated in the kettle body. Steam causes gas phase entrainment of materials. At the same time, it also avoids that when the height of the partition is designed to be too high, the material cannot flow smoothly into the next adjacent reaction chamber. When the height of the partition is designed to be too low, it is easy for the material to fail to occur in the reaction chamber at a specific temperature. After the reaction is complete, it immediately flows into the next adjacent reaction chamber, resulting in a reduction in the accuracy of the reaction. In addition, by setting the gap to gradually increase in the direction closer to the discharge port, that is, the height of the partition is limited to gradually decrease in the direction closer to the discharge port, so that the materials entering the kettle can smoothly pass through each The top of the partition between the reaction chambers sequentially flows from the reaction chamber connected to the second feed port to the reaction chamber connected to the discharge port, effectively reducing short circuit and back-mixing of materials in the kettle, and enabling precise control of the degree of reaction. .

The continuous reaction kettle provided by the present invention connects at least two vertical cylindrical shells in parallel in the horizontal direction, so that the inside of the shell can accommodate a kettle body with multiple reaction chambers, and connects two adjacent ones. The angle between the shell connections of the two vertical cylindrical structures is controlled within the above range, which can minimize the stirring flow field velocity stagnation zone formed in each reaction chamber.

Specific embodiments of the present invention will be described in further detail below with reference to the accompanying drawings.

Description of drawings

The drawings, as part of the present invention, are used to provide a further understanding of the present invention. The schematic embodiments of the present invention and their descriptions are used to explain the present invention, but do not constitute an improper limitation of the present invention. Obviously, the drawings in the following description are only some embodiments. For those of ordinary skill in the art, other drawings can be obtained based on these drawings without exerting creative efforts. In the attached picture:

Figure 1 is a schematic structural diagram of a structure of a continuous reactor of the present invention.

Figure 2 is a schematic structural diagram of another structure of the continuous reaction kettle of the present invention.

Figure 3 is a top view of a structure of the continuous reactor of the present invention.

Figure 4 is a schematic structural diagram of the high-pressure injection device of the present invention.

Figure 5 is a side view of the guide tube in the mixer of the present invention.

Figure 6 is a top view of the guide tube in the mixer of the present invention.

In the picture: 10. Kettle body; 11. Reaction chamber; 12. Shell; 13. Partition plate; 131. Fixed part; 132. Movable part; 14. Heat medium coil; 15. Material inlet; 16. Material outlet ; 17. Slurry inlet; 18. Gas phase outlet; 19. Agitator interface; 191. Axial flow agitator interface; 192. Radial flow agitator interface; 21. Three-phase mixer; 211. High-pressure gas inlet; 212. Solid-liquid slurry inlet; 213, slurry outlet; 22, high-pressure gas supply pipe; 23, solid-liquid slurry supply pipe; 24, slurry discharge pipe; 25, pressure reducing valve; 26, pressure sensor; 27, stirrer ; 271. Radial flow mixer; 272. Axial flow mixer; 273. Guide tube; 274. Guide hole; 275. Baffle; 28. Stirring shaft; 29. Mixing blade; 30. Nozzle; 31. Nozzle ; 32. Nozzle hole; 33. Tubular structure; 34. Regulating valve; 100. Continuous reaction kettle.

It should be noted that these drawings and text descriptions are not intended to limit the scope of the invention in any way, but are intended to illustrate the concept of the invention for those skilled in the art by referring to specific embodiments.

Detailed ways

In order to make the purpose, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention will be clearly and completely described below in conjunction with the drawings in the embodiments of the present invention. The following examples are used to illustrate the present invention. , but are not used to limit the scope of the present invention.

In the description of the present invention, it should be noted that the terms "upper", "lower", "front", "back", "left", "right", "vertical", "inner", "outer", etc. The indicated orientation or positional relationship is based on the orientation or positional relationship shown in the drawings. It is only for the convenience of describing the present invention and simplifying the description. It does not indicate or imply that the device or element referred to must have a specific orientation or a specific orientation. construction and operation, and therefore should not be construed as limitations of the invention.

In the description of the present invention, it should be noted that, unless otherwise clearly stated and limited, the terms "installation", "connection" and "connection" should be understood in a broad sense. For example, it can be a fixed connection or a detachable connection. to connect, or to connect in one piece; can It can be a mechanical connection or an electrical connection; it can be a direct connection or an indirect connection through an intermediate medium. For those of ordinary skill in the art, the specific meanings of the above terms in the present invention can be understood on a case-by-case basis.

In addition, the terms “first” and “second” are used for descriptive purposes only and cannot be understood as indicating or implying relative importance or implicitly indicating the quantity of indicated technical features. Therefore, features defined as "first" and "second" may explicitly or implicitly include one or more of these features. In the description of the present invention, "plurality" means at least two, such as two, three, etc., unless otherwise expressly and specifically limited.

As shown in Figures 1 to 6, a continuous reaction kettle includes: a kettle body 10, with at least two reaction chambers 11 provided inside; a slurry inlet 17, which is provided at the lower position of the kettle body 10, and is connected with the kettle body 10. The reaction chamber 11 is connected; a high-pressure injection device is connected with the slurry inlet 17 for injecting slurry into the reaction chamber 11 .

When producing polyester fibers, functional powder slurries often use glycol monomers as solvents. When mixed with polyester oligomers, there is often an excess of glycol monomers that instantly evaporates at high temperatures, resulting in functional powder. The existing online addition method cannot fully and evenly mix the functional powder slurry and polyester oligomer quickly. Therefore, in the above solution, the slurry is injected into the kettle body 10 through the slurry inlet 17 by the high-pressure injection device, and is quickly and evenly mixed with the materials located in the kettle body 10. During the mixing process, particles in the slurry are effectively avoided. Reunion between substances. By using the above-mentioned continuous reactor 100 to produce polyester fiber, functional polyester oligomers with small dispersed particle sizes of functional powder can be obtained, which improves the spinning performance of functional polyester and is suitable for the production of high-quality fibers, films and other products.

It should be noted that each reaction chamber can be provided with a slurry inlet, or only one reaction chamber can be provided with a slurry inlet. The specific number of slurry inlets can be reasonably adjusted according to actual production needs.

In some embodiments, as shown in Figure 1, the high pressure injection device includes

In some embodiments, the stirrer 27 is any one of an axial flow stirrer 27 , a radial flow stirrer 27 , or a combination stirrer 27 of an axial flow stirrer and a radial flow stirrer.

Depending on the reaction process undertaken by each reaction chamber 11 in the kettle body 10, each reaction chamber 11 can choose different forms. The stirrer 27, in which the reaction chamber 11 of adding functional powder slurry is preferably a stirrer 27 composed of a high-shear radial flow stirrer in the lower layer and a strong circulation axial flow stirrer in the upper layer, so as to facilitate the mixing of functional powder. The reaction chamber 11 used as a slurry carrier for high-temperature evaporation and removal of excess glycol monomer is preferably a strong circulation axial flow stirrer 27 to facilitate the evaporation and removal of glycol monomer. Each reaction chamber 11 in the kettle body 10 can use different forms of stirrers 27 according to different functional partitions, which can be equivalent to several reactors connected in series, greatly shortening the process flow, reducing investment costs and operating costs, and improving the reaction efficiency.

In some embodiments, the top wall of the reaction kettle is provided with a gas phase outlet 18 and a stirrer interface 19. The gas phase outlet 18 is used to discharge the gas generated during the reaction, and the stirrer interface 19 is used to connect the Blender.

In some embodiments, the agitator 27 includes a stirring shaft 28 and a stirring blade 29 provided on the stirring shaft 28. The spraying part is provided with a nozzle hole 32, and the nozzle hole 32 is connected with the stirring blade. The distance between the edges of 29 is d, and the radius of the kettle body 10 in the horizontal direction is r, satisfying r/2≤d≤r.

Due to the low fluidity of the liquid, effective mixing cannot be achieved using a high-pressure injection device. Therefore, in the above scheme, through the use of the high-pressure injection device and the stirrer 27, the distance between the nozzle hole 32 and the edge of the stirring blade 29 is formed under the above conditions, and the stirring flow field shear force is strong. Therefore, spraying the functional powder slurry into this area is beneficial to the dispersion of the functional powder slurry in the polyester oligomer and avoids re-agglomeration of the functional powder slurry.

Preferably, the distance between the nozzle hole 32 on the nozzle head 31 and the lower edge of the stirring blade 29 on the side away from the stirring shaft 28 is d1, which satisfies r/2≤d1≤r; preferably, r/ 2≤d1≤3r/4.

In some embodiments, as shown in Figures 1 and 4, the high pressure injection device includes

Three-phase mixer 21. The three-phase mixer 21 includes a cylinder with a high-pressure gas inlet 211, a solid-liquid slurry inlet 212 and a slurry outlet 213;

The injection part is connected with the slurry inlet 17 and the slurry outlet 213, and is used to inject the slurry in the three-phase mixer 21 into the reaction chamber 11;

Preferably, the solid-liquid slurry inlet 212 and the slurry outlet 213 are located at both ends of the cylinder, and the high-pressure gas inlet 211 is located on the side wall of the cylinder.

In the above scheme, the gas-liquid-solid three-phase slurry composed of solid-liquid slurry and high-pressure gas is sprayed into the reaction kettle by the injection part in the form of a high-pressure jet. In the process, an entrainment effect is generated, and the high-speed flowing slurry The low pressure in the central area flowing through will force other materials in the reactor to flow to the central area to achieve rapid and even mixing; in addition, the high-pressure gas can also act as a turbulent flow during the injection process, thereby making the slurry Further efficient and uniform dispersion greatly shortens the mixing time of materials. When producing polyester fiber products, it can solve the problem of functional powder re-agglomeration caused by the evaporation of excess glycol monomer in the functional powder slurry due to too long mixing time.

Preferably, the barrel has a cylindrical structure.

In some embodiments, as shown in Figure 4, the high-pressure gas inlet 211, the solid-liquid slurry inlet 212 and the slurry outlet 213 are respectively connected with the high-pressure gas supply pipe 22, the solid-liquid slurry supply pipe 23 and the slurry discharge pipe. 24 connected;

The high-pressure gas supply pipe 22 is provided with a pressure reducing valve 25, and the three-phase mixer 21 is provided with a pressure sensor 26. Both the pressure reducing valve 25 and the pressure sensor 26 are connected to a controller, and the controller is configured according to The pressure sensor 26 detects the pressure in the three-phase mixer 21 and controls the opening of the pressure reducing valve 25 .

The opening of the pressure reducing valve can control the supply of high-pressure gas from the high-pressure gas supply pipe to the three-phase mixer. When the pressure sensor detects that the pressure in the three-phase mixer is small, the controller controls the opening of the pressure reducing valve to increase. When the pressure sensor detects that the pressure in the three-phase mixer is relatively large, the controller controls the opening of the pressure reducing valve to decrease.

Preferably, the pressure range in the three-phase mixer 21 is controlled to be 8 to 50 bar.

In some embodiments, the spray part is a nozzle 30. The nozzle 30 includes a nozzle head 31 and a tubular structure 33. The nozzle head 31 is provided with the nozzle hole 32;

The nozzle hole 32 is connected to the slurry inlet 17; one end of the tubular structure 33 is connected to the nozzle 31, and a flow channel communicated with the nozzle hole 32 is formed inside. The tubular structure 33 is close to the nozzle hole 32. The side part of the nozzle 31 is connected with the slurry discharge pipe 24;

The slurry in the three-phase mixer is squeezed into the tubular structure along the slurry discharge pipe, and then sprayed from the nozzle hole into the reaction chamber in the kettle body.

Preferably, an adjustment valve 34 is provided inside the tubular structure 33 for adjusting the diameter of the nozzle hole 32 .

Specifically, the regulating valve includes a valve stem and a control hand plate. The valve stem is sleeved inside the tubular structure. The control hand plate is connected to the valve stem. By rotating the control hand plate, the valve stem spirals forward or spirals along the tubular structure. Move backward to adjust the size of the nozzle hole.

In some embodiments, the nozzle 31 has a cone-shaped structure, and the nozzle hole 32 is provided in a tip area of the cone-shaped structure.

The diameter of the nozzle 31 gradually becomes smaller, so the pressure gradually increases, and the material will be ejected from the nozzle hole 32 of the nozzle 31 to form a jet flow, so that the material is mixed evenly again.

In some embodiments, as shown in Figures 1 and 2, it also includes a shell, which is set on the outside of the kettle body 10 and is formed by at least two vertical cylindrical structure shells 12 connected in parallel in the horizontal direction. The connection between two adjacent shells 12 has an included angle α in the direction toward the outside of the continuous reaction kettle 100, satisfying 30°≤α≤90°. Preferably, 45°≤α≤60° is satisfied.

In the above solution, as shown in Figures 1 and 3, at least two vertical cylindrical structure housings 12 are connected and arranged in parallel in the horizontal direction, so that the inside of the housing 12 can accommodate multiple reaction chambers 11 The cauldron body 10, and two adjacent The included angle at the connection point of the two vertical cylindrical structure shells 12 is controlled within the above range, which can minimize the stirring flow field velocity retention zone formed in each reaction chamber 11 .

In some embodiments, the housing 12 includes an upper head and a lower head, which are located at the top and bottom of the kettle body 10 respectively. The slurry inlet 17 is provided on the bottom wall of the kettle body 10, so The injection part is arranged at a position opposite the lower head and the slurry inlet 17, and is connected with the slurry inlet 17;

As shown in Figures 1 and 2, the two shells located at the end of the continuous reaction kettle are composed of an upper head, a lower head and one side wall, while the shell located inside the continuous reaction kettle is only composed of an upper head and a side wall. It is composed of a lower head, which can save production costs.

In some embodiments, the height of the upper head and the lower head is configured to be 1/6 to 1 of the radius of the kettle body 10 in the horizontal direction. The velocity retention area of the stirring flow field in each reaction chamber 11 in the kettle body 10 can be further reduced.

In some embodiments, the injection nozzle 30 of the high-pressure injection device is installed at the lower head near the partition 13 .

In the above solution, compared with the area between the nozzle hole 32 and the edge of the stirring blade 29 toward the bottom wall of the kettle body 10, the distance between the nozzle hole 32 and the lower edge of the stirring blade 29 away from the stirring shaft 28 is The area formed under the above conditions has stronger stirring flow field shear force. Injecting the functional powder slurry into this area is more conducive to the dispersion of the functional powder slurry in the polyester oligomer and can make it more efficient. Avoid re-agglomeration of functional powder slurry to the greatest extent.

In some embodiments, as shown in FIG. 1 , a partition 13 is provided in the kettle body 10 . The partition 13 extends upward from the bottom wall of the kettle body 10 . The partition 13 connects the The interior of the kettle body 10 is divided into a plurality of reaction chambers 11 arranged side by side and connected with each other. There is a gap between the partition plate 13 and the top wall of the kettle body 10 , and the gap is toward the material outlet 16 The direction gradually increases;

Preferably, the height of the partition plate 13 is 1/4 to 3/5 of the height of the kettle body 10 .

In the above solution, by controlling the height of the partition 13 to 1/4 to 3/5 of the height of the kettle body 10, a sufficiently large gas phase space can be left for each reaction chamber 11 in the kettle body 10 to avoid the risk of the kettle body The glycol vapor generated within 10 days causes gas phase entrainment of polyester materials. At the same time, it is also avoided that when the height of the partition 13 is designed to be too high, the material cannot flow smoothly into the next adjacent reaction chamber 11, and when the height of the partition 13 is designed to be too low, it is easy for the material to react at a specific temperature. If sufficient reaction does not occur in the chamber 11, it immediately flows into the next adjacent reaction chamber 11, resulting in a reduction in the accuracy of the reaction.

In addition, the above solution sets the gap to gradually increase in the direction closer to the discharge port, that is, the height of the partition plate 13 is limited to gradually decrease in the direction closer to the discharge port, so that the gap entering the kettle body 10 can be gradually reduced. Materials can smoothly pass through the top of the partition 13 between each reaction chamber 11 and flow into the reaction chamber 11 connected to the outlet in sequence from the reaction chamber 11 connected to the second feed port, effectively reducing the leakage of materials in the kettle body 10 Short circuit and back-mixing can precisely control the degree of reaction.

Preferably, the gap between the partition 13 and the top wall of the reactor is adjustable.

The above solution can control the amount of reactants in each reaction chamber by adjusting the height of the partition, and avoids the problem of countercurrent flow of reactants in the existing reactor and the inability to carry out multiple reaction stages simultaneously.

In any of the above embodiments, as shown in Figure 2, the partition 13 includes:

The fixed part 131 is connected to the bottom of the reactor, extends upward from the connection, and is used to position the movable part 132;

The movable part 132 is movably connected to the fixed part 131 and is used to expand and contract along the extension direction of the fixed part 131 to adjust the size of the gap between the partition plate 13 and the reaction kettle.

The fixed part 131 includes two fixed plates that are parallel to each other and spaced apart. The two fixed plates are connected to the bottom wall of the reactor to form positioning grooves for positioning the movable part. The movable part 132 is movably connected to the fixed part through the positioning grooves. ; The above solution avoids the shaking and displacement of the partition during the adjustment process, which will cause changes in the capacity of the reaction chambers on adjacent sides and thus affect the normal progress of the reaction.

In some embodiments, the fixed part 131 is two fixed plates arranged parallel to each other and spaced apart, and the two fixed plates form positioning grooves for positioning the movable part;

The movable part 132 is movably connected to the fixed part 131 through the positioning groove.

In some embodiments, the movable portion 132 includes,

The movable plate is at least partially accommodated in the positioning groove and is movably connected to the fixed part;

A driving rod passes through the reaction kettle and is connected to the movable plate along the expansion and contraction direction of the movable plate;

The driving part is transmission connected with the driving rod, and drives the movable plate through the driving rod to realize telescopic movement.

In the above scheme, the driving rod can be arranged to be connected to the bottom of the movable plate, extend downward from the bottom of the movable plate and penetrate the bottom wall of the reaction kettle to be drivingly connected to the driving part provided at the bottom of the reaction chamber; it can also be arranged to be connected to the bottom of the movable plate. The top is connected, extends upward from the top of the movable plate, runs through the top wall of the reaction kettle, and is drivingly connected to the driving part provided on the top of the reaction chamber.

Specifically, the driving rod has threads, and the driving part can be a driving motor that automatically controls the movement of the movable plate through the driving rod, or it can be a handwheel used to realize manual control of the movable plate.

In the above solution, the driving part is a driving motor, which realizes remote automatic control of the movable plate, reduces labor costs, and can more easily realize real-time control of the movable plate; the driving part is a handwheel, which provides another option for technicians. When automatic control fails or special circumstances occur, emergency control of the movable board can be achieved by manually controlling the movement of the movable board.

Furthermore, in order to improve the accuracy of manual control by technicians, a ruler corresponding to the size of the gap between the top of the movable plate and the top wall of the reactor is provided on the drive rod, which improves the accuracy of manual control by technicians; at the same time, in order to avoid technical errors If the operator makes a mistake, the movable plate is lifted out of the fixed part, and a limit part is provided on the drive rod to limit the movement range of the movable plate.

In any of the above embodiments, as shown in Figure 2, the stirrer 27 includes a radial flow stirrer 271, which is located inside the reaction chamber 11 and has a stirring shaft and stirring blades for driving the reactants along the radial flow. flow in the direction; the guide tube 273 is fixedly connected to the reaction chamber 11. The inside of the guide tube 273 is hollow to form a cavity for accommodating the radial flow agitator 271. The wall of the cavity is provided with a guide tube. Hole 274; the radial flow stirrer is located inside the cavity. When the radial flow stirrer stirs, the reactants inside the cavity are pushed to be sprayed to the outside of the cavity through the guide hole.

The radial flow agitator drives the reactants inside the shear injection mechanism to be sprayed to the outside through the shear injection mechanism. The reactants are affected by the shear force during the high-speed injection process, thereby avoiding the agglomeration of functional powders in the reactants and achieving The functional powder is fully dispersed in the reactants.

A radial flow agitator interface 192 is provided at the bottom of the kettle body for connecting the radial flow agitator 271 .

Specifically, the guide tube 273 has a hollow cylindrical structure, with openings at both ends in the axial direction, is coaxially arranged with the radial flow agitator 271, and is sleeved on the radial flow agitator. 271 outside, with a gap between it and the stirring blade;

In some embodiments, the flow guide tube is provided with a flow guide area, and the reactants located inside the flow guide tube are sprayed from the flow guide area to the outside of the flow guide tube.

Preferably, the radius of the guide tube is 1/4 to 3/5 of the radius of the reaction chamber.

Further, the flow guide area is opposite to the end of the mixing blade and has guide holes arranged along the circumferential direction of the guide tube.

In the above scheme, the reactants are mixed with functional powder, and when the radial flow stirrer drives the reactants to flow in the radial direction, part of the reactants flows out from the guide holes on the guide tube. The area is reduced, and the reactants passing through the guide hole can be ejected from the inside of the guide tube to the outside at a high speed, and are subjected to shear force under the high-speed flow state, so that the agglomerated functional powder can be dispersed to achieve the function Uniform dispersion of powder; part of the reactants that do not flow out from the guide hole collides with the guide tube, which can also break up the agglomeration of functional powder, thereby achieving full dispersion and uniform mixing of functional powder.

Further, the high-shear reaction kettle also includes a driving part, which is drivingly connected to the radial flow agitator and used to drive the radial flow agitator to rotate.

Further, the length of the flow guide area along the axial direction of the flow guide tube is greater than the width of the mixing blade, and there is a length along the guide tube. Multiple rows of guide holes arranged in the axial direction.

Since the length of the guide area along the axial direction of the guide tube is greater than the width of the stirring blade, the reactants can be sprayed from the inside of the guide tube to the outside more quickly driven by the stirring blades, which improves the separation of functional powders in the reactants. Dispersed efficiency.

In some embodiments, as shown in FIGS. 5 and 6 , a baffle 275 is fixedly provided on the inner wall of the flow guide tube 273 ; the baffle 275 extends along the axial and radial directions of the flow guide tube 273 Extend respectively, the baffle 275 is located on one side of the mixing blade in the axial direction of the guide tube 273, and the length in the radial direction of the guide tube 273 is greater than the inner wall of the guide tube 273 and the mixing blade. the gap between the ends;

During the rotation of the radial flow mixer, the reactants are driven to move circumferentially along the guide tube. When passing through the baffle, the reactants are affected by shear force, which can further avoid agglomeration between functional powders and make the reactants mixed Functional powder is dispersed more evenly.

Specifically, the plane where the baffle is located is parallel to the axis of the guide tube, and the length along the radial direction of the guide tube is greater than the gap between the guide tube and the end of the mixing blade, and the radial flow is During the rotation of the agitator, the reactants are driven to move circumferentially along the guide tube. When passing through the baffle, the reactants are affected by shear force, which can further avoid agglomeration between functional powders and make the functional powders mixed in the reactants Dispersed more evenly.

Preferably, the baffle is coplanar with the axis of the guide tube.

On the basis of the above solution, in order to further improve the dispersion uniformity of the functional powder in the reactant, multiple baffles are installed in the axial direction of the guide tube opposite to the position of the stirring blades of the radial flow mixer, and the baffles are The plates are arranged in pairs on the upper and lower sides of the radial flow agitator in the axial direction, and the baffles located on the upper and lower sides of the radial flow agitator are arranged symmetrically, with the same spacing between the radial flow agitators, so that the radial flow agitator When the agitator passes through the baffle, it applies shear force to the reactants in multiple directions around the radial flow agitator, which can more fully avoid agglomeration between functional powders and improve the concentration of functional powders in the reactants. Dispersion uniformity.

Preferably, the gap between the baffle and the radial flow agitator is 5-50 mm.

The axis of the baffle and the guide tube is coplanar, so that the baffle can fully block the reactants that approach the baffle driven by the stirring blade, thereby increasing the reaction volume between the stirring blade and the baffle when the stirring blade passes through the baffle. The shear force received can more fully realize the dispersion of the functional powder in the reactant and effectively reduce the agglomeration of the functional powder.

Further, a plurality of baffles are provided along the circumferential direction of the guide tube opposite to the position of the stirring blades of the radial flow agitator;

The baffles are provided on both sides of the mixing blade along the axial direction of the guide tube, and the baffles located on both sides of the mixing blade Symmetrical setup.

Preferably, the number of stirring blades of the radial flow stirrer is 3-8.

In the above scheme, when the radial flow stirrer passes through the baffle, the baffle and the guide tube can cooperate with the radial flow stirrer to exert shear force on the reactants in multiple directions around the radial flow stirrer, which can more fully It can avoid agglomeration between functional powders and improve the uniformity of dispersion of functional powders in reactants.

In some embodiments, in the axial direction of the guide tube, there is a gap between one end of the baffle close to the stirring blade and the stirring blade;

Preferably, the gap between the end of the baffle close to the stirring blade and the stirring blade is 5-50 mm.

In some embodiments, the stirrer 27 further includes an axial flow stirrer 272, which is provided in the reaction kettle and used to guide the reactants to flow along the axial direction toward the radial flow stirrer 271.

An axial flow stirrer interface 191 is provided on the top of the kettle body for connecting the axial flow stirrer 272.

Further, the axial flow agitator 272 is coaxially arranged with the radial flow agitator 271 and driven coaxially or off-axis with the radial flow agitator 271 .

Specifically: when the radial flow agitator and the axial flow agitator are driven coaxially, the radial flow agitator and the axial flow agitator are drivingly connected to the first driving part through the same driving shaft, that is, the radial flow agitator and the shaft The flow mixer rotates at the same speed.

When the radial flow stirrer and the axial flow stirrer are driven off-axis, a second driving part for driving the axial flow stirrer is also provided outside the reaction kettle. The first driving part and the second driving part pass through the transmission shaft and the radial flow stirrer respectively. Flow mixer and axial flow mixer drive connection.

In the above scheme, when the radial flow stirrer and the axial flow stirrer are driven off-axis, in order to facilitate installation and maintenance, the first driving part and the second driving part are respectively located at the top and bottom of the reaction kettle; technicians can Control the rotation speed of the radial flow mixer and the axial flow mixer according to the actual production and manufacturing needs to control the mixing degree of the reactants and the dispersion degree of the functional powder to adapt to different production needs and different production process needs.

In any of the above embodiments, a heating device is provided in each of the reaction chambers, and a temperature adjustment component is provided on the heating device for adjusting the temperature in each of the reaction chambers;

Preferably, the heating device is a heat medium coil 14 , and the temperature adjustment component is a heat medium flow regulating valve 34 provided at the outlet of the heat medium coil 14 .

In the above scheme, by adjusting the opening of the heat medium flow regulating valve 34, the temperature of each reaction chamber 11 in the kettle 10 can be accurately controlled, thereby achieving precise and independent control of the low temperature of the functional powder slurry and polyester oligomer. Efficient mixing process and high-temperature evaporation removal process of excess glycol monomer as slurry carrier.

It can be understood that the temperature in each reaction chamber can be individually controlled according to different process conditions.

In some embodiments, the continuous reaction kettle further includes a material inlet 15 and a material outlet 16, which are provided on the kettle body 10 and are respectively connected to the reaction chambers 11 located at both ends of the kettle body 10.

When the continuous reactor is producing polyester fiber, the material inlet 15 is a polyester oligomer inlet, the solid-liquid slurry inlet 212 is a functional powder slurry inlet 17, and the high-pressure gas inlet 211 is a high-pressure gas inlet. Nitrogen import.

When using the existing online addition method to add the functional powder slurry to the continuous reaction kettle 100 and the polyester oligomer in the continuous reaction kettle 100, excessive glycol monomers in the functional powder slurry often appear. Instantaneous evaporation at high temperatures leads to the problem of re-agglomeration of functional powders. Therefore, in the present invention, the functional powder slurry is injected into the kettle body 10 through the slurry inlet 17 from the high-pressure injection device, causing a certain disturbance to the polyester oligomers inside the kettle body 10, thereby realizing the interaction between the functional powder slurry and the polyester slurry. The oligomers are quickly and uniformly mixed, effectively avoiding agglomeration between functional powders, and obtaining functional polyester oligomers with small dispersed particle sizes of functional powders, which not only shortens the reaction time, improves the production efficiency of functional polyester, It improves the performance of functional polyester products and also improves the spinning performance of functional polyester, making it suitable for the production of high-quality fibers and films.

It should be noted that when there are two reaction chambers in the kettle, the material inlet and the material outlet are connected to each reaction chamber respectively, and the two slurry inlets are also connected to each reaction chamber respectively; when there are three reaction chambers in the kettle, When using the above reaction chamber, the material inlet and material outlet are respectively connected with the reaction chambers located at both ends of the kettle body, and more than three slurry inlets are connected with each reaction chamber respectively.

Preferably, the material inlet, material outlet and slurry inlet are all arranged at the bottom of the kettle body.

The above are only preferred embodiments of the present invention, and do not limit the present invention in any form. Although the present invention has been disclosed above in preferred embodiments, it is not intended to limit the present invention. Anyone familiar with the technology of this patent Without departing from the scope of the technical solution of the present invention, personnel can make some changes or modify the above-mentioned technical contents into equivalent embodiments with equivalent changes. In essence, any simple modifications, equivalent changes and modifications made to the above embodiments still fall within the scope of the present invention.

Claims

A continuous reaction kettle, characterized by including:

The kettle body has at least two reaction chambers inside;

A slurry inlet is provided at the lower part of the kettle body and communicates with the reaction chamber;

A high-pressure injection device is connected to the slurry inlet and is used to inject slurry into the reaction chamber.
A continuous reaction kettle according to claim 1, characterized in that: the high-pressure injection device includes

An injection part is connected with the slurry inlet and is used to inject slurry into the reaction chamber;

A stirrer is provided in the reaction chamber, and the stirrer extends from the top to the bottom of the kettle body. There is an included angle A between the injection direction of the injection part and the extension direction of the stirrer, which satisfies 15 °≤A≤75°.
A continuous reaction kettle according to claim 2, characterized in that the included angle A satisfies 30°≤A≤60°.
A continuous reaction kettle according to claim 3, characterized in that the included angle A satisfies 30°≤A≤45°.
A continuous reaction kettle according to claim 2, characterized in that:

The agitator includes a stirring shaft and a stirring blade arranged on the stirring shaft. The spraying part is provided with a nozzle hole. The distance between the nozzle hole and the edge of the stirring blade is d. The kettle body The radius in the horizontal direction is r, satisfying r/2≤d≤r.
A continuous reaction kettle according to claim 5, characterized in that: the high-pressure injection device further includes

A three-phase mixer, the three-phase mixer includes a cylinder with a high-pressure gas inlet, a solid-liquid slurry inlet and a slurry outlet;

The injection part is connected with the slurry inlet and the slurry outlet, and is used to inject the slurry in the three-phase mixer into the reaction chamber.
A continuous reaction kettle according to claim 6, characterized in that: the solid-liquid slurry inlet and the slurry outlet are located at both ends of the barrel, and the high-pressure gas inlet is located at the barrel. on the side wall.
A continuous reaction kettle according to claim 7, characterized in that:

The high-pressure gas inlet, solid-liquid slurry inlet and slurry outlet are respectively connected with the high-pressure gas supply pipe and the solid-liquid slurry supply pipe. The pipe is connected to the slurry discharge pipe;

The high-pressure gas supply pipe is equipped with a pressure reducing valve, the three-phase mixer is equipped with a pressure sensor, the pressure reducing valve and the pressure sensor are both connected to a controller, and the controller detects The pressure in the three-phase mixer controls the opening of the pressure reducing valve.
A continuous reaction kettle according to claim 8, characterized in that:

The spray part is a nozzle, and the nozzle includes a nozzle and a tubular structure, and the nozzle is provided with the nozzle hole;

The nozzle hole is connected to the slurry inlet; one end of the tubular structure is connected to the nozzle, and a flow channel communicated with the nozzle hole is formed inside. The side of the tubular structure close to the nozzle is connected to the nozzle. The slurry discharge pipe is connected.
A continuous reaction kettle according to claim 9, characterized in that: a regulating valve is provided inside the tubular structure for adjusting the aperture size of the nozzle hole.
A continuous reaction kettle according to any one of claims 1 to 10, characterized in that: further comprising

The shell is set on the outside of the kettle body and is formed by at least two vertical cylindrical shells connected in parallel in the horizontal direction. The connection between two adjacent shells is in the direction toward the outside of the continuous reaction kettle. It has an included angle α, satisfying 30°≤α≤90°.
A continuous reaction kettle according to claim 11, characterized in that:

The shell includes an upper head and a lower head, which are located at the top and bottom of the kettle body respectively. The slurry inlet is provided on the bottom wall of the kettle body, and the injection part is arranged on the lower seal. The position of the head opposite to the slurry inlet is in communication with the slurry inlet.
A continuous reaction kettle according to claim 12, characterized in that: the upper head and the lower head are at least one of an elliptical head, a spherical head, and a butterfly head.
A continuous reaction kettle according to any one of claims 1-13, characterized in that:

The body of the kettle is provided with a partition, which extends upward from the bottom wall of the kettle, and the partition divides the inside of the kettle into a plurality of reaction chambers arranged side by side and connected to each other. , there is a gap between the partition plate and the top wall of the kettle body, and the gap gradually increases toward the direction of the material outlet of the kettle body.
A continuous reaction kettle according to claim 14, characterized in that the height of the partition is 1/4 to 3/5 of the height of the kettle body.
A continuous reaction kettle according to claim 14, characterized in that:

Each of the reaction chambers is provided with a heating device, and the heating device is provided with a temperature adjustment component for adjusting the temperature in each of the reaction chambers.
A continuous reaction kettle according to claim 16, characterized in that: the heating device is a heat medium coil, and the temperature adjustment component is a heat medium flow regulating valve provided at the outlet of the heat medium coil.